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PREFA CE
WHILE the following tables and diagrams have been arranged primarily foru se with the au thors’ Textbook of Engineering Thermodynamics it is thou ghtt hat they will be of considerable valu e to all stu dents of engineering as wel l aspracticing engineers or others who may have occasion to u ndertake thermo
dynamic compu tations .Most of the tab les have been taken from Dr . Lu oke’s largerwork on Engineering Thermodynamics , bu t some newones have been added, amongwhichare t he very convenient fou r place hyperbolic and common logarithms, theplates for which were ki ndly loaned by Professor E . V . Hu ntington .
The au thors desire to acknowledge their Obligations to the variou s sou rcesOf information u tilized in the preparation of the tab les and diagrams . Special
mention is du e Professors Marks and Dav is , for the u se of material from theirSteam Tables (Longmans
, Green to Mr . E . D . Thu rston , Jr .
,whose
invalu ab le help is grat efu lly acknowledged , and to Mr . T . M . Gunn for aid on
part of thework.
C . E . L .
JUNE . 191 5 .J . J . F.
LIST OF TA BLES
NO. PAGE1 . Conversion table of u nits of distance 5
2 . Conversion tab le of u nits of su rface 5
3 . Conversion tab le of u n its of volume 5
4 . Conversion tab le of u n it s of weights and force 5
5 . Conversion tab le of u n its of pressu re 6
6 . Conversion tab le of u n its Of work 6
7 . Conversion tab le of u nits of power 7
8. Un its Of velocity 7
9. Heat and power conversion table . 7
1 0 . Barometr ic heights, alt it u des and pressu res 8
1 1 . Conversion tab le inches Of mercu ry t o pou nds per squ are inch 1 0
1 2 . Piston posit ions for any crank angle 1 1
1 3 . Horse -
power per pou nd mean effective pressu re . 1 2
1 4 . Constants for t he cu rve PV' K 1 3
1 5 . Valu es of s for adiabat ic expansion of st eam 1 4
1 6 . Valu es of s in t he equ at ion PV constan t for variou s su bst ances and condit ions. 1 5
1 7 . Fixed temperatu res 1 5
18. Temperatu res, Centigrade'
and Fahrenheit 1 6
19. Valu es of a: for u se in Heck’s formu la for m issingwat er 18
20 . Baume—specific gravit y scale 19
2 1 . Freezing -
po int of calcium chloride b rine 19
22 . Specific heats of solids 20— 2 1
23 . Specific heats of gases 22— 23
24 . Specific heats of liqu ids 24
25 . Specific heat of sodium chloride b rine 25
26 . Coefficient of linear expansion of solids 25
27 . Coefficient of cu b ical expansion of liqu ids 26
28. Coefficient of volumetric expansion of gases and vapors at const ant pressu re 26
29. Coefficient of pressu re r ise Of gases and vapors at constant volume . 27
30. Compressib ilit y of gases by their isothermals 28
3 1 . Valu es of t he gas constant R 28
32 . Density of gases 29
33 . Ign ition temperatu res . 30
34 . The critical point 30
35 . Latent heats Of vaporization 3 1
36 . Latent heats of fu sion . 3 1
37 . Boiling-
po int s 32
38. International atom ic weights 34
39. Melting or freezing—po ints 34
40. Properties of satu rated steam 36
4 1 . Properties of su perheated steam 40
42 . Properties of satu rated ammonia vapor 41
43 . Properties of satu rated carbon dioxide vapor 50
44. R elation between pressu re, temperatu re and per cent. NHa in solu tion 54
x LIST OF TA BLES
N0 . PAGE45 . Valu es of partial pressu re of ammon ia andwat er vapors for variou s t emperat u res
and per cents. of ammon ia in solu t ion 58
46 . Absorpt ion of gases by liqu ids 60
47 . A bsorption of air in water . . 60
48. A ir requ ired for combu st ion of variou s su bst ances 6 1
49. R adiat ion coefficients 6 1
50. Coefficien t s of heat t ransfer 62
5 1 . Heats of comb u stion of fu el elemen t s and chem ical compou nds . 63
52 . Internal t hermal condu ct ivit y 65
5 3. R elat ive.
t hermal condu ct ivit y 68
5 4 . Comparison of cellu lose and average wood composit ion 69
5 5 . Composit ion and calorific power of characterist ic coals 70
56 . Combu st ib le and volat ile of coals,lign it es and peat s 78
57 . C lassification of coals by gas and coke qu alit ies . 87
58. Paraffines from Pennsylvania pet roleums 88
59. Calorific power of m ineral oils by calorimet er and calcu lat ion by densit y form u la of
Sherman and Kropfi"
89
60. Propert ies of oil- gas 90
6 1 . Composit ion of nat u ral gases 91
62 . Propert ies of m ineral o ils . 1 92
63 . Composit ion of coke oven and ret ort coal gas 94
64 . Composit ion of U . S . coke “ 98
65 . Produ ct s of b it um inou s coal dist illation 99
66 . A verage dist illat ion produ ct s of cru de m ineral oils . 99
67 . Fract ionat ion t ests of kerosenes and pet roleu ms . 100
68. Fract ionat ion t est s of gasolenes 102
69. Composit ion of blast - fu rnace gas and air gas . 1 04
70 . R ate of format ion of CO from 0 0 -
3 and carbon 106
71 . Composit ion of produ cer gas 1 08
72 . Composit ion of wat er gas 1 1 3
73 . Composit ion of oil produ cer gas 1 1 374 . Gas produ cer t est s 1 1 4
75 . Composition of powdered coal produ cer gas 1 1 6
76 . Composit ion of boiler - flu e gases 1 1 677 . Calorific powers of best a ir—gas m ixt u res 1 1 778. Lim its of proportions of explosive a ir -
gas mixt u res . 1 1 8
79. R at e of combu st ion of coal 1 1980. Diagram fact ors for Ot t o cycle gas engines 1 22
81 . Heat balances of gas and oil engines 1 2382 . Mean effect ive pressu re fact ors for Ot t o cycle 1 2483 . Valu es of C for a ir flow (Weisbach ) 1 2584 . Flowchange resrst ance fact ors FR (R ei t schel) 1 2585 . Efli crency factors for reciprocat ing st eam engines and t u rb ines 1 2686 . Chimney capacit ies (Ken t ) 1 3087 . Chimney draft 1 3 188. Common logar it hms
,t o 1 32
89. Common logarit hms,1 . 0 t o 1 34
90. Hyperbolic logarithms, t o 1 36
CHAR T PAGE1 . Work and horse-
power for single- stage compressors 1 5 1
2 . Work and horse-
power for two- stage compressors 1 52
3. Work and horse-
power for three- stage compressors 1 53
4. Mean effective pressu re of compressors, one two and three - stages 1 54
5 . Valu e of su pply pressu re in maximum work and mean effective pressu re 1 5 6
6 . R elativework of two and three- stage compressors compared t o single stage 1 57
7 . Diagram t o give economy of exponential cycles referred t o isothermal as st andard . 1 58
8. Compressor cylinder displacement for given capacity 1 59
9. Graphical determ inat ion ofmean effectivepressu re for single cylinder engines 1 60
1 0. R elations for equ al distr ibu tion of work in compou nd engine .1 6 1
1 1 . Specific heats of gases 1 62
1 2 . Specific heat of su perheated steam 163
1 3 . Equ ivalent gas densities at different pressu res and t emperat u res 1 64
1 4 . Ammon ia pressu re- temperatu re relations,for satu rat ed vapor 1 65
1 5 . Carbon dioxide pressu re—temperatu re relat ions for sat u rat ed vapor 1 66
1 6 . Steam, pressu re
- t emperatu re (Tab le XL ) 1 67
1 7. Steam , heat of t he liqu id (Tab le XL ) 1 68
18. Steam ,latent heat (Tab le XL ) 1 69
19. Steam,tot al heat (Tab le XL ) 1 70
20. Steam , Specific volume and density of t he liqu id (Tab le XL ) 1 71
2 1 . Steam , Specific volume and density of t he vapor (Tab le XL ) . 1 72
22 . Vapor pressu re of hydrocarbons and light petroleum dist illat es of t he gasolene class . 1 73
23 . Vapor pressu re of heavy petroleum dist illat es of t he kerosene class 1 74"
24 . Vapor pressu re of t he alcohols 1 75
25 . R elation between wet and dry bu lb psychromet er readings and dewpoint for airand wat er vapor . 1 76
26 . R elation between hum idity andweight of mo istu re per cu b ic foot of sat u rat ed a ir . 1 77
27 . Ammon ia -water solu tions, relat ion between t otal pressu re and t emperatu re 1 78
28. Ammonia -water solu t ions, relat ion between tot al pressu re and per cent . NHa in
solu tion 1 79
29. Ammonia -water solu tions, relat ion between t emperat u re and per cent . NHs in
solu tion 1 80
30. Fractional distillation of kerosene and pet roleums 1 81
31 . Fractional distillat ion of gasolenes . 182
32 . Composition of hypothet ical produ cer gas fromfixed carbon 183
33 . Heats of reaction for hypothetical produ cer gas from fixed carbon , B .T .U 184
34 . R elation between temperatu res and heat for gases according t o t he const ant and
variab le specific heat 185
35 . R ate of combu stion of coal with draft . 186
36 . Heat per pou nd of steam above feed temperatu re . Evaporat ion per hou r perboiler horse-
power . Factor of evaporat ion 1 87
37 . Heat balance for locomotive boiler 188
38. Influ ence of var iou s factors on boiler efficiency 1 89
39. Influ ence of variou s factors on boiler efficiency 190
LIST OF CHA R TS
xi
xii LIST OF CHA R TS
crIA n'r PAGE40. Constant volume lines for steam on the temperatu re-entropy diagram 191
4 1 . Exponent ial gas changes. Small pressu re rat ios 192
42 . Exponential gas changes. Larger pressu re rat ios 192
43 . Exponent ial gas changes. R elat ion between init ial and final rat ios of pressu res,
volumes, t emperatu res, and ent ropies .193
44 . Temperat u re- ent ropy diagramwit h lines of const ant pressu re and const ant qu alityfor steam 194
45 . The Mollier t ot al heat en t ropy diagram for steam 195
46 . R ankine cycle . Thermal efficiency . Steam in it ially dry and satu rated 196
47 . R ankine cycle . Thermal efficiency . Steam in itially of any qu al it y . 197
48. R ankine cycle . Work per lb . of steam andjet velocity . St eam init ia llydry satu rat ed 198
49. R ankine cycle. Work per lb . of st eam (m .e .p. and jet velocit y . St eam in it ia llyOf any qu ality ” 199
50 . Carnot steam cycle and derivat ives. Thermal efficiency . St eam in itially drysat u rat ed 200
5 1 . Carnot st eam cycle and der ivat ives. Thermal efficiency . St eam init ially of anyqu alit y “ 201
5 2 . Carnot st eam cycle and derivat ives. Work per lb . of st eam (m .e .p . ) and jetvelocit y . St eam init ially dry and satu rated 202
5 3 . Carnot st eam cycle and derivat ives. Work per 1h . of steam and jetveloc it y . S t eam in it ially of any qu alit y 203
5 4 . Thermal efficiency . Non - compression gas cycles, Brown, Lenoir , and Ot t o and
Langen . 204
5 5 . Work per lb . of gases and (m .e . Nonc- ompression gas cycles, Brown ,Lenoir ,
and Ot t o and Langen . . 205
5 6 . St irling gas cycle . Thermal efficiency . Heat of regenerat ion , plot ted aga instheat from t he fire 206
5 7 . Ericsson gas cycle . Thermal efficiency . Heat of regenerat ion plot t ed againstheat from t he fire 207
58. Stirlinggas cycle . Thermal effiCIency Heat of regenerat ion plot tedaga inst com
pression pressu re 208
59. Ericsson gas cycle. Thermal efficiency . Heat of regenerat ion plot ted againstcompression pressu re . 209
60. Ott o , Brayt on , Carnot, Diesel , and complet e expansion Ot t o cycles. Therma lefficiency, wit h heat su pplied . 2 10
6 1 . Ot t o, Brayt on , Carnot , Diesel, and complet e expansion O t t o cycles. Thermalefficiency, wit h compression 2 1 1
62 . Ot t o, B rayt on ,Carnot , Diesel , and complet e expansion Ot t o cycles. Work and
(m .e.p. wit h heat 2 1 2
63 . Otto, Brayt on , Carnot , Diesel, and complet e expansionOt t o cycles. Work and
(m .e .p. wit h compression 2 1 3
64 . Ott o gas cycle . Work and (m .e .p. for heat added aftercompression . 2 1 4
65 . Diesel gas cycle . Work and (m .e .p. for heat added aft er compression 2 1 5
66 . Comparison of rat ional and empiric formu las for air and steam flow. A ny init ialpressu re 2 1 6
67 . Comparison of rational and empiric formu las for air and st eam flow. A ny backpressu re 2 1 7
68. Harter’s valu es of Napier’s coeffi cient andweight of flowfor su perheat ed steam 2 18
69. Velocit y of air in pipes in t erms of pit ot t u be readings . 219
70 . Coefficient s of frict ion for air in du cts71 . Diagram t o determine chimney diameters 22 1
LIST OF CHA RTS
CHAR T PA
72 . Diagram t o determine refrigerating effect per pou nd of ammonia . 2
73 . D iagram t o determine refrigerating effect per pou nd of carbon dioxide . 2
74 . Density and specific volume of ammonia -water solu tions 2
75 . Temperatu re-entropy diagram for ammonia 2
76 . Mollier diagram for ammonia 2
77. Temperatu re-entropy diagram for carbon dioxide 2
78. Mollier diagram for carbon 2
79. Work 11 1 B .T .U. , by ammon ia vapor izing t o drysaturatedvapor 2
80. Work In B T .U . , by ammon ia vaporizing t o any qu ality or su perheat at 1 5 pou nds 2
81 . Work in by carbon dioxide vaporizing t o dry satu rated vapor 2
82 . Work in by carbon dioxide vaporizing t o any qu ality or superheat 2
TA BLE OF SYM BOLS
A area in squ are feet .
a area in squ are inches.
coefficient of linearexpansion .
Bé. Baum é .
B .H .P . b rake horse-
power ; alsoboiler horse-
power.
(bk. pr . ) back pressu re in pou nds per squ are inch .
C Centigrade .
coeffic ient for air flow.
spec ific heat .
C? specific heat at constant pressu re .
C, Specific heat at const ant volume .
C; clearance expressed in cu b ic feet .
c clearance expressed as a fract ion of t he displacement .
const ant .
D displacement in cu b ic feet .
(del . pr . ) delivery pressu re in pou nds per squ are inch .
E 1) volu metr ic efficiency (apparent) .F const ant in equ ation for pipe flow.Fahrenheit .
FR resistance factor , FR X velocity head loss du e t o resistances.
g acceleration du e t o gravity , (approx ) feet per second , per second .
H as a su bscript t o denot e high -
pressu re cylinder .
H .P . horse -
power .
h height in inches.
K coeffi cient of t hermal condu ct ivit yconstant .
K 1; t _Lan .
i f h _ as _engIne cons an In express on or orse-
power
L as a su bscript t o denot e low-
pressu re cylinder .lat ent heat .lengt h of stroke in feet .
(L .P . Cap. ) low-
pressu re capacity .
I length .
mean effective pressu re, pou nds per squ are foot .
mean back pressu re in pou nds per squ are inch .
mean effective pressu re in pou nds per squ are inch .
mean forward pressu re in pou nds per squ are inch .
N revolu tions per m inu t e or R .p.m .
P pressu re in pou nds per squ are foot .p pressu re in pou nds per squ are inch .
Q qu antity of heat or energy in B .T .U. gained by a body passing from one state to another .
R gas constant .R 0 ratio of cylinder sizes in two- stage air compressor or compound engine .
R , ratio of delivery t o supply pressu re.
xv i TA BLE OF SYMBOLS(rec . pr . ) receiver pressu re in pou nds per Squ are inch .
S pist on speed .
pou nds of steam per pou nd of air in produ cer b last .
s genera l exponent of V in expansion or compression of gases.
Sp. gr . specific gravit y .
Sp. ht. Specific heat .
(sup. pr . ) su pply pressu re, in pou nds per squ are inch .
T tempera t u re, degrees absolu t e .
t t emperat u re in degrees scale .
T¢ temperatu re-ent ropy .
V volume in cu bic feet .
1) volume .
W work in foot -
pou nds.
w"
: weight in pou nds.Wt . weight .
a: const ant in the expression for missingwater .fract ion of totalweight liqu ified from t he solid,orvaporized from t he liqu id = qu ality . If
t he vapor be superheat ed , t he number of degrees of su perheat also qu ality .
y rat io of t he volume of receiver t o t hat of t he high -
pressu re cylinder Of t he compou ndengine .
Z
2
fract ion of t he st roke of t he steam engine complet ed at cu t -O ff .
rat io of R .P .M . t o cycles per m inu t e .
a, (alpha) coefficient of cu b ical expansion .
a . const ant in equ at ion for variable specific heat at constant volume .
a ,o const ant in equ at ion for var iable specific heat at const ant pressu re .
7 , (gamma) special valu e for s for adiabat ic expansion or compressionspecific heat at const ant pressu re
spec ific heat at const ant volume
6 , (delt a) density in pou nds per cu bic foot .
(zet a ) coefficient of friction .
23, (sigma) summat ion .
<1 ) 45, (phi ) entropy .
NOTE . A small letterwhen u sed asa su bscript t o a capital in general refers t o a point on adiagram , e .g. ,P a designates pressu re at t he point A . Two small let t ers u sed as su bscript s
t oget her , refer in general t o a qu antity between two points, e .g. , Wab designates work donefrom point A t o point B .
HA NDBOOK OF
THER M ODYNA M IO TA BLES AND DIA GR A MS
PART IINTR ODUCTION
The province of EngineeringThermodynamics is to gu ide numerical therma lcompu tations dealingwi th actu al su bstances and apparatu s in accordance withthe laws of thermodynamic philosophy. In order to do this
,numerical valu es
for heat eff ect s mu st be availab le for the variou s su bstances and materials
u sed in engineering u nder the varying conditions of practice , and in su ch u ni ts
as may readily be applied ; these inclu de especially that class of u ni ts known asphysical constants which embrace , for example , su ch qu antities as the coeffi
cient s of expansion , the specific heats, latent heats of fu sion and vaporization ,the ratio of the pressu re- volume produ ct to absolu te temperatu re, t he expo
nent s in adiabatic expansion of gases and vapors, and variou s other qu antities . In addition to the physical constantswhich are necessary in the work ofthermodynamic compu tation, the solu tion of numerical prob lems is greatlyfacilitated by the u se of other correlated tab les and diagramsmany ofwhich aregiven in the present book of tab les , bu t to correctly u se su ch aids there shou ld beno ambigu ity in regard to the u nits employed .It shou ld be noted that tru e pressu res are always absolu te , that is, measu redabove a perfect vacu um or cou nted from zero
, while most pressu re gages andother dev ices for measu ring pressu re , su ch as indicators, give resu lts measu red
above or below atmospheri c pressu re . In all prob lems involving work ofgases and vapors , the absolu te valu es of the pressu resmu st be u sed ; hence , if a
gage or indicator measu rement is being considered , the pressu re of the atmos
phere fou nd by means of the barometer mu st be added to the pressu re above
atmosphere in order to obtain the absolu te or tru e pressu res . When the pressu res are belowatmosphere the combination with the barometric readingwilldepend on the record ; if the record be taken by an indicator itwill be in pou nds
per squ are inch belowatmosphere and mu st be su btracted from the baro
m etric equ ivalent in the same u nits to give the absolu te pressu re in pou nds persqu are inch . When, however, a vacu um gage reads in inches ofmercu ry belowatmosphere , as su ch gages do , the difference between its reading and the barometric gives the absolu te pressu re in inches of mercu ry directly, which can beconverted to the desired u nits by the proper factors .In general , steam pressu res are most commonly stated in pounds per squ are
2 HANDBOOK OF THERMODYNAMICinch and are designat ed as either gage or absolu te . Pressu res of compressed
air are commonly expressed in the same u ni ts as steam ,ei ther gage or absolu te ,
t hough sometimes in atmospheres . Steam pressu res belowatmosphere are conv eni ent ly stated as a vacu um of so many inches of mercu ry , or they may be
given as a pressu re of so many inches of mercu ry absolu te or so many poundsper squ are inch absolu te . The pressu res of gases stored in tanks u nder high
pressu re are frequ ently recorded in atmospheres du e to the conveni ence ofcompu tation of qu antities on this basis . Pressu res of air obtained by b lowersor fans are sometimes given in ou nces per squ are inch above atmosphere , bu tsu ch pressu res , and also differences of pressu re of air du e to chimney drau ght,or forced draught, and the pressu re of illuminating gas in city mains are commonly stated in inches ofwater. Inmany cases the data are given in other unitswhich mu st be converted by the u se of tab les, diagrams or otherwise, beforethe resu lts can be properly interpreted or intelligently compared .
T ime is an important item in all engineering work and none the less so incompu tations, so that convenient tab les and diagrams are most essential to
the solu tion of su ch problems . In some cases graphi c methods are the onlymeans of solu tion ; in others the problems may be solved directly withou t theu se of formu las, and in still others certain steps may be shortened . In manyengineering calcu lations no one isju stified in u sing a complicated mathematicalformu la ; if too mu ch time be requ ired to make the calcu lation in commercial
work itwill not bemade , therefore indirect and often approximate methods aresu bstitu ted . In su ch cases the nearest tabu lar or chart valu e mu st be u sed
,
and generally the resu lt will be as accu rat e as the work requ ires .In the following t ables and charts the accompanying title u su ally indicates the character of each table or diagram and little explanation is necessary .
The tab les for dry satu rated steam,and properties of superheated steam are
those of Marks and Davis. From the investigation made by Marks and Davisit is believed that the properties of satu rated steam given in the tab les are
correct to within one- tenth of 1 per cent . for pressu res within the range ofordinary engineering practice .
The unit of heat and of energy in these tables is amean B .T .U. or Ti“? of theheat requ ired to raise 1 lb . ofwater from 32° to 2 1 2°
The valu e of onemean B .T .U. as u sed in these tab les is equ ivalent toft .
- lbs. when the gravitational constant is cm . sec .
2which correspondsto lbs. and is the valu e for latitu de between 45 ° and For manyyears it has been most common to u se in engineering calcu lations , t he round
number 778; for most prob lems this rou nd number is still the best available
figu re , bu t where special accu racy is needed it is likely that no closer valu ecan be relied u pon than anything between and for the abovelatitu de .Investigations , particu larly by Knob loch and Jacob , by Thomas and byHenning, Showthat the Specific heat of superheated steam is not constant , bu tis a function of both pressu re and t emperatu re . The cu rves derived byMarks
TABLES AND DIAGRAMS 3
and Davis for specific heat of superheated steam from a critical examinationof the material availab le are given in the charts .As the met hod u sed in the derivation of the st eam tables is so rational and
scientific it has been adopt ed for a newdetermination of the relations betweenpressu re and temperatu re for ammonia and carbon dioxide , both irnport antsu bstances in refrigeration . The tab les of properties for ammonia and carbon
dioxide thu s determined give the final valu es of total heat , heat of liqu id , latentheat , specific volume and density of dry satu rated vapor based u pon large scaleplottings,wit hou t equ ations beyond those for the pressu re - temperatu re re la
tions for satu rated vapor . The resu lts are believed to be as re liab le as it is
possib le to have themwithou t more experiment al data .
The Mollier total heat- entropy diagram for steam makes possible the
solu tion of many prob lems involving both sat u rated and su perheated steam .
Since this chart is so convenient for tu rbine work,a scale of corresponding
steam-jet ve locities has been added to t he diagram . Temperatu re- entropyand Mollier diagrams have also been plotted for ammonia and carbon dioxide ,fromwhich thework may readily be obtained .
The analyses of gases , oils , coals , and other fu e ls given in the tableswill befou nd of great valu e tq the engineer . These valu es have been selected from the
most reliab le sou rces availab le,bu t it is worth noting that in the analyses of
oil gas there is qu ite a probability of u ncertainty in the hydrocarbons reported .
There is also some dou bt , at least for gases , in the va lu es given in the table of
igni tion temperatu res (Tab le XXXIII ) . The ignition of a combu stib le is not
by any means a simple operation especially when the fu el is in the form of an
explosive gasmixtu re . Wi th the latter the ignition temperatu re , tru e or apparent
,is different for diff erent proportions of air and fu el , and likewise still
diff erent when neu trals are present . For this reason there may be variou s igni t ion temperatu res for the same su bstance ; this is known to be tru e for gases .
