CN113692464A - Method and arrangement in a batch pulping process - Google Patents
Method and arrangement in a batch pulping process Download PDFInfo
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- CN113692464A CN113692464A CN202080025317.4A CN202080025317A CN113692464A CN 113692464 A CN113692464 A CN 113692464A CN 202080025317 A CN202080025317 A CN 202080025317A CN 113692464 A CN113692464 A CN 113692464A
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- hydrolysate
- batch cooking
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- 238000000034 method Methods 0.000 title claims abstract description 43
- 238000004537 pulping Methods 0.000 title description 6
- 239000000413 hydrolysate Substances 0.000 claims abstract description 180
- 238000010411 cooking Methods 0.000 claims abstract description 178
- 238000001816 cooling Methods 0.000 claims abstract description 62
- 238000000605 extraction Methods 0.000 claims abstract description 42
- 238000005903 acid hydrolysis reaction Methods 0.000 claims abstract description 9
- 230000007062 hydrolysis Effects 0.000 claims description 36
- 238000006460 hydrolysis reaction Methods 0.000 claims description 36
- 235000000346 sugar Nutrition 0.000 claims description 26
- 239000007788 liquid Substances 0.000 claims description 16
- 150000008163 sugars Chemical class 0.000 claims description 12
- 229920000875 Dissolving pulp Polymers 0.000 claims description 7
- 239000012530 fluid Substances 0.000 claims description 7
- HYBBIBNJHNGZAN-UHFFFAOYSA-N furfural Chemical compound O=CC1=CC=CO1 HYBBIBNJHNGZAN-UHFFFAOYSA-N 0.000 description 20
- 229920005610 lignin Polymers 0.000 description 8
- NOEGNKMFWQHSLB-UHFFFAOYSA-N 5-hydroxymethylfurfural Chemical compound OCC1=CC=C(C=O)O1 NOEGNKMFWQHSLB-UHFFFAOYSA-N 0.000 description 5
- 108010009736 Protein Hydrolysates Proteins 0.000 description 5
- RJGBSYZFOCAGQY-UHFFFAOYSA-N hydroxymethylfurfural Natural products COC1=CC=C(C=O)O1 RJGBSYZFOCAGQY-UHFFFAOYSA-N 0.000 description 5
- 230000015556 catabolic process Effects 0.000 description 4
- 238000006731 degradation reaction Methods 0.000 description 4
- 238000004519 manufacturing process Methods 0.000 description 4
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 4
- 229920002488 Hemicellulose Polymers 0.000 description 3
- 238000004140 cleaning Methods 0.000 description 3
- 238000010586 diagram Methods 0.000 description 3
- 239000002253 acid Substances 0.000 description 2
- 239000000047 product Substances 0.000 description 2
- RFSUNEUAIZKAJO-ARQDHWQXSA-N Fructose Chemical compound OC[C@H]1O[C@](O)(CO)[C@@H](O)[C@@H]1O RFSUNEUAIZKAJO-ARQDHWQXSA-N 0.000 description 1
- 229930091371 Fructose Natural products 0.000 description 1
- 239000005715 Fructose Substances 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 230000003301 hydrolyzing effect Effects 0.000 description 1
- 239000004615 ingredient Substances 0.000 description 1
- 239000012978 lignocellulosic material Substances 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 230000008092 positive effect Effects 0.000 description 1
- 239000002023 wood Substances 0.000 description 1
Images
Classifications
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- D—TEXTILES; PAPER
- D21—PAPER-MAKING; PRODUCTION OF CELLULOSE
- D21C—PRODUCTION OF CELLULOSE BY REMOVING NON-CELLULOSE SUBSTANCES FROM CELLULOSE-CONTAINING MATERIALS; REGENERATION OF PULPING LIQUORS; APPARATUS THEREFOR
- D21C1/00—Pretreatment of the finely-divided materials before digesting
- D21C1/02—Pretreatment of the finely-divided materials before digesting with water or steam
-
- D—TEXTILES; PAPER
- D21—PAPER-MAKING; PRODUCTION OF CELLULOSE
- D21C—PRODUCTION OF CELLULOSE BY REMOVING NON-CELLULOSE SUBSTANCES FROM CELLULOSE-CONTAINING MATERIALS; REGENERATION OF PULPING LIQUORS; APPARATUS THEREFOR
- D21C1/00—Pretreatment of the finely-divided materials before digesting
- D21C1/04—Pretreatment of the finely-divided materials before digesting with acid reacting compounds
-
- D—TEXTILES; PAPER
- D21—PAPER-MAKING; PRODUCTION OF CELLULOSE
