Process for Reduction of Energy Consumption During the Pretreatment of Biomass

Abstract

The present invention relates to a process for reduction of energy consumption during the pretreatment of biomass.

Claims

1. Process for reduction of energy consumption during the pretreatment of biomass characterized in that the feedstock processing parameter FPP is selected within the range of from 1.5 to 7.0 $\frac{k.Math.g*\sqrt{\%}}{h*{\mathrm{mm}}^2}.$

2. Process according to claim 1, wherein the feedstock processing parameter FPP is selected within the range of from 2.0 to 4.5 $\frac{k.Math.g*\sqrt{\%}}{h*{\mathrm{mm}}^2}.$

3. Process according to any of the foregoing claims, wherein the biomass is lignocellulosic biomass.

4. Process according to any of the foregoing claims, wherein the pretreatment resistance parameter PRP of the biomass is selected within the range of from 0.002 to 1.000 $\frac{h}{\mathrm{kg}*\sqrt{\%}}.$

5. Process according to claim 4, wherein the pretreatment resistance parameter PRP of the biomass is selected within the range of from 0.003 to 0.80 $\frac{h}{\mathrm{kg}*\sqrt{\%}}.$

6. Process according to any of the foregoing claims, wherein the biomass has a lignin to glucose ratio of from 0.35 to 0.60 wt.-%

7. Process according to any of the foregoing claims, wherein the moisture content of the biomass is selected within the range of from 5 to 60 wt.-%.

8. Process according to any of the foregoing claims, wherein the xylose content of the biomass is selected within the range of from 10.0 to 30.0 wt.-%.

9. Process according to any of the foregoing claims, wherein the steam pressure is selected within the range of from 8.0 to 15.0 bar.

10. Process according to any of the foregoing claims, wherein the biomass pretreatment is carried out for a time selected from the range of from 1 minute to 20 minutes.

Description

FIGURES AND EXAMPLES

[0040] The following examples and figures illustrate preferred embodiments of the invention but are not limiting the scope of the invention or claims.

[0041] FIG. 1 shows a preferred location and embodiment of the outletarea OA of a steam explosion pretreatment reactor

[0042] FIG. 2 shows a preferred embodiment of a nozzle equipment

[0043] Within FIG. 1 the reference number (1) is indicating the outlet area OA, reference number (2) is indicating a pipeline for conveying the pretreated biomass material to a second device, reference number (3) is indicating the outer wall of the pretreatment reactor (4) and reference number (5) is indicating a flange for fixation of the pipeline (2) to the reactor (4).

[0044] The composition of the biomass material was analyzed according to the NREL (National Renewable Energy Laboratory, USA) and ASE (Alliance for Sustainable Energy, LLC for the Department Of Energy) method: Determination of Structural Carbohydrates and Lignin on Biomass, Version 08-03-2012.

[0045] The following components have been determined:

Dry matter content (DM)
Glucose (cellulose, glucan)
Xylose (xylan)

Ash

[0046] Lignin (insoluble in acid)

[0047] The results were adjusted by subtraction of the ash content for precise reference

Exemplary calculation for example 1-0:
Dry matter content: 85.0%

Glucose (Cellulose, Glucan): 33.2%=>33.2%/((1006.0%)/100)=35.3%

Xylose (Xylan) 21.3%=>21.3%/((1006.0%)/100)=22.7%

Ash 6.0%

[0048] Lignin (insoluble in acid) 15.6%=>15.6%/((1006.0%)/100)=16.6%
Moisture content was calculated by deduction of the DM measured: 15 wt.-%

Example 1-0 (Comparative) Wheat Straw (Moisture 15 wt.-%) FPP 0.7

[0049] [00024]$\frac{\mathrm{kg}*\sqrt{\%}}{h*{\mathrm{mm}}^2}$

[0050] Wheat straw bales were loosened up in a bale crusher (Tietjen) equipped with rotation scrappers operated at 3000 rpm yielding particles with particle sizes from 10 to 40 cm. This particle size ensures smooth transport of the material and operation of the subsequent milling step. The biomass material was pneumatically transported to a hammer mill (Tietjen VDK 4.1) operated at 3000 rpm with 30 mm sieves where the wheat straw was cut to pieces with an average particle sizes of from 1 to 5 cm.

