WO1994001530A1 - Process for modulating the concentration of dissolved gases in liquid media - Google Patents
Process for modulating the concentration of dissolved gases in liquid media Download PDFInfo
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- WO1994001530A1 WO1994001530A1 PCT/GB1993/001392 GB9301392W WO9401530A1 WO 1994001530 A1 WO1994001530 A1 WO 1994001530A1 GB 9301392 W GB9301392 W GB 9301392W WO 9401530 A1 WO9401530 A1 WO 9401530A1
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- organic fluid
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- organic
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- C—CHEMISTRY; METALLURGY
- C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
- C12N—MICROORGANISMS OR ENZYMES; COMPOSITIONS THEREOF; PROPAGATING, PRESERVING, OR MAINTAINING MICROORGANISMS; MUTATION OR GENETIC ENGINEERING; CULTURE MEDIA
- C12N5/00—Undifferentiated human, animal or plant cells, e.g. cell lines; Tissues; Cultivation or maintenance thereof; Culture media therefor
- C12N5/0018—Culture media for cell or tissue culture
- C12N5/0025—Culture media for plant cell or plant tissue culture
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/02—Aerobic processes
- C02F3/025—Biological purification using sources of oxygen other than air, oxygen or ozone
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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
- C12M41/00—Means for regulation, monitoring, measurement or control, e.g. flow regulation
- C12M41/12—Means for regulation, monitoring, measurement or control, e.g. flow regulation of temperature
- C12M41/14—Incubators; Climatic chambers
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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
- C12M41/00—Means for regulation, monitoring, measurement or control, e.g. flow regulation
- C12M41/30—Means for regulation, monitoring, measurement or control, e.g. flow regulation of concentration
- C12M41/32—Means for regulation, monitoring, measurement or control, e.g. flow regulation of concentration of substances in solution
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- C—CHEMISTRY; METALLURGY
- C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
- C12N—MICROORGANISMS OR ENZYMES; COMPOSITIONS THEREOF; PROPAGATING, PRESERVING, OR MAINTAINING MICROORGANISMS; MUTATION OR GENETIC ENGINEERING; CULTURE MEDIA
- C12N2500/00—Specific components of cell culture medium
- C12N2500/02—Atmosphere, e.g. low oxygen conditions
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
- Y02W10/00—Technologies for wastewater treatment
- Y02W10/10—Biological treatment of water, waste water, or sewage
Definitions
- This invention relates to processes for modulating the concentration of dissolved gases in liquid media, especially liquid media which are associated with biological materials e.g. aqueous culture media for cells, and waste products such as polluted water and sewage which are characterised by the presence of microoganisms.
- biological materials e.g. aqueous culture media for cells, and waste products such as polluted water and sewage which are characterised by the presence of microoganisms.
- the present invention overcomes such problems by utilising a liquid transfer medium to effect the desired modulation and selecting physical properties of the liquid transfer medium and the manner in which the transfer medium is manipulated to facilitate the transfer of gases.
- this invention relates to processes for culturing cells in an aqueous growth medium.
- the invention particularly relates to procedures wherein an organic liquid which is immiscible with water is used for promoting transfer of gas to or from the growth medium.
- process of culturing cells is intended to encompass any procedure wherein prokaryotic or eukaryotic cells are grown or maintained in ⁇ itvo. Such procedures include the growth, or maintenance under steady state conditions, of unicellular organisms or organisms in which the cells grow in the form of mycelia. They also include the growth, or maintenance under steady state conditions, of cells derived from multicellular organisms. Furthermore, the procedures encompassed by the term “process of culturing cells” include procedures carried out under both aerobic and anaerobic conditions suitable for maintaining cells in a viable state as well as procedures where cells enter the retardation or stationary phase, become senescent and even eventually die.
- the processes of the invention thus includes procedures wherein cells are grown under aerobic or anaerobic conditions wherein cell multiplication occurs, with cell numbers and/or cell mass increasing.
