CN102333879A - A biomass treatment process and system - Google Patents
A biomass treatment process and system Download PDFInfo
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- CN102333879A CN102333879A CN2009801527264A CN200980152726A CN102333879A CN 102333879 A CN102333879 A CN 102333879A CN 2009801527264 A CN2009801527264 A CN 2009801527264A CN 200980152726 A CN200980152726 A CN 200980152726A CN 102333879 A CN102333879 A CN 102333879A
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- 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
- Y02P20/133—Renewable energy sources, e.g. sunlight
Abstract
The present invention provides processes and systems for treating biomass and, e.g., making biofuels, such as bioethanol, from the biomass. More particularly, one process according to the present invention includes (a) inducing at least a first portion of a composition containing biomass and a working fluid to flow into a passage of a fluid processing apparatus, (b) injecting a high velocity transport fluid into the composition through a nozzle communicating with the passage of the fluid processing apparatus, whereby the transport fluid applies a shear force to the composition such that the working fluid is atomised and a vapour and droplet flow regime is formed downstream of the nozzle, (c) condensing the vapour and droplet flow regime, (d) transferring the composition to a first holding vessel, and (e); holding the composition in the first holding vessel at a first predetermined temperature for a first predetermined period of time, wherein a liquefaction enzyme is added to the composition prior to or during the process. Thereafter, the composition may be further processed to form a biofuel, such as, e.g., bioethanol.
Description
CROSS-REFERENCE TO RELATED APPLICATIONS
The application requires the U. S. application No.12/290 of submission on October 30th, 2008; 700 right of priority, this application require the rights and interests of international application No.PCT/GB2008/050210 that submitted on March 21st, 2008 and the international application No.PCT/GB2008/050319 that submitted on May 2nd, 2008 according to 35U.S.C. § 120.The content of above-mentioned whole applications is incorporated into this to quote mode as proof, and is the same as quoting in full at this.
Technical field
The application specifically provides biomass treatment method and the system that is suitable for use in the biofuel production of (for example, comprising bio-ethanol).More specifically, the invention provides and be used for the starch that is present in the biomass compsn is become alcoholic acid single method and system with cellulose conversion.
Background technology
In recent years, become biofuel extremely important Wood Adhesives from Biomass, because human consumer and production commercial city common understanding are to environment relevant with having mineral fuel now and sustainability problem.Existing bio-fuel block is derived from sugar crop and the fermentation with crop of high-content of starch, and it is called as " first generative process " hereinafter.First generative process generally includes mixes earth (ground) starch-based initial material to form the initial hydration step of suspension-s (slurry) with water.Water can carry out preheating before with raw materials mix.Extraly, can be at vessel in heating suspension-s with activation starch, add hot suspension subsequently once more and it is mixed with Ye Huamei, starch is changed into long-chain sugar.Activation stage uses steam casing or vapo(u)r blasting heating so that suspension-s is heated to desired temperatures usually.Simultaneously, with stirring mixer, suspension-s circulation loop or both combination mixing suspensions.Yet although there is recycle pump, these heating means can cause in suspension-s case or container, producing the zone of its temperature much larger than the remainder of case.In this process, if contact with these high-temperature areas at the starch of the early stage hydration of this process, it possibly be destroyed, and for example, character changes, thereby causes lower output.These are arranged also can not provide and especially effectively mix (being confirmed as above-mentioned heat collapse problem), and cause the hydration of starch relatively poor.
These first generative processes are used independently container usually, with activation and the transformation stage that is used for this process.Usually use impeller pump to realize suspension-s is transferred to the transformation stage container from activating container, this impeller pump is applied on the suspension-s high shear and the further destruction that therefore causes hydrated starch.
Transformation stage can also be used steam casing or water jacket case, or by the case that jet heater heats, the temperature of suspension-s is brought up to the proper level of the optimal performance that is suitable for Ye Huamei.Replacedly, adopt the jet-type pulp digester to heat the suspension-s that gets in the transformation stage container.Suspension-s not only can stand with activation stage in the identical heat collapse that stood, and high-temperature area also limits the glucose yield that produces in this process.The excessive heat in these zones promotes Mei Lade (Maillard) reaction, and wherein glycan molecule is owing to being destroyed with the protein interactions that is present in equally in the suspension-s.These Maillard loss with combine to have limited obtainable glucose yield from the slitter loss of transferpump.In addition, existing liquefaction processing needs the very long residence time to be used for the suspension-s of transformation stage, transforms saccharogenesis to guarantee starch as much as possible.This time and cost to production process all has negative influence.
In food applications (in people's food and animal-feed); Crop with high-content of starch has very high value; And; Because whole crop only has very that small proportion is a starch, therefore with compare from the possible candy output of Mierocrystalline cellulose and semicellulose crop, the candy output of high-content of starch crop per hectare is lower.Therefore, the method that obtains biofuel from replacement biomass sources (such as, the wood fiber biomass of mainly being made up of xylogen, semicellulose and Mierocrystalline cellulose) is very important to the manufacturer, because wood fiber biomass is the biomass of extremely enriching.For example, it comprise all trees and grass and agriculture residue (such as, wet and losing of doing poor (distiller ' s grain), zein fiber, corn cob and bagasse).
The process that obtains biofuel from wood fiber biomass hereinafter will be referred to as " second generates " process.Second generative process (for example changes into alcohol with wood fiber biomass in three phases; Ethanol): first pretreatment stage destroys the cellularstructure of biomass; The cellulosic of biomass partly is converted to short chain sugar in second hydrolysis stage, and in the 3rd fermentation stage, these sugar is changed into alcohol.
In order to increase the hydrolysate amount, pre-treatment step need be softened biomass and destroyed its cellularstructure, thereby exposes more multifilament element and hemicellulosic materials.Destructive preprocessing process is essentially chemistry or physics usually.Current Chemical Pretreatment process relies on catalyzer to realize the biomass cytoclasis of expecting.This catalyzer is generally acid or enzyme.The shortcoming of acid is harmful to environment, and enzyme is relatively costly.Prevailing physics preprocessing process is vapo(u)r blasting (steam explosion); The United States Patent(USP) No. 4 that United States Patent(USP) No. of submitting on January 10th, 1984 at Neves 4,425,433 and Foody submitted on July 24th, 1984; Disclosed this instance in 461,648.In vapo(u)r blasting, before reaction stops owing to the barometric point that reduces pressure suddenly, utilize HP steam heating biomass some minutes.The shortcoming of vapo(u)r blasting is to handle and must be limited in the suitable processing vessel, and is discontinuous processing therefore.In addition, the candy output of vapo(u)r blasting is low relatively, and it is very high to be used for the expense of this processing at present.
In first and second generative processes in the two, with yeast fermentation sugar.But yeast is thermally sensitive, and before the yeast fermentable sugars, biomass must be cooled to about 30 ℃.The cooling biomass have not only increased the time of fermenting process, and, if must heat once more in downstream to be used for distillation, then also increased energy expenditure through the biomass of fermentation.
The first above-mentioned generative process is a kind of process of the most generally using in the present biofuel industry.In order to reduce the cost of truck crop to handle, biofuel treatment plant is usually located in the zone near plant growth, perhaps is positioned in the zone of local market of the two kinds of products (for example, ethanol and animal-feed) that have to this process.In order to make great efforts to continue further to reduce cost, between harvest time, starch-based part (for example, corn grain) of crop and the remainder (for example, stem and leaf) of crop are separated, so that only starch-based partly is transported to treatment plant.But although between harvest time, carry out this separation, the crop that betransported with about 10% weight of being used to handle is to be made up of ligno-cellulosic materials (for example, corn husk, corn ear), does not wherein have starch.Therefore, even this crop of 10% is transported to treatment plant, this output of 10% is also ignored in first generative process.
The solution of this problem also can utilize second generative process from the ligno-cellulosic materials that exists, to obtain alcohol.Yet, first and second generative processes are carried out in single treatment plant each other side by side, can remarkably influenced be arranged to processing cost.At first, making up the related cost of setting up of treatment plant with the independent processing line that is used for first and second generative processes will be much larger than the cost that is used to make up the treatment plant that only has the first generation processing line.The second, the production cost during side by side each operation of two processing also will generate the relevant cost of handling line greater than only moving first in stage each other.
Therefore, an object of the present invention is to overcome one or more in the aforesaid drawbacks.
Summary of the invention
According to a first aspect of the invention, a kind of method that is used for biomass processes is provided, has comprised:
(i) guiding comprise biomass and working fluid compsn so that the passage of its incoming fluid treatment facility;
(ii) the high-speed transfer fluid is expelled in the compsn through the nozzle that is connected with the passage of fluid treating plant; Wherein transmitting fluid applies shearing force to compsn, so that working fluid atomizes and form water vapour and drop flow pattern (flow regime) in the downstream of nozzle;
(iii) with water vapour and the condensation of drop flow pattern and compsn is transferred to first preserves container; And
(iv) under first preset temperature, compsn is remained on first and preserve one first predetermined amount of time in the container;
(v) wherein, said method also comprises the step that glycase and cellulase is added into said compsn.
Glycase can think to be suitable for starch is transformed any enzyme of saccharogenesis.Cellulase can think to be suitable for any enzyme with Mierocrystalline cellulose or semicellulose conversion saccharogenesis.
Through nozzle the step that the high-speed transfer fluid injects compsn can be comprised the area of low pressure that is created on the formation of nozzle downstream.
Condensing steps can be begun by the transmitting fluid in downstream, the said area of low pressure of condensation.
Compsn is transferred to the step of preserving container can be comprised and make compsn be increased to first preset temperature through a thermostat unit with the temperature with compsn.
First preset temperature can be between 80 and 85 degrees centigrade.First preset temperature can be 83 degrees centigrade.
Replacedly, first preset temperature can be between 72 and 80 degrees centigrade, preferably between 76 and 78 degrees centigrade, and for example 75 degrees centigrade, or 77 degrees centigrade.
Can before the passage of compsn being introduced fluid treating plant, Ye Huamei (for example starch agent and/or cellulase) be added into said composition.
Said method can also comprise:
(i) after very first time section finishes, compsn is transferred to second preserves container; And
(ii) under second preset temperature, compsn is remained on second and preserve one second predetermined amount of time in the container; Wherein, Can Ye Huamei (for example glycase) be added into compsn before the passage of compsn being introduced fluid treating plant, and can finish and second time period was added into compsn with another Ye Huamei (for example cellulase) between beginning in very first time section.
