PNNL-18401 

Prepared for the U.S. Department of Energy 

under Contract DE-AC05-76RL01830 

Preliminary Economics for the 

Production of Pyrolysis Oil from 

Lignin in a Cellulosic Ethanol 

Biorefinery 

SB Jones 

Y Zhu 

April 2009 

PNNL-18401

Preliminary Economics for the 

Production of Pyrolysis Oil from 

Lignin in a Cellulosic Ethanol 

Biorefinery 

SB Jones 

Y Zhu 

April 2009 

Prepared for 

the U.S. Department of Energy 

under Contract DE-AC05-76RL01830 

Pacific Northwest National Laboratory 

Richland, Washington 99352 
Abstract 

Cellulosic ethanol biorefinery economics can be potentially improved by converting by-product lignin 

into high valued products. Cellulosic biomass is composed mainly of cellulose, hemicellulose and lignin. 

In a cellulosic ethanol biorefinery, cellulose and hemicellullose are converted to ethanol via fermentation. 

The raw lignin portion is the partially dewatered stream that is separated from the product ethanol and 

contains lignin, unconverted feed and other by-products. It can be burned as fuel for the plant or can be 

diverted into higher-value products. One such higher-valued product is pyrolysis oil, a fuel that can be 

further upgraded into motor gasoline fuels. While pyrolysis of pure lignin is not a good source of 

pyrolysis liquids, raw lignin containing unconverted feed and by-products may have potential as a 

feedstock. This report considers only the production of the pyrolysis oil and does not estimate the cost of 

upgrading that oil into synthetic crude oil or finished gasoline and diesel. 

A techno-economic analysis for the production of pyrolysis oil from raw lignin was conducted. 

comparing two cellulosic ethanol fermentation based biorefineries. The base case is the NREL 2002 

cellulosic ethanol design report case where 2000 MTPD of corn stover is fermented to ethanol (NREL 

2002). In the base case, lignin is separated from the ethanol product, dewatered, and burned to produce 

steam and power. The alternate case considered in this report dries the lignin, and then uses fast pyrolysis 

to generate a bio-oil product. Steam and power are generated in this alternate case by burning some of the 

corn stover feed, rather than fermenting it. This reduces the annual ethanol production rate from 69 to 54 

million gallons/year. Assuming a pyrolysis oil value similar to Btu-adjusted residual oil, the estimated 

ethanol selling price ranges from $1.40 to $1.48 (2007 $) depending upon the yield of pyrolysis oil. This 

is considerably above the target minimum ethanol selling price of $1.33 for the 2012 goal case process as 

reported in the 2007 State of Technology Model (NREL 2008). Hence, pyrolysis oil does not appear to 

be an economically attractive product in this scenario. Further research regarding fast pyrolysis of raw 

lignin from a cellulosic plant as an end product is not recommended. Other processes, such as highpressure liquefaction or wet gasification, and higher value products, such as gasoline and diesel from fast 

pyrolysis oil should be considered in future studies. 

iii 
iv 

Acknowledgment 

The authors acknowledge the DOE EERE Office of Biomass Programs for funding this work and the 

modeling work performed by the National Renewable Energy Laboratory (NREL), which is publicly 

available and serves as the basis for cellulose to ethanol portion of the models. 
Contents 

Abstract............................................................................................................................................. iii

Acknowledgment ...............................................................................................................................iv

1.0 Introduction ................................................................................................................................1

2.0 Process Design Basis..................................................................................................................2

3.0 Process Flow Assumptions.........................................................................................................4

4.0 Economic Assumptions ..............................................................................................................5

5.0 Analysis and Results...................................................................................................................6

6.0 Conclusions and Recommendations...........................................................................................9

7.0 References ................................................................................................................................10

8.0 Appendix: Heat and Material Balance for the High Char Case................................................11

Figures 

Figure 1. Process Flowsheet for a Cellulosic Ethanol Plant Co-Producing Pyrolysis Oil .................2

Figure 2 Process Flowsheet for the Fast Pyrolysis System................................................................3

Figure 3 Process Flowsheet for the High Char Case........................................................................12

Tables 

Table 1. Process Assumption Summary for Fast Pyrolysis ...............................................................4

Table 2 Economic Assumptions ........................................................................................................5

Table 3 Raw Material Consumption and By-Product Production .....................................................7

Table 4 Capital and Operating Costs.................................................................................................8

Table 5 Heat and Material Balance for the High Char Case............................................................16

v 
1.0 Introduction 

The “Top Value-Added Chemicals from Biomass” report volumes I and II outline potential renewable 

fuels and chemicals from biomass (EERE 2004, PNNL 2007). This techno-economic analysis is a 

continuation of the detailed techno-economic analysis of specific products identified in these two 

volumes, as described in DOE project 4.5.1.2-10779. The objective of this task is to support the efforts of 

the Department of Energy’s Office of Energy Efficiency and Renewable Energy, Office of the Biomass 

Program (EERE OBP) by conducting process and economic modeling of products from biomass sources. 

Specifically, this report analyzes the cost of producing pyrolysis oil from cellulosic-ethanol-derived raw 

lignin. Cellulosic ethanol biorefinery economics have the potential to be improved by converting 

byproduct lignin to make higher valued products than boiler fuel. 

Cellulosic biomass is composed mainly of cellulose, hemicellulose and lignin. In a cellulosic ethanol 

plant, cellulose and hemicellullose are converted to ethanol via fermentation. The raw lignin portion is 

the partially dewatered stream containing lignin, unconverted feed and by-products. It can be burned as 

fuel for the plant or can be diverted into higher-value products. One such higher-valued product is 

pyrolysis oil, a fuel that can be further upgraded into motor gasoline fuels. While pyrolysis of pure lignin 

is not a good source of pyrolysis liquids, raw lignin containing unconverted feed and by-products may 

have potential as a feedstock. This report considers only the production of the pyrolysis oil and does not 

estimate the cost of upgrading that oil into synthetic crude oil or finished gasoline and diesel. 

1 
2.0 Process Design Basis 

The process flowsheet is based on the cellulosic-ethanol design case of the National Renewable 

Energy Laboratory (NREL 2002). A simplified block diagram of this process is shown in Figure 1. 

Feed Handling

Pretreatment 

and 

Conditioning

Saccharification

and

Fermentation

Ethanol

Distillation

and Dehydration

Wastewater

Treatment

Burner/Boiler

Turbogenerator

Corn Stover

Ethanol

Recycle Water

to Plant Steam to Plant

Solid Waste

Electricity

Evaporation and 

Solids Separation

Still Solids

Evap. Syrup

Drying and 

Fast Pyrolysis Pyrolysis Oil

Figure 1. Process Flowsheet for a Cellulosic Ethanol Plant Co-Producing Pyrolysis Oil 

Corn stover is washed and shredded. Pre-treatment with steam and dilute sulfuric acid releases the 

five- and six-carbon sugars in the hemicellulose. The pretreated feed is neutralized, and then sent to 

enzymatic saccharification to release the six-carbon sugars in the cellulose. This is followed by 

fermentation of the sugars to ethanol. The dilute ethanol stream is distilled to separate ethanol from the 

solids and the majority of the water. The ethanol is then dehydrated to 99% ethanol. The distillationbottoms stream is sent to a triple-effect evaporator to concentrate the solids. Two solid streams are 

generated: the mainly lignin portion (“still solids”) from the first evaporator and the evaporator syrup 

from the third evaporator. In the base NREL process, both solid streams are sent to the boiler to raise 

steam for power generation. Also, in the NREL case, all power for the plant is generated onsite and any 

excess electricity is sold back to the grid. The details of this part of the process can be found in the NREL 

cellulosic ethanol design report (NREL 2002). 

In the process discussed in this report, the lignin-rich “still solids” are sent to the fast-pyrolysis 

portion of the plant. The evaporator syrup supplies insufficient fuel to generate power for the entire plant; 

therefore, a portion of the corn stover feedstock is diverted to the boiler. The total feed rate of corn stover 

is maintained at 2000 dry mtpd. This size of plant is consistent with a delivered-feedstock cost of $46/dry 

2 
3 

short ton (NREL 2008). At this price, the feedstock is assumed to “reactor-throat ready.” That is, it has 

already been washed and size-reduced. 

Figure 2 shows the equipment flow diagram for the fast-pyrolysis system. Wet lignin containing 

solids from the first evaporator are dried from 50% moisture to 8% moisture using hot exhaust gases. The 

fast- pyrolysis reactor system is assumed to be a circulating fluidized-bed reactor using hot sand to 

provide the heat for the endothermic pyrolysis reactions. The reactor residence time is less than 1 second. 

During this time, the lignin and other solids in the feed break down into non-condensable gases, water, 

char and organic vapor. The reactor effluent enters a cyclone to separate sand, char, and unconverted 

solids from the vapor product. The vapor product is then rapidly quenched with cooled pyrolysis oil 

product to prevent further reaction. A portion of the non-condensable gases is recycled to the pyrolysis 

reactor to help fluidize the bed. The remainder is burnt with the char to provide reheat to the circulating 

sand. Hot exhaust flue gases from the sand heater are sent to the dryer to dry the incoming wet feed. 

Pre-treatment

(drying, 

grinding)

CFB 

Pyrolysis

(495°C)

Cyclone Quench

Filter

Combustor

Solids

Bio-Oil

Sand/Char

Cool Bio-Oil

Heated 

Sand

NonVapor Condensables

Liquid & 

Residual

Solids

Fluidizing Gas

Wet 

Lignin

Exhaust

Hot 

Combustor

Exhaust

Gas to Combustor

Figure 2 Process Flowsheet for the Fast Pyrolysis System 

 

 Three cases were modeled: the base case, the base pyrolysis case and a pyrolysis case with high char 

formation. The base case is the same as the state-of-technology case (NREL 2008). Here the plant 

produces only ethanol and by-product electricity. Since no experimental data exist for a lignin feed 

stream derived from a cellulosic ethanol plant, two cases pyrolysis cases were analyzed. One with high 

char yield and one with low char yield. In the high char case, the excess heat not needed by the dryer was 

recuperated into steam for use in the plant. 
3.0 Process Flow Assumptions 

The flowsheet was modeled using the CHEMCAD process flow software. The simulation 

assumptions for all parts of the process except the fast-pyrolysis unit are those given in the NREL design 

report (NREL 2002). The fast-pyrolysis process is similar to that described in the PNNL Pyrolysis design 

report (PNNL 2008). Table 1 lists the assumptions and sources for the fast-pyrolysis reactor. No data 

were found for fast pyrolysis of raw lignin from a cellulosic ethanol plant. Thus the operating conditions 

were estimated from two extremes: sorghum bagasse containing approximately 25% lignin and milled 

wood lignin. The model feed on a dry basis is approximately 60% lignin with the remainder being ash 

and unconverted feed. Pyrolysis of whole lignocellulosic feedstocks is well documented and results in 

high conversions and yields as high as 75% (wet) of pyrolysis oil (IEA 2007). At the other extreme is 

pure lignin. Pyrolysis of pure lignin feedstock is not easily done. Ferdous et. al. reports the pyrolysis of 

Alcell lignin at 520°C to have a 50% conversion with half the product being char and the remainder 

equally split between gas and liquid products (Ferdous 2001) . 

