US20080229657A1 - System and methods for continuous biomass processing - Google Patents

System and methods for continuous biomass processing Download PDF

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US20080229657A1
US20080229657A1 US12/050,896 US5089608A US2008229657A1 US 20080229657 A1 US20080229657 A1 US 20080229657A1 US 5089608 A US5089608 A US 5089608A US 2008229657 A1 US2008229657 A1 US 2008229657A1
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biomass
swelling agent
steam
swelling
contacted
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David Senyk
Tonya Tiedje
Darold F. McCalla
Farzaneh Teymouri
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Michigan Biotechnology Institute
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    • 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
    • C12P7/08—Ethanol, i.e. non-beverage produced as by-product or from waste or cellulosic material substrate
    • C12P7/10—Ethanol, i.e. non-beverage produced as by-product or from waste or cellulosic material substrate substrate containing cellulosic material
    • C—CHEMISTRY; METALLURGY
    • C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
    • C08H—DERIVATIVES OF NATURAL MACROMOLECULAR COMPOUNDS
    • C08H8/00—Macromolecular compounds derived from lignocellulosic materials
    • 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
    • C12P19/00—Preparation of compounds containing saccharide radicals
    • C12P19/14—Preparation of compounds containing saccharide radicals produced by the action of a carbohydrase (EC 3.2.x), e.g. by alpha-amylase, e.g. by cellulase, hemicellulase
    • 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

Definitions

  • This invention relates to biomass processing.
  • this invention is to a process for treating or swelling cellulosic biomass using a swelling agent to swell at least a portion of the biomass.
  • Utilization of cellulose in fermentation has traditionally been hindered by its relatively un-reactive nature.
  • the crystalline structure of cellulose and the physical protection provided by hemicellulose and lignin prevent efficient hydrolysis of these materials.
  • pretreating the biomass to make the cellulose fraction more accessible to a cellulase enzyme has been applied.
  • These processes developed to increase the chemical and biological reactivity of cellulose, can be physical treatments (such as milling) or chemical treatments (such as use of cellulose swelling and dissolving agents). See generally, U.S. Pat. No. 4,600,590 to Dale, U.S. Pat. No. 5,171,592 to Holtzapple et al., and WO 2006/055362.
  • ammonia fiber expansion (AFEX) process has been recognized as one of the most effective processes among the biomass pretreatment; (Mosier, N., Wyman, C., Dale, B., Elander, R., Lee, Y. Y., Holtzapple, M., Ladish, M. (2005), Bioresource Technology. 96, pp. 673-686.).
  • the AFEX process treats biomass with ammonia at moderate temperature under pressure followed by explosive pressure release to rupture the biomass and enhance the conversion of structural carbohydrate (cellulose and hemicellulose) to fermentable sugar.
  • the AFEX treatment effectuates a physico/chemical alteration in the biomass micro and macro structure.
  • AFEX increase the digestibility of the biomass by de-crystallization of cellulose (Laureano-Perez, L., Teymouri, F., Alizadeh, H., Dale, B. (2005), Applied Biochemistry and Biotechnology. 121-124, pp 1081-1099; Gollapalli, L., Dale, B., Rivers, D. (2002), Applied Biochemistry and Biotechnology.
  • AFEX process for treatment of several different lignocellulosic biomasses such as corn stover (Teymouri, F., Laureano-Perez, L., Alizadeh, H., Dale, B. (2004), Applied Biochemistry and Biotechnology. 113-116, pp., 951-963), switchgrass (Alizadeh, H., Teymouri, F., Gilbert, Th., Dale, B. (2005) Applied Biochemistry and Biotechnology. 121-124, pp., 1133-1142), corn fiber (Hanchar, R., Teymouri, F., Nielson, Ch., McCalla, D., Stowers, M.
  • corn stover Teymouri, F., Laureano-Perez, L., Alizadeh, H., Dale, B. (2004), Applied Biochemistry and Biotechnology. 113-116, pp., 951-963
  • switchgrass Alizadeh, H., Tey
  • distiller's dried grains with solubles (DDGS) (Bals, B., Dale, B., Balan, V., (2006) Energy & Fuels, 20, pp., 2,732-2,736), and bagasse have been evaluated and shown that this pretreatment helps increase enzymatic digestibility several fold over the untreated biomass.