The va lu es given in the tab les therefore mu st be considered as igni tion t em
perat u res not the ignition temperatu re .At tention is called to the general coal tab les (No . LV and LVI) , the first
ofwhich gives the proximate and u ltimate analysis of upward of 200 differentcoals covering the range from peat to anthracite . For each fu el the ca lorific
power is also given . Tab le LVI constitu tes a newtab le derived from No . LV
in which the chemical and thermal properties have been re- determined as ash
and moistu re free . In t his tab le the calorific power of the combu stib le is reported , total and as divided between the fixed carbon and the volatile parts , and
final ly the ca lorific power of the volatile itself per pou nd is found . The prod
u ct of the fractional weight of the fixed carbon and its known calorific
power , gives the heat du e to the combu stion of the fixed carbon part of the
combu stible , and this su btracted from the B .T .U. per pou nd of combu stib le
gives the heat per pou nd of combu stib le derived from its volatile . The heat
per pou nd of combu stib le derived from its volatile only, when div ided by t hefract ional Weight of volatile in the combu stib le gives the B .T .U. per pou nd of
4 HANDBOOK OF THERMODYNAMICvolatile itself. Thu s the character of heating power of the volatile of the coalsfu rnishes a newbasis of classification with direct reference to avai lab ility asfu els , and makes possib le the calcu lation of the calorific power of a coal wi thfair accu racy , from its easily fou nd proximate analysis .In general, the charts presented in this book have been drawn to a su fficientlylarge scale to permi t direct solu tion of most prob lems wit h a reasonab le degreeof accu racy. However, in certain cases i t is advisab le to plot newdi agrams toa larger scale in order to ensu re still greater accu racy of resu lt .Where it has been deemed advisab le the derivation and u se of the chart has
been given in the text ; bu t where this descriptionwou ld involve a lengthy ex
planation it has been omitted ; in su ch cases the reader is referred to the au thors’
Textbook ofEngineeringThermodynamics for a complete discu ssion of the constru ction of the diagrams . Itwill be u nderstood that the numbers of equ ationsgiven in the descriptive matter refer to the textbook qu oted . In some of thecharts the cu rves have been plotted from tabu lar valu es derived from experi
ment or calcu lated from formu las ; u nder these conditions the method of deri
vation is obviou s andwi ll not be referred to in the text .
6 HANDBOOK OF THERMODYNAMICTA BLE V
CONVER SION TABLE OF UNITS OF PRESSUREInches of A tmospheresM ercu r
lyat (S t andard at
32° Sea Level) .One lb . per sq. f t
One lb. per sq. in 1 44 . 1 .
One ou nce per sq . in 9.
One atmosphere (standard at sealevel ) 21 1 6 1 14 .696 29.924 1
One kilogramme per squ are met er 0 . 1 42234
One gramme per squ are millimet er
One kilogramme per squ are cent i2048. 1 7
FLUID PR ESSUR ESOne ft . of wat er at 39.1
° F. (max .dens. )One ft . ofwat er at 62° FFOne In . of wat er at 62° FOne in. of mercury at 32 ° F. (st andard) 1 .
One cent imet er of mercu ry at 0 ° C . .
One ft . of air at 32°F. , one atmos.
0 0005604 0 001 1 4 1 2 0 0000381 3
One ft . of air, 62° F 0 . 0005282 0 001075 5
1 PBE S SUREB M EASUR ED B r THE MERCUR Y.
COLUM N . For t empera t u res ot her t han 32° F. , t he densit yo f mercu ry. pou nds per cu b ic inch , and hence t he pressu re, pou nds per sq u are inch , du e t o a column of
mercu ry 1 inch high , is given wit h su fficient accu racy by t he following formu la :p= o.49lz— (t — 32) x0.0001 .
The mercu rial baromet er is commonly made wit h a. brass scale which has i t s st andard or correct lengt ha t 62
° F , and a linear coeffi cient of expansion of abou t for each degree Fahrenheit . Hence, to
correct t he st andard mercu ry at 32°F. , t he correct ed reading will be
H32 = H - H t_28' 6‘x
1 1 000
where H: is t he ob served height at a t emperat u re of 1° F .
TA BLE VICONVERS ION TABLE OF UNITS OF WORK
Kilogrammet ers. Foot - pou nds.
1 7 23300
0 . 138255 1
276 5 10 2000
309 691 2240
CalorieKilo °C .
. 4536
. 5 5 5 6
.Ft . -Lb .
1
777 5
3086
1 399 5
5 50
1 .98X 10‘
TABLES AND DIAGRAMS 7
TABLE VIICONVER SION TABLE OF UNITS OF POWERFoot Ou nds per Kilogrammet ers perFoot
égggggs per
mu t e.
Horse- power . Cheval-Vapeu r .
Inu t c.
1 . 60 . O 00181818 0 00184340
0 01 66667 1 0 000030303 0 0000307241 0 138252
33000 . 1 .
325485 1 .
0 . 1 205 50 0 .0002191 82 1
TABLE VIIIUNITS OF VELOCITY
Feet per Minu t e. Feet per Second.
One foot per second 60 . 1
One foot per minu t e 1 .
One statu te mile per hou r 88.
One nau t ical mile per hou r = 1 knotOne kilomet er per hou rOne met er per minu t eOne cent imet er per second 0 032808
TABLE IXHEAT AND POWER CONVER SION TABLE
false
. are. are.
1 .
.4536 .252 1 .
81 65 1 143 4536 1
. 4536 1 .8
Calor ie B .T .U. Calorie B .T .U.
per Cu . Ft . per Cu . Ft . per L it er. per Lit er.
1 3 9683 .0353 1 402
252 1 0089 0353
28 31 7 1 1 2 37 1 3 9683
7 . 1 36 1 .
B .T .U. Calor ie.
06233
13?
H.P. Sec. H.P. M in. H.P. Hou r .
. 18X 10" 1 .818X 1 0“ 3
.308X 1 0“ X10- 7
1 .252 . 5 556 2 .356x 10 3 .927x 1 0— 4
1— 2 1 . 5 58X10
- 3
.45 36 1— 2 — a
.7074 . 1 783 .3931 1- z 2.777x 1 0
- 4
60 1- 3
2545 641 1 .41 3 ><10a 3600 60 1
8 HANDBOOK OF THERMODYNAMICTAB LE X
TABLE OF BAROMETR IC HEIGHTS, ALTITUDES, AND PR ESSURE-S
(A dapted from Smithsonian Tables)Baromet ric heights are given in inches and millimet ers of mercu ry at i ts st andard density
(32°F.
A lt it u des are height s above mean sea level in feet , at whi ch t hi s baromet r ic height isstandard . (See Smithsonian Tables for correct ions for lat it u de and t emperat u re )
.Pressu res given are the equ ivalent of the baromet r ic height in lbs. per sq . in. and persq. ft.
S t andard Baromet er . Pressu re, Pou nds perA lt it u de , Feet above
Sea Level.Inches. Cent imet ers. Squ ar e Inch . Sq u are Foot .
1 53791 5061
1 47461 44351 41 28
1 3824
1 35231 3226
1 29311 2640
1 2352
1 20681 1 7861 1 5071 1 230
109571 06861 04 181 01 539890
9629937291 1 6
8863861 2
836481 1878747632
7392
71 55 1 626 76919668664546225
5997 15 771 1911265 5475 3255 105
4886 14670 1522134455 1 796 54241 1810 174030
TABLES AND DIAGRAMSTAB LE X— Contz
’
nu ed
St andard Baromet er. Pressu re. Pou nds perA lt it ude,£
eet aboveSea ev e
In0h95 ~ Sq u are Inch. Squ are Foot.
3820
371 536 1 1
35083404
3301
3 199
3097
2995 1 3 1 63
2894
27932692259224932393
22942195209719991901
1 804
1 707
1 6101 5 14
1 418
1 322
1 227
1 1 32
1 038
943
849756663
5 70477
384292
261
1 09—F18
0
73- 1 63
- 253— 343 2 1 43 0— 433
- 522- 6 1 1- 700- 788- 877
- 965
10 HANDBOOK OF THERMODYNAMIC
TAB LE XI
CONVER SION TA BLE INCHES OF MER CURY TO POUNDS PER SQUA R E INCH(Calcu lat ed for a Temperat u re of 32
°F. )
20
[0
N
H
H
O
O
co
co
oo
oo
xi
1 0 .
10 .
. 297
. 789
1 1
1 1
1 2 .
1 2 .
. 262
1 3 .
. 245
1 3
1 4
1 4 .
1 5 .
A
PP-
03
00
10
Q
Q
OD
CJ‘
CJ'!
. 491 2
.9824
. 4736
.9648
. 4560
.9472
4384
.9296
. 4208
91 2
. 4032
.894
. 3856
. 8768
3680
.8592
. 3504
.84 1 6
. 3328
.8240
3 1 5
806
280
771
753
736
227
1 0
1 1 .
1 1
1 2 .
1 2
1 3 .
13 .
1 4 .
1 4 .
1 5
fl
c>
c>
cn
01
fl
ip-
03
03
10
N
M
H
H
O
O
CO
CO
OO
W
NI
To correct for ot her t emperat u res see foot not e Tab le V
. 0491
. 5 403
03 1 5
. 5 227
. 01 39
. 505 1
.9963
. 4875
.9787
4699
.961 1
. 4523
9435
. 4347
. 9259
. 4 1 7 1
.9083
3995
.8907
. 3819
.873 1
. 364
.85 5
346
.838
329
.820
3 1 1
802
294
785
. 276
01
15
7-5
03
00
(O
to
wmxl
1 0
1 1
1 1
1 2
1 4
N
wl—‘H
O
O. 0982
. 5894
0806
. 57 18
. 0630
. 5 542
. 045 4
. 5 366
. 0278
. 5 190
. 01 02
. 501 4
.9926
. 4838
.9750
. 4662
.95 74
. 4486
.9398
. 43 10
.9222
. 4 1 3
.904
. 396
.887
1 2 . 378
.869
1 3 .
1 3 .
. 343
1 4 .
1 5 .
360
85 2
834
325
1 0 .
1 1 .
1 1 .
1 2 .
1 2 .
1 3 .
1 3 .
1 4 .
1 4 .
1 5 .
N
wi—‘i—‘C
C
Cn
flk
b-P
OJ
OO
©©m00
m
N
M
F—‘l—io
o
Cn
rh
r-P
OJ
OJ
KI
NI
Q
Q
U!
. 2947
. 7859
. 277 1
. 7683
. 2595
. 7507
. 24 19
. 7331
2243
. 7 1 5 5
. 2067
6979
. 1891
. 6803
. 1 7 1 5
. 6627
. 1 539
. 645 1
. 1 363
. 6275
. 1 18
. 6 10
. 1 01
. 592
. 083
. 5 74
. 066
. 5 5 7
. 048
. 5 39
. 030
. 5 30
Cn
n-P
Q
OJ
OO
o
co
co
oo
oo
H
1 1
1 1
1 3
1 3
1 5
mo
re
fl
fl
cfi
cb
tfl
. 3438
.8350
3262
.81 74
. 3086
. 7998
. 291 0
. 7822
. 2734
. 7646
. 25 58
. 7470
. 2382
. 7294
. 2206
7 1 18
. 2030
. 6942
. 1 85 4
. 6766
. 1 68
. 659
. 1 50
. 64 1
1 2 .
1 2 .
1 32
624
. 1 1 5
. 606
1 4 .
1 4 .
1 5 .
097‘
588
080
. 5 71
M
NJ
l—‘P-‘
O
O
01
15
15
00
00
O
CO
CO
OO
W
1 1
1 2
1 3 .
1 3 .
1 4 .
1 4
1 5
1 5
N
N’I
Q
OD
U!
. 3929
.884 1
. 375 3
. 8665
. 35 77
.8489
. 3401
.83 1 3
. 322 5
.81 37
. 3049
. 796 1
. 2873
. 7785
2697
. 7609
. 252 1
. 7433
. 2345
. 725 7
. 2 1 7
. 708
1 1 . 199
. 690
1 2 . 181
. 673
1 64
65 5
1 46
. 637
. 1 29
. 620
N
NJ
t—‘b—‘O
O
u
n
mov
on
Ch
i-P
rP
OO
CO
. 4421
.9333
. 4244
.91 57
. 4069
.8981
. 3893
.8809
. 371 7
8629
. 3541
.8453
. 3365
.8277
. 3 189
.8101
. 301 3
. 7925
. 2837
. 7788
. 266
. 757
. 248
. 739
. 231
. 722
.2 1 3
. 704
. 195
. 689
. 1 78
. 669
TABLES AND DIAGRAMS 1 1
TABLE XIIPISTON POSITIONS FOR ANY CRANK ANGLE
FROM BEGINNING OF STROKE AWAY FROM CR ANK SHAFT To FIND PIsTON PosITION FROMDEA D- CENTER MULTIPLY STROKE BY TABULA R QUANTITY
5 . 001 4 .001 5 .001 5 .0016 .0016 .0016 . 001 7 .0019
10 .0057 .0059 .0061 .0062 .0063 .0065 .0067 .0076
1 5 .0128 .0133 .01 37 .01 40 .01 42 .01 46 .01 49 .01 70
20 .0228 .0237 .0243 .0248 .0253 .0260 .0265 . 0302
25 .0357 .0368 .0379 .0388 .0394 .0405 . 041 3 .0468
30 .05 13 . 0531 .0545 .0556 .0565 .0581 .0592 .0670
35 .0698 .0721 .0740 . 0754 .0767 .0787 . 0801 .0904
40 .0910 .0939 .0962 .0981 .0997 . 1022 . 1041 . 1 1 70
45 . 1 1 52 . 1 187 . 1 21 5 . 1 237 . 1 256 . 1 286 . 1 308 . 1 468
50 . 141 6 . 1458 . 1 491 . 1 5 18 . 1 541 . 1 576 . 1 607 . 1 786
55 . 1 71 3 . 1 759 . 1828 . 1827 . 1853 . 1892 . 1922 . 2 132
60 .2026 . 2079 .2122 . 21 57 .2186 .2231 . 2295 . 2500 t
65 .2374 .2431 .2477 . 25 1 4 .2545 . 2594 . 2630 . 2886
70 .2730 .2794 .2844 . 2885 .2929 .2973 . 301 3 . 3290
75 .3 1 23 .3187 .3239 . 3282 . 3317 . 3372 . 3414 .3705
80 . 35 1 6 . 3586 . 3642 .3687 . 3725 .3784 . 3828 .4132
85 . 3944 . 401 3 .4068 . 41 1 3 . 41 5 1 .421 0 . 4254 .4564
90 .4365 . 4437 .4495 .4547 .4580 .4641 . 4686
95 . 481 6 . 4885 .4940 .4985 . 5022 . 5081 . 5 1 26 . 5436
1 00 . 5253 . 5323 . 5378 . 5424 . 5461 . 5 520 . 5 564 . 5868
105 . 5 71 1 . 5 775 . 5828 . 5870 . 5905 . 5961 . 6002 . 6294
1 10 .61 50 . 62 14 .6265 . 6306 . 6340 .6393 . 6530 . 6710
1 1 5 .6600 . 6657 .6703 . 6740 .6771 .6820 . 6856 .71 1 3
1 20 . 7026 . 7080 .71 22 . 71 57 .7186 .7231 . 7265 . 7500
125 .7449 . 7495 .7533 .7563 . 7588 .7628 . 7658 . 7868
1 30 .7844 . 7885 . 7920 .7947 . 7969 .8004 .8030 .821 4
1 35 .8223 .8258 .8286 .8308 .8327 .8357 .8379 .8535
1 40 .85 70 .8600 .8623 .8642 .8658 .8682 .8703 .8830
1 45 .8889 .8913 .8931 .8946 .8958 .8978 .8993
1 50 .91 73 .9191 .9204 .9216 .9226 .9241 .9252 .9330
1 5 5 .9420 .9432 .9452 :945 1 .9457 .9468 .9476 .9531
160 .9625 .9633 .9640 .9645 .9650 .9656 .9661 .9698
165 .9787 .9792 .9796 .9799 .9802 .9805 .9809 .9829
170 .9905 .9908 .991 1 .9912 .9913 .991 5 .9924
175 .9976 .9977 .9977 .9977 .9978 .9978 .9979 .9981
180
l=length of connect ing rod.
r radiu s of crank.
1 2
Diamet er
Cylinder ,Inches.
00
~i
an
Nlfl
uln
NIt-i
CONI)‘
1 00
. 0496
. 1 5 19
. 2590
.3709
. 4875
. 6089
. 7350
.8659
. 001 6
. 1 420
. 2872
. 4371
. 5918
. 75 1 3
.91 5 5M
N
N
N
M
N
M
H
H
H
H
H
H
H
H
HANDBOOK OF THERM ODYNAMIC
200
TA B LE XIIIHOR SE - POWER PER POUND MEAN EFFECTIVE PR ESSUR E
Speed of P ist on in Feet per M inu t e.
wwwwwwi—tH
H
H
O
O
O
O
Q
Q
O
Q
O
O
Q
m01 <0 00
.8033
.91 39
. 03 1 7
. 1 567
. 2888
. 4280
. 7279
. 0563
. 41 33
. 7989
. 2 1 30
. 65 5 7
. 0269
. 6267
. 1 5 5 1
. 71 20Cn
Cn
ih
bh
wwwwwH
H
H
H
I-‘
o
o
700
.81 63
.9371
. 0662
. 2037
. 3495
. 5036
. 6660
. 01 59
. 3990
81 5 5
2654
. 7485
2650
. 6 1 47
. 3987
. 01 43
a
mmrh
bt/O
N
M
N
H
H
H
H
H
O
O
800
. 6854
.8044
.9330
. 071 0
. 2 186
. 375 6
. 5422
. 7184
.9040
. 3038
. 74 18
. 2 1 78
. 73 18
. 2840
8742
4026
1 690
mmmfi
fi
wwwwl—AH
H
H
H
H
O
O
O
900
. 0490
. 2049
. 3709
. 5476
. 7350
.9532
. 1 420
. 5818
. 0845
6200
. 1983
.8195pwwwH
H
H
H
I—H
14 HANDBOOK OF THERMODYNAMICTAB LE XV
VALUES OF“s”FOR ADIABATIC EXPANSION OF STEAM .
A.EXPANS ION OF WATER FR OM 200 B . EXPANS ION OF DR Y SATUR ATED STEAM FR OM
LBs. A ss. 200 L 13 8. A Bs .
C . Ex pA NsION OF STEA M . SUPER R E A TED THR OUGHOUT D . EXPANS ION OF STEAM INITIALLY SUPE R H EA ’
I‘ED
Ep NsION , FR OM 200 h as. A s s. A ND 5 40° SUPER A ND FINALLY W ET , FR OM 203 h as. A B S . A ND 1 50°
HEA T ‘ SUPE RHE A ’
I‘
.
(NOTE — C rosses sat u ra t ion line at 70 lbs. abs. )
Valu es of 8 for 1 0- lb . Valu es of s for Whole Valu es of 8 for 1 0 - lb . Valu es Of S for WholeIn t ervals. R ange. Int ervals. R ange.
Calcu 200 Lbs. C alcu Cor Calcu 200 Lbs. Calcu CorPressu re. la t ed . la t ed . rect ed.
R ange. la t ed . la t ed. rect ed.
200— 190 1 35 4 190 1 35 4 l 342 200— 190 1 249
190 - 180 1 3 1 4 1 80 1 333 1 342 190— 180 1 365
180— 1 70 1 70 1 80— 1 70 1 396
1 70 - 1 60 1 60 1 70 — 1 60 1 333
1 60— 1 5 0 1 50 1 60— 1 50 1 3 1 4
1 5 0— 1 40 1 40 1 5 0— 1 40 1 325
1 40— 1 30 1 30 1 . 340 1 . 34 1 1 40— 1 30 1 35 7
1 30— 1 20 1 343 1 20 1 340 1 340 1 30— 1 20 1 302
1 20— 1 1 0 1 1 0 1 . 339 1 20— 1 1 0 1 303
1 1 0— 1 00 1 . 339 1 10— 1 00 1 270
1 00 90 1 338 1 338 1 338 1 00 90 1 396
90 80 80 90 80 1 3 1 1
80 70 l 33 1 1 335 1 33 1 1 . 335 80 70 1 337
70 60 1 340 1 334 1 332 1 . 334 70 60 1 230
60 50 1 3 1 5 1 332 1 330 1 332 60 5 0 1 1 5 0
50 40 1 327 1 330 1 329 1 . 330 5 0 40 1 1 44
40 30 1 3 18 1 327 1 328 1 327 40 30 1 1 3830 20 1 328 1 325 1 . 328 30 20 1 09320 1 0 1 323 1 322 1 .327 1 . 322 20 1 0 1 1 5 7
1 0 1 1 1 1 6
NOTE . Irregu larit ies in valu es of 8 have been correct ed by plot t ing a smoot h cu rve t hrou gh calcu lat edvalu es, and t aking correct ed valu es from t his cu rve.
Su bst ance.
All gases
All gases and vaporsAll sat u rat ed vapors .
All gases and vapors .
.r
Ammonia (NHs)Ammonia (NHs)BromineCarbon dioxideCarbonmonoxide (CO)Carbon disu lphide(CS!)
Chlorine (Cl)ChloroformE ther (C s OCgHA )Hydrogen (Hz)Hydrogen sulph (HzS)Methane (GIL)Nit rogen (N2)Nit rou s oxide (NO2) .Pint sch gasSu lphide diox (SOs)Steam, superheatedS t eam, wet
8 wetS team,
wetS
“ wetSteam,
wetSteam,
dry
232
327
4 19 4
444 7
630 5
658
1064
1084
1 435
1 546
1 753
TABLES AND DIAGRAMS 1 5
TABLE XVIVALUES OF 8 IN THE EQUATION PV" =CONSTANT FOR VAR IOUS SUBSTANCES
AND CONDITIONS
R emarks or A u t horit y.0
Isothermal 1
Constant pressu re 0 Accepted thermodyIsot hermal 0 namie law
Constant volume 00
Adiabat ic Smithsonian TablesCompressed in cylinder 1 .4 Experience
A diabatic, wet AverageAdiabatic, superheat ed 1 .3 ThermodynamicsAdiabatic 1 293 Strecker
A diabatic 1 300 Rontgen , Wu llnerA diabatic 1 . 403 Cazin, Wullner
Adiabatic l 200 BeyneAdiabat ic 1 .323 S ker
Adiabat ic 1 106 Beyne, Wu llner
A diabatic l .029 MullerA diabat ic l 410 CazinA diabat ic 1 276 M iiller
A diabat ic 1 316 MullerA diabat ic 1 410 CazinAdiabat ic 1 291 Wu llner
Adiabat ic Pintsch Co.
Adiabat ic Cazin,M ii ller
Adiabat ic Smithsonian T a b l e sAdiabat ic Variable (From less than 1 t o
more thanAdi abat ic 1 1 1 1 R ankineAdiabat ic l . 1 4X moist. P
Adiabatic moist. GrayExpanding in cylinder 1 Average from pract iceSat urat ion law 1 0646 Regnau lt
TABLE XVIIFIXED TEMPER ATURESU. s. BUREAU OF STANDA RDS
Tem'
pef‘at u re,
449
621
787
832
1 167
1216
1947
1983
261 5
2815
3187
Det ermined by the Point at whichLiqu id t in solidifiesLiqu id lead solidifiesLiqu id zinc solidifiesLiqu id su lphu r boilsLiqu id antimony solidifiesLiqu id aluminum, pure, solidifiesSolid gold meltsLiqu id copper solidifiesSolid nickel meltsSoli d palladiummeltsSolid platinummelts
1 6
I
I
I
I
l
I
l
I
HN
OO
IQ
OR
O
NI
WCO
p-n
1 0
1 1
1 4
1 5
1 6
1 7
—40 .
- 38.
—36 .
—34 .
- 32- 31 .
- 29.
- 27 .
- 25 .
- 23 .
- 22 .
- 20 .
- 18.
- 1 6 .
- 1 4 .
- 1 3 .
- 1 1 .
b
w
mmmw
mo
a
m
wo
mw
ma
mm
1 0 .
1 2 .N
»
1 5 .
1 7 .
19.
21
24 .
26 .
28.
30 .mmmm
b
a
a
m
33 .
35 .
37 .
39.
42 .
44 .
46 .
48. su
mmon
N
fi
o
m
5 1 .
5 3 .
5 5 .
5 7 . ro
e-
o
m
60 .
62 .
64 .
66 .
69.
71 .
73 .
'
a
a
m
wp
o
m
HANDBOOK OF THERMODYNAMIC
78.