Before compsn being transferred to the second preservation container, said method may further include the step with composition cools to the second preset temperature.
First preset temperature can be between 80 and 85 degrees centigrade.Preferably, first preset temperature can be 83 degrees centigrade.
Second preset temperature can be between 50 and 60 degrees centigrade.Preferably, second preset temperature can be 55 degrees centigrade.
Before compsn being transferred to the second preservation container, said method may further include:
(i) compsn is introduced in the passage of second fluid treating plant; And
The nozzle that (ii) is connected through the passage with second fluid treating plant injects compsn with the high-speed transfer fluid; Wherein, Said transmitting fluid applies shearing force to compsn; So that working fluid atomizing continued for one second time and form one second water vapour and stream of liquid droplets flow pattern in the downstream of nozzle; Wherein, before the passage of compsn being introduced the first fluid treatment facility, cellulase is added into compsn, and before the passage of compsn being introduced second fluid treating plant, Ye Huamei (for example glycase) is added into compsn.
First preset temperature can be between 50 and 60 degrees centigrade.Preferably, first preset temperature can be 55 degrees centigrade.
Second preset temperature can be between 80 and 85 degrees centigrade.Preferably, second preset temperature can be 83 degrees centigrade.
Said method may further include following steps:
(i) with the extremely predetermined leavening temperature of composition cools;
(ii) one or more starters are added into compsn; Compsn is transferred to fermenting container; And
(iii) under predetermined leavening temperature, compsn is remained on a predetermined fermentation time in the fermenting container.
Said cooling step can comprise makes compsn pass through cooling vessel.Cooling vessel can be converted mash water cooler (mash cooler).
Leavening temperature can be between 30 and 40 degrees centigrade.Preferably, leavening temperature can be 35 degrees centigrade.
In the present invention, can one or more starters be added into compsn.As used herein, " starter " comprises the known medicament that is used to promote fermenting process, and includes, but is not limited to glucoamylase and yeast.
Said method may further include the compsn of distillation warp fermentation from the residue of compsn, to propose the step of alcohol.
Said method can further include following steps:
(i) water that reclaims or condensing agent are returned to the compsn in the passage that flows into the first fluid treatment facility.
Said method can further include following steps:
(i) residue with compsn is transferred to a separator; And
(ii) solid is isolated from the residue of compsn.
Said method can further include following steps:
(i) reclaim moisture from separator; And
(ii) said moisture is returned to the compsn of the passage that flows into the first fluid treatment facility.
Said method can further include following steps:
(i) part of pilot set compound is so that it flows into the passage of second fluid treating plant;
The nozzle that (ii) is connected through the passage with second fluid treating plant injects compsn with the high-speed transfer fluid, and wherein, transmitting fluid applies shearing force to compsn, so that working fluid atomizing and form second water vapour and stream of liquid droplets flow pattern in the downstream of nozzle;
(iii) condensation second water vapour and stream of liquid droplets flow pattern and compsn is transferred to second preserves container; And
(iv) under second preset temperature, compsn is remained on second and preserve one second predetermined amount of time in the container;
(v) wherein, first fluid treatment facility and first is preserved container, and second fluid treating plant and second is preserved the container concurrent working; And
(vi) wherein, before the passage of compsn being introduced the first fluid treatment facility, glycase is added into compsn, and before cellulase is added into this part of compsn at the passage of the part of compsn being introduced second fluid treating plant.
Said method may further include following steps:
(i) the every part with compsn is cooled to predetermined leavening temperature;
(ii) one or more starters are added into compsn;
(iii) these parts with compsn are transferred to a fermenting container; And
(iv) under said predetermined leavening temperature, remain on compsn in the fermenting container and continue one and be scheduled to fermentation time.
Leavening temperature can be between 30 and 40 degrees centigrade.Preferably, leavening temperature can be 35 degrees centigrade.
In this embodiment, can one or more starters be added into compsn.Preferably, add two kinds of starters, wherein, these starters are glucoamylase and yeast.
The fermentation of first and second parts of compsn can be carried out in the single fermentation container.Replacedly, the fermentation of these parts of compsn can be carried out in isolating fermenting container.
Said method may further include the compsn of distillation warp fermentation from the residue of compsn, to propose the step of alcohol.
Said method may further include following steps:
(i) residue with compsn is transferred to separator; And
(ii) from the residue of compsn, isolate solid.
Said method may further include following steps:
(i) reclaim solids component from said separator; And
(ii) said solid is returned to the second section of the compsn in the passage of second fluid treating plant.
The second section of compsn can be the solids component that from separator, reclaims.
Transmitting fluid can be a steam.
Working fluid can be a water.
Biomass can comprise one or more starch-based crops.
According to a second aspect of the invention, a kind of system that is used to handle the compsn that comprises biomass and working fluid is provided, said system comprises:
(i) at least one fluid treating plant, said equipment has: the passage that is used to take in the compsn supply; And the transmitting fluid nozzle, have the jet exit that leads to said passage and have the throat of cross-sectional area less than the cross-sectional area of said outlet;
(ii) first preserve container, be communicated with the outlet fluid of said passage; And
(iii) fermenting container is communicated with the first preservation fluid container.
Said system may further include and is positioned at first preservation container and fermenting container intermediary first cooling vessel.
Said system may further include at first cooling vessel and fermenting container intermediary second and preserves the container and second cooling vessel.
Said fluid treating plant can comprise the one or more additive ports that are used for additive is introduced into compsn.The additive port can lead to the passage at the jet exit upper reaches.Replacedly, or extraly, the additive port can lead to the and then passage in jet exit downstream.Said system may further include other additive ports of the contiguous second preservation container.
Said system may further include second fluid treating plant and preserves second of container downstream first and preserve container, and second fluid treating plant has and is used to admit the second passage of preserving the compsn of container from first; And the second transmitting fluid nozzle, this nozzle has the jet exit that leads to second passage and has the throat of cross-sectional area less than the cross-sectional area of said outlet.
In another embodiment, said system comprises by what first fluid treatment facility and first preserved that container constitutes and first handles line, and said system comprises that further second handles line, and said second handles line comprises:
(i) second fluid treating plant, this second fluid treating plant have the second passage that is used to take in the compsn supply; And the second transmitting fluid nozzle, this nozzle has the jet exit that leads to second passage and has the throat of cross-sectional area less than the cross-sectional area of said outlet; And
(ii) second preserve container, it is communicated with the outlet fluid of second passage;
(iii) wherein, first and second handle lines parallel connection between compsn supply and fermenting container.
Said system may further include the mixing vessel that is communicated with the inlet fluid of the passage of said fluid treating plant, and the supply of said mixing vessel mixing biomass and working fluid is to form compsn.
Said system may further include the pump at said fluid treating plant or each fluid treating plant upper reaches.
Said system can comprise a plurality of fluid treating plants, thereby said a plurality of fluid treating plant is one another in series and/or parallel the connection forms an array.
Said system can comprise a plurality of second fluid treating plants, and said a plurality of second fluid treating plants are one another in series and/or parallel the connection to form an array.
Said system may further include thermostat unit, and it is used to improve the temperature of the compsn between first and/or second fluid treating plant and its first and/or second preservation container separately.
Said system may further include the distillation plant in the fermenting container downstream.Said system may further include the distillation plant in the inlet downstream of mixing vessel.Said system may further include first reflux line that distillation plant is connected to the inlet of fluid treating plant.
Said system may further include the separating device in the distillation plant downstream.Said system may further include the separating device in the inlet downstream of mixing vessel.Said system may further include second reflux line that separator is connected to the inlet of fluid treating plant.
Said separating device can comprise whizzer.
Said system may further include the transmitting fluid feeding unit that is communicated with said transmitting fluid nozzle or each transmitting fluid fluid nozzle.Said transmitting fluid feeding unit can be supplied to first and second fluid treating plants with transmitting fluid.
Transmitting fluid can be a steam, and regulon can be a vapour generator.
In another embodiment, the present invention provides according to the method that discloses here or any bio-ethanol produced in the system.For example, the present invention includes the method that is used for generating from biomass bio-ethanol, said method comprises:
(a) guiding comprise biomass first part at least and the working fluid of compsn so that the passage of its incoming fluid treatment facility;
(b) through the nozzle that is connected with the passage of fluid treating plant the high-speed transfer fluid is injected compsn, wherein, transmitting fluid applies shearing force to compsn, so that working fluid atomizing and formation water vapour and stream of liquid droplets flow pattern in the nozzle downstream;
(c) said water vapour of condensation and stream of liquid droplets flow pattern;
(d) compsn is transferred to first and preserves container;
(e) under first preset temperature, compsn is remained on first and preserves one first predetermined amount of time in the container, wherein, this processings before or during Ye Huamei is added into compsn;
(f) after first predetermined amount of time finishes, compsn is transferred to second preserves container;
(g) under second preset temperature, compsn is remained on second and preserve one second predetermined amount of time in the container;
(h) with the extremely predetermined leavening temperature of composition cools;
(i) starter is added into compsn;
(j) compsn is transferred to fermenting container; And
(k) under predetermined leavening temperature, remain on compsn in the fermenting container and continue a predetermined fermentation time comprises bio-ethanol with generation fermenting compsn.
Description of drawings
To only preferred implementation of the present invention be described with reference to accompanying drawing now through instance, in the accompanying drawing:
Fig. 1 is the vertical section figure according to fluid treating plant of the present invention;
Fig. 2 is the synoptic diagram according to first embodiment of the system that is used to handle the biomass compsn of the present invention;
Fig. 3 is the synoptic diagram according to second embodiment of the system that is used to handle the biomass compsn of the present invention;
Fig. 4 is the synoptic diagram according to the 3rd embodiment of the system that is used to handle the biomass compsn of the present invention;
Fig. 5 is the synoptic diagram according to the 4th embodiment of the system that is used to handle the biomass compsn of the present invention;
Fig. 6 is the synoptic diagram according to the 5th embodiment of the system that is used to handle the biomass compsn of the present invention;
Fig. 7 is the synoptic diagram according to the 6th embodiment of the system that is used to handle the biomass compsn of the present invention;
Fig. 8 shows the graphic representation of the pressure, temperature variation of biomass when biomass are passed through the fluid treating plant shown in Fig. 1.
Embodiment
Fig. 1 is the vertical xsect that passes a fluid treatment facility (being labeled as 10 generally).This treatment facility 10 comprises housing 12, defines a longitudinally extending channels 14 in this housing.This passage has inlet 16 with outlet 18 and have the rounded section of substantially constant.In other words, the cross-sectional area of passage 12 is from entering the mouth 16 to outlet 18 substantially constant.
