Bio-soda pulping of lignocellulosic residues of palma rosa grass: …nopr.niscair.res.in/bitstream/123456789/7277/1/IJCT 17(1... · 2010. 1. 29. · Bio-pulping The LCR of C. martini

Indian Journal of Chemical Technology

Vol. 17, January 2010, pp. 60-70

Bio-soda pulping of lignocellulosic residues of palma rosa grass: An attempt

towards energy conversion

Dharm Dutt*, C H Tyagi, S Agnihotri, A Kumar & Siddarth

1

Department of Paper Technology, Indian Institute of Technology Roorkee, Saharanpur Campus, Saharanpur, India

1National Institute of Fashion Technology, Bangalore 560 071, India

Email: [email protected]

Received 8 May 2009; revised 14 September 2009

The lignocellulosic residues (LCR) of Cymbopogon martini after steam distillation had 13.6% lignin, 74.4%

holocellulose and 25.4% pentosan. Phanerochaete chrysosporium degraded 30.11% of lignin, 62.25% of pentosan and

18.60% of holocellulose of the original value of LCR of C. martini after 28 days at 40°C in solid-state culture with a higher

in vitro dry matter digestibility. The steam distillation and Phanerocheate chrysosporium treatment of LCR of C. martini

abated the mass transfer problem and facilitated the faster penetration of cooking liquor. The pulp yield was mitigated by

0.63% with insignificant decrease in kappa number and 0.81% with 1.32 units decrease in kappa number for bio-soda and

bio-soda-O2 pulping processes respectively when cooked at 11% alkali dose compared to soda pulping (active alkali14%)

with a saving of 3% cooking chemicals.

Keywords: Cymbopogon martini, Lignocellulosic residues, Phanerochaete chrysosporium, Biodelignification, Soda

pulping

World demand for paper and paperboard is expected

to grow from the current production of 300 million

tonnes to over 420 million tonnes by the year 2010

with an average growth rate of 2.8% per annum1. In

India, the annual current production gap is 0.7 million

tonne and will become 1.5 times greater during 2010-

15. In India, forest and woodlands occupy around

20%, agricultural land 50% and uncultivated, non-

agricultural and barren land 30% respectively of a

total land area of 328.8 million ha2. Many fast

growing annual and perennial plants have been

identified, cultivated and studied for their suitability

for pulp and paper manufacture3. Cymbopogon

martini (commonly known as palma rosa) is used to

extract essential oils of commercial importance by

steam distillation method and LCR of C. martini is

mainly used for land filling and a fraction is burnt to

generate steam for the stripping; the rest is left in the

fields where natural biodegradation occurs4. This

hitherto unexploited source of fibres from C. martini

was successfully utilized for the production of

bleachable grade pulp5. The openness of the pile, the

heterogeneity of the tissues and the vast exposed

surface area favour the growth and colonization of a

multitude of micro organisms6

in the waste material.

The present study has been undertaken to study the

bio-delignification of LCR of C. martini with

P. chrysosporium followed by soda delignification in

order to produce bleachable grade pulp.

Experimental Procedure

Raw materials collection

Cymbopogon martini was collected from Punjab

Agriculture University Jalandhar (India) at the start of

the rainy season. The freshly cut C. martini was hand-

chopped and sun-dried for 20 days and then palma

rosa oil was extracted by steam distillation in crude

iron direct-fired stills having false bottom, over which

the C. martini is charged. The LCR after extraction

were air dried and kept in ventilated polythene bags.

Morphology and proximate chemical analysis

In order to get more accurate results, three samples

from each stalk/branch were taken at 10% (base),

50% (middle) and 90% (top) of its height/length

respectively, an approach similar to that followed by

Dutt7. For fibre length determination, small slivers

were obtained and macerated with 10 mL of 67%

HNO3 and boiled in a water bath (100±2°C) for 10

min8. The slivers were then washed, placed in small

flasks with 50 mL distilled water and the fibre

bundles were separated into individual fibres using a

DUTT et al.: BIO-SODA PULPING OF LIGNOCELLULOSIC RESIDUE OF PALM ROSA GRASS

61

small mixer with a plastic end to avoid fibre breaking.