Table 1. Process Assumption Summary for Fast Pyrolysis 

Process Area Process 

Parameter 

Low Char 

Case 

High Char 

Case 

Literature 

Values 

Source 

Lignin stream Water 45% 45% 

Lignin 33% 33% 

Ash 10% 10% 

Bio-solids and 

by-products 

12% 12% 

Pyrolysis feed dryer % Moisture to 

pyrolysis reactor 

8% 8% 8% PNNL 2008 

Fast pyrolysis 

reactor 

Temperature 490oC 499oC 510oC Piskorz 1998(a)

Gas yield 13% 19% 12.40% Piskorz 1998(a)

Char yield 26% 44% 14.20% Piskorz 1998(a)

Water yield 8% 6% 11.20% Piskorz 1998(a)

Pyrolysis oil 

yield 

53% 31% 62.20% Piskorz 1998(a)

Pyrolysis oil C 66% 54% 55% Nunn 1985(b) 

Wet basis H 9% 9% 5% Nunn 1985(b)

O 25% 37% 31% Nunn 1985(b)

(a) Sorghum bagasse 

(b) milled wood lignin 

4
4.0 Economic Assumptions 

The capital and operating costs are calculated in a Microsoft Excel spreadsheet using results from the 

CHEMCAD process simulation. A simple return-on-investment calculation is used to estimate the 

product selling price. All capital costs are reported in year-2007 dollars to be consistent with the current 

state of technology values (NREL 2008). The total capital investment is factored from installed equipment costs (NREL 2002). The operating labor was determined by assuming one operator per shift per 

major processing area. Most labor categories (control lab, supervisory, administrative) are factored from 

the operating labor. Maintenance materials, labor and local taxes and insurance are factored from the 

capital investment. These data and their sources are summarized in Table 2. 

Table 2 Economic Assumptions 

Value Units or Basis Reference 

 Stream factor 96% NREL 2002 

 Construction Overnight(a)

 Plant life 20 Years NREL 2002 

 Depreciation 20 Years straight line 

Rate of return on capital 10% 

Labor 

 Operating labor 42 $/hr Burdened with 10% shift 

overlap 

SRI PEP 2007 

 Maintenance labor 1.0% Of total installed capital (TIC) SRI PEP 2007 

 Control lab labor 20% Of operating labor SRI PEP 2007 

 Operator per shift per major unit 1 

Materials 

 Maintenance 1.0% Of TIC SRI PEP 2007 

 Operating supplies 10% Of operating labor SRI PEP 2007 

 Overhead 80% Of total labor SRI PEP 2007 

 Local taxes and insurance 2% Of total fixed capital SRI PEP 2007 

 General and administrative 5% Of product value SRI PEP 2007 

(a) “Overnight construction” means no costs are associated with the construction phase, that is, 

 construction is as if it happens “overnight.” 

5
5.0 Analysis and Results 

Table 3 summarizes the raw material consumption and by-product electricity generation for each 

case. Three cases are considered: 

 Base Case: the lignin is burned in the boiler to produce plant steam and power, 

 Fast Pyrolysis Low Char Case: the lignin is dried and then fast pyrolyzed with a minimum of 

char formation, some corn stover is diverted from fermentation for use as boiler feed, and 

 Fast Pyrolysis High Char Case: the lignin is dried and then fast pyrolyzed with a maximum of 

char formation and some corn stover is diverted from fermentation for use as boiler feed. 

The high-char-formation case was modeled to account for uncertainty in the pyrolysis yields. No data 

are available specifically for fast-pyrolysis yields from cellulosic ethanol lignin. Thus a worst case was 

modeled where the process yields more char than oil. 

Chemical consumption per gallon of ethanol produced as shown in Table 3 is nearly the same for 

each case. However, the costs associated with each item are increased in the high and low char cases due 

to the reduced ethanol yield as compared with the base case. The fast pyrolysis oil produced in the high 

and low char cases are taken as an operating credit. It is assumed that the pyrolysis oil has the same value 

as residual oil with the price adjusted proportionately to reflect the difference in heating values of the two 

oils. All three cases generate power slightly in excess of that needed by the plant. Credit is taken for the 

excess power under the assumption that it can be sold to the grid. 

Table 4 summarizes the yields and capital and operating costs for each case. Note that each case 

assumes a feed rate of 2000 MTPD dry stover to the plant gate. In the base case, most of the cellulosic 

and hemicellulosic material is fermented to ethanol. The lignin and any unconverted sugars are sent to 

the boiler to generate steam and power. When lignin is diverted from the boiler to a fast pyrolysis unit, 

another fuel must be substituted in the boiler. While additional stover above 2000 mtpd could have been 

brought into the plant to serve as boiler fuel, the price will likely be higher than the $46/ton assumed here. 

This is due to the additional transportation costs needed to widen the biomass collection area in order to 

increase the federate to the plant. Thus, in the fast pyrolysis scenario, a small portion of the corn stover 

was diverted from fermentation to the boiler. This reduces the available amount of cellulose and 

hemicellulose in the fermentation step, resulting in a 22% reduction in ethanol yield for the pyrolysis 

case. Routing part of the feed to the boiler also affects the capital costs. The capital cost of adding a 

pyrolysis unit is more than offset by the reduction in capital for the pretreatment, fermentation and 

product-separation portions of the plant. However, the value of pyrolysis oil is not sufficient to justify the 

reduction in ethanol yield, as can be seen by the estimated selling price. 

It appears that producing pyrolysis oil from lignin will likely increase the selling price of ethanol by 

approximately 7-15 cents/gallon.

6
Table 3 Raw Material Consumption and By-Product Production 

Base Case 

No Pyrolysis Oil 

Pyrolysis with Low 

Char Formation Case 

Pyrolysis with High 

Char Formation Case 

Unit Cost 

Consumption 

/gal EtOH ¢/gal 

Consumption 

/gal EtOH ¢/gal 

Consumption 

/gal EtOH ¢/gal 

Raw Materials(a)

Corn stover 46 $/dry 

ton 

0.011 st 51.20 0.014 st 66.11 0.014 st 66.11 

Clarifier polymer 1.299 $/lb 0.000 lb 0.00 0.010 lb 1.23 0.010 lb 1.23 

Sulfuric acid 0.013 $/lb 0.895 lb 1.16 0.895 lb 1.11 0.895 lb 1.11 

Lime 0.036 $/lb 0.652 lb 2.36 0.652 lb 2.27 0.652 lb 2.27 

Corn steep liquor 0.084 $/lb 0.351 lb 2.94 0.351 lb 2.83 0.351 lb 2.83 

Purchased cellulase 0.057 $/lb 1.825 lb 10.48 1.825 lb 10.08 1.825 lb 10.08 

Diammonium 

phosphate 

0.073 $/lb 0.044 lb 0.32 0.044 lb 0.31 0.044 lb 0.31 

Propane 0.002 $/lb 0.005 lb 0.00 0.005 lb 0.00 0.005 lb 0.00 

Make-up water 0.000 $/lb 46.187 lb 0.56 46.187 lb 0.54 46.187 lb 0.54 

BFW Chemicals 1.403 $/lb 0.000 lb 0.04 0.000 lb 0.04 0.000 lb 0.04 

Cooling water 

chemicals 

1.061 $/lb 0.001 lb 0.06 0.001 lb 0.06 0.001 lb 0.06 

WWT Chemicals 0.164 $/lb 0.013 lb 0.22 0.013 lb 0.21 0.013 lb 0.21 

WWT Polymer 2.652 $/lb 0.000 lb 0.01 0.000 lb 0.01 0.000 lb 0.01 

Ash disposal 0.009 $/lb 1.214 lb 1.14 1.214 lb 1.14 1.214 lb 1.14 

Gypsum disposal 0.009 $/lb 1.966 lb 1.84 1.966 lb 1.84 1.966 lb 1.84 

Gross Raw Material 

Cost 

72.32 87.76 87.76 

By-product 

credits:(b) 

Pyrolysis oil 120 ¢/gal 0.00 gal 0.00 -0.20 gal -29.22 -0.08 gal -20.19 

Utilities 

Electricity(c) 4 ¢/kwh -2.12 kwh -8.49 -1.48 kwh -5.20 -2.54 kwh -6.41 

(a) Unit costs from NREL design case escalated to 2007 with the design-case worksheet (NREL 2002). 

(b) Pyrolysis oil value based on the 2007 EIA price for residual oil and adjusted for BTU content. 

(c) Electricity costs from NREL design case escalated to 2007 with the design-case worksheet (NREL 2002). 

The capital and operating costs are shown in Table 4. 

7
Table 4 Capital and Operating Costs 

Base Case 

Low Char 

Formation 

Case 

High Char 

Formation 

Case 

Ethanol, million gal/yr 69 54 54 

MTPD dry stover 2000 2000 2000 

Investment, U.S. $ million 

Total installed capital 135 127 127 

Total indirect costs 85 80 80 

Total fixed capital 220 207 207 

Production costs, U.S. $/gal 

Raw materials 0.72 0.88 0.88 

By-products 0.00 -0.29 -0.20 

Utilities -0.08 -0.05 -0.06 

 

Variable costs, U.S. $/gal 0.64 0.53 0.61 

 

Maintenance materials 0.04 0.05 0.05 

Operating supplies 0.00 0.00 0.00 

Operating labor 0.03 0.04 0.04 

Maintenance labor 0.02 0.02 0.02 

Control laboratory 0.01 0.01 0.01 

 

Total direct costs, U.S. $/gal 0.73 0.66 0.74 

 

Plant overhead 0.03 0.04 0.04 

Taxes and insurance 0.03 0.04 0.04 

Depreciation 0.16 0.19 0.19 

 

Plant gate cost, U.S. $/gal 0.95 0.93 1.01 

0.00 0.00 0.00 

General and administrative, sales 

and research 0.07 0.08 0.08 

0.00 

Production costs, U.S. $/gal 1.02 1.02 1.09 

 

Selling price, U.S. $/gal (10% 

ROI) 1.33 1.40 1.48 

8
6.0 Conclusions and Recommendations 

A techno-economic analysis (TEA) using a CHEMCAD-based process model and Excel-based 

production-cost spreadsheet of cellulosic-derived lignin conversion to pyrolysis oil was performed. Fast 

pyrolysis of raw lignin from a cellulosic plant has not been demonstrated. Furthermore, the minimum 

amount of cellulosic material needed in the lignin stream to allow high conversions and high yields of 

liquid products is not known. However, this screening study suggests that producing fast pyrolysis oil as 

an end product in a biorefinery is too low of a value fuel to positively impact ethanol economics. Thus 

further research into fast pyrolysis as an end product is not recommended. If a higher valued product 

could be produced, then this option may have merit. Examples of higher valued products are upgrading 

the fast pyrolysis oil to gasoline or extracting chemicals such as levoglucosan. Estimating the economics 

for these higher valued products is beyond the scope of this work. However, this work can serve as a basis 

for future biorefinery studies. 

Upgrading the raw lignin stream from an ethanol biorefinery to valuable products has the potential to 

improve the economics of a cellulosic biorefinery. It is recommended that techno-economic work be 

continued to identify those products worth pursuing. Since the lignin has high moisture content, it is 

recommended that future studies consider wet processing methods such as high-pressure liquefaction or 

gasification for fuels production. Upgrading fast pyrolysis oil and chemical production should also be 

considered. 

9
7.0 References 

EERE. 2004. Werpy T et al. 2004. Top Value Added Chemicals from Biomass Volume I: Results of 

Screening for Potential Candidates from Sugars and Synthesis Gas. DOE/GO-102004-1992, U.S. 

Department of Energy, Richland, Washington. 

Ferdous, D. el.al. 2001. Fuel Processing Technology. 70:9-26. 

IEA 2007. Biomass Pyrolysis. IEA Bioenergy. Task 34 Booklet. T34:2007:01 

http://www.ieabioenergy.com/MediaItem.aspx?id=5416

NREL. 2002. Aden et al. 2002. Lignocellulosic Biomass to Ethanol Process Design and Economics 

Utilizing Co-Current Dilute Acid Prehydrolysis and Enzymatic Hydrolysis for Corn Stover. NREL/TP510-32438, National Renewable Energy Laboratory, City, State. 