Tuck 20 16 axially extends to the housing 12 and defines in its outside one and be used to introduce between the pressurising of compressible transmitting fluid 22 from entering the mouth.22 have the inlet 24 that can be connected to MPTS body source (not shown in figure 1) between pressurising.Tuck 20 portion within it defines the inlet 16 and the upstream portion of passage 16.Tuck 20 has the far-end 26 away from inlet 16.The thickness of the far-end 26 of tuck 20 increases earlier and reduces again subsequently, thereby limits an inside tapered surface 28.Housing 12 has wall 30, and thickness increases this wall in the position of the conical surface 28 of contiguous tuck 20.The increase of this thickness makes the part of wall 30 have surface 32, and it has the corresponding inside tapering of tapering with the conical surface 28 of tuck 20.Between them, the conical surface 28 of tuck 20 and the conical surface 32 of wall 30 define a ring nozzle 34.This nozzle 34 have with pressurising between 22 the flow nozzle entrances 36 is communicated with, the jet exit 40 that leads to passage 14 and at nozzle entrance 36 and jet exit 40 intermediary nozzle throats 38.The cross-sectional area of nozzle throat 38 is less than the cross-sectional area of nozzle entrance 36 or jet exit 40.Passage 14 also comprises mixing region 17, and and then it be arranged in said passage in downstream of jet exit 40.
Fig. 2 shows first preferred implementation of the system that is used to handle the biomass compsn, and it has combined the fluid treating plant of type shown in Fig. 1.The biomass compsn is the compsn that comprises biomass and working fluid.In this embodiment of here describing, preferred working fluid is a water, but other fluids that are suitable for carrying out said method also can be used.The term that uses in this specification sheets " biomass " is used for describing any biomaterial that can be used as fuel or energy source.The limiting examples of the biomass of suitable type comprise forest product, untreated wood-based product, energy crops and short vegetative period coppice forest and animal excrements, from industry and the biodegradable municipal product and the high-energy crop (such as rape, sugarcane and corn) of food-processing.Yet although do not limit the biomass of particular type, the most preferred biomass that are used for system and method for the present invention are starch-based crops, such as cereal, wheat and barley.Said biomass can also be used in the system and method for the present invention with the form before pulverizing.
Be labeled as 50 treatment system generally and comprise fluid treating plant 10 and the preservation container 52 that is communicated with outlet 18 fluids of treatment facility 10.Preferably, preserving container 52 is insulating, and is surrounded by the hot water jacket (not shown), and comprises electric motor driving whisking appliance (not shown), to mix the also content of stirred vessel 52.System 50 also comprises cooling vessel 52 that is communicated with preservation container 52 fluids and the fermenting container 56 that is communicated with cooling vessel 54 fluids.Transmitting fluid supply 58 is connected between the pressurising of treatment facility 10 and enters the mouth 24, enters the mouth so that transmitting fluid is supplied between pressurising.Although not shown, this system can also be included in the pump at the fluid treating plant upper reaches, to be used for fluid is introduced the passage 14 of treatment facility 10.Similarly, can comprise thermostat unit (TCU) (not shown) in the system 50, it is between fluid treating plant 10 and preservation container 52.TCU comprises one or more fluid treating plants of type shown in Fig. 1.In TCU, have under the situation more than a treatment facility, these treatment facilities are arranged in series preferably.Thermostat unit can little by little increase any fluidic temperature that flows to preservation container 52 from fluid treating plant 10.
The system 50 that in Fig. 2, is enclosed in the dotted line can be mounted to prior biological matter processing line, perhaps, if necessary, can optional feature be added into system 50, to create complete biomass processes line.In this case, this system can also comprise mixing vessel 60, and it is positioned at treatment facility 10 upper reaches and is communicated with inlet 16 fluids of equipment 10.Preferably, mixing vessel 60 is surrounded by the hot water jacket (not shown) and has electric motor driving whisking appliance (not shown), to be used to mix the also content of stirred vessel 60.Mixing vessel 60 also comprises the first and second additive circuits 62,66, and it is connected to first and second additives supply 64,68 separately.System can also comprise the third and fourth additive circuit 70,74 that is connected to fermenting container 56, is used for starter is supplied to fermenting container from the third and fourth additive supply 72,76.Distil container 80 can be communicated with fermenting container 56 fluids.In addition, can provide to keep case (not label), it is between fermenting container 56 and separation vessel 90.Distil container 80 has outlet 84 and can also comprise reflux line 82, and this reflux line perhaps directly or via the mixing vessel shown in Fig. 2 60 (if existence) is communicated with inlet 16 fluids of treatment facility 10.At last, system 50 can also comprise the separation vessel 90 that is connected with distil container 80 fluids with being communicated with.Separation vessel 90 preferably includes whizzer and comprises second reflux line 92 and drain line 94.As the reflux line 82 of distil container 80, second reflux line 92 also or directly perhaps is communicated with inlet 16 fluids of treatment facility 10 via mixing vessel 60.Drain line 94 allows the content in the separator 90 to be excluded or to discharge.
Fig. 3 shows second embodiment of native system, and it is labeled as 150 generally.This system 150 comprises the fluid treating plant 10 of type shown in Fig. 1 and the first preservation container 52 that is communicated with outlet 18 fluids of treatment facility 10.System 150 also comprises and preserves cooling vessel 54 that container 52 fluids are communicated with first and at the fermenting container 56 in cooling vessel 54 downstream.Transmitting fluid supply 58 is connected between the pressurising of treatment facility 10 and enters the mouth 24, enters the mouth so that can transmitting fluid be supplied between pressurising.Second embodiment and the first embodiment difference be, system 150 comprises that also second preserves the container 152 and second cooling vessel 154, and the miscellaneous part between first cooling vessel 54 and fermenting container 56 of they and system 150 is connected in series.Preferably, the first and second preservation containers 52,152 all are insulating, and are all surrounded by the hot water jacket (not shown), and comprise the electric motor driving whisking appliance separately, to mix and to stir the content of said container 52,152.
In system 150, the first additive supply 164 is connected to the inlet 16 of treatment facility 10 through the first additive circuit 162, and the second additive supply 168 is connected to second through the second additive circuit 166 and preserves container 152.System 150 can also comprise the third and fourth additive circuit 70,74 that is connected to fermenting container 56, to be used for that starter is supplied to fermenting container from the third and fourth additive supply 72,76.
The system 150 that in Fig. 3, is centered around in the dotted line can be mounted in the prior biological matter processing line, perhaps, if desired, can additional parts be added into system 150, to create complete biomass processes line.In this case, this system can also comprise mixing vessel 60, and it is positioned at treatment facility 10 upper reaches and is communicated with inlet 16 fluids of equipment 10.Preferably, mixing vessel 60 is surrounded by the hot water jacket (not shown) and has electric motor driving whisking appliance (not shown), to be used to mix the also content of stirred vessel 60.Under the situation of the part of mixing vessel 60 formation systems 150, the first additive circuit 162 can be connected to the inlet of mixing vessel 60 rather than fluid treating plant 10.Distil container 80 can be connected to the outlet 160 of fermenting container 56.Distil container 80 has outlet 84 and can also comprise reflux line 82, and this reflux line perhaps directly or via the mixing vessel shown in Fig. 3 60 (if existence) is communicated with inlet 16 fluids of treatment facility.At last, system 150 can also comprise the separation vessel 90 that is connected with distil container 80 fluids with being communicated with.Separation vessel 90 preferably includes whizzer and comprises second reflux line 92 and drain line 94.As the reflux line 82 of distil container 80, second reflux line 92 also or directly perhaps is communicated with inlet 16 fluids of treatment facility via mixing vessel 60.Drain line 94 allows the content in the separator 90 to be removed or to discharge.
Fig. 4 to Fig. 7 shows other preferred implementations of system of the present invention.As first and second preferred implementations of native system; Other embodiments of these of native system can be augmented the mixing vessel shown in Fig. 2 and Fig. 3, distil container and separation vessel; But for the simple reasons, do not explain or describe the container that these are augmented with respect to these other embodiments.
Fig. 4 shows the 3rd embodiment of system of the present invention, and it is labeled as 250 generally.System 250 comprises the fluid treating plant 10 of type shown in Fig. 1 and the first preservation container 52 that is communicated with outlet 18 fluids of treatment facility 10.System 250 also comprises the cooling vessel 54 that is communicated with fermenting container 56 fluids, and the two all preserves container 52 downstream first.Transmitting fluid supply 58 is connected between the pressurising of treatment facility 10 and enters the mouth 24, enters the mouth so that can transmitting fluid be supplied between this pressurising.The difference of the embodiment of the 3rd embodiment and front is; System 250 comprises that further second fluid treating plant 210 and second preserves container 252, and they are connected in series with the miscellaneous part between the first preservation container 52 and cooling vessel 54 of system 250.Second treatment facility 210 is identical with first treatment facility 10 shown in Fig. 1 basically, and has and be connected to second transmitting fluid supply 258 that enters the mouth between its corresponding pressurising.
In system 250, the first additive supply 264 is connected to the inlet 16 of first treatment facility 10 through the first additive circuit 262, and the second additive supply 268 simultaneously is connected to the inlet of second treatment facility 210 through the second additive circuit 266.System 250 can also comprise the third and fourth additive circuit 70,74 that is connected to fermenting container 56, to be used for that starter is supplied to fermenting container from the third and fourth additive supply 72,76.Fermenting container 56 has outlet 260.
Fig. 5 shows the 4th embodiment of system of the present invention, and it is labeled as 350 generally.System 350 comprises first and second processing circuitry, and they are parallel and be connected to the shared fermenting container 56 that is positioned at downstream.First processing circuitry comprises the first fluid treatment facility 10 of type shown in Fig. 1, the first preservation container 52 that is communicated with outlet 18 fluids of first treatment facility 10 and first cooling vessel 54 that is communicated with the first preservation container, 52 fluids.The first transmitting fluid supply 58 is connected between the pressurising of first treatment facility 10 and enters the mouth 24, enters the mouth so that can transmitting fluid be supplied between pressurising.Second handles line comprises and is similarly second fluid treating plant 310 of type shown in Fig. 1, the second preservation container 352 that is communicated with the outlet fluid of second treatment facility 310 and second cooling vessel 354 that is communicated with the second preservation container, 352 fluids.System 350 can comprise and be used for transmitting fluid is supplied to second transmitting fluid supply 358 that enters the mouth between the pressurising of second treatment facility 310.