80 .
82 .
84 .
86 .
87 .
89.
91 .
93
95 .
96 .
1 00 .
1 02 .
1 04 .
1 05 .
1 07 .
1 09.
1 1 1 .
1 1 3 .
1 1 4 .
1 1 6 .
1 18.
1 20 .
1 22 .
1 23 .
1 25 .
1 27 .
1 29.
1 31 .
1 32 .
1 34 .
1 36 .
1 38.
1 40 .
1 4 1 .
1 43 .
1 45 .
1 47 .
1 49.
1 50 .
1 5 2 .
1 5 4 .
1 5 6 .
1 58.
1 59.
1 61 .
1 63
1 65 .
1 67 .
1 68.
1 70 .
1 72 .
1 74 .
1 76 .
1 77 .
1 79.
181 .
183 .
1 85 .
1 86 .
1 88.
190 .
1 92 .
194 .
195 .
N
Q
O
W
re
na
mes
mp
a
m
wa
mm
wwb
m
wh
o
m
N
IF
Q
W
wh
en»
N
P
O
W
N
P
O
W
n
a
mes
(I)
ma
ca
w
ma
ca
w
HHM
HHM
HHHHI—‘HHH
HHHHHHP—iP—‘I—‘I—‘HHHHHH
HHHHl—‘H
HHHHHHHHHHHHHH
HHHHHHHH
TA BLE XVIII
3 1 6 .
3 18.
320 .
321 .
323 .
325 .
327 .
329.
330 .
332 .
334 .
336 .
338.
339.
34 1 .
343 .
345 .
347 .
348.
35 0 .
35 2 .
354 .
35 6 .
35 7 .
359.
36 1 .
363 .
365 .
366 .
368.
370
372 .
374 .
375 .
377 .
379.
381 .
383 .
384 .
386 .
388.
390 .
392 .
393 .
395 .
397 .
399.
401 .
402 .
404 .
406 .
408.
41 0 .
41 1 .
41 3 .
4 1 5 .
41 7 .
4 19.
420 .
422 .
424 .
426 .
428.
429
43 1 .
433 . S
a
m
mp
a
m
wa
a
m
wp
a
m
mp
a
m
wp
mm
wh
o
m
wma
m
wa
mm
N
ma
m
N
Q
OJ
M
re
sumes
to
w
N
IP
TEMPER ATURES, CENTIGR ADE AND FAHRENHEIT
HHHHHh‘
HHHr—‘Hr—lv—flHHHHHHHHHHP‘
HHHHHHHHHHHHHHHHH
950
960
970
980
990
1 000
1 01 0
1020
1 030
1 040
1 050
1060
1 070
1 080
1 090
1 1 00
1 1 1 0
1 1 20
1 1 30
1 1 40
1 1 5 0
1 1 60
1 1 70
1 180
1 190
1 200
1 2 1 0
1 220
1 230
1 240
1 250
1 260
1 270
1 280
1 290
1 300
1 31 0
1 320
1 330
1 340
1 35 0
1 360
1 370
1 380
1 390
1 400
1 4 10
1 420
1 430
1 440
1 450
1 460
1 470
1 480
1 490
1 5 00
1 5 10
1 5 20
1 530
1 540
1 5 50
1 600
1 650
1 700
1 750
1800
1 742
1 760
1 778
1 796
181 4
1832
1850
1868
1886
1904
1922
1 940
1958
1976
1994
201 2
2030
2048
2066
2084
2 102
21 20
21 38
21 5 6
2 1 74
2192
22 10
2228
2246
2264
2282
2300
2318
2336
2354
2372
2390
2408
2426
2444
2462
2480
2498
25 1 6
2534
25 5 2
2570
2588
2606
2624
2642
2660
2678
2696
2714
2732
2750
2768
2786
2804
2822
291 2
3002
3092
3182
3272
o
0
0
05
O
r-‘
Q
NWOO
O
IF
M
O
O
S
Q
Q
mO
TABLES AND DIAGRAMS 1 7
TA BLE XVIII— Continu edTEMPERATURES, FAHRENHEIT AND CENTIGRADE
21 0 .
31 0 .
1 2_s
360 .
4 10 .
426 - 7
1
1
1
1
1
1 5 1 0 .
1
1 52 1
1
1
1
1
1 8 HANDBOOK OF THERMODYNAMICThe missing water, or difference between t he actu al steam consumption of an
engine and that shown by the indicator cards is given by Prof. Heck as:
Missing water 0-27Indicated steam pIZ
in which 8= the ratio of cylinder- displacement su rface in sq . ft . t o displace
ment in cu . ft . , or
Z = fraction of card length completed at cu t - off ;
of engine ; d= dia . cyl. in in . ; L = st roke in ft .
The term (332 — x1 ) is t o be supplied from Table XIX and is t he difference
between the a: for the high pressu re and that for t he low pressu re , both
absolu te.
8
TABLE XIX
VALUES OF 3: FOR USE IN HECK’S FORMULA FOR MISSING WATERA bsolu t e A bsolu t e A bsolu t e
St eam Pressure.
2;S team Pressu re.
3;Steam Pressu re.
3
O 1 70 70 1 65 3931 175 75 304 1 70 3972 1 79 80 3 10 180 4053 183 85 31 6 185 4094 186 90 190 4 136 191 95 327 1958 196 1 00 42010 200 105 338 21 0 4271 5 210 1 10 343 220 43 120 220 1 1 5 348 230 44125 229 120 353 24030 238 125 358 250 45435 246 1 30 362 5 260 460 .540 254 1 35 367 270 46745 262 140 280 47350 1 45 376 290 47955 277 1 50 300 48560 284 1 55 385
i-‘
l-‘
b-‘
HHH
TABLES AND DIAGRAMSBAUME SPECIFIC GRAVITY SCALE
TAB LE XX
19
Specific grav i ties are for 60°F. referred t o water at same temperature as unity, at which
temperature It weighs lbs. per cubic foot.
Degrees Baumé
for liqu idsheavier thanwater.
for liqu ids lighter thanwater.RELATION BETWEEN SPECIFIC GRAVITY AND BA UM E
.60
70
.80
.90
00
.00
. 10
20
.30
40
. 50
Degrees Baumé.
A dapted from Smithsonian TablesNo. 65 .
1 Specific gravity less than particularly u sefu l for liqu ids fu el, oils, and alcohols.Specific gravi t ies greater than part icularly u seful for nan- freez ing br ines.
Densit y of Solu t ion .
HHI-t
I-t
HHI-i
v-fl
N
NN
NHHHH
GNP-
NO
OO
ONh
N
TAB LE XXIFREEZING- POINT OF CALCIUM CHLOR IDE
U. S . BUREAU or STANDARDs
Per cent 0 110 11 byWt .
Freezing-point .
9— 13— 1 6— 20— 24— 29— 34— 40
FreesgnEpOInt
20
Cl
HANDBOOK OF THERMODYNAMIC
Su bstance.
Tin (cas t )
Zinc (east)Bronze
Brass
Brickwork, M asonr
Bu t ter
Cast IronWrought IronM arbleSteelSandStene
88 05
8 75—9
Co
2 . 1 — 3
SPECIFIC HEATSu t hon t
Smi thson ian TablesSmi thson ian TablesSmi thsonian TablesSmi t hsonian Tables
22 HANDBOOK OF THERMODYNAMIC
Su bst ance.
Hydrogen, H2
Nit rogen, N2
Ammonia, NH;
Carbon diox.,C0 2
Carbon monoxide .
Methane, CH.
138112 0 16 , CoHo
Et hylene, CzH4
3
3
Cr
3996
.409
3 410
2240
2300
2438
2419
2464
2497
. 2374
. 2375
. 2366
. 2429
.2430
. 2389
5202
5356
5 125
1843
2025
. 2 1 69
2425
2426
. 5929
2990
3325
3754
4040
TA BLE
SPECIFIC HEATS OF GASES
At Temperat u re .
— 28
1 2— 198
21 - 1 00
20—440
20— 630
0— 200
20— 440
20 630
20—800
0— 100
0— 200
20—440
20— 630
20—800
20—1 00
23— 100
27— 200
24— 2 16
— 28
1 5— 1 00
1 1 — 2 14
23— 99
26 — 198
18— 208
34— 1 1 5
35 — 1 80
1 16— 218
53 6— 388 4
70— 21 2
68— 824
68— 1 66
22— 392
68— 824
68— 1 1 66
68— 1 472
32 — 21 2
32— 392
68— 824
68— 1 1 66
68— 21 2
73— 2 1 2
80— 392
75 —4 21
—45
59— 21 2
52—4 1 7
74— 2 10
79—388
64— 406
93— 239
95— 356
241 —4 24
50—396
A u t hori t y.
R egnau ltR egnau ltWiedeman
Holborn—A u st inHolborn- A u st inR egnau ltHolborn—A u st inHolborn- A u st inHolborn—A u st inR egnau ltR egnau ltKolbow—A u st inHolborn- A u st inHolborn—A ust inWiedemanWiedemanWiedeman
R egnault
R egnau ltR egnau ltR egnau ltWiedemanWiedemanR egnault
WiedemanWiedeman
R egnau ltR egnau lt
Co
2 . 4219
171 5
1703
.401 1
1 558
1734
4505
.2 131
TABLES AND DIAGRAMS 23
XXIIIRATIOS AND DIFFERENCES
Det ermined from Cv Co7713-52(Op-Cu) CI):
00
(T ) in f t .- lbs.
- Y
Wiedeman C, and .9881
C
C
—p= l .4o8at 4
°— 1 6
°C . by Lummer and Pringsheim
0
Holborn and A u st in C, and .0637
Cat 5
°t o 14
°C .
Cr
Holborn and A u st in C, and . 0704 1 .4 1 05
0»
00by Cazm
Wiedeman C, .2389 and .0686
Cat 5
°
to 1 4°C . by Lummer and Pringsheim
0
Wiedeman C, and mean of . 1 191
by Wu llner
Regnault and .0467
ge= L2995 by Luminer and Pringsheim
0Wiedeman C, .2425 and mean of .0691
by Wu llner
R egnau lt C, .5929 1 424 1 1 0 719 1 316
£2=L316 at 30° C . by Mu ller00
C, o0859 66 789 1 4031
Wiedeman C, .2990 andC
at 60 C . by0
Pagliani
.0636Regnault and at 100
° C . by0
Wiillner
HANDBOOK OF THERMODYNAMIC24
some-
2;
comp
s”
;
9
382?
EC
aam
336
3
282
33
C
am
5?
q
doo
mo
Q
a
fieqwo
m
flawamo
fi
pfi
sa
nwo
fi
nono
q
fim
cowsm
com
a
wafiam
mafimm
no
Eo
m
553
3.
e
e
e
e
e
e
e
e
e
e
e
e
e
e
e
e
e
e
e
u
aoum
Et
a
u
fiG
MH
83
2.9
2
83282
33
8.8
893
54.
85
5.5
82
s
83
6
5855
5
83
8.sso
fls
fim
Ess
a
sacu
sfim
35
9m
mo
fio
aol
awu
floo
qr?
350-
588;
.
hfiu
oa
fifl
fl
35
qEC
385Oa
an
ommm
MN
saw
383sew
none
?sow
Sna
gs
enu
<
0
8330
0
88
q
Sma
c
k-e
m
mo
0
530
34»
e
3.
8
t
encane
m
1
3384
389.
7
36Joaoo
jwEH.
33
fis
sam
.
oo
aa
finsw
Densi t y.3 6
1
Su bst ance.
Aluminum.
Carbon cokeCarbon
graphit e.
Copper .
SteelLeadNickelBrasses and
bronze .
R ubber .
Glass
Solder .
IcePorcelain.WoodWax
Concrete .
TABLES AND DIAGRAMS 25
TAB LE XXVSPECIFIC HEAT OF SODIUM CHLOR IDE BR INE
Sp.gr . Sp. Heat . Temp. F. A u t horit y.
1 007 l 992 — 0 Common1 6 978 Thomsen4 9 .995 66 — 1 1 5 Winkelmann5 0 .960 — 0 Common
1 073 10 0 892 0 Common892 59— 1 20 Teudt
.912 59— 194 Teudt
.887 61 — 1 26 Marignac1 2 3 871 64 4 Winkelmann
1 1 1 5 892 — 0 Common18 8 841 63 1 25 Teudt
18 8 854 68 192 Teudt
1 1 50 20 0 829 Common
791 6 64 68 Winkelmann24 5 791 64 Thomsen
1 191 783 Common
TABLE XXVICOEFFICENT OF LINEAR EXPANSION OF SOLIDS
0 .
“a“ “
am
.2313 1 285 1 75 1 04— 1 1 1 2 Fizeau and
0882 1 692 40 049 094 1 04 west!.054 40 . 03 1 04
. 0786 40 .0437 1 04
. 1 678 40 .0932 1 04
1 061 1 2 10 40 059 0672 1 04
1 095 1 322 40 06085 0735 104
2924 40 1 625 104
1 279 40 . 071 104
.0899 40 . 05 104
. 2234 40 . 1 24 1 104
2918 40 1 621 104
Limits ofl7 0889 1 1 67 32— 1652 determination770 1 6 7— 25 3 4278 62— 77 5 Kohlrausch
058 0897 0- 100 . 03222— .O498 32—21 2 Limits ofdetermination
2508 0— 100 1 338 32- 21 5 Smeaton. 375 — 20 to — 1 .2083 - 4 BrunnerParaffin . 0— 1 6; 38
—49 . 5921 ; 32 R odwell- 1 20
041 3 20—790 68— 1 45 4 Braun
.0325 2—34 .0181 Limits of1 0—26 ; 50—78 8 Kepp43—57
1 430 0795 Clark.046 .0256 ClarkMasonry .
26
Su bst ance.
Alcohol (met hyl)Calcium chloride
, per cent .
Calcium chloride,CaClg,40.9per cent .
Hydrochlor ic acid, ILO
Hydrochloric acid , HCH—50 HzO .
Mercu r
Olive oilPhenol, C.H.OPet roleum, Sp.gr . .8467
Sodium chloride, NaCl, per cent . .
Su lphu ric acid, HzSO.Sulphu ric acid, HgSO.
Su bst ance.
HydrogenHydrogenCarbon dioxideCarbon dioxideCarbon dioxide 0°
Carbon dioxide 84 °— 100°Carbon dioxide 0°Carbon dioxide 64°Carbon dioxide 0°Carbon dioxide 0°Carbon dioxide 0°
Carbon dioxide 0°
Carbon monoxideNit rou s oxideSu lphur dioxideSulphur dioxide .
n n n n n n n
TABLE XXVIICOEFFICIENT OF CUBICAL EXPANSION OF LIQUIDS
a XIO’ A t Temp. 0: X 1 03
per C . C . per
1 433 0796
1 385 1 1 —81 0770
1 1 68 — 7 .0649
0506 18— 25 0281
05 10 1 7— 24 0283
. 21 50 — 1 5 . 1 195
0489 0—30 0272
0933 0— 30 05 19
01 79 0099
0742 0412
0899 3— 1 57 0500
1039 05 77
1067 0593
0489 0— 30 0272
.0799 0—30 0444
TABLE XXVIIICOEFFICIENT OF VOLUMETR IC EXPANSION OF GASES AND
CONSTANT PRESSURE(Heated withou t change of st at e.)
n n n n n n n n no o o o o o o o oo o o o o o o o oo o o o o o o o oo o o o o o o o oo o o o o o o oo o o o o o o o o
e e e e e e e e e
0 0 0 0 0 0 0 0 0
0 0 0 0 0 0 0 0 0
0 0 0 0 0 0 0 0 0o o o o o o o o oWat er vapor (st eam) 0°— 1 19Water vapor 0
°Wat er vapor O°Wat er vapor O°Wat er vapor 0°
o o o o o o o o o0 0 0 0 0 0 0 0 0o o o o o o o o o
Pressu re (Cm Hg)76
256
76
254
76
252
atm.
atm .
atm.
atm .
atm .
atm .
atm.
atm.
76
76
1 atm.
1 atm.
1 atm.
1 atm.
1 atm.
a,xloo
per Deg. C .
. 3671
. 3693
. 3661 3
. 3661 6
. 3710
. 3845
. 5 1 36
.4747
. 7000
. 5435
.6204
.8450
.65 1 4
. 3669
.3719
.3903
.3980
.4187
. 41 89
. 4071
. 3938
. 3799
HANDBOOK OF THERMODYNAMIC
A t Temp.
F .
36— 1 58
32— 1 78
19— 1 40
64— 77
63— 75
5— 100
32— 86
32—86
97— 3 1 4
75 — 248
32—86
32—86
per Deg . F.
. 2040
. 2055
. 2034
.20342
. 2060
. 21 35
. 2855
. 2635
.38885
. 3020
. 3446
. 6100
. 470
.362
. 204
. 2065
.21 7
.221
. 23261
. 23272
. 2261 7
. 2 1878
.21 1 1
PierreKoppPierreDeckerDeckerPierreMar ignacMar ignacSpringPinetteFrankenheimMarignacarignac
Marignac
VAPOR S AT
A u t hority.
R egnaultR egnau ltR egnau ltR egnau ltR egnau ltR egnau ltAndrewsAndrewsA ndrewsA ndrewsAndrewsAndrewsAndrewsAndrewsR egnau ltR egnaultR egnau ltR egnault
HimHimHirn
TABLE XX IXTABLES AND DIAGR AMS 27
COEFFICIENT OF PRESSURE R ISE OF GASES AND VAPOR S AT CONSTANT
Su bst ance.
Carbon dioxideCarbon dioxideCarbon dioxideCarbon dioxideCarbon dioxideCarbon dioxide 0°—64°Carbon dioxide 64°Carbon dioxide 0°Carbon dioxide 64°Carbon dioxide 0°Carbon dioxide 64°Carbon monoxide
Su lphu r dioxide SOs.
VOLUME(Heatedwithou t change of state.)
Pressu re (Cm Hg)
1 atm.
1 atm.
1 atm.
76— 1 04
1 74
793
1 6 4 atm
25 87 8.
33 53
1 atm
1 atm.
1 atm.
1 atm.
1 atm.
¢,X 100
per Deg. C.
. 3767
. 3703
.3663
.3660
. 3662
.3665
. 3670
.3648
.365 1
. 3658
.3665
.3690
. 3887
.4100
. 3671
. 3670
. 3706
. 3726
3686
. 3752
.4252
. 4754
5 728
5406
6973
6334
3656
3705
3674
3845
. 2091 5
. 2057
. 2035
. 20335
. 20345
. 20360
. 20370
. 20265
. 20285
. 20320
. 22775
. 20395
. 2059
.2070
.20475
.2361
. 2641
.256
. 3182
.30035
.38740
.35 190
.2037
.20353
.2031
.20375
.20410
2041
21350
M eleander
M eleander
M eleander
M eleander
M eleander
M eleander
R egnau ltR egnau ltRegnau ltJollyJonyM eleander
R egnault
R egnau lta .t
AndrewsAndrewsAndrewsAndrewsAndrewsgna
Regnau ltJolly
c
c
28 HANDBOOK OF THERMODYNAMICTA BLE
COMPRESSIBILITY OF GASES BY THE IR ISOTHERMALS . VALUES OFPVATAND AT 1 ATMOSPHERE
Pressure in A tmosphere. 300 5 00
9265 91 40 9624 1 1 560
.9730 l .0974 1 .2 144 1 .3400
1 . 5 5 1 1 .668 l .78251 .9866
.9910 1 .0390 1 1358 1 .2568
1 .000 1 1 380 1 . 2090 1 .28281 . 5 1 34 l . 5858 1 .6588
at.890
1 .000
9290 8625 832 7450 5850
9750 95 5 5 9380 8875 8700
Calculated from Smithsonian TablesNos. 55 and 58, reporting Amagat’s results
TABLE XXXIVALUES OF THE GAS CONSTANT R
Det erm ined fromDet ermined fromVolume of One Lb.Specific B eat s by Au t horit y for
R“11
11
; Specific Volume.
768 267 765 893 RayleighRayleigh
andLeduo
0 , R a leighCO Le u c
ThomsonLiqu id at 32°
49 450 54 1 53 Saussure
30 HANDBOOK OF THERMODYNAMICTABLE XXX III
IGNITION TEMPERATURES, °F*
Subst ance . Igni t ion Temperat u re. Su bst ance. Ign it ion Temperat u re.
Carbon, C 752 (Sexton) Methane, OH4 . 1 201 (Meyer )Soft coal 600 Met hane, CH4 1 21 3 (LeChat elier)Anthr acit e 750 Et hane, Os 1 14 1 (A llen)Peat 430 E thylene, C2H4 1 1 24 (A llen)Lignit e du st 300 (St rohmeyer ) Et hylene, OgH4 1 124 (Meyer)Hydrogen,
H2 1 077 (Olsen) Propylene, CaHs 940 (A llen)Hydrogen, H2 1 1 24 (Meyer) A cetylene, Os 1 038 (A llen)Hydrogen, H2 1031 (Le Chat elier ) A cet ylene, Cs 896 (R obmson)Carbon monoxide, CO. . 1253 (Allen) Propane, CsHe 1 01 7
Carbonmonoxide, CO. . 1 347 (Meyer ) A lcohol , CzHaOH 1 292
Carbon monoxide, CO. 1 21 1 (Le Chat eli er ) Coal gas 1 1 00 (R obinson)Methane, CHI 1 2 1 2 (A llen)
‘ Owing t o t he cont rolling infl u ences of propor t ions and ot her fact ors on igni t ion t emperat u re s t he valu egiven are of dou b t fu l accu racy for the igni t ion t emperat u re. at least for gases.
TA BLE XXXIVTHE CR ITICAL POINT
Crit ical PresC rit ical Temp.
su res.
Cri t icalDensit y
Su bst ance , Symbol.Lbs
Wat er A u t hori t y. A u t horit y.at
0° C . A t m . per
4°C = 1 .
Sq .i n .
Hydrogen Hz— 243 5 — 390 1 20 294 Olszewski
Oxygen Oz 1 1 8 1 1 80 4 5 01 735 65 3 1 Wroblewski2Dewar
Nit rogen N:— 1 46 .
1 — 232 8 35 1 5 1 5 . 442 1 Olszewski2Wroblewski
Ammonia NH; 266 1 1 5 . 1 690 DewarAmmonia NH; 1 1 3 . 1 660 Vincent and
Chappu isCarbon dioxide. C0 : 3 1 . 35 1 070 . 464 Amagat
Carbon dioxide. . CO: 1 1 30 . 45 2 1 A ndrews2Caillet et and
Mat h iasWat er HzO +358. 1
. 429 NadeidiniWat er HsO +364 . 3 687 . 7 194 . 6 1 2859 Bat t eli 26 8 NadejdiniWat er 11 20 +365 .0 689 200 5 2944 Caillet et and 1 3 Bat t eli
ColardeauWat er HzO +374 . T rau be and
TeichnerWat er HzO +374 . 6 706 . 3 3200 Holborn and
Baumann
Wat er E zO +374 5 706 1 3200 M arks
TABLES AND DIAGRAMSTABLE XXXV
31
LATENT HEAT OF VAPORIZ AT ION AT ONE ATMOSPHERE PRESSURESelected fromLandolt, Bfimstein, M eyerhofi, and Smi thsonian Physical Tab les.
Su bst ance.
291 32
297 38
296 5Water H0532 0
CeH. 109
1 32 1
1 54 5
56 .25
50 . 76
31 .80
Alcohol, methyl OHOHAlcohol, ethyl Os oH 206 4
Alcohol+5%water .
C io a
H len .H
535
534
964 6
957 6
10 .3
482
372
386
1 09 5
1 57 1
c
1 7
100
LATENT HEATS OF FUSIONSelect ed from Landolt, BOrnst ein, M eyerhofi , and Smi thsonian Physical Tables.
A luminum .
LeadIronCopper
Ammonia .
Ice-water . .
Regnault
60 8 R e au lt62 6 Strombeck212 Andrews212 Schall
R egnau lt
R egnau lt
32 Matthias85 7 Mat thias6 Caillet et
87 4 Matthias148 Wirtz1 72 4 Schall
1 73 1 Brix
1 54 4 M a
1 Goldstein
A u t horit y.
