WO1981002898A1 - Procede et dispositif de production de cultures utiles et/ou de metabolites - Google Patents

Procede et dispositif de production de cultures utiles et/ou de metabolites Download PDF

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Publication number
WO1981002898A1
WO1981002898A1 PCT/US1981/000416 US8100416W WO8102898A1 WO 1981002898 A1 WO1981002898 A1 WO 1981002898A1 US 8100416 W US8100416 W US 8100416W WO 8102898 A1 WO8102898 A1 WO 8102898A1
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WO
WIPO (PCT)
Prior art keywords
fermentation
zone
generally
tray
zones
Prior art date
Application number
PCT/US1981/000416
Other languages
English (en)
Inventor
R Prentice
D Mastarone
Original Assignee
Solargizer Int Inc
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Priority claimed from US06/136,053 external-priority patent/US4328317A/en
Priority claimed from US06/136,054 external-priority patent/US4378434A/en
Application filed by Solargizer Int Inc filed Critical Solargizer Int Inc
Priority to AU70798/81A priority Critical patent/AU7079881A/en
Publication of WO1981002898A1 publication Critical patent/WO1981002898A1/fr

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    • C—CHEMISTRY; METALLURGY
    • C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
    • C12M—APPARATUS FOR ENZYMOLOGY OR MICROBIOLOGY; APPARATUS FOR CULTURING MICROORGANISMS FOR PRODUCING BIOMASS, FOR GROWING CELLS OR FOR OBTAINING FERMENTATION OR METABOLIC PRODUCTS, i.e. BIOREACTORS OR FERMENTERS
    • C12M27/00—Means for mixing, agitating or circulating fluids in the vessel
    • C12M27/02—Stirrer or mobile mixing elements
    • C—CHEMISTRY; METALLURGY
    • C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
    • C12M—APPARATUS FOR ENZYMOLOGY OR MICROBIOLOGY; APPARATUS FOR CULTURING MICROORGANISMS FOR PRODUCING BIOMASS, FOR GROWING CELLS OR FOR OBTAINING FERMENTATION OR METABOLIC PRODUCTS, i.e. BIOREACTORS OR FERMENTERS
    • C12M23/00—Constructional details, e.g. recesses, hinges
    • C12M23/02—Form or structure of the vessel
    • C12M23/04—Flat or tray type, drawers
    • C—CHEMISTRY; METALLURGY
    • C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
    • C12M—APPARATUS FOR ENZYMOLOGY OR MICROBIOLOGY; APPARATUS FOR CULTURING MICROORGANISMS FOR PRODUCING BIOMASS, FOR GROWING CELLS OR FOR OBTAINING FERMENTATION OR METABOLIC PRODUCTS, i.e. BIOREACTORS OR FERMENTERS
    • C12M23/00—Constructional details, e.g. recesses, hinges
    • C12M23/34—Internal compartments or partitions
    • C—CHEMISTRY; METALLURGY
    • C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
    • C12M—APPARATUS FOR ENZYMOLOGY OR MICROBIOLOGY; APPARATUS FOR CULTURING MICROORGANISMS FOR PRODUCING BIOMASS, FOR GROWING CELLS OR FOR OBTAINING FERMENTATION OR METABOLIC PRODUCTS, i.e. BIOREACTORS OR FERMENTERS
    • C12M29/00—Means for introduction, extraction or recirculation of materials, e.g. pumps
    • C12M29/20—Degassing; Venting; Bubble traps