- the process also includes procedures where cells are maintained under conditions where substantially no increase in cell numbers and/or mass occurs.
- the latter procedures include processes wherein cells are being cultured for the purpose of producing products of primary or secondary metabolism.
- oxygen-containing gas for example air
- Additional measures include the use of agitation, for example by providing agitators, impellors and associated structures such as baffles within the culture vessel in order to enhance the contacting of the culture medium with the oxygen containing gas.
- Other measures include the use of shaken vessels and in the case of cultured animal cells, the use of roller bottles in which a moving thin film of culture medium is continuously renewed.
- Achieving a high rate of gas transfer is also important in circumstances where it is desired to remove gaseous products of metabolism from culture media.
- products of metabolism would normally include carbon dioxide.
- Other gaseous products of anaerobic metabolism include hydrogen and hydrogen sulfide.
- it is customary to use a stream of inert gas in order to scrub these by-products from the culture medium.
- PFCs have been used to transfer oxygen to aqueous culture media by spraying oxygenated PFC liquids into or onto cell cultures.
- the droplets of oxygenated PFC being dense, settle to the bottom of the fermentor vessel, transferring oxygen to the medium as they fall.
- the PFC accumulates at the bottom of the vessel from where it can be recovered, reoxygenated and pumped back into the top as a spray, thus continuing the cycle.
- the coarse droplet size and the relatively short residence time of the droplets in situ severely limits the rate and efficiency with which oxygen can be transferred to the culture medium.
- a process for modulating the concentration of a dissolved gas in a liquid medium wherein transfer of gas to or ' from the medium is promoted by use of an organic fluid, which when in the liquid state is immiscible with the liquid medium and is capable of dissolving the gas, characterised in that the organic fluid is transferred between zones operated at different temperatures in which the fluid exists respectively in the liquid and the gaseous states, gas dissolves in the organic fluid in a zone where the organic fluid is in the liquid state and separation of gas from the organic fluid takes place in a separate zone.
- separation may take place in a zone where the organic fluid is converted from the liquid to the gaseous state, in which case the gas may be evolved as the organic fluid passes from the liquid to the gaseous state.
- the invention may more specifically be defined in terms of a process for transferring gas to or from a liquid medium, which comprises contacting the medium with a transfer fluid which when in the liquid state is immiscible with the liquid medium and is capable of dissolving the gas, characterised in that the transfer fluid is transferred between zones operated at different temperatures in which the transfer fluid exists respectively in the liquid and the gaseous states, gas dissolves in the transfer fluid in a zone where the transfer fluid is in the liquid state and separation of gas from the transfer fluid takes place in a separate zone.
- a process for modulating the concentration of a dissolved gas in a liquid medium wherein transfer of gas to or from the medium is promoted by use of an organic fluid, which when in the liquid state is immiscible with the liquid medium and is capable of dissolving the gas, characterised in that the organic compound is transferred between zones operated at different temperatures in which the compound exists respectively in the liquid and the gaseous states, whereby gas dissolves in the organic fluid in a zone where the organic fluid is in the liquid state, and is evolved when the organic fluid passes from the liquid to the gaseous state.
- gas may be transferred directly from the organic fluid to the liquid medium, or more preferably, the organic fluid is converted from the liquid to the gaseous state as it contacts the liquid medium and the evolved gas is then made available for dissolution in the liquid medium.
- the invention further provides a process of for modulating the concentration of a dissolved gas in a liquid medium wherein transfer of gas to or from the medium is promoted by use of an organic fluid, which when in the liquid state is immiscible with the liquid medium and is capable of dissolving the gas, characterised in that the organic compound is transferred between zones operated at different temperatures in which the compound exists respectively in the liquid and the gaseous states, whereby gas dissolves in the organic fluid in a zone where the organic fluid is in the liquid state, and the organic fluid undergoes a change of state between the liquid and gaseous states while in contact with the liquid medium.
