• 专利附录
  • 专利说明
  • 权利要求
  • 类似技术
  • 同族专利
  • 引用文献
  • 法律状态
  • 优先权
    • 专利摘要:
    processes for fermenting singas and for starting a main fermenter for fermenting singas. a process for fermenting singas is provided which is effective in decreasing an amount of time required to inoculate a main reactor. the process includes propagating a culture of acetogenic bacteria to provide an inoculum for a main reactor and fermenting singas in the main reactor.
    公开号:BR112013033711B1
    申请号:R112013033711-7
    申请日:2012-05-31
    公开日:2021-07-13
    发明作者:Peter Simpson Bell；Ching-Whan Ko
    申请人:Jupeng Bio (Hk) Limited；
    IPC主号:
    专利说明:

    [001] This Order claims the benefit of US Provisional Orders 61/571,564 and 61/571,565, both filed June 30, 2011 and 61/573,845, filed September 13 2011, all of which are incorporated in their entirety herein. by reference.
    [002] A process for fermenting synthesis gas is provided. More specifically, the process includes propagating an effective culture for use as an inoculum for a main reactor and fermenting synthesis gas in the main reactor. FUNDAMENTALS
    [003] Anaerobic microorganisms can produce ethanol from carbon monoxide (CO) through fermentation of gaseous substrates. Fermentations using anaerobic microorganisms of the genus Clostridium produce ethanol and other useful products. For example, US patent 5,173,429 describes Clostridium Ijungdahlii ATCC No. 49587, an anaerobic microorganism that produces ethanol and acetate from synthesis gas. US Patent 5,807,722 describes a method and apparatus for converting waste gases to organic acids and alcohols using Clostridium ljungdahlii ATCC No. 55380. US Patent 6,136,577 describes a method and apparatus for converting waste gases to ethanol using Clostridium ljungdahlii ATCC No. 55988 and 55989.
    [004] CO is often supplied to fermentation as part of a gaseous substrate in the form of a synthesis gas. Gasification of carbonaceous materials to produce producer gas or synthesis gas or syngas that includes carbon monoxide and hydrogen is well known in the art. Typically, such a gasification process involves a partial or air-deprived oxidation of carbonaceous material in which a substoichiometric amount of oxygen is fed to the gasification process to promote the production of carbon monoxide as described in WO 2009/154788.
    [005] Fermentation processes with acetogenic bacteria can include one or more seed reactors, one or more growth reactors and at least one main reactor. Acetogenic bacteria are normally grown to a certain cell density in a seed reactor. The seed reactor is then used to inoculate a growth fermenter. The growth fermenter will usually be a larger size than the seed reactor. Acetogenic bacteria in the growth reactor are then grown to a desired cell density. The growth reactor can then be used to inoculate another larger growth reactor or it can be used to inoculate a main reactor. The main reactor will be of a larger size than the growth reactor. In view of this process, inoculating a main reactor starting from a seed reactor requires time. Also, if a growth reactor fails, the process needs to be restarted, requiring even more time. SUMMARY
    [006] A process for fermenting singas is provided which is effective in decreasing an amount of time required to inoculate a main reactor. In this aspect, the total time from inoculation of a seed reactor to inoculation of a main reactor is shortened. The process also provides faster startups in the event of a reactor failure.
    [007] In one aspect, a process for fermenting singas is provided which includes propagating a culture of acetogenic bacteria effective to inoculate a main reactor. Propagation includes: i) inoculating a first culture of acetogenic bacteria in a pre-reactor to provide a minimum viable cell density, and ii) growing the acetogenic bacteria culture in the pre-reactor to provide a target cell density in the pre- reactor. Propagation can further be described by the following equations: (a) where, if (the pre-reactor target cell density multiplied by the pre-reactor volume) + (a main reactor volume multiplied by (a pre-reactor volume) reactor ^ a volume of the pre-reactor that is transferred)) is greater than or equal to a minimum viable cell density, transfer a volume from the pre-reactor to the main reactor in an effective amount to provide a minimum viable cell density in the reactor main, or (b) if (the pre-reactor target cell density multiplied by the pre-reactor volume) ^ (a main reactor volume multiplied by (a pre-reactor volume ^ a pre-reactor volume which is transferred)) is less than a minimum viable cell density, transfer a volume from the pre-reactor to a subsequent pre-reactor in an amount effective to provide a minimum viable cell density in the subsequent pre-reactor. Step ii is repeated until a volume from the pre-reactor is transferred to the main reactor. The fermentation of singas is then carried out in the main reactor.