[0051] The cut wheat straw was transported to the thermal pre-treatment reactor with a pin drum feeder (Metso; PDF 2545) followed by a transportation screw (Metso; FFS 211) and plug screw (Metso; ADI 180). The pin drum feeder adjusted a mass flow {dot over (m)} of 400 kg (DM)/h. The wheat straw had a dry matter content of 85 wt.-%, a xylose content of 22.7 wt.-% and a lignin content of 16.6 wt.-% resulting in a PRP of 0.47

[00025]$\left(\frac{h}{\mathrm{kg}*\sqrt{\%}}\right).$

[0052] In the pretreatment reactor vessel (Metso; RHA 740) the wheat straw was continuously pre-treated with steam at a temperature of 160 C. for 5 min without addition of any chemicals. The steam consumption was measured by Vortex Flowmeter Proline from Endress & Hauser at 1.755 kg/h. After this hydrothermal pre-treatment, the pretreated wheat straw was transported to a cyclone (Schrader; DN1200) to separate the organic materials from the gases.

[0053] The pretreatment reactor vessel had an outlet with a cross-sectional area of about 283 mm.sup.2 and the FPP (Feedstock Processing Parameter) was selected 0.7

[00026]$\frac{\mathrm{kg}*\sqrt{\%}}{h*{\mathrm{mm}}^2}$

The used steam amount per 1 kg DM was measured to 4.4 kg. Results are shown in table 5.

Example 1-A Wheat Straw (Moisture 15 wt.-%) FPP 3.3

[0054] [00027]$\frac{\mathrm{kg}*\sqrt{\%}}{h*{\mathrm{mm}}^2}$

[0055] Preparation of the Biomass was carried out as defined in example 1-0. The composition was identical to example 1-0 (PRP=0.47

[00028]$\left(\frac{h}{\mathrm{kg}*\sqrt{\%}}\right).$

[0056] The FPP (Feedstock Processing Parameter) was modified to 3.3

[00029]$\frac{\mathrm{kg}*\sqrt{\%}}{h*{\mathrm{mm}}^2}$

by adapting the outlet area to 65 mm.sup.2. The steam consumption was measured to amount to 403 kg/h and corresponded to a specific steam consumption of 1.0 kg per 1 kg DM, which represented an effective reduction of steam consumption of 77% in comparison to example 1-0. Results are shown in table 5.

Example 1-B Wheat Straw (Moisture 15 wt.-%) FPP 2.3

[0057] [00030]$\frac{\mathrm{kg}*\sqrt{\%}}{h*{\mathrm{mm}}^2}$

[0058] Preparation of the Biomass was carried out as defined in example 1-0. The wheat straw had a dry matter content of 85 wt.-%, a xylose content of 21.3 wt.-% and a lignin content of 15.6 wt.-% resulting in a PRP of 0.47

[00031]$\left(\frac{h}{\mathrm{kg}*\sqrt{\%}}\right).$

The FPP (Feedstock Processing Parameter) was modified to 2.3

[00032]$\frac{\mathrm{kg}*\sqrt{\%}}{h*{\mathrm{mm}}^2}$

by adapting the outlet area to 90 mm.sup.2. The steam consumption was measured to amount to 558 kg/h and corresponded to a specific steam consumption of 1.4 kg per 1 kg DM, which represented an effective reduction of steam consumption of 68.2% in comparison to example 1-0. Results are shown in table 5.

Example 1-C Wheat Straw (Moisture 15 wt.-%) FPP 7.0

[0059] [00033]$\frac{\mathrm{kg}*\sqrt{\%}}{h*{\mathrm{mm}}^2}$

[0060] Preparation of the Biomass was carried out as defined in example 1-0. The composition was identical to example 1-B (PRP=0.47

[00034]$\left(\frac{h}{\mathrm{kg}*\sqrt{\%}}\right).$

[0061] The FPP (Feedstock Processing Parameter) was modified to 7.0

[00035]$\frac{\mathrm{kg}*\sqrt{\%}}{h*{\mathrm{mm}}^2}$

by adapting the outlet area to 30 mm.sup.2. The steam consumption was measured to amount to 186 kg/h and corresponded to a specific steam consumption of 0.5 kg per 1 kg DM. Results are shown in table 5.