- D21C—PRODUCTION OF CELLULOSE BY REMOVING NON-CELLULOSE SUBSTANCES FROM CELLULOSE-CONTAINING MATERIALS; REGENERATION OF PULPING LIQUORS; APPARATUS THEREFOR
- D21C11/00—Regeneration of pulp liquors or effluent waste waters
- D21C11/0007—Recovery of by-products, i.e. compounds other than those necessary for pulping, for multiple uses or not otherwise provided for
-
- D—TEXTILES; PAPER
- D21—PAPER-MAKING; PRODUCTION OF CELLULOSE
- D21C—PRODUCTION OF CELLULOSE BY REMOVING NON-CELLULOSE SUBSTANCES FROM CELLULOSE-CONTAINING MATERIALS; REGENERATION OF PULPING LIQUORS; APPARATUS THEREFOR
- D21C3/00—Pulping cellulose-containing materials
- D21C3/02—Pulping cellulose-containing materials with inorganic bases or alkaline reacting compounds, e.g. sulfate processes
-
- D—TEXTILES; PAPER
- D21—PAPER-MAKING; PRODUCTION OF CELLULOSE
- D21C—PRODUCTION OF CELLULOSE BY REMOVING NON-CELLULOSE SUBSTANCES FROM CELLULOSE-CONTAINING MATERIALS; REGENERATION OF PULPING LIQUORS; APPARATUS THEREFOR
- D21C5/00—Other processes for obtaining cellulose, e.g. cooking cotton linters ; Processes characterised by the choice of cellulose-containing starting materials
-
- D—TEXTILES; PAPER
- D21—PAPER-MAKING; PRODUCTION OF CELLULOSE
- D21C—PRODUCTION OF CELLULOSE BY REMOVING NON-CELLULOSE SUBSTANCES FROM CELLULOSE-CONTAINING MATERIALS; REGENERATION OF PULPING LIQUORS; APPARATUS THEREFOR
- D21C9/00—After-treatment of cellulose pulp, e.g. of wood pulp, or cotton linters ; Treatment of dilute or dewatered pulp or process improvement taking place after obtaining the raw cellulosic material and not provided for elsewhere
- D21C9/008—Prevention of corrosion or formation of deposits on pulp-treating equipment
-
- C—CHEMISTRY; METALLURGY
- C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
- C12P—FERMENTATION OR ENZYME-USING PROCESSES TO SYNTHESISE A DESIRED CHEMICAL COMPOUND OR COMPOSITION OR TO SEPARATE OPTICAL ISOMERS FROM A RACEMIC MIXTURE
- C12P2201/00—Pretreatment of cellulosic or lignocellulosic material for subsequent enzymatic treatment or hydrolysis
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- Life Sciences & Earth Sciences (AREA)
- Engineering & Computer Science (AREA)
- Wood Science & Technology (AREA)
- Chemical & Material Sciences (AREA)
- Inorganic Chemistry (AREA)
- Paper (AREA)
Abstract
The present invention is a method of extracting a hydrolysate in a batch cooking system for producing pulp, a hydrolysate extraction arrangement and a batch cooking system. The method comprises the following steps: providing a lignocellulosic feedstock to a batch digester vessel; acid hydrolysis of lignocellulosic feedstock in a batch digester vessel; removing the hydrolysate from the batch cooking vessel; and cooling the removed hydrolysate to below 140 ℃ as quickly as possible on its way from the batch cooking vessel to the hydrolysate extraction tank after removal from the batch cooking vessel, wherein the cooling is performed during a period of 0-2 minutes from when the hydrolysate leaves the batch cooking vessel.
Description
Technical Field
The present invention relates to a method for extracting hydrolysate in a batch cooking process for producing pulp. The invention also relates to a hydrolysate extraction arrangement configured for extracting hydrolysate in a batch cooking system for producing pulp, and a batch cooking system for producing pulp.
Background
In some pulping processes, such as dissolving pulp production, lignocellulosic feedstock is first hydrolyzed to remove unwanted hemicellulose, and then subjected to alkaline cooking to remove lignin. Hydrolysis in batch cooking systems is typically carried out by adding steam to the lignocellulosic feedstock. During the hydrolysis process, hemicellulose (mainly C5 sugars) is degraded and released from the wood. If fructose should be extracted and processed, the hydrolysis product containing dissolved sugars needs to be removed from the vessel where the hydrolysis is carried out before changing the pH and carrying out the alkaline cooking. In the alkaline cooking process, the sugar is broken down into non-valuable ingredients.