- organic fluid in the liquid state and containing dissolved gas may be contacted with the liquid medium, and dissolved gas transferred to the liquid medium without the organic liquid being converted to the gaseous state.
- dissolved gas for example oxygen
- the organic fluid in the liquid state may be contacted with the liquid medium, the organic fluid converted to the gasous state while in contact with the liquid medium and organic fluid in the gaseous state and liquid medium then separated from one another.
- the evolved organic compound in the gaseous state is preferably condensed, then used to dissolve a further quantity of gas and recycled to release dissolved gas to the liquid medium.
- step (ii) solution from step (i) is transferred to a second zone operated at a temperature above the boiling point of the organic liquid wherein the organic fluid passes from the liquid to the gaseous state with evolution of gas,
- step (iii) gas evolved in step (ii) contacts the liquid medium and dissolves therein,
- organic fluid in the liquid state from step (iv) is utilised to dissolve gas in step (i) .
- organic fluid in the liquid state is contacted with the liquid medium and dissolved gas contained in the liquid growth medium is transferred to the organic liquid.
- the organic liquid containing the dissolved gas may then be separated from the liquid medium and if desired, recycled for reuse after stripping dissolved gas therefrom.
- organic fluid in the gaseous state may be contacted with the liquid medium, the organic fluid converted to the liquid state while in contact with the liquid medium and organic fluid in the liquid state and liquid medium may then be separated from one another.
- organic fluid in the liquid state and containing dissolved gas may be separated from the liquid medium and transferred to a separate zone where the organic fluid is converted to the gaseous state, and dissolved gas is evolved and separated from the organic fluid.
- the liquid medium would be at a temperature below the boiling point of the organic fluid.
- a process for modulating the concentration of a dissolved gas in a liquid medium wherein removal of gas from the medium is promoted by use of an organic fluid, which when in the liquid state is immiscible with the liquid medium and is capable of dissolving the gas characterised in that:
- step (i) the organic compound in the liquid state is contacted with the liquid medium in a first zone operated at a temperature below the boiling point of the organic compound whereby gas dissolved in the liquid medium is transferred to the organic liquid, to form a solution of the gas in the organic liquid, (ii) solution from step (i) is transferred to a second zone operated at a temperature above the boiling point of the organic liquid wherein the organic fluid passes from the liquid to the gaseous state with evolution of gas,
- step (iii) gas evolved in step (iii) is separated from the organic fluid
- step (v) organic fluid in the liquid state from step (iv) is in step (i) .
- the process of the invention is especially applicable to modulating the concentration of gases in aqueous media, especially aqueous media which are intended for use as aqueous growth media for biological materials.
- the process of the invention may be used to modulate the concentration of dissolved gases in a step of one of the following biological procedures:
- the present invention when directed to the culturing of cells, provides a process of culturing cells in an aqueous growth medium wherein transfer of gas to or from the medium is promoted by use of an organic fluid, which when in the liquid state is immiscible with the aqueous growth medium and is capable of dissolving the gas, characterised in that the organic fluid is transferred between zones operated at different temperatures in which the fluid exists respectively in the liquid and the gaseous states, gas dissolves in the organic fluid in a zone where the organic fluid is in the liquid state and separation of gas from the organic fluid takes place in a separate zone.
- separation may take place in a zone where the organic fluid is converted from the liquid to the gaseous state, in which case the gas may be evolved as the organic fluid passes from the liquid to the gaseous state.
- a process of culturing cells in an aqueous growth medium wherein transfer of gas to or from the medium is promoted by use of an organic fluid, which when in the liquid state is immiscible with the aqueous growth medium and is capable of dissolving the gas, characterised in that the organic compound is transferred between zones operated at different temperatures in which the compound exists respectively in the liquid and the gaseous states ' , whereby gas dissolves in the organic fluid in a zone where the organic fluid is in the liquid state, and is evolved when the organic fluid passes from the liquid to the gaseous state.