The macerated fibre suspension was finally placed on

a slide (standard, 7.5 × 2.5 cm) by means of a

medicine dropper9. For fibre diameter, lumen

diameter and cell wall thickness determination, cross-

sections were obtained from the same height/length as

mentioned above and were stained with 1:1 aniline

sulphate–glycerine mixture to enhance cell wall

visibility (cell walls retain a characteristic yellowish

colour). All fibre samples were viewed under a

calibrated microscope; a total of 25 randomly chosen

fibres were measured from each sample for a total of

75 fibre measurements from each stalk/branch. Three

derived values were also calculated using fibre

dimensions: slenderness ratio (fibre length/fibre

diameter), flexibility coefficient (lumen diameter/fibre

diameter) ×100 and Runkel ratio (2×fibre cell wall

thickness/lumen diameter)10,8

. The hand-chopped

culms of C. martini before and after steam distillation

were milled separately into powder in a laboratory

Wiley mill and a fraction passing through −48 mesh

size but retained on +80 mesh size was used for

analysis of water solubility (T 207 cm-99), 1% NaOH

solubility (T 212 om−98), alcohol-benzene solubility

(T 204 cm−97), holocellulose (T 249 cm−00), lignin

(T 222 om−02), ash (T 211 om−93) and pentosan

(T 223−cm-01) content as per Tappi Standard Test

methods: 2000.

Inoculum preparation

P. chrysosporium was isolated from decaying

wood and confirmed as xylanase producer when

cultured on xylan rich culture medium. The fungus

was sub-cultured on medium having 2% wheat bran

and 2% agar (w/v) without any nutrient salt at 40°C

for 4-6 days and maintained at 4°C until used.

Streptopenicilline (185 µg/mL) was aseptically added

to check any bacterial growth. The inoculum was

produced under submerged fermentation in a medium

having 2% wheat bran powder and 40 mL of nutrient

salt solution having KH2PO4, 1.5; NH4Cl, 4; MgSO4 0.5; KCl, 0.5 and yeast extract 1 g/L in distilled water

with trace elements solution (0.04 mL/L) having

FeSO4.7H2O, 200; ZnSO4.7H2O, 180 and

MnSO4.7H2O, 20 µg/L. Desired pH of the solution

was adjusted with 1.0 N NaOH /H2SO4. Two discs

of 8 mm diameter from 5 day old culture of

P. chrysosporium were aseptically inoculated in each

of the flasks. These flasks were incubated at 100 rpm

and 40°C and harvested after 8th day. The contents

were centrifuged at 15000 x g (Sigma centrifuge:

model 2K15) and 4°C and the filtrate was analyzed

for xylanases and CMCase activity11

, and lignin

peroxidase activity12

. In order to observe the growth

of fungus, the pellets were re-suspended in 10 mL of

1 M NaOH and boiled for 20 min12

. 1 mL of

homogeneous solution was taken and centrifuged at

10,000 x g for 2 min. The protein concentration of the

cleared supernatant was determined13

. Incubation

period, pH, and temperature with different carbon

sources (glucose/lactose) and complex nitrogen

sources (corn steep liquor/yeast extract) were

optimized to get maximum biomass production with

higher enzyme activity.

Bio-pulping

The LCR of C. martini was chopped into small

pieces of 2 to 2.5 cm long. Erlenmeyer flasks of

capacity 2 L each were filled with 50 g of LCR of

C. martini (oven dry weight basis). In each flask 100

mL of distilled water was added and autoclaved at 15

Pa for 15 min14

. Inoculum prepared under optimized

conditions was inoculated aseptically in each flask.

