Evaporative Concentration of a Thermally Sensitive Chemicalchambro/Chen 4450 Lecture Presentation Rev B... · Factor 10,840 Bottom Line = Heat Loss Small Scale Has It Large Scale

Evaporative Concentration of a Thermally Sensitive Chemical

Chen 4450 Process SafetyAuburn UniversityNovember 27, 2006

Guest SpeakerRobert D’Alessandro, P.E.Director of Process EngineeringDegussa Corporation

Auburn University Chen 4450 Process Safety Robert D‘Alessandro, P.E.

Introduction

Five Main Principles of Inherently Safer Chemical Plants:

Limitation of Effects

Use equipment fit for its service

Webster: Existing in something as an inseparable element.

Synonyms: Innate, native, inbred, ingrained

Substitution

Use safer chemicals

Simplification

Use less complexity

An Integral Part Of

Attenuation or Moderation

Use the least hazardous conditions

Intensification or Minimization

Use less hazardous chemicals


Lecture Objectives

Recognizing potential reactivity problems

Safety aspects of connected equipment

Safety instrumented systems

Adiabatic calorimeters for obtaining proper data

Gassy systems versus tempered systems

Vapor-liquid disengagement in vessels

Two-phase venting versus “all vapor” venting

Introduction to the following process safety related concepts:

Reactive System

Pressure Relief

ExampleEvaporative

Concentration of a

Thermally Sensitive ChemicalIntegrating process safety into process design


Evaporative Concentration

Process Flow Diagram - RA 2nd Stage Concentration

Steam60 psig

Z-100Three Stage Steam

Jet Vacuum System

Chilled Water5 C

T

70 wt% RAFrom 1st StageConcentration

Steam150 psig

Process OffgasTo Thermal Oxidizer

90 wt% RATo Crystalazer Chilled Water

5 C

Process CondensateTo Treatment

Note 1: Barometric LegNote 2: Equilization LineNote 3: 3 Barometric Legs

P

L

L

RO

F

T

R-100

P-100

A-100X-100

V-101

P-101

X-101

83 C

70 C

15 C

20 C

20mmHgA

2,500 PPH

1,944 PPH

Cond.

250 PPH

806 PPH

10mmHgA

16.7psia

16.7psia

1 32

575,200Btu/hr

308,800Btu/hr

21.7 C

15.2 C


Signs of Inherent Trouble

“70 wt% RA begins, at what the chemists describe as, a slow decomposition when temperatures exceed 120 °C.”

Be suspicious of “normal” laboratory data

“The chemists also noted some foaming when this slow decomposition occurred.”

Hints from Chemists or Operators



MSDS – Material Safety Data Sheet:Excellent source of general safety information

OSHA type data is good – hygiene, PPE, medical, fire fighting, etc.

Physical property data is usually good

“MSDS for 70 wt% RA also indicates this temperature limit.”

However, my experience indicates:Reactivity data is lacking and sometimes wrong

Better now then in the past, but still needs improvement

Better for common petrochemicals then for specialty chemicals



The hints from the chemists tell us that additional data is needed.

What kind of data?


Laboratory Scale Data

Consider:A typical organic fluid at 80 °C in some container

Surrounded by still air at 20 °C

Factor 10,840

Bottom Line = Heat Loss

Small Scale Has It

Large Scale Doesn’t

?? WHY ??

Laboratory Heat LossEquipment Btu / Hour / Lb

Test Tube10 ml

Beaker100 ml

Cooling Rate°C / Minute

0.09

0.06

542

341

Full Scale Heat LossEquipment Btu / Hour / Lb

Reactor660 gallons

Reactor6600 gallons

0.048

0.004

4.6

0.05

Cooling Rate°C / Minute


Surface Area to Volume Ratio

0.0

1.0

2.0

3.0

4.0

5.0

6.0

7.0

8.0

0.001 0.010 0.100 1.000 10.000 100.000 1000.000

Volume (Gallons)

Surf

ace

Are

a / V

olum

e (S

F/G

allo

n)

L / D = 1

L / D = 4

3.8 ml 38 ml 380 ml 3800 ml (S/V)Lab Scale >>> (S/V)Commercial Scale

Heat Generation ~ Volume of Contents

Heat Loss ~ Surface AreaSmall Scale Experiments Must

Eliminate Heat Loss

Surface AreaVolume Volume Ratio

10ml

100ml

1000gallons

5000gallons

124

57

2

1

10.5

4.9

0.145

0.085




Two Forms of Heat LossBoth are magnified by large surface to volume ratios

Heat loss to the sample container caused by thermal capacity of test cell.