- gas may be transferred directly from the organic fluid to the aqueous growth medium, or more preferably, the organic fluid is converted from the liquid to the gaseous state as it contacts the aqueous growth medium and the evolved gas is then made available for dissolution in the aqueous growth medium.
- the invention further provides a process of culturing cells in an aqueous growth medium wherein transfer of gas to or from the medium is promoted by use of an organic fluid, which when in the liquid state is immiscible with the aqueous growth medium and is capable of dissolving the gas, characterised in that the organic compound is transferred between zones operated at different temperatures in which the compound exists respectively in the liquid and the gaseous states, whereby gas dissolves in the organic fluid in a zone where the organic fluid is in the liquid state, and the organic fluid undergoes a change of state between the liquid and gaseous states while in contact with the aqueous growth medium.
- organic fluid in the liquid state and containing dissolved gas may be contacted with the aqueous growth medium, and dissolved gas transferred to the aqueous growth medium without the organic liquid being converted to the gaseous state.
- dissolved gas for example oxygen
- the organic fluid in the liquid state may be contacted with the aqueous growth medium, the organic fluid converted to the gasous state while in contact with the aqueous growth medium and organic fluid in the gaseous state and aqueous growth medium then separated from one another.
- the evolved organic compound in the gaseous state is preferably condensed, then used to dissolve a further quantity of gas and recycled to release dissolved gas to the aqueous growth medium.
- step (ii) solution from step (i) is transferred to a second zone operated at a temperature above the boiling point of the organic liquid wherein the organic 1 fluid passes from the liquid to the gaseous state with evolution of gas,
- step (iii) gas evolved in step (ii) contacts the aqueous growth medium and dissolves therein,
- step (v) organic fluid in the liquid state from step (iv) is utilised to dissolve gas in step (i).
- organic fluid in the liquid state is contacted with the aqueous growth medium and dissolved gas contained in the aqueous growth medium is transferred to the organic liquid.
- the organic liquid containing the dissolved gas may then be separated from the aqueous growth medium and if desired, recycled for reuse after stripping dissolved gas therefrom.
- organic fluid in the gaseous state may be contacted with the aqueous growth medium, the organic fluid converted to the liquid state while in contact with the aqueous growth medium and organic fluid in the liquid state and aqueous growth medium may then be separated from one another.
- organic fluid in the liquid state and containing dissolved gas may be separated from the aqueous growth medium and transferred to a separate zone where the organic fluid is converted to the gaseous state, and dissolved gas is evolved and separated from the organic fluid.
- the aqueous growth medium would be at a temperature below the boiling point of the organic fluid.
- a process of culturing cells in an aqueous growth medium wherein removal of gas from the medium is promoted by use of an organic fluid, which when in the liquid state is immiscible with the aqueous growth medium and is capable of dissolving the gas characterised in that:
- the organic compound in the liquid state is contacted with the aqueous growth medium in a first zone operated at a temperature below the boiling point of the organic compound whereby gas dissolved in the aqueous growth medium is transferred to the organic liquid, to form a solution of the gas in the organic liquid,
- step (ii) solution from step (i) is transferred to a second zone operated at a temperature above the boiling point of the organic liquid wherein the organic fluid passes from the liquid to the gaseous state with evolution of gas,
- step (iii) gas evolved in step (iii) is separated from the organic fluid
- organic fluid in the liquid state from step (iv) is in step (i) .
- the organic fluid used in the method of the invention may be a pure compound or a mixture of compounds.
- PFC is used as an abbreviation for PFC
- perfluorochemical includes, but is not restricted to perfluorocarbons i.e. compounds of the formulae:
- n is a positive integer from 1 to 30, preferably from 4 to 20.
- x may be minus 2 (as in the first formula, zero (as in the second formula) or a positive even integer from 2 to 20, preferably from 2 to 15 and most preferably from 2 to 10.
- PFC further includes compounds containing atoms in addition to carbon or fluorine, including atoms of nitrogen, oxygen and sulfur.