Example 1-D Wheat Straw (Moisture 20 wt.-%) FPP 3.7

[0062] [00036]$\frac{\mathrm{kg}*\sqrt{\%}}{h*{\mathrm{mm}}^2}$

[0063] Preparation of the Biomass was carried out as defined in example 1-0. The wheat straw had a dry matter content of 80 wt.-%, a xylose content of 21.3 wt.-% and a lignin content of 15.6 wt.-% resulting in a PRP of 0.41

[00037]$\left(\frac{h}{\mathrm{kg}*\sqrt{\%}}\right).$

[0064] The FPP (Feedstock Processing Parameter) was modified to 3.7

[00038]$\frac{\mathrm{kg}*\sqrt{\%}}{h*{\mathrm{mm}}^2}$

by adapting the outlet area to 65 mm.sup.2. The steam consumption was measured to amount to 403 kg/h and corresponded to a specific steam consumption of 1.0 kg per 1 kg DM, which represented an effective reduction of steam consumption of 77.0% in comparison to example 1-0. Results are shown in table 5.

Example 1-E Wheat Straw (Moisture 10 wt.-%) FPP 2.3

[0065] [00039]$\frac{\mathrm{kg}*\sqrt{\%}}{h*{\mathrm{mm}}^2}$

[0066] Preparation of the Biomass was carried out as defined in example 1-0. The wheat straw had a dry matter content of 90 wt.-%, a xylose content of 20.0 wt.-% and a lignin content of 17.0 wt.-% resulting in a PRP of 0.67

[00040]$\left(\frac{h}{\mathrm{kg}*\sqrt{\%}}\right).$

[0067] The FPP (Feedstock Processing Parameter) was modified to 2.3

[00041]$\frac{\mathrm{kg}*\sqrt{\%}}{h*{\mathrm{mm}}^2}$

by adapting the outlet area to 65 mm.sup.2. The steam consumption was measured to amount to 403 kg/h and corresponded to a specific steam consumption of 1.0 kg per 1 kg DM, which represented an effective reduction of steam consumption of 77.0% in comparison to example 1-0. Results are shown in table 5.

Example 2-0 (Comparative) Wheat Straw (Moisture 15 wt.-%) FPP 0.8

[0068] [00042]$\frac{\mathrm{kg}*\sqrt{\%}}{h*{\mathrm{mm}}^2}$

[0069] Wheat straw bales were loosened up in a bale crusher (Tietjen) equipped with rotation scrappers operated at 3000 rpm yielding particles with particle sizes from 10 to 40 cm. This particle size ensures smooth transport of the material and operation of the subsequent milling step. The biomass material was pneumatically transported to a hammer mill (Tietjen) operated at 3000 rpm with 30 mm sieves where the wheat straw was cut to pieces with an average particle sizes of from 1 to 5 cm.

[0070] The cut wheat straw was transported to the thermal pre-treatment reactor with a pin drum feeder (Metso) followed by a transportation screw (Metso) and plug screw (Metso). The pin drum feeder adjusted a mass flow {dot over (m)} of 25,000 kg (DM)/h. The composition was identical to example 1-B (PRP=0.008

[00043]$\left(\frac{h}{\mathrm{kg}*\sqrt{\%}}\right).$

[0071] In the pretreatment reactor vessel (Metso) the wheat straw was continuously pre-treated with steam at a temperature of 160 C. for 5 min without addition of any chemicals. The steam consumption was measured by Vortex Flowmeter Proline from Endress & Hauser at 1.755 kg/h. After this hydrothermal pre-treatment, the pretreated wheat straw was transported to a cyclone (Schrader) to separate the organic materials from the gases.