First and second cooling vessel 54,354 all are communicated with the fermenting container that is positioned at downstream 56 fluids.
In system 350, the first additive supply 364 is connected to the inlet 16 of first treatment facility 10 through the first additive circuit 362, and the second additive supply 368 simultaneously is connected to the inlet of second treatment facility 310 through the second additive circuit 366.System 350 can also comprise the third and fourth additive circuit 70,74 that is connected to fermenting container 56, to be used for that starter is supplied to fermenting container from the third and fourth additive supply 72,76.Fermenting container 56 has outlet 360, and it can link to each other with the distil container of type shown in Fig. 2 fermenting container 56 with separation vessel, with the enlarged edition system.In system 350, exist under the situation of distil container and separation vessel, system 350 can comprise the corresponding reflux line (not shown) that distil container and separation vessel are linked to each other with the inlet of second treatment facility 310.System 350 can also be included in first and second and handle the mixing vessel (not shown) at the line upper reaches, or is used for special use first and second mixing vessels of each first and second processing line.
Fig. 6 and Fig. 7 show the 5th and the 6th embodiment according to system of the present invention.Said system (being labeled as 450 and 550 generally) is similar with the system 50 shown in Fig. 2.They have separately preserves container 52, the cooling vessel 54 that is communicated with preservation container 52 fluids and the fermenting container 56 that is communicated with cooling vessel 54 fluids.The difference of the system of system 450,550 and aforementioned embodiments is the fluid treating plant aspect.Be not at preservation container 52 upper reaches single fluid treatment facility to be set, each system 450,550 all adopts the array fluid treatment facility.
In the system 450 of the 5th embodiment, array fluid treatment facility 10 is provided, wherein equipment 10 is arranged in with being one another in series and preserves container 52 upper reaches.Can the shared one single transmitting fluid supply of this array processing equipment 58 (as shown in Figure 6), perhaps each treatment facility can have its oneself dedicated transmissions fluid supply.System 450 can comprise the first and second additive circuits 462,466, and it is connected to the corresponding first and second additive supplies 464,468 inlet 16 of the first fluid treatment facility 10 in the said array.As the embodiment of front, the third and fourth additive circuit 70,74 may reside in the system 450, so that the corresponding third and fourth additive supply 72,76 is connected to fermenting container 56.
In the system 550 of the 6th embodiment, an array fluid treating plant 10 is provided, wherein first pair and the second pair of equipment 10 are arranged in abreast and preserve container 52 upper reaches.This array processing equipment can shared single transmitting fluid supply, and perhaps every pair of treatment facility can have first and second transmitting fluids supply 58,558 separately, as shown in Figure 7.Likewise, each independent means 10 can have its oneself dedicated transmissions fluid supply.System 550 can comprise the first and second additive circuits 562,566, and they are connected to the corresponding first and second additive supplies 564,568 inlet 16 of the first fluid treatment facility 10 of each centering that forms said array.As the embodiment of front, can there be the third and fourth additive circuit 70,74 in the system 450, so that the corresponding third and fourth additive supply 72,76 is connected to fermenting container 56.
To illustrate and describe work of treatment fluid and the method for compositions that comprises biomass now.
First embodiment of present method adopts the system 50 of first embodiment shown in Fig. 2.The compsn that is processed comprises the mixture and the working fluid of biomass.Aforesaid, biomass can obtain from large-scale various sources, but preferably, biomass are starch-based crop (for example, cereal).Also as described above, working fluid is water preferably.Biomass and working fluid may be combined in together to form compsn in the position away from system 50.Replacedly, if system 50 comprises mixing vessel 60, then compsn can form in mixing vessel 60.Incorporating the starch-based crop that (mass addition flow rate) flow velocity will be pulverized into controlled quality introduces in the working fluid in the mixing vessel 60.The introducing of cereal can manually or automatically be accomplished, and can introduce continuously or in batches.The mixing of crop and working fluid causes compsn to form suspension-s.With isolating mode, the glycase and the cellulase that also will be kept in the first and second additive supplies 64,68 via corresponding first and second additives supply circuit 62,66 are added into compsn.Preferably, the weight ratio of crop and liquid component is 20-40% in the suspension-s.Alternatively, also can one or more PH instrumentalities (for example, the sulfuric acid of dilution, ammoniacal liquor) and/or tensio-active agent be added into suspension-s this moment.
Used glycase α enzyme preferably in each embodiment of treatment process described herein, its activity is between 750 and 824 AGU/g.The activity of enzyme embodies with the wet crop or the feed of per unit mass.
Hot water is sent to in the water jacket of mixing vessel 60, and hot water jacket is heated to suspension-s in the container 60 thereupon and is generally 30-60 ℃ temperature, be most preferably 30-40 ℃, and suspension-s was remained under this temperature 30-120 minute.The electric motor driving stirrer stirs with soft (that is, low-shearing power) and stirs suspension-s, simultaneously suspension-s is remained in the mixing vessel 60.
With desired temperatures suspension-s is remained on a competent time period in the mixing vessel 60, prepare so that starch component is complete hydration.When suspension-s has soaked time enough in mixing vessel 60, it is discharged and introduce the passage 14 of fluid treating plant 10 via inlet 16 from container 60.Can utilize gravity that compsn is introduced fluid treating plant 10.Replacedly, if there is pump, then pump can be introduced fluid treating plant 10 with compsn under the low-shearing power condition.
With reference to figure 1, when suspension-s arrives fluid treating plant 10, suspension-s will be through entering the mouth 16 flow channels 14 and then flow out from exporting 18.Enter the mouth 24 between pressurising preferably transmitting fluid (its in this limiting examples preferably steam) is delivered to from transmitting fluid supply 58 at the pressure between the 5-7 crust.Through enter the mouth 24 and pressurising between 22 introduce transmitting fluids and make and penetrate vapo(u)r blasting stream with very high speed (being preferably supersonic speed) from jet exit 40.When steam is launched in the suspension-s, the transfer of momentum and quality takes place between steam and the suspension-s, this causes the working fluid component atomizing of suspension-s, thereby forms water vapour and drop flow pattern.In other words, the working fluid in the compsn is fractured into very little drop, and it scatters with successive water vapour state.Turbulent flow through producing in the mixing region 17 of passage 14 (being caused by the diffusion of steam when nozzle 34 comes out) is strengthened this transfer.The steam that is injected in the mixing region 17 applies shearing force to suspension-s, and its working fluid component that not only atomizes is suspended in the cellularstructure of pulverizing crop in the suspension-s but also destroy.Any starch granules that this cyto-architectural destruction will exist separates from crop, meanwhile, and with possibly how to expose the ligno-cellulosic materials that also is present in the compsn.
Can in the graphic representation of Fig. 8, see at compsn when the fluid treating plant 10, the temperature and pressure of compsn, it shows at compsn during through in the equipment 10 of Fig. 1 each, the curve of said temperature and pressure.This graphic representation has been divided into four section A to D, and its each section with equipment 10 is corresponding.Section A is corresponding to the section of passage 14 between inlet 16 and nozzle 34.Section B is corresponding to the upstream zone of between the middle portion of nozzle 34 and mixing region 17, extending of mixing region 17.Section C is corresponding to the downstream section that between the aforementioned middle portion of mixing region 17 and outlet 18, extends of mixing region 17, and section D shows when the temperature and pressure of compsn during through outlet 18 simultaneously.
The section B of the graphic representation of Fig. 8 begin the place with vapo(u)r blasting to compsn.The injection of steam (preferably with supersonic speed) with and in the diffusion when nozzle 34 leaves, and then produce the area of low pressure in the section in nozzle 34 downstream in mixing region 17.At the some place that the speed by steam and geometric condition and heat and mass transfer determines, the speed of steam will reduce and steam will begin condensation.Vapor condensation can continue and in the downstream section of mixing region 17, form condensation shockwave (condensation shock wave).The formation of condensation shockwave makes the pressure of compsn increase sharply, and is visible like the section C from Fig. 8, and liquid state is returned in compsn condensation in the section D of Fig. 8.
Like top explanation, when steam was injected in the compsn through nozzle 34, pressure possibly take place and descends in 17 upstream zone in the mixing region.This pressure descends and in this upstream zone of the adjacent nozzles outlet 40 of mixing region 17, forms partial vacuum at least.When being disclosed in injected steam, test can in zone 17, reach about 90% vacuum.
As foregoing, the shearing force and the caused concurrent turbulent flow that are applied to compsn through the steam of injecting have been destroyed the cellularstructure of pulverizing crop that is suspended in the suspension-s.During the condensation shockwave that forms through said partial vacuum and in mixing region 17 at suspension-s, the pressure change that cellularstructure is further produced is destroyed, shown in the section B and the pressure curve among the C of Fig. 8.
When the crop in the starch granules slave unit 10 was separated, because the introducing of steam, these particles were almost at once by further hydration, heating and activation.When suspension-s passed through, equipment 10 simultaneous pumpings and heating combination were to accomplish hydration and activation or to make the starch component agglutination.In other words, these particles absorb water when hot owing to exist, and the even matter that therefore starch granules can take place expands.This makes the hydrogen bonded between the intragranular starch polymer fluff, and irreversible decomposition can take place the crystalline structure of granule interior.
In addition, this equipment is mixed to glycase and cellulase in the compsn, and the even matter distribution of starch that realization is liquid and ligno-cellulosic materials and liquid therewith starch and the height of ligno-cellulosic materials contact.When compsn left equipment 10, the temperature of compsn was preferably between 74-76 ℃.
Temperature when compsn is left equipment 10 is chosen as any cause thermal damage of avoiding during starch component activation and cytoclasis compsn.Yet this temperature can be lower than the temperature of the optimum performance that is suitable for glycase and cellulase.Therefore, need can compsn without undergoing the situation of excessive temperature or additional shearing force under the temperature of rising compsn.Can use the optional thermostat unit (TCU) between equipment 10 and preservation container 52 to realize this soft heating.
Aforesaid, TCU comprises one or more fluid treating plants of type shown in Fig. 1.Control is supplied to the pressure of the steam of the equipment that constitutes TCU, so that when comparing with the pressure of the steam of the fluid treating plant that is supplied to the TCU upper reaches 10, aforementioned pressure is relatively low.The preferred steam input pressure of the equipment of TCU is between the 0.5-2.0 crust.Thus, transmitting fluid speed is very low, thereby when compsn process TCU, the steam that does not have or almost do not have shearing force or condensation to impact through injection imposes on compsn.On the contrary, TCU only uses the temperature that LP steam comes to raise lenitively compsn.