The flasks were incubated at 400C and were examined

everyday to check the fungal growth. The fungal

treated LCR of C. martini was analyzed for lignin

(T 222 om−02), pentosans (T 223−cm-01),

holocellulose (T 249 cm−00) and α-cellulose (T 203

cm-99) as per Tappi Standard Test Methods: 2000. Chemical pulping

The LCR of C. martini before and after treatment

with P. chrysosporium were cooked in WEVERK

rotary electrically heated digester of capacity 0.02 m3

by soda pulping process. The effect of AQ and O2 on

kappa number and screened pulp yield during soda

pulping was also studied. After completion of

cooking, the pulp was washed on a laboratory flat

stationary screen having 300 mesh wire bottom for

the removal of residual cooking chemicals. The pulp

was disintegrated and screened through WEVERK

vibratory flat screen with 0.15 mm slits and the

screened pulp was washed, pressed and crumbled.

The pulp was evaluated for kappa number (T 236 cm-

85), screened pulp yield and screening rejects as

per Tappi Standard Test Methods: 2000.

P. chrysosporium treated C. martini was cooked by

soda and soda-O2 cooking processes and comparisons

of screened pulp yield, screening rejects and kappa

number of LCR of C. martini with soda and alkali-O2 pulping processes was done.

INDIAN J. CHEM. TECHNOL., JANUARY 2010

62

Results and Discussion Morphological characteristics reveal that the

average fibre length of C. martini is 0.96 mm, while

fibre diameter, cell wall thickness, and lumen

diameter are 30.53, 6.42 and 20.58 µm, respectively,

which resemble to those of hard woods15

(Table 1).

The fibres are tapered at one end and cell cavity is

wide and nearly empty. The steam distillation process

reduces the hot water soluble from 15.90 to 0.1%

which indicates that palma rosa oil is leached out

along with extraneous components, such as inorganic

compounds, tannins, gums, sugars, colouring matters

and starches. The alcohol-benzene soluble, which is

5.4%, remains unaffected after steam distillation. The

reduction in 1% NaOH soluble from 37.9 to 27.5% is

attributed due to the leaching of water soluble

materials along with some low-molecular-weight

carbohydrates, like starches etc. C. martini contains

13.67% lignin, 25.38% pentosan and 74.51%

holocellulose. It indicates that C. martini produces

high pulp yield at milder cooking conditions. The

silica contents are slightly higher i.e. 2.2%.

