US20020069987A1 - Integrated processing of biomass and liquid effluents - Google Patents
Integrated processing of biomass and liquid effluents Download PDFInfo
- Publication number
- US20020069987A1 US20020069987A1 US10/072,219 US7221902A US2002069987A1 US 20020069987 A1 US20020069987 A1 US 20020069987A1 US 7221902 A US7221902 A US 7221902A US 2002069987 A1 US2002069987 A1 US 2002069987A1
- Authority
- US
- United States
- Prior art keywords
- ethanol
- liquor
- digester
- water
- process according
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Abandoned
Links
- 239000002028 Biomass Substances 0.000 title claims abstract description 16
- 239000007788 liquid Substances 0.000 title claims abstract description 7
- 238000012545 processing Methods 0.000 title description 5
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 claims abstract description 100
- 238000000034 method Methods 0.000 claims abstract description 61
- 230000008569 process Effects 0.000 claims abstract description 60
- 238000000855 fermentation Methods 0.000 claims abstract description 25
- 230000004151 fermentation Effects 0.000 claims abstract description 25
- CZMRCDWAGMRECN-UGDNZRGBSA-N Sucrose Chemical compound O[C@H]1[C@H](O)[C@@H](CO)O[C@@]1(CO)O[C@@H]1[C@H](O)[C@@H](O)[C@H](O)[C@@H](CO)O1 CZMRCDWAGMRECN-UGDNZRGBSA-N 0.000 claims abstract description 16
- 229930006000 Sucrose Natural products 0.000 claims abstract description 15
- 238000004537 pulping Methods 0.000 claims abstract description 15
- 229960004793 sucrose Drugs 0.000 claims abstract description 15
- 239000002699 waste material Substances 0.000 claims abstract description 14
- 239000000463 material Substances 0.000 claims abstract description 3
- 238000006243 chemical reaction Methods 0.000 claims abstract 2
- SRBFZHDQGSBBOR-IOVATXLUSA-N D-xylopyranose Chemical compound O[C@@H]1COC(O)[C@H](O)[C@H]1O SRBFZHDQGSBBOR-IOVATXLUSA-N 0.000 claims description 26
- HYBBIBNJHNGZAN-UHFFFAOYSA-N furfural Chemical compound O=CC1=CC=CO1 HYBBIBNJHNGZAN-UHFFFAOYSA-N 0.000 claims description 22
- 241000609240 Ambelania acida Species 0.000 claims description 17
- 239000010905 bagasse Substances 0.000 claims description 17
- 229920005610 lignin Polymers 0.000 claims description 17
- 235000000346 sugar Nutrition 0.000 claims description 15
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 14
- PYMYPHUHKUWMLA-UHFFFAOYSA-N arabinose Natural products OCC(O)C(O)C(O)C=O PYMYPHUHKUWMLA-UHFFFAOYSA-N 0.000 claims description 13
- SRBFZHDQGSBBOR-UHFFFAOYSA-N beta-D-Pyranose-Lyxose Natural products OC1COC(O)C(O)C1O SRBFZHDQGSBBOR-UHFFFAOYSA-N 0.000 claims description 13
- QTBSBXVTEAMEQO-UHFFFAOYSA-N Acetic acid Chemical compound CC(O)=O QTBSBXVTEAMEQO-UHFFFAOYSA-N 0.000 claims description 12
- 239000000203 mixture Substances 0.000 claims description 11
- 238000004519 manufacturing process Methods 0.000 claims description 10
- 235000013379 molasses Nutrition 0.000 claims description 8
- 150000008163 sugars Chemical class 0.000 claims description 7
- 241000196324 Embryophyta Species 0.000 claims description 6
- XEKOWRVHYACXOJ-UHFFFAOYSA-N Ethyl acetate Chemical compound CCOC(C)=O XEKOWRVHYACXOJ-UHFFFAOYSA-N 0.000 claims description 6
- 239000000126 substance Substances 0.000 claims description 5
- 241001465754 Metazoa Species 0.000 claims description 4
- 229920001221 xylan Polymers 0.000 claims description 4
- 150000004823 xylans Chemical class 0.000 claims description 4
- 239000003337 fertilizer Substances 0.000 claims description 3
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims description 2
- VMHLLURERBWHNL-UHFFFAOYSA-M Sodium acetate Chemical compound [Na+].CC([O-])=O VMHLLURERBWHNL-UHFFFAOYSA-M 0.000 claims description 2
- 239000002253 acid Substances 0.000 claims description 2
- 239000001632 sodium acetate Substances 0.000 claims description 2
- 235000017281 sodium acetate Nutrition 0.000 claims description 2
- CSCPPACGZOOCGX-UHFFFAOYSA-N Acetone Chemical compound CC(C)=O CSCPPACGZOOCGX-UHFFFAOYSA-N 0.000 claims 3
- 239000012452 mother liquor Substances 0.000 claims 3
- LRHPLDYGYMQRHN-UHFFFAOYSA-N N-Butanol Chemical compound CCCCO LRHPLDYGYMQRHN-UHFFFAOYSA-N 0.000 claims 2
- 150000007513 acids Chemical class 0.000 claims 1
- 238000001816 cooling Methods 0.000 claims 1
- 238000007865 diluting Methods 0.000 claims 1
- 230000008020 evaporation Effects 0.000 claims 1
- 238000001704 evaporation Methods 0.000 claims 1
- 230000008016 vaporization Effects 0.000 claims 1
- 239000007787 solid Substances 0.000 abstract description 5
- 230000009467 reduction Effects 0.000 abstract description 4
- 239000000047 product Substances 0.000 description 22
- 238000011084 recovery Methods 0.000 description 17
- 238000010411 cooking Methods 0.000 description 6
- 238000004821 distillation Methods 0.000 description 6
- 230000007613 environmental effect Effects 0.000 description 5
- 239000000706 filtrate Substances 0.000 description 4
- 229910052500 inorganic mineral Inorganic materials 0.000 description 4
- 239000011707 mineral Substances 0.000 description 4
- 239000002904 solvent Substances 0.000 description 4
- 238000010025 steaming Methods 0.000 description 4
- 238000004148 unit process Methods 0.000 description 4
- 238000013459 approach Methods 0.000 description 3
- 239000006227 byproduct Substances 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- 239000002994 raw material Substances 0.000 description 3
- 239000002023 wood Substances 0.000 description 3
- 240000004808 Saccharomyces cerevisiae Species 0.000 description 2
- 240000000111 Saccharum officinarum Species 0.000 description 2
- 235000007201 Saccharum officinarum Nutrition 0.000 description 2
- 229920002472 Starch Polymers 0.000 description 2
- 235000013405 beer Nutrition 0.000 description 2
- 238000004061 bleaching Methods 0.000 description 2
- 229920002678 cellulose Polymers 0.000 description 2
- 239000001913 cellulose Substances 0.000 description 2
- 239000012141 concentrate Substances 0.000 description 2
- 238000011161 development Methods 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 239000006052 feed supplement Substances 0.000 description 2
- 230000010354 integration Effects 0.000 description 2
- 239000002655 kraft paper Substances 0.000 description 2
- 239000010808 liquid waste Substances 0.000 description 2
- BDAGIHXWWSANSR-UHFFFAOYSA-N methanoic acid Natural products OC=O BDAGIHXWWSANSR-UHFFFAOYSA-N 0.000 description 2
- 238000002360 preparation method Methods 0.000 description 2
- 235000019698 starch Nutrition 0.000 description 2
- 239000008107 starch Substances 0.000 description 2
- ZMBHCYHQLYEYDV-UHFFFAOYSA-N trioctylphosphine oxide Chemical compound CCCCCCCCP(=O)(CCCCCCCC)CCCCCCCC ZMBHCYHQLYEYDV-UHFFFAOYSA-N 0.000 description 2
- 238000005406 washing Methods 0.000 description 2
- OSWFIVFLDKOXQC-UHFFFAOYSA-N 4-(3-methoxyphenyl)aniline Chemical compound COC1=CC=CC(C=2C=CC(N)=CC=2)=C1 OSWFIVFLDKOXQC-UHFFFAOYSA-N 0.000 description 1
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 1
- 241000283690 Bos taurus Species 0.000 description 1
- 229920000297 Rayon Polymers 0.000 description 1
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 description 1
- LSNNMFCWUKXFEE-UHFFFAOYSA-N Sulfurous acid Chemical compound OS(O)=O LSNNMFCWUKXFEE-UHFFFAOYSA-N 0.000 description 1
- TVXBFESIOXBWNM-UHFFFAOYSA-N Xylitol Natural products OCCC(O)C(O)C(O)CCO TVXBFESIOXBWNM-UHFFFAOYSA-N 0.000 description 1
- 238000005903 acid hydrolysis reaction Methods 0.000 description 1
- 239000003674 animal food additive Substances 0.000 description 1
- 230000000675 anti-caries Effects 0.000 description 1
- 239000007864 aqueous solution Substances 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 150000001720 carbohydrates Chemical class 0.000 description 1
- 235000014633 carbohydrates Nutrition 0.000 description 1
- 238000012824 chemical production Methods 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 230000002860 competitive effect Effects 0.000 description 1
- 239000012043 crude product Substances 0.000 description 1
- 238000013461 design Methods 0.000 description 1
- 235000013325 dietary fiber Nutrition 0.000 description 1
- 229910001873 dinitrogen Inorganic materials 0.000 description 1
- 239000002270 dispersing agent Substances 0.000 description 1
- 238000006073 displacement reaction Methods 0.000 description 1
- 230000008030 elimination Effects 0.000 description 1
- 238000003379 elimination reaction Methods 0.000 description 1
- 150000002148 esters Chemical class 0.000 description 1
- 239000000835 fiber Substances 0.000 description 1
- 238000001914 filtration Methods 0.000 description 1