  • the major AFEX operating parameter variations include: temperature (70-110° C.), moisture content (20-80 wt %), ammonia loading (0.5-2.5 g ammonia per gram of dry biomass), residence time (5-30 min). The most effective conditions are chosen based on the highest glucose and xylose yield from enzymatic hydrolysis of the treated biomass.
  • the present invention provides a biomass pretreatment system and fermentation processes incorporating a biomass or cellulose treatment system in a simple and scalable design.
  • the invention may be practiced using a plug flow reactor capable of accomplishing several of the desired functions simultaneously while meeting desired or predetermined process conditions.
  • An advantage of the present invention is the ability to continuously provide required residence time and expansion.
  • residence time is provided by continuous flow of the ammonia/moistened biomass.
  • the process incorporates a retention coil or auger and ammonia expansion occurs across a pressure reduction device (valve, orifice, or other mechanical devices).
  • a process for swelling biomass includes contacting the biomass with a swelling agent as the biomass and swelling agent are transported through a reactor system.
  • the reactor system is at a pressure sufficient to maintain the swelling agent predominantly in the liquid phase, and the contact is for a time sufficient to allow the swelling agent to swell at least a portion of the biomass.
  • a fermentation process includes a pretreatment system in which biomass is contacted with a swelling agent as the biomass and swelling agent are transported through a reactor system.
  • the reactor system is at a pressure sufficient to maintain the swelling agent predominantly in the liquid phase, and the contact is for a time sufficient to allow the swelling agent to swell at least a portion of the biomass. At least a portion of the biomass that has been contacted with the swelling agent is then fermented.
  • steam is applied to the biomass to achieve a total moisture content of from 20 wt % to 90 wt % as the steam mixes with the biomass.
  • steam is applied to the biomass to achieve a temperature of from 60° C. to 200° C. as the swelling agent mixes with the biomass.
  • the steam is applied to the biomass prior to contacting with the swelling agent.
  • the steam is applied to the biomass after contacting with the swelling agent.
  • the steam is applied to the biomass during contacting with the swelling agent, which means that at or near concurrent application of steam and swelling agent with biomass can also be utilized.
  • the biomass is contacted with the swelling agent at a ratio of swelling agent to biomass of from 0.1:1 to 2.5:1 dry weight basis (dwb).
  • the steam can be applied by way of a mixing device to mix the steam with the biomass or by way of a transport device to transport the biomass.
  • the steam is applied by way of a mixing and transport device to mix and transport the biomass.
  • the biomass is contacted with the swelling agent for at least one minute to swell the biomass.
  • the swelled biomass is dried to provide a vapor stream and a dried biomass stream such that the vapor stream contains at least a portion of the swelling agent and moisture from the biomass.
  • FIG. 1 is a schematic diagram depicting a system for continuous biomass processing in accordance with an embodiment of the present invention
  • FIG. 2 is a schematic diagram depicting an overall system for continuous biomass processing in accordance with an embodiment of the present invention
  • FIGS. 3-9 are schematic diagrams depicting alternate embodiments of a system for continuous biomass processing in accordance with an embodiment of the present invention.
  • FIG. 10 is a schematic diagram depicting components that could be used for a system for continuous biomass processing in accordance with an embodiment of the present invention using a heating heat exchanger to heat ammonia to, at or near reaction temperature;
  • FIGS. 11-13 are schematic diagrams depicting components and system variations that could be used for a system for continuous or semi-continuous biomass processing in accordance with an embodiment of the present invention.
  • the present invention relates to the use of a process for treatment of cellulosic biomass using a swelling agent to swell the biomass.
  • the swelling of the biomass increases the chemical and biological reactivity of biomass for subsequent processing.
  • the invention incorporates the use of the pretreatment system in fermentation processes.
  • the present invention is capable of providing a variety of functions desired for treatment of biomass with swelling agent. These functions include: 1) pressurizing the biomass and swelling agent, 2) mixing and generating a homogeneous mixture of swelling agent and biomass, 3) heating the biomass and swelling agent, 4) providing adequate residence time, 5) releasing the pressure quickly.