PionchonPersonPionchon
R ichardsMassolPerson and R egnau ltR egnaultDesains
Smi th
32 HANDBOOK OF THERMODYNAMICTAB LE XXXVII
BOILING- POINTS (AT HG)
Selected from Landolt , BOrnst ein , M eyerhot’f, and Smithsonian Physical Tables.
ents
Inorganic com
pounds
Hydrogenn
Ni t t o en
Bromine
Phosphoru sPot assiSodiump u r
Bismu thCadmiumea
Inc
Ant imonya .esmmu 11
SilverCopper
Chromiumron
AmmoniaCarbon monoxideSu lphu r dioxide.
mc c. .on e
H — 252 5 — 41 2
O 182 7 —297
194 4 — 318
33 6 28 5
Br 61 1 1 42
P 287 5 58
K 71 2 1 372
Na 750 1 382
444 7 837
n 2270 4 1 18
B1 1 430 2607d 2 1 440
1 525 2777
n 918 1 686
Sb 1 440 2622
1 1 20 2047
1 3272
A 1955
( hi 2310 4192
n 1900 3452
Cr 2200 3992e 4442
NH; 38 5 — 37 4191 5 - 313
79 1 — l 10 5
SO: 10 8 12 6
n .2 1 347
192 2 — 314191 4 - 312 5
A u t horit y.
Dewar, 1901Holborn, 1901Olszewski
Mean of Thorpe, v an derSchrotter , 1848Perman, R ufl , and JohannPerman, R ufl’, and JohannR othe, 1903GreenwoodBaru s, 1894
GreenwoodBerthelotGreenwoodGreenwoodGreenwoodGreenwoodG :nwoodGreenwoodGreenwoodGreenwoodRegnau lt, 1863Mean of Wroblewski an
R egnau lt, 1863Freyer andMeyerWroblewskiOlszewski
TABLES AND DIAGRAMSTA BLE XXXVII— Continu ed
BOILING- POINTS (AT H0 )
33
Selected from Landolt , BOrnstein, M eyerhofi, and Smithsonian Physical Tables.
Class.
Hy d t oc a r bonconst it u ent s ofl i q u i d and
gaseou s fu els
Parafiine series,CuH2n+ 2
Ethylene series,Ce n
Subst ance. Symbol.
Methane CH;
Ethane OsPropane CaHs
Bu tane C4H1 0Pent ane CslHexane OsHu
Hept ane C7H1 6
0 0133 11 6 OsHl s
Nonane C gHzo
Decane C lo gUndecane Cu HuDodecane CmHze
Tridecane C 1 3H23
Tetradecane. . GuHsoPent adecane . ClsHaz
Hexadecane. . GWHMHept adecane . CnHas
Octadecane C1 8H33
Nonadecane. . C1 9H4o
Ethylene 0 2H4Propylene CaHs
Bu t ylene C4H3
Amylene CaHmHexylene OsHmHept ylene C7HI4
Oct ylene CaHmNonylene Cn s
Decylene CmHzo
A cetylene CsMethyl alcohol . CHaOH
Ethyl- alcohol . . Cs OH
Napht has Mixt ureBenzines Mixt ure
Boiling-
point .
C .
— 1 65
93
45
1
69
1 50
1 73
195
21 4
234
252
270
287
303
31 7
330
- 103
1
36
69
96— 99
122— 1 23
1 40— 1 42
1 75
85
66
78
F.
— 265
1 35
49
302
384
5 18
5 77
602
626
1 53 4
58 5
33 8
96 8
1 56 2
205— 2 10
25 1 — 25 5
284—288
347
- 1 21
1 72 . 4
424 app.
1 77 app.
A u t horit y.
YoungLadenbergYoung, HamlenBu t lerow
,You ng
Thorpe, YoungSchorlemmer
Thorpe, YoungThorpe, You ngKraftKraf t
KraftKraftKraftKraftKraftKraftKraftKraftKraftOlszewskiLadenburg-KriigelSiebenWagner
Wreden
Morgan
M éslinger
Beilst einBeilsteinVillardGeneralGeneral
34 HANDBOOK OF THERMODYNAMICTAB LE XXXVIII
INTERNATIONAL ATOMIC WE IGHTSSelected from R eport of the Internat ional Commi t tee on A t omicWeights, Journal Amer.
Chem. Soc., 1910.
t We'
ht . A t omic Weight .Subst ance. Symbol . AH 1 .
TA BLE XXXIXMELTING OR FREEZING- POINTS (A '
r HG)
Selected from Landolt , BOrnst ein, M eyerhofi , and Smithsonian Physical Tables.
Freezing-
point .Class. Subst ance. S ymbols. A u t horit y.
C . F.
Elements: H — 432 Travers, 1902O 230 382 5 GeneralN - 347 Fischer-AltCl 102 1 5 1 5 Olszewski
Mercu ry Hg 38 Vincent ini andOmodei, 1888Bromine Br 7 . 3 Van der Plaats, 1886Phosphoru s P Helfi, 1893Potassium K Holt and Sims 1894Sodium Na 97 Ku rnakowandPu schin,1902Su lphur . S
1 13
153
5 5236- 247 Depending on form of S
TABLES AND DIAGRAMSTABLE XXXIX— Continued
35
MELTING OR FREEZ ING- POINTS (AT HG)
Selected from Landolt, BOrnstein, M eyerhofi, and Smithsonian Physical Tables.
Class.
Elements:
Inorganic com
pounds
Hydr o carb o nconst it u entsofl i q u i d a n dgaseous fu elPar-affine series,
2n+z
Et hylene Ser ies,2”
Subst ance.
Ti nBismu thC dLeadZincAntimonyMagnesiumA luminumSilver0
CO’
er
Manganese
S iliconN ickelCobaltChromiumIronPlat inumTungst en
AmmoniaCalcium chlor ideCarbon monoxideCarbon di oxideSodium chlor ideSu lphu r dioxide.Zinc chloride .
EthaneNonaneDecaneUndecaneDodecaneTridecaneTet radecanePentadecaneHept adecaneOct adecaneNonadecane
Et hyleneE t hyl alcohol
Freezing-
point .
C .
419624
961
10631 083
1 225
14201 450
‘
1 4901 5051 6001 75 5295 0
780— 203
5782076
1922
— 1 71 41
1
1 69130
5 1 7
62 1
7871 1 54
1 171
1 217165 1
1 71 89222322592264
281 3
2792291 23192
5347
— 1 041 454
— 331 5
1 5 10— 105
— 31 4
41
50
272- 202
A u t hori t y.
Ku rnakowandPu schin, 1902Callendar , 1899Ku rnakowandPuschin, 1902Holborn and DayHolborn andDayFay and A shleyHeycoékandNeville, 1895Holborn and DayHolborn andDayR oberts and A u st inR oberts and A u st inDay - Sosman
GeneralCarnelley, Pictet , 1879GeneralGeneralR oberts andA u st inMean of thr eeWaidner Burgess,Wat erbu rgLadenbu rgandKru ge 1900R u ff and Plato, 1903Wroblewski, Olszewski(mean)
GeneralR u ff and Plat o, 1903Faraday , 1845Brau n , 1 875Wroblewski, 1884
LIQUID DENS ITY. 446 at 32
° F.
.733 at 32° F.
. 745 at 32° F.
.756 at 32° F .
. 765 at 32° F.
.771 at 32° F.
. 775 at 40° F.
776 at 10°
C .
. 775 at 18°C .
. 777 at 22° C .
. 777 at 28°C .
. 777 at 32° C .
. 610
.806 at 32° F.
36 HANDBOOK OF THERMODYNAMICTABLE XLPROPERTIES OF SATURATED STEAM
(Condensed from Marks and Davis’s St eam Tables and Diagrams, 1909, by permission ofthe publishers, Longmans, Green Co.)
Vacuum Tot al Heat A boveinHi
gizesA bsolu t e Tempera
32°F'
Lat ent YéightSf
Gau ge1153323: t iZb In t he 5
38
2 i1 '
Lb f ciil
per Sq .in. heat . Wat er , Heat - u nits S team . Pou nd.v er se- ia Heat - u ni ts
32 3294 .000304
40 2438 .00041 0
1702 . 000587
(L2562 0 1208 .000828
0 871 .001 1 4810 .001 570
0 .002 1 31
100
lbs.
gauge
.0521 3
.05445235 . 5 203 8 1 1 58.8 95 5 1 .05676
.05907
Ent ropyof t heWat er.
Ent ropyof Evaporat ion.
H
H
Ht-‘
H
H
P—‘
I—l
H
H
l—iI—‘H
b—‘HH
H
en8
HHHHHHH
H
H
HHHHH
H
00Q
38 HANDBOOK OF THERMODYNAMIC
Gau ge Absolu t ePressu re Pressu re t u re,Pou nds Pou nds Fahrenper Sq .in . per Sq .in. heat .
129.
1 31
1 33 .
1 35
1 37
1 39.
1 41 .
143 .
145 .
1 47 .
p—L
1—1
I
i
q
TABLE XL— Continu ed
Tot al Heat A bove32 ° F.
In t he In t heWat er , S t eam ,
Heat - u ni t s Heat - u nit s
Heat ,L H — hHeat - u nit s
Cu . Ft . in1 Lb . of
St eam.
ro
wwwwwwwwwwwwwww
wwwwwwwwwp
fi
p
wmmmfla
p
p
e
ux
fi
fi
fi
an
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owCr
ea
mer
. 22
1 6
1 0
.05
00
.94
.89
.84
. 79
. 74
. 69
65
. 60
. 56
. 5 1
. 47
.429
. 347
268
. 192
1 18
047
978
912
.848
. 786
. 726
. 668
. 61 1
. 556
. 504
. 402
. 354
. 308
. 263
219
1 75
1 33
. 092
. 052
. 01 2
.974
.938
.902
.868
.834
.801
Weight of1 C u . Ft .
S t eam ,
Pou nd.
. 191 5
. 1937
. 1959
. 1980
. 2001
. 2023
. 2044
. 2065
. 2087
. 21 09
. 2 1 30
. 2 1 5 1
. 2172
. 2 193
. 22 1 5
. 2237
. 2258
. 2300
. 2343
. 2336
. 2429
. 2472
. 25 1 4
. 25 56
. 2599
. 2641
. 2683
. 2726
. 2769
. 281 2
. 2854
. 2897
. 2939
. 2981
. 3023
. 3065
. 3107
. 31 50
. 3192
. 3234
. 3276
0
0
0
Ent ropyof Evaporat ion.
. 1 581
. 1 561
. 1 540
. 1 520
. 1 500
. 1 481
. 1 461
. 1442
. 1423
. 1 404
. 1385
. 1367
. 1348
. 1330
. 1312
. 1295
. 1277
. 1 242
. 1 208
. 1 174
. 1 141
. 1 108
. 1 076
. 1045
. 1014
. 0984
.0954
.0924
.0895
. 0865
.0837
. 0809
.0782
.0755
.0728
.0702
. 0675
.0649
.0624
.0599
.0574
.0550
.0525
. 0501
.0477
.0454
.0431l v—‘b—flb—‘b—‘H
I—‘H
H
H
H
H
H
H
H
HH
H
H
H
H
HH
H
H
H
HP-‘
H
H
HHHHHHHl—‘H
H
l—‘b—‘H
h—iH
r—eh—‘b—fl
Gauge Absolu t ePressure Pressu rePou nds Pou ndsper Sq .in . per So.in .
Temperat u re.Fahrenheat .
TABLES AND DIAGRAMSTABLE XL— Contz
'
nu ed
TotalHeat Above32° F.
In t he In t heWat er , S team.
Heat - u n it s Heat - u nit s
1 197 .
1 197 .
1 197 .
1 198.
1 198.
1 198.
1 199.
1 199.
1 199.
1 200 .
1 200 .
1 200 .
1 201 .
1 201 .
1 202 .
1 202 .
1 203 .
1 203 .
1 204 .
1 204 .
1 204 .
1 205 .
1 205 .
1 206 .
1 206 .
1 206 .
1 207 .
1 208
1 209
1 210
1 2 10
1 2 10
H
mkKI
OD
QO
CJI
l-‘
Ofi
HQ
HU‘
M
CD
Q
N
CD
O
M
wml
Lat entHeat .
L H — hHeat - u nit s
Volume, Weight ofCu . Ft . in 1 C u . Ft .
1 Lb. of S t eam.
St eam. Pou nd .
Ent ropyof t heWat er .
39
Ent ropyof Evaporat ion .
. 0387
.0365
.0343
.0321
.0300
.0278
. 0257
. 0235
. 021 5
.0195
.0174
.01 54
. 0134
. 01 14
.0095
.0076
.0056
.0038
.0019HHHH
HHHHH
HHHHHH
HH
HH
40 HANDBOOK OF THERMODYNAMICTAB LE XLI
i
f”.PROPERTIES OF SUPERHEATED STEAM
(Condensed from Marks and Davis's S t eam Tables and Diagrams)
l
i l
c =specific volume in cu b ic feet per pou nd , h = t ot al heat . from wat er at 32° F. in B .T .U. per pou nd,
Pressu reA bsolu t e.Pou ndsper Sq .in .
20
40
60
80
1 00
1 20
1 40
1 60
180
200
220
240
260
280
300
350
400
450
500
Temp.
Sat .
S t eam .
1 1. = ent ropy , from wat er at 32
Degrees of Superheat .
0 20 5 0 1 00 1 50 200 250 300 400 5 00
10 .49 1 1 .33
1 1 79 3 121 8. 4 1 242 .4 1 266 . 4 1 361 .6 1409.36761 1 . 7089 1 .7674 1 .81891 .8427 1 .8867 1 .92711 7
1 1 87 .3 1276 .4 1 324 .3
6432 1 . 6568 1 .7062 1 . 784947 5 651 2 3 1 234 . 3 1 283 . 6 1 307 .8 1 331 .91 3798 1427 .9200 1 . 6532 1 . 6833 1 . 73681 . 761 2 1 . 7840 1 .8265 1 .8658
6 1 2
. 3 1239. 7 1 264 .7 1 289. 4 1 3 1 3 . 61 . 63581 .6658 1 . 6933 1 .71881 . 74281 . 7656
.85 6 481 1 269. 3 1 318 .4 1 342 .7 1439.4
. 601 6 1 . 62 1 6 1 . 67891 .704 1 1 . 7280 1 . 7505
. 32
. 5894 1 6096 1 .6395 1 . 6666 1 . 691 6 1 .7792
. 3
.0 1 224 . 5 1 25 1 . 3 1 301 . 7 1 326 . 2 1 350 . 68
. 75
904
92 9.8823
8
2 1 285 . 2 1 310 .3 1 359.81408.8 1457 .75 3 1 . 6049 1 .6787 1 . 7005 1 . 741 5 1 . 7792
3. 26
0
1
1 .
7 .
1
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. 2 1291 .91 3 1 7 . 2 14 1 6 .4 1465 773 1 . 61 33 1 . 6375 1 . 7223
. 2 1418 6 146804 1 . 6082 1 .6765
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HANDBOOK OF THERMODYNAMIC48
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HANDBOOK OF THERMODYNAMIC52
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HANDBOOK OF THERMODYNAMIC
204
201 .
198.
20 1
194
195
1 91
191
186
190
185
1 80
1 83
1 78
1 80
1 75
1 75
1 7 1
1 70
1 70
1 68
1 65
1 65
1 64
1 60
1 61
1 5 6
1 5 6
1 5 6
1 5 2
1 5 1
1 49
1 5 1
1 47
1 47
1 44
1 43
1 4 1
1 43
1 40
1 39
1 37
1 34
1 32
1 33
1 3 1
1 30
1 29
1 26
1 25
1 22
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mmmmm
TA BLE
SOLUTIONS OFR ELATION BETWEEN PR ESSURE ,
TEMPER ATURE,Upper figu res are S tarr values,
POUNDS PE R SQUAR E INCH GAGE
20 25 45 50
234 247 4
232 242 25 1 260 286
23 1 243 3
226 236 5 254 281
230 242 1
225 235 5 25 3 280
225 236 6
219 229 238 280
22 1 232 3 24 1
21 4 224 5 233
220 231 2 240
2 1 3 223 232 268
2 14 225 8
207 2 1 7 5 235 268
2 1 2 224 1
206 21 6 225 234 26 1 266
299 220 5 237
202 21 2 5 22 1 25 7
205 2 1 6 2 25 7
198 208 5 2 1 7 225 258
204 2 1 5 3
197 207 5 2 1 6 224 25 7
199 2 19 3
193 293 246 25 2
197 209
1 91 202 24 5
194 205 222
188 198 5 207 21 5 247
1 89 200 6
184 194 0 203 21 1 237
1 85 196 1 236 1
1 79 190
180 191 9
1 75 1 85 5 228 233
1 79 191 0 199 6
1 74 1 84 5 227 232 5
1 76 1 87 4 196 1
1 71 1 81 5 1 90 198
1 72 183 4 192
1 67 1 78
1 7 1 182 9
1 67 1 77 5 1 86 219 224
1 67 1 78 7
1 63 1 73 5 1 82 190 2 1 5
1 63 1 74 5
1 59 1 69 5 1 78 1 86 21 1
1 62 1 73 3
1 5 7 1 68 5 1 77 1 85 2 1 0
1 59 1 70 1
1 5 5 1 65 5 1 74 1 82“
207
1 5 4 1 65 6
1 5 1 1 61 5 1 70
1 5 0 1 6 1 6
1 47 1 5 7 5
XLIV TABLES AND DIAGRAMS 5 5
AMMONIA IN WATERAND PER CENT NHa IN SOLUTIONlower figu res are new.
Anov n orm Su m u xm Am ospnnnn ‘5
6?F‘ 0
65 £ 2 3
306
301
309
290
289
283
280
267
264
262
243
239
222;
21 3 5
56 HANDBOOK OF THERMODYNAMICfIUynxaa
SOLUT IONS OFRELATION BETWEEN PR ESSURE TEMPERATURE
,
POUNDS PER SQUAR E INCH GAGE
Per
Cent
NH:
by
Weight
199
197
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192 .
191
188.
187 . 00
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TABLES AND DIAGRAMSXLIV— Contz
’
nu edAMMONIA IN WATERAND PER CENT NH. IN SOLUTIONABOVE ONE STANDAR D A 'r u osm mnm
58 HANDBOOK OF THERMODYNAMICTA BLE XLV
AM MONIA — WATER SOLUTIONS
VALUES OF PARTIAL PRESSURES OF AMMONIA AND WATER VAPOR FOR
VAR IOUS TEMPERATURES AND PER CENTS OF AMMONIA IN SOLUTION"5 El E] “
a“a a E! “
a‘
8 a 52 <3 3 3 5 33 0 8. 5 5
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25 {33 5 $3 $5. 3 5 25 35. 3 5
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s 5 2 33 5 3 58 .2 2 5 3 5 3 2 6
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g Press. Inches Hg Press. Inches Hg Press. Inches Hg
32 236 1 77 41 3 5 1 2 1 58 670 788 1 58 946256 197 453 5 71 197 768 867 197 l 064
276 236 5 1 2 591 236 827 945 2 16 1 1 61
295 276 5 71 650 276 926 1 041 256 1 297
31 5 31 5 630 709 31 5 1 024 1 1 6 295 1 45 5
354 35 5 709 788 35 5 l 343 1 28 335 1 6 1 5394 413 807 866 394 1 260 1 4 1 5 374 1 789434 472 906 965 452 1 41 7 1 5 75 433 2 008 2 .
492 532 1 024 1 062 5 1 1 1 573 1 6 1 75 473 2 223
552 590 1 1 42 1 18 590 1 770 l 9 1 925 5 52 2 477
68. 6 1 1 670 1 281 1 3 1 3 19 649 1 958 2 2 1 25 61 1 2 736670 748 1 318 1 5 1 45 5 728 2 183 2 2 2 34 689 3 029
729 847 1 5 76 1 6 1 592 826 2 4 18 2 6 2 58 788 3 368
807 945 1 752 1 8 1 75 925 2 675 2 8 2 835 866 3 701
885 1 O6 1 945 2 1 925 1 043 2 968 3 3 09 985 4 075
86 985 1 2 2 185 2 1 2 1 25 1 180 3 305 3 5 3 49 1 1 22 4 6 1 2
1 085 1 36 2 445 2 5 2 30 1 34 3 64 3 8 3 70 1 28 4 981 18 1 5 1 5 2 695 2 8 2 52 l 495 4 01 5 4 l 4 06 1 435 5 4951 28 1 69 2 97 3 2 725 1 672 4 397 4 5 4 42 1 6 1 5 6 035 61 38 1 89 3 27 3 4 3 01 1 870 4 880 5 4 82 1 81 6 631 45 5 2 1 25 3 580 3 8 3 29 2 085 5 375 5 2 5 27 2 03 7 301 65 5 2 36 01 5 4 3 58 2 30 5 88 6 5 72 2 245 7 965 81 81 1 2 62 431 4 6 3 90 2 56 6 46 6 5 6 18 2 50 8 681 970 2 95 4 920 5 4 23 2 81 5 7 045 7 6 78 2 76 9 542 1 5 3 21 5 36 5 2 4 58 3 1 1 7 69 7 8 7 33 3 05 10 382 320 3 54 5 860 5 9 4 96 3 44 8 40 8 5 7 89 3 37 1 12 520 3 88 6 400 6 4 5 35 3 80 9 1 5 9 8 55 3 70 1 2 25 1 2 .
2 740 4 29 7 030 7 5 80 4 22 10 02 10 9 25 4 07 1 3 322 95 5 4 73 7 685 7 8 6 25 4 65 1 0 90 1 1 9 89 4 5 1 4 393 1 5 5 2 1 8 36 8 2 6 72 5 1 2 1 1 84 1 2 1 0 06 4 98 1 5 04
1 40 3 37 5 77 9 1 4 9 7 2 5 63 1 2 83 1 2 9 1 1 45 5 49 16 94 1 6 9
1 0 1 5
1 38 1
1 57 1
1 77 2
21 7 2 3256 2
50 295 2
335 3
394 3
453 3 55 12 4
TABLES AND DIAGRAMS 59
TABLE XLV— Continu ed
Per cent5
3 3 8 5 3 3 E 3 3 E Ea s" o (5 3g 0 8 o a
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a Press. Inches 1 13 Press. Inches Hg Press. Inches Hg
68 3 09 590 680 3 8 4 22 571 4 791 5 5 5 5 5 52 6 102 63 4 670 070 4: 4 61 65 5 26 5 4 6 1 631 6 7313 74 767 507 4 6 5 04 729 5 769 6 6 7 71 7 414 09 847 937 5 5 5 5 827 6 377 6 6 7 33 81 8 1 4 84 49 965 455 5 4 6 08 926 7 006 7 7 98 906 8 886
86 4 9 1 1 0 6 1 6 66 04 7 70 7 8 8 66 1 005 9 6655 35 1 24 59 6 8 7 26 18 8 44 8 5 9 5 1 1 2 10 62
5 86 1 4 26 7 4 7 92 32 9 24 9 3 10 35 1 26 1 1 61
6 37 1 5 55 925 7 9 8 63 47 1 0 1 0 1 0 1 1 28 1 42 1 2 706 94 l 75 69 8 8 9 38 67 1 1 05 1 1 1 2 25 1 59 1 3 847 5 1 95 45 9 5 10 18 87 1 2 05 1 2 13 22 1 77 14 99 1 58 19 2 1 65 35 5 10 4 1 1 02 07 1 3 09 1 3 14 30 1 98 1 6 288 88 2 42 30 1 4 1 1 9 32 14 22 14 4 1 5 45 2 2 1 7 65
9 6 2 68 28 12 2 1 2 88 56 1 5 44 1 5 7 16 62 2 44 19 06 191 0 38 2 97 35 1 3 3 1 3 85 83 1 6 68 1 7 1 7 9 2 69 20 591 1 22 3 25 47 1 4 5 14 95 1 3 18 08 18 19 3 2 97 22 271 2 05 3 58 63 1 5 51 2 95 3 96 91 1 71 3 95 4 37 32 18 21 5 0 4 81 81 201 6 5 5 29 79 2 1 2
2 72
3 0
3 29
3 62
4 02
4 41
53 . 4 8757 l2 5 36
5 92
6 5
7 1 37 8
8 5 59 3310 2
1 1 1
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1 3 2
1 4 351 5 61 6 9518 45
60 HANDBOOK OF THER M ODYNAM IC
TAB LE XLVIABSORPTION OF GASES BY LIQUIDS
Selected from Smithsonian Physical Tables.
Values of x¢= v olume of gases referred t o 32° F. and ins. Hgwhi ch one v olume ofwater can absorb at atmospheric pressure and temperatu re of first column .
.02542
TABLE XLVIIABSORPTION OF A IR IN WATER (Wmm n, 1904)
Air free of 003 andNE measured at ins. and 32°F.
Cu .ft .Sum ofT
3632” 253332
9
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0 10 . 19 20 . 141 9-91
2 9- 64
3
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6
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9 8.06
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1 1 7 68 16 50
13
1 4
1 5
62 HANDBOOK OF THER M ODYNAM ICTAB LE L
COEFFICIENTS OF HEAT TRANSFER
AVER A GE PR A CTICE
Thermal Action in Substances.