- 235000003599 food sweetener Nutrition 0.000 description 1
- 235000019253 formic acid Nutrition 0.000 description 1
- -1 hexose sugars Chemical class 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 229910010272 inorganic material Inorganic materials 0.000 description 1
- 239000011147 inorganic material Substances 0.000 description 1
- 238000002955 isolation Methods 0.000 description 1
- 239000007791 liquid phase Substances 0.000 description 1
- 238000011068 loading method Methods 0.000 description 1
- HEBKCHPVOIAQTA-UHFFFAOYSA-N meso ribitol Natural products OCC(O)C(O)C(O)CO HEBKCHPVOIAQTA-UHFFFAOYSA-N 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 239000003960 organic solvent Substances 0.000 description 1
- 238000012856 packing Methods 0.000 description 1
- 239000008188 pellet Substances 0.000 description 1
- 239000000575 pesticide Substances 0.000 description 1
- 239000002244 precipitate Substances 0.000 description 1
- 238000001556 precipitation Methods 0.000 description 1
- 238000011027 product recovery Methods 0.000 description 1
- 102000004169 proteins and genes Human genes 0.000 description 1
- 108090000623 proteins and genes Proteins 0.000 description 1
- 239000002964 rayon Substances 0.000 description 1
- 238000007670 refining Methods 0.000 description 1
- 238000011160 research Methods 0.000 description 1
- 230000000717 retained effect Effects 0.000 description 1
- 238000012216 screening Methods 0.000 description 1
- 239000002002 slurry Substances 0.000 description 1
- 238000000638 solvent extraction Methods 0.000 description 1
- 239000007858 starting material Substances 0.000 description 1
- 239000003765 sweetening agent Substances 0.000 description 1
- 239000000811 xylitol Substances 0.000 description 1
- 235000010447 xylitol Nutrition 0.000 description 1
- HEBKCHPVOIAQTA-SCDXWVJYSA-N xylitol Chemical compound OC[C@H](O)[C@@H](O)[C@H](O)CO HEBKCHPVOIAQTA-SCDXWVJYSA-N 0.000 description 1
- 229960002675 xylitol Drugs 0.000 description 1
Images
Classifications
-
- 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
-
- A—HUMAN NECESSITIES
- A23—FOODS OR FOODSTUFFS; TREATMENT THEREOF, NOT COVERED BY OTHER CLASSES
- A23J—PROTEIN COMPOSITIONS FOR FOODSTUFFS; WORKING-UP PROTEINS FOR FOODSTUFFS; PHOSPHATIDE COMPOSITIONS FOR FOODSTUFFS
- A23J1/00—Obtaining protein compositions for foodstuffs; Bulk opening of eggs and separation of yolks from whites
- A23J1/001—Obtaining protein compositions for foodstuffs; Bulk opening of eggs and separation of yolks from whites from waste materials, e.g. kitchen waste
- A23J1/005—Obtaining protein compositions for foodstuffs; Bulk opening of eggs and separation of yolks from whites from waste materials, e.g. kitchen waste from vegetable waste materials
-
- A—HUMAN NECESSITIES
- A23—FOODS OR FOODSTUFFS; TREATMENT THEREOF, NOT COVERED BY OTHER CLASSES
- A23K—FODDER
- A23K10/00—Animal feeding-stuffs
- A23K10/10—Animal feeding-stuffs obtained by microbiological or biochemical processes
- A23K10/12—Animal feeding-stuffs obtained by microbiological or biochemical processes by fermentation of natural products, e.g. of vegetable material, animal waste material or biomass
-
- A—HUMAN NECESSITIES
- A23—FOODS OR FOODSTUFFS; TREATMENT THEREOF, NOT COVERED BY OTHER CLASSES
- A23K—FODDER
- A23K10/00—Animal feeding-stuffs
- A23K10/30—Animal feeding-stuffs from material of plant origin, e.g. roots, seeds or hay; from material of fungal origin, e.g. mushrooms
- A23K10/33—Animal feeding-stuffs from material of plant origin, e.g. roots, seeds or hay; from material of fungal origin, e.g. mushrooms from molasses
-
- C—CHEMISTRY; METALLURGY
- C05—FERTILISERS; MANUFACTURE THEREOF
- C05F—ORGANIC FERTILISERS NOT COVERED BY SUBCLASSES C05B, C05C, e.g. FERTILISERS FROM WASTE OR REFUSE
- C05F5/00—Fertilisers from distillery wastes, molasses, vinasses, sugar plant or similar wastes or residues, e.g. from waste originating from industrial processing of raw material of agricultural origin or derived products thereof
-
- 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
- C12P7/00—Preparation of oxygen-containing organic compounds
- C12P7/02—Preparation of oxygen-containing organic compounds containing a hydroxy group
- C12P7/04—Preparation of oxygen-containing organic compounds containing a hydroxy group acyclic
- C12P7/06—Ethanol, i.e. non-beverage
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
- Y02A40/00—Adaptation technologies in agriculture, forestry, livestock or agroalimentary production
- Y02A40/10—Adaptation technologies in agriculture, forestry, livestock or agroalimentary production in agriculture
- Y02A40/20—Fertilizers of biological origin, e.g. guano or fertilizers made from animal corpses
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E50/00—Technologies for the production of fuel of non-fossil origin
- Y02E50/10—Biofuels, e.g. bio-diesel
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P60/00—Technologies relating to agriculture, livestock or agroalimentary industries
- Y02P60/80—Food processing, e.g. use of renewable energies or variable speed drives in handling, conveying or stacking
- Y02P60/87—Re-use of by-products of food processing for fodder production
Definitions
- This invention relates to a process for the manufacture of multiple valuable products from various wastes generated during the production and recovery of cane sugar, as well from other agricultural cellulosic biomass materials.
- the cane sugar industry generates vast quantities of liquid wastes and solid residues during the production of its primary product. These include sugar cane bagasse and liquor streams containing large quantities of low-grade sugars. Bagasse is usually burned inefficiently in boilers to generate steam and power. The liquid waste streams, mostly molasses, are usually sold as low-grade cattle feed additives.
- the cane sugar industry is normally a highly competitive, low profit industry.
- One approach to improve profitability is to convert these wastes and residues into saleable products that can add to the revenues of the industry.
- the value of this approach has been recognized for a number of years and considerable research and commercial development has been undertaken to identify useful products, such as furfural and papermaking pulp that can be generated from these wastes.
- organosolv pulping A new type of pulping technology, known as organosolv pulping, has distinct advantages for the cane sugar industry. It has almost no environmental problems, is less capital intensive than kraft, it produces multiple co-products, is ideally suited to pulping non-wood biomass that contain high levels of inorganic materials, and can be profitably operated on a much smaller scale than conventional pulping processes. Organosolv pulping has been described in numerous patents and publications including U.S. Pat. No. 3,585,104 Kleinert, U.S. Pat. No. 4,100,016 Diebold et al., U.S. Pat. No. 4,496,426 Baumeister et al.
- organosolv pulping has numerous advantages over conventional chemical pulping methods, such as the kraft, sulfite and the soda processes, in the pulping of wood and other woody biomass resources, it suffers from a disadvantage of significant losses of the relatively costly organic solvent from the process. If the solvent employed is ethanol the environmental consequences of this loss is minor, but the economic consequences can be important, since they can make the operating costs of an organosolv process higher than those for conventional chemical pulping processes. This requires the provision of substantial quantities of expensive make-up solvent to the process. This higher operating cost is one major reason that has held back the commercial acceptance of organosolv pulping processes.
- Such a pulp mill processing bagasse would ideally be situated adjacent to a cane sugar mill, since the bagasse is a low value product of these mills. Therefore no transportation costs would be incurred for the raw material.
- Another low value by-product of the sugar mill is molasses, a high sugar content liquid by-product. It is well recognized that molasses can be readily fermented commercially to yield ethanol. It therefore represents a low cost fermentation feedstock present at the sugar mill.
- ethanol-based organosolv pulping is highly compatible with an agricultural economy. Its primary process chemical is ethanol, which can be easily produced by fermentation of waste sugars and starch. Furthermore, many of the co-products of the process find immediate use and value in agriculture, such as animal feed supplements and slow release fertilizer and pesticides.