[0072] The FPP (Feedstock Processing Parameter) was modified to 0.8

[00044]$\frac{\mathrm{kg}*\sqrt{\%}}{h*{\mathrm{mm}}^2}$

by adapting the outlet area to 16,000 mm.sup.2. The steam consumption was measured to amount to 99,200 kg/h and corresponded to a specific steam consumption of 4.0 kg per 1 kg DM. Results are shown in table 5.

Example 2-A Wheat Straw (Moisture 15 wt.-%) FPP 3.1

[0073] [00045]$\frac{\mathrm{kg}*\sqrt{\%}}{h*{\mathrm{mm}}^2}$

[0074] Preparation of the Biomass was carried out as defined in example 2-0. The composition was identical to example 2-0 (PRP=0.008

[00046]$\left(\frac{h}{\mathrm{kg}*\sqrt{\%}}\right).$

[0075] The FPP (Feedstock Processing Parameter) was modified to 3.1

[00047]$\frac{\mathrm{kg}*\sqrt{\%}}{h*{\mathrm{mm}}^2}$

by adapting the outlet area to 4,200 mm.sup.2. The steam consumption was measured to amount to 26,040 kg/h and corresponded to a specific steam consumption of 1.0 kg per 1 kg DM which represented an effective reduction of steam consumption of 73.8% in comparison to example 2-0. Results are shown in table 5.

Example 3-0 (Comparative) Corn Stover (Moisture 17 wt.-%) FPP 0.6

[0076] [00048]$\frac{\mathrm{kg}*\sqrt{\%}}{h*{\mathrm{mm}}^2}$

[0077] Preparation of the Biomass was carried out as defined in example 1-0. The corn stover had a dry matter content of 83 wt.-%, a xylose content of 19.7 wt.-% and a lignin content of 17.8 wt.-% resulting in a PRP of 0.547

[00049]$\left(\frac{h}{\mathrm{kg}*\sqrt{\%}}\right).$

The FPP (Feedstock Processing Parameter) was modified to 0.6

[00050]$\frac{\mathrm{kg}*\sqrt{\%}}{h*{\mathrm{mm}}^2}$

by adapting the outlet area to 283 mm.sup.2. The steam consumption was measured to amount to 1811 kg/h and corresponded to a specific steam consumption of 4.5 kg per 1 kg DM. Results are shown in table 5.

Example 3-A Corn Stover (Moisture 17 wt.-%) FPP 0.6

[0078] [00051]$\frac{\mathrm{kg}*\sqrt{\%}}{h*{\mathrm{mm}}^2}$

[0079] Preparation of the Biomass was carried out as defined in example 1-0. The corn stover was identical to example 3-0 (PRP of 0.547

[00052]$\left(\frac{h}{\mathrm{kg}*\sqrt{\%}}\right)).$

The FPP (Feedstock Processing Parameter) was modified to 2.9

[00053]$\frac{\mathrm{kg}*\sqrt{\%}}{h*{\mathrm{mm}}^2}$

by adapting the outlet area to 63 mm.sup.2. The steam consumption was measured to amount to 403 kg/h and corresponded to a specific steam consumption of 1.0 kg per 1 kg DM which represented an effective reduction of steam consumption of 77.7% in comparison to example 3-0. Results are shown in table 5.

Example 3-B Corn Stover (Moisture 30 wt.-%) FPP 0.6

[0080] [00054]$\frac{\mathrm{kg}*\sqrt{\%}}{h*{\mathrm{mm}}^2}$

[0081] Preparation of the Biomass was carried out as defined in example 1-0. The corn stover had a dry matter content of 70 wt.-%, a xylose content of 19.7 wt.-% and a lignin content of 17.8 wt.-% resulting in a PRP of 0.412

[00055]$\left(\frac{h}{\mathrm{kg}*\sqrt{\%}}\right).$

The FPP (Feedstock Processing Parameter) was modified to 3.6

[00056]$\frac{\mathrm{kg}*\sqrt{\%}}{h*{\mathrm{mm}}^2}$

by adapting the outlet area to 67 mm.sup.2. The steam consumption was measured to amount to 429 kg/h and corresponded to a specific steam consumption of 1.1 kg per 1 kg DM which represented an effective reduction of steam consumption of 76.3% in comparison to example 3-0. Results are shown in table 5.