The disposal of the hydrolysate can be problematic because it is very viscous and prone to fouling on, for example, piping, screens and tank surfaces. Connecting piping and tanks used in systems for extracting sugars often have fouling problems and require cleaning when removing hydrolysates from cooking vessels used for extracting sugars. Any cleaning and interruptions in the production process are of course negative.
Summary of The Invention
It is an object of the present invention to improve the efficiency of hydrolysate extraction in a pulping system.
This is achieved by a method of extracting a hydrolysate in a hydrolysate extraction arrangement and a batch cooking system according to the independent claims.
According to one aspect of the present invention, there is provided a method of extracting a hydrolysate in a batch cooking process for producing pulp, the method comprising the steps of:
-providing a lignocellulosic feedstock to a batch cooking vessel;
-performing an acid hydrolysis of the lignocellulosic feedstock in a batch cooking vessel;
-removing hydrolysate from the batch cooking vessel; and
-cooling the removed hydrolysate to below 140 ℃ as soon as possible on its way from the batch cooking vessel to the hydrolysate extraction tank after removal from the batch cooking vessel, wherein the cooling is performed during a period of 0-2 minutes from the moment the hydrolysate leaves the batch cooking vessel.
According to another aspect of the invention, a batch cooking system for producing pulp is provided. The batch cooking system comprises a batch cooking vessel and a hydrolysate extraction arrangement configured to extract a hydrolysate in the batch cooking system, whereby the hydrolysate extraction arrangement is connected to a hydrolysate outlet of the batch cooking vessel and comprises:
-a hydrolysate removal pipe comprising a batch cooking vessel connector configured to connect to a hydrolysate outlet of a batch cooking vessel of a batch cooking system;
-a hydrolysate extraction tank connected to the hydrolysate removal pipe and configured to receive the hydrolysate removed from the batch cooking vessel via the hydrolysate removal pipe; and
-cooling means configured to cool any hydrolysate removed from the batch cooking vessel to 140 ℃ as soon as possible after removal from the batch cooking vessel, wherein the cooling is performed during a period of 0-2 minutes from when the hydrolysate leaves the batch cooking vessel, wherein the cooling means is arranged in connection with the hydrolysate removal pipe and cools the removed hydrolysate on its way from the batch cooking vessel to the hydrolysate extraction tank.
According to another aspect of the present invention, there is provided a hydrolysate extraction arrangement configured to extract hydrolysate in a batch cooking system for producing pulp, the hydrolysate extraction arrangement comprising:
-a hydrolysate removal pipe comprising a batch cooking vessel connector configured to connect to a hydrolysate outlet of a batch cooking vessel of a batch cooking system;
-a hydrolysate extraction tank connected to the hydrolysate removal pipe and configured to receive the hydrolysate removed from the batch cooking vessel via the hydrolysate removal pipe; and
-cooling means configured to cool any hydrolysate removed from the batch cooking vessel to 140 ℃ as soon as possible after removal from the batch cooking vessel, wherein the cooling is performed during a period of 0-2 minutes from the moment the hydrolysate leaves the batch cooking vessel, wherein the cooling means (15)
Is arranged in connection with the hydrolysate removal pipe (7) and cools the removed hydrolysate on its way from the batch cooking vessel to the hydrolysate extraction tank.
Thus, a method and system for extracting hydrolysate in a pulping system is provided that is more efficient and reliable than prior art systems. The tendency of the hydrolysate to form scale is greatly reduced due to cooling after removal from the batch cooking vessel. When the hydrolysate is cooled, furfural formation is reduced and lignin degradation is also reduced. This will reduce the tendency for fouling to occur. Furthermore, the stability of the sugar solution is radically improved due to the reduced rate of sugar degradation and a more efficient sugar extraction may be provided. A more reliable process is provided due to little fouling and substantially no system cleaning, and a better sugar yield may be provided due to reduced sugar degradation.
In one embodiment of the invention, the method further comprises the step of extracting sugars from the removed hydrolysate.
In one embodiment of the invention, the process further comprises the step of alkaline cooking in a batch cooking vessel after removal of the hydrolysate.
In one embodiment of the invention, the batch cooking process is a process for producing dissolving pulp.
In one embodiment of the invention, the step of performing acid hydrolysis of the lignocellulosic feedstock in a batch digester vessel comprises steam hydrolysis and/or liquid hydrolysis.
In one embodiment of the invention, the step of cooling the removed hydrolysate comprises cooling the hydrolysate to below 120 ℃. In one embodiment of the invention, the step of cooling the removed hydrolysate comprises cooling the hydrolysate to below 100 ℃.