- This invention solves the problem of the high capital cost of a dedicated small fermentation plant to provide make-up ethanol by physically integrating the fermentation of molasses into the process equipment of an organosolv pulp mill. A single mill consisting of organosolv pulping of biomass residues integrated with the processing and fermentation of aqueous waste streams will result in major profits for the cane sugar industry. At the same time such a strategy will result in a high degree of environmental protection and support for the development of adjacent industrial activities based on the co-products of this process.
- the present invention provides a process for delignifying biomass fibrous residues comprising digesting biomass fibrous residues in a mixture of ethanol and water in a digester at elevated temperature and pressure.
- the process would include the step of treating spent liquor to recover lignin, acetic acid, furfural, xylose and other co-products, as well as recovering alcohol for re-use in the process and subjecting various liquid sugar waste streams of the process and from a cane sugar mill to fermentation in order to produce ethanol and other fermentation products which may be used in the process.
- the recovery of ethanol from the spent cooking liquors and the recovery of ethanol from the fermentation liquors would be accomplished in the same process equipment.
- These two processes, the organosolv pulping and the fermentation of waste sugar streams, would be accomplished in the same plant, which would allow equipment, heat and energy integration providing considerable economic advantages.
- This process concept is applicable to other biomass residues as well as cane-sugar residues.
- the distillation tower in the process could recover not only ethanol for recycle, but also furfural and ethyl acetate, two valuable products that are generated during the bagasse cooking stage. Both can be sold, probably as crude products suitable for upgrading at a centralized facility. Such activities would encourage the formation of additional local industries designed to support the sugar cane processors using the technology described in this invention. Other local industries could take the lignin produced in these mills and convert it to value-added products, such as concrete admixtures and dye dispersants. Other options presented by this invention include the recovery of xylose (a sugar present in large quantities, mostly as xylan, in bagasse).
- xylose This could be sold in the world market for pure xylose that is used as a starting material in the production of the anti-caries sweetener, xylitol.
- Xylose can also be converted to furfural. If market prices support this option then xylose recovery could be maximized by extended steaming of the bagasse prior to cooking. Xylose would be recovered from the steaming condensate.
- FIG. 1 is a flow diagram identifying the unit process steps of an integrated process for the production of pulp and several useful by-products from bagasse, a biomass residue of the cane sugar industry. While not every unit process is essential for the economic success of the invention, the combination of all these unit processes provides maximum utility of the invention.
- the present invention is directed at a single integrated process that converts biomass residues from the cane sugar industry, sometimes referred to as bagasse, into a series of valuable products including, but not limited to, papermaking pulps.
- the process is integrated with the element of fermentation of waste and low-grade molasses to produce ethanol, other fermentation products and high protein animal feed. Other sources of low grade, but fermentable carbohydrate may be substituted for molasses in this invention.
- a key element incorporated into the process is organosolv delignification of bagasse. This element utilizes some of the alcohol generated in the fermentation element.
- the organosolv element generates products such as lignin, xylose, furfural, acetic acid and pulp for use in papermaking, dietary fibre, or as chemical cellulose.
- Much utility is gained by integrating these several elements into a single process.
- the advantages include heat and energy reduction through process integration, capital reduction through the co-processing of various process streams and waste minimization opportunities through the combining of several process streams.
- the process starts with the preparation of the bagasse into a form suitable for packing into a pressure vessel, identified in FIG. 1 as a digester.
- the preferred form is into stem sections of approximately ten centimeters in length, but any similar form is appropriate.
- a compressed pellet is also appropriate as feed for the digester.
- the digester is one of a series of batch digesters that may be rotating spheres, or a continuous conveyed inclined or horizontal tube configuration, but could also be a vertical tubular batch or continuous design.
- FIG. 1 a preferred configuration of a rotating globe batch digester configuration is illustrated.
- the operations described below for one digester are identical to those for the additional digesters that are operated sequentially at appropriate intervals to allow optimal use of the remaining equipment in the process.
- nitrogen gas may be substituted for steam for the air displacement.
- All valves are now closed and the pump, 43 , in the line exiting the 2 nd liquor tank is turned on.
- the 2 nd liquor tank is full of aqueous alcohol at the desired concentration and temperature.
- This liquor was used as a wash liquor from a previous digester cook and was retained between cooks in the 2 nd Liquor Tank, 3 .
- the preferred alcohol concentration in water is in the range of 35%-70% (w/w) and the preferred temperature is in the range of 170°-205° C.
- This liquor is pumped through a heat exchanger, 44 , to maintain its desired temperature and then into the top of the digester through the top liquor line.
- This hot liquor circulation is continued for the appropriate time necessary to raise the contents of the digester to the desired cooking temperature.
- the liquor exit valve, 46 is closed and the desired weight of hot liquor, usually 2 to 5 times the dry weight of the bagasse, is Pumped into the digester from the 2 nd Liquor Tank. Liquor flow is then stopped, steam is continually sent to a jacket surrounding the digester to maintain its temperature at the desired cooking temperature and the globe digester is rotated for the desired cooking time.
- This time is normally between 30 minutes and 3 hours, with the preferred time being between one and two hours.
- the rotation of the digester is stopped with the liquor outlet line and surrounding screen at the bottom of the digester.
- Part of the hot black liquor is then flashed into a Flash Tank, 6 .
- the valve at the top of the 2 nd Liquor Tank is then closed and the return liquor is diverted to the Spent Liquor Tank.
- Residual liquor in the 2 nd Liquor Tank is pumped down to a level sufficient to keep the suction side of the pump flooded. Liquor remaining in the Digester is drained through the lower screens into a drain line from where it is also pumped to the Spent Liquor Tank.
- the alcohol-rich vapors are condensed and returned to the Recovery Alcohol Tank, 9 , for re-use in the process.
- the partially-delignified fibres are now sluiced from the Digester through the bottom valve, using water or preferably condensate from the evaporator.
- This sluiced pulp is sent to a tank, 51 , from which it is pumped continuously to conventional pulp refining, washing, screening, cleaning and bleaching operations.
- the liquor from these operations can be processed by conventional means for alcohol recovery and sodium acetate recovery.
- the spent liquor under pressure in the Spent Liquor Tank, 4 is flashed into a Flash Tank, 6 , and the vapors condensed through the Blow-Down Condenser, 35 , and returned to the Recovery Alcohol Tank, 9 , for re-use.
- the condensed liquor in the Flash Tank, containing the extracted lignin is then pumped to the Lignin Precipitation Tank, 7 , where it is mixed rapidly with stillage from the Distillation Tower, 14 , and the pH adjusted to below 3.0 with acid and the mixture cooled to about 17°. Lignin precipitates from the mixture and forms a slurry.
- a suitable filtering device such as a drum filter, 13
- the lignin is removed as a wet cake that is sent to an appropriate drier
- the filtrate is pumped to a Recovery Feed Tank, 54 .
- the filtrate is pumped to an appropriately designed Distillation Tower, 14 .
- Such a tower would have a lower steam stripping section and an upper rectifying section, or be composed of two columns having these functions.
- alcohol together with some esters, is recovered as an overhead condensate and returned to the Recovery Alcohol Tank for re-use in the process.
- Furfural which is present in the filtrate, accumulates at one of the lower trays in the rectifier section where it is drawn off, cooled and mixed with water before being sent to the Decanter.
- the lower liquid phase in the decanter is crude furfural, which is upgraded to merchant furfural in a commercially available system.
- the upper layer is aqueous alcohol, which is passed back to the Distillation Tower to recover the alcohol by mixing with the tower feed stream. Steam to power the stream stripping section is provided by Reboilers at the bottom of the tower.
- the aqueous condensate from the Evaporator is passed to a commercially-available solvent extraction unit, 21 , such as those employing tri-octyl phosphine oxide, (TOPO), for recovery of acetic acid, formic acid, furfural and ethanol as separate marketable products.
- solvent extraction unit 21 such as those employing tri-octyl phosphine oxide, (TOPO), for recovery of acetic acid, formic acid, furfural and ethanol as separate marketable products.
- TOPO tri-octyl phosphine oxide
- Molasses is used as the fermentation raw material in a fermentation plant, 26 , employing yeast to produce ethanol and other fermentation products.
- This medium may be supplemented with additional sugars from acid-hydrolysis products of waste cellulose, as required for maximum productivity. Additional minerals that may be required at this stage can be supplied from the waste liquor stream of the xylose recovery plant.
- the beer is pumped to a Filter, 31 , where yeast and other solids are removed and dried for sale as high-protein animal feed supplement.
- the clarified beer is then passed to the Recovery Feed Tank, 54 , mixed with the filtrate from the Lignin Recovery Filter and pumped to the Distillation Tower for recovery of ethanol and other components.