NREL. 2008. Aden A. 2008. Biochemical Production of Ethanol from Corn Stover: 2007 State of 

Technology Model. NREL/TP-43205, National Renewable Energy Laboratory, City, State. 

Nunn T. et.al. 1985. Industrial Engineering and Chemical Process Design and Development. 24:844-

852. 

Piskorz J. et al. 1998. Journal of Analytical and Applied Pyrolysis. 46:15-29. 

PNNL. 2007. Holladay J. et al. 2007. Top Value Added Chemicals from Biomass Volume II: Results of 

Screening for Potential Candidates from Biorefinery Lignin. PNNL-16983, Pacific Northwest National 

Laboratory, Richland, Washington. 

PNNL. 2008. Jones S.B. et al. 2008. Production of Gasoline and Diesel from Biomass via Fast 

Pyrolysis, Hydrotreating and Hydrocracking: A Design Case. In review. PNNL-18284, Pacific 

Northwest National Laboratory, Richland, Washington. 

10
11

8.0 Appendix: Heat and Material Balance for the High Char 

Case 
12

245 

From A500

LP STM

232

Overliming

310

Saccharification  Tank

550

To 600

Recycle Watr

302

550

LP STM

 Area 100 Corn Stover Feed Handling

Corn Stover

Area 200 Pretreatment and Hydrolyzate Conditioning

Area 300 Saccharification and Fermentation

Area and S

T-512 SCBR

Well Water Vent

347

523

101

102

Polymer

101

106

102

Water Losses

108

103

Conveyer

103

Grinder

107 104

109

104

Underflow

304

203

HP STM

215

105

PREHYDROLYSIS

Sulfuric Aci

219

244

H-244

201

H-201

2520

T-232 224

250

253

200

H-200

227

Ca(OH)2

209

T-209

229

To Landfill

222

2228

2209

P-209 

PNEUMAPRESS

212

S-205

232

301 H-301

303

311

312

Enzyme

305

309

921

923

924

CWS

CW S

CW S

A500 Water

 T 20  P 1.0  W 76261 

 T 74  P 3.0  W 33553 

 T 20  P 1.0  W 22 

55

212

211

211

A-201

214

M-202

202

2217

204

217

218

T-203

925

926

235

H-205

261

922

265

AIR

252

WET SOLIDS

222

259

WET AIR

FILTRATE

T

220 205

2240

240

 T  P  W 

230

2230

2227

228

255

260

621

10

2521

262

2522

260

216

524

Figure 3 Process Flowsheet for the High Char Case 
Air

806

Ev ap

Superheater

Economizer

0

865 855

856

857

852 855

851

852

853

848 850

854

851 854

862

864

To S215 To S302 To D501 To D502

865

To Evaprator

Cond 501&502

Area 800 Combustor and Steam Turbine

tillation, Dehydration, Evaporation,

quid Separation

Cond E302

239

P-239

560

From A500

H-801

804

Air Blower

BURNERS

8047

8049

8040

FLUE GAS

Blow d

812

Superheated 

811

H-811

813

BFW

To S216

823

815

8823

8812 8830

P-811 E-811

811

W ell MU 

8597

Mol Sieve 

861

Ev ap Cond

8045

8813

 T 165 C P 1.0 bar W 317001 kg/h

 T 300 C P 87.7 bar W 3840 kg/h

 T 148 C P 4.5 bar W 497 kg/h T 115 C

 P 1.7 bar W 3789 kg/h

 T 148 C P 4.5 bar W 8975 kg/h

 T 148 C P 4.5 bar W 60776 kg/h

 T 26 C P 1.7 bar W 22447 kg/h

 T 139 C P 99.6 b W 12800

 T 137 C P 3.3 bar W 0 kg/h

 T 139 C P 99.6 bar W 128000 kg/h

814

842

 T 163 C P 4.5 bar W 0 kg/h

843

 T 163 C P 4.5 bar W 0 kg/h

844

 T 163 C P 4.5 bar W 497 kg/h

845

 T 163 C P 4.5 bar W 54164 kg/h

846

 T 163 C P 4.5 bar W 6612 kg/h

 T 118 C P 1.7 bar W 3789 kg/h

 T 190  P 12.5 

 T 268  P 13.2 

 T 177  P 98.9 

 T 510  P 87.2 

 T 820  P 1.0 

 T 640  P 1.0 

 T 270  P 1.0 

 T 24 C P 1.0 bar W 205000 kg/h

 T 25  P 1.0 

 T 40 C P 1.0 bar W 4845 kg/h

8815

 T 308  P 98.2 

8819

8818 T 300 

 P 87.7 

 T 301  P 87.7 

 T 300  P 87.7 

To Mol Sve

870

to Dearatr 871

873

863

856

821

869

828

T-828

To 

 T 121 C P 2.0 bar W 2379 kg/h

OLYSIS

 T 49 C P 1.00 bar

From A600

EVAP BTMS

 T 268 C P 13.2 bar W 29043 kg/h

idify

one

Drum Filter

2239

840

615

575

8044

8043

 T 220  P 1.0 

 T 82 C P 2.0 bar W 1478 kg/h

 T 20 C P 1.0 bar W 22000 kg/h

8001 8002

V

1

849

 T 163 C P 4.5 bar W 0 kg/h

CORN STOVER

804 8042

3

8816

From U1100 6112

872

8873

TO 

 T 137 C P 3 bar W 28810 kg/h

 T 180 C P 10 bar W 28810 kg/h

8872

8692

Figure 3, cont. Process Flowsheet for the High Char Case 

13
285

310

Saccharification  Tank

325

DAP

330

335

336

345

350

355

319

318 DAP

574

550

506

501

322

335

336

515

A900 W ater

561

541

544

545

Lignin Sep

562

Air

Co-Fermentor

557

536

1003

338

337

316

302

Corn Steep L

Corn Steep L

550

506

596597

LP STM

To S215 

Area 300 Saccharification and Fermentation

Area 500 Distillation, Dehydrationand Solid-Liquid Separation

Air to Comb

EV-501 EV-502

1003

558 559

VLP STEAM

1921

1922

TK-306

H-201

H-512

T-512 SCBR

D-501 Beer C

501

Well Water Vent

512

517

522

5519

Mol. Sieve 

526

525

P-511

5525

573

P-504

H-503

579

580

528

529

EV-50

530 

347

503

507

510

531 4

5

1

516

572

 T 117 C P 2.1305 bar W 303483 kg/h

 T 87 C P 0.6181 bar W 235471 kg/h

 T 40 C P 3.2424 bar W 202278 kg/h

 T 40 C P 3.2424 bar W 194620 kg/h

 T 71 C P 0.3192 bar W 56741 kg/h

 T 71 C P 0.3192 bar W 137879 kg/h

527

325

323

326

317

331

551

523

 T 86 C P 0.6181 bar W 68012 kg/h

304

308

552

510

511

502

D-502 Dist

5521

524

229

To Landfill To S216

301 H-301

303

311

311

315

320

320

321

SEED PROD

931 932

CWS

H-310

312

Enzyme

305

309

LP STM

502

 T 87  P 0.6181 

1910

LP STM

1920

1911

Beer Col Reb

1923

D502 Reblr

5511

5618

9

1912

1913

1924 1925

508

5523

518 5518

5531

576

531

 T 63 C P 0.2232 bar W 79735 kg/h 

524

Figure 3, cont. Process Flowsheet for the High Char Case 

14
574

A900 Water

561

541

544

545

Lignin Sep

562

CT BLOW DOWN

536

1003

Air to Comb

EV-502

1003

558 559

VLP STEAM

1921

1922

526

P-511

5525

573

P-504

579

580

528

529

EV-503

532

530 533

TK-514

507

542

4

5

1

516

572

 T 40 C P 3.2424 bar W 202278 kg/h

 T 40 C P 3.2424 bar W 194620 kg/h

 T 71 C P 0.3192 bar W 56741 kg/h

 T 71 C P 0.3192 bar W 137879 kg/h

 T 63 C P 0.2232 bar W 58144 kg/h

527

 T 86 C P 0.6181 bar W 68012 kg/h

5102

5211

To S102

To S211

517

597

5219 To S219

502

D-502 Dist

LP STM

534

H-517

957 958

 T 87 CW S P 0.6181 

 T 71  P 0.3293 

1920

1923

D502 Reblr

5618

9

1924 1925

800

800 TO BOILER

 T 74 C P 2 bar

 T 74 C W 33553 kg/h P 2 bar W 182897 kg/h

 T 74 C P 2 bar W 16113 kg/h

 T 74 C P 2 bar W 77488 kg/h

5571

576 Area 600 Wastewater Tre

To T-914

Area 900 Process Water

T-606

To Combust

P-606

AIR

T-914

ANAEROBIC

606

607

914

629

617

618

614

2241

8821

535

944

H-244 Vapor

612

950 5251

600

 T 74 C P 2 bar W 55743 kg/h

BLR BLOWDOWN

EVAP COND

531

 T 63 C P 0.2232 bar W 79735 kg/h

SAND RECYCLE

CYCLONE

AIR

COM BUSTOR

WET ASH

QUENCH WATER

QUENCH COLM

SOLIDS

FLUE GAS

CHAR & SAND

PYROLYZER

EXHAUST

FILTER

1801 1800

AREA 1100 PYROLYSIS UNIT

1105

513

P-513

DRYER

FUEL GAS

WET SOLIDS

571

11101111

1113

1121

1120

1124

1160

1161

1116

CWS CWR

1147

1131

1140

1138

1133 1134 1135

1137

1132

1139

SAND HEATER

1103

1126

1101

6110

BFW

1130

1127

6111

To Deareator

9611

Figure 3, cont. Process Flowsheet for the High Char Case 

15
Table 5 Heat and Material Balance for the High Char Case 

Stream No. 1 3 5 101 102 103 104 105 106 107 108 

Stream Name Corn Stover A500 Water Underflow Underflow Polymer Water LossesUnderflow 

Temp C 25.0489 25.6756 21 20 73.8 45 -26.44 45 -27.7742 20 -27.7742 -27.77Pres bar 1.0234 1 0.9818 1.0132 3.0397 1.0132 1.0132 1.0132 1.0132 1.0132 1.0132 1.0Enth MW 0 -1.4844 -309.27 -163.13 -144.29 -38.56 -3.4701 -260.41 -307.41 -0.09766 -304.04 -3.37Vapor mass fraction 01000000000

Total kg/h 0 213776.27 70051.4874 76261 33553 8912.7038 786.3577 100137.043 109814 22.14 109049.758 764.2Flowrates in kg/hGlucose 00000000000

Cellulose 0 0 0 24261.5609 0 0 0 24261.5609 24261.5609 0 24261.5609 

Xylose 00000000000

Xylan 0 0 0 13666.3191 0 0 0 13666.3191 13666.3191 0 13666.3191 

Lignin 0 0 0 11670.1175 0 0 0 11670.1175 11670.1175 0 11670.1175 

Acetate 0 0 0 1901.7093 0 0 0 1901.7093 1901.7093 0 1901.7093 

Organism 00000000000

Solslds 0 0 0 5768.6186 0 0 0 5768.6186 5768.6186 0 5768.6186 

Gypsum 00000000000

Lgnsol 0 0000000000

HMF 0 0.0001 0 0 0.0282 0.008 0 0.0201 0.0282 0 0.0282 

C5Sugar 00000000000

C6Sugar 00000000000

C5Solid 0 0 0 1895.8035 0 0 0 1895.8035 1895.8035 0 1895.8035 

C6Solid 0 0 0 2267.8775 0 0 0 2267.8775 2267.8775 0 2267.8775 

CaH2O2 00000000000Ash 0 0 0 3390.0019 0 0 0 3390.0019 3390.0019 0 3390.0019 

Ethanol 0 1.1023 0.0009 0 26.0112 6.7131 0.8402 18.4579 26.0112 0 25.171 0.84

Water 0 391.1629 70051.4378 11438.9706 32763.9479 8704.2143 769.1693 34751.6747 44202.9202 22.14 43455.889 747.02Furfural 0 4.1699 0 0 39.0794 10.5845 0.8129 27.682 39.0794 0 38.2665 0.8