CapacityCarryingHeatSampleCapacityCarryingHeatSystem

≡Φ Phi Factor

tpftf

pbb

tpftf

pbbtpftf

CmCm

CmCmCm

+=+

≡Φ 1

If ThenTUAQ Δ=

Heat loss to surroundings caused by temperature difference .

0=ΔT 0=Q

Decrease Test Cell Mass

Increase Sample Mass

Commercial Vessel Phi Factor = 1.05 to 1.10Goal for Small

Scale Equipment


Adiabatic Calorimeters

ARC – Accelerating Rate Calorimeter

Invented by D.I. Townsend at Dow Chemical in the late 1970s

Solved the ΔT problem

But not the thermal inertia problemHeavy Wall Test Cell

Containment T

Sample T

Heating Elements

Containment Vessel

Can not track very fast reactions

Very sensitive at low reaction rates

Still has important applications

High Thermal Inertia Adiabatic Calorimeter

Phi Factor: 2.0 ≤ Φ ≤ 4.0

Heavy wall test cell

Built to withstand internal pressure


Adiabatic CalorimetersLow Thermal Inertia Adiabatic Calorimeters

Invented by DIERS in the early 1980s

Solved the ΔT problem

Solved the thermal inertia problem

Can track very fast reactions

Not sensitive at low reaction rates

Phi Factor: 1.05 ≤ Φ ≤ 1.15

Thin wall test cell

Pressure compensation prevents test cell rupture



Containment vessel isolation ball valve

Containment Vessel Pressure Transducer

Test Cell Pressure Transducer

“Super”Magnetic Stirrer

Auxiliary Fill Line

Rupture Disk(1900 psig)

3-Way ValveFilling Test Cell

or Pressure Equalization



Thin Walled Low Thermal Inertia Test Cell

Insulation for Maintaining Adiabatic Conditions

A View of the InsidePressure Containment


The type of data that is needed is now known!

The experiment must now be specified.


Data from a Low Thermal Inertia Adiabatic Calorimeters


Tempered Versus Gassy SystemsTempered Liquid Phase Systems:

T & P related directly to each other via the vapor pressure of components

In Open Systems:Heat generation or addition causes vaporization of components

Vaporization provides liquid phase cooling

When vapor removal is sufficient, T (and P) stops increasing

In Closed Systems:Essentially no vaporization occurs

Pressure increases in step with increasing temperature

Examples of Tempered Systems:Styrene polymerization

Methanol vessel under fire

Blowdown of a vessel containing liquid propane


Tempered Versus Gassy SystemsGassy Liquid Phase Systems:

Non-condensable gases are present or formed by reaction

T & P are not simply related by the vapor pressure of the components

In Open Systems:Heat generation or addition does not cause vaporization

Cooling effects from vaporization do not occur

Instead, the sensible heat content (temperature) of the liquid increases

Examples of Gassy Systems:Decomposition of some organic peroxides

Decomposition of some polymers

Blow-down of a subcooled liquid containing dissolved gas

In Closed Systems:Pressure increases almost without bounds

Rossonic Acid Decomposition


Experimental Specification

Testing 90 wt% RA in a Low Thermal Inertia Adiabatic Calorimeter:Stainless Steel Open Test Cell

Containment Backpressure = 300 psig

Charge = 90 g (Fill ~ 75%) (Phi Factor ~ 1.1)

Hold at 70 °C

Test Normal Operating Condition

Heat (4 °C Increments) and

Search (5 minute holds)

Until self-heating is observed

Convert to adiabatic mode

Allow test cell to self cool


Adiabatic Calorimeter Data

Temperature Versus Time

50

75

100

125

150

175

200

225

250

0 2000 4000 6000 8000 10000 12000 14000

Time (seconds)

Tem

pera

ture

(C)

Heat & Search

Normal Operating Condition

Self-Heating Detected

∆T ~ 120 °C

Adiabatic Operation



Pressure Versus Time

250

275

300

325

350

375

400

425

0 2000 4000 6000 8000 10000 12000 14000

Time (seconds)

Pres

sure

(psi

a)