Definitions

  • This invention relates to a process for stimulating the growth of a microorganism culture in a series of growth zones and withdrawing metabolites produced by the culture.
  • An aspect of this invention relates to a continuous process for the production of useful metabolites from a culture, utilizing metabolic processes of the culture.
  • Another aspect of this invention relates to a continuous process for the production of useful metabolites (e.g. organic liquids or solids or useful gases such as carbon dioxide) from a carbohydrate-containing nutrient medium by fermentation of the medium.
  • useful metabolites e.g. organic liquids or solids or useful gases such as carbon dioxide
  • Still another aspect of this invention relates to the fermentation of a fermentable feedstock on a continuous basis (as opposed to a batch basis).
  • a still further aspect of this invention relates to a process for continuously converting carbohydrate-containing materials to a "beer” comprising from 1 to about 20% by weight or by volume of an alkanol (preferably ethyl alcohol) dissolved in water.
  • an alkanol preferably ethyl alcohol
  • microorganisms provide the catalytic action for the conversion is a relatively recent discovery going back only to the time of Louis Pasteur.
  • chemists and micrbbiologists have spent many decades of effort investigating and utilizing the metabolic processes of microorganisms for industrial applications.
  • recovery of the metabolites themselves is the goal, e.g. in the manufacture of alcoholic beverages, solvents, fuels, pharmaceuticals, and the like.
  • recovery of residues from the microorganism culture is of equal or greater importance.
  • the ultimate goal of the process may be the recovery of an enzyme secreted by the organisms during an organism growth phase, recovery of the nutrient material in an. upgraded form (e.g.
  • the growth of an inoculum or starter culture into a very much larger population of microorganisms is not necessarily a smooth, easily controlled process but may instead occur in spurts or phases.
  • the first stage of the growth of ah inoculum is sometimes referred to as the initiation phase.
  • the cells may be generally resting or adjusting to their environment. Typically, they are not sufficiently well adjusted or sufficiently mature to achieve growth through the typical growth mechanism of binary fission.
  • the microorganism culture may pass rather rapidly into the so-called logarithmic growth phase, during which the cell population increases in accordance with a geometric progression.
  • the logarithmic growth phase can continue more or less unhindered until the concentration of metabolites in the culture begins to reach a level which slows down or even stops further growth.
  • This terminal phase of the growth cycle often results because of toxic effects of metabolites upon the culture.
  • the metabolically produced ethyl alcohol is poorly tolerated by most yeasts. Some yeasts can tolerate no more than about 2% by volume of ethyl alcohol in the fermentation or production medium. Other yeasts can tolerate as much as 15% or more. Given the present state of the art, however, there are no yeasts which could tolerate the concentration of ethyl alcohol in strong alcoholic beverages (e.g. 80 U.S. proof and higher), hence the need to obtain these strong drinks by distillation.
  • Another factor which can contribute to the termination of the logarithmic growth phase is the exhaustion or substantial exhaustion of nutrients.
  • This exhaustion of nutrients may be arranged for deliberately so as to stop, the microbiological production process at a desired point.
  • maintenance nutrients can be added.
  • introduction of nutrients into a growth or production medium can involve risks of contamination or poisoning, introduction of extraneous microorganisms, or disruption of the environment within the growth zone (e.g. the loss of anaerobic conditions).
  • This invention contemplates a process which will continually bring both fresh and partly metabolized nutrient material into contact with a microorganism culture which is in the logarithmic growth phase, whereby the ratio of live, mature, rapidly growing, metabolite-tolerant microorganisms to nutrient material is generally maintained at an optimally high level, thereby increasing production through shortening of lag times, initiation and other relatively dormant phases, environmental adjustment, and exhaustion of nutrients or other conditions which may force the culture into a terminal growth phase.
  • This invention also contemplates a process for stimulating the growth of a microorganism culture and for recovering useful metabolites which can be carried out generally continuously.
  • Some microorganism cultures e.g. those used to produce citric acid
  • Some microorganism cultures tend to form a solid or semi-solid structure which facilitates continuous addition of nutrients and continuous withdrawal and recovery of the citric acid.
  • special conditions or manipulative steps are necessary to accomplish the same degree of continuous production with microorganisms which are normally kept suspended or dispersed in the nutrient medium.
  • this invention relates to a process and apparatus for stimulating the growth of a «microorganism . culture in a series of growth zones and withdrawing metabolites produced by the culture from one or more of these growth zones.
  • the metabolites are useful, e.g. in a continuous process for the production of oxygen-containing aliphatic compounds from a carbohydrate-containing nutrient medium by fermentation of the medium, these metabolites can be recovered.
  • this invention involves the process of:
  • step (e) further repeating steps (b) and (c) in successively lower tray-like growth zones until substantial multiplication of the microorganisms in the culture has been obtained (e.g. the culture has been brought to a sustained logarithmic growth phase);
  • a preferred microorganism growth culture comprises brewer's yeast and a hydrolyzed starch-containing aqueous nutrientmedium.
  • the invention also relates to an apparatus wherein the conversion or fermentation zone is divided up in at least two different ways.
  • the space within the fermentation zone is divided into a plurality of vertically arranged, tray-like fermentation zones for the temporary retention, continuous receiving, and continuous gravity discharge of the fermentable feedstock.
  • each tray-like fermentation zone is further divided into movable segments.
  • the fermentation apparatus is provided with means for collecting and withdrawing a substantial portion of the broth, "beer", or the like (i.e.. the partially fermented feedstock) from the interior of the fermentation apparatus and recirculating it, alone or in combination with fresh feedstock, to the topmost tray-like fermentation zone.
  • a "beer” or water solution containing a useful percentage of liquid fermentation products can then be withdrawn from the lower end of the fermentation zone.