In case compsn is through TCU, then compsn preferably is in the temperature between 80-85 ℃, and is most preferably 83 ℃.Compsn flows downstream into thereupon to be preserved in the container 52.The water jacket of preserving container 52 holds hot water, and hot water remains on the aforementioned temperature place with suspension-s.If do not have TCU in the system 50, then increase to the temperature of suspension-s in the expected range and keep this temperature subsequently with hot water jacket.Remain in the preservation container 52 compsn and lasting one sufficient residence time, to allow glycase and cellulase with the starch that exists, Mierocrystalline cellulose and semicellulose conversion saccharogenesis.When the residence time finishes, compsn is transferred to fermenting container 56.Therefore, method and system of the present invention can be used for generating polysaccharide from biomass, if necessary, polysaccharide further is processed into alcohol, such as ethanol, and bio-ethanol especially.
The temperature of the compsn that is used to ferment and is most preferably 35 ℃ preferably between 30 and 40 ℃.In order to reduce the compsn temperature of preserving between container 52 and the fermenting container 56, compsn can pass through cooling vessel 54, and it is to work with the identical mode of traditional converted mash water cooler.Replacedly, if cooling vessel 54 does not exist, then can compsn be stayed in the fermenting container 56, to be cooled to preferred temperature.
Preferably, in fermenting container 56, perhaps be close to the upper reaches of fermenting container, starter is added in the compsn.Starter is included in the third and fourth additive supply 72,76 and via corresponding additive circuit 70,74 and is transferred in the compsn.Used starter can be glucoamylase and yeast.Be in the preferred temperature scope in case added starter and compsn, then in said preferred temperature scope, remain in the fermenting container compsn and the lasting enough time, change into alcohol with the sugar that allows starter to exist, such as bio-ethanol.
In case fermentation stage is accomplished, transferable compsn is to carry out follow-up distillation and to separate.Foregoing, these follow-up processing can be or can not be the parts of system and method for the present invention.In distil container 80, compsn is boiled, and any alcohol (ethanol) that is present in the compsn all volatilizes, and discharge via outlet 84.Can molecular sieve be set to remove any residual impurity in the alcohol in the downstream of outlet.Extraly, the water reclamation system (not shown) can be set, it is between distil container 80 and separator vessel 90.Known ground, the compsn residue of staying in the distil container 80 is " not filtering vinasse (whole stillage) ".Not filtering vinasse is made up of two kinds of staples: the non-starch element (also being known as " losing poor (distiller ' s grain) ") and the water (also being known as " spent wash (thin stillage) ") that pulverize crop.This is not filtered vinasse be transferred to separation vessel 90, so that can be poor separated from one another with spent wash with losing from distil container 80.Preferably, utilize whizzer to realize separating.If desired, can isolating spent wash be added back in the compsn via reflux line 92.Lose the poor animal-feed of can processing and be used as.
The method that the method that the system 150 of second embodiment shown in Figure 3 is adopted and the system 50 of first embodiment are adopted is similar.Pending compsn comprises the mixture of biomass and working fluid.Preferably, biomass are that starch-based crop (for example, cereal) and working fluid are preferably water.Biomass and working fluid may be combined in together to form compsn in the position away from system 50.Replacedly, if system 150 comprises mixing vessel 60, then compsn can form in mixing vessel 60.Incorporate the starch-based crop that flow velocity will pulverize into controlled quality and introduce the working fluid in the mixing vessel 60.The mixing of crop and working fluid causes compsn to form suspension-s.With isolating mode, the glycase that is kept in the first additive supply 164 also is added into compsn via first additive supply circuit 162.The first additive circuit 162 can directly be supplied to mixing vessel 60 (if existence) with glycase, perhaps is supplied to the inlet 16 of fluid treating plant 10.Preferably, the weight percent of crop and liquid component is 20-40% in the suspension-s.Alternatively, also can tensio-active agent and/or one or more PH instrumentalities be added into suspension-s this moment.
Hot water is sent in the water jacket of mixing vessel 60, and hot water jacket is heated to the suspension-s in the container 60 thereupon and is generally 30-60 ℃ temperature, is most preferably 30-40 ℃, and suspension-s was remained under this temperature 30-120 minute.The electric motor driving whisking appliance stirs with soft (that is, low-shearing power) and stirs suspension-s, simultaneously suspension-s is kept in the mixing vessel 60.
With preferred temperature suspension-s is kept at a sufficient time section in the mixing vessel 60, prepares so that starch component is complete hydration.When suspension-s soaks time enough in mixing vessel 60, suspension-s is discharged and via inlet 16 suspension-s introduced the passage 14 of fluid treating plant 10 from container 60.Can under action of gravity, compsn be introduced fluid treating plant 10.Replacedly, if there is pump, then pump can be introduced fluid treating plant 10 with compsn.Use low shear pump in this case.Equipment used in the method for this fluid treating plant 10 and first embodiment is identical.The mode of operation of equipment 10, the mechanism that wherein takes place and to the final effect of compsn all the method with first embodiment is the same, as described with reference to Fig. 1 and Fig. 8.Therefore, no longer be described in greater detail here.
When the crop in the starch granules slave unit 10 was separated, because the introducing of steam, particle almost can be further by hydration, heating and activation.When suspension-s passed through, equipment 10 simultaneous pumpings and heating combination were to accomplish hydration and activation or to make the starch agglutination.In addition, equipment is mixed to glycase in the compsn, provides the even matter of liquid starch material to distribute and contacts with the height of liquid starch material.When compsn left equipment 10, the temperature of compsn was preferably between 74-76 ℃.
As the method for first embodiment, can comprise the thermostat unit (TCU) of the above-mentioned type in the system 150, so that the temperature of the compsn that raises lenitively in the same manner as described above.In case through TCU, compsn preferably is in the temperature between 80-85 ℃ to compsn, and is most preferably 83 ℃.Subsequently compsn is transferred to first and preserves container 52.The water jacket of the first preservation container 52 accommodates hot water, and hot water remains on the aforementioned temperature place with suspension-s.If do not have TCU in the system 150, then increase in the expected range, and keep this temperature then with the temperature of hot water jacket with suspension-s.Compsn is kept at first preserves in the container 52 and lasting first residence time, the starch that this first residence time enough allows glycase will be present in the compsn transforms saccharogenesis.When first residence time finished, compsn is transferred to second preserves container 152.
When compsn forwards second to when preserving container 152, the temperature of compsn and is most preferably 55 ℃ preferably between 50 and 60 ℃.Preserve the compsn temperature that container 52 and second is preserved between the container 152 in order to reduce by first, compsn can pass through cooling vessel 54, and it is to work with the identical mode of traditional converted mash water cooler.Replacedly, if there is not cooling vessel 54, then compsn can be stayed in the second preservation container 152 to be cooled to preferred temperature.The hot water jacket of the second preservation container 152 remains on the temperature of compsn in the expected range.With relevant supply circuit 166 cellulase is added into the compsn in the second preservation container 152 via the second additive supply 168.Add cellulase, so that react with semicellulose with the Mierocrystalline cellulose that is present in the ligno-cellulosic materials that compsn exposes during through fluid treating plant 10.Compsn is kept at second preserves in the container 152 and lasting one second residence time, whole Mierocrystalline celluloses and semicellulose that this second residence time enough allows cellulase to exist transform saccharogenesis.When second residence time finished, compsn is transferred to fermenting container 56.
The temperature of the compsn that is used to ferment and is most preferably 35 ℃ preferably between 30 and 40 ℃.In order to reduce the compsn temperature between the second preservation container 152 and the fermenting container 56, compsn can pass through second cooling vessel 154, and it is to work with the identical mode of traditional converted mash water cooler.Replacedly, if there is not second cooling vessel 154, can compsn be stayed in the fermenting container 56 to be cooled to preferred temperature.
Preferably, in fermenting container 56 or the upper reaches that are close to fermenting container starter is added into compsn.Starter is included in the third and fourth additive supply 72,76 and is sent in the compsn via respective additive circuit 70,74.Used starter can be glucoamylase and yeast.Be in the preferred temperature scope in case added starter and compsn, then in the preferred temperature scope, be kept in the fermenting container compsn and a lasting fermentation time, the sugar that this fermentation time enough allows starter to exist changes into alcohol.
In case fermentation stage is accomplished, then transferable compsn is to carry out follow-up distillation and to separate.In distil container 80, compsn is boiled, and be present in any alcohol (such as the ethanol) volatilization in the compsn and discharge via outlet 84.Can molecular sieve be set in the outlet downstream, to remove any residual impurity in the alcohol.Extraly, the water reclamation system (not shown) can be set, it is between distil container 80 and separator vessel 90.Stay that the compsn residue is known as " not filtering vinasse " in the distil container 80.This does not filter vinasse and is made up of two kinds of staples: the non-starch element (being known as " losing poor ") and the water (being known as " spent wash ") that pulverize crop.This is not filtered vinasse be transferred to the separation vessel 90 from distil container 80, can be separated from one another so that lose poor and spent wash.Preferably, realize separating with whizzer.If desired, can isolating spent wash be added back in the compsn via reflux line 92.Lose the poor animal-feed of can processing and be used as.
The method (as shown in Figure 4) that the system 250 of the 3rd embodiment adopts is similar with the method that the system 50,150 of first and second embodiments adopts.Pending compsn is formed by the mixture and the working fluid of biomass, and prepares with the top identical mode of describing with respect to second embodiment of mode.Yet, be with cellulase but not glycase at first is added into compsn from the first additive supply 264.Can under action of gravity, compsn be introduced first fluid treatment facility 10, perhaps under the low-shearing power condition, pump can be introduced first fluid treatment facility 10 with compsn.First and second fluid treating plants 10,210 that adopt in this method all with above-mentioned first and second embodiments in used identical.The mode of operation of equipment 10,210, the mechanism that wherein takes place and to the final effect of compsn all with before with reference to Fig. 1 and Fig. 8 describe the same.Therefore, no longer be described in greater detail here.