    [008] In one aspect, a process for fermenting singas is provided which includes propagating a culture of acetogenic bacteria effective to inoculate a main reactor. Propagation includes: i) inoculating a first culture of acetogenic bacteria in a pre-reactor to provide a minimum viable cell density, and ii) growing the acetogenic bacteria culture in the pre-reactor to provide a target cell density in the pre- reactor. Propagation can further be described by the following equations: (a) where, if (the density of pre-reactor target cells multiplied by the pre-reactor volume) ^ (a main reactor volume multiplied by (a pre-reactor volume). reactor + a volume of the pre-reactor that is transferred)) is greater than or equal to a minimum viable cell density, transfer a volume of the pre-reactor to the main reactor in an effective amount to provide a minimum viable cell density in the reactor main, or (b) if (the pre-reactor target cell density multiplied by the pre-reactor volume) ^ (a main reactor volume multiplied by (a pre-reactor volume ^ a pre-reactor volume which is transferred)) is less than a minimum viable cell density, transfer a volume from the pre-reactor to a subsequent pre-reactor in an amount effective to provide a minimum viable cell density in the subsequent pre-reactor. The fermentation of singas is then carried out in the main reactor.
    [009] In another aspect a process is provided for starting a main fermenter for fermentation of singas. The process includes inoculating a first culture of acetogenic bacteria in a seed reactor to provide a minimum initial viable cell density in the seed reactor of at least about 0.2 grams per liter. The acetogenic bacteria culture is grown with syngas to provide a cell density in the seed reactor of at least about 5 grams per liter. A first seed reactor is inoculated with an inoculum from the seed reactor in an amount effective to provide a cell density in the growth reactor of at least about 0.2 grams per liter. The culture is grown with syngas to provide a cell density in the first growth reactor of at least about 5 grams per liter. A second growth reactor is inoculated with an inoculum from the first growth reactor in an amount effective to provide a cell density in the growth reactor of at least about 0.2 grams per liter. The culture is grown with syngas to provide a cell density in the second growth reactor of at least about 5 grams per liter. A main fermenter is inoculated with an inoculum from the second growth reactor in an amount effective to provide a cell density in the main reactor of at least about 0.2 grams per liter. BRIEF DESCRIPTION OF THE FIGURES
    [0010] The above aspects and other aspects, characteristics and advantages of various aspects of the process will be more apparent from the following figure.
    [0011] FIG. 1 illustrates a process for fermenting singas.
    [0012] Corresponding reference characters indicate corresponding components throughout the various views of the drawings. Those skilled in the art will appreciate that elements in the figures are illustrated for simplicity and clarity and are not necessarily drawn to scale. For example, the dimensions of some of the elements in the figures may be exaggerated relative to other elements to help improve understanding of various aspects of the present method and apparatus. Furthermore, common but well-understood elements that are useful or necessary in commercially viable aspects are often not represented in order to facilitate a less obstructed view of these various aspects. DETAILED DESCRIPTION
    [0013] The following description is not to be taken in a limiting sense, but is merely for the purpose of describing the general principles of exemplary modalities. The scope of the invention is to be determined with reference to the Claims.
    [0014] A series of one or more pre-reactors is provided which is effective to quickly supply an inoculum to a main reactor. The one or more pre-reactors and the main reactor are operatively connected to allow culture transfer. Each of the one or more prereactors is inoculated with a minimum viable cell density and is then grown to provide a target cell density for subsequent inoculation. A volume of about 25% to about 75% of any pre-reactor is transferred to a subsequent reactor. The remaining volume is kept and can be used for reinculation should any subsequent reactors fail. Definitions
    [0015] Unless otherwise defined, the following terms as used throughout this Descriptive Report for the present disclosure are defined as follows and may include both singular and plural forms of definitions defined below:
    [0016] The term "about" modifying any quantity refers to the variation in that quantity found under real world conditions, for example, in the laboratory, pilot plant or production facility. For example, an amount of an ingredient or a measurement employed in a mixture or quantity when modified by “about” includes the variation and degree of care typically employed in measurement under an experimental condition in a production plant or laboratory. For example, the quantity of a component of a product when modified by “about” includes the variation between batches in multiple plant or laboratory experiments and the inherent variation in the analytical method. Whether or not modified by “about”, amounts include equivalents to those amounts. Any amount stated herein and modified by "about" may also be used in this disclosure as the amount not modified by "about".
    [0017] "Carbonaceous material" as used in this document refers to material rich in carbon, such as coal and petrochemicals. However, in this Descriptive Report, carbonaceous material includes any carbon material, whether solid, liquid, gas or plasma. Among the numerous items that can be considered carbonaceous materials, this disclosure includes: carbonaceous material, carbonaceous liquid product, carbonaceous industrial liquid recycling, carbonaceous municipal solid waste (MSW or msw), carbonaceous urban waste, carbonaceous agricultural material, carbonaceous forest material , carbonaceous wood waste, carbonaceous building material, carbonaceous plant material, carbonaceous industrial waste, carbonaceous fermentation residue, carbonaceous petrochemical co-products, carbonaceous alcohol production co-products, carbonaceous coal, tires, plastic, waste plastic, kiln tar coke, soft fiber, lignin, black liquor, polymers, waste polymers, polyethylene terephthalate (PETA), polystyrene (PS), sewage sludge, anima waste, crop residues, energy crops, forest processing residues, wood processing, livestock waste, poultry waste, processing waste of food, fermentation process residues, ethanol co-products, used grain, used micro-organisms or their combinations.