Figure 1 reveals the impact of incubation period on

protein concentration and xylanase and peroxidase

activities of P. chrysosporium using 2% wheat bran,

NSS 10 mL, pH 6.5 and temperature 400C. On wheat

bran, the production of xylanase by P. chrysosporium

increases with increasing incubation period and the

maximum xylanase activity of 21.79 IU/mL is

observed on 8th day of incubation while peroxidase

activity (0.32 IU/mL) increases with increasing the

incubation period up to 14th day of incubation

(Fig. 1A). It is because the ligninolytic activity

induces in the secondary phase of growth when the

culture medium is deficient of carbon, sulphur and

Fig. 1A−Optimzation of incubation period

Table 1―Morphological characteristics and chemical

composition of C. martini

Morphological characteristics

Parameters Test values

Fibre length (L) (mm) 0.96±0.07

Fibre width (D) (µm) 30.53± 2.6

Lumen diameter (d) (µm) 20.58±2.9

Cell wall thickness (w) (µm) 6.42± 0.6

Flexibility coefficient, [(d/D) x 100] 67.4

Slenderness ratio (L/D) 31.4

Runkel ratio (2 w/d) 0.6

Chemical composition

Before steam

distillation

After steam

distillation

Cold water soluble (%) 12.2±0.1 —

Hot water soluble (%) 15.9±.08 0.1±0.02

Alcohol-benzene soluble (%) 5.4±.06 5.3±.003

1% NaOH soluble (%) 37.9±.05 27.5±.004

Lignin (%) 13.67±.07 13.5±0.06

Pentosan (%) 25.4±.09 25.38±0.07

Holocellulose (%) 74.51±0.1 74.4±0.02

Ash (%) 4.5±0.04 4.4±0.03

Silica (%) 2.2±0.02 2.2±0.01 ±refers to standard deviation


63

nitrogen16

. Both protein biomass (0.303 mg/mL) as

well as xylanase production start to decline after 12th

day of incubation. It suggests that the enzyme

production is dependent on biomass but only during

exponential phase of growth of fungi. On onset of

death phase, the protein biomass as well as the

enzyme activity decreases17

. Thus, their harvesting

time must be correlated to their production25

.

Metabolic enzymes like, proteases and

transglycosidases might also affect xylanase yield26

.

Figure 1B reveals that variation in pH from 5.0-7.0,

and keeping other factors same as described above,

enhances the enzyme production and the optimum

enzyme activity of 24.12 IU/mL is observed at

pH 6.5. The maximum protein concentration of

0.38 mg/mL and peroxidase activity 0.33 IU/mL is

observed at pH 6.0.The peroxidase activity is

observed higher in acidic than alkaline pH. However,

the mycelial biomass is slightly less at pH 7.5, but the

xylanase activity is quite comparable to the optimum

value. There are two pH optima, one at 6.5 and other

at 7.5. It is known that pH dependent unavailability of

inorganic elements affects the production of

enzyme18,19

. It may also be possible that these may be

multiple isoforms of the enzyme, which are produced

at different pH optima with different activities. The

pH exerts a regulatory effect on production of both

primary and secondary metabolites20

. Any enzyme

mediated reaction is affected by culture pH which

might cause changes in productivity. Structures like,

membranes in contact with external environment, can

also undergo chemical changes in response to pH.

Microorganisms may need to adapt their function to

cope up with pH change. If this change is too abrupt,

response of microbes might lag behind or overshoot.

The pH may also determine solubility of some media

components. Thus, pH change might cause some

micronutrients to precipitate and impossible to

assimilate21

.

At 25°C, P. chrysosporium yields the lowest

enzyme activity, which increases with increasing

temperature up to 400C and thereafter, it decreases to

half at 50°C (Fig. 2). It may be possible due to lower

transport of substrate across the cells at lower

temperature causing lower yield of the product. At

higher temperature, maintenance energy requirement

of cellular growth is high due to thermal denaturation

of enzymes of the metabolic pathway resulting in

lower production of the metabolites22

. Optimum

xylanase activity of P. chrysosporium (23.14 IU/mL

at 40°C) suggests that the fungus is slightly

thermophilic and of commercial use because the

industrialists prefer thermophilic microorganisms for

the production of the biocatalysts as the cost of

maintenance at higher temperature is cheaper than

that at lower temperature. The maximum supernatant

protein concentration at 40°C is 0.38 mg/mL and

peroxidase activity is 0.28 IU/mL.

Fig. 1B−Optimzation of initial pH


64

The effect of different carbon sources i.e. glucose

and lactose on protein concentration and xylanase and

peroxidase activities of P. chrysosporium using 2%

wheat bran, 10 mL NSS, 15 mL yeast extract, pH 6.5

and incubation period and temperature 8 days and

40°C respectively has been studied. Glucose is found

to be the better additional carbon source for biomass

production (Fig. 3A). The possible explanation is that

xylan is a complex substrate and addition of glucose

as a carbon source may facilitate the initial growth of

the fungus, which may then utilize bulk of wheat bran

easily. In case of lactose (Fig. 3B), enzyme activity

Fig. 2−Optimization of incubation temperature

Fig. 3 A−Effect of glucose concentration on protein concentartion, xylanase and peroxidase activity


65

and mycelial biomass is lesser compared to glucose. It

suggests that the fungus preferably consume the

simplest carbon source (glucose) than lactose. Lactose

is reported a poor source of carbon for the growth of

fungi23

. In both the cases, additional supply of

glucose/lactose as carbon source shows adverse effect

on the production of xylanases. The concentration of

glucose (>1.0 g/L) acts as a repressor23,24

. Xylanase

repression in the presence of easily metabolizable

carbon sources in the growth medium, suggested that

enzyme synthesis is controlled by transition state

regulators and catabolite repression25

. Xylanase

induction, in general, is a complex phenomenon and

the level of response to an inducer varies with the

organisms26

.