  • One embodiment of the present invention is providing for a reactor system that uses a plug flow reactor while meeting desired process conditions.
  • an ammonia addition system works by running pressurized ammonia, from a pressurized ammonia tank 100 , through a cooling heat exchanger 102 , then through a metering pump 104 , followed by a flow meter 106 , then through a heating heat exchanger 108 to add in heat, then proceeding into a reactor 110 .
  • the cooling heat exchanger is configured to cool the ammonia below a vaporization point, therefore keeping it predominantly in liquid form through the metering pump. This allows for accurate measurement of the ammonia.
  • the heat exchanger is configured to heat the measured ammonia flowing through the system to at or near reaction temperature prior to flowing through the reactor.
  • FIGS. 11-13 Other components and process schematics are shown at FIGS. 11-13 .
  • FIG. 11 a continuous or semi-continuous reactor is illustrated.
  • FIG. 12 illustrates another variation of a schematic for a process that uses a heat exchanger to bring ammonia to at or near reaction temperature. It is noted that the given components in line in this process may also involve various other combinations including heating exchangers and/or including steam to increase the biomass to reaction temperature. All possible heating heat exchange combinations are contemplated to fall within the design and scope of the present invention.
  • the pressurization and transport of the biomass utilizes a positive displacement pump.
  • Possible mixing devices can include mechanically powered inline mixers, annular jet pumps, externally and internally modulated steam injection heaters. Annular jet pumps and steam injection heaters may also serve multiple functions in the continuous reactor. For example, these devices can act as one or more of a heating device, a transport device and a mixing device. Residence time is preferably provided by a retention pipe or auger.
  • biomass is contacted with a swelling agent, and this mix of biomass and swelling agent are continuously transported through a reactor system.
  • continuous it is meant that the mix does not need to be collected in a vessel. Rather, the biomass and swelling agent are flowed at a relatively constant rate through the reaction system.
  • the reaction system can include a vessel, but the flow of the mixture is relatively uninterrupted as at least a portion of the biomass is swelled during the flow.
  • Biomass refers to living and recently dead biological material that can be used as fuel or for industrial production. Generally, biomass refers to plant matter grown for use as biofuel, but it also includes plant or animal matter that can be used for production of fibers, chemicals or heat. Biomass may also include biodegradable wastes that can be burned as fuel. It excludes organic material which has been transformed by geological processes into substances such as coal or petroleum.
  • Particularly suitable biomass includes such plant matter containing a relatively high content of cellulose.
  • biomass or plant matter include miscanthus, switchgrass, hemp, corn (e.g., stover or cob), poplar, willow, sugarcane and oil palm (palm oil).
  • Even municipal wastes such as newspaper can all be used as suitable biomass material.
  • biomass examples include stems, leaves, hulls, husks, wood, wood chips, wood pulp, and sawdust.
  • paper waste include discard photocopy paper, computer printer paper, notebook paper, notepad paper, typewriter paper, newspapers, magazines, cardboard, and paper-based packaging materials.
  • the biomass is predominantly one or more C 4 grasses.
  • C 4 grasses are classified by their pathway of carbon dioxide metabolism, which involves intermediates with 4 carbon atoms. This is described in Biology of Plants , by Raven, Evert, and Curtis, Worth Publishing Co., second edition, 1976, pages 116-117, incorporated herein by reference.
  • Particularly preferred C 4 grasses are C 4 perennial grasses. Perennial grasses do not require yearly planting and fertilization and are therefore more suitable for fermentation and ethanol production than annual grasses.
  • Particularly preferred C 4 perennial grasses include switchgrass, miscanthus, cord grass, and rye grass. These grasses are particularly fast growing.
  • Cord grass is classified as a C 4 grass even though a portion of its growth cycle uses C 3 metabolism.
  • the pressure of the reaction system i.e., the portion of the system in which there is contact of the biomass and swelling agent and swelling of at least a portion of the biomass occurs
  • the swelling agent should remain predominantly in the liquid phase while contacting the biomass, and while swelling of at least a portion of the biomass occurs.
  • the conditions of the system are such that the swelling agent will be considered to be maintained predominantly in the liquid phase.