Example 4-0 (Comparative) Corn Stover (Moisture 17 wt.-%) FPP 0.7

[0082] [00057]$\frac{\mathrm{kg}*\sqrt{\%}}{h*{\mathrm{mm}}^2}$

[0083] Preparation of the Biomass was carried out as defined in example 2-0. The corn stover was identical to example 3-0 resulting in a PRP of 0.009

[00058]$\left(\frac{h}{\mathrm{kg}*\sqrt{\%}}\right).$

The FPP (Feedstock Processing Parameter) was modified to 0.7

[00059]$\frac{\mathrm{kg}*\sqrt{\%}}{h*{\mathrm{mm}}^2}$

by adapting the outlet area to 16,000 mm.sup.2. The steam consumption was measured to amount to 102,400 kg/h and corresponded to a specific steam consumption of 4.1 kg per 1 kg DM. Results are shown in table 5.

Example 4-A Corn Stover (Moisture 17 wt.-%) FPP 3.0

[0084] [00060]$\frac{\mathrm{kg}*\sqrt{\%}}{h*{\mathrm{mm}}^2}$

[0085] Preparation of the Biomass was carried out as defined in example 4-0. The corn stover was identical to example 3-0 resulting in a PRP of 0.009

[00061]$\left(\frac{h}{\mathrm{kg}*\sqrt{\%}}\right).$

The FPP (Feedstock Processing Parameter) was modified to 3.0

[00062]$\frac{\mathrm{kg}*\sqrt{\%}}{h*{\mathrm{mm}}^2}$

by adapting the outlet area to 3,800 mm.sup.2. The steam consumption was measured to amount to 24,320 kg/h and corresponded to a specific steam consumption of 1.0 kg per 1 kg DM which represented an effective reduction of steam consumption of 76.3% in comparison to example 4-0. Results are shown in table 5.

Example 5-0 (Comparative) Barley Straw (Moisture 13 wt.-%) FPP 0.7

[0086] [00063]$\frac{\mathrm{kg}*\sqrt{\%}}{h*{\mathrm{mm}}^2}$

[0087] Preparation of the Biomass was carried out as defined in example 1-0. The barley straw had a dry matter content of 87 wt.-%, a xylose content of 18.8 wt.-% and a lignin content of 14.2 wt.-% resulting in a PRP of 0.521

[00064]$\left(\frac{h}{\mathrm{kg}*\sqrt{\%}}\right).$

The FPP (Feedstock Processing Parameter) was modified to 0.7

[00065]$\frac{\mathrm{kg}*\sqrt{\%}}{h*{\mathrm{mm}}^2}$

by adapting the outlet area to 283 mm.sup.2. The steam consumption was measured to amount to 1,641 kg/h and corresponded to a specific steam consumption of 4.1 kg per 1 kg DM. Results are shown in table 5.

Example 5-A Barley Straw (Moisture 13 wt.-%) FPP 2.9

[0088] [00066]$\frac{\mathrm{kg}*\sqrt{\%}}{h*{\mathrm{mm}}^2}$

[0089] Preparation of the Biomass was carried out as defined in example 5-0. The barley straw was identical to example 5-0 resulting in a PRP of 0.521

[00067]$\left(\frac{h}{\mathrm{kg}*\sqrt{\%}}\right).$

The FPP (Feedstock Processing Parameter) was modified to 2.9

[00068]$\frac{\mathrm{kg}*\sqrt{\%}}{h*{\mathrm{mm}}^2}$

by adapting the outlet area to 66 mm.sup.2. The steam consumption was measured to amount to 383 kg/h and corresponded to a specific steam consumption of 1.0 kg per 1 kg DM which represented an effective reduction of steam consumption of 76.7% in comparison to example 5-0. Results are shown in table 5.