    [0018] The term "soft fiber" or "soft fiber" or "fibrosoft" or "fibrousoft" means a type of carbonaceous material that is produced as a result of softening and concentrating various substances; in one example carbonaceous material is produced by steam autoclaving various substances. In another example, the soft fiber may include steam autoclaving municipal, industrial, commercial and medical waste resulting in a loose fibrous material.
    [0019] The term “municipal solid waste” or “MSW” or “msw” means waste that may include domestic, commercial, industrial and/or residual waste.
    [0020] The term "singás" or "synthesis gas" means synthesis gas which is the name given to a gas mixture that contains varying amounts of carbon monoxide and hydrogen. Examples of production methods include steam reforming of natural gas or hydrocarbons to produce hydrogen, the gasification of coal and in some types of gasification facilities from waste to energy. The name comes from their use as intermediates in the creation of synthetic natural gas (SNG) and for the production of ammonia or methanol. Singás comprises use as an intermediate in the production of synthetic petroleum for use as a fuel or lubricant via Fischer-Tropsch synthesis and previously the methanol process for Mobil gasoline. Singas consists primarily of hydrogen, carbon monoxide and some carbon dioxide, and has less than half the energy density (ie, BTU content) of natural gas. Singas is fuel and is often used as a fuel source or as an intermediate for the production of other chemicals.
    [0021] The terms "fermentation", "fermentation process" or "fermentation reaction" and the like are intended to encompass both the growth phase and the biosynthesis phase of the process. In one aspect, fermentation refers to the conversion of CO to alcohol. Pre-Reactor Project
    [0022] According to the process, a culture of acetogenic bacteria is inoculated into a pre-reactor to provide a minimum cell density. In this aspect, the prereactor can be one or more seed reactors and one or more growth reactors. The seed reactor may have a volume of about 500 liters or less, in another aspect about 400 liters or less, in another aspect about 300 liters or less, in another aspect about 200 liters or less, in another aspect about 100 liters or less and in another aspect about 50 liters or less. Growth reactors may have a volume of about 250,000 liters or less, in another respect about 150,000 liters or less, in another respect about 100,000 liters or less, in another respect about 50,000 liters or less, in another respect about 10,000 liters or less and in another aspect about 1,000 liters or less. As used herein, “volume” refers to an uncarbonated liquid working volume.
    [0023] The seed reactor can be supplied with singás including, for example, bottled singás. In this regard, the use of a seed reactor having a volume of 500 liters or less allows the seed reactor to be filled with bottled singas. The use of bottled singas can be important if a supply of singas from a gasification process is not available. Useful synga compositions are described in this document. In one aspect, pre-reactors can be filled with recycled gas from the main reactor.
    [0024] The seed reactor culture is grown to a target cell density in the pre-reactor and a volume from the seed reactor is used to inoculate a subsequent pre-reactor having a larger volume than the seed reactor. In this aspect, the second pre-reactor can be one or more growth reactors. In one important aspect, the process used at least two growth reactors, in another aspect at least three growth reactors and in another aspect at least four growth reactors.
    [0025] One aspect of a process for fermenting singas is generally illustrated in Figure 1. In this aspect, the process includes a seed reactor 100, a first growth reactor 200, a second growth reactor 300, and a main reactor 400. Each reactor can be supplied with syngas via a 500 gas supply. Nutrients may be supplied to each reactor via a 600 nutrient supply. Each reactor may include an agitator 150 and at least one impeller 250. Medium of each reactor may be sent to a 550 chiller/heat exchanger and chilled medium can be cycled back to the reactor vessel. Medium from one reactor can be transferred to the next reactor via a 700 transfer line.
    [0026] Medium from each reactor can be sent to a recycle filter 350. Concentrated cells 425 can be returned to the reactor vessel and permeate 450 can be sent for further processing. Further processing may include separation of desired product such as, for example, ethanol, acetic acid and butanol. Pre-Reactor Operation
    [0027] The operation of the pre-reactor allows a quick start for inoculation of a main reactor. In this regard, the time from inoculation of a first pre-reactor to inoculation of a main reactor is about 20 days or less, in another aspect about 15 days or less, and in another aspect about 10 days or less. The process also allows for faster recovery should any of the pre-reactors fail.