  • the beer can also contain suspended or dispersed solids.
  • an apparatus of this invention comprises:
  • a generally vertically disposed conversion or fermentation tower defining a generally vertically extending space containing the plurality of vertically arranged, tray-like fermentation zones, each fermentation zone having a floor with a drain or discharge opening therein for continuous discharge by gravity of the partially fermented feedstock or production medium to the fermentation zone immediately below it,
  • a collection means under one of the drain openings in a fermentation zone for continuously collecting a portion of the partially fermented feedstock (b) a collection means under one of the drain openings in a fermentation zone for continuously collecting a portion of the partially fermented feedstock, (c) a feedstock conveying means, communicating with the upper end of the vertically extending space within the tower, which conveying means continuously conveys fermentable feedstock to the uppermost of the fermentation zones, (d) a partially converted feedstock recirculation means for continuously recirculating partially converted or fermented feedstock or production medium collected by the collection means to this uppermost fermentation zone (either directly or via the feedstock conveying means), whereby the fermentable feedstock conveyed to the uppermost of the fermentation zones continuously includes both fresh fermentable feedstock and partially fermented feedstock, and
  • Each tray-like conversion or fermentation zone has a generally upwardly extending wall for retaining the convertible feedstock within it, and within this wall there are provided movable partitions, so that this tray-like zone is divided into continuouslymovable segments for advancing the convertible (e.g. fermentable) feedstock toward the drain opening at a controlled rate. and for agitating the partially converted feedstock or production medium.
  • a particularly preferred arrangement involves a set of paddles or vanes or partitions extending radially outward from the center of each fcray-like fermentation zone.
  • a single drive shaft can simultaneously rotate all the sets of vanes or paddles in all of the traylike zones. The rate of rotation of the drive shaft can be set to provide the desired retention time in the tower.
  • the recirculation is to bring the biological catalytic medium (e.g. microorganism culture still in a rapid growth stage), which has progressed at least partway down the tower, into contact with a fresh energy source of fresh fermentable material and/or to recirculate this medium before the relatively toxic metabolites (e.g. alkanols, aldehydes, ketones, etc.) reach a concentration which inhibits further enzymatic or biological activity.
  • the biological catalytic medium e.g. microorganism culture still in a rapid growth stage
  • a fresh energy source of fresh fermentable material e.g. alkanols, aldehydes, ketones, etc.
  • FIGURE 1 is a side elevational view of a fermentation or conversion apparatus of this invention with parts broken away to show the internal structure of the fermentation tower;
  • FIGURE 2 is a cross-sectional view taken along line 2-2 of FIGURE 1;
  • FIGURE 3 is a cross-sectional view, taken along line 3-3 of FIGURE 2;
  • FIGURE 4 is a fragmentary perspective view of the conversion or fermentation tower, with portions broken away to show the internal structure of a tray-like conversion or fermentation or growth zone and its movable partitions or vanes;
  • FIGURE 5 is an enlarged fragmentary view of top and bottom seal and bearing housings of the conversion or fermentation apparatus of FIGURE 1, with parts broken away to show the internal structure within these housings;
  • FIGURE 6 is a fragmentary perspective view, on a reduced scale, of the arrangement of tray-like conversion or fermentation or growth zones, with the movable partitions removed and parts broken away to illustrate the location of drain openings in the various zones;
  • FIGURE 7 is a schematic representation of a complete system for the. production of liquid metabolites, gaseous metabolites, and high-protein solid residues, which system utilizes an embodiment of this invention.
  • the process of this invention can have a variety of uses generally related to industries such as alcoholic beverage manufacture and synthesis of solvents, fuels, pharmaceuticals, etc.
  • a common thread running through processes of this invention is that a living inoculum is multiplied and brought to a high growth rate in the presence of a nutrient medium, and the products of the resulting live culture and/or the residues from the culture are the principal objectives of the microbiological synthesis.
  • usefulmetabolites being one or more of the following: gaseous products such as carbon dioxide, oxygen containing aliphatic liquids or solids such, as lower (C 1 to C 6 , preferably C 2 -C 5 ) alkanols, carbonylcontaining compounds (aldehydes, ketones, and carboxylic acids), and more complex compounds such as riboflavin.
  • gaseous products such as carbon dioxide
  • oxygen containing aliphatic liquids or solids such, as lower (C 1 to C 6 , preferably C 2 -C 5 ) alkanols
  • carbonylcontaining compounds aldehydes, ketones, and carboxylic acids
  • complex compounds such as riboflavin.
  • the oxygen-containing aliphatic compounds can be polyfunctional but are typically monomeric in nature.
  • a particularly preferred embodiment of this invention involves the conversion of a carbohydrate-containing material to a "beer” and a solid residue which, though depleted in carbohydrate, is substantially enhanced (percentage-wise) in protein. Indeed, because of the inclusion of dead cellular material in the residue, the protein level can be increased in an absolute sense as well.
  • a typical example of a fermentable feedstock useful in this invention is a starchy mash (potato mash, corn mash, or the like). When food supplies are under economic pressure, driving th'e cost of feed grains, legumes, tubers, etc. upward, a fermentable feedstock can be prepared from agricultural waste materials such as weeds, cornstalks, corncobs, and the like.
  • Corn grain is reported to contain about 9% by weight of protein, a substantial portion of the balance of this grain being starch and other polysaccharides. Most animals (and humans as well) do not need such a high proportion of carbohydrate in their diet, and protein enrichment would normally be desirable for a diet heavily slanted toward corn grain, corn meal, or corn flour.
  • a substantial portion of the carbohydrate material in the corn grain is converted to useful organic liquids such as lower alkanols, with carbon dioxide being another useful by-product.
  • the residual corn nutrient obtained from the process can contain 30% by weight of protein as opposed to
  • suitable fermentable feedstocks are carbohydrate-containing, either in the form of material containing carbohydrate per se (e.g. sugars, starches, celluloses and hemi-celluloses, and other mono- and polysaccharides) or glycosides and the like, wherein a polysaccharide chain is linked to a non-carbohydrate nucleus.