Example 6-0 (Comparative) Barley Straw (Moisture 13 wt.-%) FPP 0.7

[0090] [00069]$\frac{\mathrm{kg}*\sqrt{\%}}{h*{\mathrm{mm}}^2}$

[0091] Preparation of the Biomass was carried out as defined in example 2-0. The barley straw was identical to example 5-0 resulting in a PRP of 0.008

[00070]$\left(\frac{h}{\mathrm{kg}*\sqrt{\%}}\right).$

The FPP (Feedstock Processing Parameter) was modified to 0.7

[00071]$\frac{\mathrm{kg}*\sqrt{\%}}{h*{\mathrm{mm}}^2}$

by adapting the outlet area to 16,000 mm.sup.2. The steam consumption was measured to amount to 92,800 kg/h and corresponded to a specific steam consumption of 3.7 kg per 1 kg DM. Results are shown in table 5.

Example 6-A Barley Straw (Moisture 13 wt.-%) FPP 2.7

[0092] [00072]$\frac{\mathrm{kg}*\sqrt{\%}}{h*{\mathrm{mm}}^2}$

[0093] Preparation of the Biomass was carried out as defined in example 6-0. The barley straw was identical to example 6-0 resulting in a PRP of 0.008

[00073]$\left(\frac{h}{\mathrm{kg}*\sqrt{\%}}\right).$

The FPP (Feedstock Processing Parameter) was modified to 2.7

[00074]$\frac{\mathrm{kg}*\sqrt{\%}}{h*{\mathrm{mm}}^2}$

by adapting the outlet area to 4,500 mm.sup.2. The steam consumption was measured to amount to 26,100 kg/h and corresponded to a specific steam consumption of 1.0 kg per 1 kg DM which represented an effective reduction of steam consumption of 71.9% in comparison to example 6-0. Results are shown in table 5.

Example 7-0 (Comparative) Bagasse (Moisture 40 wt.-%) FPP 1.0

[0094] [00075]$\frac{\mathrm{kg}*\sqrt{\%}}{h*{\mathrm{mm}}^2}$

[0095] Preparation of the Biomass was carried out as defined in example 1-0. The bagasse had a dry matter content of 60 wt.-%, a xylose content of 22.0 wt.-% and a lignin content of 19.2 wt.-% resulting in a PRP of 0.345

[00076]$\left(\frac{h}{\mathrm{kg}*\sqrt{\%}}\right).$

The FPP (Feedstock Processing Parameter) was modified to 1.0

[00077]$\frac{k.Math.g*\sqrt{\%}}{h*{\mathrm{mm}}^2}$

by adapting the outlet area to 283 mm.sup.2. The steam consumption was measured to amount to 1,557 kg/h and corresponded to a specific steam consumption of 3.9 kg per 1 kg DM. Results are shown in table 5.

Example 7-A Bagasse (Moisture 40 wt.-%) FPP 3.9

[0096] [00078]$\frac{k.Math.g*\sqrt{\%}}{h*{\mathrm{mm}}^2}$

[0097] Preparation of the Biomass was carried out as defined in example 7-0. The bagasse was identical to example 7-0 resulting in a PRP of 0.345

[00079]$\left(\frac{h}{\mathrm{kg}*\sqrt{\%}}\right).$

The FPP (Feedstock Processing Parameter) was modified to 3.9

[00080]$\frac{k.Math.g*\sqrt{\%}}{h*{\mathrm{mm}}^2}$

by adapting the outlet area to 74 mm.sup.2. The steam consumption was measured to amount to 407 kg/h and corresponded to a specific steam consumption of 1.0 kg per 1 kg DM which represented an effective reduction of steam consumption of 73.9% in comparison to example 7-0. Results are shown in table 5.

Example 8-0 (Comparative) Bagasse (Moisture 40 wt.-%) FPP 1.1

[0098] [00081]$\frac{k.Math.g*\sqrt{\%}}{h*{\mathrm{mm}}^2}$

[0099] Preparation of the Biomass was carried out as defined in example 2-0. The bagasse was identical to example 7-0 resulting in a PRP of 0.006

[00082]$\left(\frac{h}{\mathrm{kg}*\sqrt{\%}}\right).$

The FPP (Feedstock Processing Parameter) was modified to 1.1

[00083]$\frac{k.Math.g*\sqrt{\%}}{h*{\mathrm{mm}}^2}$

by adapting the outlet area to 16,000 mm.sup.2. The steam consumption was measured to amount to 88,000 kg/h and corresponded to a specific steam consumption of 3.5 kg per 1 kg DM. Results are shown in table 5.