Sulfuric Acid 0 0 0 0 0 0 0 0 0 0 0 

Nitrogen 0 168469 0.0039 0 0 0 0 0 0 0 0 

Carbon Dioxide 0 17.9352 0.0033 0 0 0 0 0 0 0 0 

Oxygen 0 44890.871 0.0382 0 0 0 0 0 0 0 0 

Ammonia 00000000000

Lactic Acid 0 0.0009 0.005 0 1.3482 0 0 1.3482 1.3482 0 1.3482 

Acetic Acid 0 2.0409 0 0 722.5768 191.184 15.5354 515.8574 722.5768 0 707.0414 15.53

Methane 0 0 0 0 0 0 0 0 0 0 0 

Nitrogen Dioxide 0 0 0 0 0 0 0 0 0 0 0 

Sulfur Dioxide 0 0 0 0 0 0 0 0 0 0 0 

DAP 000000000002-2-4-TriMth-C5 00000000000Hydrogen 0 0 0 0 0 0 0 0 0 0 0 

Carbon 00000000000

Carbon Monoxide 0 0 0 0 0 0 0 0 0 0 0 

16
Stream No. 214 215 216 217 218 219 220 222 227 228 229 2

Stream Name LP STM HP STM Recycle Watr Ca(OH)2 To Landfill 

Temp C 73.6046 163.2652 267 190 101.1 36.7532 101.1 50 20 50.0325 52.5328 52.56

Pres bar 3.0397 4.4786 13.1722 38.7669 1.0132 1.0132 1.0132 1 1.0132 2.0265 1.0132 2.02

Enth MW -337.94 -32.867 -105.1 -738.38 -144.88 -688.79 -586.94 -1149.4 -8.6251 -926.06 -20.826 -907Vapor mass fraction 0 1 1 0 1 0 0 0 0 01.78E-06

Total kg/h 79128.1188 8975.0001 29042.5201 217282.709 39835.1765 161535 177447.532 308015.669 2331.7899 238116 6133.3985 2328

Flowrates in kg/hGlucose 0 0 0 1887.0023 0 14.8202 1887.0023 1899.013 0 1771.9691 9.3511 1762.6

Cellulose 0 0 0 22223.5898 0 5.4601 22223.5898 22228.0159 0 111.1394 110.5837 0.55

Xylose 0 0 0 13976.8518 0 163.8025 13976.8518 14109.602 0 13169.903 69.5009 13100.40

Xylan 0 0 0 341.6581 0 0.78 341.6581 342.2903 0 1.7114 1.7029 0.00

Lignin 0 0 0 11086.6117 0 55.3808 11086.6117 11131.4934 0 55.6571 55.3788 0.27

Acetate 00000000000

Organism 0 0 0 0 0106.0816 085.9718 0 0 0 

Solslds 106.8592 0 0 5875.4781 0 1723.0453 5875.4781 7271.887 0 6861.7527 36.2112 6825.54

Gypsum 0 0 0 0 0 0 0 0 02728.0646 4201.7444 21.1

Lgnsol 0 0 0 583.5059 0 173.9427 583.5059 724.4744 0 683.8315 3.6087 680.22HMF 0 0 0 88.1958 0.1608 36.6606 88.035 117.7457 0 112.9064 0.5958 112.3

C5Sugar 0 0 0 2380.9848 0 155.2223 2380.9848 2506.7818 0 2341.334 12.3558 2328.97

C6Sugar 0 0 0 2708.2656 0 443.8268 2708.2656 3067.9568 0 2865.4715 15.1218 2850.34

C5Solid 0 0 0 222.7605 0 0 222.7605 222.7605 0 0 0 

C6Solid 0 0 0 56.697 0 0 56.697 56.697 0 0 0 

CaH2O2 00000000 2331.7899 1157.7868 511.9401 2.57

Ash 0 0 0 3390.0019 0 17.9403 3390.0019 3404.5414 0 17.0227 16.9376 0.08

Ethanol 55.3796 0 0 73.8375 58.0866 21.8403 15.7509 32.7729 0 31.911 0.1684 31.74

Water 76639.144 8975.0001 29042.5201 147175.543 38990.1268 156542.14 108185.416 234728.608 0 202007.447 1066.0438 200941.4

Furfural 99.8393 0 0 565.9027 344.9017 234.7835 221.001 407.3621 0 392.6971 2.0724 390.62

Sulfuric Acid 1641.1199 0 0 1641.1199 0 28.0804 1641.1199 1663.8773 0 0 0 

Nitrogen 0 0 0 0 0 0 01.8626 01.8626 0.0098 1.85Carbon Dioxide 0 0 0 0 022.6203 00.3966 00.3966 0.0021 0.39

Oxygen 0 0 0 0 0 0 01.0972 01.0972 0.0058 1.09Ammonia 00000000000

Lactic Acid 0 0 0 1.3482 0.0023 742.5714 1.3459 603.1483 0 571.7846 3.0174 568.76

Acetic Acid 585.7761 0 0 3003.3522 441.8991 1045.9956 2561.4532 3407.3079 0 3230.1278 17.0462 3213.08

17
Stream No. 239 240 250 252 253 255 259 260 261 262 302 303 

Stream Name WET SOLIDSAIR WET AIR To combustorTO 600 LP STM

Temp C 52.4998 50 50.4926 36.7532 36.7532 50 40 50 38 38 163.26 147.741 

Pres bar 1.0132 1 1 1.0132 1.0132 1 9.6259 1 1 1 4.4786 4.4786 

Enth MW -927.96 -916.35 -1270.7 -558.21 -130.57 -233 -0.0016604 -1.2258 -0.65558 -0.68983 -29.141 -33.91 Vapor mass fraction 1.77E-06 1.76E-06 0 0 0 0 1 1 1 0 10.0003125

Total kg/h 238967.372 235784.061 335687.526 130913 30622.0067 72231.587 3744.6703 4089.5237 3931.4011 158.1227 7957.6491 7957.6491 Flowrates in kg/hGlucose 1771.9691 1771.9691 1892.4713 12.0108 2.8095 127.044 0 0 0 0 0 0 

Cellulose 111.1394 111.1394 22118.468 4.425 1.0351 22116.8769 0 0 0 0 0 0 

Xylose 13169.903 13169.903 14071.1538 132.7506 31.0519 939.6995 0 0 0 0 0 0 

Xylan 1.7114 1.7114 340.7352 0.6321 0.1479 340.5788 0 0 0 0 0 0 

Lignin 55.6571 55.6571 11086.6135 44.8823 10.4985 11075.8362 0 0 0 0 0 0 

Acetate 000000000000

Organism 0 0 106.0816 85.9718 20.1098 85.9718 0 0 0 0 0 0 

Solslds 6861.7527 6861.7527 7562.3115 1396.4096 326.6358 410.1344 0 0 0 0 0 0 

Gypsum 4222.8586 021.1142 0 0 0 0 0 0 0 0 0 

Lgnsol 683.8315 683.8315 753.8398 140.9685 32.9741 40.643 0 0 0 0 0 0 

HMF 112.9064 112.9064 124.0996 29.7109 6.9497 4.8393 0 0.0001 0 0.0001 0 0 

C5Sugar 2341.334 2341.334 2523.8513 125.797 29.4253 165.4476 0 0 0 0 0 0 

C6Sugar 2865.4715 2865.4719 3136.9709 359.691 84.1357 202.4852 0 0 0 0 0 0 

C5Solid 0 0222.7605 0 0222.7605 0 0 0 0 0 0 

C6Solid 0 056.697 0 056.697 0 0 0 0 0 0 

CaH2O2 514.5127 02.5725 0 0 0 0 0 0 0 0 0 

Ash 17.0227 17.0227 3391.0043 14.5394 3.4009 3387.5186 0 0 0 0 0 0 

Ethanol 31.911 31.911 36.7448 17.7001 4.1402 0.8619 0 0.6781 0.643 0.0351 0 0 

Water 202007.447 202007.447 263338.068 126866.625 29675.5171 32721.1684 0 323.4317 166.9911 156.4406 7957.6491 7957.6491 

Furfural 392.697 392.6971 449.7974 190.2759 44.5076 14.665 0 3.9147 3.6061 0.3087 0 0 

Sulfuric Acid 0 1554.0614 115.1391 22.7572 5.3232 109.8159 0 0 0 0 0 0 

Nitrogen 1.8626 1.8626 1.8527 0 0 0 2872.4811 2870.6182 2870.6167 0.0016 0 0 

Carbon Dioxide 0.3966 0.3966 4.6827 18.3322 4.2881 0 0 17.9356 17.9352 0.0004 0 0 

Oxygen 1.0972 1.0972 1.0914 0 0 0 872.1891 871.0919 871.091 0.0009 0 0 

Ammonia 000000000000

Lactic Acid 571.7845 571.7846 740.8992 601.803 140.7684 31.3637 0 0.0005 0 0.0005 0 0 

Acetic Acid 3230.1278 3230.1281 3588.55 847.7074 198.2882 177.18 0 1.8528 0.5181 1.3347 0 0 

18
Stream No. 309 311 312 315 316 317 318 319 320 321 323 325 

Stream Name Enzyme DAP Corn Steep L DAP Co

Temp C 64.216 65 20 41 41 41 20 20 40.37 41 41 20 

Pres bar 1.0132 1.0132 1.0132 1.0132 1.0132 1.0132 1.0132 1.0132 1.0132 1.0132 1.0132 1.0132 Enth MW -1288.1 -1287.8 -22.177 -1295.7 -129.57 -1166.2 -0.3511 -3.7405 -133.66 -134.01 -129.95 -0.35186 Vapor mass fraction 1.50E-06 1.74E-06 0 0 0 0 0 0 00.04933500

Total kg/h 341010.404 341010.404 5322.84 341010.404 34101.046 306909.443 106 848 35055.0465 35055.0713 33417.8721 106.23 Flowrates in kg/hGlucose 1892.4713 24256.6032 0 24256.6032 2425.6603 21830.9419 0 0 2425.6603 157.6677 157.6677 0 

Cellulose 22118.468 840.5 0 840.5 84.05 756.45 0 0 84.05 84.05 84.05 0 

Xylose 14071.1538 14071.152 0 14071.152 1407.1153 12664.0367 0 0 1407.1153 196.9963 196.9963 0 

Xylan 340.7352 340.7352 0 340.7352 34.0735 306.6617 0 0 34.0735 34.0735 34.0735 0 

Lignin 11086.6135 11086.6135 0 11086.6135 1108.6614 9977.9522 0 0 1108.6614 1108.6614 1108.6614 0 

Acetate 000000000000

Organism 549.4741 549.4741 443.3925 549.4741 54.9474 494.5267 0 0 54.9474 169.1464 169.1464 0 

Solslds 7562.3115 7562.3115 0 7562.3115 756.2312 6806.0804 0 0 756.2312 756.2311 756.2311 0 