  • an optional step of the process of this invention includes hydrolysis of the carbohydrate-containing feedstock.
  • Starchy feedstocks such as corn mash can be hydrolyzed to sugars rather quickly with moderate heat and a catalyst such as an amylase or an organic or inorganic acid.
  • the inoculum is then added to the hydrolyzed material, thereby providing a culture containing as its nutrient medium an aqueous solution of a naturally-occurring monosaccharide (glucose, fructose, mannose, galactose, gulose, similar aldohexoses and ketohexoses, ribose, or similar pentoses), their disaccharides, and their low molecular weight oligomers.
  • a naturally-occurring monosaccharide glucose, fructose, mannose, galactose, gulose, similar aldohexoses and ketohexoses, ribose, or similar pentoses
  • Some unhydrolyzed starch may be dispersed in the nutrient medium, along with suspended cellulosic matter, proteinaceousmatter, etc.
  • Other by-products of the food and agricultural industries can provide a similar nutrient medium, typical of such by-products being
  • gaseous metabolites are typically removed from the growth zones or fermentation zones through a suction or degassing apparatus.
  • This apparatus may also incidentally remove some water and organic liquids which are at least as volatilizable as water.
  • the "beer” water solution pf organic liquids
  • removed from at least the lowermost of the growth or fermentation zones will typically contain the organic liquids, water, and dissolved and suspended residues from the nutrient medium.
  • Various means for separating these components of the beer are well known in the art, including distillation, reverse osmosis, hyperfiltration, stripping, solvent extraction, settling, centrifugation, and various combinations of these techniques, including repetitions of substantially the same technique (e.g.
  • a mixture of finely ground starchy material suspended in water is introduced into a hydrolytic reactor 130 through supply line 132.
  • a second supply line 134 is provided for the introduction of a catalytic agent for the hydrolysis (e.g. an acid or an amylase-containing medium).
  • the output from reactor 130 is blended in-line at 136 with still another medium containing an inoculum, this medium being introduced through line 138.
  • the inoculum is a yeast, it will ordinarily be desirable to introduce air or oxygen through line 140 to stimulate yeast growth.
  • line 140 will be the only means in the s «ystem for introducing air or oxygen, since substantially the entire fermentation process from feed line 35 onward is preferably conducted with the exclusion of the ambient atmosphere.
  • the retention time in any given zone is a function of a number of factors, but it is preferred to make all zonal retention times generally equal.
  • a typical retention time in each zone ranges from about one to 100 minutes, and a typical total elapsed time for the flow from tower feed conduit 32 to the tower bottom or catch trough 121 below the lowermost zone is only a few hours or less, e.g. one to 20 hours.
  • the actual residence time in tower 11 is difficult to determine with precision, since the process of this invention involves recirculation of culture or production medium from lower zones to a higher zone, e.g. from zone 15c and lower to uppermost zone 15a.
  • the recirculation system 20 is preferably designed to accomodate at least 10 or 20% of the total capacity of tower 11; more preferably, at least 40% of the total production medium in the fermentation apparatus is in the recirculation system 20, substantially the balance being in tower 11.
  • One way of determining a residence time is to measure the influx through line 32 and the beer flow rate through, line 41. To provide a complete material balance, the gases removed through degassing manifold 18 should also be taken into account.
  • the culture tapped off into recirculation system 20. is pumped very gently to uppermost growth or fermentation zone 15a through conduit 32a.
  • pump 34 exerts less than about one atmosphere (14.7 p.s.i.g.) gauge pressure, more typically less than about 0-2 atmospheres or less than about 20 kPa. It has. been found that the culture (inoculum and nutrient medium) in the tower 11 and recirculation system 20 is well suited to gentle pumping and gravity flow. In the case of a fermentation with yeast, the culture contains a liquid nutrient medium. (It should be understood that the nutrient medium is considered a "liquid” even when it contains dispersed or suspended solid matter.) Liquid nutrient media such as a hydrolyzed mash (e.g.
  • corn mash, potato mash, etc. has a relatively low viscosity, not greatly different from the viscosity of water itself. Even the logarithmic growth of microorganisms in the culture does not so seriously increase the viscosity as to interfere with gravity flow and pumping. Furthermore, the constantly moving segments Cdescribed subsequently) in the growth or fermentation zones 15a, 15b, etc. help to provide agitation, generally uniform suspension or slurrying of solid, settlable matter and microorganism cells, and prevention of excess settling of material near the center or the periphery of fermentation or growth zones 15a, 15b, etc.
  • recirculation system 20 brings a culture which is preferably in a logarithmic growth phase up to the topmost growth or fermentation zone 15a.
  • This recirculation step accomplishes several objectives. It withdraws the rapidly growing culture from a lower zone of tower 11 before that culture approaches the termination phase too closely. It also brings the rapidly-growing culture into contact with fresh nutrient material, thereby partially making up for depletion of carbohydrate resulting from metabolic processes occurring in tower 11. It further inoculates zone 15a with rapidly multiplying microorganisms, so that the fresh culture introduced through, tower feed conduit 32 is brought to the logarithmic growth phase relatively quickly. Withdrawal of gaseous fermentation products
  • degassing manifold 18 also helps to maintain growth and favor desired chemical reactions.
  • the idealized chemical reaction for the early and middle stages of a carbohydrate fermentation with alcohol producing organisms is:
  • a weight ratio of at least 1:1 solid nutrient material; yeast will permit yeast growth. Maintenance of the logarithmic growth phase, however, may require a considerably higher ratio, e.g. 6:1 nutrient:yeast. These ratios assume a nutrient consisting essentially of monosaccharides, with sufficient phosphates, nitrogen-containing compounds, and the like to support yeast growth. In this invention, the incoming inoculum will typically be provided with a large excess of nutrient material. The culture in the recirculation system 20, on the other hand, will tend to be at or near the ratio favoring the most rapid growth of yeast organisms.