  • the pressure condition of the reaction system will depend upon the type of swelling agent.
  • the swelling agent is ammonia
  • the pressure condition will be that at which ammonia is predominantly in the liquid phase.
  • Other examples of swelling agents include: 1) water soluble amines having the structure NRR 1 R 2 where R, R 1 and R 2 are either the same or different and are selected from the group consist of H or hydrocarbons containing 1 ⁇ 60 carbons, optionally substituted with oxygen, nitrogen, sulfur or phosphorous, or where two or more of the R groups are attached to form a cyclic group.
  • Preferred examples of swelling agents include ammonia, methyl amine, dimethylamine, N-methyl, ethylamine, tripropylamine, and morpholine; 2) water soluble ammonium ions having the structure +NRR 1 R 2 R 3 where R, R 1 , R 2 and R 3 are either the same or different and are selected from the group consisting of H or hydrocarbons containing 1 ⁇ 60 carbons, optionally substituted with oxygen, nitrogen, sulfur or phosphorous, or where two or more of the R groups are attached to form a cyclic group.
  • Preferred examples include, ammonium hydroxide, ammonium chloride, and trimethylammonium chloride; 3) hydroxides, carbonates, and bicarbonates of lithium, sodium, potassium, magnesium, and calcium, such as sodium hydroxide, magnesium carbonate, and calcium carbonate (lime); 4) water soluble mono, or poly carboxylic acids containing 1 ⁇ 20 carbons such as carbonic, acetic, trifloroacetic, succinic and citric; 5) inorganic acids such as sulfuric, sulfurous, nitric, nitrous, phosphoric, and hydrochloric, including agents that form inorganic acids when dissolved in water such as sulfur dioxide, which forms sulfurous acid when dissolved in water.
  • the reactor system is at a pressure of from 50 psig to 600 psig.
  • the reaction system is at a pressure of from 100 psig to 450 psig.
  • the contact of the biomass with the swelling agent is also for a period of time sufficient to swell at least a portion of the biomass.
  • the swelling agent contacts the biomass for at least one minute, more preferably for at least two minutes, and most preferably for at least five minutes.
  • steam is applied to the biomass.
  • the steam can be applied before, during or after the biomass is first contacted with the swelling agent.
  • the steam is preferably saturated steam.
  • the steam is applied to the biomass to maintain the appropriate moisture content as the steam mixes with the biomass.
  • the presence of moisture in the biomass allows faster and more even distribution of the swelling agent in the biomass.
  • the moisture in the biomass particularly affects hydrolysis of hemicellulose in the biomass, and thereby enhances the overall effect of the pretreatment.
  • too high of a moisture content will dilute the overall swelling agent content in the process and also pose an unnecessary burden on any recovery of the swelling agent and on any drying of the biomass that has been contacted with the swelling agent and steam.
  • steam is applied to maintain a moisture content of from 20 wt % to 90 wt % on a total weight basis as the steam mixes with the biomass. More preferably, steam is applied to maintain a moisture content of from 60 wt % to 90 wt %, and most preferably from 70 wt % to 85 wt % on a total weight basis as the steam mixes with the biomass.
  • the steam is applied to the biomass to maintain the appropriate temperature as the swelling agent mixes with the biomass. Too low of a temperature will have little if any swelling effect on the biomass. Too high of a temperature can result in undesirable chemical reactions and generate potential inhibitory compounds that adversely affect downstream processes such as hydrolysis and fermentation.
  • steam is applied to achieve a temperature of from 60° C. to 200° C. as the steam mixes with the biomass. More preferably, steam is applied to achieve a temperature of from 80° C. to 120° C., and most preferably from 90° C. to 110° C. as the stream mixes with the biomass.
  • the biomass is contacted with the swelling agent at a predetermined weight ratio of swelling agent to biomass.
  • the weight ratio should be high enough to swell at least a significant portion of the biomass within an acceptable amount of time. The weight ratio need not be too high, however. Otherwise, excessive swelling can result such that the swelling agent can cause cellulose in the biomass to plasticize, thereby reducing chemical and biological reactivity of the biomass contacted with the swelling agent on downstream processes. Downstream processes that can be particularly impacted include hydrolysis and fermentation reaction processes.