At first come the pretreatment of fiber cellulosic material and sneak into cellulase with first treatment facility 10.First treatment facility 10 also partly separates also partly hydrated starch particle with starch granules from crop.Second treatment facility 210 is used for complete hydration and activation starch and sneak into glycase.This equipment is mixed to cellulase in the compsn, provides owing to ligno-cellulosic materials is destroyed the even matter distribution of any Mierocrystalline cellulose that exposes and semicellulose by first treatment facility 10 and contacts with its height.When compsn left first equipment 10, the temperature of compsn and was most preferably 55 ℃ preferably between 50-60 ℃.Subsequently compsn is transferred to first and preserves container 52.
The water jacket of the first preservation container 52 holds hot water, and hot water remains on aforementioned temperature with suspension-s.Compsn is kept at first preserves in the container 52 and lasting first residence time, Mierocrystalline cellulose and semicellulose that this first residence time enough allows cellulase will be present in the compsn transform saccharogenesis.When first residence time finished, compsn is transferred to second treatment facility 210, add glycase via second additive supply 268 this moment.
Aforesaid, second fluid treating plant 210 to be working with first treatment facility, 10 identical modes, and the starch component of compsn is had identical effect.In addition, this equipment is sneaked into glycase in the compsn, provides the even matter of liquid starch material to distribute and contacts with its height.When compsn left second equipment 210, the temperature of compsn was preferably between 74-76 ℃.As before, can have thermostat unit, so as compsn is transferred to second preserve container 252 before, the temperature of compsn is increased between 80 and 85 ℃ lenitively.The water jacket of the second preservation container 252 holds hot water, and hot water remains on the aforementioned temperature place with suspension-s.If do not have TCU in the system 250, then increase in the expected range, and keep this temperature subsequently with the temperature of hot water jacket with suspension-s.Compsn is remained on second preserve in the container 252 and lasting one second residence time, the starch that this second residence time enough allows glycase will be present in the compsn transforms saccharogenesis.When second residence time finished, compsn is transferred to fermenting container 56.
The same with aforementioned embodiments, the temperature of the compsn that is used to ferment and is most preferably 35 ℃ preferably between 30 and 40 ℃.In order to reduce the compsn temperature between the second preservation container 252 and the fermenting container 56, compsn can pass through cooling vessel 54, and it is to work with the identical mode of traditional converted mash water cooler.Replacedly, if there is not cooling vessel 54, then compsn can be stayed in the fermenting container 56 to be cooled to preferred temperature.This fermentation stage is identical with the fermentation stage of front embodiment.In case fermentation stage is accomplished, then can be via outlet 260 metastatic compositions to be used for follow-up distillation stage and separation phase, they also can be identical with the distillation stage and the separation phase of front embodiment.
The method of the 4th embodiment is used the system 350 shown in Fig. 5, and wherein before compsn was transferred to shared fermenting container 56, starch and cellulose components with compsn in the first and second processing lines of parallel running transformed saccharogenesis.The biomass of having described above and the types of compositions of working fluid have the glycase that is added into compsn via the first additive supply 364.The synthetic compsn is introduced first handles line and at first arrive first treatment facility 10, so, through transmitting fluid with the identical mode of having described of the various fluid treating plants said composition that atomizes.Therefore, the starch component of 10 hydrations of first fluid treatment facility and activated compositions, and glycase is mixed in the compsn in heterogeneity.
Once more; When compsn leaves first equipment 10; The temperature of compsn preferably between 74-76 ℃, and therefore, in case compsn leaves first equipment; Then or through thermostat unit or through the water-jacket typ first preservation container 52 come it is mildly heated, be in 80-85 ℃ scope of expectation up to compsn.Subsequently, compsn is kept at first preserves in the container 52 and lasting one first residence time, this first residence time enough allows glycase that the starch component of compsn is transformed saccharogenesis.Subsequently compsn is transferred to fermenting container 56 to carry out the fermentation step of top said type.Cooling vessel 56 can reduce the temperature of compsn before fermentation, perhaps can compsn be stayed cooling in the fermenting container 56.After fermentation, via exporting 360 exhaust compositions to be used for follow-up distillation and to separate.
The solid that obtains from separation phase and lose and poorly mix with the working fluid that adds and/or the liquid ingredient of between distillation or separation period, discharging subsequently is to form another batch biomass components.Cellulase is added into said composition, and it is introduced into second via second treatment facility 310 subsequently and handles line.Second treatment facility 310 is to work with the identical mode of having described of those equipment; Thus, compsn is mixed in the compsn through the cellularstructure of the solid material in the further destroying compositions of second treatment facility, 310 meetings and with the even quality of cellulase.Preferably, compsn leaves second equipment 310 under the temperature between 50 and 60 ℃, and is transferred to the second preservation container 352.Compsn is kept at second preserves in the container 352 and lasting second residence time, Mierocrystalline cellulose and semicellulose that this second residence time is enough to cellulase will be exposed in second equipment 310 transform saccharogenesis.Subsequently, metastatic composition if desired, shifts via second cooling vessel 354 so that in fermenting container 56, ferment.
The method of this embodiment can be adjusted; Make that the part of initial composition is delivered to first and second simultaneously handles line; And before the starch component of compsn and Mierocrystalline cellulose and these two portions of hemicellulose components were transferred to fermenting container 56, the first circuit converted starch composition and second circuit transformed saccharogenesis with Mierocrystalline cellulose and hemicellulose components.Therefore, the second processing line is not the residue that must after separation phase, receive compsn.
Fig. 6 with shown in Fig. 7 system adopted the 5th with the method for the 6th embodiment the method with the system of Fig. 2 and Fig. 3 used first and second embodiments is identical basically.In the 5th and the 6th embodiment; The interpolation of the formation of biomass compsn, glycase and cellulase, treated compsn are preserved stop and the transfer of compsn and follow-up fermentation in the container at one or two, and be all identical with those embodiments of front.The difference of the 5th and the 6th embodiment is that the single fluid treatment facility is replaced by an array fluid treating plant.In the 5th embodiment of Fig. 6, said array is formed by a plurality of treatment facilities that are arranged in series with each other.In the 6th embodiment of Fig. 7, said array is formed by two pairs of placed in-line treatment facilities, wherein every pair with another to parallel.The quantity and the configuration thereof that should be understood that said fluid treating plant can be used in method and system of the present invention.
The work of each equipment and the mechanism and the effect that wherein produce, all with described identical.Use the array of type shown in Fig. 6 and Fig. 7, make treatment facility maximum effect in the following areas: the intimate mixing of the destruction of the hydration of starch component and activation, ligno-cellulosic materials and exposure and enzyme and compsn.Compare with single treatment facility, use array can allow the temperature of compsn to raise more progressively through said array.This can through change be transferred in the said array each in succession the supply pressure and/or the density of the transmitting fluid of equipment realize, raise with the expectation of guaranteeing the compsn temperature and only realize later on through last equipment in the said array at compsn.
Cooling vessel, distil container and the separation vessel that possibly be included in the system of the present invention unless otherwise indicated, are conventional arrangements.Therefore, do not describe them in this manual in detail comprehensively.
The invention provides and be used for transforming the two single processing system and method for the starch that is present in the biomass compsn and Mierocrystalline cellulose.Do like this, the present invention makes the alcohol maximization that obtains from compsn, comprises inevitably the alcohol that from the Mierocrystalline cellulose that is transferred to treatment plant along with the crop of collecting together and ligno-cellulosic materials, obtains.Therefore, the present invention has compensated the cost that transmits this additional materials basically.Through converted starch and cellulose components together the two, the processing different with needs with handle line and come respectively the existing system of converted starch and cellulose components to compare, the present invention has practiced thrift cost significantly.
The present invention obtains other advantages and has had benefited from using the fluid treating plant of describing type here.Use the fluid treating plant of said type to allow the also starch component of activated compositions of the present invention's heating, avoid producing very hot zone simultaneously, starch component can be destroyed in this zone.Prevent that these zones from also reducing or eliminated because the reaction caused U.S. rad effect of the starch of protein and extraction.These reactions can stop starch to transform saccharogenesis, and therefore reduce output.In addition, soft under the low temperature mixes to return with low shear pump guarantees there is not high shear, and high shear can destroy and be kept at one of them and preserve in container or the starch component of transfer compositions between container.This destruction has been limited obtainable final glucose yield from feed.
Compare with using single agitator paddle and/or independent recirculation loop, this treatment facility guarantees that also the component of compsn mixes more up hill and dale.With in the cards comparing before, the atomizing of working fluid guarantees that also compsn mixes more equably.This improved mixing has increased and has been added so that starch and cellulose components are transformed the glycase of saccharogenesis and the usefulness of cellulase.
Conversion about ligno-cellulosic materials; In the time of in treatment facility; The shearing action and the condensation/compression shock that are applied to the biomass components of compsn have further improved performance of the present invention, because this more how this material that will be present in the biomass comes out.In fact, this allows the whole starch granuless in the feed all separated, thereby compares with conventional process, has improved the starch activation rate, because through the mechanical activation in the treatment facility enzyme activation is replenished.This also allows said method that basic 100% the starch transformation efficiency to sugar is provided especially.Therefore, method of the present invention is only required in preparation and compsn is delivered to is preserved container and carry out before the transformation stage, and compsn through treatment facility once.Thereby, owing to do not lose the cumulative time during handling, therefore improved output greatly.
Expose more starch and also meaned before compsn is transferred to fermenting process, need less glycase to realize diastatic value (the dextrose equivalent value) 12-18 that expects.In addition, condensation/compression shock is with low relatively temperature killing bacteria, thereby reduces the loss in any follow-up fermenting process.
In addition, will inject the biomass compsn with the atomizing working fluid and produce water vapour and the drop flow pattern such as the transmitting fluid of steam, with comparing that the pre existing treating processes is realized, this guarantees the cellularstructure of composition components is destroyed greatly.In addition, realize owing to destroy at least partly to inject through transmitting fluid, when comparing with existing Chemical Pretreatment process, the destruction that the present invention can obtain expected degree with the catalyzer or the additive of decrease.The destruction of in fact, realizing through the transmitting fluid injection can be eliminated the needs to this pretreatment additive fully.The transmitting fluid injection of treatment facility guarantees that successive is sheared and the turbulent flow masterpiece is used for compsn.Therefore, process of the present invention can be a successive, need not to be included in the processing in the autonomous container (such as container required in the steam explosion preprocessing process).
The high shear parts that provided by high-speed transfer fluid injection not only help to destroy the cellularstructure of biomass, and the working fluid component of atomizing compsn, with the heating of guaranteeing compsn and the tight and homogeneous of enzyme with mix.This improved heating has reduced the required time of the necessary chemical reaction realizing preserving in the container and the amount of enzyme with mixing.