In one embodiment of the invention, the step of cooling the removed hydrolysate comprises cooling the hydrolysate within a time period of 0 to 1 minute from the moment the hydrolysate leaves the batch cooking vessel.
In one embodiment of the invention, the cooling device is a heat exchanger.
In one embodiment of the invention, the batch cooking vessel is a pressurized vessel and the batch cooking system further comprises a hydrolysis arrangement connected to the batch cooking vessel and configured for adding fluid to the batch cooking vessel for performing hydrolysis of the lignocellulosic feedstock provided in the batch cooking vessel.
In one embodiment of the invention, the hydrolysis arrangement is configured for adding steam and/or liquid to the batch cooking vessel for hydrolysis.
In one embodiment of the invention, the batch cooking system further comprises a liquid addition arrangement connected to the batch cooking vessel and configured for adding lye into the batch cooking vessel for alkaline cooking after hydrolysis in the batch cooking vessel and after removal of the hydrolysate from the batch cooking vessel.
In one embodiment of the invention, the batch cooking system is a system for producing dissolving pulp.
Brief description of the drawings
FIG. 1 is a schematic diagram of a batch cooking system according to one embodiment of the present invention.
Fig. 2 is a flow diagram of a method of extracting a hydrolysate according to one embodiment of the present invention.
Figures 3a and 3b show graphs of furfural and HMF content in the hydrolysate at different temperatures.
Detailed description of the embodiments
Fig. 1 schematically shows a batch cooking system 1 for producing pulp according to one embodiment of the invention. The batch cooking system 1 comprises a batch cooking vessel 3 and a hydrolysate extraction arrangement 5 according to the invention, which hydrolysate extraction arrangement 5 is connected to a hydrolysate outlet 11 of the batch cooking vessel 3.
The batch cooking vessel 3 may be a conventional batch cooking vessel for producing pulp. Only some of the components and features of batch cooking vessel 3 relevant to the present invention will be described herein. The batch cooking vessel 3 comprises an inlet 4a for receiving the lignocellulosic feedstock and an outlet 4b for discharging the contents of the batch cooking vessel 3 after it has been treated in the vessel. The treatment of the lignocellulosic feedstock in the batch cooking vessel 3 comprises acid hydrolysis followed by alkaline cooking. The batch digester vessel 3 is a pressurized vessel. Acid hydrolysis of lignocellulosic feedstock is carried out by adding a fluid to batch cooking vessel 3. The added fluid may be steam and/or liquid added to the batch cooking vessel 3. The steam and/or liquid may be water and may optionally contain an acid component for improving the hydrolysis. In the case of water alone, the acid contained in the lignocellulosic material is considered sufficient to effect hydrolysis. In fig. 1, this is shown in a hydrolysis arrangement 21 connected to the batch cooking vessel 3, which hydrolysis arrangement 21 is configured to add at least one fluid to the batch cooking vessel to perform hydrolysis as described above. According to the invention, it is suitable to add a liquid for hydrolysis, which may have been previously steamed. The liquid may be, for example, water. According to the invention, which will be described in more detail below, the hydrolysate will be removed from the batch cooking vessel and extracted more efficiently by adding liquid for carrying out the hydrolysis. If sugar is extracted from the hydrolysate, such sugar extraction with the addition of liquid for carrying out the hydrolysis can be more efficient than hydrolysis achieved by adding only steam.
The batch cooking vessel 3 further comprises a liquid addition arrangement 27 configured to add lye to the batch cooking vessel 3 for alkaline cooking in the batch cooking vessel 3. The hydrolysis is followed by alkaline cooking in a batch cooking vessel. According to the invention, alkaline cooking is also carried out after removal of the hydrolysate from the batch cooking vessel 3. If, for example, the sugar should be extracted from the hydrolysate, it is necessary to remove the hydrolysate containing dissolved sugar from the batch cooking vessel in which the hydrolysis is carried out before changing the pH and carrying out the alkaline cooking. In the alkaline cooking process, the hydrolyzed dissolved sugars are destroyed into valueless components.
According to the invention, the hydrolysate should be removed from the batch cooking vessel 3 after the hydrolysis has been carried out and before the alkaline cooking step is started. The hydrolysate is removed via a hydrolysate outlet 11 arranged in the batch cooking vessel 3. The hydrolysate outlet 11 may for example be arranged in the upper half of the batch cooking vessel. However, it may also be arranged in the lower half of the batch cooking vessel. The hydrolysate can be pushed out of the bottom of the batch cooking vessel 3, e.g. from the bottom of the batch cooking vessel 3, by increasing the pressure in the batch cooking vessel, e.g. by adding another fluid (e.g. water or liquid) to the batch cooking vessel. Another option is to pump or discharge the hydrolysate from the batch cooking vessel 3.