Gypsum 21.1142 21.1142 0 21.1142 2.1114 19.0028 0 0 2.1114 2.1114 2.1114 0 

Lgnsol 753.8398 753.8397 0 753.8397 75.384 678.4557 0 0 75.384 75.384 75.384 0 

HMF 124.0996 124.0996 0 124.0996 12.41 111.6896 0 0 12.41 12.41 12.4099 0 

C5Sugar 2523.8513 2523.8513 0 2523.8513 252.3851 2271.4661 0 0 252.3851 280.5274 280.5274 0 

C6Sugar 3136.9709 4414.9217 0 4414.9217 441.4922 3973.4293 0 0 441.4922 441.4922 441.4922 0 

C5Solid 222.7605 222.7605 0 222.7605 22.276 200.4844 0 0 22.276 22.276 22.276 0 

C6Solid 56.697 56.697 0 56.697 5.6697 51.0273 0 0 5.6697 5.6697 5.6697 0 

CaH2O2 2.5725 2.5725 0 2.5725 0.2573 2.3153 0 0 0.2573 0.2573 0.2573 0 

Ash 3391.0043 3391.0043 0 3391.0043 339.1004 3051.9039 0 0 339.1004 339.1004 339.1004 0 

Ethanol 36.7448 36.7448 0 36.7448 3.6745 33.0703 0 0 3.6745 1633.8554 1592.0399 0 

Water 268217.56 265853.465 4879.4477 265853.465 26585.3447 239268.104 0 848 27433.3445 27452.8295 27400.2234 0 Furfural 449.7974 449.7974 0 449.7974 44.9797 404.8176 0 0 44.9797 44.9797 44.4698 0 

Sulfuric Acid 115.1391 115.1391 0 115.1391 11.5139 103.6252 0 0 11.5139 11.5139 11.5139 0 

Nitrogen 1.8527 1.8527 0 1.8527 0.1853 1.6675 0 0 0.1853 0.1853 0.0001 0 

Carbon Dioxide 4.6827 4.6827 0 4.6827 0.4683 4.2144 0 0 0.4683 1557.7903 23.5018 0 

Oxygen 1.0914 1.0914 0 1.0914 0.1091 0.9822 0 0 0.1091 7.5285 0.0055 0 

Ammonia 000000000000

Lactic Acid 740.8992 740.8992 0 740.8992 74.0899 666.8093 0 0 74.0899 129.8801 129.88 0 

Acetic Acid 3588.55 3588.55 0 3588.55 358.855 3229.6948 0 0 358.855 426.2911 426.019 0 

Methane 000000000000

Nitrogen Dioxide 0 00000000000

Sulfur Dioxide 000000000000

DAP 0 0 0 0 0 0106 0106 104.1629 104.1629 106.23 

19
Stream No. 336 337 338 501 502 506 508 510 511 512 515 516 

Stream NameTemp C 40.9352 41 51.697 95 41 100 99.0442 113.2729 91.7119 116 37.1918 120.4596 

Pres bar 1.0132 1.0132 1.0132 4.053 1.0132 4.8231 1.8892 1.9384 1.6779 1.6779 4.053 4.3468 Enth MW -1261.2 -39.192 -1261.2 -1368.4 -1260.6 -1366.5 -3.5616 -134.34 -40.942 -40.644 -32.075 -125.44 Vapor mass fraction 0 0 0.059362 0.00040053 0 0.00039771 1 1 0.99992 100

Total kg/h 331047.191 10238.5711 331047.304 353760 323630 353760 1660.1368 48616.7744 25831.903 25831.903 19091.7542 29525.0963 

Flowrates in kg/hGlucose 21328.9533 0 63.9846 63.9846 63.9846 63.9846 0 0 0 0 0 0 

Cellulose 815.285 25.215 815.285 840.5 840.5 840.5 0 0 0 0 0 0 

Xylose 12475.2023 0 748.5122 748.5122 748.5122 748.5122 0 0 0 0 0 0 

Xylan 330.5132 10.2221 330.5132 340.7353 340.7353 340.7353 0 0 0 0 0 0 

Lignin 10754.0151 332.5984 10754.0151 11086.6135 11086.6135 11086.6135 0 0 0 0 0 0 

Acetate 000000000000

Organism 643.763 19.9102 1135.5483 1155.4586 1155.4586 1155.4586 0 0 0 0 0 0 

Solslds 7335.4422 226.8693 7335.4422 7562.3115 7562.3115 7562.3115 0 0 0 0 0 0 

Gypsum 20.4808 0.6334 20.4808 21.1142 21.1142 21.1142 0 0 0 0 0 0 Lgnsol 731.2246 22.6152 731.2246 753.8397 753.8397 753.8397 0 0 0 0 0 0 

HMF 120.3766 3.723 120.3766 124.0996 124.0995 124.0996 0 0.0888 0 0 0 0.0888 

C5Sugar 2475.4338 50.5295 1068.9459 1119.4754 1119.4754 1119.4754 0 0 0 0 0 0 

C6Sugar 4282.4736 75.4951 2890.6695 2966.165 2966.165 2966.165 0 0 0 0 0 0 

C5Solid 216.0777 6.6828 216.0777 222.7605 222.7605 222.7605 0 0 0 0 0 0 

C6Solid 54.9961 1.7009 54.9961 56.697 56.697 56.697 0 0 0 0 0 0 

CaH2O2 2.4954 0.0772 2.4954 2.5726 2.5726 2.5726 0 0 0 0 0 0 

Ash 3289.2742 101.7301 3289.2742 3391.0043 3391.0043 3391.0043 0 0 0 0 0 0 

Ethanol 1576.357 48.7533 19086.9508 20125.6153 18610.4821 20125.6153 976.4801 18997.3946 23698.6457 23698.6457 18982.6157 14.7626 Water 259495 8025.6162 259579 295624.461 267039.155 295624.461 431.215 29201.9543 2132.0895 2132.0895 107.9716 29094.0773 Furfural 435.8088 13.4786 435.8088 455.2627 443.8883 455.2627 5.4887 236.1783 0.0591 0.0591 0.0591 236.1192 

Sulfuric Acid 111.6849 3.4542 111.6849 115.139 115.139 115.139 0 0 0 0 0 0 

Nitrogen 1.6175 0.05 1.6175 0.0006 0.0006 0.0006 0.0006 0 0 000

Carbon Dioxide 26.8847 0.8315 16754.8623 247.2211 233.0453 247.2211 246.1115 1.1096 1.1096 1.1096 1.1096 0 Oxygen 0.9581 0.0296 32.9088 0.024 0.0222 0.024 0.0239 0 0 000

Ammonia 000000000000

Lactic Acid 772.7886 1152.3726 1117.6733 2270.0462 2270.0444 2270.0462 0.0001 1.3676 0 0 0 1.3676 Acetic Acid 3546.043 109.6714 4152.9097 4263.6704 4259.6412 4263.6704 0.8169 178.6808 0 0 0 178.6808 Methane 000000000000

Nitrogen Dioxide 0 00000000000

Sulfur Dioxide 000000000000

DAP 204.0811 6.3118 196.1697 202.4815 202.4815 202.4815 0 0 0 0 0 0 

20
Stream No. 522 523 524 525 526 527 528 529 530 531 532 533 

Stream Name Well Water 

Temp C 116 49.2528 26 87.0895 87.0895 86.487 71.0548 71.0548 71.2455 63.3463 63.3463 62.5145 

Pres bar 1.6779 1.0132 1.0132 0.6181 0.6181 0.6181 0.3192 0.3192 0.3293 0.2232 0.2232 0.2232 Enth MW -26.666 -51.385 -123.36 -916.78 -249.61 -292.67 -525.99 -208.99 -245.49 -275.26 -214.23 -251.91 Vapor mass fraction 1 0.99936 0 2.90E-06 1 7.02E-06 0 1 1.15E-05 0 1 4.69E-05 

Total kg/h 19091.7542 20953.3948 28011.3594 235470.714 68012.2636 68012.2636 137879.196 56740.7874 56740.7874 79735.2309 58144 58144 1

Flowrates in kg/hGlucose 0 0 063.9846 0 056.8544 0 056.8544 0 0 

Cellulose 0 0 0840.5 0 016.1736 0 016.1736 0 0 

Xylose 0 0 0748.5121 0 0648.1553 0 0648.1553 0 0 

Xylan 0 0 0340.7353 0 06.5567 0 06.556700

Lignin 0 0 011086.6135 0 0213.3372 0 0213.3372 0 0 

Acetate 000000000000

Organism 0 0 01155.4586 0 0555.8557 0 0555.855700

Solslds 0 0 0 7562.3115 0 0 6719.6051 0 0 6719.605100

Gypsum 0 0 021.1142 0 00.4063 0 00.4063 0 0 

Lgnsol 0 0 0 753.8397 0 0 669.8356 0 0 669.8356 0 0 

HMF 0 0.0001 0 123.844 0.1668 0.1668 109.942 0.1014 0.1014 109.8329 0.1091 0.1091 C5Sugar 0 0 01119.4754 0 0994.7266 0 0994.7265 0 0 

C6Sugar 0 0 0 2966.165 0 0 2568.4759 0 0 2568.475900

C5Solid 0 0 0222.7605 0 04.2865 0 04.286500

C6Solid 0 0 056.697 0 01.091 0 01.091 0 0 

CaH2O2 0 0 02.5726 0 0 0 0 0 0 0 0 

Ash 0 0 03391.0043 0 065.2523 0 065.2523 0 0 

Ethanol 18982.6157 1543.4823 0 31.1905 120.5525 120.5525 4.0738 23.641 23.641 0.3324 3.7414 3.7414 

Water 107.9716 1049.1178 28011.3594 198777.387 67214.019 67214.019 120473.609 56153.0132 56153.0132 63064.5348 57409.0707 57409.0707 1Furfural 0.0591 11.3977 0 70.2409 143.356 143.356 16.5697 45.8439 45.8439 3.1367 13.433 13.433 Sulfuric Acid 0 0 0115.139 0 0102.3085 0 0102.3085 0 0 

Nitrogen 0 1.85280000000000Carbon Dioxide 1.1096 18303.04920000000000

Oxygen 0 40.46330000000000

Ammonia 000000000000

Lactic Acid 0 0.0018 0 2266.4819 2.1972 2.1972 2012.4651 1.4511 1.4511 2010.4273 2.0378 2.0378 

Acetic Acid 0 4.0289 0 3552.2003 531.9725 531.9725 2639.6188 516.7417 516.7417 1924.0465 715.5725 715.5725 Methane 000000000000

Nitrogen Dioxide 0 00000000000Sulfur Dioxide 000000000000

DAP 0 0 0202.481500000000

21
Stream No. 550 551 552 557 558 559 560 571 572 573 574 575 

Stream Name Vent Air From A500 WET SOLIDS A900 Water EVAP BTMS Temp C 34.171 50.4061 41.8714 25 404.576 40 40 40 40 40 20 63.4809 

Pres bar 0.9119 0.9119 4.053 1.0132 9.6317 9.6317 1.0132 1.0132 3.2424 3.2424 1.0132 3.2424 Enth MW -47.109 -127.64 -1388.2 1.19E-08 0.48461 -0.0020127 -0.8183 -118.59 -808.66 -30.617 -462.22 -275.25 Vapor mass fraction 100111100000

Total kg/h 18834.7073 30130.0504 353760 4618.3987 4618.3987 4618.3987 4844.8852 32965.7291 202278.497 7658.512 104788.002 79735.2309 1

Flowrates in kg/hGlucose 0 0 63.9846 0 0 0 0 4.8928 59.0917 2.2373 0 56.8544 

Cellulose 0 0 840.5 0 0 0 0 823.69 16.81 0.6364 0 16.1736 

Xylose 0 0 748.5122 0 0 0 0 74.8512 673.6609 25.5056 0 648.1553 Xylan 0 0 340.7353 0 0 0 0 333.9206 6.8147 0.258 0 6.5567 Lignin 0 0 11086.6135 0 0 0 0 10864.8812 221.7323 8.3951 0 213.3372 Acetate 000000000000