  • a healthy, rapidly multiplying yeast culture is quickly resupplied with nutrients, while the fresh incoming culture is bolstered in microorganism population so as to speed up the metabolism of the incoming nutrient material and thereby reduce retention time or residence time in tower 11.
  • the upper growth or fermentation zones are not allowed to get too high in nutrient:yeast ratio (e.g. not too far beyond 6:1), while the lower zones are not allowed to get too low in this ratio (e.g.
  • the gases withdrawn through degassing manifold 18 are conveyed to a condenser 208, which condenses any organic liquids and water volatilized by the degassing system.
  • the condensed liquids pass through line 210 so that they can be combined with the beer withdrawn from the bottom of the tower 11 through beer conduit 41.
  • the resulting combination of liquids, nutrient residues, etc. is conveyed to a separation zone 340, which can utilize the principles of. distillation, hyperfiltration, reverse osmosis, solvent extraction, rectification, stripping, or any other desired prior art technique for liquid/liquid or liquid/solid separation.
  • volatilizable metabolites are isolated and concentrated and flow out through line 346, while solid residues (proteinenriched mash or the like) flow out through line 342.
  • Water removed from the beer and the nutrient medium flows out through line 348 and can be discarded or reused in the process.
  • Suitable separation or concentration equipment can be obtained from commercial suppliers or custom built according to principles well known and well understood in the arts of distillation, solvent extraction, stripping, vacuum evaporation, reverse osmosis, and the like. For example, a conventional distillation column will suffice for the manufacture of 100 to 190 U.S. proof fuel alcohol. The conversion of such fuel alcohol to absolute alcohol (e.g.
  • the continuous fermentation apparatus 10 comprises principally the fermentation tower 11 and the recirculation system 20.
  • the recirculation system 20 includes a collection means, in this case a collection trough 23 positioned a little less than half-way down the length of the tower 11 (also referred to hereinafter as a fermentation tower).
  • a collection means 23 shown in phantom
  • Additional collection means can be provided, as shown in Figure 7.
  • a single collection means 23 is adequate to keep a substantial portion of the total fermentation medium in apparatus 10 continuously flowing through the recirculation system 20.
  • there will be an optimum location for collection means 23 for any given substrate or feedstock, there will be an optimum location for collection means 23. For some substrates and some conditions or desired products, location of the collection means closer to the top of the tower
  • Collection means 23 conveys partially fermented material through conduit 25 and valve 27 and check valve 29 to recirculation reservoir 21, which has a capacity approximately equal to four fermentation or growth zones, e.g. 15a, 15b, 15c, and 15d, generally referred to hereinafter as fermentation zones.
  • the material in reservoir 21 can pass through recirculation feed conduit 31 and valve 33 to mixing tee 39 for in-line mixing with raw feed from conduit 35 (and check valve 37). In any event, mixing tee 39 communicates with the tower feed means 32.
  • valve 33 can be used to bypass mixing tee
  • bypass conduit 32a which communicates directly with the uppermost fermentation zone 15a. See also Figure 7, wherein this alternate route is represented schematically.
  • the use of bypass 32a is preferred for sensitive microorganism cultures, e.g. yeasts, a preferred yeast being conventional brewer's yeast or "bottom yeast".
  • the entire recirculation and feed system is preferably as water-tight and air-tight as is reasonably practical under the circumstances. If the fermentation apparatus 10 needs to be provided with a source of oxygen for microorganisms or the like which multiply more rapidly under aerobic conditions, air or oxygen can be introduced upstream of tower feed conduit 32 (as shown in Figure 7 ⁇ , with the objective of optimizing organic liquid production in tower 11. Alternatively, as noted previously, one can deliberately introduce various gases.. (O 2 , CO 2 , etc. into tower 11 to stimulate or suppress various types of chemical or biological action. Fermentation tower 11 includes an outer shell 13 ( Figures 1 through 4) which defines a generally
  • the nature of the substrate or feedstock, the nature of the fermentation conditions, the desired products, the desired retention time, and so forth will determine the optimum number of tray-like fermentation zones 15a, 15b, etc.
  • at least three tray-like fermentation zones (15a through 15c) would ordinarily be preferred. So that the energy requirements for concentrating the beer will not be too unattractive economically, at least six tray-like fermentation zones (15a through 15f) would be continuously operating in a tower constructed according to this invention.
  • the particular tower 11 shown in Figure 1 has eight such tray-like fermentation zones (15a through 15h), but it will be understood that even more zones can be utilized, depending upon the factors described previously.
  • the retention time in the topmost tray-like fermentation zone 15a is within the range of 5 to 100 minutes, depending upon the speed of rotation of the movable segments within the zone. In the production of fuel alcohol from a mash Ccorn mash, potato mash, etc.), 10 to 20 minutes would be a more typical retention time.
  • a typical flow time from the topmost zone 15a to the inner bottom plate 121 is 80 to 160 minutes, with a substantial portion of the discharge or gravity flow from fermentation zone
  • tower feed conduit 32 preferably communicates with the interior space above tray-like fermentation zone 15a, so that gravity flow begins as the feed from conduit 32 enters the upper end of the space defined by shell 13 of tower 11.
  • tower feed conduit 32 passes through top plate 111. of outer shell 13 in a fluid-tight manner.
  • tray-like fermentation zone 15a is divided into movable segments by means of movable partitions or divider vanes or paddles 157a. These partitions 157a rotate about the longitudinal axis of the fermentation tower 11.
  • partitions 157a rotate, while the generally horizontal floor 65a and the vertically extending cylindrical wall 55a of fermentation zone 15a remain stationary. Despite the movement of partitions 157a with respect to the stationary wall 55a and floor 65a, substantially fluid-tight segmentation of zone 15a can be provided by techniques known in the art. Alternatively (but less preferably from the standpoint of convenience of manufacture), partitions 157a, wall 55a, and floor 65a can be a single, integral structure.
  • each segment of the tray preferably contains its own drain or discharge opening which is normally closed except for the period of time needed to discharge its contents into the next lower tray at the conclusion of a tray revolution.