Containment Pressure

Self-Heating Detected

Pressure Rise ~ 90 psiClosed Test Cell ~ 12,000 psi



Self Heat Rate Versus Recipricol Temperature

0.01

0.10

1.00

10.00

100.00

-3.0 -2.9 -2.8 -2.7 -2.6 -2.5 -2.4 -2.3 -2.2 -2.1 -2.0 -1.9 -1.8 -1.7 -1.6 -1.5

Recipricol Temperature

Self

Hea

t Rat

e (C

/min

)

110 C

94 C

Heat & Search

Based on Lab Data

Onset Temperature

Maximum Self-Heat Rate 80 °C/minute

Second Reaction

ArrheniusKinetics



Pressure Rise Rate Versus Recipricol Temperature

0.01

0.10

1.00

10.00

100.00

1000.00

-2.6 -2.5 -2.4 -2.3 -2.2 -2.1 -2.0 -1.9

Recipricol Temperature

Pres

sure

Ris

e R

ate

(psi

/min

)

Maximum Pressure Rise Rate

180 psi/minute


Now the proper data is known and available!

So lets examine the Auburnite design concept




Process Flow Diagram - RA 2nd Stage Concentration

Steam60 psig

Z-100Three Stage Steam

Jet Vacuum System

Chilled Water5 C

T


Steam150 psig

Process OffgasTo Thermal Oxidizer

90 wt% RATo Crystalazer Chilled Water

5 C

Process CondensateTo Treatment

Note 1: Barometric LegNote 2: Equilization LineNote 3: 3 Barometric Legs

P

L

L

RO

F

T

R-100

P-100

A-100X-100

V-101

P-101

X-101

83 C

70 C

15 C

20 C

20mmHgA

2,500 PPH

1,944 PPH

Cond.

250 PPH

806 PPH

10mmHgA

16.7psia

16.7psia

1 32

575,200Btu/hr

308,800Btu/hr

21.7 C

15.2 C



Jacket Jacketor or

Total Working Tubes Tubes

R-100 2nd Stage ConcentratorPressure Vessel

476 gallons

395 gallons 4'0" ID x 4'0" TT 30 psig & FV 100 psig & FV

316L Stainless

Steel

316L Stainless Steel

A-1002nd Stage Concentrator Agitator

Pitched Blade Turbine NA NA

2 - 18" Impellers 50 RPM x 5 HP NA NA

316L Stainless

SteelNA

X-1002nd Stage Concentrator Overhead

Shell & Tube Exchanger NA NA 630,000 Btu/hr 30 psig & FV 100 psig & FV

Carbon Steel Carbon Steel

P-1002nd Stage Concentrator Bottoms Pump

Centrufugal NA NA 10 GPM x 50' TDH 100 psig NA316

Stainless Steel

NA

Z-1002nd Stage Concentrator Vacuum System

Steam Jets & Direct Contact Condensers

NA NA 15 PPH @ 10 mmHgA 3 Stages 200 psig & FV NACarbon Steel NA

V-1012nd Stage Concentrator Distillate Receiver

Pressure Vessel

264 gallons

172 gallons 3'0" ID x 4'0" TT 15 psig & FV NA

Carbon Steel NA

X-1012nd Stage Concentrator Distillate Receiver



P-1012nd Stage Concentrator Distillate Receiver

Centrifugal NA NA 60 GPM x 100' TDH 100 psig NADuctile

Iron NA

Characteristics Shell ShellVolume

Service TypeItem

N

umbe

r Design PressureEquipment List - 2nd Stage Concentration

Materials of Construction



Steam60 psig

T


90 wt% RATo Crystalazer

L

RO

F

T

R-100

P-100

A-100

83 C

70 C

20mmHgA

2,500 PPH

1,944 PPH

Cond.

70 C556 PPH

Water Vaporto OverheadCondenser

Saturated Steam @ 60 psig

Temperature = 153 °C

Onset Temperature = 94 °C

This doesn’t look good!

Inventory ~ 395 gallons

Mass ~3,300 pounds

Wetted Area ~ 62 ft2

Normal Operating T = 70 °C

Onset Temperature = 94 °C

Close, but OK



Steam60 psig

T


90 wt% RATo Crystalazer

L

RO

F

T

R-100

P-100

A-100

83 C

70 C

20mmHgA

2,500 PPH

1,944 PPH

Cond.