  • the biomass is contacted with the swelling agent at a ratio of swelling agent to biomass of from 0.1:1 to 2.5:1 dwb. More preferably, the biomass is contacted with the swelling agent at a ratio of swelling agent to biomass of from 0.3:1 to 1.5:1 dwb, most preferably from 0.9:1 to 1.1:1 dwb.
  • the ruptured biomass is preferably dried to provide a vapor stream and a dried biomass stream.
  • the vapor stream contains at least a portion of the swelling agent and moisture from the ruptured biomass.
  • the vapor can be condensed or recycled or both in the process.
  • the swelling agent in the vapor is recovered and reused in the recycle stream.
  • the ruptured biomass in dried or undried form, is a highly desirable feed for fermentation, as the ruptured biomass will have a significant amount of cellulose available for fermentation compared to the untreated or unruptured biomass.
  • Fermentation can be anaerobic (deficient in oxygen) as well as aerobic (oxygenated). Under aerobic conditions, microorganisms such as yeast cells can break down sugars to end products such as CO 2 and H 2 O. Under anaerobic conditions, yeast cells utilize an alternative pathway to produce CO 2 and ethanol.
  • the fermentation reaction of the present invention is preferably anaerobic, i.e., partially or completely deficient in oxygen. Fermentation can also be used to refer to the bulk growth of microorganisms on a growth medium where no distinction is made between aerobic and anaerobic metabolism.
  • the ruptured biomass is preferably contacted with one or more cellulase enzymes in an aqueous mixture.
  • the cellulase can be provided as a purified enzyme or can be provided by a cellulase-producing microorganism in the aqueous mixture.
  • Cellulase can include any enzyme that effects the hydrolysis or otherwise solubilizes cellulose (including insoluble cellulose and soluble products of cellulose). Suitable sources of cellulase include such commercial cellulase products as SpezymeTM CP, CytolaseTM M104, and MultifectTM CL (Genencor, South San Francisco, Calif.).
  • cellulase hydrolysis are typically selected in consideration of the conditions suitable for the specific cellulase source, e.g, bacterial or fungal.
  • cellulase hydrolysis can be carried out at a temperature of from 30° C. to 60° C. and a pH of from 4.0 to 8.0.
  • cellulase hydrolysis is carried out at a temperature of from 30° C. to 48° C. and a pH between of from 4.0 to 6.0.
  • the aqueous mixture of biomass and enzyme can further advantageously comprise an ethanologenic microorganism for fermentation.
  • the microorganism in one that has the ability to convert a sugar or oligosaccharide to ethanol.
  • the hydrolysis product can be separated and then fermented with the microorganism.
  • ethanologenic microorganisms examples include ethanologenic bacteria and yeast.
  • the microorganisms are ethanologenic by virtue of their ability to express one or more enzymes which, individually or together, convert a sugar to ethanol.
  • Saccharomyces such as S. cerevisiae
  • Other examples of microorganisms that convert sugars to ethanol include species of Schizosaccharomyces (such as S. pombe ), Zymomonas (including Z. mobilis ), Pichia ( P. stipitis ), Candida ( C. shehatae ) and Pachysolen ( P. tannophilus ).
  • Preferred examples of ethanologenic microorganisms include ethanologenic microorganisms expressing alcohol dehydrogenase and pyruvate decarboxylase, such as can be obtained with or from Zymomonas mobilis.
  • the ethanologenic microorganism can express xylose reductase and xylitol dehydrogenase, which convert xylose to xylulose.
  • Xylose isomerase converts xylose to xylulose, as well.
  • the ethanologenic microorganism can further express xylulokinase, which catalyzes the conversion of xylulose to xylulose-5-phosphate.
  • Additional enzymes to complete the pathway can include transaldolase and transketolase. These enzymes can be obtained or derived from microorganisms such as Escherichia coli, Klebsiella oxytoca and Erwinia species.
  • microorganisms capable of fermenting both pentoses and hexoses to ethanol are employed.
  • Particularly preferred microorganisms include Klebsiella oxytoca P2 and Escherichia coli KO11.
  • FIG. 1 illustrates a schematic diagram of a possible embodiment utilizing the objects of the present invention for a continuous biomass treatment system, and is generally shown at 10 .