Organism 0 0 1155.4586 0 0 0 0 577.7293 577.7293 21.8735 0 555.8557 Solslds 0 0 7562.3115 0 0 0 0 578.2827 6984.0291 264.4239 0 6719.6051 

Gypsum 0 0 21.1142 0 0 0 0 20.6919 0.4223 0.016 0 0.4063 

Lgnsol 0 0 753.8397 0 0 0 0 57.6454 696.1944 26.3588 0 669.8356 

HMF 0 0.0001 124.0996 0 0 0 0.0001 9.4702 114.3738 4.3303 0 109.8329 

C5Sugar 0 0 1119.4754 0 0 0 0 85.6052 1033.8702 39.1436 0 994.7265 C6Sugar 0 0 2966.165 0 0 0 0 296.6165 2669.5483 101.0724 0 2568.4759 C5Solid 0 0 222.7605 0 0 0 0 218.3053 4.4552 0.1687 0 4.2865 

C6Solid 0 0 56.697 0 0 0 0 55.563 1.1339 0.0429 0 1.091 

CaH2O2 0 02.5726 0 0 0 02.57260000

Ash 0 0 3391.0043 0 0 0 0 3323.1843 67.8201 2.5678 0 65.2523 Ethanol 28.3489 1515.1336 20125.6153 0 0 0 0.4593 1.9258 28.8054 1.0906 0 0.3324 

Water 475.1486 28585.3309 295624.461 0 0 0 224.1718 14976.1441 183577.068 6950.453 104788.002 63064.5348 1

Furfural 0.0233 11.3744 455.2627 0 0 0 0.5638 4.8074 64.8697 2.456 0 3.1367 

Sulfuric Acid 0 0 115.139 0 0 0 0 8.8046 106.3345 4.026 0 102.3085 Nitrogen 1.8527 0 0.0006 3648.5353 3648.5353 3648.5353 3648.3834 0.1521 0 0 0 0 

Carbon Dioxide 18288.8727 14.1758 247.2211 0 0 0000000

Oxygen 40.4615 0.0018 0.024 969.8633 969.8633 969.8633 969.7831 0.0802 0 0 0 0 

Ammonia 000000000000

Lactic Acid 0 0.0018 2270.0462 0 0 0 0.0009 173.3149 2093.1662 79.2498 0 2010.4273 Acetic Acid 0 4.0289 4263.6704 0 0 0 1.5228 270.1105 3280.5669 124.2063 0 1924.0465 Methane 000000000000

Nitrogen Dioxide 0 00000000000

Sulfur Dioxide 000000000000

DAP 0 0202.4815 0 0 0 0202.48150000

22
Stream No. 596 597 612 614 615 617 618 619 620 621 623 

Stream Name LP STM To Anaerobic From A600 To 600

Temp C 163.26 147.741 81.1983 81.536 81.6342 81.536 81.5361 52.8112 21 35.0121 0 Pres bar 4.4786 4.4786 2.0265 2.0265 2.0265 2.0265 2.0265 1.0132 0.9818 1 0 

Enth MW -1.8203 -2.1182 -309.07 -3.5383 -3.5433 -305.53 -305.53 -305.57 -1.3884 -173.22 0 Vapor mass fraction 1 0.0003125 0 1 1 0 0 0.33471 1 0 0 

Total kg/h 497.0711 497.0711 71889.3232 1476.6225 1478.0052 70412.7028 70412.7028 101106.802 31055.3256 39993.296 0 700

Flowrates in kg/hGlucose 00000000000

Cellulose 00000000000

Xylose 00000000000

Xylan 00000000000

Lignin 00000000000

Acetate 00000000000

Organism 00000000000

Solslds 00000000000

Gypsum 00000000000

Lgnsol 00000000000

HMF 0 00.1942 0 0 0 0 0 00.16090

C5Sugar 00000000000

C6Sugar 00000000000

C5Solid 00000000000

C6Solid 00000000000

CaH2O2 00000000000

Ash 00000000000

Ethanol 0 0 71.1546 0.062 0.0623 1.3611 1.3611 1.3611 0.0127 58.1217 0 

Water 497.0711 497.0711 70855.7421 252.1075 253.4381 70399.336 70399.336 70399.336 351.4123 39146.5666 0 700

Furfural 0 0 363.0621 0 0 0 0 0 0 345.2103 0 

Sulfuric Acid 00000000000

Nitrogen 0 0 0.0016 0.0016 0.0016 0 0 23545 23545 0.0016 0 Carbon Dioxide 0 0 0.0004 877.1952 877.2455 10.7803 10.7803 10.7803 16.0637 0.0004 0 

Oxygen 0 0 0.0009 0.0009 0.0009 0 0 7149.1088 7142.8502 0.0009 0 

Ammonia 00000000000

Lactic Acid 0 0 0.5038 0 0 0.5038 0.5038 0.5038 0 0.0029 0 

Acetic Acid 0 0 598.6655 0 0 0 0 0 0 443.2338 0 

Methane 0 0 0 347.2553 347.2569 0.7222 0.7222 0.7222 0 0 0 

23
Stream No. 700 701 703 800 804 811 812 813 814 815 821 823 

Stream Name Gasoline Ethanol TO BOILER Air Well MU WateSuperheated BFW To S216 Blowdown CO

Temp C 37.1918 20 36.6272 63.4809 24 26 510 139 267.9948 163.339 299.7772 189.943 Pres bar 4.053 1.0132 1.0132 3.2424 1.0132 1.7225 87.2003 99.6126 13.1722 4.4786 87.7474 12.4832 Enth MW -32.075 -0.49893 -32.574 -275.25 -0.057737 -98.858 -433.4 -547.21 -104.95 -312.18 -15.614 -36.658 Vapor mass fraction 0 0 0 0 1 0 1 0 1 1 0 1 Total kg/h 19091.7542 788.1077 19879.8621 79735.2309 205000 22447 124160 128000 29042.5024 85117.4729 3840.0311 10000.001 Flowrates in kg/hGlucose 0 0 0 56.8544 0 0 0 0 0 0 0 0 Cellulose 0 0 0 16.1736 0 0 0 0 0 0 0 0 Xylose 0 0 0 648.1553 0 0 0 0 0 0 0 0 Xylan 0 0 0 6.5567 0 0 0 0 0 0 0 0 Lignin 0 0 0 213.3372 0 0 0 0 0 0 0 0 Acetate 0 0 0 0 0 0 0 0 0 0 0 0 Organism 0 0 0 555.8557 0 0 0 0 0 0 0 0 Solslds 0 0 0 6719.6051 0 0 0 0 0 0 0 0 Gypsum 0 0 0 0.4063 0 0 0 0 0 0 0 0 Lgnsol 0 0 0 669.8356 0 0000000HMF 0 0 0 109.8329 0 0 0 0 0 0 0 0 C5Sugar 0 0 0 994.7265 0 0 0 0 0 0 0 0 C6Sugar 0 0 0 2568.4759 0 0 0 0 0 0 0 0 C5Solid 0 0 0 4.2865 0 0 0 0 0 0 0 0 C6Solid 0 0 0 1.091 0 0 0 0 0 0 0 0 CaH2O2 0 0 0 0 0 0 0 0 0 0 0 0 Ash 0 0 0 65.2523 0 0 0 0 0 0 0 0 Ethanol 18982.6157 0 18982.6157 0.3324 0 0000000Water 107.9716 0 107.9716 63064.5348 0 22447 124160 128000 29042.5024 85117.4729 3840.0311 10000.001 Furfural 0.0591 0 0.0591 3.1367 0 0000000Sulfuric Acid 0 0 0 102.3085 0 0 0 0 0 0 0 0 Nitrogen 0 0 0 0 161950 0 0 0 0 0 0 0 Carbon Dioxide 1.1096 0 1.1096 0 0 0 0 0 0 0 0 0 Oxygen 0 0 0 0 43050.0018 0000000Ammonia 0 0 0 0 0 0 0 0 0 0 0 0 Lactic Acid 0 0 0 2010.4273 0 0 0 0 0 0 0 0 Acetic Acid 0 0 0 1924.0465 0 0 0 0 0 0 0 0 Methane 0 0 0 0 0 0 0 0 0 0 0 0 Nitrogen Dioxide 0 0 0 0 0 0000000Sulfur Dioxide 0 0 0 0 0 0 0 0 0 0 0 0 DAP 0 0 0 0 0 0 0 0 0 0 0 0 2-2-4-TriMth-C5 0 788.1077 788.1077 0 0 0000000

24
Stream No. 844 845 846 848 849 850 851 852 854 855 856 861 

Stream Name To Mol Sve To D501 To D502 to Dearatr To Evaprator Evap Cond Temp C 163.339 163.339 163.339 163.339 163.339 117.9874 117.9874 117.9874 50.7428 50.7428 50.7581 115.21 Pres bar 4.4786 4.4786 4.4786 4.4786 4.4786 1.7225 1.7225 1.7225 0.1013 0.1013 4.2556 1.7023 Enth MW -1.8228 -198.65 -24.25 -87.452 -3.67E-08 -93.788 -78.884 -14.903 -79.884 -79.884 -87.847 -16.312 Vapor mass fraction 1 1 1 1 10.60031 0.60031 0.60031 0.60031 0.60031 0 0 

Total kg/h 497 54164.0071 6612 23844.4667 0 23844.4667 20055.4662 3789.0001 20055.4679 20055.4679 20055.4679 3789.0001 Flowrates in kg/hWater 497 54164.0071 6612 23844.4667 0 23844.4667 20055.4662 3789.0001 20055.4679 20055.4679 20055.4679 3789.0001 Stream No. 865 869 871 872 873 921 922 923 924 925 926 931 Stream Name Cond E302 To WWT VENT BFW CWS CWS CWS CWS 

Temp C 147.74 120.6474 137 137 138.5518 28 37 28 37 28 37 28 

Pres bar 4.4786 2.0265 3.3437 3.3437 99.6126 4.1341 4.1341 4.1341 4.1341 4.1341 4.1341 4.1341 Enth MW -38.291 -10.227 0 -671.03 -547.28 -2215 -2207.3 0 0 -50.393 -50.273 0 

Vapor mass fraction 001000000000

Total kg/h 8975.0001 2379.2136 0 156810 128000 502646.004 502646.004 0 0 11448.3755 11448.3755 0 

Flowrates in kg/hWater 8975.0001 2379.2136 0 156810 128000 502646.004 502646.004 0 0 11448.3755 11448.3755 0 

Furfural 0 0 0 0 0 0 0 0 0 0 0 0 

Sulfuric Acid 000000000000

Nitrogen 0 0 0 0 0 0 0 0 0 0 0 0 

Carbon Dioxide 0 0 0 0 0 0 0 0 0 0 0 0 Oxygen 0 0 0 0 0 0 0 0 0 0 0 0 

Ammonia 000000000000Lactic Acid 0 0 0 0 0 0 0 0 0 0 0 0 

Acetic Acid 000000000000

25
Stream No. 955 956 957 958 1003 1103 1105 1110 1111 1113 1114 1

Stream Name CWS CWSTemp C 28 37 28 37 40 241.1346 48.8889 563.4046 499.2643 499.2643 499.2643 499.26

Pres bar 4.1341 4.1341 4.1341 4.1341 1.0132 1.5648 1.5648 1.5648 1.5648 1.5648 1.5648 1.56Enth MW -2190 -2184.8 -15872 -15834 -0.8183 -116.5 -59.05 -1184.2 -1184.2 -1161.3 -9.7811 -115Vapor mass fraction 0 0 0 0 1 1 00.72911 0.7719300