Corn steep liquor is better complex nitrogen source

(29.53 IU/mL) than yeast extract (22.49 IU/mL) for

mycelial biomass and xylanase production under

submerged fermentation condition (Fig 4 A, B). The

additional supply of corn steep liquor/yeast extract in

the medium shows positive effect on xylanase

production and mycelial biomass but peroxidase

activity decreases in presence of additional supply of

nitrogen sources. It is also reported by several

Fig. 3 B−Effect of lactose concentration on protein concentartion, xylanase and peroxidase activity

Fig. 4A−Effect of yeast extract concentration on protein concentartion, xylanase and peroxidase activity


66

researchers that, nitrogen compounds act as a

repressor of ligninolytic activity27

. It suggests that

corn steep liquor/yeast extract is consumed by fungus

in limited amount and is probably utilized only in

early stage of growth because in lag phase, fungus

synthesizes its protein and nucleic acid components

for growth and development28,23,24

. Bakri et al.23

reported that yeast extract was the best source for

xylanase production by Penicillium canescens while

Technapun et al.29

reported that yeast extract had

negative effect on xylanase production in

Streptomyces species. Thus, the present investigation

supports the earlier observations that additional

supply of organic nitrogen enhances the enzyme

production to certain extent. Figure 5A reveals that initially fungus attacks the

pentosan followed by holocellulose and α-celluloses

respectively, and lignin is utilized by the fungus only

in final stage of bio-pulping on 18th day of incubation.

As lignin is not degraded due to primary growth of P.

chrysosporium, so it does not induce ligninolytic

activity5.

Fig. 4B−Effect of corn steep liquor concentration on protein concentartion, xylanase and peroxidase activity

Fig. 5A−Effect of incubation period on bio-chemical composition of C. martini after treatment with P. chrysosporium


67

Figure 5B reveals that pentosan, holocellulose and

α-celluloses degrade fast compared to lignin beyond

incubation temperature of 40°C. Therefore, 40°C may

be considered as an optimum temperature for

biopulping of C. martini with P. chrysosporium. The

favourable tropical conditions, the openness of the

pile, the heterogeneity of the tissues and the vast

exposed surface area favour the growth and

colonization of the fungus on the distilled waste of

C. martini. Therefore, it requires less incubation

period compared to softwood as well as for

hardwood30

. In 28 days at 40°C, P. chrysosporium

degrades 30.11% of lignin, 62.25% of pentosan and

18.60% of holocellulose from LCR of C. martini;tThe

ranges of experimental weight loss observed for

Cymbopogon citratus, 8-42% and for Cymbopogon

winterianus are 1.6 to 37%31

. Antai and Crawford30

have shown, for instance, that in 10 weeks at 28°C,

C. versicolor degraded more dry matter, 63.8% in

grasses than in hardwoods or softwoods (about 40%).

Somewhat higher weight losses have been reported

for cereal straws and some specific white-rot32-35

.