- Such compounds can be represented by the general formulae n (2n-x+m) (II)
- n and x are as defined above and m is from 1 to 6, preferably from 1 to 3 and most preferably 1.
- Specific examples include perfluoroalkanes, perfluorocycloalkanes and perfluoroalkyltetrahydrofurans.
- Figure 1 illustrates apparatus according to the invention adapted for growth of cells under aerobic conditions
- Figure 2 illustrates apparatus according to the invention adapted for growth of cells under anaerobic conditions.
- fermentation system 110 consists of fermentation vessel 112 connected to a system for circulating PFCs.
- the circulation system includes a condensor 114 connected via conduit 116 to the head space 118 of fermentation vessel 112.
- the upper portion of the condensor is provided with a cooling coil 120 for condensing PFC vapour entering the condensor via conduit 116.
- the lower part of the condensor is fitted with a contacting device 122 for effecting gas exchange between oxygen containing gas introduced via line 124, and the PFC liquid resulting from condensation of the PFC vapour.
- Any conventional gas/liquid contacting device may be used for effecting gas exchange.
- an oxygen-containing gas e.g. air
- condensor 120 and the associated contacting device 122 can also be used for removing carbon dioxide from the off-gases leaving fermentor 112 via conduit 116.
- the outlet of the condensor is connected via conduit 126, pump 128 and conduit 130 to the sump 132 of the fermentation vessel 112.
- a resevoir 13 connects into line 130 via metering valve 136 for introducing make-up quantities of PFC into the system.
- the fermentation vessel 112 is fitted with customary internal fittings including impellor 138 and temperature control coils 140.
- a charge of suitably sterilised culture medium is introduced into the fermentation vessel and innoculated with a starter culture of the cells to be grown.
- the temperature of the culture medium is maintained at a temperature suitable for growth by circulating heat exchange medium through the heat exchange coils l4 ⁇ .
- the circulatory system is charged with a selected PFC fluid which has a boiling point which is below the temperature of the aqueous growth medium in the fermentation vessel.
- the temperature of the condensor 114 and the associated apparatus downstream thereof are maintained at a temperature below the boiling point of the PFC fluid so as to maintain it in the liquid state at least until it enters or is about to enter the fermentation vessel 112.
- the organic fluid is saturated with oxygen in device 122 and introduced in the liquid state into the sump of fermentation vessel 112 via conduit 126 and pump 128.
- the PFC boils in the sump of the fermentation vessel and the oxygen gas dissolved therein is evolved. Bubbles 142 of PFC in the gaseous state and bubbles of evolved oxygen gas rise through the fermentation vessel and the oxygen is dissolved in the aqueous growth medium.
- Fermentation system 110 described above in connection with Figure 1 of the drawing is especially adapted for growing cells ⁇ under aerobic conditions utilising a water immiscible organic fluid as a carrier gas for introducing oxygen into the fermentation vessel.
- a water immiscible organic fluid as a carrier gas for introducing oxygen into the fermentation vessel.
- the PFC fluid used to transport oxygen would be selected to have a boiling point below 37 * C.
- the organic fluid would have a boiling point within the range of 20-37 ⁇ C.
- the temperature of the organic fluid when introduced into the sump 132 of the fermentation vessel in the liquid state at a temperature of approximately 2 ⁇ C, the temperature of the organic fluid would increase until it boiled within the fermentation vessel, releasing its charge of oxygen which would dissolve in the aqueous fermentation medium and become available to the animal cells being grown.
- the process of the invention is additionally applicable to the growth of cells under anaerobic conditions, in which case the water immiscible organic fluid would normally be used to remove gaseous products of metabolism from the aqueous growth medium.
- fermentation system 210 consists of fermentation vessel 212 connected to a system for circulating PFCs.
- the circulation system includes a pump 228 connected via line 230 to the sump 232 of vessel 212 and leading via conduit 226 to an evaporator 214.