  • all drain openings are fixed and constantly open. Relocation or rearrangement of drain openings can be provided by removing individual tray-like fermentation zones 15a through
  • tower feed conduit 32 feeds into that segment of the tray-like fermentation zone 15a which is, at the time it receives the feed, substantially empty and at least three-fourths of a revolution away from the drain opening.
  • FIGS 2-4 and 6 illustrate the operation of the fermentation zone 15c, which receives the discharge or gravity feed or flow from fermentation zone 15b, zone 15b being in turn fed by fermentation zone 15a.
  • This third fermentation zone 15c is selected to illustrate the operation of all tray-like fermentation zones 15a through 15h, since these zones operate in substantially the same manner.
  • zone 15c illustrates the use of the collection means 23 to tap off a substantial portion of the gravity flow from zone 15c for recirculation through recirculation system 20 to bypass 32a or to mixing tee 39 and tower feed conduit 32..
  • tray-like fermentation zone 15c is divided into eight segments by movable partitions 157c. Movable partitions 157c all radiate outward from the center of zone 15c. They are rotatable and are rotated by means of paddle arms 155c. Paddle arms 155c are attached to paddles
  • Such in-plant assembly can be carried out conveniently by inserting the tray-like fermentation zones 15a through 15h into shell 13 one at a time, with drive shaft 151 in place and with each set of paddles (beginning with paddles 157h) dropped down onto each tray-like fermentation zone (beginning with 15h) and attached to the drive shaft through a linkage including the paddle arms (starting with 155h) and other elements which will now be described.
  • paddle arm 155d is integral with a hub 159d which snuggly engages drive shaft 151 and is attached thereto with pins 259 ( Figure 3).
  • paddles 157d are integral with the.paddle arm/hub assembly 155d/159d which is connected to drive shaft 151 at hub 159d.
  • these elements can all be disassembled to permit removal of the movable segments for cleaning, repair, and the like.
  • the lower end (approximately the lower half) of hub 159d surrounds and encloses a cylindrical vertical sleeve 153d as shown in Figures 3 and 4.
  • Sleeve 153c (Fig. 3) coincides with and defines the central opening 163c in the floor 65c of fermentation zone 15c.
  • This opening 163c and the vertically extending sleeve 153c which occupies the opening,and openings and sleeves above and below it in overlying and underlying fermentation zones (sleeve 153b of zone 15b, sleeve 153d of zone 15d, etc., best illustrated. in Figure 6) define a generally vertically extending shaft tunnel for drive shaft 151.
  • tray-like fermentation zone 15c is preferably a generally vertically-extending toroidal space closed off at its lower end by floor 65c, which floor 65c is a two-dimensional torus.
  • floor 65c which floor 65c is a two-dimensional torus.
  • the top edge of paddles 157c is just below the top edge of wall 55c.
  • the upper or free surface of the fluid fermentation medium in zone 15c preferably is no higher than the topmost edge of paddles 157c and is optimally slightly lower.
  • each adjacent pair of paddles 157c, in combination with the subtended portion of wall 55c and sleeve 153c defines a movable segment having an angle or circumferential portion A.
  • angle A is 45°.
  • angle A would normally not exceed 180° and typipally be not more than 90°.
  • the complexity of the structure of fermentation zone 15c might be greatly increased if angle A were less than 45°.
  • the .elements of fermentation zone 15c can-be constructed from relatively lightweight .plastics such as polyolefins (even "high density" polyethylene has a specific gravity less than 1.0), at least some of the elements in the zone (e.g. hub 159c) may be constructed of metal (e.g. stainless steel) and, in any event, the total weight of zone 15c filled nearly to the brim with a fermentation medium weighing at least about one kilogram per liter will be extremely heavy and require an adequate support structure.
  • This support structure is illustrated in Figure 2, wherein a portion of floor 65c has been broken away to show support ribs 175c, extending radially outward from support ring 173c.
  • Braces 171c tie together the radial ribs 175c in a chord-like concentric arrangement which provides additional structural strength.
  • Each radial rib 175c is designed to engage a hanger 177c, much in the manner of a key fitting into a key-way. This rib/ hanger engagement fixes the tray-like fermentation zone 15c in the desired position but also permits removal of the tray-like zone 15c, e.g. by hoisting the zone 15c directly upward.
  • the centrally-located support ring 173c is in register with sleeve 153c and thus also forms a part of the shaft tunnel through which drive shaft 151 runs. As shown in Figure 3 and Figure 2, the inside diameter of support ring 173c is slightly larger than the outside diameter of sleeve 153c or even the lower half of hub 159c.
  • conduit or tube 17c which removes gaseous fermentation products (e.g. carbon dioxide) from fermentation zone 15c and conveys these gaseous products to the suction or degassing manifold 18.
  • gaseous fermentation products e.g. carbon dioxide
  • trough 23 which collects a substantial portion of the downward flow from zone 15c and conveys it, through conduit 25 and valve 27 to the recirculation system 20 ( Figure 1).
  • drain opening 165c is substantially, but not exactly, radially oriented with respect to the center of floor 65c.
  • drain opening 165c is offset ..from but generally parallel and in closely spaced relation to a radius extending from the center of floor 65c, i.e. from the generally vertical axis of fermentation tower 11.
  • porthole 300 ( Figure 2) provided with a glass or plastic lens (not visible in Figure 2) is included in the structure of shell 13 for this purpose.
  • An additional advantage of porthole 300 is that further conduits, troughs, or the like can be inserted into the interior of fermentation tower 11 using suitable peripheral sealing collars or the like (not shown), thereby avoiding the necessity or cutting through shell 13 if such additional elements become desirable after the construction of tower 11 is complete.
  • drive shaft 151 extends along the entire vertical axis of tower 11 and is driven by a motor 200 and chain drive means 201 located outside of the sealed subatmospheric interior space defined by shell 13 of tower 11.
  • motor 200 and the chain drive 201 are shown at the bottom of tower 11. In actual practice, it may be convenient to drive the drive shaft 151 from at its top end.
  • top seal and bearing housing 113 is a substantially cylindrical projection extending upwardly from top plate 111. Reinforcing rib 115 also extends upwardly from top plate 111 and radially outward from housing 113. Housing 113 is provided with a seal 119 which prevents leakage of ambient air into the interior of tower 11 by sealingly engaging the outer surface of drive shaft 151. This sealing engagement does not prevent rotation of drive shaft 151, however.