    [0028] According to the process, a culture of acetogenic bacteria is inoculated into a pre-reactor or seed reactor to provide a minimal cell density. As used herein, "minimum cell density" means a viable cell density of at least about 0.1 gram per liter, in another aspect at least about 0.2 gram per liter, in another aspect at least about 0.3 grams per liter, in another aspect at least about 0.4 grams per liter, and in another aspect at least about 0.5 grams per liter. The minimum cell density will not exceed approximately 1.2 grams per liter. In another aspect, the first culture used to inoculate a pre-reactor or seed reactor has a pH of 6.5 or less, in another aspect 4.5 or less and in another aspect about 4.0 to about 4, 5. The first culture used to inoculate a pre-reactor or seed reactor has an acetic acid concentration of about 10 grams per liter or less, in another aspect, about 1 to about 10 grams per liter, in another aspect about 1 to about 5 grams per liter, in another aspect about 1 to about 3 grams per liter, and in another aspect about 2 grams per liter.
    [0029] The acetogenic bacteria are grown in the pre-reactor until a target cell density is reached. As used herein, "pre-reactor target cell density" means a viable cell density of at least about 5 grams per liter, in another aspect at least about 10 grams per liter, in another aspect at least about 15 grams per liter and in other respect at least about 20 grams per liter. The pre-reactor target cell density will generally not exceed about 50 grams per liter. In another aspect, prereactor target cell density is about 12 to about 15 grams per liter and in another aspect about 20 to about 24 grams per liter.
    [0030] In one aspect, each subsequent pre-reactor has a larger volume than its preceding pre-reactor. According to this process, a volume ratio of the pre-reactor volume transferred to a subsequent pre-reactor, or a main reactor, is from about 0.02 to about 0.5, and in another aspect from about 0.02 to about 0.2. In another aspect, about 20 to about 75% of a volume of a pre-reactor is used to inoculate a subsequent pre-reactor, or main reactor. Other reactor volumes that can be transferred include about 30 to about 70%, about 40 to about 60%, and about 45 to about 55%. In this regard, maintaining a volume allows for faster recovery should a subsequent reactor fail. As used in this document, “reactor failure” refers to a condition in which gas conversions do not occur and cells appear visually dead upon microscopic evaluation. In this regard, once a reactor failure occurs, the reactor can be reset within 24 hours.
    [0031] Upon reaching a target cell density in a pre-reactor, subsequent steps in the process can be described as follows:

    [0032] then, a volume of the pre-reactor is transferred to a main reactor in an amount effective to provide a minimum cell density in the main reactor; or

    [0033] then, a volume of the pre-reactor is transferred to a subsequent pre-reactor in an amount effective to provide a minimum cell density in the main reactor. This step of transferring from one pre-reactor to another can be repeated until transferring to a main reactor.
    [0034] In another aspect, upon reaching a target cell density in a pre-reactor, subsequent steps in the process can be described as follows:

    [0035] then, a volume of the pre-reactor is transferred to a main reactor in an amount effective to provide a minimum cell density in the main reactor; or

    [0036] then, a volume of the main reactor can be adjusted and a volume of the pre-reactor can be transferred in an amount to provide a minimum viable cell density in the main reactor. The volume of the main reactor is then increased over time to a desired volume while maintaining a minimum viable cell density.
    [0037] Each reactor can be operated in an effective manner to maximize cell growth and maintain culture health. In one aspect, the medium used in each reactor can be the same or different. Examples of suitable means include those described in US Patent 7,285,402, PCT/US2009/001522, and US Provisional Applications 61/458,899, 61/458,903 and 61/458,976, all filed December 3, 2010, and all of which are incorporated in their entirety herein by reference. Higher concentration levels of one or more vitamins can be used during the growth phase.
    [0038] In one aspect, a seed reactor can be inoculated with about 0.3 to about 0.7 grams of cells per liter. Singas can be sprayed into the seed reactor at a rate of about 0.5 to about 2.0 liters per minute, otherwise about 0.75 to about 1.25 liters per minute. Initial agitation is conducted at about 10 to about 40% of the total agitation power. Agitation rates can be increased to full power for one hour. For example, agitation rates can be increased from about 100 to about 1000 rpm for smaller reactors and increases can be correspondingly smaller for larger reactors. Acetogenic Bacteria
    [0039] In one aspect, the microorganisms used include acetogenic bacteria. Examples of useful acetogenic bacteria include those of the Clostridium genus, such as Clostridium ljungdahlii strains, including those described in WO 2000/68407, EP 117309, US Patents 5,173,429, 5,593,886 and 6,368,819, WO 1998/00558 and WO 2002/08438, strains of Clostridium autoethanogenum (DSM 10061 and DSM 19630 from DSMZ, Germany) including those described in WO 2007/117157 and WO 2009/151342 and Clostridium ragsdalei (P11, ATCC BAA-622) and Alkalibaculum bacchi (CP11, ATCC BAA-1772) including those described respectively in US Patent 7,704,723 and "Biofuels and Bioproducts from Biomass-Generated Synthesis Gas", Hasan Atiyeh, presented at Oklahoma EPSCoR Annual State Conference, April 29, 2010 and Clostridium carboxidivorans (ATCC PTA-7827) disclosed in US Patent Application 2007/0276447. Other suitable microorganisms include those of the genus Moorella, including Moorella sp. HUC22-1, and those of the Carboxydothermus genus. Each of these references is incorporated into this document for reference. Mixed cultures of two or more microorganisms can be used.