Landscapes
- Life Sciences & Earth Sciences (AREA)
- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Polymers & Plastics (AREA)
- Zoology (AREA)
- Biotechnology (AREA)
- Organic Chemistry (AREA)
- Biochemistry (AREA)
- Health & Medical Sciences (AREA)
- Food Science & Technology (AREA)
- Wood Science & Technology (AREA)
- Molecular Biology (AREA)
- Physiology (AREA)
- Animal Husbandry (AREA)
- Microbiology (AREA)
- Botany (AREA)
- Biomedical Technology (AREA)
- Sustainable Development (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Environmental & Geological Engineering (AREA)
- Bioinformatics & Cheminformatics (AREA)
- General Engineering & Computer Science (AREA)
- General Health & Medical Sciences (AREA)
- Genetics & Genomics (AREA)
- Mycology (AREA)
- Preparation Of Compounds By Using Micro-Organisms (AREA)
Abstract
An integrated process for the combined fermentation and the conversion of liquid and solid residues generated by the cane sugar industry into a variety of useful products. The process also relates to the treatment of other biomass materials. The process combines elements of alcohol-based organosolv pulping with fermentation in a fully integrated operation. This process eliminates the need for separate costly facilities, thus reducing capital and operating costs, providing opportunities for heat and energy reduction and a high degree of internal process recycle. The process would replace costly waste and residue treatment operations with revenue generating operations.
Description
- Australian Patent Application No: 51888/00; Filing Date: Aug. 8, 2000; Relationship: Equivalent claims
- U.S. Provisional Patent Application No. 60/307,712; Filing Date: Jul. 26, 2001; Relationship: Equivalent claims
- This invention relates to a process for the manufacture of multiple valuable products from various wastes generated during the production and recovery of cane sugar, as well from other agricultural cellulosic biomass materials.
- The cane sugar industry generates vast quantities of liquid wastes and solid residues during the production of its primary product. These include sugar cane bagasse and liquor streams containing large quantities of low-grade sugars. Bagasse is usually burned inefficiently in boilers to generate steam and power. The liquid waste streams, mostly molasses, are usually sold as low-grade cattle feed additives.
- The cane sugar industry is normally a highly competitive, low profit industry. One approach to improve profitability is to convert these wastes and residues into saleable products that can add to the revenues of the industry. The value of this approach has been recognized for a number of years and considerable research and commercial development has been undertaken to identify useful products, such as furfural and papermaking pulp that can be generated from these wastes.
- A new type of pulping technology, known as organosolv pulping, has distinct advantages for the cane sugar industry. It has almost no environmental problems, is less capital intensive than kraft, it produces multiple co-products, is ideally suited to pulping non-wood biomass that contain high levels of inorganic materials, and can be profitably operated on a much smaller scale than conventional pulping processes. Organosolv pulping has been described in numerous patents and publications including U.S. Pat. No. 3,585,104 Kleinert, U.S. Pat. No. 4,100,016 Diebold et al., U.S. Pat. No. 4,496,426 Baumeister et al. Although organosolv pulping has numerous advantages over conventional chemical pulping methods, such as the kraft, sulfite and the soda processes, in the pulping of wood and other woody biomass resources, it suffers from a disadvantage of significant losses of the relatively costly organic solvent from the process. If the solvent employed is ethanol the environmental consequences of this loss is minor, but the economic consequences can be important, since they can make the operating costs of an organosolv process higher than those for conventional chemical pulping processes. This requires the provision of substantial quantities of expensive make-up solvent to the process. This higher operating cost is one major reason that has held back the commercial acceptance of organosolv pulping processes.
- One approach to reducing the cost of make-up solvent required by an organosolv pulp mill, to make it economically attractive, is to produce the required make-up solvent on site. For an ethanol-based organosolv pulp mill a fermentation facility can be constructed adjacent to the pulp mill for this purpose. However, if constructed on a small size sufficient for the make-up needs of a small pulp mill, the relative capital costs of such a fermentation facility would make it economically unattractive. Furthermore, if the pulp mill uses wood as a raw material, the fermentation plant would need to purchase fermentation feedstock, such as sugar or starch, at considerable cost. This problem can be overcome for an ethanol-based organosolv pulp mill processing agricultural residues, such as bagasse. Such a pulp mill processing bagasse would ideally be situated adjacent to a cane sugar mill, since the bagasse is a low value product of these mills. Therefore no transportation costs would be incurred for the raw material. Another low value by-product of the sugar mill is molasses, a high sugar content liquid by-product. It is well recognized that molasses can be readily fermented commercially to yield ethanol. It therefore represents a low cost fermentation feedstock present at the sugar mill.
- Even more attractive for the cane sugar industry is that ethanol-based organosolv pulping is highly compatible with an agricultural economy. Its primary process chemical is ethanol, which can be easily produced by fermentation of waste sugars and starch. Furthermore, many of the co-products of the process find immediate use and value in agriculture, such as animal feed supplements and slow release fertilizer and pesticides. This invention solves the problem of the high capital cost of a dedicated small fermentation plant to provide make-up ethanol by physically integrating the fermentation of molasses into the process equipment of an organosolv pulp mill. A single mill consisting of organosolv pulping of biomass residues integrated with the processing and fermentation of aqueous waste streams will result in major profits for the cane sugar industry. At the same time such a strategy will result in a high degree of environmental protection and support for the development of adjacent industrial activities based on the co-products of this process.
- The present invention provides a process for delignifying biomass fibrous residues comprising digesting biomass fibrous residues in a mixture of ethanol and water in a digester at elevated temperature and pressure.
- The process would include the step of treating spent liquor to recover lignin, acetic acid, furfural, xylose and other co-products, as well as recovering alcohol for re-use in the process and subjecting various liquid sugar waste streams of the process and from a cane sugar mill to fermentation in order to produce ethanol and other fermentation products which may be used in the process. The recovery of ethanol from the spent cooking liquors and the recovery of ethanol from the fermentation liquors would be accomplished in the same process equipment. These two processes, the organosolv pulping and the fermentation of waste sugar streams, would be accomplished in the same plant, which would allow equipment, heat and energy integration providing considerable economic advantages. This process concept is applicable to other biomass residues as well as cane-sugar residues. The potential advantages of integrating these two formerly separate activities into a single operating unit are numerous. They include lower total capital costs, combining different liquor streams for common product recovery, opportunities for process heat and energy reduction, internal process chemical production, reduced transportation costs, substantial environmental improvement and the potential for the use of larger, more efficient equipment in a shared operation. Separate facilities operating in isolation may not be economic. This identifies the unit processes and the product flows in an integrated total process that would provide these advantages to the cane sugar industry.
- The distillation tower in the process could recover not only ethanol for recycle, but also furfural and ethyl acetate, two valuable products that are generated during the bagasse cooking stage. Both can be sold, probably as crude products suitable for upgrading at a centralized facility. Such activities would encourage the formation of additional local industries designed to support the sugar cane processors using the technology described in this invention. Other local industries could take the lignin produced in these mills and convert it to value-added products, such as concrete admixtures and dye dispersants. Other options presented by this invention include the recovery of xylose (a sugar present in large quantities, mostly as xylan, in bagasse). This could be sold in the world market for pure xylose that is used as a starting material in the production of the anti-caries sweetener, xylitol. Xylose can also be converted to furfural. If market prices support this option then xylose recovery could be maximized by extended steaming of the bagasse prior to cooking. Xylose would be recovered from the steaming condensate.
- Utilizing this invention could lead to higher value pulps which would have high alpha-cellulose content and therefore be suitable for rayon production. The result for the cane sugar industry of practicing this invention would be the elimination of costly environmental control operations and the production of significant revenues from the sale of several value-added products. These products would in turn create opportunities for the introduction of ancillary industries.
- In the accompanying drawing, which illustrates by way of example the embodiment of this invention,
- FIG. 1 is a flow diagram identifying the unit process steps of an integrated process for the production of pulp and several useful by-products from bagasse, a biomass residue of the cane sugar industry. While not every unit process is essential for the economic success of the invention, the combination of all these unit processes provides maximum utility of the invention.
- The present invention is directed at a single integrated process that converts biomass residues from the cane sugar industry, sometimes referred to as bagasse, into a series of valuable products including, but not limited to, papermaking pulps. The process is integrated with the element of fermentation of waste and low-grade molasses to produce ethanol, other fermentation products and high protein animal feed. Other sources of low grade, but fermentable carbohydrate may be substituted for molasses in this invention. A key element incorporated into the process is organosolv delignification of bagasse. This element utilizes some of the alcohol generated in the fermentation element. The organosolv element generates products such as lignin, xylose, furfural, acetic acid and pulp for use in papermaking, dietary fibre, or as chemical cellulose. Much utility is gained by integrating these several elements into a single process. The advantages include heat and energy reduction through process integration, capital reduction through the co-processing of various process streams and waste minimization opportunities through the combining of several process streams. These elements and advantages are illustrated in the process flow diagram, FIG. 1.
- The process starts with the preparation of the bagasse into a form suitable for packing into a pressure vessel, identified in FIG. 1 as a digester. The preferred form is into stem sections of approximately ten centimeters in length, but any similar form is appropriate. A compressed pellet is also appropriate as feed for the digester. As illustrated the digester is one of a series of batch digesters that may be rotating spheres, or a continuous conveyed inclined or horizontal tube configuration, but could also be a vertical tubular batch or continuous design. In FIG. 1 a preferred configuration of a rotating globe batch digester configuration is illustrated. The operations described below for one digester are identical to those for the additional digesters that are operated sequentially at appropriate intervals to allow optimal use of the remaining equipment in the process.