  • the upper end of drive shaft 151 is held in the desired orientation by bearing 117, which also permits rotation of drive shaft 151.
  • FIG 5 also illustrates the structure of bottom seal and bearing housing 123, which is similar in design and in concept to the top housing 113.
  • the bottom seal and bearing housing 123 extends both upwardly and downwardly from, inner bottom plate 121.
  • Above plate 121 the vacuum and ambient air exclusion conditions are maintained. Providing these conditions above bottom plate 121 is desirable, since, while only a very minor amount of fermentation (if any) may be taking place in the space immediately above plate 121, this plate 121 nevertheless serves as a catch trough for the discharge from lowermost fermentation zone 15h ( Figure 1).
  • Bottom plate 121 is slanted downwardly so as to direct the flow of the beer into a suitable withdrawing means, in this case beer conduit 41. (The beer is pumped by pump 43 to a conventional apparatus for further processing of the beer, including concentration of the organic liquids in the beer; see Figure 1.)
  • housing 123 is provided with bottom seal 129 and bottom bearing 127, which are similar in design to top seal 119 and top bearing 117.
  • the drive means for drive shaft 151 i.e. motor 200 and drive chain 201 can therefore be located outside of the sealed interior of tower 11.
  • Drive chain 201 can engage the lower end of drive shaft 151 by any suitable means such as the sprocket 203 shown in Figure 1.
  • a brace or rib 116 radiates from the outer surface of housing 123 out to the inside surface of shell 13.
  • withdrawing means 41 can be for removing suspended or dispensed residues only while manifold 18 can be for removing the gaseous metabolites Operation of the Apparatus
  • the incoming mash or other fermentable feedstock is preferably blended with an active microorganism culture before passing through check valve 37.
  • Partially fermented material and the highly active, rapidly growing culture are preferably conveyed to the first tray-like fermentation zone 15a via bypass 32a, while the flow from valve 37 is conveyed to zone 15a through conveying means or conduit 32.
  • the gravity feed from conduits 32 and 32a falls into a movable segment of zone 15a defined by a pair of adjacent paddles 157a. This segment rotates through almost a full revolution before reaching the drain opening and discharging into zone 15b.
  • a similar sequence of events occurs in zone 15b and the fermentation medium then drops through the drain in zone 15b into the movable segment just "beyond" drain opening 165c in zone 15c.
  • This movable segment describes about 7/8 of a revolution (about 315°) before its leading paddle 157c reaches drain opening
  • the material in trough 23 exits through shell 13 via conduit 25 and into the recirculation system 20, from which it flows via bypass 32a to tower 11, to begin a new pass through zones 15a, 15b, etc., starting with zone 15a.
  • the material collected in trough 23 contains a vastly multiplied microorganism culture.
  • at least the first three fermentation zones 15a, 15b, and 15c provide fermentation, agitation, and organism multiplication in this preferred mode of operation, thereby providing a high ratio of active microorganisms to fermentable material.
  • zone 15d continues to rotate and flow downard through zones 15e, 15f, 15g, and 15h of tower 11 until it is discharged from the lowermost zone 15h onto inner bottom plate 121, which acts as a catch trough feeding the beer conduit 41.
  • the location of drain openings 165a, 165b, etc. is illustrated in Figure 6.
  • the fixed drain openings (165b, 165c, ⁇ 65d, etc.) will be located as follows with respect to 270° in zone 15a: 165b ( Figure 6) at 225°, 165c at 180°. (Fig. 6), 165d ( Figure 6) at 135°, 165e (not shown) at 90°, 165f (not shown) at 45°, 165g (not shown) at 0°, and 165h (not shown) at 315°.
  • zone 15b As will be apparent from Figure 6, the clockwise-rotating segment in zone 15b which has just passed 225° will receive a gravity feed from zone 15a. This segment will then be out of register with the drain opening and will pass through 360° and all the way around to 225° before coming into register and discharging into zone 15c. (In other words, the material discharged into zone 15b is retained for about 7/8 of a full revolution of drive shaft 151.)
  • the segment of zone 15c receiving the discharge from zone 15b will have just passed 180°, i.e. just "beyond" opening 165c, and will have to pass through 360° and around to 130° before reaching the portion of floor 65c which has opening 165c.
  • the material retained in this segment will then drain out into trough 23 and zone 15d.
  • the segment of zone 15d receiving the discharge will have just passed 135° and will have to rotate about 7/8 of a revolution to reach the drain opening.
  • the sequence of events in zone 15d is repeated for zones 15e, 15f
  • the beer withdrawn from the inner bottom plate 121 will typically be a water solution" containing, for example, about 3-20% by weight of ethyl alcohol and relatively smaller amounts of acetaldehyde, acetone, acetic acid, and fusel oil.
  • the vacuum within shell 13 is continuously maintained, the feedstock continuously introduced through conduit 32, and the beer continuously withdrawn through conduit 41. Because of the effect of recirculation system 20, at least some of any live culture in apparatus 10 can be continuously recirculated to increase its hardiness and efficiency; the balance of the culture will typically become part of the "bottoms" or solid residue of the process, as explained earlier.
  • yeast/carbohydrate medium is the preferred culture or production medium
  • other cultures are suitable, particularly those which secrete a carbohydrase enzyme (zymase, glucase, cellobiase, cellulase, amylase, lactase, sucrase, or similar carbohydrases).
  • a carbohydrase enzyme zymase, glucase, cellobiase, cellulase, amylase, lactase, sucrase, or similar carbohydrases.
  • Various isomerases, hydrolases, proteases, lipases, etc. are also provided by live cultures known in the art.
  • the presently preferred metabolic product of the yeast/carbohydrate medium or culture is 100-190 U.S. proof fuel alcohol, which can be made anhydrous if desired.
  • each floor 65a, 65b, 65c, etc. is provided with a peripheral sealing member (e.g. a rubbery element) which sealingly engages the interior surface of shell 13.
  • the support structure for each floor can be provided in a manner substantially similar to that shown in Figure 2 Drawing, i.e. radial ribs 175, hangers 177, braces 171, and support ring 173.
  • This large-scale production embodiment is also advantageous when manufacturing the entire interior of tower 11 out of stainless steel (for use in making food-grade products).