    [0040] Some examples of useful bacteria include Acetogenium kivui, Acetoanaerobium noterae, Acetobacterium woodii, Alkalibaculum bacchi CP11 (ATCC BAA-1772), Blautia producta, Butyribacterium methylotrophicum, Caldanaerobacter subterraneous, Caldanaerobacter subterraneousformate pacificus, Carboxydium Clostridium acetobutylicum P262 (DSM 19630 from DSMZ Germany), Clostridium autoethanogenum (DSM 19630 from DSMZ Germany), Clostridium autoethanogenum (DSM 10061 from DSMZ Germany), Clostridium autoethanogenum (DSM 23693 from DSMZ Germany), Clostridium autoethanogenum (DSMZ Germany) , Clostridium carboxidivorans P7 (ATCC PTA-7827), Clostridium coskatii (ATCC PTA-10522), Clostridium drakei, Clostridium ljungdahlii PETC (ATCC 49587), Clostridium ljungdahlii ERI2 (ATCC 55380), Clostridium ljungdahlii (ATCC 49587). ljungdahlii O-52 (ATCC 55889), Clostridium magnum, Clostridium pasteurianum (DSM 525 from DSM Z Germany), Clostridium ragsdali P11 (ATCC BAA-622), Clostridium scatologenes, Clostridium thermoaceticum, Clostridium ultunense, Desulfotomaculum kuznetsovii, Eubacterium limosum, Geobacter sulfurreducens, Methanosarcina acetivorans, Methanosarcina, P. Ruminococcus productus, Thermoanaerobacter kivui, and mixtures thereof. singas
    [0041] Singas can be supplied from any known source. In one aspect, singas can be of carbonaceous material gasification origin. Gasification involves partial combustion of biomass in a restricted supply of oxygen. The resulting gas mainly includes CO and H2. In this aspect, the singas will contain at least about 10% by mole of CO, in one aspect, at least about 20% by, in another aspect about 10 to about 100% by mole, in another aspect, about 20 to about 100% mole CO, in another aspect about 30 to about 90% mole CO, in another aspect about 40 to about 80% mole CO, and in another aspect about 50 to about 70% by mole of CO. The syngas will have a CO/CO2 molar ratio of at least about 0.75. Some examples of suitable gasification methods and apparatus are provided in Serial Numbers 61/516,667, 61/516,704 and 61/516,646, all of which were filed on April 6, 2011 and all of which are incorporated herein by reference.
    [0042] In another aspect, the syngas used to propagate acetogenic bacteria may be substantially CO. As used herein, "substantially CO" means at least about 50% mole CO, in another aspect at least about 60% mole CO, in another aspect at least about 70% mole CO, in in another aspect at least about 80% by mole of CO, and in another aspect at least about 90% by mole of CO. EXAMPLE 1: Startup with Two Growth Reactors
    [0043] A seed fermenter (90 liters) is inoculated with Clostridium ljungdahlii. Singas was fermented until a cell density of about 12 grams/liter was obtained. One half of the seed fermenter (about 45 liters) is used to inoculate a first growth reactor to provide a total volume in the first growth reactor of about 1390 liters and a starting cell density of about 0.38 grams per liter. Singas is fermented for 140 hours from the time of inoculation to provide a cell density of about 12 grams per liter. Culture from the first growth reactor (about 703 liters) is used to inoculate a second growth reactor to provide a total volume in the second growth reactor of about 22200 liters and a cell density of about 0.38 grams per liter . Singas is fermented for 140 hours from the time of inoculation to provide a cell density of about 12 grams per liter. Second growth reactor culture (about 12,000 liters) is used to inoculate a main reactor to provide a total main reactor volume of about 350,000 to 400,000 liters and a cell density of about 0.40 grams per liter. The total elapsed time from inoculation of the first growth reactor to inoculation of the main reactor is 11.7 days. EXAMPLE 2: Startup with Seed Reactor and a Growth Reactor
    [0044] A seed fermenter (about 1600 liters) is inoculated with Clostridium ljungdahlii. Singas was fermented until a cell density of about 12 grams/liter was obtained. One half of the seed fermenter (about 700 liters) is used to inoculate a first growth reactor to provide a total volume in the first growth reactor of about 2250 liters and a starting cell density of about 0.38 grams per liter. Singas is fermented for 140 hours from the time of inoculation to provide a cell density of about 12 grams per liter. First growth reactor culture (about 11,000 liters) is used to inoculate a main reactor to provide a total main reactor volume of about 350,000 to 400,000 liters and a cell density of about 0.38 grams per liter. The total elapsed time from inoculation of the first growth reactor to inoculation of the main reactor is 9.2 days.