- Following preparation of the fibrous residue (bagasse) into the useful form described above it is conveyed by conveyer,41, to the top of the digester for loading into the digester. Once the digesters, is filled with a pre-determined amount of bagasse, the conveyer is stopped and the digester is closed. An exhaust valve, 46, located behind a screen, 42, in the bottom of the digester is now opened and low-pressure steam (less than 50 psi) is allowed to enter the top of the digester through a pipe, 45. This steaming, which is required to displace air in the fibre bed, continues until temperature sensors in the exhaust line indicate that steam is exiting from the bottom of the digester. Any condensate of the steaming exits through the same line. Alternatively, if the moisture content of the bagasse is too high, nitrogen gas may be substituted for steam for the air displacement. All valves are now closed and the pump, 43, in the line exiting the 2nd liquor tank is turned on. The 2nd liquor tank is full of aqueous alcohol at the desired concentration and temperature. This liquor was used as a wash liquor from a previous digester cook and was retained between cooks in the 2nd Liquor Tank, 3. The preferred alcohol concentration in water is in the range of 35%-70% (w/w) and the preferred temperature is in the range of 170°-205° C. This liquor is pumped through a heat exchanger, 44, to maintain its desired temperature and then into the top of the digester through the top liquor line. Once the digester starts to fill, liquor exits the bottom of the digester from behind a screen, 42, constructed around the outlet line at the bottom of the digester, from where it is returned to the top of the 2nd Liquor Tank, 3. This hot liquor circulation is continued for the appropriate time necessary to raise the contents of the digester to the desired cooking temperature. At this point the liquor exit valve, 46, is closed and the desired weight of hot liquor, usually 2 to 5 times the dry weight of the bagasse, is Pumped into the digester from the 2nd Liquor Tank. Liquor flow is then stopped, steam is continually sent to a jacket surrounding the digester to maintain its temperature at the desired cooking temperature and the globe digester is rotated for the desired cooking time. This time is normally between 30 minutes and 3 hours, with the preferred time being between one and two hours. At the end of this time the rotation of the digester is stopped with the liquor outlet line and surrounding screen at the bottom of the digester. Part of the hot black liquor is then flashed into a Flash Tank, 6. The valve at the top of the 2nd Liquor Tank is then closed and the return liquor is diverted to the Spent Liquor Tank. Residual liquor in the 2nd Liquor Tank is pumped down to a level sufficient to keep the suction side of the pump flooded. Liquor remaining in the Digester is drained through the lower screens into a drain line from where it is also pumped to the Spent Liquor Tank. Next, clean aqueous alcohol at the concentration and temperature previously described is pumped from the 1st Liquor Tank, 2, into the top and bottom lines of the Digester and returned to the 2nd Liquor Tank, 3, using the appropriate valves and pumps. After the 1st Liquor Tank has been almost emptied liquor flow to the Digester is stopped and the remaining liquor in the Digester is drained down and pumped to the 2nd Liquor Tank through the appropriate lines and valves. The Digester is now depressurized by opening the valves in the top line and the vapors passed to a Blow-Down Condenser, 35. The alcohol-rich vapors are condensed and returned to the Recovery Alcohol Tank, 9, for re-use in the process. The partially-delignified fibres are now sluiced from the Digester through the bottom valve, using water or preferably condensate from the evaporator. This sluiced pulp is sent to a tank, 51, from which it is pumped continuously to conventional pulp refining, washing, screening, cleaning and bleaching operations. The liquor from these operations can be processed by conventional means for alcohol recovery and sodium acetate recovery.
- The spent liquor under pressure in the Spent Liquor Tank,4, is flashed into a Flash Tank, 6, and the vapors condensed through the Blow-Down Condenser, 35, and returned to the Recovery Alcohol Tank, 9, for re-use. The condensed liquor in the Flash Tank, containing the extracted lignin, is then pumped to the Lignin Precipitation Tank, 7, where it is mixed rapidly with stillage from the Distillation Tower, 14, and the pH adjusted to below 3.0 with acid and the mixture cooled to about 17°. Lignin precipitates from the mixture and forms a slurry. This is pumped to a suitable filtering device, such as a drum filter, 13, where the lignin is removed as a wet cake that is sent to an appropriate drier, while the filtrate is pumped to a Recovery Feed Tank, 54. From this tank the filtrate is pumped to an appropriately designed Distillation Tower, 14. Such a tower would have a lower steam stripping section and an upper rectifying section, or be composed of two columns having these functions. In this tower alcohol, together with some esters, is recovered as an overhead condensate and returned to the Recovery Alcohol Tank for re-use in the process. Furfural, which is present in the filtrate, accumulates at one of the lower trays in the rectifier section where it is drawn off, cooled and mixed with water before being sent to the Decanter. The lower liquid phase in the decanter is crude furfural, which is upgraded to merchant furfural in a commercially available system. The upper layer is aqueous alcohol, which is passed back to the Distillation Tower to recover the alcohol by mixing with the tower feed stream. Steam to power the stream stripping section is provided by Reboilers at the bottom of the tower.
- Aqueous stillage from the bottom of the Distillation Tower containing sugars, some lignin and minerals, is sent to an appropriately designed multi-stage evaporator,19, where it is concentrated to about 25% solids. This concentrate is pumped to an Evaporator Concentrate Decanter, 23, where a lower layer of oily lignin is recovered and dried. The upper aqueous layer containing xylose, xylans, other sugars and minerals, is sent to a commercially available xylose recovery unit, 24, for production of purified xylose. The effluents from this unit include waste hexose sugars, which are passed to the fermentation operations for alcohol production, and an aqueous solution of minerals, which are returned to the cane fields as fertilizer.
- The aqueous condensate from the Evaporator is passed to a commercially-available solvent extraction unit,21, such as those employing tri-octyl phosphine oxide, (TOPO), for recovery of acetic acid, formic acid, furfural and ethanol as separate marketable products. The clean water that exits this unit is useful in the pulp washing and bleaching operations.
- Molasses is used as the fermentation raw material in a fermentation plant,26, employing yeast to produce ethanol and other fermentation products. This medium may be supplemented with additional sugars from acid-hydrolysis products of waste cellulose, as required for maximum productivity. Additional minerals that may be required at this stage can be supplied from the waste liquor stream of the xylose recovery plant. After fermentation is complete in a sequential battery of batch Fermenters, the beer is pumped to a Filter, 31, where yeast and other solids are removed and dried for sale as high-protein animal feed supplement. The clarified beer is then passed to the Recovery Feed Tank, 54, mixed with the filtrate from the Lignin Recovery Filter and pumped to the Distillation Tower for recovery of ethanol and other components.
- By this invention a range of valuable products is produced from the solid and liquid residues of the cane sugar industry.
Claims (12)
1. An integrated process performing fermentation of low value (molasses) and waste sugars together with the conversion of biomass residues from the cane sugar industry (bagasse) for the production of multiple useful products. Such process combines the elements of alcohol-based organosolv pulping and ethanol fermentation into a single integrated process.
2. A process, as in claim 1 , in which the useful products are any combination, or number, of products including unbleached papermaking pulp, bleached papermaking pulp, high alpha-cellulose pulp, organosolv lignin, furfural, acetic acid, ethyl acetate, sodium acetate, xylose, xylan, butanol, acetone, high-protein animal feed, plant fertilizer, uronic acids and ethanol.
3. A process for delignifying biomass fibrous residues comprising, digesting biomass fibrous residues in a mixture of ethanol and water in a digester at elevated temperature and pressure, continually exposing the mixture of ethanol and water to the fibrous residues in a suitable digester, or by circulating the mixture of ethanol and water between the digester and a holding tank for a time sufficient to at least partially delignify the biomass fibrous residues and form a pulp, draining the mixture to a spent liquor tank at the end of the circulation time, causing the remaining liquor and partially delignified biomass to transfer from the digester to a blow tank by opening the valve to the blow tank.
4. A process according to claim 3 , wherein the process includes the step of recovering lignin and other chemicals from the mixture of ethanol and water contained in the spent liquor tank.
5. A process according to claim 3 or claim 4 , wherein the mixture of ethanol and water in the digester is maintained at a temperature in a range from 170 to 205° C.
6. A process according to claim 5 , wherein the pressure in the digester and the holding tank is maintained at a level sufficient to prevent the mixture of water and ethanol from vaporizing.
7. A process according to any one of claims 3 to 6 , wherein the mixture of ethanol and water in the digester contains ethanol and water in a ratio in a range from 35% to 70% by weight ethanol to water.
8. A process according to any one of claims 3 to 7 , wherein the circulation time lies in a range from 30 minutes to 3 hours.
9. A process according to claim 8 , wherein the circulation time lies in a range from 1 to 2 hours.
10. A process according to any one of claims 3 to 9 , wherein the process includes transferring the contents of the spent liquor tank to a flash tank to enable volatile material to evaporate thereby leaving a lignin-rich condensed liquor, lowering the pH of the condensed liquor to a level below 3, diluting the condensed liquor with an aqueous stream and cooling the condensed liquor to cause lignin to precipitate from the mother liquor and separating lignin from the mother liquor.
11. A process according to claim 10 , wherein the process includes the steps of distilling the diluted mother liquor to recover ethanol and furfural therefrom leaving an aqueous stillage.