Giv ing Up Heat. R eceiv ing Heat.
Liquid warming
GaswarmingLiquid cooling
Liquid boiling
Liqu idwarming
Gas coolingGaswarmingLiquid boiling
Liqu id warming
Vapor condensing .
GaswarmingLiquid boiling
B .T .U. per Hou r per
Squ are Foot perDegree.
50— 75
2— 6
1 00
10— 20
30— 50
2— 5
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1 50— 350
1 000
2 - 4
400—600
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Liquid heat exchangers, aquaammonia water and beercoolers
,ammonia absorber
cooling coilsHot -water radiators and cooling tower surfaces, dependingon air v elocity and characterof water su rfaceShell brine coolers with cirenlator ; tank brine coolersW ithout circulator ; doublepipe brine coolers dependingon v elocity and hot liquidev aporatorsBrine coolers in cold storagerooms depending on air circu
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mental feed-water heaterhigh .v elocitySteam radiators and pipesVacuum ev aporators W ith con
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PAR AFFINES (CnH2n+2) FROM PENNSYLVANIA PETROLEUMBoiling- point. M clee 0
1351
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55333
Name. Formu la.
Specnfic (Erawt y u larat 32 F. W elght
C . F. A pprox. C .
M ethane CH. 16 75 25
Gas Ethane . CzHo . 446 30 80 . 1 2Propane CaHg— 25 1 3 . 5 36 44 81 .84 18. 16
Bu tane C4Hm 0 32 . 60 58
Pentane normal . CsHu 38 1 00 4 . 627 at 5 7 72
. 628
Pentane iso CsHm 30 86 658at 68 72 83 33 1 6 . 67
Hexane normal . CsHu 69 . 664 86 83 . 76
Hexane iso 0 611 14 6 1 . 683 at 68 86 83 . 76
Heptane normal . C7H1 , . 699 100
Heptane iso C7H1a 91 . 702 at 68 100
Octane normal . . Can 1 25 257 . 703 1 1 4
Octane iso C sHm 1 18 . 718at 68 1 14 1 5 . 79
Nonane Co o 1 36 . 741 1 28 1 5 . 62
Decane 0 1 0s 1 73 . 73 at 68 1 42
. 757
Endecane Cq 4 182 . 774 at — 1 5 1 5 6Liqu id
. 75 5
Dodecane CmI‘Iza 198 . 773 at — 1 0 1 70
. 776Tridecane C ISHZB 216 . 792 1 84Tetradecane GuHso 238 . 775 at 39 198 1 5 . 1 5Pentadecane OISH32 258 2 1 2
Hexadecane 0 1 511 34 280 536 . . 775 at 64 226Octodecane C 18H38 254
Eicosane 0 2011 42 205 401 . 778at 99 282 85 10Tricosane 0 23111 43 234 453 . . 779at 1 18 324Cs sz 352
Paraffine (myricle) Cz7Hsa 380 85 . 26Solid Parafii ne (ceryl) . CacHez 370 698 422
ETHYLENES (CnHzn) AND NA PHTHALENES FR OM R USSIANPETROLEUM
Ethylene . (3q 28 85 7Propylene . CsHa 42 85 7Bu tylene . C4Hs . 635 56 85 7Amylene . CsHm 70 85 7Hexylene 0 15l 1 58 . 76 84 85 7Heptylene O7H14 . 71 4 98 85 7Octylene . CeHm . 733 1 1 2 85 7
Oct . Naphthalene Cn o- l- Hs . 771 85 7
Nonylene CgHm 1 26 85 7Diamylene c1lo . 777 85 7
Cns 356 1 54 85 7C 12H24 168 85 7
Dodeca Naphthalene C l 18+Hs .803 162+6 85 7 14 3Cq a 464 . 196 85 7
Triamylene C lsHso 2 1 0 85 7Tet raamylene Co m ov er 280 85 7
90 HANDBOOK OF THER M ODYNA M IC
TA BLE LIX— Continu ed
CALOR IFIC POWER OF HYDROCAR BON OILS BY CALOR IM ETER AND
CALCULATION BY DENSITY FOR M ULA OF SHER M AN AND KR OPFFB .T .U. per Pou nd .
SNo . Class of Oil. 111 1
7 1,
Degrees Bé.
En
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1 5 °C . Calo Calcu l .rimet er . S .&K. Form
42 8820 28 75 19643 19400 1 22
43 Kansas , cru de . .8828 19249 19396 . 73
44 .8833 19474 19390 .42
45 Indian Territory .8860 19454 19370 .42
46 .8862 19372 19370 .Ol
47 Indian Territory .8900 19418 19342 .39
48 Texas,cru de .891 4 19242 19332 .45
49 .8970 1935 5 19294 .31
50 .9007 19359 19267 . 47
5 1 .9050 19228 19238 .05
5 2 .9065 19352 19228 . 63
5 3 Kansas, cru de .9066 19089 19226 . 69
54 .9087 19282 192 1 3 . 35
5 5 Kansas, cru de .91 14 19303 19194 . 55
56 Texas, cru de .91 37 19028 191 78 . 76
5 7 Texas, cru de .91 53 19246 191 68 .3958 Texas , cru de .91 5 5 19008 191 66 .80
59 California, cru de .91 58 18572 19166 +2 5860 Fu el Oil .91 70 191 03 191 57 . 28
61 California, cru de .91 79 1 8779 191 50 + 1 9462 California, cru de .9182 18985 191 49 .83
63 Texas, cru de .9336 19080 19048 16
64 California , cru de .9644 18589 18858
TA BLE LX
PROPERTIES OF OIL GAS
Volum etric A naly sis. A t 32° F. and Hg Pressu re.
No . Description . $5 C F
B -TliUo
‘Der 13 1
11 11] De?
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£ 5co . 0 2 n g.
High . Low. High. Low.
1 Thwa ite oil gas . 63 . 1 9 4 5 06 26072 238692 Pintsch American oil 63 . 1 5 . 6 . 4 8 1 1 73 . 1 074 . 2281 5 208893 Pintsch American Oil 61 2 6 . 4 28 3 2 7 1 9 6 1 260 7 1 064 247 1 0 208544 Oil gas 58 3 23096 18650Pi ntsch gas from
petroleum residu e 24 3 1 7 . 898. 24260 22000Pintsch gas fromparafi ne oil 19065 1 7509Ameri can petroleumoil gas 41 2 . 2 22607 20812Pintsch gas, M ooreea 5 . 5 3 20060 1 6940
9 General 48. 32 . 3 23 . 1 6 7 1 6 . 20874 1 65831 0 Cru de oil R etort gas,
England 1 4 . 3 1 1 07 . 23282 185421 1 Engl i sh shale oil gas.
You ng and 19. . 63 . 24 1 5 22333 20682
The hydrocarbon analy ses in this tab le for oi l gas are q u ite u ncertain, b u t less so than the hydrocarbons equ i v alent t o kerosene and gasolene.
1 6
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TABLES AND DIAGRAM S 91
TA BLE LXI
COM POSITION OF NATUR AL GA SES
Volumetric Analysis.Sou rce. A u thority
0 2. 0 11 4. H2. CO. Cz 'Hc. N2. C0 1 .
West Virginia R eport Gas Eng.
Com . N . E . L . . 4
Kansas R eport Gas Eng.d
. 25
Cau casu s BunsenCau casu s Bu nsenKokomo, Lev in . 3 . 55 .3 . 29
Kokomo, Ind Eng. M . J . 3 . 5 5 .3 .29
St . Mary’s, Ohio . Lev in .35 . 44 . 2Lu cke .35 . 44 . 2Marion, Ind Eng. M . J . 5 5 6 . 1 5 . 3Marion, Ind Lev in . 5 5 . 6 . 1 5 .3Findlay,Ohio Eng. M . J .39 .4 1 .35 . 25Findlay, Ohio . . Lev in . 39 .41 . 35
English . Lewes 4
R u ssian . . Lewes 6 .98
Cau casu s Bu nsen 6 .98 .492 . 18
Anderson , Ind ‘ng .42 .73 .47 .26
Anderson, Ind Lev in . 42 . 73 .47 . 26
Ohio Lewes .35 5 . 75Fostoria, Ohio Eng. M . J . 35 1 .89 . 5 5 . 20 . 20Mu ncie, Ind Lev in . 35 .4 . 25Mu ncie, Ind Eng. M . J .35 . 45 .25 .25 .Findlay, Ohio. . Gill . 3 . 5 3 .3
. 5 3 1
Cau casu s Bu nsen 1 .94 .93
Cau casu s Bu nsen 6Leechbu rg, Pa Hoyle . 26 .35
1 .6
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Com . N . E . 1 . 2 . 5 5
Bu tler County, Pa . . Hoyle . 66
Bu tler Cou nty, Pa . . Hoyle . 34
U. S Ford 1 . .8
Pittsburgh, Pa . Lev in .8 20 . 1 . , 8
Penna Jiiptner 22 . . 6 3 0 .6
Pittsburgh, Hoyle .8 22 . . 6 3 0 .6
U. S Ford .8 .8 .6
U. S Ford . 78 . 58
U. S FordFord .8 . 4 .4
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98 HANDBOOK OF THER M ODYNA M ICTA BLE Lx lV
COMPOSITION OF UNITED STATES COKE
(M ainly from U. S . Geological Survey R eports)Ori gi n.
Ivffi
l
e
s
'
t"
From Connelsville bituminou s coal, 72 hou rs roasting . . 23From Connelsville bit uminou s coal, 48hou rs roasting . 19Foundry Ganley Mountain, U.S .Geological Survey . . 75Foundry Milwaukee Solvay, U.S .G.S .27From Connelsville, U.S .G.S 1 8From A labama coal,
No . 1 . 33From Arkansas coal, No . 6 1 . 30From Illinois coal,
No . 2 1 . 5 7From Illinois coal,
No. 3 .96From Indiana coal,
No. 1From Indi an Territory, No . 2From Iowa,
NO. 1 2 . 1 1From Iowa,
No . 3 1 .80From Kentucky,
No . 1 . 5 1From Kentucky, No . 4 . 5 2From M issour i, No . 2From West Virginia, No . 1 . . 40FromWest Virginia, No . 2 . 59FromWest Virgin ia, No. 3 . . 38From West Virgin ia, No. 4 . 20From West Vir gini a, No . 5 . 42FromWest Virginia, No . 6 1 . 00FromWest Virgini a, NO. 1 0 . 60
00FromWest Virginia, No . 1 .Connelsville average of 3, J . B . ProctorChattanooga,Tenn .
,average of 4
, J . B . ProctorBirmingham, A la .,average of 4, J . B . ProctorPocahontas, Va .
,average of 3, J. B . Proctor
NewR iver, W . Va ., average of 8, J. B . ProctorBig Stone Gap , Ky . , average of 7, J . B . ProctorA labama, run- of—mine, fou ndry, M oldenke 1
A labamawashed slack, fou ndry, M oldenkeColoradowashed slack, foundry, M oldenke
Illinoiswashed slack, foundry, M oldenke 2 .
. 23Pennsylvaniawashed slack, foundry, M oldenkePennsylvania washed slack, foundry, M oldenke
Tennessee,foundry
,M oldenkeTennessee
,foundry
,M oldenke 1 .
1 6Virginia, foundry, M oldenke
Virginia,foundry, M oldenke 1
67
60
West Virginia,fou ndry, M oldenkeWest Vir ginia, foundry, M oldneke
Proposed standard foundry coke specification
. 34
.75
. 44
78
. 22
67
52
Volati le.
1 .
. 5 1
.35
. 48
. 32
. 72
.85
.83
. 44
. 24
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. 79
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. 73
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Fixed 1Carbon.
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. 7
TABLES AND DIAGR AM STABLE LXV
PRODUCTS OF BITUMINOUS GAS COAL DISTILLATION (JUPTNER )(Variation with coal composition )
England. Commentry
Specific Gr .
60° F.
. 590
.625
. 635
.680
.717
.742
.780
.800
85
.980
. 725 765
.817 828
840 860
870 897
.908 91 2
91 5 920
1
136
1 07
94—92
91 — 83
76—70
65
58
49
44
35
28— 22
1 3
63— 53
4 1 — 39
37— 33
3 1 — 26
23— 22
99
Blanay .
1
.88
BoilinPai nt,
32
64
86— 1 58
1 40—21 2
321 2— 265 a
300— 5 75 3300— 700 g
4
Russian
Coal from
Moistu reAsh 7 .06Coal composition0 2
per °F*“bywe‘ght H2CN2 1 1
wei ghtGas Pr°du °ed Per Vol. cu bic meter
C0 2
CO
Hz
Volumetric analysis CH.
of gasCsHe .79 .99
OgH4
TABLE LXVIAVER AGE DISTILLATION PRODUCTS OF CRUDE MINERAL OILS (R OBINSON)
se
am.Class.
Fi eld?
Cymogene smallPetroleum ether. . R higolene . 1Gasolene 1
C naphtha 10Petroleum spirit. B naphtha 2
A naphtha (benzene) 2
L m kerosene Water white 1 2 20a p
Ordinary kerosene . 40 — 55
Intermedi ate as oLubricating oil
Heavy oils Paraffine 2
R esidue and loss 5 — 10
Petrol Gasolene or benzene . 5 — 1 6
Lamp oils Kerosene . 30 —40
Intermediate Solar oil . 1 0 - 12
Spindle oil. . 1 2 — 1 5
Lubricating oils . Engine oil . 25 —40Cylinder oil 3 5Fuel oil R esidu e, astatki orgou dron 1 0 - 1 5 900 950 25— 1 7
1 00 HANDBOOK OF THER M ODYNAM ICTABLE LXVII
FR ACTIONATION TESTS OF KEROSENES AND PETROLEUMS
No. Class and Den si ty of Original.
American kerosene 9
R obinson 10 43 5Sp .gr . . 797 1 6 .821
Bé..831
836
. 786
.799
.816
.829
R obinson 18 419 831Sp .gr . .825 12 464 9
Bé. 6 509 .857
.864
.877
A lsatian petroleum302 392
4 gngler d
go
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l
chest opal 392 482
13125143 482 572
5 72 608
“Kaiser oil 302 392
5Engler Schestopal 32 . 3 392 482Sp .gr . . 795 26 3 482 572
Bé. 1 1 7 572 608
302Pennsylvani a kerosene 22 302 392
6Maschinenfabrik, Augsburg 19 25 392 482SP-gf -800 482 572Ré. 45
572 608
1 02 HANDBOOK OF THER M ODYNA M ICTABLE LXVIII
FRACTIONATION TESTS OF GA SOLENESTemp. of Di sti llation .
Volumetric Density of DensityNo. Class and Densi ty of Ori g inal . Per Cent D i sti llate, Baumé
.
Di sti lled. Deg. F. at Deg. F. at 60°F.
Beginning . End.
39 1 58 21 2 . 722
1 ggs
gilenggg
lwnfl 49 21 2 248 . 748
Bé'
595 248 271 . 757
271 . 767
48 1 58 2 1 2 . 727
2 Sgs
g
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bm fl 37 2 1 2 248 . 747
Bé°
(50 2 248 271 . 762
271 . 767
1 49 21 2 . 708
3 gf gilen
gnlmcm t ] 21 2 248 . 742
Bé'
248 271 . 754271 . 769
1 49 21 2 . 707 68
4 gfglen
gmlmoun” 2 1 2 248 . 743
Bé248 271 . 75 1
3 271 . 770
1 45 21 2 . 704
5 gfgen
gmlmouml 21 2 248 . 742
Bé248 271 . 753 56271 . 772
1 49 21 2 . 71
6 gf gfilen
gnlmouml 21 2 248 . 744
M248 271 . 753271 . 769 52
1 40 2 1 2 . 706
7 gf gilenglglmwnt l 2 1 2 248 . 742
Bé'
64 7 248 271 . 750271 . 770
66 1 40 21 2 . 700 70
8 glis
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Bé.
248 271 . 741271 . 762
59 145 21 2 . 701
ggéggkéglgmwnt l 2 1 2 248 . 736
Bé.
271 . 750271 . 765
1 45 2 12 . 699
1 0 gfg'
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21 2 248 . 730
Bé.
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68 1 36 2 12 . 699 70 . 1
1 1 ggs
ggkr
fgmlmm fl 212 248 . 736
Bé.
248 271 . 750
271 I l l l l l l t .736
TABLES AND DIAGRAM S 1 03
TAB LE LXVIII— Continu edFR ACTIONATION TESTS OF GASOLENES
Temp. of Di stillation.
Volumetric Denqm' Of DensitNo. Class and Densi ty of Origi nal . Per Cent Disti llate. BaumDi sti lled. Deg. F
:at De
findF. at GO° F.
Beginnmg.
Gasolene [mount] iizi iii 33 19331 2 Sp .gr. . 700248 271B6. 70
5 271
22
222 22
2 224
358251) 7 8
3 248 271 .7553 271 .768
1 49 21 2 .705
1 4(874880 1n [l3l°t 26 21 2 248 .740
Bé$65 3
248 271 . 754271 . 770
68 1 49 21 2 .705
1 5 38
80144119
71 7[1310t 23 2 1 2 248 .743
B120825 .
3248 271 . 755
4
271 . 773
2 6Gasolene [Blount] g;5
51
1
1
3 248 3231 3
15312525 5
1 7248
“
271 .758271 . 770
Gasolene [Blount] 32 223 233 2?1 7
248 271 . 749 575 .
271 . 770
73 1 31 21 2 .697 71
5931011 1141 2 12 248 .736
mm 05 248 271 .75 1
Bé 68- 63 271 . 768
74 1 40 21 2 .696Gasolene [Blou nt l 21 2 248 .73619 Sp .gr . - 705
248 271 .745Bé. 68 6 271 .764 53 2
1 76 1 761 76
Gasolene [Chambers] 626 28622 2
‘i 220
20 Spar . - 71R6 67 18
31 1
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106 HANDBOOK OF THERMODYNAMICRATE OF FORMATION OF CO FR OM C0 2 AND CARBON
Form of Carbon.
Fine, amorphou sCharcoal, 2— 5 mm .
Charcoal, hazel nu t .
Coke, 2— 5 mmCoke, hazel nu tGas carbon,
2— 5 mm .
Gas coke, hazel nu t . .
1 . Charcoal, 5
2 . Charcoal, 5 mm . .
3 . Charcoal, 5 mm . .
4 . Charcoal, 5 mm . .
5 . Charcoal, 5 mm . .
Charcoal, 5 mm
6. Coke
Temp .
Deg. F.
1 472
1 472
1 472
1 472
1 472
1 472
1 472
1 472
1 472
1 472
1 472
1 472
1 472
1 472
1 472
1 472
1 562
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1 652
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1 6971 6971 6971 6971 697
1 697
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1832
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1 832
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201 2
2012
2012
201 2
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1 652
1 652
1 652
TA BLE LXX
T ime.
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TA BLE LXX— Continu ed
RATE OF FOR M ATION OF CO FROM 00 2 AND CARBON
Volumetric A nalysis.
Form of Carbon. 8653161
1
1
1
6
35 . CO COA u thority.
00“ CO0 0 2 co+0 0 2
1 652 1 6 4 .9 .05 1 . 0496 . Coke 1652 .027 .026 Clement
1652 .8 .008 .008
1832 1 23 21 .6 . 784
1832 80 . 644
1333 33 52 .
g1 1 2 529
9 32 . . 47 . 320l . Coke
1832 . 1 6 . 1 39Clement
1 832 . 1 3 . 1 1 5
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201 2 90 2 9 971
201 2 30 854
201 2 1 3 . 661
2012
g;. 5 5
?20 2 3 6 . 318. Coke
201 2 30 . 4 . 437 . 304Clement
201 2 . 31 6 . 240
201 2 . 284 . 22 1
201 2 . 272 . 21 4
201 2 1 3 3 . 1 54 . 1 33
2 192 19 98.9 .989
2192 1 33
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2192 8. 4 . .9539. Coke
2 192 . 685Clement
2192 . 78 . 439
2192 33 5 504 . 335
2372 . 1 999 .9
39
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Clement2372 .834
201 2 34 .878
201 2 . 601
1 0. A nthracite 201 2 .91 . 477 Clement201 2 . 43 . 302
201 2 . 36 . 265
2192 47 . 3 .997
2192 1 0 1 4 4 5 .95 856
1 1 . A nthracite 2192 . 71 5 Clement2192 . 73 . 423.
2 192 . 45 . 3 10
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2372 .965
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b—l O3 . 20 . 021 3 . 0208
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TAB LE LXXVCOMPOSITION OF POWDER ED COAL , PR ODUCER GA S
Volumetric A nalysis. Per Cent . R atio. gugnggl:Sample .
CO CO
OH4 Nz 0 0 2 CO +0 0 2High . Low.
1 . 63 1 19 1 1 1
2 . 63 1 40 129
3 3 20 . 62 1 1 2 1 03
4 . 79 1 28 1 19
5 . 63 1 18 109
TA BLE LXXVICOMPOSITION OF BOILER FLUE GASES— (VOLUM ETR IC )
Stat. Boiler, IllinoisGozl,U. S . Geological Su rv ey . Locomoti v e Boiler, U. S . Geological Su rv ey .
A vil
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A nalysis.CO CO
A nalysis .CO C0
C0 2 CO+COz CO: CO +COzCO: 0 2 C0 C0 2 0 2 C0
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5 . 04 . 0068 . 00674 . 1 7 . 01 48 . 0147
6 . 03 . 00485 . 00482 . 23 . 0193 .0189
9 .07 . 0109 . 0108 . 1 4 . 01 17 .01 55
1 6 . 1 0 . 01 52 . 01 49 . 1 5 . 01 25 . 01 23
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20 .08 .01 1 1 . 01 1 . 20 .01 47 . 01 45
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1 18 HANDBOOK OF THERMODYNAMICTABLE LXXVIII
LIMITS OF PR OPORTION FOR EXPLOSIVE AIR -GA S MIXTURE SGas. A u thor ity .
Combining When A ir is in W hen Gas is inProportion. Excess. Excess.
Carbon monoxide EitnerBunte
29 6 1 3 0 75 ClowesHydrogen 29 6 Eitner
29 6 Bu nteM .I .T.
C lowesWater gas, theoretical Eitner
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6 25 GroverBoston illuminating gas . M I T
M .I .T.
M .I .T.
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ClowesEthylene 6 . 5 4 1 1 4 6 Eitner
6 5 4 1 10 5 BunteM ethane . Eitner
Bu nteClowes
Ether Eitner2 75 Bu nte
Benzene 2 . 7 2 65 EitnerBu nteEitner
Pentane BunteEitner
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65°Bé M .I .T.
Alcohol 6 5 3 95 1 3 65 Eitner3 95 Bunte
Blau oil gas HallockPintsch oil gas . 5 .0 13 .0 Lu ckeEthane 4 0 22 0 Clowes
1 19TABLES AND DIAGRAMScm.
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1 22 HANDBOOK OF THER M ODYNAM IC
TA BLE LXXXDIAGR AM FACTORS FOR OTTO CYCLE GAS ENGINES
Engine.
Fou r cycleFou r cycle
40'
H.P . four cycleCockerill
CockerillLetombe
Winterthu rCie . Berlin AnhaltBenzDeu tz
SchmitzOtto- Deu tz
Winterthu r’
SchmitzWinterthu r
Du dbridge
NationalGiildner
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S ize in Inches. Compression.
T estA u thority .
M eyer
Bu rstall
Hopkinson 6 37
Hubert
WitzFrancoisWitzAllaireWitzMethot
M athot
Me thotWitzMethotSchrotter
WitzHirschBu rstall 4
2 44
Press. afterPress.before
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795
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608
529
TABLES AND DIAGRAM S 1 23
TABLE LXXX— Continu ed
DIAGRAM FACTORS FOR OTTO CYCLE ENGINES
Compression. Effi ciencies, Per Cent.
Press. after A ir CardProse.before Standard .
Fou r cycle .468
. 595
6 1 2 . 318
6 1 2 . 313
6 1 2 . 646
6 12 .358
6 12 . 721
6 1 2 . 572
6 1 2 . 53
82 1 3 M eyer . 794
1 3 . 665
8‘
1 3 35 .2 . 574
Compression pressu re ratio has been calcu lated assuming an initial pressure of lbs .per squ ar e inch.
TAB LE LXXXIHEAT BALANCES OF GAS AND OIL ENGINES (PER CENT on GAs on OIL HEAT )
R adiation
Engine and A u thority. I.H .P . B .H .P . Friction . Exhau st. Jacket.333333321
for .