The batch cooking system 1 may be a system for producing dissolving pulp. In the production of dissolving pulp, hemicellulose is removed from lignocellulosic feedstock by acid hydrolysis before lignin is removed in the alkaline cooking step.
According to the present invention, a hydrolysate extraction arrangement 5 is provided, which is configured to extract hydrolysate in a batch cooking system 1 for producing pulp. The hydrolysate extraction arrangement 5 is during use connected to the hydrolysate outlet 11 of the batch cooking vessel 3 in the batch cooking system 1 as described above. The hydrolysate extraction arrangement 5 comprises a hydrolysate removal pipe 7, which hydrolysate removal pipe 7 comprises a batch cooking vessel connector 8 configured to be connected to a hydrolysate outlet 11 of the batch cooking vessel 3. The hydrolysate extraction arrangement 5 further comprises a hydrolysate extraction tank 13 and a cooling device 15, the tank 13 being connected to the hydrolysate removal pipe 7 and arranged for receiving the hydrolysate removed from the batch cooking vessel 3 via the hydrolysate removal pipe 7, the cooling device 15 being configured for cooling any hydrolysate removed from the batch cooking vessel 3. The cooling device 15 may be arranged in connection with the hydrolysate removal pipe 7 as shown in fig. 1. The hydrolysate should preferably be cooled as quickly as possible after removal from batch cooking vessel 3. For example, the cooling means 15 may be arranged in a position such that the cooling of the hydrolysate is performed within a time period of 0-2 minutes from the moment the hydrolysate leaves the batch cooking vessel or within a time period of 0-1 minute from the moment the hydrolysate leaves the batch cooking vessel.
The cooling means 15 may be configured to cool the hydrolysate to below 140 ℃ or below 120 ℃ or below 100 ℃. A typical temperature of the contents of the batch cooking vessel 3 may be, for example, about 170 ℃. In one embodiment of the invention the cooling means 15 is configured to cool the hydrolysate to a temperature of 70 to 140 ℃ and in one embodiment of the invention the cooling means 15 is configured to cool the hydrolysate to a temperature of 80 to 120 ℃ or 90 to 100 ℃. By cooling the hydrolysate, the hydrolysate can be extracted more efficiently. The hydrolysate is usually very viscous and difficult to handle. For example, severe fouling can occur in tanks, pipes, recycle lines, screens, etc. in equipment used to treat the hydrolysate. The stickiness of the hydrolysate and its tendency to form scale may be due to furfural and lignin produced by the dissolved sugars. The production of furfural is a function of time, i.e., the longer the sugar exposure to such conditions, the higher the concentration of furfural in solution. The lignin content also increases during the hydrolysis time. The scale is mainly composed of lignin and furfural and sugars.
It has surprisingly been found that by cooling the hydrolysate to e.g. below about 140 ℃ or below 120 ℃ or below 100 ℃, the stickiness and the tendency to form scale is greatly reduced and the extraction of the hydrolysate from the pulping process can be greatly improved. Thereby also improving the extraction of sugars from the hydrolysate. The positive effect of cooling, i.e. the reduction of scale, is surprisingly high even when the temperature drop is relatively small.
Furthermore, in these types of cooking systems for producing pulp, it is traditionally very important to maintain the high temperature of the material to avoid energy losses. Thus, the solution of using such a cooled hydrolysate is not obvious to the skilled person.
The cooling device 15 may be a heat exchanger. Another option may be to add cold fluid to the hydrolysate as it is removed from the batch digester vessel 3. However, this dilutes the hydrolysate, which may not be advantageous in all applications.
FIG. 2 is a flow diagram of a method according to an embodiment of the invention. The method is a method of extracting a hydrolysate in a batch cooking process for producing pulp, comprising the steps of:
s1: the lignocellulosic feedstock is supplied to a batch digester vessel 3.
S2: acid hydrolysis of lignocellulosic feedstocks is carried out in a batch digester vessel. This step may include steam hydrolysis and/or liquid hydrolysis as described above. It is appropriate to add liquid to batch cooking vessel 3 for hydrolysis to improve the hydrolytic extraction.
S3: the hydrolysate is removed from the batch cooking vessel 3.