Example 8-A Bagasse (Moisture 40 wt.-%) FPP 3.8

[0100] [00084]$\frac{k.Math.g*\sqrt{\%}}{h*{\mathrm{mm}}^2}$

[0101] Preparation of the Biomass was carried out as defined in example 8-0. The bagasse was identical to example 8-0 resulting in a PRP of 0.006

[00085]$\left(\frac{h}{\mathrm{kg}*\sqrt{\%}}\right).$

The FPP (Feedstock Processing Parameter) was modified to 3.8

[00086]$\frac{k.Math.g*\sqrt{\%}}{h*{\mathrm{mm}}^2}$

by adapting the outlet area to 4,750 mm.sup.2. The steam consumption was measured to amount to 26,125 kg/h and corresponded to a specific steam consumption of 1.0 kg per 1 kg DM which represented an effective reduction of steam consumption of 70.3% in comparison to example 8-0. Results are shown in table 5.

TABLE-US-00005 TABLE 5 Exam- ple Xylose (Xylan) [wt. %] Lignin [wt. %] Moisture [wt. %] Mass Flow {dot over (m)} [kg/h] Outlet area OA [mm.sup.2] [00087]$\begin{array}{c}\mathrm{PRP}\\ \left[\frac{h}{\mathrm{kg}*\sqrt{\%}}\right]\end{array}$ Steam Consumption [kg/ (mm.sup.2 * h)] Steam Consump- tion [kg/h] Steam Consumption [kg(steam)/ kg(TS)] Steam Saving [%] [00088]$\begin{array}{c}\mathrm{FPP}\\ \left[\frac{\mathrm{kg}*\sqrt{\%}}{h*{\mathrm{mm}}^2}\right]\end{array}$ 1-0 22.7 16.6 15 400 283 0.47 6.2 1,755 4.4 0.7 1-A 22.7 16.6 15 400 65 0.47 6.2 403 1.0 77.0 3.3 1-B 21.3 15.6 15 400 90 0.47 6.2 558 1.4 68.2 2.3 1-C 21.3 15.6 15 400 30 0.47 6.2 186 0.5 89.4 7.0 1-D 21.3 15.6 20 400 65 0.41 6.2 403 1.0 77.0 3.7 1-E 20.0 17.0 10 400 65 0.67 6.2 403 1.0 77.0 2.3 2-0 21.3 15.6 15 25,000 16,000 0.008 6.2 99,200 4.0 0.8 2-A 21.3 15.6 15 25,000 4,200 0.008 6.2 26,040 1.0 73.8 3.1 3-0 19.7 17.8 17 400 283 0.547 6.4 1,811 4.5 0.6 3-A 19.7 17.8 17 400 63 0.547 6.4 403 1.0 77.7 2.9 3-B 19.7 17.8 30 400 67 0.412 6.4 429 1.1 76.3 3.6 4-0 19.7 17.8 17 25,000 16,000 0.009 6.4 102,400 4.1 0.7 4-A 19.7 17.8 17 25,000 3,800 0.009 6.4 24,320 1.0 76.3 3.0 5-0 18.8 14.2 13 400 283 0.521 5.8 1,641 4.1 0.7 5-A 18.8 14.2 13 400 66 0.521 5.8 383 1.0 76.7 2.9 6-0 18.8 14.2 13 25,000 16,000 0.008 5.8 92,800 3.7 0.7 6-A 18.8 14.2 13 25,000 4,500 0.008 5.8 26,100 1.0 71.9 2.7 7-0 22.0 19.2 40 400 283 0.345 5.5 1,557 3.9 1.0 7-A 22.0 19.2 40 400 74 0.345 5.5 407 1.0 73.9 3.9 8-0 22.0 19.2 40 25,000 16,000 0.006 5.5 88,000 3.5 1.1 8-A 22.0 19.2 40 25,000 4,750 0.006 5.5 26,125 1.0 70.3 3.8