Beck engine, Kennedy 4 7
Griffin engine, Kennedy . 3 9
A tkinson engine, Kennedy 9 6
Otto (b'
ossley engine, Kennedy. .8 excess
Comp. R atio. R .P .M . d/a (Air - gas)187 Slaby247 Slaby187 Slaby ‘7 1 8
247 7 . 40, SlabyGeneral, MethotWestinghou se, Bibbins .
300 H .P. engine at 197H .P .,Eberly 33 . 5 1 0 0 24 1 excess
294H.P,Eberly 1 3 6
335 H.P . ,Eberly 1 0 6 . 1
6HP . engine, I.C .E 31 .8 5 27 1
24HP . engine, I.C .E 5 29 6
Deu tz 2 H.P ., Wimplinger 5 4 25 50 4 3 1
Giildner 20 H.P. Schrii t er . .
Walrath 75 H.P., Geer and Yane
300 H.P .,Goldsmith and Hart
Hornsby, R obinson 29 5
De la Vergne F . H., TowlPierce- Arrow, Chase 8
Including radiation. 1’ Inclu ding pumps. t Including ext ernal radiation.
1 24 HANDBOOK OF THERM ODYNAM ICTA BLE LXXXII
M EAN EFFECTIVE PRESSURE FACTOR S FOR OTTO CYCLE ENGINES
Eq. (933)
Pm Pa 9 Pa 9 Pa. Pa 9
Pa [1 _ (P— z ) 7] P972
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1 .0000 .000 . 21 5 0 . 4592— 1 0 - 1 0 . 394658
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. 786 091 7 495 2082 4662
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65 6 . 1 546 .895 1804 4960 2 680- 1 0 - 1 0 1 0 9 25 6 148— 1 0 - 1 0 . 428074
6 1o . 1 797 97 1 . 1 695 . 5 0891 0 10 1 0 — 1 0 - 1 0 . 4981 72
5 69 m1 . 1 60 1 . 5 195
9 75 54 12- 1 0 1 0 . 097924 9 204928- 1 0 - 1 0 .4481 70. 595 22 12 19 . 1 5 18 . 5
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985 91 7 1 . 1 1 36 . 5 8101 0 1 0 . 29984 1 9 05 5 5 5 6— 1 0 9 764 1 69- 1 0 . 496787
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TA BLE LXXXVII
THEORETICAL DR AFT PRESSUR E IN INCHES OF WATER * IN A CHIM NEY
1 00 FT . HIGH
(For other heights t he draft v aries directly as t he height)
T emperatu re of External A i r (Barometer 30 Ins.)
200°
0 . 192
The avai lable draf twill be t he tabu lar valu es less t he amou nt consumed by friction in t hestack . In stackswhose diameter is determined by Eq . 1005 t he net draftwill be 80 per centof t he tabu lar valu es. Hence t o obtain from the table t he height of stack necessary t o produ ce a net draft of say ih . , t he theoretical draftwill be X in . , which canbe obtainedwith a stack 1 00 ft . highwith flu e- gas temperatu re of 420
°F. , and air temperatu re
of 0°
F. ; or a stack 1 25 ft . high when t he air temperatu re is 60° F. and the flu e temperatu re
1 34 HANDBOOK OF THERMODYNAMICLOGAR ITHMS TO THE BA SE 1 0
These two pages giv e the common logari thms of numbers between 1 and 10, correct to four
places. M ov ing t he decimal point 1 3 places t o t he r ight (or lef t ) in t he number is equ i v alen t to
adding 13 (or — n) t o t he logari thm. Thu s, log 00 1 7453 :— 2
To f aci litate interpolation , t he tenths of t he tabu lar d i fferences are giv en at t he end of each
line, sothat the difi erences themselv es need not be considered. In u sing these aids, fi rst find t he
nearest tabu lar entry, and then add (t o mov e t o t he r igh t) or su btract (t omov e to t he lef t) , as t he
casemay requ i re.
Pages 1 32— 137 ar e repr inted by permission from Huntingtons“Fou r Place Tables.
"
Tenthsof theTabular llifferenol
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1 1 39 1 1 73 1 206 1 239 1 271 1 303 1335 1 367 1 399 1 430 1 461 TOavoidinterno
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3222 3243 3263 3284 3304 3324 3345 3365 3385 3404 3424 810
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7016
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71 85
7267
7348
7427
7505
7582
7657
7731
7803
7875
7945
801 4
8082
81 49
821 5
8280
8344
8407
8470
8531
8591
865 1
8710
8768
8825
8882
8938
8993
9047
91 01
91 54
9206
9258
9309
9360
9410
9460
9509
9557
9605
9652
9699
9745
9791
9836
98810026
4
7024
71 1 0
7193
7275
7356
7435
75 13
7589
7664
7738
7810
7882
7952
8021
8089
81 56
8222
8287
8351
8414
8476
8537
8597
8657
871 6
8774
8831
8887
8943
8998
9053
91 06
91 59
921 2
9263
931 5
9365
941 5
9465
951 3
9562
9609
9657
9703
9750
9795
9841
9886
0030
5 6
7042
71 26
72 10
7292
7372
745 1
7528
7604
7679
7752
7825
7896
7966
8035
81 02
81 69
8235
8299
8363
8426
8488
8549
8609
8669
8727
8785
8842
8899
8954
9009
9063
91 1 7
91 70
9222
9274
9325
9375
9425
9474
9523
9571
9619
9666
9713
9759
9805
9850
9894
9939
9983
'
7
7050
7135
7218
7300
7380
7459
7536
761 2
7686
7760
7832
7903
7973
8041
8109
81 76
8241
8306
8370
8432
8494
8555
861 5
8675
8733
8791
8848
8904
8960
901 5
9069
91 22
91 75
9227
9279
9330
9380
9430
9479
9528
9576
9624
9671
971 7
9763
9809
9854
9899
9943
9987
8
7059
71 43
7226
7308
7388
7466
7543
7619
7694
7767
7839
7910
7980
8048
81 16
8182
8248
831 2
8376
8439
8500
8561
8621
8681
8739
8797
8854
8910
8965
9020
9074
91 28
9180
9232
9284
9335
9385
9435
9484
9533
9581
9628
9675
9722
9768
981 4
9859
9903
9948
9991
9
7067
71 52
7235
731 6
7396
7474
755 1
7627
7701
7774
7846
791 7
7987
805 5
81 22
81 89
8254
8319
8382
8445
8506
8567
8627
8686
8745
8802
8859
891 5
8971
9025
9079
91 33
9186
9238
9289
9340
9390
9440
9489
9538
9586
9633
9680
9727
9773
9818
9863
9908
9952
9996
1 0
7076
71 60
7243
7324
7404
7482
7559
7634
7709
7782
7853
7924
7993
8062
81 29
8195
8261
8325
8388
845 1
85 1 3
8573
8633
8692
875 1
8808
8865
8921
8976
9031
9085
91 38
9191
9243
9294
9345
9395
9445
9494
9542
9590
9638
9685
9731
9777
9823
9868
991 2
9956
Tanthsof tho
1 35
TabularDifference
t-‘
P
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HHHHHH
H
H
H
D—‘HHHHHH
l-‘HHHH
HHHHH
HHHHH
H
H
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N
N
N
N
N
M
i—‘H
H
H
H
H
H
H
H
b-‘
H
H
N
N
N
N
N
N
N
N
N
N
N
N
N
N
N
N
N
N
N
N
lQ
N
N
N
N
N
N
N
N
N
N
N
N
N
N
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o
o
o
o
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H
H
H
H
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I—‘I—l
4
N
N
N
N
N
N
N
N
N
N
N
N
N
N
N
(0
10
10
10
10
(0
10
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10
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03
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1 36 HANDBOOK OF THERMODYNAMICLOGA R ITHM S TO THE
These two pages giv e t he natu ral (hyperbolic, or Napier ian) logar i thms of
numbers between 1 and 1 0, correct t o
f ou r places.
1 1 places t o t he r igh t (or lef t) in the num
ber is equ iv alen t t o adding 73 times
(or n t imes t o the logari thm.
Log,E (Base e
1 2
L3
L5
L6
L7
L8
L9
251
232
243
234
25
21 5
2 7
21 3
25 )
:3 2
343
3 5
.3 6
21 7
3 8
11 9
44 2
14 3
44 4
4544 6
44 744 841 9
0
0953
1 823
2624
3365
4055
4700
5306
5878
6419
7419
7885
8329
8755
91 63
955 5
0647
1 31 4
1 632
1939
2238
2528
2809
3083
3350
3610
L3863
41 10
435 1
4586
481 6
5041
5261
5476
5686
5892
1
01 00
1 044
1906
2700
3436
41 21
4762
5365
5933
6471
6981
7467
7930
8372
8796
9203
9594
2
0198
1 1 33
1989
2776
3507
41 87
4824
5423
5988
6523
7031
75 14
7975
841 6
8838
9243
9632
9969100060332
0682
1 019
1 346
1 663
1969
2267
2556
2837
3 1 10
3376
3635
3888
4 1 34
4375
4609
4839
5063
5282
5497
5 707
591 3
0367
071 6
1 053
1 378
1 694
2000
2296
2585
2865
3 1 37
3403
3661
391 3
41 59
4398
4633
4861
5085
5304
5 5 18
5728
5933
3
0296
1 222
2070
2852
3577
4253
4886
5481
6043
6575
7080
7561
8020
8459
8879
9282
9670
0043
0403
0750
1 086
1 410
1 725
2030
2326
261 3
2892
3 1 64
3429
3686
3938
4 183
4422
4656
4884
5 107
5326
5 539
5 748
5953
4
0392
1 3 10
2 1 5 1
2927
3646
4318
4947
5 539
6098
6627
71 29
7608
8065
8502
8920
9322
9708
0080
0438
0784
1 1 19
1 442
1 756
2060
2355
2641
2920
3191
3455
371 2
3962
4207
4446
4679
4907
5 1 29
5347
5 560
S769
5974
5
0488
1 398
2231
3001
371 6
4383
5008
5 596
61 52
6678
71 78
7655
8109
8544
8961
9361
9746
01 1 6
0473
0818
1 1 5 1
1 474
1 787
2090
2384
2669
2947
3218
3481
3737
3987
4231
4469
4702
4929
5 1 5 1
5369
5 581
S790
5994
1
2
3
4
M ov ing t he decimal point 27
8
9
6
0583
1 484
23 1 1
3075
3784
4447
5068
5653
6206
6729
7227
7701
81 54
8587
9002
9400
9783
01 52
0508
0852
1 184
1 506
181 7
21 19
241 3
2698
2975
3244
3507
3762
4012
4255
4493
4725
495 1
5 1 73
5390
5602
581 0
601 4
BA SE e
7
0677
1 5 70
2390
3 1 48
3853
45 1 1
5 1 28
5 71 0
6259
6780
7275
7747
8198
8629
9042
9439
9821
0188
0543
0886
1 21 7
1 5 37
1 848
2 1 49
2442
2726
3002
3271
3533
3788
4036
4279
45 1 6
4748
4974
5 195
541 2
5623
5831
6034
8
0770
1 65 5
2469
3221
3920
4574
5 1 88
5 766
631 3
6831
7324
7793
8242
8671
9083
9478
9858
0225
0578
0919
1 249
1 5 69
1 878
2 1 79
2470
2754
3029
3297
3558
381 3
4061
4303
4540
4770
4996
521 7
5433
5644
585 1
6054
1 - 32 - 5
3 - 7
4 0 7897 - 1 0
5 0 4871 - 1 2
6 - 1 4
7 - 1 7
8 - 19
9 (LZ 767 - 21
9 1 0
0862
1 740 1 823
2546 2624
3293 3365
3988 4055
4637 4700
5 247 5306
5822 5878
6366 6419
6881
7372 7419
7839 7885
8286 8329
871 3 875 5
91 23 91 63
95 1 7 955 5
9895
0260
061 3 0647
0953
1 282 1 31 4
1 600 1 632
1909 1939
2208 2238
2499 2528
2782 2809
3056 3083
3324 3350
3584 361 0
3838
4085 41 1 0
4327 435 1
4563 4586
4793 481 6
5019 5041
5239 5 261
5454 5476
5665 5686
5872 5892
6074
Tenths of theTabularDifference‘1 2 £3 44 5
10 1929 38 48
9 17 26 35 44
8 16 24 32 40
7 15 22 30 37
7 14 21 28 34
6 1 3 1926 32
6 1 2 1824 30
6 1 1 1 7 23 29
5 1 1 1 6 22 27
5 1 0 1 5 21 26
5 1 0 1 5 20 24
91 4 1923
91 3 1 822
91 3 1 7 21
83U3 1 6 20
8 1 2 1 6 20
81 1 1 5 19
7 1 1 1 5 18
7 1 1 1 4 18
7 1 0 1 4 17
7 1 0 1 3 16
6 1 0 1 3 1 6
91 2 1 5
91 2 1 5
91 2 14
81 1 1 4
81 1 1 4
81 1 1 3
8 10 1 3
8 10 1 3
7 1 0 1 2
7 1 0 1 2
91 2
91 1
91 1
91 1
91 1
81 1
810
81 0N
N
N
N
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PART II
CHARTSCONSTRUCTION AND USE OF DIAGRAM S
Chart 1 . This chart gives t he work requ ired to compress and delivera cub ic foot of (sup.pr . air
,or t he horse-
power to compress anddeliver 1 000 cu .
f t . of (su p.pr . ) air per minu te, if t he ratio of pressu re (del.pr . (sup.pr . t hevalu e of 8 and t he (su p.pr . ) are known ,and compression occu rs in one stage.
Thework or H.P . for any number of cu b ic feet IS directly proportional to number of feet. The cu rves are dependent u pon t he formu las, Eq . for t he casewhen and Eq . (49) for t he case when 8 is not equ a l to 1 . They weredrawn as follows
On a horizontal base variou s valu es of R P are laid off , startingwith'
t he valu e2 at t he origin . The valu es for work were then fou nd for a number of va lu esof R Pwith a constant valu e of and 8. A verticalwork scalewas thenlaid off from origin of R I, and a cu rve drawn throu gh t he points fou nd bythe intersection of horizontal lines throu gh valu es of work, with verticallines throu gh corresponding valu es of R P
. The processwas then repeated forother valu es of s and cu rves similar to t he first
, drawn for t he other valu es of 8.
From t he constru ction so far completed it is possib le to find t hework per cu b icfoot for any pressu re ratio and any valu e of 8 for one by projectingup from t he proper valu e of R P to t he cu rve of valu e of 8 and then horizontallyto t he sca le of work . It will be noted from these formu las, however, thatt he work may be laid ofi on t he horizontal base and a grou p of lines drawn so
that t he slope of t he line equ als ratio of work for any supply pressu re to thatfor the originally u sed. For convenience, in order that t he grou p of
8 cu rves and t he latter grou p may be as distinct as possib le, t he origin of t he
latter grou p is taken at t he opposite end of t he base line . If from t he point for
work originally fou nd, a projection ismade horizontally to t he propercu rve
,t he valu e for work with this will be fou nd directly below.
It will be noted that from point of intersection of t he vertica l from t he R 1,valu ewith t he 8 cu rve, it is on ly necessary to project horizontally far enou gh tointersect t he desired cu rve
,and since no information of valu e will
be fou ndby continu ing to t hework scale for t he original this is omitted
from t he diagram.
In brief , then , the u se of this chart consists in projecting upward from t he
proper valu e of 1?p to t he proper 8 cu rve, then passing horizontally to t he valu eof and finally downward to t hework scale. A s an example of the u se
of t he cu rve : Find the work to compress 1 000 cu . ft . of free air from 1 to 87}1 39
140 HANDBOOK OF THERMODYNAMICatmospheres adiabatically . On t he cu rve project u pward from R p
= 8.5 to
cu rve of then over to cu rve and down to read workChart 2. This gives t he work requ ired to compress and deliver a cu bic
foot of air or t he horse-
power to compress and deliver 1 000 cu . f t . of
air per minu te if t he ratio of pressu res, t he va lu e of 8 and areknown and if compression occu rs in two stageswith best- receiver pressu re and
perfect intercooling . The work or HP . for any other number of cu bic feetmay be fou nd by mu ltiplying work per foot by t he number of feet . The
method of arriving at this chartwas exactly t he same as that for one stage .
A s an example of t he u se of t he chart , find t hework to compress 5 cu . ft . of
free air from 1 to 8%atmospheres adiabatically in two stages. Project upwardfrom R p
= 8.5 to cu rve then over to cu rve and down to read5 320 ft .
- lbs. per cu bic foot .
Chart 3 . This chart gives t he work necessary to compress and deliver acu bic foot of air
, or horse—
power to compress and deliver 1 000 cu . f t . of
(sup. pr . ) air per minu te, if t he ratio of pressu res, t he valu e of 8, and t he (sup.
pr . ) are known and if t he compression occu rs in three stageswith best- receiverpressu res and perfect intercooling . The work or horse—
power for any othernumber of cu bic feet may be fou nd by mu ltiplying t he work for one foot byt he number of feet .
As an example of u se of this chart, determine t he horse-
power to compress100 cu . ft . free air per minu te adiabatically in three stages from 1 5 lbs. per squ areinch abs. to 90 lbs. per squ are inch gage . From R p
= 7, project to cu rve of
then over to 1 5 and down , and t he horse-
power will befou nd to be
Chart 4 . This chart is for finding t he of compressors. In t he
case of mu lti- stage compressorswith best- receiver pressu re and perfect intercooling, t he of each cylindermay be fou nd by considering each cylinderas a single- stage compressor ; or t he of t he compressor referred to theL P . cylinder may be found.
The chart depends on t he fact that t he work per cu bi c foot of gas
is equ al to t he for t he no- clearance case and that t hewith clearance isequ al to t he for no clearance, times t he volumetric efficiency . Diagrams 1 , 2 and 4 are reprodu ctions of Charts 2 , 3 and 4 to a smaller
scale and hence need no explanation as to derivation . Their u semay be brieflyshown . From t he given ratio of pressu res project u pward to t he proper cu rve,then horizontally to t he and downward to readwork per cu bic feet of
gas.
The volumetric effi ciency diagram was drawn in t he following manner :From Eq . (59) vol . eff .
= (l+o showing that it depends u pon threevariab les, R P , c and s. A horizontal scale of valu es of R I) was laid off . Valu es
of R pa
lwere fou nd and a vertical scale of this qu antity laid off from t he same
origin as t he R p valu es. Throu gh t he intersection of t he verticals from variou s
142 HANDBOOK OF THER M ODYNA M ICgives a graphical means of finding this valu e of when t he
clearance and valu e of 8 are known . It also gives on the right- hand of t he charta means for finding t he for this condition . The figu rewas drawn bymeans of Eqs. (1 39) and
To find t he to give maximum work for any it is on lynecessary to project from t he proper valu e of 8 to t he given clearance cu rve,and then horizontally to read t he valu e of R P
. The divided by thisgives t he desired. To obtain t he project upward from t he
valu e of 8 to t he clearance cu rve, then horizontally to read t he ratioThe mu ltiplied by this qu anti ty gi ves the m .e.p.
A s an example of t he u se of this chart let it be requ ired to find t hefor t he case of maximumwork for 9X 1 2 in . dou b le- acting compressor runn ing200 having 5 per cent clearance and delivering against 45 lbs. per squ areinch gage ; also t he horse -
power . Compression su ch that 8
Projecting from t he valu e for 8 on t he left- hand diagram to t he line of
5 per cent clearance find R Pto be hence lbs. per
squ are inch absolu te = 6 .4 lbs. per squ are inch gage. A gain, proj ecting fromvalu e for 8 on right- hand diagram to line of 5 per cent c learance find
Chart 6 . This chart is designed to showt he saving in work done in com
pressing and delivering gases by two- stage or three- stage compression withbest - receiver pressu re and perfect intercooling over that requ ired for compressing and delivering t he same gas between t he same pressu res in one stage. The
chart was made by lay ing off on a horizontal base a scale of pressu re ratios.
From t he same origin a scale of work for two or three stage divided by t hework of one stage was drawn vertically . For a number of valu es of R I, t he
work to compress a cu bic foot of gaswas fou nd for one,two and three stage
for each valu e of 8. The valu es fou nd by dividing t he work of two or threestage by t hework of single stagewere plotted above t he proper R P valu es, andopposite t he proper ratio , valu es and cu rves drawn throu gh all points for onevalu e of 8. To find t he saving by compressing in two or three stages projectfrom t he proper R P valu e to t he chosen 8 cu rve for t he desired number ofstages, then horizontally to read t he ratio of mu lti - stage to one- stage work .
This valu e gives per cent power needed for one stage that will be requ ired tocompress t he same gas mu lti - stage . Saving by mu lti - stage as a percentageof single stage is oneminu s t he valu e read.
To illu strate t he u se of this chart , find t he per cent of work needed to compress a cu b i c foot of air adiabatically from 1 to 8%atmospheres in two stagescompared to doing it in one stage . From examples u nder charts Nos. 1 and
2 itwas fou nd thatwork per cub ic footwas 6300 ft .- lbs. and5 320 f t .
- lbs. respec
t iv ely ,for one and two- stage compression, or that two stagewas per cent
TABLES AND DIAGR AM S 1 43
of onest age. From 8%project upon Chart 6 to 8 for two stage,and
over to read per cent ,which is nearly the same.
Chart 7. This chart, designed by M r . T . M . Gu nn , shows t he economycompared to isotherma l compression .
The chart was drawn on t he basis of t he following equ ationarance)
m .e .p. actu al —z- E , actu a lValu esof this expressionwereworked ou t for each exponent, for assumed valu esof R P . A scale of valu es of R 1, was laid off horizontally and from t he same
origin a vertical scale of valu es of t he ratio of isothermal to adiabatic . Theresu lts foundwere then plotted, each point above it s proper R p and oppositei t s ratio valu e. Cu rveswere then drawn throu gh all t he points fou nd for t he
same valu e of 8. In a similar way a set of cu rves for two- stage and a set for
three- stage compression were drawn .
This chart is also u sefu l in obtaining t he of the cycle if t heand t he volumetric efficiency of t he cylinder be known . A second horizontalscale laid off above the R P scale shows t he per pou nd of (sup.pr . for)t he isothermal no—clearance cycle . This is fou nd to be equ al to log , R P , since
t he for no clearance is equ al to thework per cu bic foot of gas,
which, in tu rn ,for t he isothermal case is loge R P or log. R p when
1 .
Knowing t he ratio of pressu res, economy compared to isothermal can befound as explained above . A lso knowing R p t he per pou nd ini t ial is
found from t he u pper scale .
Sin ce t he latter qu antity is assumed to be known, by mu ltiplying it byfactor j u st fou nd there is obtained isotherma l . Since volumetriceffi ciency is assumed known , all t he factors are known for t he first equ ationgiven above which, rearranged, reads
nce)actu a
hermal) + E v
Chart 8. This chart is drawn to give t he cylinder displacement for a
desired capacity,with variou s valu es of R p , 8 and clearance. From t he formu la
Eq . (L .P .
The right - hand portion of t he diagram is for t he pu rpose of finding valu esof (RM l
lfor variou s valu esof R I, and 8, and is constru cted as in Chart 2 . Thevalu es of t he lower sca le on the left - hand diagram give valu es of D (L . P .Cap. )
(l +o— cR pi ) , where capacity is taken at 100 cu .ft ., this scale was laid
ou t and t he c learance cu rves points fou nd by solving t he above equ ation forvariou s valu es of for each valu e of c. To obtain t he displacement meces
sary for a certain capacity with a given valu e of R p , c and 8, project upwardfrom R ,,
to t he proper 8 cu rve across to t he a cu rve and down to read displacement perh u ndred cu b ic feet . A lso on t he left- hand diagram are drawn lines ofpiston speed, and on left- hand edge a scale of cylinder areas and diameters togive displacements fou nd on horizontal scale. To obtain cylinder areas orapproximate diameters in inches project from displacement to piston speed line
144 HANDBOOK OF THER M ODYNA M ICand across to read cylinder area or diameter . Figu res given are for 1 00 cu .f t .
per minu te. For any other volume t he displacement and area of cylinder willA s an example of t he u se of Chart 8, let it be requ ired to find t he low-
pressu re cylinder size for a compressor to handle 1 5 00 cu . ft . of free air per minu te.
R eceiver pressu re to be 45 lbs. per squ are inch gage and to be atmos
phere . Piston speed limited to 5 00 f t . per minu te . Compression to be so that8 and clearance = 4 per cent . Proj ecting u pward from R p
= 4 to 8
across to c= 4% ,and down to piston speed = 500, find t he diameter of
a cylinder for 1 00 cu . ft . per minu te is For 1 5 00 cu . f t . t he diameterwillbe as«E xes ins.