Find that also method and system of the present invention can also improve the fermenting speed in the follow-up fermenting process.Improved hydration of the present invention also makes some the protein hydration in the biomass feed.These hydrated protein matter are used as the extra feed of fermented yeast, thereby have improved the zymic leavening property.
Although one or more cooling vessel are described as the part that forms system of the present invention, be appreciated that these cooling vessel are preferred components of native system, and nonessential parts.Although cooling vessel allows the temperature of compsn between preservation container and fermenting container, to reduce, this cooling can be carried out in preserving container or fermenting container self.This cooling vessel can comprise (for example) interchanger, refrigerator, toroidal swirl type water cooler, cascade cooler etc.
Treatment facility can be modified as and comprise one or more additive ports, thereby allows enzyme is added directly in the treatment facility, rather than is added in the mixing vessel.The additive port can be arranged to lead in the device channels at the jet exit upper reaches.Replacedly, or additionally, the additive port can be arranged to lead in the passage that is close to the nozzle downstream, and the mixing region of admission passage.
Used treatment facility array can replace the individual curing equipment shown in the embodiment of other explanations in the system of the 5th and the 6th embodiment.In the embodiment of existence of the present invention more than a fluid treating plant, two or more in these a plurality of treatment facilities can be shared the supply of single transport stream body.Replacedly, the whole treatment facilities that are present in the system can be shared the supply of single transport stream body.
Although the system of above-mentioned preferred implementation comprises the additive circuit of system that corresponding additive supply is connected to, these for system and method for the present invention not necessarily.Can every kind of additive manually be added in the system at the desired location place, need not special-purpose feeding mechanism and relevant supply circuit.
Described, mixing vessel is preferred components and the nonessential parts of system of the present invention.Likewise, the initial step that in mixing vessel, forms the compsn of biomass and working fluid in the treating processes neither be essential.If there is not mixing vessel, compsn can form at remote location, and is pumped into subsequently in the system of the present invention to handle.
Under the situation that used enzyme requires, the system and method for first embodiment can be modified as, and the temperature of compsn during its residence time in preserving container can be between 72 and 80 ℃, and preferably between 76 and 78 ℃.
Preferred transmitting fluid used in the method and system of the present invention is a steam.Yet, can use the transmitting fluid of replacement.For example, can use the condensable gas (such as carbonic acid gas) of the heat of replacement to substitute.
Should be understood that method of the present invention is not limited to use above-mentioned specific αDian Fenmei.Can adopt the glycase (such as βDian Fenmei or λ glycase) of replacement to substitute.Further, should also be understood that can with every type be added into compsn more than a kind of glycase and cellulase.Can also conceive other enzymes (that is, the enzyme beyond glycase, cellulase or the hemicellulase) that can act on biomass, and they fall within the scope of the invention all with the mode identical basically with acting on starch, Mierocrystalline cellulose or semicellulose.
Under the situation that does not deviate from scope of the present invention, can combine these and other modifications and improvement.
Claims (74)
1. method that is used to handle biomass comprises:
(a) guiding comprises the passage of the incoming fluid treatment facility of first part at least of the compsn of biomass and working fluid;
(b) through the nozzle that is connected with the passage of said fluid treating plant the high-speed transfer fluid is injected said mixture; Said thus transmitting fluid applies shearing force to said compsn, so that the atomizing of said working fluid and formation water vapour and drop flow pattern in said nozzle downstream;
(c) said water vapour of condensation and drop flow pattern;
(d) said compsn is transferred to first and preserves container; And
(e) preserve first predetermined amount of time in the container under first preset temperature said compsn being preserved said first, wherein, this processings before or during Ye Huamei is added into said compsn.
2. method according to claim 1 wherein, is selected said Ye Huamei: starch-sugared saccharase, Mierocrystalline cellulose or half fiber-sugared saccharase and their combination from the group that is made up of following material.
3. method according to claim 2, wherein, said starch-sugared saccharase is a glycase, and said Mierocrystalline cellulose or half fiber-sugared saccharase are cellulase or hemicellulase or the two.
4. method according to claim 1, wherein, step (b) comprises that generation is formed on the area of low pressure in said nozzle downstream.
5. method according to claim 1, wherein, said transmitting fluid is the condensable gas of from the group that is made up of steam and carbonic acid gas, selecting.
6. method according to claim 1, wherein, step (d) comprises makes said compsn be increased to said first preset temperature through thermostat unit with the temperature with said compsn.
7. method according to claim 1, wherein, said first preset temperature is between 80 ℃ and 85 ℃.
8. method according to claim 7, wherein, said first preset temperature is 83 ℃.
9. method according to claim 1, wherein, said first preset temperature is between 72 ℃ and 80 ℃.
10. method according to claim 9, wherein, said first preset temperature is between 76 ℃ and 78 ℃.
11. method according to claim 9, wherein, said first preset temperature is 75 ℃ or 77 ℃.
12. method according to claim 3 wherein, is added into said compsn with glycase and cellulase in step (a) before.
13. method according to claim 1 further comprises:
(f) after said first predetermined amount of time finishes, said compsn is transferred to second preserves container; And
(g) under second preset temperature said compsn is being preserved preservation second predetermined amount of time in the container said second.
14. method according to claim 1, wherein, (a) is added into said compsn with first Ye Huamei before in step, and finishes and said second predetermined amount of time is added into said compsn with second Ye Huamei between beginning at said first predetermined amount of time.
15. method according to claim 14, wherein, said first Ye Huamei is that glycase and said second Ye Huamei are cellulase or hemicellulase or the two.
16. method according to claim 13 further comprises, in step (f) before with said composition cools to said second preset temperature.
17. method according to claim 13, wherein, said second preset temperature is between 50 ℃ and 60 ℃.
18. method according to claim 17, wherein, said second preset temperature is 55 ℃.
19. method according to claim 13 further comprises:
(e
1) in step (f) before, at least the first compsn is introduced the passage of second fluid treating plant; And
(e
2) nozzle that is connected through the passage with said second fluid treating plant injects the second high-speed transfer fluid at least a portion of said compsn; Said thus transmitting fluid applies shearing force to said compsn; So that said working fluid atomizes and forms second water vapour and drop flow pattern in the nozzle downstream of said second fluid treating plant; Wherein, (a) is added into said compsn with first Ye Huamei before in step, and at step (e
1) before second Ye Huamei is added into said compsn.
20. method according to claim 19, wherein, said first preset temperature is between 50 ℃ and 60 ℃.
21. method according to claim 20, wherein, said first preset temperature is 55 ℃.
22. method according to claim 19, wherein, said second preset temperature is between 80 ℃ and 85 ℃.
23. method according to claim 22, wherein, said second preset temperature is 83 ℃.
24. method according to claim 19 further comprises:
(h) with the extremely predetermined leavening temperature of said composition cools;
(i) starter is added into said compsn;
(j) said compsn is transferred to fermenting container; And
(k) under said predetermined leavening temperature, said compsn is preserved predetermined fermentation time to generate fermenting compsn in said fermenting container.
25. method according to claim 24, wherein, step (h) comprises makes said compsn pass through cooling vessel.
26. method according to claim 25, wherein, said cooling vessel is the converted mash water cooler.
27. method according to claim 24, wherein, said predetermined leavening temperature is between 30 ℃ and 40 ℃.
28. method according to claim 27, wherein, said predetermined leavening temperature is 35 ℃.
29. method according to claim 24, wherein, said starter is from by selecting glucoamylase, yeast and their group that constitutes.
30. method according to claim 24 further comprises: (l) the said fermenting compsn of distillation is to extract alcohol from the residue of said compsn.
31. method according to claim 30 further comprises: (m) water of any recovery or condensation product are returned to the said compsn of the passage that flows into said first fluid treatment facility.
32. method according to claim 31 further comprises:
(n) any remaining set compound is transferred to separator; And
(o) solid is isolated from said remaining set compound.
33. method according to claim 32 further comprises:
(p) from said separator, reclaim moisture; And
(q) said moisture is returned to the said compsn in the passage that flows into said first fluid treatment facility.
34. method according to claim 3 further comprises:
(f
2) in step (e) afterwards, guide at least a portion, the second section of said compsn to flow into the passage of second fluid treating plant;
(g
2) nozzle that is connected through the passage with said second fluid treating plant injects the high-speed transfer fluid second section of said compsn; Thus; Said transmitting fluid applies shearing force to the second section of said compsn, thereby said working fluid atomizes and forms second water vapour and drop flow pattern in the nozzle downstream of said second fluid treating plant;
(h
2) said second water vapour of condensation and drop flow pattern and the second section of said compsn is transferred to second preserves container; And
(i
2) under second preset temperature second section of said compsn is being preserved preservation second predetermined amount of time in the container said second; Wherein, said first fluid treatment facility and first is preserved container and said second fluid treating plant and the second preservation container concurrent working; And; Introduce in first part before the passage of said first fluid treatment facility said compsn; Said glycase is added into the first part of said compsn, and before the passage of the second section of said compsn being introduced said second fluid treating plant, cellulase is added into the second section of said compsn.
35. method according to claim 34 further comprises:
(j
2) each part of said compsn is cooled to predetermined leavening temperature;
(k
2) starter is added into each part of said compsn;
(l
2) each part of said compsn is transferred at least one fermenting container; And
(m
2) under the said predetermined leavening temperature each part of said compsn is being preserved predetermined fermentation time to form fermenting compsn in said at least one fermenting container.
36. method according to claim 35, wherein, said leavening temperature is between 30 ℃ and 40 ℃.
37. method according to claim 36, wherein, said leavening temperature is 35 ℃.
38. method according to claim 35, wherein, said starter is from by selecting glucoamylase, yeast and their group that constitutes.
39. method according to claim 35, wherein, the first part of said compsn and the fermentation of second section are carried out in the single fermentation container.
40. method according to claim 35, wherein, the first part of said compsn and the fermentation of second section are carried out in isolating fermenting container.
41. method according to claim 35 further comprises, distills said fermenting compsn from the residue of said compsn, to extract alcohol.
42. method according to claim 35 further comprises:
(n
2) any remaining non-fermentation part of said compsn is transferred to separator; And
(o
2) solid is separated from the non-fermentation part of the residue of said compsn.
43., further may further comprise the steps according to the described method of claim 42:
(p
2) reclaim said solid from said separator; And
(q
2) said solid is returned to the passage of said second fluid treating plant.
44. according to the described method of claim 42, wherein, the second section of said compsn is the said solids component that from said separator, reclaims.