  • moistened biomass 12 may be pressurized in a positive displacement pump 14 or any other means to pressurize the biomass known in the art.
  • Aqueous or anhydrous ammonia is added to moistened biomass upstream (such as at 16 ) of an annular jet pump 18 .
  • ammonia may also alternatively refer to anhydrous ammonia or other swelling agents known in the art.
  • Steam may used as a transport, heating and/or moisturizing fluid. For example, steam can be injected by way of an annular jet pump 18 to heat the ammonia and biomass suspension, generate a homogeneous suspension, and aid in transporting the mixture through a retention pipe 20 .
  • Retention pipe 20 is illustrated as curved, but may be straight in this and in all variations shown in the all the figures. It is noted that in addition to steam, other types of heat exchangers may be used to heat the ammonia to at or near reaction temperature. Once the suspension has passed through the retention pipe, the pressure is rapidly decreased such as across a pressure reduction valve 22 , orifice, or other mechanical device allowing for the vaporization of the ammonia and subsequent separation and recycle back into the process. It is also noted that in this Fig. and in all figures which use steam and ammonia, that the steam optionally may be introduced upstream of the introduction of the ammonia. Further, steam and ammonia may be introduced simultaneously.
  • FIG. 2 shows an example of incorporation of the biomass treatment process with an ethanol manufacturing facility.
  • the treated biomass following enzyme hydrolysis is particularly suitable in any application that utilizes C5, C6 or a mixed C5/C6 sugar solution.
  • FIG. 3 is another schematic of the process illustrated in FIG. 1 .
  • FIG. 4 offers a slight variation of the schematic illustrated in FIGS. 1 and 3 .
  • the annular jet pump is replaced by direct-contact steam injection for combined heating and mixing of the biomass/ammonia suspension. This could be accomplished by using spargers, mixing tees and internally modulated steam injection heaters as are known in the art. Steam may also drive the suspension as well as add pressure to the system.
  • FIGS. 5 and 6 differ from FIGS. 1 and 4 by using a retention auger 30 to replace a retention pipe.
  • the auger would be configured to provide the required residence time for the biomass under pressure prior to depressurizing across a pressure reduction valve, orifice, or other mechanical device. Such configuration and schematic could be developed using methods well known in the art.
  • FIGS. 7 and 8 show replacement of the annular jet pump or direct-contact steam injectors with an inline mixer 40 or continuous stirred tank reactor (CSTR).
  • the steam and/or ammonia could be added upstream or directly into the inline mixer or CSTR.
  • the inline mixer and CSTR could provide mixing and all or some of the required mixing time.
  • FIG. 9 is a variation of FIG. 3 in that an auger may optionally be used.
  • an ammonia addition system works by running pressurized ammonia, from a pressurized ammonia tank 100 , through a cooling heat exchanger 102 , then a metering pump 104 , followed by a flow meter 106 , then through a heating heat exchanger 108 to add in heat, then proceeding into a reactor 110 .
  • the cooling heat exchanger is configured by means known in the art to cool the ammonia below a vaporization point, therefore keeping it predominantly in liquid form through the metering pump. This allows for accurate measurement of the ammonia.
  • the heat exchanger is configured to heat the measured ammonia flowing through the system to at or near reaction temperature prior to flowing through the reactor.
  • FIGS. 11-13 Other component and process schematics are shown at FIGS. 11-13 .
  • FIG. 11 a continuous or semi-continuous reactor system is illustrated.
  • FIG. 12 illustrates another variation of a schematic for a process that uses a heat exchanger to bring the swelling agent to at or near reaction temperature. It is noted that the given components in line in this process may also involve various other combinations including heating exchangers and/or including steam to increase the biomass to reaction temperature. A wide variety of heating heat exchange combinations are contemplated to fall within the design and scope of the present invention.
  • the reactor system of this invention is energy efficient.
  • mixing energy is provided by steam through a direct steam injection nozzle.
  • the invention is relatively easy to operate and maintain. In one embodiment, there are no moving parts in the reactor. In another embodiment, the reactor has no dynamic seals that could allow ammonia leakage into the work environment.