Chart 9. This diagram for mean effective pressu re in terms of initial and
back pressu re, clearance, compression and cu t - off , facilitates t he solu tion of Eq .
Themean effective pressu re is t he difference between mean forward and
mean back pressu re. The former isdependent u pon clearance, cu t - off and initia l
pressu re . In t he example shown on t he figu re by letters and dotted lines,clearance is assumed 5 per cent , shown at A . Project horizontally to t he pointF,
on t he contou r line for t he assumed cu t - off , 1 2 per cent . Project downwardto t he logarithmi c scale for “mean forward pressu re in terms of initial pressu reto t he point G. On t he scale for “initial pressu re ”
find t he point H,represent
ing t he assumed initial pressu re, 1 1 5 lbs. absolu te. Throu ghG andH a straightline is passed to t he point K on t he scale for “mean forward pressu re,” wheret he valu e is read, m.f .p. lbs. absolu te.
M ean back pressu re is similarly dependent u pon clearance, compressionand back pressu re , and t he same process is followed ou t by t he points, A ,
B, C,
D
and E ,reading t hemean back pressu re, lbs. absolu te at t he point E . Then
by su btraction lbs.
Chart 1 0 is arranged to showwhat conditionsmu st be fu lfilled in order toobtain equ al work with complete expam i on in both cylindem in a compou nd
engine, fini te receiver , logarithmic law,no clearance, when low-
pressu re ad
mission and high-
pressu re exhau st are not simu ltaneou s. The diagram repre
sents graphi cally t he conditions expressed in Eqs. (283) to
To illu strate i t s u se assume that in an engine operating on su ch a cycle,t he volume of receiver is times t he high-
pressu re displacement , 1 .5 = y,1
then5
:.667 . Locate t he pom t A on t he scale at bottom of diagram ,
corresponding to this valu e . Project u pward to t he cu rvemarked ratio of cu t — offs”and at t he side , C, read ratio of cu t - offs Z H/Z L :
.5 72 . Next extending t he
line A B to it s intersection D ,with t he cu rveGH, t he point D is fou nd. From Dproject horizontally to t he contou r line representing t he given ratio of initialto back pressu re . In this case , initial pressu re is assumed t en times back pressu re . Thu s t he point E is located. D irectly above E at t he t op of t he sheet isread t he cylinder ratio
,at F .
If cylinder ratio and initial and final pressu res are t he fu ndamental data of
the problem ,t he ratio of cu t - offs and ratio of high-
pressu re displacements to
receiver volumemay be fou nd by reversing the order .
146 HANDBOOK OF THER M ODYNA M ICto t he right to“ the intersection , where t he dewpoint is read by interpolationbetween t he contou r cu rves at (C) to be 595 ° F . These cu rves are drawn for abarometric pressu re of ins. (standard) andwill not apply correctly, whent he barometer is not equ al to this, thou gh with fair approximation , so long as
t he difference in barometer is not great . Where there is mu ch departu re t heformu la mu st be u sed. Chart 26 givesweight of aqu eou s vapor per cu bic footofmixtu re, in grains ( 77 1
07 lb .) and also t he degree of humidity . The temperatu re of t he dewpoint 596
° F is located at (C’
) on t he right- hand side . Interpolat ion between t he ends of t he contou rs for weight , gives grains percu bic foot . On t he same scale t he temperatu re of t he air , F is represented at
point (A ) projecting to t he intersecting point D and down to t he bottom of
t he diagram gives on t he scale for degree of hum idity , 60 per cent .
Charts 27 , 28 and 29. These diagrams have been plotted chiefly from ex
periment al data : t he lower valu es are new, bu t t he u pper are those given by
Starr several years ago and generally accepted by refrigeration engineers, - as
standard.
These data refer to t he equ ilibrium conditions of t he solu tion , and in
u sing them for practical prob lems care mu st be taken to avoid applying themto other conditions, for example to solu tions that are not homogeneou s, or inwhich there has not been su fficient time for t he establishment of equ ilibrium.
Charts 30 and 31 . These represent variou s fractionation tests plotted incu rve form , on which are indicated t he boiling-
points of known hydrocarbons,and bands are added for t he class of distillate in accordancewith t he R ob insonclassification . Horizontal distances represent fractions distilled, a fractionbeing t he per cent by volume that has been discharged between two given t emperat u res in a boiling mass, t he temperatu re continu ally rising . Incidentallyit may be noted that t he temperatu re is different in t he vapor than in t he boiling liqu id, thou gh that of t he liqu id is u su allv taken . The rate of boiling orapplication of heat very seriou sly affects these cu rves
,any one of which might
easily be changed thereby .
Chart 33 . This diagram gives t he heats of reaction plotted as a fu nction of
S alone, laid off horizontally, and a separate cu rve drawn for each valu e of t heg—gz ratio, 2, 6 , 1 5 and infinity. The vertical distances are heats of reaction ,first , per pound of gases produ ced and second, per pou nd of carbon, t he formerbeing a measu re of temperatu re rise, and t he latter of efficiency of reaction .
These two heats are derived from Eq . (658) in t he two Eqs. (661 ) andS is t heweight of steam per pou nd of air reacting .
Chart 34 . Here one set of t he M allard andLe Chatelier valu es for t hemean
specific heat of variou s gases given in Eq . (674) has been u sed to calcu late t he
t emperatu re rise above 32° for variou s qu antities of heat . For any heat increment per pou nd of gases there is a corresponding temperatu re increment that
can be read off directly . Thu s, for C0 2 , consider 1 lb . to receive 1 000starting at 32
°F. , t he temperatu re rise wou ld be 3290° F.
— 32°
1’
TABLES AND DIAGR AM S 1 47
whereas from 1000° F . as a starting point this same 1 000 B .T .U. wou ld yield a
temperatu re of 3690° F . or a rise of
Chart 36 . The valu es of t he factor of evaporation and equ ivalent pou nds ofwater per hou r per boiler horse-
power may be fou nd directly from the cu rves,
which also give t he heat per pou nd for dry satu rated, wet or superheated steamabove any feed-water temperatu re . The constru ction of this chart is given on
t he diagram.
Charts 38and 39. These represent a number of boiler testswith some one
item of importance, selected to showt he effect of variou s conditions of serviceand fu els in t he same and different boilers, all ofwhich are self explanatory .
Chart 40. Calcu lation and u se of diagram ,giving constant volume lines for
steam . To illu strate t he method, t he location of t he line of constant volume of2 cu . ft . will be traced. Let t he first temperatu re be taken at 800
° F . absolu te
for t he first point A , corresponding to 340° F . From t he steam tab les dry saturated steam at 340° F . has a specific volume of cu . ft . , sothat t he qu ality
when t he volume is 2 cu . ft . is 3 7
2
per cent . The entropy of t he
water at 340° F. ,from t he steam tab les, is therefore t he entropy in
crease inmaking this steam from 32° F . and at 340
° F .= entropy of t he steam
+entropy of water content — entropy at 32°
d) , ¢32 X— 0 Another point B is located by assuming a temperatu reth= 44o
°
F. or Tb = 900, for which ¢b by t he same method.
To illu strate t he use of t he diagram in solving prob lems,suppose 1 lb . ofwet
atmospheric pressu re steam ,occupying 1 0 cu . ft . be enclosed in tank and heated
t o raise t he pressu re to 30 lbs. per squ are inch absolu te, find t he final t emperat u re, entropy and dryness. From lbs. per squ are inch on t he pressu rescale project to point P on t he constant volume line of 10 cu . ft . and followthisline to t he point C for 30 lbs. per squ are inch absolu te pressu re. Proj ectingfrom C to D t he absolu te temperatu re is fou nd to be 7 10° or t = 25o° F.
, and
projecting from C to E t he entropy ¢c The final qu alityCM
OHper cent .
A gain, if heat be added to raise the temperatu re to 842° absolu te t he entropyis fou nd by following t he 1 0 cu . ft . line to t he point K opposite the temperatu re,and projecting down from K to Q t he entropy is fou nd «pk —
qt ”
The qu ality may be read ofi directly from Chart 44 which carries linesof constant qu ality that might be superimposed on this constant - volumechart .
Charts 41 , 42 and 43 . These have been drawn to facilitate calcu lations ofP, V,
T relations for expansions and compression having variou s valu es of 8;Charts 41 and 42 have been plotted to a vertical scale of with a dou ble
horizontal scale for t he corresponding and Each cu rve is for a
different valu e of 8, as marked on it . These are also given on logarithmi c
1 48 HANDBOOK OF THERM ODYNA M ‘
IC
cross- section paper in Chart 43 as arranged by Gu nn , where all lines become
straight , to which an entropy scale is added.
Chart 44 . Calcu lation and u se of temperatu re entropy diagram, lines of
constant pressu re and qu ality. Let it be assumed that t he line of qu ality80percent is to be located, starting with t he pressu re of 200 lbs. per squ are inch ab
solu te, point A . From t he steam tables t F . or Ta t he en
tropy of t he liqu id is .5 437 , of evaporation complete, so that ¢aTo locate a point B in t he su perheat region
at t he same pressu re and for 1 00°
of su perheat , t he steam tab les are fou nd
to give directly ¢bThe following problem will serve as an example of t he u se of t he diagram.
Steam at a pressu re of 1 60 lbs. per squ are inch absolu te, dry and satu rated ex
pands adiabatically to atmospheric pressu re and to some u nknown qu ality tobe fou nd. From t he point C representing t he ini tial condition project vertically down to t he pressu re line at point D . By interpolation t he qu alityis fou nd to be per cent , as point D lies between t he two lines of 80 per centand 90 per cent qu ality .
A nother examplewill illu strate t he passage into t he su perheat region . A t
mospheric exhau st steam at 20 lbs. per squ are inch absolu te , is superheated 1 20°by a reheater and then expands adiabatically in an exhau st steam tu rbine to anabsolu te pressu re of half a pou nd per squ are inch absolu te, to find t he finalqu ality . The initial condition is represented by point E ,
from which projecting downward to t he low-
pressu re line at H,lying between 80 per cent and 90
per cent , t he qu ality is found by interpolation to be per cent and t he t em
perat u re by projecting to K,is T The corresponding volumesmay beread off from C hart 40.
Chart 45 . The M ollier D iagram . On this diagram t he total heats above32
°are ordinates, and entropy from 32° are abscissa , plotted in a series of cu rves.
On this chart t he vertical distance from any pressu re, temperatu re or qu ality,to any other , is t he work done in heat u nits, by t he whole cycle inc lu ding anadiabatic expansion ; this can be marked off on a strip of paper and referred tot he scale of heat to permit t he work to be read directly , or t he ordinate of t he
lowcan be su btracted from that of t he high point . A s this is so convenient fortu rbine work a scale of corresponding steam jet velocities has been plotted
beside that for total heats. A large scale chart of this sort is very necessarywhen many calcu lations of this natu re are to be made and su ch may be plotted
from t he steam tables.
Chart 46 . To illu strate t he u se of t he diagram,t he following prob lemwill be
graphically solved. Find t he R ankine cycle effi ciency,heat and steam con
sumption for an initial pressu re of 1 50 lbs. per squ are inch gage and dry saturated steamwith a back pressu re of 1 0 lbs. per squ are inch absolu te. Startingat t he initial pressu re point B , project up to t he 10- lb . back pressu re cu rve pointC,
and then across to t he efficiency scale point D,reading there a thermal
efficiency of per cent and a heat consumption of B .T .U. per hou rper I.H.P. Continu ing across horizontally to t he back pressu re cu rve of 1 0
1 50 HANDBOOK OF THER M ODYNAM IC500 B .T .U. per pound of gases. Starting at t he 500 B .T .U. pointG, pass up to
t he cycle cu rve at H and then across to t he point K on t hework scale, readingft .
- lbs. Passing horizontally across to t he point L and thence downward to point M t he mean effective pressu re is found to be lbs. per
squ are inch.
Chart 56 . Stirling gas cycle. To illu strate t he u se of this chart , find t heeffi ciency, cyc li c and fu el heat consumption for a Stirling cycle, for 300 B .T .U.
supplied from fire per pound of working gases, 30 atm . compression ,and a fu r
nace effi ciency of 40per cent . Starting at poin t E at t he valu e 300 on t he u pperscale, pass vertically up to point F on t he efficiency cu rve referred to fire heat
,
and horizontally to G,reading thermal effi ciency of per cent , and cyclic
heat supplied 4050 B .T .U. per hou r per I.H.P . Continu ing across to point Hon t he 40 per cent fu rnace effi ciency cu rve and down to fire heat scale at K
,
t hefire heat supplied is fou nd to be B .T .U. per hou r per I.H .P .
Charts 57 and 59. A similar procedu re applies to t he cu rves for t he
Ericsson cycle,which needno detailed explanation .
Chart s 60 and 61 . A diabatic compression cycles. Illu strating t he u se
of t he cu rves t he solu tion of t he following problem is traced graphi cally on
Chart 60. R equ ired t he thermal efficiency, cyclic heat , and fu el consumption fort he D iesel cycle, su ppliedwith an oil yielding 1 500 B .T .U. per cu bic foot in itsvapor, t he cycle receiv ing 600 B .T .U. per pou nd of working gases after 1 0 atm.
compression . From t he 600 point E on t he heat- supplied scale pass u p to t he1 0 atm . compression Diesel cu rve F, and horizontally across to t he efficiencyscale G reading per cent and 8900 B .T .U. per hou r per I .H.P . Continu ing
across to t he fu el calorific power cu rve of 1 500 B .T .U. per cu bic foot H ,and
thence down to K ,t he fu el consumption is fou nd to be 6 cu .ft .
The second set of efficiency cu rves, Chart 6 1 , is u sed in exactly t he samewayasChart 60, t he only difference between t he two being t he scales.
Charts 66 and 67 . Comparison of rational and emperio formu las for air andsteam flow. These have been calcu lated for air from Eq . (25 ) u sing 7and by t he M ollier diagram for steam . To this diagram are added some cu rvesof experimental flowlaws stated in Eqs. (952) and
Chart 69. Velocity of air pipes. This diagram was calcu lated from Eq
(968) and also by t he simple equ ation in which density changes are neglected.
These give comparative resu lts as indicated in t he chart,reprodu ced from
Kneeland.
Chart 71 . Chimney diameter . This diagram corresponds to Eq . (1 005 )which assumes that t he minimum - cost steel stack has a diameter dependingsolely upon t he horse-
power of t he boilers it serves, and a height proportionalto t he net draft requ ired.
Charts 72 and 73 . R efrigerating effect,ammonia and carbon- dioxide.
See t he diagrams for constru ction and u se.
1 5 1TABLES AND DIAGRAM S
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Work per Cu . Ft . of (Su p. Pr .) Gas -24 44
CHA R T 4.— M ean Eff ective Pressu re of Compressors, One Two and Three- stages.
TABLES AND DIAGRAM S 1 5 5
Init ial Pressu re Lbs. per Sq. In. A bs.
E fl fi z a a w h o m w m a fi m
R at io of Pressu res
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Work per Cu . Ft . of . (Su p. Pr . ) Gas+ l44m
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CHA RT 4.— M ean Effective Pressu re of Compressors, One Two and Three- stages.
1 5 6 HANDBOOK OF THER M ODYNAM IC
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1 58 HANDBOOK OF THERM ODYNAM IC
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TABLES AND DIAGRAM S 1 59
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1 62 HANDBOOK OF THER M ODYNAM IC
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and
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CHART
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TABLES AND DIAGRAM S 1 63
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1 64 HANDBOOK OF THER M ODYNAM ICPressur e inP ou ndsPer Sq . In. A bs..
17 16 14 13 12
30 1 1 ]I
l .9
Density at Volume atUpper Scale — R atioDensity at any T&P
Lower Scale R ati o Volume at any T&P
Density at 32° F.
Inner Scale R ati oDensity at any T
CHA RT 1 3 .
— Equ ivalent Gas Densities A t Diff erent Pressu res and Temperatu res.
Ou ter Scale=
1 66 HANDBOOK OF THERM ODYNAM IC
(Critical Temperatu reDiv ided by any oth er Temperatu re)
Temperat u res in DegreesFahr .
CHART 1 5 .
— Carbon Dioxide Pressure~ temperat ure R elations for Saturated Vapor.
«3
ures
L
per
Sq.
In.
TABLES AND DIAGR AM S
380
360
810
59
57
Temperat u re inDegreesFahr .
CHA RT 1 6.— Steam,
Pressu re- temperatu re (Table XL) .
1 67
1 68 HANDBOOK OF THERM ODYNAM IC
Upper Hor izont al Scale=Pressu ree in Ls ’er Sq . In. A bs.
Lower u Temperatu re in DegreesF.
Ver tical Scale=Heat Per Pou nd in B .T .UsA bov e 82
CHA RT l7.
— Steam , Heat of the Liqu id (Table XL) .
1 70
tal
Heat
,
B.T.Us
H
HANDBOOK OF THER M ODYNA M IC
Lower Sdalé Temperat u reDegreesFahrenhei t
Upper Scale= Pressu re Lbs. Per Squ are Inch A bsolu te
8 1 000 1 152
Temperatu re, Fah renh ei t;
50
25
1 00 1 10
Temperatu re. Fahrenhelo
15“
270 290
40 50 210 220 500 670 580
CHA RT 19.— Steam ,
Total Heat (Table XL) .
00.7
00.8
57. 1
58
58.
.TABLES AND DIAGR AM S
47
0 1 80 490
160 470
1 71
Density
m9o
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500
480
"
Vert icalfi cale=Densi ty.Pou ndsper Cu .Ft .
Horizont al.Scale=Temperatu reFahrenhei t
CHA RT 20.
— Steam , Specific Volume and Density of t he Liqu id (Table XL) .
1 72
Left
Hand
Scale
Cubic
Feet
per
Pound
,
Right
Hand
Scale
Poundsper
Cubic
Foot
.
, 105
1 200
1 450
5 0
1 800
HANDBOOK OF THER M ODYNAM IC
93
230
,
130430
23°
30
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330
155 180 305
20
1 55 200 245 290
bl
W ) 2400
30 80 130
F,605
1 05 5 55
380 530 555
355 505
.8
330 480 505
Lower scale=Temp.in DegreesFahn .
'
Upper Scale Lbs.pcr Sq .In .Abs.
CHA RT 2 1 .
— S team,Specific Volume and Density of t he Vapor (Table XL ) .
1 74 HANDBOOK OF THER M ODYNAM IC
Temperatu re Deg . Cent igrade
.50 60 70 100
Pressure
Inches
of
Mercury
N!b
Temperat ure Degx Fahrenheit
CHA RT 23.— Vapor Pressu re of Heairy Petroleum Distillates of the Kerosene Class.
8
29
Pressure
M.M
'u
0
Merc
Mercury
Pressure,
TABLES AND DIAGR AM S
Temperat u re. Deg. Cent igrade
Temperat u re Degrees.Fahrenheit
CHART 24.— Vapor Pressure of the Alcohols.
1 75
Pressure,
MM
.
0
M
1 76 HANDBOOK OF THERM ODYNAM ICDifference in Temperatu re:Wet and Dry Bu lbs:Degrees Fahrenheit
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Difference in Temperatu re:Wet and Dry Bu lbs: DegreesCentigrade
CHA RT 25 .
— R elation between Wet and Dry Bu lb Psychrometer R eadings and DewPoint forAir andWater Vapor .
178 HANDBOOK OF THERM ODYNAM IC
CHA RT 27.
— Ammonia -water Solu tions, Relation betweenTotal Pressu re and Temperatu re
(Dotted Lines M ollier Data) .
TABLES AND DIAGR AM S 1 79
CHA RT 28.
— Ammonia-water Solu tions , R elation between Total Pressu re andPer Cent NHa in Solu tion .
180 HANDBOOK OF THER M ODYNAM IC
0 5 10 1 1 -8 1 5 20 30 333335 45 50
PercentbyWeight of Ammonia in Solu t ion
CHA RT 29.— Ammonia-wat er Solu tions
, R elation between Temperatu re and
Per Cent NHa in Solu tion .
182 HANDBOOK OF THERM ODYNAM IC
Per Cent by Volume Di st illed
CHA RT 31 .— Fractional Disti llation of Gasolenee.
ume
olum
TABLES AND DIAGR AM S
.zxpu s,
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fromFixed
Carbon.
183
184 HANDBOOK OF THER M ODYNA M IC
CHA RT 33.— Heats of R eaction for Hypothetical Produ cer Gas from Fixed Carbon,B . T . U.
TABLES AND DIAGRAM S 87
2790 1300
2790 1200
2790 1 100
Upper Line=Temperat u re for Satur at ion
Lower Line=A hsolu t e Pressu res
CHA RT 36.
— Heat per Pou nd of Steam above Feed Temperatu re. Ev aporation per Hou rD
per Boiler Horse-
power . Factor of Evaporation.
Each of the u pper cu rves gives directly the total heat per pound of steam above 32°and the distance between them and the lower cu rv e intercept, that for any feed-water t em
perat u re, by a vertical distance. If , therefore, A B be the total heat for t he steam above32
°at 1 00 lbs. per sq . in . absolu te and 20
°
superheat and DE the heat of li qu id at 200° F .
feed temperatu re above then A C, t he v erticaldistancebetween these two points, is theheat per pou nd of steam above the feed temperatu re 200° F . for 100 lbs. steam with 20°
superheat. This can be marked on a slip of paper and read OH on the extra scale t o the
right in terms of,heat in or factor of evaporation, or actu al weight of water that
must be evaporated per hou r t o give a boiler horse-
power.
188 HANDBOOK OF THERM ODYNA M IC
4 5 (i 7 8 9 10 1 1 12 13 14 1 5 16Ev aporat ion From at 212
°
F.per Squ are Foot of Heat ing Su rfaceper Hour .
CHA RT 37.— Heat Balance for LocomotiveBoilerWorking Under Various R ates of Evaporation.
190 HANDBOOK OF THERM ODYNAM IC
Draft ov er Fire in inchesof Wat er
Thickness of Firehu nches Pou ndsof Dry Coal Fired tper Hr . per
Sq . Ft . of Grate Su r face
1 2 8 4 5 6 7
Evaporat ionPer Sq. Ft . 0:Heating Evaporat ion per sq. Ft . of Heat ingSurfaceperHp. Su rfaceper Hr.
CHA RT 39.
— Influence of Various Factors on Boiler Efficiency.
TABLES AND DIAGRAM S . 191
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Ve‘
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’penSecond
CHA R T 70.
— Coefficient s of Friction g' for A ir in Du cts.
These valu es of the coefficient of friction are given by R iet schel for straight du cts of
brick and iron for v elocities u p t o 50 f t . per second ; for iron du cts different v alu es are giv enfor perimeters or circumferences from 8 t o 1 00 in . They are intended especially for air
du cts with t he u su al velocities of air,6 t o 24 f t . per secondwhen served by fans, and 3 t o
8 f t . per secondwhen the flowis du e t o natu ral draft.
222 HANDBOOK OF THER M ODYNA M IC
O:
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CHA R T 72 .
- Chart t o Determine Available R efrigerating Effect per Pou nd of Ammoni a
for Any R efrigerator Pressu re and A ny R efrigerat or or Liqu id Temperatu re .
Constru ction and u se of Diagrams, Charts 72 and 73 . These diagrams are for t he pu r
pose of finding the refrigerating eff ect per pou nd of flu id, which is made u p of t he latentheat, or asm u ch of it as is av ailable, less t he heat necessary t o cool t he liqu id from i t s originaltemperatu re t o that du e t o the pressu re in t he coils, plu s the heat absorbed in su perheatingt he v apor .
A hor izontal scale of pressu res is laid off in both directions for a vertical ax is carry inga B .T .U. scale. In t he section t o t he right of t he center axis cu rves are drawn representingvariou s temperatu res of t he liqu id before entering the refr igerator coils. These are so
drawn that the vertical scale opposite t he intersection of a vertical from any pressu re withany cu rve gives t he latent heat for that pressu re, less the heat requ ired t o cool t he liqu id.
This is the available heat for refrigerating if t he vapor leaves the coils dry and satu rated.
TABLES AND DIAGRAM S 223
R efrigerator Coil Pm . Lbs. Sq. In. Ga.
CHA RT 73 .
— Chart t o Determine Available R efrigeratingEfi‘ect per Pou nd of Carbon Dioxidefor any R efrigerator Pressu re and any R efrigerator or Liqu id Temperatu re.