Table 2 reveals the experimental conditions and

results of soda pulping of LCR of C. martini at

different alkali doses i.e. 10 to 18% (as Na2O) while

keeping other conditions constant as mentioned. The

results indicate that the screened pulp yield increases

with increasing alkali dose from 10 to 14% when

C. martini is delignified at H-Factor 553.21. Further,

on increasing alkali doses screened pulp yield

decreases from 44.73 to 42.8%, whereas, kappa

number drops from 22.12 to 20.6 and thereafter

insignificant decrease is noticed. In the initial stage of

cooking rapid solublization of bulk of lignin occurs

and beyond an alkali dose of 14% slow solublization

of residual lignin occurs. The bulk delignification

corresponds to the removal of easily assessable lignin

present in the middle lamella and residual lignin

corresponds to the removal of lignin present in the

primary wall, secondary wall layers and inter-

connection cavities. The delignification of wood in

alkaline pulping is also associated with the

solublization of significant amount of hemicelluloses36

.

The results of effect of temperature on pulp yield and

kappa number during soda pulping indicate that the

screened pulp yield increases from 41.98 to 44.73% up

to H- factor 553.21 and kappa number drops from

28.42 to 22.12. Further, on increasing H-factor from

1212.24 to 3033.98 screened pulp yield drops sharply

while kappa number decreases slowly. In other words,

at the transition point, lower pulp lignin contents were

obtained at 150°C. Beyond a temperature of 150°C,

degradation of carbohydrates contents occurs due to

peeling reactions37,38

. Therefore, it is not sensible to

cook C. martini beyond a temperature of 150°C. Table

2 also reveals the effect of cooking time on pulp yield

and kappa number during soda pulping of LCR of C.

martini while keeping other variables constant as

mentioned. The results indicate that the screened pulp

yield increases from 40.56 to 44.73% up to H- factor

553.21 and kappa number drops from 32.45 to 22.12.

Beyond that screened pulp yield drops sharply while

kappa number remains almost constant. The lignin

content associated with middle lamella decreases

Fig. 5B−Effect of incubation temperature on bio-chemical composition of C. martini after treatment with P. chrysosporium


68

sharply up to a reaction time of 3 h. It means that the

bulk delignification phase is over up to this transition

point and it is not economical to continue pulping

reaction beyond this particular reaction time. The bulk

delignification phase is converted into residual

delignification beyond a reaction time of 3 h at 150°C.

Table 3 shows the effect of AQ and O2 during soda

pulping of LCR of C. martini. The addition of 0.1%

AQ at optimum cooking condition of soda-AQ

process reduces kappa number by 1.12 units and

increases pulp yield by 0.72%. Similarly, an O2

pressure of 5 kg/cm2 improves pulp yield by 1.07%

and mitigates kappa number by 1.65 units compared

to soda pulping process. The lignin of C. martini is

much more susceptible to the action of oxygen and

results a pulp with higher delignification. There is no

diffusion problem of dissolved oxygen because of its

more open and loose structure and low specific

gravity39

.

Figure 6 shows a comparison between soda, bio-

soda, soda-O2 and bio-soda-O2 pulping processes. The

pulp yield of bio-soda pulp is slightly less (0.63%)

due to removal of xylan when cooked at the same

kappa number as that of soda pulp with a chemical

savings of 3%. The bio-soda-O2 pulp shows a

decrease in pulp yield by 0.81% and kappa number

reduction by 1.32 units with a chemical savings of 3%

compared to soda-O2 pulp.

Table 2―Effect of NaOH, cooking temperature and cooking time on pulp characteristics of LCR of C. martini during soda pulping

aEffect of NaOH dose (%) (as Na2O) Parameters

12 14 16 18

Screened pulp yield (%) 43.4±0.3 44.7±0.2 43.6±0.3 42.8±0.3

Screening rejects (%) 2.8±0.10 1.9±0.15 0.6±0.01 0.3±0.01

Unscreened pulp yield (%) 46.2±0.4 46.7±0.2 44.3±0.2 43.2±0.2

Kappa number 26.2±0.2 22.1±0.3 21.5±0.3 20.6±0.4 bEffect of cooking temperature (0C)

140 150 160 170

Whole cycle H-factor 223.42 553.21 1212.24 3033.98


Screening Rejects (%) 3.78±0.15 1.98±0.10 0.98±0.01 0.50±0.01


Kappa number 28.42±0.1 22.12±0.2 21.34±0.3 18.72±0.1 cEffect of cooking time (h)