Total kg/h 497538.44 497538.44 3605820.07 3605820.07 4844.8852 129827.222 19281.2176 920480 920480 909549 9548.9486 9000Flowrates in kg/hGlucose 0 0 0 0 0 04.8928 4.8928 0.0001 0.0001 0.0001

Cellulose 0 0 0 0 0 0823.69 823.69 0.0022 0.0022 0.0022

Xylose 0 0 0 0 0 074.8512 74.8513 0.0002 0.0002 0.0002

Xylan 0 0 0 0 0 0333.9206 333.9206 0.0008 0.0008 0.0008

Lignin 0 0 0 0 0 010864.8812 10864.8812 0.0275 0.0275 0.0275 

Acetate 00000000000

Organism 0 0 0 0 0 0577.7293 577.7293 0.0014 0.0014 0.0014

Solslds 0 0 0 0 00.0004 578.2827 578.2827 0.0016 0.0016 0.0016Gypsum 0 0 0 0 0 020.6919 20.6919 20.6919 20.6919 20.6919

Lgnsol 0 0 0 0 0 057.6454 57.6454 0.0002 0.0002 0.0002

HMF 0 0 0 00.0001 09.4702 9.4702000

C5Sugar 0 0 0 0 0 085.6052 85.6053 0.0003 0.0003 0.0003

C6Sugar 0 0 0 0 0 0296.6165 296.6165 0.0008 0.0008 0.0008C5Solid 0 0 0 0 0 0218.3053 218.3053 0.0005 0.0005 0.0005

C6Solid 0 0 0 0 0 055.563 55.563 0.0001 0.0001 0.0001

CaH2O2 0 0 0 0 0 02.5726 2.5726 2.5726 2.5726 2.5726

Ash 000000 3323.1843 3323.1843 3323.1843 3323.1843 3323.1843 

Ethanol 0 0 0 00.4593 1.7278 0.1981 0.1981 0.198100

Water 497538.44 497538.44 3605820.07 3605820.07 224.1718 18199.5168 1540.2177 1540.2177 2434.2451 00Furfural 0 0 0 00.5638 4.313 0.4944 0.4944 0.494400

Sulfuric Acid 0 0 0 0 0 08.8046 8.8046 8.804600Nitrogen 0 0 0 0 3648.3834 84475.2995 0.0156 95.9293 191.8275 0 0 

Carbon Dioxide 0 0 0 0 022960.525100 1299.9962 00

Oxygen 0 0 0 0969.7831 3906.8611 0.0082 0.0165 0.0165 0 0 

Ammonia 00000000000

Lactic Acid 0 0 0 00.0009 0173.3149 173.3149 173.314900

Acetic Acid 0 0 0 01.5228 242.3311 27.7795 27.7795 377.314900

Methane 0 0 0 0 00.0001 0199.9984 399.997800

Nitrogen Dioxide 0 0 0 0 00.450800000

Sulfur Dioxide 0 0 0 0 07.699800000DAP 0 0 0 0 0 0202.4815 202.4815 202.4815 202.4815 202.4815

2-2-4-TriMth-C5 00000000000

Hydrogen 0 0 0 0 00.2433 0602.1655 1204.33300

Carbon 0 0 0 0 0 0 0 05999.983 5999.983 5999.983

Carbon Monoxide 0 0 0 0 028.2569 0299.9981 599.997200

Ethane 0 0 0 0 0 0 0 0199.999400

Propane 00000000000

HydroxyAcetone 00000000000

Formaldehyde 000000000002-5-Xylenol 00000000000

Sulphur 0 0 0 0 0 0 0 00.524500

Hydroxyacetalde 00000000 1006.6621 00Pyrolignin 00000000 2516.6585 00Levoglucosan 0 0 0 0 0 0 0 0223.702700

Toluene 0 0 0 0 0 0 0 0292.267600

Silicon Dioxide 0 0 0 0 0 0 0900000 900000 900000 09000

26
Stream No. 1123 1124 1126 1127 1130 1131 1132 1133 1134 1135 1137 1138 

Stream NameTemp C 105.3141 1596.2098 963.8307 530 499.2643 68 68.0491 68.0491 68.0491 65.5555 65.5555 45 

Pres bar 1.5648 1.5648 1.5648 1.5648 1.5648 1.5648 2.7369 2.7369 2.7369 2.7369 2.7369 2.3922 Enth MW -9.0077 3.9088 -39.804 -56.964 -22.917 -566.35 4.54E-06 -566.11 -566.11 -566.31 -549.32 -550.86 Vapor mass fraction 1 0 1 10.77193 0 0 0 0 0 0 0 

Total kg/h 120747.026 4604.2961 116142.716 116142.716 10930.3544 165107.24 0.5245 165039.655 165039.13 165039.13 160088 160088 

Flowrates in kg/hGlucose 0.000100000000000

Cellulose 0.0022 0.00040000000000

Xylose 0.000200000000000

Xylan 0.0008 0.00030000000000

Lignin 0.0275 0.00010000000000

Acetate 000000000000

Organism 0.0014 0.00010000000000Solslds 0.0016 0 0.0004 0.0004 0 0000000

Gypsum 20.6919 0.00070000000000Lgnsol 0.0002 00000000000HMF 0 0 0 0 05.4077 05.575 5.575 5.575 5.4077 5.4077 

C5Sugar 0.000300000000000

C6Sugar 0.000800000000000

C5Solid 0.0005 0.00050000000000

C6Solid 0.000100000000000

CaH2O2 2.5726 4400.26460000000000

Ash 3323.1843 1.54770000000000

Ethanol 0 0 0 0 0.1981 0.7751 0 0.7748 0.7748 0.7748 0.7516 0.7516 

Water 0 0 4763.5916 4763.5916 2434.2451 31221.3936 0 31216.7478 31216.7478 31216.7478 30280.2497 30280.2497 

Furfural 0 0 0 0 0.4944 10.2535 0 10.2486 10.2486 10.2486 9.9411 9.9411 

Sulfuric Acid 0 0 0 0 8.8046 293.4858 0 293.4859 293.4859 293.4859 284.6813 284.6813 

Nitrogen 84475.2995 0 84475.1648 84475.1648 191.8275 0.0075 0 0.0075 0.0075 0.0075 0.0072 0.0072 Carbon Dioxide 0 0 22960.5251 22960.5251 1299.9962 1.089 0 1.0887 1.0887 1.0887 1.0561 1.0561 

Oxygen 25620.6228 0 3906.7875 3906.7875 0.0165 0 0 0 0 0 0 0 

Ammonia 000000000000

Lactic Acid 0 0 0 0 173.3149 5765.2605 0 5765.2733 5765.2733 5765.2733 5592.3155 5592.3155 

Acetic Acid 0 0 0 0 377.3149 8194.0744 0 8190.1622 8190.1622 8190.1622 7944.4577 7944.4577 Methane 199.9983 0 0.0001 0.0001 399.9978 0.0376 0 0.0376 0.0376 0.0376 0.0364 0.0364 Nitrogen Dioxide 0 0 0.4508 0.4508 0 0000000

Sulfur Dioxide 0 0 7.6998 7.6998 0 0000000

DAP 202.4815 202.48150000000000

2-2-4-TriMth-C5 000000000000

Hydrogen 602.1654 0 0.2433 0.2433 1204.333 0.0731 0 0.0731 0.0731 0.0731 0.0709 0.0709 

Carbon 5999.983 0.00010000000000

Carbon Monoxide 299.9981 0 28.2569 28.2569 599.9972 0.0343 0 0.0343 0.0343 0.0343 0.0333 0.0333 

Ethane 0 0 0 0 199.9994 0.0171 0 0.0171 0.0171 0.0171 0.0166 0.0166 

Propane 000000000000

HydroxyAcetone 000000000000

Formaldehyde 000000000000

2-5-Xylenol 000000000000

Sulphur 0 0 0 00.5245 0.5245 0.5245 0.52450000

Hydroxyacetalde 0 0 0 0 1006.6621 29589.168 0 29578.3208 29578.3208 29578.3208 28691 28691 

Pyrolignin 0 0 0 0 2516.6585 82451.3562 0 82406.9041 82406.9041 82406.9041 79934.6981 79934.6981 

Levoglucosan 0 0 0 0 223.7027 7171.6759 0 7168.0897 7168.0897 7168.0897 6953.0475 6953.0475 Toluene 0 0 0 0 292.2676 402.5874 0 402.2781 402.2781 402.2781 390.2097 390.2097 

Silicon Dioxide 000000000000

27
Stream No. 1145 1146 1147 1148 1150 1160 1161 1800 1801 1911 1912 19

Stream Name Pyro Oil CWS CWR LP STM 

Temp C 68 68 68 68 70.5453 15.5555 1371.0712 35 40.5555 164 147.574 147.5

Pres bar 1.5648 1.5648 1.5648 1.5648 1.5648 1.2201 1.2201 4.4606 4.1159 4.4583 4.4583 4.45Enth MW -1.0586 -1.0586 -0.52929 -0.52929 -27.193 -24.561 -20.652 -1051.6 -1050.1 -198.33 -230.83 -230Vapor mass fraction 1 1 1 10.22087010010

Total kg/h 2396.1675 2396.1675 1198.0837 1198.0837 8466.0881 5561.496 10165.7917 239351.112 239351.112 54165.173 54165.173 54165.Flowrates in kg/hGlucose 00000000000

Cellulose 0 0 0 0 0 00.00040000

Xylose 00000000000

Xylan 0 0 0 0 0 00.00030000

Lignin 0 0 0 0 0 00.00010000

Acetate 00000000000

Organism 0 0 0 0 0 00.00010000

Solslds 00000000000

Gypsum 0 0 0 0 0 00.00070000

Lgnsol 0 0000000000

HMF 0 0 0 00.1672000000

C5Sugar 00000000000C6Sugar 00000000000C5Solid 0 0 0 0 0 00.00050000

C6Solid 00000000000

CaH2O2 000000 4400.2646 0 0 00

Ash 0 0 0 0 0 01.54770000Ethanol 0 0 0 00.1977000000

Water 0 0 0 0 2429.6004 5561.496 5561.496 239351.112 239351.112 54165.173 54165.173 54165.