70 C556 PPH

Water Vaporto OverheadCondenser

Quick Calculation

Perry’s Handbook

For stainless steel, jacketed vessels with organics and condensing steam

OHT Coefficient = 50 -150 Btu/h/sf/F

U ∆T T condBtu/h/sf/F °C °C

80 62 132100 50 120120 42 112

( ) ( )

UAQTTUAQ

ftAhBtu

lbBtuhlbQ

=Δ⇒Δ=

=

==

22.62/000,559

/1005/556



Inventory Concerns:Inventory is relatively large for such a potentially energetic material.

Reducing inventory doesn’t work…………. Why?

Wall Temperature Concerns:Inside wall temperature is probably higher than decomposition onset T

No choice at the required capacity with the current configuration

Single Failure Upset Cases of Concern:Loss of agitation

Failed open steam valveResults in Increasing wall temperature

Are there any others?



Multiple Sequential Failure Upset Cases of Concern:Loss of cooling + stuck open steam valve

Loss of vacuum + stuck open steam valve

Failed closed pressure valve + stuck open steam valve

And others!

CONCLUSIONS:An uncontrolled exothermic decomposition appears plausible

The concentrator relief device should be sized for this case

Fortunately, the necessary data is available!

But should sizing be based on “all vapor” venting or two-phase flow?


Why Does Two-Phase Venting Occur

Results of Water Blowdown Experiments:

Final Liquid Volume

For “All Vapor” Venting

485 Gallons


Why Does Two-Phase Venting Occur

Valve Opens

Pressure Falls

If Rate of Bubble Generation is High Enough Liquid Swells to the Top of the Vessel

Liquid Swell Caused by Volume Generation

Not Liquid Entrainment

Highly Dependent on Physical Characteristics of Components

Volumetric Generation

LiquidSwell


Rossonic Acid Decomposition

Volumetric Generation of Non-Condensable Gas


“The chemists also noted some foaming when this slow decomposition occurred.”

Remember this clue!

Concentrator Fill ~ 83 %

CONCLUSION: Design for Two-Phase Flow


Larger Relief Devices Are NeededWhen Two-Phase Flow OccursVolume Balance Concept – Closed System

Gas Generating

Exothermic Reaction

T & P

Increase

Wouldn’t It Be NiceVOLUME

GENERATIONRATE

VOLUMEEXPANSION

RATE=

CONSTANT

PRESSURE


Larger Relief Devices Are NeededWhen Two-Phase Flow OccursVolume Balance Concept – Open System

A More Realistic

System

VOLUMEGENERATION

RATE

VOLUMEDISCHARGE

RATE=

CONSTANT

PRESSURE


Larger Relief Devices Are NeededWhen Two-Phase Flow OccursVolume Balance Concept – Open System

Definition of a Successful Emergency Relief Device:

Provides a balance between volume generation and volume dissipation

For the “Worst Credible” case conditions

At a pressure no greater than the maximum allowable pressure


Larger Relief Devices Are NeededWhen Two-Phase Flow OccursVolume Balance Concept

Vg = Volume Generation Rate = Volume Discharge Rate = Vd

⎭⎬⎫

⎩⎨⎧

====ρρρGAGAWVV dg

Mass Flow Through Relief Device

Two-Phase Density

Two-Phase Mass Flux

Relief Device X-Sectional Area

2

3

3

2

ftsft

ftlbfts

lbG

==⎭⎬⎫

⎩⎨⎧ρVolumetric Flux =


Larger Relief Devices Are NeededWhen Two-Phase Flow OccursVolume Balance Concept Saturated Hexane at 320 °F & 132.8 psia

Two Phase Density

0

10

20

30

40

0.0 0.2 0.4 0.6 0.8 1.0

Inlet Void Fraction

Two

Phas

e D

ensi

ty (l

b/cf

)

Increasing Vapor Content

Critical Mass Flux

500

600

700

800

900

0.0 0.2 0.4 0.6 0.8 1.0

Inlet Void Fraction

Crit

ical

Mas

s Fl

ux (l

b/sf

/s)



Larger Relief Devices Are NeededWhen Two-Phase Flow Occurs

0

50

100

150

200

250

300

350

400

450

0.0 0.1 0.2 0.3 0.4 0.5 0.6 0.7 0.8 0.9 1.0

Inlet Void Fraction

Volu

met

ric F

lux

(cf/s

/sf)

ALL LIQUID ALL VAPOR

⎭⎬⎫

⎩⎨⎧

====ρρρGAGAWVV dg

Volume Balance Concept Saturated Hexane at 320 °F & 132.8 psia



Simple Ideal Vent Sizing Results

Inside Diameter = 4’0” T-T Length = 4’0” Total Volume = 475 gallons

Fill Volumes = 428 gallons (90 %), 333 gallons (70 %), 238 gallons (50 %)