    [0045] Although the invention in this document has been described by means of specific embodiments, examples and applications thereof, numerous modifications and variations can be made thereto by those skilled in the art without departing from the scope of the invention set forth in the Claims.
    权利要求:
    Claims (12)
    [0001]
    1. Process for Fermenting Synthesis Gas, characterized in that it comprises propagating a culture of acetogenic bacteria effective to inoculate a main reactor, the propagation including i) inoculating a first culture of acetogenic bacteria in a pre-reactor to provide a density of minimal viable cells, ii) growing the culture of acetogenic bacteria in the pre-reactor to provide a target cell density in the pre-reactor, (a) where if (the density of pre-reactor target cells multiplied by the pre-reactor volume reactor) + (a main reactor volume multiplied by (a pre-reactor volume ^ a pre-reactor volume that is transferred)) is greater than or equal to a minimum viable cell density, transfer a pre-reactor volume to the main reactor in an amount effective to provide a minimum viable cell density in the main reactor or, (b) if (the prereactor target cell density multiplied by the prereactor volume) ^ (one volume a main reactor volume multiplied by (a pre-reactor volume ^ a pre-reactor volume that is transferred)) is less than a minimum viable cell density, transferring a pre-reactor volume to a subsequent pre-reactor in an amount effective to provide a minimum viable cell density in a subsequent pre-reactor and iii) repeat step (ii) until a volume of the pre-reactor is transferred to the main reactor.
    [0002]
    2. Process for Fermenting Synthesis Gas, according to Claim 1, characterized in that the minimum viable cell density is at least 0.2 grams per liter; and/or by the fact that the pre-reactor target cell density is at least 5 grams per liter; and/or by the fact that 25% to 75% of a volume of a pre-reactor is used to inoculate a subsequent pre-reactor or main reactor; and/or by the fact that a volume ratio of the prereactor volume transferred to a subsequent prereactor volume or main reactor volume is from 0.02 to 0.5.
    [0003]
    Process for Fermenting Synthesis Gas, according to Claim 1, characterized in that the synthesis gas has a molar ratio of CO/CO2 of at least 0.75; and/or by the fact that the first culture has a pH of 6.5 or less and an acetic acid concentration of 10 grams per liter or less; and/or by the fact that the synthesis gas has 20 to 100% by mole of CO; and/or by the fact that the synthesis gas used to propagate acetogenic bacteria is CO.
    [0004]
    4. Process for Fermenting Synthesis Gas, according to Claim 1, characterized in that the acetogenic bacteria are selected from the group consisting of Acetogenium kivui, Acetoanaerobium noterae, Acetobacterium woodii, Alkalibaculum bacchi CP11 (ATCC BAA-1772), Blautia producta, Butyribacterium methylotrophicum, Caldanaerobacter subterraneous, Caldanaerobacter subterraneous pacificus, Carboxydothermus hydrogenoformans, Clostridium aceticum, Clostridium acetobutylicum, Clostridium acetobutylicum (DSM 19630 from DSMZ Germany), Germany Clostridium autoethane DSM61 (DSM 19630 from DSMDSM Germany), Germany , Clostridium autoethanogenum (DSM 23693 from DSMZ Germany), Clostridium autoethanogenum (DSM 24138 from DSMZ Germany), Clostridium carboxidivorans P7 (ATCC PTA-7827), Clostridium coskatii (ATCC PTA-10522, Clostridium drakei, Clostridium 497) (Clostridium PET58l , Clostridium ljungdahlii ERI2 (ATCC 55380), Clostridium ljungdahlii C-0 1 (ATCC 55988), Clostridium ljungdahlii O-52 (ATCC 55889), Clostridium magnum, Clostridium pasteurianum (DSM 525 from DSMZ Germany), Clostridium ragsdali P11 (ATCC BAA-622), Clostridium scatologenes, Cloultstridium desulfensema, Clostridium thermoaceticum, Clostridium thermoaceticum, Clostridium , Eubacterium limosum, Geobacter sulfurreducens, Methanosarcina acetivorans, Methanosarcina barkeri, Morrella thermoacetica, Morrella thermoautotrophica, Oxobacter pfennigii, Peptostreptococcus productus, Ruminococcus productus, Thermoanaerobacter kivui, and mixtures thereof.