Furfural 0 0 0 00.4895000000

Sulfuric Acid 0 0 0 08.8046000000

Nitrogen 191.8273 191.8273 95.9136 95.9136 0.0002 000000

Carbon Dioxide 0 0 0 0 1299.9966 000000

Oxygen 0.0165 0.0165 0.0082 0.0082 0 000000

Ammonia 00000000000

Lactic Acid 0 0 0 0173.3273000000

Acetic Acid 0 0 0 0373.4028000000

Methane 399.9966 399.9966 199.9983 199.9983 0.0011 000000

Nitrogen Dioxide 0 0000000000

Sulfur Dioxide 00000000000

DAP 0 0 0 0 0 0202.48150000

2-2-4-TriMth-C5 00000000000

Hydrogen 1204.3308 1204.3308 602.1654 602.1654 0.0022 000000

Carbon 0 0 0 0 0 00.00010000

Carbon Monoxide 599.9962 599.9962 299.9981 299.9981 0.001 000000

Ethane 0 0 0 0199.9995000000

Propane 00000000000

HydroxyAcetone 00000000000

Formaldehyde 00000000000

2-5-Xylenol 00000000000

Sulphur 00000000000

Hydroxyacetalde 0 0 0 0995.8152000000

Pyrolignin 0 0 0 0 2472.2078 000000

Levoglucosan 0 0 0 0220.1161000000

Toluene 0 0 0 0291.9584000000

Silicon Dioxide 00000000000

28
Stream No. 1924 1925 2217 2227 2228 2230 2239 2240 2241 2520 2521 25

Stream Name FILTRATE H-244 Vapor 

Temp C 147.574 147.574 197.7722 49.8868 50 52.5328 52.5328 50 35.0121 99.8733 35 35.0

Pres bar 4.4583 4.4583 39.7802 1 1.0132 1.0132 2.0265 1 1 1.0132 1.0132 

Enth MW -28.21 -28.21 -736.32 -924.98 -926.07 -907.13 -927.95 -916.35 -173.22 -164.81 -172.53 -173Vapor mass fraction 0 0 01.73E-06 01.78E-06 01.76E-06 00.195120

Total kg/h 6611.818 6611.818 217282.68 238116 238116 232834 238967.372 235784.061 39993.296 39835.1765 39835.1765 39993.2

Flowrates in kg/hGlucose 0 0 0 1771.9691 1771.9691 1762.618 1771.9691 1771.9691 0 0 0 

Cellulose 0 0 24261.5609 111.1394 111.1394 0.5557 111.1394 111.1394 0 0 0 

Xylose 0 0 0 13169.903 13169.903 13100.4023 13169.903 13169.903 0 0 0 

Xylan 0 0 13666.3191 1.7114 1.7114 0.0086 1.7114 1.7114 0 0 0 Lignin 0 0 11670.1175 55.6571 55.6571 0.2783 55.6571 55.6571 0 0 0 

Acetate 0 01901.709300000000

Organism 0 0 0 0 0 0 0 0 0 0 0 

Solslds 0 0 5875.4781 6861.7527 6861.7527 6825.5415 6861.7527 6861.7527 0 00Gypsum 0 0 0 0 2728.0646 21.1142 4222.8586 0 0 0 0 

Lgnsol 0 0 0 683.8315 683.8315 680.2227 683.8315 683.8315 0 0 0 

HMF 0 0 0.0201 112.9064 112.9064 112.3106 112.9064 112.9064 0.1609 0.1608 0.1608 0.16

C5Sugar 0 0 02341.334 2341.334 2328.9784 2341.334 2341.334 0 0 0 

C6Sugar 0 0 0 2865.4715 2865.4715 2850.3496 2865.4715 2865.4719 0 00C5Solid 0 01895.8035 0 0 0 0 0 0 0 0 

C6Solid 0 02267.8775 0 0 0 0 0 0 0 0 

CaH2O2 0 0 0 2331.7899 1157.7868 2.5725 514.5127 0 0 00

Ash 0 0 3390.0019 17.0227 17.0227 0.0851 17.0227 17.0227 0 0 0 

Ethanol 0 0 73.8375 31.911 31.911 31.7426 31.911 31.911 58.1217 58.0866 58.0866 58.12

Water 6611.818 6611.818 149408.337 202007.447 202007.447 200941.406 202007.447 202007.447 39146.5666 38990.1268 38990.1268 39146.56Furfural 0 0 127.5213 392.6971 392.6971 390.6247 392.697 392.6971 345.2103 344.9017 344.9017 345.2

Sulfuric Acid 0 0 1641.1199 1554.0614 0 0 0 1554.0614 0 0 0 

Nitrogen 0 0 0 1.8626 1.8626 1.8527 1.8626 1.8626 0.0016 0 0 0.00

Carbon Dioxide 0 0 0 0.3966 0.3966 0.3945 0.3966 0.3966 0.0004 0 0 0.00

Oxygen 0 0 0 1.0972 1.0972 1.0914 1.0972 1.0972 0.0009 0 0 0.00Ammonia 00000000000

Lactic Acid 0 0 1.3482 571.7846 571.7846 568.7671 571.7845 571.7846 0.0029 0.0023 0.0023 0.00

Acetic Acid 0 0 1101.6335 3230.1278 3230.1278 3213.0816 3230.1278 3230.1281 443.2338 441.8991 441.8991 443.23

29
Stream No. 5251 5511 5518 5519 5520 5521 5523 5525 5571 5618 6110 6

Stream Name To T-914 BFW To DeareaTemp C 74.1511 122.534 86.9859 116 37 70.9641 70.9722 87.1343 63.4809 120.3871 137 179.88

Pres bar 2.0265 2.1305 0.6181 1.6779 1.0132 1.5513 1.7225 2.0265 3.2424 2.0272 10 Enth MW -240.8 -1197.8 -1199.7 -13.978 -32.077 -16.538 -16.538 -916.77 -275.25 -125.45 -123.14 -111Vapor mass fraction 0 00.053693 1 0 0 0 0 02.59E-06 00.600

Total kg/h 55743.0011 303483 303483 6740.1483 19091.7542 6740.1483 6740.1483 235470.714 79735.2309 29525.0963 28809.6111 28809.6

Flowrates in kg/hGlucose 0 63.9846 63.9846 0 0 0 0 63.9846 56.8544 0 0 

Cellulose 0 840.5 840.5 0 0 0 0 840.5 16.1736 0 0 

Xylose 0 748.5122 748.5121 0 0 0 0 748.5121 648.1553 0 0 

Xylan 0 340.7353 340.7353 0 0 0 0 340.7353 6.5567 0 0 

Lignin 0 11086.6135 11086.6135 0 0 0 0 11086.6135 213.3372 0 0 

Acetate 0 0 0 0 0 0 0 0 0 0 0 

Organism 0 1155.4586 1155.4586 0 0 0 0 1155.4586 555.8557 0 0 

Solslds 0 7562.3115 7562.3115 0 0 0 0 7562.3115 6719.6051 0 0 

Gypsum 0 21.1142 21.1142 0 0 0 0 21.1142 0.4063 0 0 

Lgnsol 0 753.8397 753.8397 0 0 0 0 753.8397 669.8356 0 0 

HMF 0.115 124.0108 124.0108 0 0 0 0 123.844 109.8329 0.0888 0 

C5Sugar 0 1119.4754 1119.4754 0 0 0 0 1119.4754 994.7265 0 0 

C6Sugar 0 2966.165 2966.165 0 0 0 0 2966.165 2568.4759 0 0 

C5Solid 0 222.7605 222.7605 0 0 0 0 222.7605 4.2865 0 0 

C6Solid 0 56.697 56.697 0 0 0 056.697 1.091 0 0 

CaH2O2 0 2.5726 2.5726 0 0 0 0 2.5726 0 00

Ash 0 3391.0043 3391.0043 0 0 0 0 3391.0043 65.2523 0 0 

Ethanol 45.0873 151.7402 151.743 4716.0304 18982.6157 4716.0304 4716.0304 31.1905 0.3324 14.7626 0 

Water 55096.5895 265991.385 265991.385 2024.1179 107.9716 2024.1179 2024.1179 198777.387 63064.5348 29094.0773 28809.6111 28809.6Furfural 61.7581 213.5954 213.5969 0 0.0591 0 0 70.2409 3.1367 236.1192 0 

Sulfuric Acid 0 115.139 115.139 0 0 0 0115.139 102.3085 0 0 Nitrogen 0 0 0 0 0 0 0 0 0 0 0 

Carbon Dioxide 0 0 0 01.1096 0 0 0 0 0 0 

Oxygen 0 0 0 0 0 0 0 0 0 0 0 

Ammonia 00000000000

Lactic Acid 1.733 2268.6788 2268.679 0 0 0 0 2266.4819 2010.4273 1.3676 0 

Acetic Acid 537.7159 4084.1736 4084.1727 0 0 0 0 3552.2003 1924.0465 178.6808 0 

Methane 0 0 0 0 0 0 0 0 0 0 0 

Nitrogen Dioxide 0 0000000000

Sulfur Dioxide 00000000000

DAP 0 202.4815 202.4815 0 0 0 0 202.4815 0 00

30
Stream No. 8040 8042 8043 8044 8045 8047 8049 8597 8692 8812 8813 88

Stream Name FLUE GAS Mol SieveTemp C 165.3185 25.0489 220 48.7963 820 639.5961 270 147.74 120.6474 267.9948 177 307.92Pres bar 0.9686 1.0234 1 1 0.9686 0.9686 0.9686 4.4786 2.0265 13.1722 98.9236 98.23

Enth MW -429.03 -0.01048 10.351 -326.68 -349.28 -372.63 -417.2 -2.1204 -6.2795 -448.67 -541.4 -518Vapor mass fraction 1 1 10.76943 1 1 1 0 0 1 0 

Total kg/h 317001.079 205000 213776.27 316989.512 317001.136 317001.079 317001.079 497 1460.8174 124160 128000 1280Flowrates in kg/hGlucose 0 0 056.85440000000Cellulose 0 0 07015.21840000000

Xylose 0 0 0648.15530000000

Xylan 0 0 03949.05530000000

Lignin 0 0 03579.9660000000

Acetate 0 0 0548.61060000000

Organism 0 0 0555.85570000000

Solslds 0 0 08383.75040000000

Gypsum 0.4063 0 00.4063 0.4063 0.4063 0.40630000

Lgnsol 0 0 0 669.8354 0 000000

HMF 0 0 0.0001 109.833 0 000000C5Sugar 0 0 0994.72630000000C6Sugar 0 0 02568.47570000000C5Solid 0 0 0551.19340000000

C6Solid 0 0 0655.33480000000

CaH2O2 00000000000

Ash 1043.2097 0 0 1043.2097 1043.2097 1043.2097 1043.2097 0 0 00

Ethanol 0 0 1.1023 1.497 0 000000

Water 83693 0 391.1629 67009.0732 83693 83693 83693 497 1460.8174 124160 128000 1280Furfural 0 0 4.1699 7.3065 0 000000Sulfuric Acid 102.3084 0 0102.3085 102.3085 102.3084 102.30840000

Nitrogen 168969.777 161950 168469 168469 168969.792 168969.777 168969.777 0 0 00

Carbon Dioxide 51734.942 0 17.9352 895.1807 51735 51734.942 51734.942 0 0 00Oxygen 11430.4258 43050.0018 44890.871 44890.8745 11430.4329 11430.4258 11430.4258 0 0 00Ammonia 00000000000

Lactic Acid 0 0 0.0009 2010.4286 0 000000

Acetic Acid 0 0 2.0409 1926.0861 0 000000Methane 0 0 0347.25690000000

Nitrogen Dioxide 0 0000000000

Sulfur Dioxide 00000000000

DAP 00000000000

2-2-4-TriMth-C5 27.0875 0 0 027.0875 27.0875 27.08750000

31
32

Stream No. 8821 8823 8830 8872 8873 9611Stream Name BLR BLOWDOWN TO U1100

Temp C 321 267.9948 267.9948 137 137 179.8844Pres bar 113.484 13.1722 13.1722 3.3437 3.3437 10

Enth MW -16.67 -36.136 -307.58 -123.28 -547.74 -111.95Vapor mass fraction 1 1 1 0 0 0.60031

Total kg/h 4521 10000.001 85117.4729 28809.9194 128000 28809.6111Flowrates in kg/hGlucose 0 0 0 0 0 0

Cellulose 000000

Xylose 000000

Xylan 000000

Lignin 000000

Acetate 0 0 0 0 0 0

Organism 000000

Solslds 0 0 0 0 0 0

Gypsum 000000

Lgnsol 0 0 0 0 0 0

HMF 000000

C5Sugar 000000

C6Sugar 000000

C5Solid 000000

C6Solid 000000

CaH2O2 000000

Ash 000000

Ethanol 0 0 0 0 0 0

Water 4521 10000.001 85117.4729 28809.9194 128000 28809.6111Furfural 000000

Sulfuric Acid 000000

Nitrogen 000000

Carbon Dioxide 000000

Oxygen 000000

Ammonia 000000Lactic Acid 000000

Acetic Acid 000000