S4: the removed hydrolysate was cooled. This step may include cooling the hydrolysate to less than 140 ℃ or less than 120 ℃ or less than 100 ℃, as described above. In one embodiment of the invention, this step may comprise cooling the hydrolysate to a temperature of 70 to 140 ℃ or a temperature of 80 to 120 ℃ or a temperature of 90 to 100 ℃. Furthermore, it is desirable that the cooling should be carried out as soon as possible after removal from batch cooking vessel 3 to avoid fouling in the equipment. The hydrolysate is cooled on the way from the batch cooking vessel 3 to the hydrolysate extraction tank 13. The step of cooling the removed hydrolysate may comprise cooling the removed hydrolysate over a period of 0-2 minutes from when the hydrolysate leaves the batch cooking vessel or over a period of 0-1 minute from when the hydrolysate leaves the batch cooking vessel. The step of cooling the removed hydrolysate may comprise cooling the hydrolysate by means of a heat exchanger 15.
According to some embodiments of the invention, the method further comprises step S5: extracting sugars from the removed hydrolysate. This step is performed after step S4 of cooling the removed hydrolysate. When the hydrolysate has been cooled as described above according to the present invention, the extraction rate of sugars from the hydrolysate is greatly increased. Since the rate of sugar degradation is reduced after cooling of the hydrolysate, the stability of the sugar solution is fundamentally improved and a more efficient sugar extraction can be provided. In some embodiments of the invention, lignin may also be extracted from the hydrolysate.
According to some embodiments of the invention, the method further comprises step S6: after removal of the hydrolysis products, alkaline cooking is carried out in a batch cooking vessel 3. Step S6 may be performed at any time after step S3 as described above.
Figure 3a is a graph of furfural content in the hydrolysate after 0, 2, 4 and 6 hours at different temperatures. It clearly shows that the amount of furfural starts to increase when the temperature is above 140 ℃. Below 140 ℃, the amount of furfural is very limited.
Fig. 3b is a graph of HMF (hydroxymethylfurfural) content in the hydrolysate at different temperatures. Likewise, the HMF content increases at temperatures above 140 ℃, but is very limited at lower temperatures. Furfural and HMF can form sticky scale in the equipment together with lignin, so that when the hydrolysate is cooled to a temperature below 140 ℃ as soon as possible after removal from the batch digester vessel according to the invention, the scale can be greatly reduced.
Claims (20)
1. A method of extracting a hydrolysate in a batch cooking process for producing pulp, the method comprising the steps of:
-providing a lignocellulosic feedstock to a batch cooking vessel;
-performing an acid hydrolysis of the lignocellulosic feedstock in a batch cooking vessel;
-removing hydrolysate from the batch cooking vessel; and
-cooling the removed hydrolysate to below 140 ℃ as soon as possible on its way from the batch cooking vessel to the hydrolysate extraction tank after removal from the batch cooking vessel, wherein the cooling is performed during a period of 0-2 minutes from the moment the hydrolysate leaves the batch cooking vessel.
2. The method of claim 1, wherein the method further comprises the step of extracting sugars from the removed hydrolysate.
3. The process of claim 1 or 2, further comprising the step of alkaline cooking in a batch cooking vessel after removing the hydrolysate.
4. The method of any one of the preceding claims, wherein the batch cooking process is a process for producing dissolving pulp.
5. The process according to any one of the preceding claims, wherein the step of performing acid hydrolysis of the lignocellulosic feedstock in a batch digester vessel comprises steam hydrolysis and/or liquid hydrolysis.
6. A method according to any one of the preceding claims, wherein the step of cooling the removed hydrolysate comprises cooling the hydrolysate to below 120 ℃ or below 100 ℃.
7. The method of any one of the preceding claims, wherein the step of cooling the removed hydrolysate comprises cooling the hydrolysate over a period of 0 to 1 minute from the time the hydrolysate exits the batch cooking vessel.
8. A method according to any one of the preceding claims, wherein the step of cooling the removed hydrolysate comprises cooling the hydrolysate via a heat exchanger.