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Abstract

Procede et dispositif servant a stimuler la croissance d'une culture de micro-organismes dans une serie de zones de croissance et a extraire les metabolites produits par la culture. Le procede chimique a lieu dans une serie de zones de conversion (par exemple fermentation) empilees verticalement qui sont subdivisees en segments mobiles. L'ecoulement d'une zone a l'autre est induit par la force de gravite. Une partie du milieu de production est recirculee vers une zone superieure, par exemple la zone la plus elevee, et les metabolites sont extraits des zones. Les metabolites utiles comprennent des liquides organiques tels que des alcanols issus de la fermentation des hydrates de carbone. Dans le dispositif (10) convenant specialement au procede: une tour de fermentation disposee generalement verticalement definit un espace s'etendant generalement verticalement contenant les zones arrangees verticalement (15a-15h). Une zone typique, par exemple la zone (15c) possede un plancher (65c) possedant une ouverture de drainage (165c) pour la decharge en continu par gravite de la matiere premiere partiellement convertie vers la zone inferieure suivante (15d). Chaque zone (par exemple 15c) est subdivisee en des segments mobiles en continu par des separations mobiles (157c) servant a faire avancer la matiere premiere dans la zone vers l'ouverture de drainage. Un moyen de recuperation (23) dispose sous une ouverture de drainage (165c) recupere continuellement une partie de la matiere premiere partiellement convertie et la recircule au travers d'un systeme de recirculation (20) vers la zone la plus elevee (15a). Les produits du procede sont extraits par un moyen approprie (41) en communication avec l'extremite inferieure de la tour (11).
PCT/US1981/000416 1980-03-31 1981-03-31 Procede et dispositif de production de cultures utiles et/ou de metabolites WO1981002898A1 (fr)

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US06/136,053 US4328317A (en) 1980-03-31 1980-03-31 Continuous chemical conversion or fermentation apparatus
US136054 1980-03-31
US06/136,054 US4378434A (en) 1980-03-31 1980-03-31 Process for the production of useful cultures and/or metabolites

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Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2006056838A1 (fr) * 2004-11-29 2006-06-01 Elsam Engineering A/S Hydrolyse enzymatique de biomasses ayant une teneur en matieres seches elevee
WO2014120087A1 (fr) * 2013-01-29 2014-08-07 Singapore Technologies Dynamics Pte Ltd Procédé pour la conception modulaire, la fabrication et l'assemblage de systèmes de biocolonne intégrés avec des sorties en aval multiples
WO2023214436A1 (fr) * 2022-05-05 2023-11-09 Madras Christian College Dispositif de photobioculture à plusieurs niveaux

Families Citing this family (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB9506338D0 (en) * 1995-03-28 1995-05-17 Switched Reluctance Drives Ltd Improved position encoder

Citations (4)

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Publication number Priority date Publication date Assignee Title
US409956A (en) * 1889-08-27 Malting and germinating apparatus
US2155134A (en) * 1935-12-05 1939-04-18 Deutsches Reich Reichsmonopolv Fermentation process
US3575813A (en) * 1966-12-01 1971-04-20 Nestle Sa Continuous fermentation apparatus
US3923605A (en) * 1973-10-18 1975-12-02 Tore Gedde Arrangement for biological decomposition of excrements and kitchen refuse and the like

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US409956A (en) * 1889-08-27 Malting and germinating apparatus
US2155134A (en) * 1935-12-05 1939-04-18 Deutsches Reich Reichsmonopolv Fermentation process
US3575813A (en) * 1966-12-01 1971-04-20 Nestle Sa Continuous fermentation apparatus
US3923605A (en) * 1973-10-18 1975-12-02 Tore Gedde Arrangement for biological decomposition of excrements and kitchen refuse and the like

Cited By (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2006056838A1 (fr) * 2004-11-29 2006-06-01 Elsam Engineering A/S Hydrolyse enzymatique de biomasses ayant une teneur en matieres seches elevee
US7598069B2 (en) 2004-11-29 2009-10-06 Inbicon A/S Enzymatic hydrolysis of biomasses having a high dry matter (DM) content
EP2154236A1 (fr) * 2004-11-29 2010-02-17 Inbicon A/S Hydrolyse enzymatique de biomasses ayant une teneur en matières sèches élevée
US7842490B2 (en) 2004-11-29 2010-11-30 Inbicon A/S Enzymatic hydrolysis of biomasses having a high dry matter (DM) content
EA014759B1 (ru) * 2004-11-29 2011-02-28 Инбикон А/С Ферментативный гидролиз биомасс, имеющих высокое содержание сухого вещества
WO2014120087A1 (fr) * 2013-01-29 2014-08-07 Singapore Technologies Dynamics Pte Ltd Procédé pour la conception modulaire, la fabrication et l'assemblage de systèmes de biocolonne intégrés avec des sorties en aval multiples
US10072240B2 (en) 2013-01-29 2018-09-11 Singapore Technologies Dynamics Pte Ltd Method for modular design, fabrication and assembly of integrated biocolumn systems with multiple downstream outputs
WO2023214436A1 (fr) * 2022-05-05 2023-11-09 Madras Christian College Dispositif de photobioculture à plusieurs niveaux

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