Design Pressure (DP) = 50, 75, 100, 150 psig

Maximum Pressure = (1.1) DP (10% accumulation)

Maximum Pressure Rise Rate = 180 psi per minute

Consider the following cases:


Simple Ideal Vent Sizing Results

Concentrator475 Gallon Vessel

0

50

100

150

200

250

300

350

400

450

25 50 75 100 125 150 175

Design Pressure (Psig)

Vent

Are

a (S

q In

)

Fill Ratio = 90%

Fill Ratio = 70%

Fill Ratio = 50%

~ 12” Vent

~ 23” Vent


A large vent is required due to two-phase flow

Can two-phase flow be avoided?


Yes

By allowing enough room for vapor disengagement


Vessel DisengagementBubbly Flow Regime

Co = 1.2

0.00

0.10

0.20

0.30

0.40

0.50

0.60

0.70

0.80

0.90

1.00

0.1 1.0 10.0 100.0

Dimensionless Superficial Vapor Velocity

Vess

el A

vera

ge V

oid

Frac

tion

Onset/Disengagement Boundary

Vessel Condition

Vapor Venting Region

Two Phase Venting Region

Inside Diameter = 4’0”

T-T Length = 4’0”

Total Volume = 475 gallons

DP = 50 psig & FV

Disengagement

Maximum Fill ~ 17 %



With less inventory, how can the heat needed for the normal evaporation be added?

Decrease the concentrator inventory

Avoid two-phase flow

Size the relief device for “all vapor” venting

Basis for New Concentrator Design Concept


New Concentrator Design

Inside Diameter = 4’0”

T-T Length = 5’0”

Total Volume = 535 gallons

DP = 50 psig & FV

DT = 500°F 70 wt% RA

Emergency Water

Water Vapor

90 wt% RA

20 mmHg

70°C

LC On Upstream Vessel

5 psig Saturated

Steam

Tube Side

Condensation

Conditions

11.5 psia

93°C

Pumping

TrapSide View Top View

Baffles

Working Volume = 70 gallons

Maximum Volume = 100 gallons

Relief Device = 6” PSE based on vapor flow only

Minimization, Moderation, Limitation of Effects


Is This Enough?

Shutdown Based On:

Redundant High Level

Redundant Process Temperature

Redundant Tube Side Steam Pressure

Quench water addition triggered by high process temperature only.

Shutdown

Feed & Steam

Safety Instrumented Systems (SIS) - Interlocks

Independent of the Basic Process Control System (BPCS)


Concentrator – Top View

Emergency Vent Line

Normal Vent Line

Car Seal Open

Full Port Block Valve

Rupture Disk

(hidden)


Concentrator – Bottom View

Process Outlet Pipe

Steam

Condensate Line

Stab-In

Tube Bundle

SIS Redundant

Temperature

Transmitters


Concentrator – Bottom View

SIS Redundant Level Switches

Process Outlet Pipe

BPCS Level Transmitter


What Could Have Been Done Differently?

Conduct a high phi factor calorimeter test to better understand reaction mechanism.

Conduct calorimeter tests to determine if the reaction system tempers at the maximum allowable working pressure of the vessel.

Conduct a blowdown test to obtain a better feeling for disengagement dynamics.

Use more sophisticated tools to analyze the possibility of utilizing smaller vent sizes.