- a reservoir 234 connects into line 230 via metering valve 236 for introducing make-up quantities of PFC into the system.
- the lower part of evaporator 214 is provided with a heating coil 220 for evaporating PFC introduced into the evaporator via line 226.
- the upper portion of the evaporator 214 is fitted with a contacting device 222 for scrubbing PFC vapour evaporated in the lower part of the evaporator with a scrubbing liquid introduced via line 224.
- the outlet of the evaporator is connected via conduit 216, to the head space of the fermentation vessel 212.
- the fermentation vessel 212 is fitted with customary internal fittings including impellor 238 and temperature control coils 240.
- a charge of suitably sterilised culture medium is introduced into the fermentation vessel and innoculated with a starter culture of the cells to be grown.
- the temperature of the culture medium is maintained at a temperature suitable for growth by circulating heat exchange medium through the heat exchange coils 240.
- the circulatory system is charged with a selected PFC fluid which has a boiling point which is above the temperature of the aqueous growth medium in the fermentation vessel.
- the temperature of the evaporator 214 and line 216 are maintained at a temperature above the boiling point of the PFC fluid so as to maintain it in the gaseous state at least until it enters or is about to enter the fermentation vessel 212.
- the organic fluid is evaporated in evaporator 214 and after being scrubbed in contacting device 222 the PFC vapours are led via conduit 216 to the head space of the fermentor.
- the PFC vapour condenses within the fermentor and droplets of condensed PFC fall downwardly within the fermentor as a "rain" 242 of condensed liquid PFC.
- the condensed PFC scrubs the aqueous growth medium, and gaseous products of metabolism dissolve in the condensed PFC.
- the PFC containing the dissolved products of metabolism accumulate in the sump 232 of the fermentation vessel, where they are transferred via conduit 230 and pump 238 to evaporator 232.
- PFC vapours leaving evaporator 214 via condiut 216 are cooled and condensed to form PFC liquid which is used to scrub gaseous products of metabolism from the aqueous fermentation medium as described above.
- the condensation of PFC vapour either takes place outside of fermentation vessel 218 in a separator condensor (not shown) or the vapour can be lead directly into fermentation vessel 218 where its temperature is reduced to below its boiling point and condensation takes place.
- the apparatus illustrated in Figure 2 can be used for growing thermophilic microorganisms under anaerobic conditions.
- the apparatus in Figure 2 may be used to grow the extreme thermophile Pyrococcus fu ⁇ iosus.
- P furioxsus is a strictly anaerobic heterotroph and grows by a fermentative-type metabolism. Both simple and complex carbohydrates can be utilised with the production of carbon dioxide hydrogen. If elemental sulphur (S_) is present in the growth medium as the electron acceptor, H_S is produced in addition to C0_ and H_S. Effective growth of such anaerobic heterotrophs depends upon the removal of gaseous products of metabolism, such as H_ and H_S from the culture medium.
- S_ elemental sulphur
- the aqueous culture medium When culturing such extreme thermophiles, the aqueous culture medium would normally be maintained at a high temperture, for example, approximately 0 ⁇ C and hydrogen or hydrogen sulphide would tend to accumulate in the culture medium as a by-product of metabolism.
- Non-cell-disrupting aeration of the culture can be improved by utilising the well established oxygen carrying capacity of PFC liquids.
- Rate of transport of the 0_ to the culture medium can be increased by rapid boiling-off of the PFC liquid allowing rapid recycling of low volumes of PFC liquid with corresponding cost savings.
- Varying the rate of reintroduction of recondensed PFC liquid to the fermentor can give fine control over gas exchange rates (e.g.aeration) throughout the fermentation.
- the whole system (fermentor and PFC liquid recondenser loop) can be pre-sterilised, either chemically or by steam) .
- bio-fuels from biomass high efficiency and safe collection of biogas, etc.