2.0 2.5 3.0 3.5

Whole cycle H-factor 327.96 470.54 553.21 635.69


Screening rejects (%) 4.78±0.41 2.10±0.10 1.98±0.02 0.62±0.01


Kappa number 32.45±0.10 26.30±0.10 22.12±0.10 19.12±0.15 ±refers to standard deviation.

aLiquor to raw material ratio 5:1, temperature raising time 1.5 h, max cooking

temperature 1500C, temperature keeping time 3.0 h and H-factor 553.2

bLiquor to raw material ratio 5:1, NaOH charged 14% (as Na2O), temperature raising time 1.5 h and temperature keeping time 3.0 h

cLiquor to raw material ratio 5:1, NaOH charged 14% (as Na2O), temperature raising time 1.5 h and max cooking temperature 1500C

Table 3―Effect of AQ and O2 pressure on pulp characteristics of

LCR of C. martini during soda pulping

AQ dose (%) (o d wood basis) Parameters

00 0.05 0.10 0.20

Screened pulp

yield (%)

44.73±0.1 45.05±0.1 45.45±0.2 45.12±0.3

Screening rejects

(%)

1.98±0.01 1.07±0.02 1.02±0.01 0.40±.01

Unscreened pulp

yield (%)

46.71±0.2 46.12±0.3 46.47±0.4 45.52±0.3

Kappa number 22.12±0.1 21.50±0.1 21.00±0.2 18.45±0.2

O2 pressure ( kgf/cm2)

00 05 08 10

Screened pulp

yield (%)

44.73±0.2 45.80±0.3 45.30±0.1 44.23±0.1

Screening rejects

(%)

1.98±0.03 1.32±0.01 0.98±0.01 0.50±0.01

Unscreened pulp

yield (%)

46.71±0.2 46.12±.2 46.28±1 44.73±0.2

Kappa number 22.12±0.1 20.47±0.1 19.23±0.2 18.50±0.1

±refers to standard deviation.

Cooking conditions: Liquor to raw material ratio 5:1, temperature

raising time 1.5 h, max cooking temperature 1500C, temperature

keeping time 3.0 h and H-factor 553.2


69

Conclusions

Both steam distillation and P. chrysosporium

treatment makes LCR of C. martini suitable for

chemical pulping by abating the mass transfer

problem of O2 and facilitates the faster penetration of

cooking liquor. Thus, LCR left after steam distillation

is renewable, alternative and hitherto unexploited

source of fibers for paper industry. After 28 days at

40°C, P. chrysosporium degrades lignin, pentosan and

holocellulose by 30.11, 62.25 and 18.60%

respectively of the original value of C. martini. The

optimum pulping conditions for soda pulping are:

maximum cooking time and temperature 3 h and

150°C respectively, alkali dose 14 % (as Na2O) and

liquor to LCR ratio 5:1. The addition of 0.1% AQ

improves pulp yield by 0.72% and reduces kappa

number by 1.12 units and an O2 pressure of 5 kg/cm2

with AQ improves pulp yield by 1.07% and reduces

kappa number by 1.65 units compared to soda pulp.

The bio-soda and bio-soda-O2 pulping processes save

3% alkali compared to soda pulping, when LCR of C.

martini was cooked to get the same kappa number as

that of soda pulp. Bio-soda and bio-soda-O2 processes

mitigate the pulp yield by 0.63 and 0.81% but kappa

number reduction is 1.32 units for bio-soda-O2

process.

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Fig. 6−Comparison between soda, alkali-O2, bio-soda and bio-soda-O2 pulping


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Bio-soda pulping of lignocellulosic residues of palma rosa grass: …nopr.niscair.res.in/bitstream/123456789/7277/1/IJCT 17(1... · 2010. 1. 29. · Bio-pulping The LCR of C. martini