45. method according to claim 5, wherein, said transmitting fluid is a steam.
46. method according to claim 1, wherein, said working fluid is a water.
47. method according to claim 1, wherein, said biomass comprise one or more starch-based crops.
48. a system that is used to handle the compsn that comprises biomass and working fluid, said system comprises:
(a) at least one fluid treating plant, it comprises: passage has the inlet of the supply that is used to receive said compsn; And the transmitting fluid nozzle, said nozzle has and leads to the jet exit in the said passage and have the throat of cross-sectional area less than the cross-sectional area of said outlet;
(b) first preserve container, be communicated with the outlet fluid of said passage; And
(c) fermenting container is communicated with the said first preservation fluid container.
49. according to the described system of claim 48, further comprise, be positioned at said first and preserve container and said fermenting container intermediary first cooling vessel.
50., further comprise the second preservation container and second cooling vessel between said first cooling vessel and said fermenting container according to the described system of claim 49.
51. according to the described system of claim 50, wherein, said fluid treating plant comprises at least one the additive port that is used for additive is introduced said compsn.
52. according to the described system of claim 51, wherein, said at least one additive port leads in the passage at the said jet exit upper reaches.
53. according to the described system of claim 51, wherein, said at least one additive port leads in the passage that is right after said jet exit downstream.
54., comprise that further contiguous said second preserves the additive port of container according to claim 52 or 53 described systems.
55. according to the described system of claim 48; Further comprise: second fluid treating plant and preserve second of container downstream said first and preserve container; Said second fluid treating plant has and is used to receive the second passage and the second transmitting fluid nozzle of preserving the compsn of container from said first, and the said second transmitting fluid nozzle has and leads to the jet exit in the said second passage and have the throat of cross-sectional area less than the cross-sectional area of said outlet.
56. according to the described system of claim 48, further comprise: preserve the first processing line and the second processing line that container constitutes by first fluid treatment facility and first, said second handles line comprises:
(a
1) second fluid treating plant; The second passage and the second transmitting fluid nozzle with the supply that is used to receive said compsn, the said second transmitting fluid nozzle have and lead to the jet exit in the said second passage and have the throat of cross-sectional area less than the cross-sectional area of said outlet; And
(b
1) be communicated with the outlet fluid of said second passage second preserve container, wherein, said first handles line and second handles line and between the supply of said compsn and said fermenting container, walks abreast and be connected.
57. according to the described system of claim 48; Further comprise: mixing vessel with entrance and exit; Said mixing vessel is communicated with the inlet fluid of the passage of said fluid treating plant, and said mixing vessel mixes the supply of biomass and working fluid to form said compsn.
58. according to the described system of claim 48, further comprise: pump at said at least one treatment facility upper reaches.
59., further comprise: be one another in series and/or parallel the connection to form a plurality of fluid treating plants of array according to the described system of claim 48.
60., further comprise: be one another in series and/or parallel the connection to form a plurality of second fluid treating plants of array according to the described system of claim 48.
61. according to the described system of claim 50; Further comprise: thermostat unit is used to raise in said first fluid treatment facility and/or second fluid treating plant and its first preservation container separately and/or the temperature of the compsn between the second preservation container.
62. according to the described system of claim 61, wherein, said thermostat unit is a vapour generator.
63., further be included in the distillation plant in said fermenting container downstream according to the described system of claim 57.
64. according to the described system of claim 63, wherein, said distillation plant is in the inlet downstream of said mixing vessel.
65., further comprise: first reflux line that said distillation plant is connected to the inlet of said fluid treating plant according to the described system of claim 64.
66. according to the described system of claim 63, further comprise: separating device in said distillation plant downstream.
67., further comprise: separating device in the inlet downstream of said mixing vessel according to the described system of claim 64.
68., further comprise: second reflux line that said separating device is connected to the inlet of said fluid treating plant according to the described system of claim 67.
69. according to claim 66 or 67 described systems, wherein, said separating device comprises whizzer.
70., further comprise: the transmitting fluid feeding unit that is communicated with at least one fluid of said transmitting fluid nozzle according to the described system of claim 56.
71. according to the described system of claim 70, wherein, said transmitting fluid feeding unit with transmitting fluid be supplied to said first fluid treatment facility and second fluid treating plant the two.
72. according to the described system of claim 48, wherein, said transmitting fluid is a steam.
73. through the bio-ethanol of producing according to the described system of claim 48.
74. a method that is used for producing from biomass bio-ethanol comprises:
(a) guiding comprises the passage of the incoming fluid treatment facility of first part at least of the compsn of biomass and working fluid;
(b) through the nozzle that is connected with the passage of said fluid treating plant the high-speed transfer fluid is injected said compsn; Thus; Said transmitting fluid applies shearing force to said compsn, so that the atomizing of said working fluid and formation water vapour and drop flow pattern in said nozzle downstream;
(c) said water vapour of condensation and drop flow pattern;
(d) said compsn is transferred to first and preserves container;
(e) preserve first predetermined amount of time in the container under first preset temperature said compsn being preserved said first, wherein, this processings before or during Ye Huamei is added into said compsn;
(f) after said first predetermined amount of time finishes, said compsn is transferred to second preserves container;
(g) under second preset temperature said compsn is being preserved preservation second predetermined amount of time in the container said second;
(h) with the extremely predetermined leavening temperature of said composition cools;
(i) starter is added into said compsn;
(j) said compsn is transferred to fermenting container; And
(k) under said predetermined leavening temperature, said compsn is preserved predetermined fermentation time comprises bio-ethanol with generation fermenting compsn in said fermenting container.
Applications Claiming Priority (3)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| US12/290,700 US8193395B2 (en) | 2007-05-02 | 2008-10-30 | Biomass treatment process and system |
| US12/290,700 | 2008-10-30 | ||
| PCT/IB2009/007443 WO2010049815A2 (en) | 2008-10-30 | 2009-10-28 | A biomass treatment process and system |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN102333879A true CN102333879A (en) | 2012-01-25 |
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ID=42102382
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| CN2009801527264A Pending CN102333879A (en) | 2008-10-30 | 2009-10-28 | A biomass treatment process and system |
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| EP (1) | EP2340313A2 (en) |
| JP (1) | JP2012507276A (en) |
| KR (1) | KR20110079849A (en) |
| CN (1) | CN102333879A (en) |
| BR (1) | BRPI0921727A2 (en) |
| CA (1) | CA2741994A1 (en) |
| WO (1) | WO2010049815A2 (en) |
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| ES2335290T3 (en) | 2004-02-26 | 2010-03-24 | Pursuit Dynamics Plc. | METHOD AND DEVICE FOR GENERATING FOG. |
| US20080103217A1 (en) | 2006-10-31 | 2008-05-01 | Hari Babu Sunkara | Polyether ester elastomer composition |
| DE602005017748D1 (en) | 2004-02-26 | 2009-12-31 | Pursuit Dynamics Plc | IMPROVEMENTS OF A METHOD AND DEVICE FOR PRODUCING A FOG |
| US8419378B2 (en) | 2004-07-29 | 2013-04-16 | Pursuit Dynamics Plc | Jet pump |
| GB0618196D0 (en) | 2006-09-15 | 2006-10-25 | Pursuit Dynamics Plc | An improved mist generating apparatus and method |
| CA2808227A1 (en) * | 2010-08-24 | 2012-03-01 | Delaval Holding Ab | Antibacterial method for ethanol fermentation processes comprising hydrogen peroxide and peracetic acid |
| GB201119007D0 (en) * | 2011-11-03 | 2011-12-14 | Pdx Technologies Ag | An improved fluid processing pparatus and method |
| DE102012025027A1 (en) * | 2012-12-20 | 2014-06-26 | Reiflock Abwassertechnik Gmbh | Apparatus and method for the treatment of biomass |
| GB201705768D0 (en) | 2017-04-10 | 2017-05-24 | Kanu Ifeyinwa Rita | Anaerobic digester |
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| NL283530A (en) * | 1961-08-19 | |||
| US4201596A (en) * | 1979-01-12 | 1980-05-06 | American Can Company | Continuous process for cellulose saccharification |
| US4425433A (en) | 1979-10-23 | 1984-01-10 | Neves Alan M | Alcohol manufacturing process |
| US4461648A (en) | 1980-07-11 | 1984-07-24 | Patrick Foody | Method for increasing the accessibility of cellulose in lignocellulosic materials, particularly hardwoods agricultural residues and the like |
| RU2152465C1 (en) * | 1998-09-22 | 2000-07-10 | Казаков Владимир Михайлович | Cavitational unit |
| US6659635B2 (en) * | 1999-01-26 | 2003-12-09 | Kvaerner Pulping Ab | Method for introducing a first fluid into a second fluid, preferably introduction of steam into flowing cellulose pulp |
| JP5188180B2 (en) * | 2004-07-29 | 2013-04-24 | パースーツ ダイナミクス ピーエルシー | Jet pump |
| WO2008023060A1 (en) * | 2006-08-25 | 2008-02-28 | Novozymes A/S | Fermentation process |
| SI2142658T1 (en) * | 2007-05-02 | 2011-12-30 | Pursuit Dynamics Plc | Liquefaction of starch-based biomass |
| EP2060544A1 (en) * | 2007-11-16 | 2009-05-20 | APV Systems Ltd. | Method and apparatus for preparing material for microbiologic fermentation |
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2009
- 2009-10-28 KR KR1020117012141A patent/KR20110079849A/en not_active Application Discontinuation
- 2009-10-28 CA CA2741994A patent/CA2741994A1/en not_active Abandoned
- 2009-10-28 CN CN2009801527264A patent/CN102333879A/en active Pending
- 2009-10-28 JP JP2011533851A patent/JP2012507276A/en active Pending
- 2009-10-28 WO PCT/IB2009/007443 patent/WO2010049815A2/en active Application Filing
- 2009-10-28 EP EP09796432A patent/EP2340313A2/en not_active Withdrawn
- 2009-10-28 BR BRPI0921727A patent/BRPI0921727A2/en not_active IP Right Cessation
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| BRPI0921727A2 (en) | 2018-01-30 |
| CA2741994A1 (en) | 2010-05-06 |
| JP2012507276A (en) | 2012-03-29 |
| KR20110079849A (en) | 2011-07-08 |
| WO2010049815A2 (en) | 2010-05-06 |
| EP2340313A2 (en) | 2011-07-06 |
| WO2010049815A3 (en) | 2010-09-30 |
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Application publication date: 20120125 |