- a further advantage of the use of PFCs in accordance with the invention results from the fact that PFC fluids exhibit extremely low heats of vaporisation and condensation, e.g. the latent heat of vaporisation (at b.p.) of a typical PFC (FC87 b.p. 30°C) is only 24 cals/g and for FC 77 is 20 cals/g (c.f. water at 540 cals/g).
- thermophilic fermentation as carried out in the apparatus depicted in Figure 2, the vessel-heating effect of introducing FC 77 PFC vapour (b.p. 110°C) at 120"C and condensing it (at 10% volume fraction) down to a vessel running temp of, for instance, 0 ⁇ C represents a vessel temp, rise of only 4°C (energy requirement of 6,559 kcals).
- Animal cell cultures running in batch mode, start at 2-3 x 10 5 cells/ml, doubling daily to 2 million/ml by day 4 and decline after day 7• Perfusion cultures operate at 50-200 x 10 cells/ml and typically last 40-80 days.
- thermophilic systems many of the extremely thermophilic (growth optimum at 90 ⁇ C) Archeobactevia are sulphate metabolisers and many require the provision of elemental sulphur in the growth medium which generally results in the formation of H_S which is both toxic and corrosive to equipment. Continuous removal of this gas from the culture medium is currently very difficult.
- Pyrococcus furiosus which has been studied for the production of a range of enzymes including proteases, amylases, pullulanase and ⁇ -glucosidase. All of the enzymes are of significant commercial importance and improving methods of obtaining them in commercially viable quantities from these bacteria is of great interest.
- the organism has an optimal growth temperature of 95"C and is able to grow in the absence of sulphur but it produces hydrogen which becomes toxic to the organism and limits growth yield and the resulting low cell yields render industrial scale-up of such fermentation commercially non-viable.
- the current optimum method for removal of hydrogen is to flush the vessel with an anaerobic (e.g. Argon) gas.
- the method of the invention is not only applicable to the transfer to aqueous growth media of gases which play a major role in metabolism (e.g. oxygen in the case of aerobic fermentations) , but it can also be used to establish or maintain any desired or necessary gas or gas mixture at an appropriate concentration within the medium (e.g. to exert fine control of microaerophilic conditions) .
- the invention may also be applied to the "harvesting" of gases produced by fermentations, e.g. "biogas”, CH j ,, H_, NH,, H_S, S0_, CO- etc.
- gases produced by fermentations e.g. "biogas”, CH j ,, H_, NH,, H_S, S0_, CO- etc.
- Other areas of application include photosynthetic cell growth.
- microbial including fungal and yeast
- the PFCs could then be used to improve the process by either adding specific gases to aid the process of remove gases (of any type) that might otherwise inhibit the process.
- the “material/substance” could then come from different sources:
- biological e.g. sewage waste, foodstuffs (and wastes derived from foodstuff manufacture), etc.