Alternate Schemes to Consider

Falling Film EvaporatorA very good alternative

Usually have low heat transfer coefficients

Probably more expensive then vessel/tube bundle combination

Agitated Thin Film EvaporatorNot the best for low viscosity liquids

Considerably more expensive then vessel/tube bundle combination


Connected Equipment

Jacket Jacketor or

Total Working Tubes Tubes

R-100 2nd Stage ConcentratorPressure Vessel

476 gallons

395 gallons 4'0" ID x 4'0" TT 30 psig & FV 100 psig & FV

316L Stainless

Steel

316L Stainless Steel

A-1002nd Stage Concentrator Agitator

Pitched Blade Turbine NA NA

2 - 18" Impellers 50 RPM x 5 HP NA NA

316L Stainless

SteelNA

X-1002nd Stage Concentrator Overhead



P-1002nd Stage Concentrator Bottoms Pump

Centrufugal NA NA 10 GPM x 50' TDH 100 psig NA316

Stainless Steel

NA

Z-1002nd Stage Concentrator Vacuum System

Steam Jets & Direct Contact Condensers

NA NA 15 PPH @ 10 mmHgA 3 Stages 200 psig & FV NACarbon Steel NA

V-1012nd Stage Concentrator Distillate Receiver

Pressure Vessel

264 gallons

172 gallons 3'0" ID x 4'0" TT 15 psig & FV NA

Carbon Steel NA

X-1012nd Stage Concentrator Distillate Receiver



P-1012nd Stage Concentrator Distillate Receiver

Centrifugal NA NA 60 GPM x 100' TDH 100 psig NADuctile

Iron NA

Characteristics Shell ShellVolume

Service TypeItem

N

umbe

r Design PressureEquipment List - 2nd Stage Concentration

Materials of Construction


Summary

Critical information often comes from inconspicuous place.

Keep your eyes and ears wide open!!

Guessing is unacceptable

In God we trust, everyone else bring the right data!!

Avoid two-phase emergency venting where possible

Its always easier to ride your bicycle down-hill

Be weary of lab scale data when exothermic reactions are involved.

Scale-up is usually not included in a chemistry curriculum!!

A safety concept can not be realized without having the proper data

Don’t go skydiving without reading the parachute instructions

Chemistry knowledge is a key ingredient for process safety.

Don’t sell your Morrison & Boyd on eBay!!


Summary

What can happen, will happen.

Remember Murphy’s Law.

Keep the “stuff” in the pipes

Once you start skidding, you are out of control.

Integrate the safety concept and the process design

Avoid problems by changing the basic process and/or equipment

Pressure relief should be the last line of defense

But not the only line of defense.

Use the right equipment.

Don’t try to fix your car without the right tools.


Closing Remarks

Contact Information – Call or Write Anytime !!

Email: [email protected] (best method)

Phone: 251-443-2420 (I travel allot, so be patient)

Address:

Robert D’Alessandro

Degussa Corporation

4301 Degussa Road

Theodore, AL 36590-0606

I will be glad to help in anyway I can !!

mailto:[email protected]


Closing Remarks

Thank you !!

Auburn University

Professor Chambers, Professor Eden, and Professor Roberts

Degussa Corporation

Professor Riemenschneider, Dr. Kemnade

Students in Chen 4450

Evaporative Concentration of a Thermally Sensitive Chemical IntroductionLecture ObjectivesEvaporative ConcentrationSigns of Inherent TroubleSigns of Inherent TroubleSigns of Inherent TroubleLaboratory Scale Data Laboratory Scale Data Laboratory Scale Data Adiabatic CalorimetersAdiabatic CalorimetersAdiabatic CalorimetersAdiabatic CalorimetersEvaporative ConcentrationTempered Versus Gassy SystemsTempered Versus Gassy SystemsExperimental SpecificationAdiabatic Calorimeter DataAdiabatic Calorimeter DataAdiabatic Calorimeter DataAdiabatic Calorimeter DataEvaporative ConcentrationEvaporative ConcentrationEvaporative ConcentrationEvaporative ConcentrationEvaporative ConcentrationEvaporative ConcentrationEvaporative ConcentrationWhy Does Two-Phase Venting OccurWhy Does Two-Phase Venting OccurEvaporative ConcentrationLarger Relief Devices Are Needed�When Two-Phase Flow OccursLarger Relief Devices Are Needed�When Two-Phase Flow OccursLarger Relief Devices Are Needed�When Two-Phase Flow OccursLarger Relief Devices Are Needed�When Two-Phase Flow OccursLarger Relief Devices Are Needed�When Two-Phase Flow OccursLarger Relief Devices Are Needed�When Two-Phase Flow OccursSimple Ideal Vent Sizing ResultsSimple Ideal Vent Sizing ResultsEvaporative ConcentrationVessel DisengagementEvaporative ConcentrationNew Concentrator DesignIs This Enough? Concentrator – Top ViewConcentrator – Bottom ViewConcentrator – Bottom ViewWhat Could Have �Been Done Differently? Alternate Schemes to Consider Connected EquipmentSummarySummaryClosing RemarksClosing Remarks

Documents

Evaporative Concentration of a Thermally Sensitive Chemicalchambro/Chen 4450 Lecture Presentation Rev B... · Factor 10,840 Bottom Line = Heat Loss Small Scale Has It Large Scale