12. A process according to claim 11 , including the steps of concentrating the aqueous stillage by evaporation, allowing a liquid lignin fraction to settle, removing the liquid lignin fraction from an upper layer of the aqueous stillage thereby leaving an aqueous layer containing xylose, xylan and other sugars.
Priority Applications (1)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
US10/072,219 US20020069987A1 (en) | 2000-08-08 | 2002-02-09 | Integrated processing of biomass and liquid effluents |
Applications Claiming Priority (4)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
AU51888/00 | 2000-08-08 | ||
AU51888/00A AU779714B2 (en) | 1999-08-11 | 2000-08-08 | Process for treating biomass fibrous material |
US30771201P | 2001-07-26 | 2001-07-26 | |
US10/072,219 US20020069987A1 (en) | 2000-08-08 | 2002-02-09 | Integrated processing of biomass and liquid effluents |
Publications (1)
Publication Number | Publication Date |
---|---|
US20020069987A1 true US20020069987A1 (en) | 2002-06-13 |
Family
ID=27154755
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
US10/072,219 Abandoned US20020069987A1 (en) | 2000-08-08 | 2002-02-09 | Integrated processing of biomass and liquid effluents |
Country Status (1)
Country | Link |
---|---|
US (1) | US20020069987A1 (en) |
Cited By (51)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
EP1462565A1 (en) * | 2003-03-26 | 2004-09-29 | Yuen Foong Yu Paper MFG Company, Limited | Method for producing a plant nutrition composition from a biopulp filtrate and a formulated plant nutrition so produced |
US20050269048A1 (en) * | 2003-06-03 | 2005-12-08 | Fortune Forest & Lignin S.A. De C.V. | Novel catalytic reactor process for the production of commercial grade pulp, native lignin & unicellular protein |
US20060162239A1 (en) * | 2004-12-23 | 2006-07-27 | Van Den Brink Peter J | Process for the hydrogenation of a lactone or of a carboxylic acid or an ester having a gamma-carbonyl group |
WO2006134126A1 (en) * | 2005-06-15 | 2006-12-21 | Shell Internationale Research Maatschappij B.V. | A process for organosolv pulping and use of a gamma lactone in a solvent for organosolv pulping |
US20070100162A1 (en) * | 2003-12-15 | 2007-05-03 | Leonardus Petrus | Process for the liquefaction of lignocellulosic material |
US20070259412A1 (en) * | 2006-05-08 | 2007-11-08 | Biojoule Limited | Process for the production of biofuel from plant materials |
US20090062516A1 (en) * | 2006-05-08 | 2009-03-05 | Biojoule Limited | Lignin and other products isolated from plant material, methods for isolation and use, and compositions containing lignin and other plant-derived products |
WO2009028969A1 (en) * | 2007-08-31 | 2009-03-05 | Biojoule Ltd | Lignin and other products isolated from plant material, and methods and compositions therefor |
US20100048884A1 (en) * | 2008-07-16 | 2010-02-25 | Srinivas Kilambi | Solvo-thermal hydrolysis of cellulose |
US20100069626A1 (en) * | 2008-07-16 | 2010-03-18 | Sriya Innovations | Nano-catalytic-solvo-thermal technology platform bio-refineries |
US20100146844A1 (en) * | 2008-12-17 | 2010-06-17 | Bp Corporation North America Inc. | Process, Plant And Biofuel From Lignocellulosic Feedstock |
US20100146842A1 (en) * | 2008-12-17 | 2010-06-17 | Bp Corporation North America Inc. | Process, plant and biofuel for integrated biofuel production |
US20100152496A1 (en) * | 2008-12-17 | 2010-06-17 | Bp Corporation North America Inc. | Process, Plant And Butanol From Lignocellulosic Feedstock |
US20100146843A1 (en) * | 2008-12-17 | 2010-06-17 | Bp Corporation North America Inc. | Process, Plant And Biofuel For Integrated Biofuel Production |
US20100251608A1 (en) * | 2008-12-17 | 2010-10-07 | Bp Corporation North America Inc. | Process, Plant, and Biofuel From Lognocellulosic Feedstock |
US20100269990A1 (en) * | 2009-04-23 | 2010-10-28 | Greenfield Ethanol Inc. | Separation of reactive cellulose from lignocellulosic biomass with high lignin content |
US20110046399A1 (en) * | 2009-08-07 | 2011-02-24 | Rene Johan Haan | Process for preparing a hydroxyacid or hydroxyester |
US20110076732A1 (en) * | 2008-12-17 | 2011-03-31 | BP Biofuels UK Limited | Process, Plant, and Butanol From Lignocellulosic Feedstock |
US20110076724A1 (en) * | 2008-12-17 | 2011-03-31 | BP Biofuels UK Limited | Process, Plant, and Biofuel for Integrated Biofuel Production |
US20110112326A1 (en) * | 2009-08-07 | 2011-05-12 | Jean-Paul Lange | Process for hydrogenation |
US20110126448A1 (en) * | 2008-12-17 | 2011-06-02 | BP Biofuels UK Limited | Process, Plant, and Biofuel For Integrated Biofuel Production |
WO2011126369A1 (en) * | 2010-04-09 | 2011-10-13 | Stichting Dienst Landbouwkundig Onderzoek | Acetic acid based refining process of biomass |
US20120108798A1 (en) * | 2008-10-17 | 2012-05-03 | Mascoma Corporation | Production Of Pure Lignin From Lignocellulosic Biomass |
US20120115193A1 (en) * | 2008-07-16 | 2012-05-10 | The Texas A&M University System | Transformation of glycerol and cellulosic materials into high energy fuels |
US20120202260A1 (en) * | 2009-09-04 | 2012-08-09 | Lignol Innovations Ltd. | Hybrid biorefining and gasification of lignocellulosic feedstocks |
EP2150572A4 (en) * | 2007-05-31 | 2013-03-27 | Lignol Innovations Ltd | Continuous counter-current organosolv processing of lignocellulosic feedstocks |
US8409357B2 (en) | 2011-05-04 | 2013-04-02 | Renmatix, Inc. | Self-cleaning apparatus and method for thick slurry pressure control |
WO2013066196A1 (en) * | 2011-11-03 | 2013-05-10 | Lignin Polymers Limited | Method for removal of toxic waste from timber |
WO2013070305A1 (en) * | 2011-08-31 | 2013-05-16 | Dx Resources, Llc | Method and apparatus for ethanol production |
CN103321075A (en) * | 2013-05-22 | 2013-09-25 | 大连工业大学 | Method for recovering low-boiling-point alcohol process pulping waste liquid components |
US8609379B2 (en) | 2010-12-20 | 2013-12-17 | Shell Oil Company | Process for the production of alcohols from biomass |
US8663800B2 (en) | 2011-05-04 | 2014-03-04 | Renmatix, Inc. | Lignin production from lignocellulosic biomass |
WO2014060674A1 (en) * | 2012-10-18 | 2014-04-24 | IFP Energies Nouvelles | Method for producing ethanol from biomass, including recirculating an internal flow containing ethanol upstream from or within the pretreatment |
WO2014060673A1 (en) * | 2012-10-18 | 2014-04-24 | IFP Energies Nouvelles | Method for producing alcohols and/or solvents from a biomass, including recirculating an internal flow including alcohols and/or solvents upstream from or within the pretreatment |
US8759498B2 (en) | 2011-12-30 | 2014-06-24 | Renmatix, Inc. | Compositions comprising lignin |
WO2014134697A1 (en) * | 2013-03-06 | 2014-09-12 | Citrotec Indústria E Comércio Ltda | Improvement to vinasse-concentration plant integrated with an ethanol distillation facility |
US8889384B2 (en) | 2010-10-07 | 2014-11-18 | Shell Oil Company | Process for the production of alcohols from biomass |
US9187862B2 (en) | 2010-11-05 | 2015-11-17 | Greenfield Specialty Alcohols Inc. | Bagasse fractionation for cellulosic ethanol and chemical production |
US9255189B2 (en) | 2011-07-28 | 2016-02-09 | Greenfield Specialty Alcohols Inc. | Ethanol production with two stage continuous steam pre-treatment of lignocellulosic biomass |
US9446326B2 (en) | 2011-08-31 | 2016-09-20 | Dx Resources Llc | Method and apparatus for ethanol production |
US9708490B2 (en) | 2009-05-28 | 2017-07-18 | Fibria Innovations Inc. | Derivatives of native lignin |
US9840621B2 (en) | 2011-03-24 | 2017-12-12 | Fibria Innovations Inc. | Compositions comprising lignocellulosic biomass and organic solvent |
EP3279329A1 (en) | 2006-07-21 | 2018-02-07 | Xyleco, Inc. | Conversion systems for biomass |
US9932707B2 (en) | 2010-11-05 | 2018-04-03 | Greenfield Specialty Alcohols Inc. | Bagasse fractionation for cellulosic ethanol and chemical production |
US9982174B2 (en) | 2010-02-15 | 2018-05-29 | Fibria Innovations Inc. | Binder compositions comprising lignin derivatives |