- chemical both inorganic (e.g. sequestration of (heavy) metals in biomining, metal containing wastes, nuclear materials, etc.) and organic (chemicals/polymers used in pharmaceuticals, petrochemicals, pesticide manufacture, dyestuffs, foodstuffs, xenobiotics, etc.. )
Abstract
Description
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Priority Applications (5)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
JP50308693A JPH08501927A (en) | 1992-07-07 | 1993-07-02 | Method for adjusting concentration of gas dissolved in liquid medium |
GB9500282A GB2284216B (en) | 1992-07-07 | 1993-07-02 | Process for modulating the concentration of dissolved gases in liquid media |
CA 2139762 CA2139762A1 (en) | 1992-07-07 | 1993-07-02 | Process for modulating the concentration of dissolved gases in liquid media |
EP19930914869 EP0650519A1 (en) | 1992-07-07 | 1993-07-02 | Process for modulating the concentration of dissolved gases in liquid media |
AU45087/93A AU4508793A (en) | 1992-07-07 | 1993-07-02 | Process for modulating the concentration of dissolved gases in liquid media |
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
GB9214379.1 | 1992-07-07 | ||
GB9214379A GB9214379D0 (en) | 1992-07-07 | 1992-07-07 | Process for culturing cells |
Publications (1)
Publication Number | Publication Date |
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WO1994001530A1 true WO1994001530A1 (en) | 1994-01-20 |
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Application Number | Title | Priority Date | Filing Date |
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PCT/GB1993/001392 WO1994001530A1 (en) | 1992-07-07 | 1993-07-02 | Process for modulating the concentration of dissolved gases in liquid media |
Country Status (6)
Country | Link |
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EP (1) | EP0650519A1 (en) |
JP (1) | JPH08501927A (en) |
AU (1) | AU4508793A (en) |
CA (1) | CA2139762A1 (en) |
GB (2) | GB9214379D0 (en) |
WO (1) | WO1994001530A1 (en) |
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WO2002022775A1 (en) * | 2000-09-13 | 2002-03-21 | Csir | Bio-reactor device |
WO2010083956A3 (en) * | 2009-01-23 | 2011-03-03 | Bayer Technology Services Gmbh | Gassing system |
US9127246B2 (en) | 2010-02-22 | 2015-09-08 | Life Technologies Corporation | Methods for condensing a humid gas |
US9457306B2 (en) | 2014-10-07 | 2016-10-04 | Life Technologies Corporation | Regulated vacuum off-gassing of gas filter for fluid processing system and related methods |
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US10688429B2 (en) | 2014-03-21 | 2020-06-23 | Life Technologies Corporation | Gas filter systems for fluid processing systems |
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Citations (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
FR2177051A1 (en) * | 1972-03-23 | 1973-11-02 | Tanabe Seiyaku Co | |
US4177246A (en) * | 1978-02-24 | 1979-12-04 | Stoddard Xerxes T | Wet oxidation of materials |
EP0164813A2 (en) * | 1984-06-14 | 1985-12-18 | Teijin Limited | Method of cultivating animal or plant cells |
-
1992
- 1992-07-07 GB GB9214379A patent/GB9214379D0/en active Pending
-
1993
- 1993-07-02 CA CA 2139762 patent/CA2139762A1/en not_active Abandoned
- 1993-07-02 EP EP19930914869 patent/EP0650519A1/en not_active Withdrawn
- 1993-07-02 GB GB9500282A patent/GB2284216B/en not_active Expired - Fee Related
- 1993-07-02 JP JP50308693A patent/JPH08501927A/en active Pending
- 1993-07-02 WO PCT/GB1993/001392 patent/WO1994001530A1/en not_active Application Discontinuation
- 1993-07-02 AU AU45087/93A patent/AU4508793A/en not_active Abandoned
Patent Citations (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
FR2177051A1 (en) * | 1972-03-23 | 1973-11-02 | Tanabe Seiyaku Co | |
US4177246A (en) * | 1978-02-24 | 1979-12-04 | Stoddard Xerxes T | Wet oxidation of materials |
EP0164813A2 (en) * | 1984-06-14 | 1985-12-18 | Teijin Limited | Method of cultivating animal or plant cells |
Non-Patent Citations (1)
Title |
---|
J.L ROLS & G. GOMA: "Enhancement of oxygen transfer rates in fermentation using oxygen-vectors.", BIOTECHNOLOGY ADVANCES, vol. 7, no. 1, 1989, OXFORD, G.B., pages 1 - 14, XP023926974, DOI: doi:10.1016/0734-9750(89)90900-2 * |
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Also Published As
Publication number | Publication date |
---|---|
AU4508793A (en) | 1994-01-31 |
GB9214379D0 (en) | 1992-08-19 |
GB2284216B (en) | 1996-04-17 |
GB9500282D0 (en) | 1995-03-08 |
JPH08501927A (en) | 1996-03-05 |
CA2139762A1 (en) | 1994-01-20 |
GB2284216A (en) | 1995-05-31 |
EP0650519A1 (en) | 1995-05-03 |
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