In the section t o the left of the center axis are two sets of cu rves, the lower , representingtemperatu res of t he vapor leaving t he coils, is so drawn that t he valu e of t he left- handvertical scale opposite a point of intersection of a vertical from any pressu rewith any cu rv e,
gives t he heat absorbed in superheating t he vapor . The sum of this and t he valu e fou nd inthe first section gives t he total refrigerating efi'ect for the casewhen the vapor leaves t he coilsin a su perheated state. The upper cu rves in this section represent qu ality of t he v apor ift he liqu id has not been entirely evaporated and are so drawn that t he valu e on the verticalscale oppos
ite t he point of intersection of a vertical from any pressu re with any cu rve,shows t he heat u navailable for refrigerating, du e t o incomplete evaporation of t he liqu id, and
t he diff erence between thisvalu e and that fou nd in the first section gives the total refrigerating efiect for the case ofwet vapor leaving t he coils.
As an example of the u se of Chart 72 let it be requ ired t o find the refrigerating effect perpou nd of ammoniawhen the pressu re in the coils is 20 lbs. gage, the temperatu re of t he liqu id
224 HANDBOOK OF THERM ODYNAM IC
per Lb .
.0186 .018 .0174 . 0166“5°
Lm Per Cu . Fb.
CHA RT 74 .
— Density and Specific Volume of Ammonia -wat er Solu tions.
before entering t he coil is 70° F. and
(a ) Vapor leaves dry and satu rated;(b) Vapor leaves per cent. dry ;(c) Vapor leaves at a temperatu re of 30° F.
From 20 in the r ight- hand section (Chart 72 ) project u p t o cu rv e The valu e on t hev ertical scale at this point is 502 which is t he valu e for case (a ) . From 20 in t heleft- hand section project t o cu rve per cent. the v alu e on t he left- hand vertical scale is43
, therefore, for case (b) t he resu lt is 5 02 43 459B.T .U. For case (c) , project from20 t o cu rve t he valu e on the vertical scale corresponding towhich is hence t he resu ltfor this case is 502
The refrigeration per pou nd of flu id may be obtained from Eq . bu t since theseare all tabu lar valu es, except the heat of air and of v apor su perheat, t he determinationscan be readi ly made by means of t he charts. From the data of these diagrams the dis
placements of compressors and pumps may be compu ted directly by t he u se of t he slider u le. When superheated vapor densities are t o be ev alu ated
, either v apor— ammonia or
carbon dioxide~ may be assumed t o behave as a perfect gas, v olumes being directly, anddensity inv ersely proportional t o absolu te temperatu res.
The volume per pou nd of ammonia solu tionsmay be read off directly from Chart 74.
226 HANDBOOK OF THERM ODYNAM IC
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INDEX
(Numbers refer t o pages)Absorptionf o
é'
air in water (Winkler) , table0 7of gases by liquids table of , 60
A ccu racy of Marks andDavis tables, 2
A diabatic expansion of steam,values of 8
,table, 1 4Ai r, absorption of in wat er, table of, 60
and steam flow, charts of, 2 16, 21 7and{t
ar
get vapor
, dewpoint, chart of,flow, coefficient of friction for, in ducts,chart of
,220
values of C for,table of
, 1 1 3
gas, blast- furnace, composition of,table , 99
mixtures, best calorific properties of,table,1 07explosive, lim its of propo rtion ,table of,1 08.
re
?u ired for combustion
,table of
,6 1
v e ocity of, in pipes , chart of, 219Alcohols, vapor pressure of, chart, 1 75Altitudes and barometric pressures, 8Ammonia, gas , Mollier diagram for, 226
pressure- temperature relations,for satu
rated vapor , chart oi , 1 65refrig
2
e2
r2
ating effect per pound,chart
,
solutions, table of relations of, 5 4tables of properties of, howderived, 3T¢ diagram for, 225vapor, properties of saturated, table of,
41water solutions, table of partial pressures, 58relation between temperature and percent NH3 in solution chart of, 180relation between total ressu re andper cent NHa in soluti on, chart of ,1 79
relation between total pressure andt em erat u re
,chart of, 1 78
work a sorbed in refrigeration by,charts of, 229A tomicweights, international, table of, 34Average di stillation, products of, crude
mineral oils, table of, 90Balance, heat
hgor locomotive boiler, diagramof 1Barometric, heights, altitudes and pressures,tables of, 8
pressure , howu sed , 1Baumé specific gravity scale, table of, 19Bituminous as coal distillation, products of,
tab e, 95
Blast- furnace gas and air gas,composition of
,table, 99Boiler efii ciency , influ ence of various factorson , charts, 189, 190flue gases, composition of, table, 1 06horse- power evaporation per hour
,chart of, 187locomotive, heat balance for, diagramof, 188Boiling points,table of
,32Brayton gas 0 cle, thermal effi ciency, heat
and u el consumption,charts of
,use of diagrams, 1 5 0Brine, sodium chloride, specific heat of,table, 25British thermal unit v lau e of , 2.
of s t eam and gases , variation of withtemperature, chart, 185Calcium chloride, freezing points, table of, 19Calorific power and composition of coals
,table of, 70of hydrocarbon oils, table of, 90of mineral oils,table of
, 89properties of best air- gas mixtures
,table of, 1 1 7Carbon dioxide, Mollier diagram for, 227pressure- temperature relations for satu
rated vapor, char t oi , 1 66refrigerating eff ect of
,per pound
,chartof, 223tables of propert ies of, howderived , 3
v apo
gbproperties of satu rated, table of,
work absorbed in refrigeration by,charts of 230Carnot steam cycle and derivatives . Ther
mal efficiency and heat consumption,charts of
,200
,201use of charts
, 1 49work andjet velocity, charts of, 202 , 203Cellulose andwood, comparison of, table, 69Centigrade and Fahrenheit temperatures
,table of, 1 6Charts, construction and u se of, 1 39— 1 5 0Chemical heat s of combustion
0 7Chimneys, dimensions of, by Kent’s formula , table, 1 30relation of diameter to horse- power,chart of
, 221construction of chart, 1 50Classification of coals by gas and coke qualities, table of, 87
newbasis of, 4
232
CO from 00 2, rate of formation , table of, 1 06Goals, classification of by gas and coke
qualities, table of, 87combustible and volatile of , table of, 78combu stion,rate of , table , 1 19
newbasis of classification of, 4newtable of chemical and thermal prop
ert ies of, 3powdered,producer gas
,composition of
,table, 1 1 6rate of combustion of with draft , diagram of
,1 86table <
f
3 f
ggmposit ion and calorific power
07Carnot gas cycle, thermal efficiency, heatand fu el consumption
,charts of ,use of diagrams , 1 50Coefficient of cubical expansion of liqu ids,table of , 26of friction for air in du cts
,chart of
,220of heat transfer
,table of
,62of linear expansion of solids, table of, 25of pressure rise of gases and vapors
,constant volume,table of
,27of radiation
,table of
,6 1of volumetric expansion of gases and
ggpors, constant pressure, table of,Coke oven , and retort coal gas, compositionof , table, 94
United States, composition of , table ,9Combu stible and volatile of coals lignites andpeat
,table of
, 78Combustion , air required for, table of , 6 1heats of,table of
, 63of coal,rate of
,table of , 1 19
rate of with draft , chart of , 186Complete- expansion Otto , gas cycle , thermalefficiency,heat and fu el consumption , charts of , 2 1 0, 2 1 1use of diagrams,1 50Common logarithms
,1 32 , 1 34Composition and calorific power of charac
t erist ic coals,table of, 70of blast - fu rnace gas and air gas
,table of
,
99, 1 04of boiler flue gases , table of, 1 1 6of coke oven and retort coal gas,table of
,
94of hypothetical producer gas from fixedcarbon , chart of , 183of natural gases,table of , 91of oil producer gas
,table of
,1 1 3of powc
fisered coal , produ cer gas, table of ,
1 1of producer gas,table of, 1 08of United States coke, table of, 98of water gas, table of, 1 1 3Compound engines, equal distribution of
work in , chart of , 1 6 1Compression gas cycles, thermal efficiency ,heat and gas consumption,chartsof, 207— 21 1
work and charts of,21 2 , 21 3Compressibility of gases
,table of, 82
INDEXCompressor cylinder displacement forgiven capacity
,chart of
,1 59Compressors, one , two and three stages,
mean eff ective pressures of,chartsof , 1 54Conductivity
,thermal , table of internal, 65table of relative , 68Constant , gas, values of R , table of, 28pressure and constant quality lines forsteam with T4; diagram, 194volume , gases and vapors , coefficientof pressure rise of, table , 27lines for steam on the q diagram
,191
cor
l
i
sltzru ct ion and use of diagram
,Constants for the curve PV' K,table of
,for use in Heck’s formula for missingwater, table of , 18Construction and use of charts
,1 39— 1 50Consumption , fuel, Brayton gas cycle ,charts of
,2 1 0, 2 1 1Carnot
,2 1 0
,2 1 1complete- expansion Otto, 21 0, 2 1 1
D iesel,2 1 0, 2 1 1
Ericsson , 207, 209Otto
,2 1 0, 2 1 1
Stirling,206
,208gas, and thermal efficiency, non - compression cycles
,charts of
,204heat, and thermal efficiency, Carnotsteam cycle , charts of , 200, 201
R a
l
r
géine cycle, steam ,
charts of, 196 ,Conversion table, heat and power, 7inches of mercury to pounds per squ areinch
,1 0of units of distance
, 5of power , 7of pressu re,6of surface
, 5of volume, 5of weight and force
, 5of work , 6Crank angle and piston position,table of
,
1 1Critical point , table of, 30Crude m ineral oils, average distillation , produ ct s of , table , 99Cubical expansion of liquids
,coefficient of
,table,26Cylinder, compressor, displacement for givencapacity
,chart of
, 1 59
Densities, equivalent gas, at diff erent press
l
i
érles and temperatures
,chart of
,of gas, comparison of experimental andcomputed values, table of , 29Density and specific volume of ammonia
water solutions , chart , 224of the liquid (steam ) , chart of, 1 7 1 , 1 72Determ ination of m .e .p. for single- cylinderengines, chart of , 1 60construction and use of chart
, 1 44Dewp0 1n
1
t
7
f
6
0 r air and water vapor,chart of
,
234Gas,Brayton cycle, charts of, 2 1 0, 2 1 1Carnot
,21 0, 21 1complete- expansion Otto ,
Diesel,21 0, 21 1
Ericsson,207
,209
Otto,21 0, 21 1
Stirling cycle , charts of, 206, 208cycles compression , work and m .e .p.charts,of
,Brayton
,2 10
,2 1 1Carnot
,21 0
,2 1 1complete- expansion Otto , 21 0, 21 1
Diesel,2 1 0
,21 1 , 2 1 5
Ericsson,207 , 209
Otto , 2 1 0, 2 1 1 , 2 1 4Stirling , 206 , 208thermal efficiency , heat and fuel consumption
,charts of,Brayton
,2 1 0
,2 1 1Carnot
,2 1 0
,21 1complete—expansion Otto
,2 10, 21 1
D iesel , 21 0, 2 1 1Ericsson
,207, 209
Otto , 2 1 0, 21 1Stirling, 206, 208non- compression
,thermal efficiency of,charts , 204
work and charts of , 205densities equ ivalent at diff erent p ressures and temperatu res,chart of
,
1 64comparison of experimental and compu t ed valu es of, table of , 29engines, Otto cycle, diagram factors for ,table of
,1 22from fixed carbon , heats of reaction forhypothetic producer, chart of , 184
composition of hypothetic producer,chart of
,183oil produ cer
,composition of
,table , 1 1 3pressure - temperature- volume relations
,charts of, 192produ cer,composition of
,table
,1 01tests
,table of
,1 1 4
PV and T relations, chart of , 193water, composition of , table , 1 1 3Gases,absorption of by liqu ids
,table of
, 60and vapors at constant volume , p ressure rise of , coefficient of , table, 27at constant pressure,coefficient of
volumetric expansion , table of, 26boiler flue,composition of , table, 1 1 6
compressibility of,table
,28natu ral
,composition of, table , 91
relation between temperatu res and heat,chart of
,185specific heat of, chart , 1 62 ; of table , 22Gasolenes
,fractional distillation of, chart of
182fractionation tests of,table of, 1 02
vapor pressure of, chart of, 1 73B arter’s weight of flow, superheated steam,chart of
,218
Heat and fuel consumption, compression gascycles,charts of ,Brayton
, 21 0, 21 1Carnot,2 1 0
,21 1
INDEXHeat and fuel consumption
,complete- expansi on Otto , 2 1 1
D iesel,
E ricsson,207
,209
Otto , 2 1 0, 2 1 1Stirling , 206, 208and gas consumption
,and thermaleffi ciency
,non- compression gas
cycles , charts of, 204and power conversion table,7and temperatu res , relation of, for gases ,chart of
,185balance for locomotive boiler
,diagramof
,188balances of gas and oil engines
,table of
,
1 23consumption and thermal efficiency ,Carnot steam cycles, charts of,200, 201
R ankine cycle, (steam ) , charts of. 196,197latent , steam ,
chart of, 1 69of fpsion for variou s substances
,table
0ofvaporization for various substances,table of,3 1of the liquid
,steam
,chart of , 1 68per pound of steam above feed t em
perat u re, chart of, 187speci
z
fi
z
c of gases,chart of
,1 62 ; table of,of liqu ids , table of, 24of solids , table of, 20of su perheated steam
,2 ; chart of , 1 63supplied and work
,compression gascycles
,chart of
,2 1 4
,2 1 5total entropy diagram for steam , Mollier
,195steam , chart of, 1 70transfer, table of coefficients of, 62
u nit of,2
Heats of combu stion of fuel elements andchemical compou nds,table of
,63of reaction for hypothetical produ cergas from fixed carbon
,chart of
,184
Heck’s formula fo r m issing wate1 , 18Horse—power of chimneys
,diameter for ,charts of
,221per pou nd table of
,1 2per cu. ft. per minu te su pplypressure gas , for single - stage compressors
,chart of
,1 5 1for
1giro—stage compressors
,chart of
,for three- stage compressors,chart of
,
1 53constru ction and use of chart forsingle— stage, 1 39
two stage,1 40three-
,stage 1 40
Humidity andweight of moisture,cubic footsaturated a i r , chart of , 1 77construction and use of chart,1 45
Hydrocarbon oils, calorific power of , table , 90Hydrocar
1
b
7
0
3
ns, vapor pressu re of, chart of ,Hyperbolic logarithms
,1 36
INDEXHypothetical producer gas from fixed carbon, composition of, chart of, 1 83
beat s of reaction of,chart, 184
Ignition temperatures, 3 ; tables of , 30Inches of mercury to pounds per square inch
,conversion table, 1 0of water, theoretical draft pressure ,table of, 1 1 7
Indicator card , m issing water from ,1 8
Internal thermal conductivity, table of , 65International atom ic weights, table of , 34Isothermals , compressibility of gases by ,table of, 28Jet velocity and work , Carnot steam cycle ,charts of , 202, 203
Ranking
e , cycle (steam ) , charts of, 198,19
Kerosene and petroleums , fractional distillation of , chart of, 181fractional tests of, table of , 1 00Kerosenes , vapor pressure of, chart of, 1 74Latent heats of fusion
,table of, 3 1of vaporization , table of, 3 1of steam
,chart of
,1 69
Lignite,composition and calorific power of,
Lignites,combustible and volatile of,83,85 ,86
Limit s of proportion for explosive air- gasm ixtures , table of, 1 18
Linear expansion of solids , coefficient of ,table, 25Liquid and gaseous fuels
,boiling points of ,table , 33
Liquids,absorption of gases by , table of , 60coefficient of cubical expansion of table ,26specific heats of
,table , 24
Logarithms to the base e , 1 36to the base 1 0 , 1 32, 1 34Marks and Davis’ steam tabl es, 36, 40Maximum work and supply pressu re, chartof , 1Mean B .T .U. value of , 2eff ective pressure and h .p. , table of, 1 2and maximum work , chart of, 1 5 6and work non- compression gas cycles ,chart of, 205
Diesel cycle , for heat added , chartof, 2 1 5Otto cycle , for various amounts ofheat added
,chart of, 21 4compression gas cycles , Brayton ,Carnot
,Diesel , Otto and completeexpansion Otto , chart-s of, 21 2, 2 1 3
Mean eff ective p ressure , det ermmat i on of ,for single cylinder engines, chart of,1 60factors for Otto cycle engines, table of ,24
of compressors, one, two and threestages,charts of , 1 5 4, 1 5 5construction and use of charts, 1 40
235
Melting or freezing points, table of, 34Mineral oils, calorific power of, table of, 89crude, average distillation , products of,table of
, 99properties of,table of , 92
Missing water, Heck’s formula for, 18Moistu re, weight of, per cubic foot of satu
rated air, chart of , 1 77Mollier diagram f or ammonia , 226for carbon dioxide 227
t ot alglg
eat entropy diagram for steam ,
Multi- stage compressors,mean eff ectivepressure of , chart of, 1 54
Napierian logarithms, 1 36Napier’s co
gfficient of steam flow,
chart of,
2 1
Naphthalei
ne
8
8
8
from Russian petroleum, table0 J
Natu ral gases,composition of
,table , 91
Non - compression cycles,thermal e fficiency ,heat and gas consumption , chartsof, 204use of diagrams
,1 49
Work and m .e .p. chart of, 205Oil and gas engines, heat balances of, tableof , 1 23Oil gas, properties of, table of 90produ cer gas
,composition of, table of,
Oils, hydrof
carbon,calorific power of , table
0 90
m in eral,calorific power of , table of, 89crude
,average distillation , productsof
,table of
,99properties of
,table of , 92
Otto- cycle gas engines, diagram factors fo r ,table of, 1 22
mean eff ective pressu re factors for,tables of,1 24thermal effic iency , heat and fu el consumption
,charts of
,21 0
,2 1 1use of diagrams , 1 50
work , and m .e .p. for various amounts ofheat added,chart of
,2 1 4
Paraffines from Pennsylvania petroleum ,table of,88Parr’s psychrometric diagrams, 1 76 , 1 77Peat
,composition and calorific power of, 77combu stible and volatile of , 86Petroleum and kerosene, fractional distillation of
,chart of, 181distillates
,vapor pressure of heavy
,chart of,1 74
et hylef
nes and naphthalenes from ,table
0 88
kerose
éi es, fractionation tests of , table of ,
1 0light,vapor pressure of
,chart of, 1 73
paraffines from ,table of
,88Pipes
,velocity of air in , chart of, 192Piston positions for any cran k angle , table of,1 1
am
Pitot t u bef
readings and velocity of air, chart0 2 19Pounds per squ are inch to inches of mercury
,
conversion table , 1 0Power and heat, conversion table, 7and table of,1 2umts of
,conversion table of , 7Pressure
,barometric
,table of
,8constant of steam
,with T¢ diagram , 194in inches of water,theoretical draft ,table of
,1 3 1
mean eff ective , for compressors, one twoand three stages, chart of, 1 54rise
,of gases and vapors at constantvolume
,coefficient of
,table
,27temperatu re
,relations for satu ratedvapor
,carbon dioxide
,chart of, 1 66for satu rated vapor of ammonia,chart of
,1 65steam
,chart of
,1 6 , 1 67volume relations of gases
,charts of ,
192units of, conversion table , 6vapor of heavy petroleum distillates ,chart of
,1 74of hyd rocarbons, chart of, 1 73
volume and T¢ relations of gases, chartof,193
ratios, constants for, table of , 1 3values of , for gases, variou s conditions
,table of
,28Pressures, interpretation of , 1Produ cer gas
,composition of
,table of
,108from fixed carbon
,composition of hypothetical
,chart of
,183hypothetical from fixed carbon
,heats of reaction,chart of, 184powdered coal , composition of, table of,
1 1 6tests of,table of
,1 1 4Products of bituminou s gas coal distillation
,table of, 99of cru de m ineral oils,average distillation , table of , 99Properties of ammonia and carbon dioxide ,tables of , howderived , 3of m ineral oils , table of, 92of oil gas
,table of
,90of saturated carbon dioxide vapor
,tableof , 50ammonia vapor, table of, 4 1steam
,table of , 36of su perheated steam ,
tables of,40Psychrometer readings , chart of, 1 76. Construction and u se of chart
,1 45
Quality, constant steam ,lines of with T¢diagram
,194
R ,gas constant
,table of, 28
R adiation coefficients , table of, 6 1R ankine cycle (steam ) thermal efficiency andheat consumption
,charts of
,196,
197use of charts,148, 1 49
work and jet velocity, charts of, 198,199
INDEXR ate of combustion of coal with draft, diagram of , 186table of, 1 19of formation of CO from C0 2 and carbon
,table of
,1 06
R ational and empiric formulas,air and steamflow
,charts of
, 2 1 6 , 2 1 7
R eaction,heats of
,for hypothetical producergas from fixed carbon
,chart of
,184
R efrigerating effect per pound ammonia,chart of
,222carbon dioxide , chart of, 223
R efrigeration , work absorbed in by ammonia, charts of, 229by carbon dioxide , charts of, 230
R elative thermal conductivity,table of
, 68
work of two- stage compressors, compared to single- stage
,chart of
,1 5 7
R esistance factors , flowchange, table of, 1 25R etort coal and coke oven gas
,compositionof
,table of
, 94
3 values of for adiabatic expansion of steam ,table of,1 4for variou s su bstances and conditions
,
1 5
Saturated ammonia vapor,properties of
,table,4 1
carbor
ti dB
oxide vapor,properties
,table
0 5steam, table of properties of, 36S ingle cylinder engines
,determ ination of
mean eff ective pressure in,chartfor, 1 60
- stage ' compressors, horse - power percu . ft . per m inu te supplypressu re gas, chart of, 1 5 1
work per cubic foot su pply pressu re,chart of
,1 5 1
Sodium chloride brine,specific heat of table
,
25
Solids, coefficient of linear expansion of,table of,25specific heats of
,table
,20
Solu tions, ammonia-water,relation betweento tal pressu re and per cent NH3 insolution , chart of, 1 79
relation between total pressu re andtemperatu re , chart of, 1 78between temperature and per centNH3 in solution , chart of, 180table of relations of
, 5 4of partial pressu res,58
Specific gravity scale , Baumé , table of, 19heat of sodium chloride brine,table of
,of gases, chart of, 1 62 ; table of, 22of liqu ids,table of
,24of solids
,table of
,20of
1zi
z
i
iperheat ed steam , 2 ; chart of,
volume and density of the liquid,
(steam ) , chart of, 1 7 1 , 1 72Stack
,see Chimney .
Steam , adiabatic expansion of, values of sfor, table of , 1 4and ai r flow, charts of, 21 6, 2 1 7
238
Vapor pressure of hydrocarbons of the gasolene class,chart of , 1 73
Vaporization,latent heat of
,table of
, 3 1
Velocity of air in pipes, chart of , 219un i ts of,table of
,7
Volatile and combustible of coals,lignites
,and peat,table of
, 78Volume, p ressure and T4; relations of gases ,charts of , 193
- temperatu re - pressure relations of gases,charts of
, 192
u nits of , conversion table , 5Volumetric efficiency of compressors
,chartof, 1 54construction and use of chart
,1 40expansion of gases and vapors at constant pressure
,coefficient of
,tableof, 26
Water, absorption of air by , table of , 60gas, composition of , table of , 1 13m i ssing
,from indicator card,
18Wei ght anid force
,units of
,conversion table
0 5Weights , atomic , international , table of,Wet and dry bulb psychrometer readings,
chart of , 1 76Wood and cellu lose,table of comparison of
,
69Work absorbed in refrigeration by ammonia,charts of
,229by carbon dioxide
,charts of, 230
INDEXWork absorbed and jet velocity, Carnotsteam cycle , charts of, 202 , 203
R ankine cycle, (steam) , charts of , 198,199and m .e .p. Diesel cycle for variou samounts of heat added , chart of2 1 5
Otto cycle , chart of , 21 4for the compression gas cycles,Brayton,Carnot , Diesel , Otto ,and complete expansion Otto
,chart of,21 2
,2 1 3 , 2 1 4, 2 1 5for non - compression gas cycles ,charts of
,205use of diagram
,1 49Work
,equ al distribu tion of in compou ndengines
,chart of, 1 61
maximum,and su pply pressu re
,chartof
,1 5 6of two - stage and three - stage compressors , compared to single- stage ,
chart of, 1 5 7per cubic foot of supply pressure gas forsingle- stage compressors , char t of,1 5 1construction and use of chart
,1 39for twc)
2
- stage compressors,chart of
,
1 5constru ction and use of chart,1 40for three- stage compressors
,chart of
,
1 53construction and use of chart,1 40un i ts of, conversion table, 6