9. A batch cooking system (1) for producing pulp, the batch cooking system (1) comprising a batch cooking vessel (3) and a hydrolysate extraction arrangement (5), the hydrolysate extraction arrangement (5) being configured to extract hydrolysate in the batch cooking system (1), whereby the hydrolysate extraction arrangement (5) is connected to a hydrolysate outlet (11) of the batch cooking vessel (3) and comprises:
-a hydrolysate removal pipe (7) comprising a batch cooking vessel connector (8) configured to be connected to a hydrolysate outlet (11) of a batch cooking vessel (3) of a batch cooking system (1);
-a hydrolysate extraction tank (13) connected to the hydrolysate removal pipe (7) and configured to receive the hydrolysate removed from the batch cooking vessel (3) via the hydrolysate removal pipe (7); and
-a cooling device (15) configured to cool any hydrolysate removed from the batch cooking vessel (3) to 140 ℃ as soon as possible after removal from the batch cooking vessel, wherein the cooling is performed during a period of 0-2 minutes from when the hydrolysate leaves the batch cooking vessel, wherein the cooling device (15) is arranged in connection with the hydrolysate removal pipe (7) and cools the removed hydrolysate on its way from the batch cooking vessel to the hydrolysate extraction tank.
10. A batch cooking system according to claim 9, wherein the cooling device (15) is configured to cool the hydrolysate to below 120 ℃ or below 100 ℃.
11. A batch cooking system according to any one of claims 9-10, wherein the cooling device (15) is arranged in such a position that the cooling of the hydrolysate takes place during a period of 0-1 minutes from the moment the hydrolysate leaves the batch cooking vessel.
12. A batch cooking system according to any one of claims 9-11, wherein the cooling device (15) is a heat exchanger.
13. A batch cooking system according to any one of claims 9-12, wherein the batch cooking vessel (3) is a pressurized vessel, and wherein the batch cooking system further comprises a hydrolysis arrangement (21), which hydrolysis arrangement (21) is connected to the batch cooking vessel (3) and is configured for adding a fluid to the batch cooking vessel for hydrolysis of the lignocellulosic feedstock provided in the batch cooking vessel (3).
14. A batch cooking system according to claim 13, wherein the hydrolysis arrangement (21) is configured for adding steam and/or liquid to the batch cooking vessel (3) for hydrolysis.
15. A batch cooking system according to any one of claims 9-14, wherein the batch cooking system (1) further comprises a liquid addition arrangement (27) connected to the batch cooking vessel (3) and configured for adding lye into the batch cooking vessel (3) for alkaline cooking after hydrolysis in the batch cooking vessel (3) and after removal of the hydrolysate from the batch cooking vessel (3).
16. A batch cooking system according to any one of claims 9-15, wherein the batch cooking system (1) is a system for producing dissolving pulp.
17. A hydrolysate extraction arrangement (5) configured to extract a hydrolysate in a batch cooking system (1) for producing pulp, the hydrolysate extraction arrangement (5) comprising:
-a hydrolysate removal pipe (7) comprising a batch cooking vessel connector (8) configured to be connected to a hydrolysate outlet (11) of a batch cooking vessel (3) of a batch cooking system (1);
-a hydrolysate extraction tank (13) connected to the hydrolysate removal pipe (7) and configured to receive the hydrolysate removed from the batch cooking vessel (3) via the hydrolysate removal pipe (7); and
-a cooling device (15) configured to cool any hydrolysate removed from the batch cooking vessel (3) to 140 ℃ as soon as possible after removal from the batch cooking vessel, wherein the cooling is performed during a period of 0-2 minutes from when the hydrolysate leaves the batch cooking vessel, wherein the cooling device (15) is arranged in connection with the hydrolysate removal pipe (7) and cools the removed hydrolysate on its way from the batch cooking vessel to the hydrolysate extraction tank.
18. The hydrolysate extraction arrangement according to claim 17, wherein the cooling device (15) is configured to cool the hydrolysate to below 120 ℃ or below 100 ℃.
19. A hydrolysate extraction arrangement as claimed in any one of claims 17 to 18, wherein the cooling means (15) is provided in a position such that cooling of the hydrolysate takes place over a period of 0 to 1 minute from the time the hydrolysate leaves the batch cooking vessel.
20. A hydrolysate extraction arrangement as claimed in any one of claims 17 to 19, wherein the cooling device (15) is a heat exchanger.