US10053745B2 (en) | 2010-01-19 | 2018-08-21 | Renmatix, Inc. | Production of fermentable sugars and lignin from biomass using supercritical fluids |
US10533030B2 (en) | 2010-02-15 | 2020-01-14 | Suzano Canada Inc. | Carbon fibre compositions comprising lignin derivatives |
US10793646B2 (en) | 2014-09-26 | 2020-10-06 | Renmatix, Inc. | Adhesive compositions comprising type-II cellulose |
US20210348113A1 (en) * | 2016-07-22 | 2021-11-11 | Vito Nv (Vlaamse Instelling Voor Technologisch Onderzoek Nv) | Method and system for producing products by fermentation |
CN113862318A (en) * | 2021-09-28 | 2021-12-31 | 北京化工大学 | A green and efficient refining system and method for lignocellulose |
KR20240059598A (en) | 2022-10-27 | 2024-05-07 | 류장근 | artificial intelligence based System and Method for business processing |
Citations (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US4470851A (en) * | 1981-03-26 | 1984-09-11 | Laszlo Paszner | High efficiency organosolv saccharification process |
US5730837A (en) * | 1994-12-02 | 1998-03-24 | Midwest Research Institute | Method of separating lignocellulosic material into lignin, cellulose and dissolved sugars |
US5807952A (en) * | 1994-09-19 | 1998-09-15 | Midwest Research Institute | Process for producing phenolic compounds from lignins |
-
2002
- 2002-02-09 US US10/072,219 patent/US20020069987A1/en not_active Abandoned
Patent Citations (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US4470851A (en) * | 1981-03-26 | 1984-09-11 | Laszlo Paszner | High efficiency organosolv saccharification process |
US5807952A (en) * | 1994-09-19 | 1998-09-15 | Midwest Research Institute | Process for producing phenolic compounds from lignins |
US5730837A (en) * | 1994-12-02 | 1998-03-24 | Midwest Research Institute | Method of separating lignocellulosic material into lignin, cellulose and dissolved sugars |
Cited By (78)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
EP1462565A1 (en) * | 2003-03-26 | 2004-09-29 | Yuen Foong Yu Paper MFG Company, Limited | Method for producing a plant nutrition composition from a biopulp filtrate and a formulated plant nutrition so produced |
US7396434B2 (en) * | 2003-06-03 | 2008-07-08 | Jose Antonio Rodriguez Rivera | Catalytic reactor process for the production of commercial grade pulp, native lignin and unicellular protein |
US20050269048A1 (en) * | 2003-06-03 | 2005-12-08 | Fortune Forest & Lignin S.A. De C.V. | Novel catalytic reactor process for the production of commercial grade pulp, native lignin & unicellular protein |
US20070100162A1 (en) * | 2003-12-15 | 2007-05-03 | Leonardus Petrus | Process for the liquefaction of lignocellulosic material |
US20060162239A1 (en) * | 2004-12-23 | 2006-07-27 | Van Den Brink Peter J | Process for the hydrogenation of a lactone or of a carboxylic acid or an ester having a gamma-carbonyl group |
US8003818B2 (en) | 2004-12-23 | 2011-08-23 | Shell Oil Company | Process for the hydrogenation of a lactone or of a carboxylic acid or an ester having a gamma-carbonyl group |
WO2006134126A1 (en) * | 2005-06-15 | 2006-12-21 | Shell Internationale Research Maatschappij B.V. | A process for organosolv pulping and use of a gamma lactone in a solvent for organosolv pulping |
US20070034345A1 (en) * | 2005-06-15 | 2007-02-15 | Leonardus Petrus | Process for organosolv pulping and use of a gamma lactone in a solvent for organosolv pulping |
US20100136642A1 (en) * | 2006-05-08 | 2010-06-03 | Biojoule Limited | Recovery of lignin and water soluble sugars from plant materials |
US8822657B2 (en) | 2006-05-08 | 2014-09-02 | Vertichem Corporation | Recovery of lignin and water soluble sugars from plant materials |
AU2007248991B2 (en) * | 2006-05-08 | 2010-12-23 | Vertichem Corporation | Integrated processing of plant biomass |
US8309694B2 (en) | 2006-05-08 | 2012-11-13 | Vertichem Corporation | Recovery of lignin and water soluble sugars from plant materials |
US7649086B2 (en) | 2006-05-08 | 2010-01-19 | Biojoule Ltd. | Integrated processing of plant biomass |
WO2007129921A1 (en) * | 2006-05-08 | 2007-11-15 | Biojoule Ltd. | Process for the production of biofuel from plant materials |
EP2479341A1 (en) | 2006-05-08 | 2012-07-25 | Vertichem Corporation | Process for the production of biofuel from plant material |
US20070259412A1 (en) * | 2006-05-08 | 2007-11-08 | Biojoule Limited | Process for the production of biofuel from plant materials |
US20090062516A1 (en) * | 2006-05-08 | 2009-03-05 | Biojoule Limited | Lignin and other products isolated from plant material, methods for isolation and use, and compositions containing lignin and other plant-derived products |
US7985847B2 (en) | 2006-05-08 | 2011-07-26 | Biojoule Ltd. | Recovery of lignin and water soluble sugars from plant materials |
EP3279329A1 (en) | 2006-07-21 | 2018-02-07 | Xyleco, Inc. | Conversion systems for biomass |
EP2150572A4 (en) * | 2007-05-31 | 2013-03-27 | Lignol Innovations Ltd | Continuous counter-current organosolv processing of lignocellulosic feedstocks |
US8053566B2 (en) | 2007-08-31 | 2011-11-08 | Vertichem Corporation | Methods for isolating and harvesting lignin and isolated lignin preparations produced using the methods |
US20090069550A1 (en) * | 2007-08-31 | 2009-03-12 | Biojoule Limited | Lignin and other products isolated from plant material, methods for isolation and use, and compositions containing lignin and other plant-derived products |
WO2009028969A1 (en) * | 2007-08-31 | 2009-03-05 | Biojoule Ltd | Lignin and other products isolated from plant material, and methods and compositions therefor |
US20100069626A1 (en) * | 2008-07-16 | 2010-03-18 | Sriya Innovations | Nano-catalytic-solvo-thermal technology platform bio-refineries |
US8546561B2 (en) | 2008-07-16 | 2013-10-01 | Renmatix, Inc. | Nano-catalytic-solvo-thermal technology platform bio-refineries |
US8546560B2 (en) | 2008-07-16 | 2013-10-01 | Renmatix, Inc. | Solvo-thermal hydrolysis of cellulose |
US20120115193A1 (en) * | 2008-07-16 | 2012-05-10 | The Texas A&M University System | Transformation of glycerol and cellulosic materials into high energy fuels |
US9340768B2 (en) * | 2008-07-16 | 2016-05-17 | The Texas A&M University System | Transformation of glycerol and cellulosic materials into high energy fuels |
US20100048884A1 (en) * | 2008-07-16 | 2010-02-25 | Srinivas Kilambi | Solvo-thermal hydrolysis of cellulose |
US20120108798A1 (en) * | 2008-10-17 | 2012-05-03 | Mascoma Corporation | Production Of Pure Lignin From Lignocellulosic Biomass |
US20100146843A1 (en) * | 2008-12-17 | 2010-06-17 | Bp Corporation North America Inc. | Process, Plant And Biofuel For Integrated Biofuel Production |
US20100251608A1 (en) * | 2008-12-17 | 2010-10-07 | Bp Corporation North America Inc. | Process, Plant, and Biofuel From Lognocellulosic Feedstock |
US8152867B2 (en) | 2008-12-17 | 2012-04-10 | Bp Biofuels Uk Ltd. | Process, plant and biofuel for integrated biofuel production |
US8158833B2 (en) | 2008-12-17 | 2012-04-17 | Bp Biofuels Uk Ltd. | Process, plant and butanol from lignocellulosic feedstock |
US20110126448A1 (en) * | 2008-12-17 | 2011-06-02 | BP Biofuels UK Limited | Process, Plant, and Biofuel For Integrated Biofuel Production |
US20100152496A1 (en) * | 2008-12-17 | 2010-06-17 | Bp Corporation North America Inc. | Process, Plant And Butanol From Lignocellulosic Feedstock |
US20110076724A1 (en) * | 2008-12-17 | 2011-03-31 | BP Biofuels UK Limited | Process, Plant, and Biofuel for Integrated Biofuel Production |
US20100146844A1 (en) * | 2008-12-17 | 2010-06-17 | Bp Corporation North America Inc. | Process, Plant And Biofuel From Lignocellulosic Feedstock |
US20110076732A1 (en) * | 2008-12-17 | 2011-03-31 | BP Biofuels UK Limited | Process, Plant, and Butanol From Lignocellulosic Feedstock |
US20100146842A1 (en) * | 2008-12-17 | 2010-06-17 | Bp Corporation North America Inc. | Process, plant and biofuel for integrated biofuel production |