    [0005]
    5. Process for Fermenting Synthesis Gas, characterized in that it comprises propagating a culture of acetogenic bacteria effective to inoculate a main fermentation reactor, the propagation including i) inoculating a first culture of acetogenic bacteria in a pre-reactor to provide a minimum viable cell density, ii) growing the acetogenic bacteria culture in the pre-reactor to provide a target cell density in the pre-reactor, (a) where if (the density of pre-reactor target cells multiplied by the volume of the prereactor) + (a main reactor volume multiplied by two) is greater than or equal to a minimum viable cell density, transfer a volume from the prereactor to the main reactor in an effective amount to provide a minimum viable cell density in the main reactor or, (b) if (the pre-reactor target cell density multiplied by the pre-reactor volume) ^ (one main reactor volume multiplied by two) is men Rather than a minimum viable cell density, adjust the main reactor volume and transfer a volume from the pre-reactor to the main reactor in an effective amount to provide a minimum viable cell density in the main reactor and increase the main reactor volume , while maintaining a minimum viable cell density.
    [0006]
    6. Process for Fermenting Synthesis Gas, according to Claim 5, characterized in that the minimum viable cell density is at least 0.2 grams per liter; and/or by the fact that the pre-reactor target cell density is at least 5 grams per liter; and/or by the fact that the synthesis gas has a molar ratio of CO/CO2 of at least 0.75.
    [0007]
    7. Process for Fermenting Synthesis Gas, according to Claim 5, characterized in that the synthesis gas has 20 to 100% by mole of CO; and/or by the fact that the synthesis gas used to propagate acetogenic bacteria is CO; and/or the fact that the first culture has a pH of 6.5 or less and an acetic acid concentration of 10 grams per liter or less.
    [0008]
    8. Process for Fermenting Synthesis Gas, according to Claim 5, characterized in that the acetogenic bacteria are selected from the group consisting of Acetogenium kivui, Acetoanaerobium noterae, Acetobacterium woodii, Alkalibaculum bacchi CP11 (ATCC BAA-1772), Blautia producta, Butyribacterium methylotrophicum, Caldanaerobacter subterraneous, Caldanaerobacter subterraneous pacificus, Carboxydothermus hydrogenoformans, Clostridium aceticum, Clostridium acetobutylicum, Clostridium acetobutylicum P262 (DSM 19630 from DSMD Germany, DSM 19630 autoogenumtri (DSM 19630 from DSMD Germany, Germanye 19630 autogentrium autogenum ), Clostridium autoethanogenum (DSM 23693 from DSMZ Germany), Clostridium autoethanogenum (DSM 24138 from DSMZ Germany), Clostridium carboxidivorans P7 (ATCC PTA-7827), Clostridium coskatii (ATCC PTA-10522), Clostridium drakei, Clostridium 4 PETCjung l ), Clostridium ljungdahlii ERI2 (ATCC 55380), Clostridium ljungdahli i C-01 (ATCC 55988), Clostridium ljungdahlii O-52 (ATCC 55889), Clostridium magnum, Clostridium pasteurianum (DSM 525 from DSMZ Germany), Clostridium ragsdali P11 (ATCC BAA-622), Clostridium scatologenes, Clostridium pasteurianum, Clostridium thermoaceticum , Desulfotomaculum kuznetsovii, Eubacterium limosum, Geobacter sulfurreducens, Methanosarcina acetivorans, Methanosarcina barkeri, Morrella thermoacetica, Morrella thermoautotrophica, Oxobacter pfennigii, Peptostreptococcus productus, Ruminococcus productus, Thermoanaerobacter mixtures thereof.
    [0009]
    9. Process To Start Main Fermenter For Synthesis Gas Fermentation, the process characterized by the fact that it comprises: inoculating a first culture of acetogenic bacteria in a seed reactor to provide a minimum initial viable cell density in the seed reactor. at least 0.2 grams per liter; growing the acetogenic bacteria culture with syngas to provide a cell density in the seed reactor of at least 5 grams per liter; inoculating a first growth reactor with a seed reactor inoculum in an amount effective to provide a cell density in the growth reactor of at least 0.2 grams per liter; growing the culture with synthesis gas to provide a cell density in the first growth reactor of at least 5 grams per liter; inoculating a second growth reactor with an inoculum from the first growth reactor in an amount effective to provide a cell density in the growth reactor of at least 0.2 grams per liter; growing the culture with synthesis gas to provide a cell density in the second growth reactor of at least 5 grams per liter; and inoculating a main fermenter with an inoculum from the second growth reactor in an amount effective to provide a cell density in the main reactor of at least 0.2 grams per liter.
    [0010]
    10. Process for Starting Main Fermenter for Synthesis Gas Fermentation according to Claim 9, characterized in that the first culture has a pH of 6.5 or less and an acetic acid concentration of 10 grams per liter or any less; and/or by the fact that 25% to 75% of a volume from the seed reactor is inoculated into the first growth reactor, 25% to 75% of a volume from the first growth reactor is inoculated into the second growth reactor and % to 75% of a volume from the second growth reactor is inoculated into the main fermenter; and/or by the fact that a ratio of reactor volume to reactor volume receiving the inoculum is 0.02 to 0.5.