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US20090221042A1 (en) * 2006-05-01 2009-09-03 Dale Bruce E Process for the Treatment of Lignocellulosic Biomass
US20100206499A1 (en) * 2009-02-13 2010-08-19 Zilkha Biomass Acquisitions Company L.L.C. Methods for Producing Biomass-Based Fuel With Pulp Processing Equipment
US20100275507A1 (en) * 2006-08-16 2010-11-04 Bioecon International Holding N.V. Stable suspensions of biomass comprising inorganic particulates
US8236173B2 (en) 2011-03-10 2012-08-07 Kior, Inc. Biomass pretreatment for fast pyrolysis to liquids
US8945245B2 (en) 2009-08-24 2015-02-03 The Michigan Biotechnology Institute Methods of hydrolyzing pretreated densified biomass particulates and systems related thereto
US8968515B2 (en) 2006-05-01 2015-03-03 Board Of Trustees Of Michigan State University Methods for pretreating biomass
US9039792B2 (en) 2009-08-24 2015-05-26 Board Of Trustees Of Michigan State University Methods for producing and using densified biomass products containing pretreated biomass fibers
US9102964B2 (en) 2012-04-27 2015-08-11 The Michigan Biotechnology Institute Process for treating biomass
US9175323B2 (en) 2012-04-27 2015-11-03 The Michigan Biotechnology Institute Process for treating biomass
US9206446B2 (en) 2006-05-01 2015-12-08 Board Of Trustees Of Michigan State University Extraction of solubles from plant biomass for use as microbial growth stimulant and methods related thereto
US9650657B2 (en) 2010-04-19 2017-05-16 Board Of Trustees Of Michigan State University Methods for producing extracted and digested products from pretreated lignocellulosic biomass
US9850512B2 (en) 2013-03-15 2017-12-26 The Research Foundation For The State University Of New York Hydrolysis of cellulosic fines in primary clarified sludge of paper mills and the addition of a surfactant to increase the yield
US9951363B2 (en) 2014-03-14 2018-04-24 The Research Foundation for the State University of New York College of Environmental Science and Forestry Enzymatic hydrolysis of old corrugated cardboard (OCC) fines from recycled linerboard mill waste rejects
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US9458482B2 (en) 2009-08-24 2016-10-04 The Michigan Biotechnology Institute Methods of hydrolyzing pretreated densified biomass particulates and systems related thereto
US8945245B2 (en) 2009-08-24 2015-02-03 The Michigan Biotechnology Institute Methods of hydrolyzing pretreated densified biomass particulates and systems related thereto
US9650657B2 (en) 2010-04-19 2017-05-16 Board Of Trustees Of Michigan State University Methods for producing extracted and digested products from pretreated lignocellulosic biomass
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US8425766B2 (en) 2011-03-10 2013-04-23 Kior, Inc. Biomass pretreatment for fast pyrolysis to liquids
US10202660B2 (en) 2012-03-02 2019-02-12 Board Of Trustees Of Michigan State University Methods for increasing sugar yield with size-adjusted lignocellulosic biomass particles
US9102964B2 (en) 2012-04-27 2015-08-11 The Michigan Biotechnology Institute Process for treating biomass
US9938662B2 (en) 2012-04-27 2018-04-10 The Michigan Biotechnology Institute Process for treating biomass
US9175323B2 (en) 2012-04-27 2015-11-03 The Michigan Biotechnology Institute Process for treating biomass
US9850512B2 (en) 2013-03-15 2017-12-26 The Research Foundation For The State University Of New York Hydrolysis of cellulosic fines in primary clarified sludge of paper mills and the addition of a surfactant to increase the yield
US9951363B2 (en) 2014-03-14 2018-04-24 The Research Foundation for the State University of New York College of Environmental Science and Forestry Enzymatic hydrolysis of old corrugated cardboard (OCC) fines from recycled linerboard mill waste rejects
WO2018191176A3 (fr) * 2017-04-09 2019-01-10 Locus Ip Company, Llc Production efficace de bioéthanol dans des réacteurs mobiles
US11414640B2 (en) 2017-10-31 2022-08-16 Locus Ip Company, Llc Matrix fermentation systems and methods for producing microbe-based products

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