Applications Claiming Priority (3)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| SE1950405A SE543924C2 (en) | 2019-04-02 | 2019-04-02 | A method for extracting hydrolysate in a batch pulp production process |
| SE1950405-9 | 2019-04-02 | ||
| PCT/SE2020/050253 WO2020204780A1 (en) | 2019-04-02 | 2020-03-09 | A method and arrangement in a batch pulp production process |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN113692464A true CN113692464A (en) | 2021-11-23 |
| CN113692464B CN113692464B (en) | 2022-09-16 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202080025317.4A Active CN113692464B (en) | 2019-04-02 | 2020-03-09 | Method and arrangement in a batch pulping process |
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| EP (1) | EP3947807A4 (en) |
| CN (1) | CN113692464B (en) |
| BR (1) | BR112021012894A2 (en) |
| SE (1) | SE543924C2 (en) |
| WO (1) | WO2020204780A1 (en) |
| ZA (1) | ZA202104455B (en) |
Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN1094108A (en) * | 1992-12-02 | 1994-10-26 | 沃斯特-阿尔潘工业技术公司 | A kind of method of making dissolving pulp |
| CN1824379A (en) * | 1999-06-23 | 2006-08-30 | Rm防火材料有限公司 | Process for pre-hydrolysis of biomass |
| US20090093028A1 (en) * | 2007-10-05 | 2009-04-09 | Joy Doran Peterson | Apparatus and methods for treating biomass |
| CN102472006A (en) * | 2010-03-11 | 2012-05-23 | 梅特索纸业公司 | Method for producing pulp |
| CN103451987A (en) * | 2013-08-23 | 2013-12-18 | 湖南骏泰浆纸有限责任公司 | Method and device for extracting pre-hydrolysis liquid from dissolving pulp |
| CN104302776A (en) * | 2012-05-17 | 2015-01-21 | 国际壳牌研究有限公司 | Method and system for processing biomass material |
| BR112018010183A2 (en) * | 2016-02-16 | 2018-11-21 | Valmet Oy | method for recovering concentrated hydrolyzate after hydrolysis of cellulosic material |
Family Cites Families (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4668340A (en) * | 1984-03-20 | 1987-05-26 | Kamyr, Inc. | Method of countercurrent acid hydrolysis of comminuted cellulosic fibrous material |
| US6176971B1 (en) * | 1998-11-18 | 2001-01-23 | Andritz-Ahlstrom Inc. | Heat economy enhancements for the recovery and use of energy obtained from spent cooking liquors |
| US6603026B2 (en) * | 2001-08-07 | 2003-08-05 | Gene E. Lightner | Heterocyclic compounds produced from biomass |
| FI123036B (en) | 2006-02-10 | 2012-10-15 | Metso Paper Inc | Process for collection of hydrolysis products |
| WO2017088061A1 (en) * | 2015-11-25 | 2017-06-01 | Iogen Energy Corporation | System and method for cooling pretreated biomass |
-
2019
- 2019-04-02 SE SE1950405A patent/SE543924C2/en unknown
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2020
- 2020-03-09 WO PCT/SE2020/050253 patent/WO2020204780A1/en unknown
- 2020-03-09 EP EP20782370.9A patent/EP3947807A4/en active Pending
- 2020-03-09 BR BR112021012894A patent/BR112021012894A2/en active Search and Examination
- 2020-03-09 CN CN202080025317.4A patent/CN113692464B/en active Active
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2021
- 2021-06-28 ZA ZA2021/04455A patent/ZA202104455B/en unknown
Patent Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1094108A (en) * | 1992-12-02 | 1994-10-26 | 沃斯特-阿尔潘工业技术公司 | A kind of method of making dissolving pulp |
| CN1824379A (en) * | 1999-06-23 | 2006-08-30 | Rm防火材料有限公司 | Process for pre-hydrolysis of biomass |
| US20090093028A1 (en) * | 2007-10-05 | 2009-04-09 | Joy Doran Peterson | Apparatus and methods for treating biomass |
| CN102472006A (en) * | 2010-03-11 | 2012-05-23 | 梅特索纸业公司 | Method for producing pulp |
| CN104302776A (en) * | 2012-05-17 | 2015-01-21 | 国际壳牌研究有限公司 | Method and system for processing biomass material |
| CN103451987A (en) * | 2013-08-23 | 2013-12-18 | 湖南骏泰浆纸有限责任公司 | Method and device for extracting pre-hydrolysis liquid from dissolving pulp |
| BR112018010183A2 (en) * | 2016-02-16 | 2018-11-21 | Valmet Oy | method for recovering concentrated hydrolyzate after hydrolysis of cellulosic material |
Also Published As
| Publication number | Publication date |
|---|---|
| SE543924C2 (en) | 2021-09-28 |
| BR112021012894A2 (en) | 2021-11-09 |
| CN113692464B (en) | 2022-09-16 |
| SE1950405A1 (en) | 2020-10-03 |
| EP3947807A4 (en) | 2023-01-04 |
| WO2020204780A1 (en) | 2020-10-08 |
| ZA202104455B (en) | 2023-11-29 |
| EP3947807A1 (en) | 2022-02-09 |
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