US20100269990A1 (en) * | 2009-04-23 | 2010-10-28 | Greenfield Ethanol Inc. | Separation of reactive cellulose from lignocellulosic biomass with high lignin content |
US8603295B2 (en) | 2009-04-23 | 2013-12-10 | Greenfield Specialty Alcohols Inc. | Separation of reactive cellulose from lignocellulosic biomass with high lignin content |
US9708490B2 (en) | 2009-05-28 | 2017-07-18 | Fibria Innovations Inc. | Derivatives of native lignin |
US10435562B2 (en) | 2009-05-28 | 2019-10-08 | Fibria Innovations Inc. | Derivatives of native lignin, lignin-wax compositions, their preparation, and uses thereof |
US20110046399A1 (en) * | 2009-08-07 | 2011-02-24 | Rene Johan Haan | Process for preparing a hydroxyacid or hydroxyester |
US8580978B2 (en) | 2009-08-07 | 2013-11-12 | Shell Oil Company | Process for preparing a hydroxyacid or hydroxyester |
US20110112326A1 (en) * | 2009-08-07 | 2011-05-12 | Jean-Paul Lange | Process for hydrogenation |
US20120202260A1 (en) * | 2009-09-04 | 2012-08-09 | Lignol Innovations Ltd. | Hybrid biorefining and gasification of lignocellulosic feedstocks |
US10053745B2 (en) | 2010-01-19 | 2018-08-21 | Renmatix, Inc. | Production of fermentable sugars and lignin from biomass using supercritical fluids |
US10858712B2 (en) | 2010-01-19 | 2020-12-08 | Renmatix, Inc. | Production of fermentable sugars and lignin from biomass using supercritical fluids |
US9982174B2 (en) | 2010-02-15 | 2018-05-29 | Fibria Innovations Inc. | Binder compositions comprising lignin derivatives |
US10533030B2 (en) | 2010-02-15 | 2020-01-14 | Suzano Canada Inc. | Carbon fibre compositions comprising lignin derivatives |
WO2011126369A1 (en) * | 2010-04-09 | 2011-10-13 | Stichting Dienst Landbouwkundig Onderzoek | Acetic acid based refining process of biomass |
US8889384B2 (en) | 2010-10-07 | 2014-11-18 | Shell Oil Company | Process for the production of alcohols from biomass |
US9187862B2 (en) | 2010-11-05 | 2015-11-17 | Greenfield Specialty Alcohols Inc. | Bagasse fractionation for cellulosic ethanol and chemical production |
US9932707B2 (en) | 2010-11-05 | 2018-04-03 | Greenfield Specialty Alcohols Inc. | Bagasse fractionation for cellulosic ethanol and chemical production |
US8609379B2 (en) | 2010-12-20 | 2013-12-17 | Shell Oil Company | Process for the production of alcohols from biomass |
US9840621B2 (en) | 2011-03-24 | 2017-12-12 | Fibria Innovations Inc. | Compositions comprising lignocellulosic biomass and organic solvent |
US8663800B2 (en) | 2011-05-04 | 2014-03-04 | Renmatix, Inc. | Lignin production from lignocellulosic biomass |
US8840995B2 (en) | 2011-05-04 | 2014-09-23 | Renmatix, Inc. | Lignin production from lignocellulosic biomass |
US8409357B2 (en) | 2011-05-04 | 2013-04-02 | Renmatix, Inc. | Self-cleaning apparatus and method for thick slurry pressure control |
US9255189B2 (en) | 2011-07-28 | 2016-02-09 | Greenfield Specialty Alcohols Inc. | Ethanol production with two stage continuous steam pre-treatment of lignocellulosic biomass |
WO2013070305A1 (en) * | 2011-08-31 | 2013-05-16 | Dx Resources, Llc | Method and apparatus for ethanol production |
US9446326B2 (en) | 2011-08-31 | 2016-09-20 | Dx Resources Llc | Method and apparatus for ethanol production |
EP2773725A4 (en) * | 2011-11-03 | 2015-07-08 | Solray Holdings Ltd | Method for removal of toxic waste from timber |
WO2013066196A1 (en) * | 2011-11-03 | 2013-05-10 | Lignin Polymers Limited | Method for removal of toxic waste from timber |
US9963555B2 (en) | 2011-12-30 | 2018-05-08 | Renmatix, Inc. | Compositions comprising lignin |
US8759498B2 (en) | 2011-12-30 | 2014-06-24 | Renmatix, Inc. | Compositions comprising lignin |
FR2997093A1 (en) * | 2012-10-18 | 2014-04-25 | IFP Energies Nouvelles | PROCESS FOR PRODUCING ALCOHOLS AND / OR SOLVENTS FROM BIOMASS WITH RECYCLING OF AN INTERNAL FLOW COMPRISING ALCOHOLS AND / OR SOLVENTS UPSTREAM OR WITHIN PRETREATMENT |
FR2997094A1 (en) * | 2012-10-18 | 2014-04-25 | IFP Energies Nouvelles | PROCESS FOR PRODUCING ETHANOL FROM BIOMASS WITH RECYCLING OF AN INTERNAL FLOW COMPRISING ETHANOL UPSTREAM OR WITHIN PRETREATMENT |
WO2014060673A1 (en) * | 2012-10-18 | 2014-04-24 | IFP Energies Nouvelles | Method for producing alcohols and/or solvents from a biomass, including recirculating an internal flow including alcohols and/or solvents upstream from or within the pretreatment |
WO2014060674A1 (en) * | 2012-10-18 | 2014-04-24 | IFP Energies Nouvelles | Method for producing ethanol from biomass, including recirculating an internal flow containing ethanol upstream from or within the pretreatment |
WO2014134697A1 (en) * | 2013-03-06 | 2014-09-12 | Citrotec Indústria E Comércio Ltda | Improvement to vinasse-concentration plant integrated with an ethanol distillation facility |
CN103321075A (en) * | 2013-05-22 | 2013-09-25 | 大连工业大学 | Method for recovering low-boiling-point alcohol process pulping waste liquid components |
US10793646B2 (en) | 2014-09-26 | 2020-10-06 | Renmatix, Inc. | Adhesive compositions comprising type-II cellulose |
US20210348113A1 (en) * | 2016-07-22 | 2021-11-11 | Vito Nv (Vlaamse Instelling Voor Technologisch Onderzoek Nv) | Method and system for producing products by fermentation |
CN113862318A (en) * | 2021-09-28 | 2021-12-31 | 北京化工大学 | A green and efficient refining system and method for lignocellulose |
KR20240059598A (en) | 2022-10-27 | 2024-05-07 | 류장근 | artificial intelligence based System and Method for business processing |
Similar Documents
Publication | Publication Date | Title |
---|---|---|
US20020069987A1 (en) | Integrated processing of biomass and liquid effluents | |
US11254957B2 (en) | Hydrothermal-mechanical conversion of lignocellulosic biomass to ethanol or other fermentation products | |
FI81844B (en) | FOERFARANDE FOER FRAMSTAELLNING AV KOLHYDRATMATERIAL OCH KRAFTMASSA OCH ANORDNING FOER ANVAENDNING VID FOERFARANDET. | |
US4668340A (en) | Method of countercurrent acid hydrolysis of comminuted cellulosic fibrous material | |
US9453249B2 (en) | Process for producing hemicellulose sugars and energy from biomass | |
US4174997A (en) | Method and apparatus for continuous hydrolysis of cellulosic fiber material | |
US8262854B2 (en) | Method for recovering hydrolysis products | |
CA1100266A (en) | Organosolv delignification and saccharification process for lignocellulosic plant materials | |
US3585104A (en) | Organosolv pulping and recovery process | |
US4100016A (en) | Solvent pulping process | |
US8193324B2 (en) | Continuous counter-current organosolv processing of lignocellulosic feedstocks | |
US20120305207A1 (en) | Method for vapor phase pulping with alcohol and sulfur dioxide | |
AU779714B2 (en) | Process for treating biomass fibrous material | |
US20120202253A1 (en) | Alcohol sulfite biorefinery process | |
CN111770952B (en) | Method for processing lignocellulosic biomass | |
EP3307897B1 (en) | Hydrothermal-mechanical treatment of lignocellulosic biomass for production of fermentation products | |
WO1999067409A1 (en) | Method of treating biomass material | |
US1690954A (en) | Process for the extraction of cellulose or paper pulp from fibrous vegetable matter containing the same | |
US4608121A (en) | Process for continuous digestion of finely-divided material with heat capacity flows of substantially the same magnitude | |
NO863018L (en) | PROCEDURE FOR DRAINAGE OF LIGNOCELLULOSE. | |
AU2003212395A1 (en) | Process for producing furfural, formic acid and acetic acid from spent pulp-cooking liquor | |
US2429143A (en) | Manufacture of ethyl alcohol from sulphite residual liquor | |
BR112012007929A2 (en) | method for the production of alcohol and other power boiler woody biomass extract bioproducts | |
US3030277A (en) | Method of making acetic anhydride from lignified cellulose | |
US7282115B2 (en) | Method for mitigating the interference caused by high-molecular weight-by-products in pulping processes |
Legal Events
Date | Code | Title | Description |
---|---|---|---|
STCB | Information on status: application discontinuation |
Free format text: ABANDONED -- FAILURE TO RESPOND TO AN OFFICE ACTION |