    [0011]
    11. Process for Starting Main Fermenter for Synthesis Gas Fermentation, according to Claim 9, characterized by the fact that the seed reactor has a volume of 500 liters or less; and/or by the fact that the synthesis gas has a molar ratio of CO/CO2 of at least 0.75; and/or by the fact that the synthesis gas has 20 to 100% by mole of CO; and/or by the fact that the synthesis gas used to propagate acetogenic bacteria is CO.
    [0012]
    12. Process for Starting Main Fermenter for Synthesis Gas Fermentation, according to Claim 9, characterized in that the acetogenic bacteria are selected from the group consisting of Acetogenium kivui, Acetoanaerobium noterae, Acetobacterium woodii, Alkalibaculum bacchi CP11 (ATCC BAA -1772), Blautia producta, Butyribacterium methylotrophicum, Caldanaerobacter Caldanaerobacter subterraneous pacificus, Carboxydothermus hydrogenoformans, Clostridium aceticum, Clostridium acetobutylicum, Clostridium acetobutylicum P262 (DSM 19627 from DSM 19627 from DSM CCATTII (PTATCtridium CCATtridium) -10522), Clostridium drakei, Clostridium ljungdahlii PETC (ATCC 49587), Clostridium ljungdahlii ERI2 (ATCC 55380), Clostridium ljungdahlii C-01 (ATCC 55988), Clostridium ljungdahlii O-52 (ATCC 55889), Clostridium ljungdahlii magnumstridium (ATCC 55889), 525 from DSMZ Germany), Clostridium ragsdali P11 (ATCC BAA-622), Clostridium scatologenes, Clostridium thermoaceticum, Clostridium ultunense, Desulfotomaculum kuznetsovii, Eubacterium limosum, Geobacter sulfurreducens, Methanosarcina acetivorans, Methanosarcina barkeri, Morrella thermoacetica, Morrella product autotrophica, Oxobacter pfennigii, Peptostreptococcus, and their mixtures.
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    同族专利:
    公开号 | 公开日
    MX348760B|2017-06-27|
    BR112013033713A2|2017-07-04|
    TWI576430B|2017-04-01|
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    AU2012275931A1|2014-01-23|
    JP2014518090A|2014-07-28|
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    BR112013033711A2|2017-01-24|
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    KR102004557B1|2019-07-26|
    TWI563079B|2016-12-21|
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    法律状态:
    2017-01-31| B15I| Others concerning applications: loss of priority|
    2018-04-03| B06F| Objections, documents and/or translations needed after an examination request according [chapter 6.6 patent gazette]|
    2020-04-07| B06U| Preliminary requirement: requests with searches performed by other patent offices: procedure suspended [chapter 6.21 patent gazette]|
    2020-08-04| B25D| Requested change of name of applicant approved|Owner name: JUPENG BIO SA (CH) |
    2020-08-18| B25G| Requested change of headquarter approved|Owner name: JUPENG BIO SA (CH) |
    2020-09-01| B25A| Requested transfer of rights approved|Owner name: JUPENG BIO (HK) LIMITED (CN) |
    2021-04-13| B06A| Patent application procedure suspended [chapter 6.1 patent gazette]|
    2021-06-08| B09A| Decision: intention to grant [chapter 9.1 patent gazette]|
    2021-07-13| B16A| Patent or certificate of addition of invention granted [chapter 16.1 patent gazette]|Free format text: PRAZO DE VALIDADE: 20 (VINTE) ANOS CONTADOS A PARTIR DE 31/05/2012, OBSERVADAS AS CONDICOES LEGAIS. |
    优先权:
    申请号 | 申请日 | 专利标题
    US201161571565P| true| 2011-06-30|2011-06-30|
    US201161571564P| true| 2011-06-30|2011-06-30|
    US61/571,564|2011-06-30|
    US201161573845P| true| 2011-09-13|2011-09-13|
    US61/573,845|2011-09-13|
    US13/471,858|US20130005010A1|2011-06-30|2012-05-15|Bioreactor for syngas fermentation|
    US13/471,827|2012-05-15|
    US13/471,827|US9976158B2|2011-06-30|2012-05-15|Method and apparatus for syngas fermentation with high CO mass transfer coefficient|
    US13/471,858|2012-05-15|
    US13/473,167|US8592191B2|2011-06-30|2012-05-16|Process for fermentation of syngas|
    US13/473,167|2012-05-16|
    PCT/US2012/040327|WO2013002949A1|2011-06-30|2012-05-31|Process for fermentation of syngas|
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