US3630848A - Continuous fermentation method and device - Google Patents

Continuous fermentation method and device Download PDF

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Publication number
US3630848A
US3630848A US786930A US3630848DA US3630848A US 3630848 A US3630848 A US 3630848A US 786930 A US786930 A US 786930A US 3630848D A US3630848D A US 3630848DA US 3630848 A US3630848 A US 3630848A
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organisms
micro
set forth
mass
circuit
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Louis Alfred August Lefrancois
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LOUIS ALFRED AUGUSTE LEFRANCOI
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LOUIS ALFRED AUGUSTE LEFRANCOI
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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
    • C12M23/00—Constructional details, e.g. recesses, hinges
    • C12M23/02—Form or structure of the vessel
    • 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
    • C12M27/18—Flow directing inserts
    • C12M27/24—Draft tube
    • 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
    • C12M29/18—External loop; Means for reintroduction of fermented biomass or liquid percolate
    • 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
    • C12M41/18—Heat exchange systems, e.g. heat jackets or outer envelopes
    • C12M41/24—Heat exchange systems, e.g. heat jackets or outer envelopes inside the vessel
    • 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
    • Y10—TECHNICAL SUBJECTS COVERED BY FORMER USPC
    • Y10S—TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10S435/00—Chemistry: molecular biology and microbiology
    • Y10S435/813—Continuous fermentation
    • 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
    • Y10—TECHNICAL SUBJECTS COVERED BY FORMER USPC
    • Y10S—TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10S435/00—Chemistry: molecular biology and microbiology
    • Y10S435/818—Aeration or oxygen transfer technique
    • 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
    • Y10—TECHNICAL SUBJECTS COVERED BY FORMER USPC
    • Y10S—TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10S435/00—Chemistry: molecular biology and microbiology
    • Y10S435/819—Fermentation vessels in series

Definitions

  • the fermentation devices having given the best results during the last few decades are those in which the batch is kept under regular internal circulation and so arranged that the circuit comprises two phases, Le. a relatively fast upward or ascending phase during which most of the elements fed thereto are absorbed by these micro-organisms, and a lower downward or descending phase in which the internal metabolisms take place in anaerobiosis or in any case in a very moderate aerobiosis, by using propitious media further containing all the elements necessary for the growth of the micro-organisms.
  • This continuity makes it possible to obtain at all points of the circuit such stable, controllable and adjustable mechanical, physical, chemical and biological conditions as can be determined or calculated beforehand.
  • This regular circulation permits transforming the aerated wort into a homogeneous fluid consisting of an intimate mixture of gaseous and liquid substances.
  • the relatively low density of the pseudoemulsion thus obtained varies according to the kind of wort to be processed.
  • a physical medium having a substantial homogeneity, as far as its weight is concerned is obtained throughout the mass or batch, its specific gravity being slightly greater at the bottom of the vessel, due mainly to the static pressure prevailing therein.
  • the upper layer cannot separate by density, provided that the rate of flow is kept at a sufficient value.
  • the wort to be treated is distributed into a film having an extremely high degree of fineness and a great surface area.
  • the feed values are so adjusted that during the ascending phase the substances will be consumed up to the predetermined and desired values, as a function of the medium available and of the constant microorganisms content.
  • the micro-organism will always perform its metabolism in a medium remaining substantially constant at each point thereof, this medium undergoing but slight and continuous variations.
  • the micro-organism is well adapted thereto and can thus grow in a medium the carbon content of which, in an assimilable form, is as low as desired.
  • the proportion of the carbon fed thereto along the circuit, preferably upstream of the insufflation zone, is as low as desired and consumed very rapidly.
  • the present invention provides a continuous process for fermenting and producing any micro-organism, wherein the working liquid mass circulates in a regular, permanent closed circuit, the mass being maintained constant by properly setting the feed and extraction rates.
  • the aforesaid circulation is obtained by blowing gas at a rate sufficient to cause on the one hand the complete batch to be transformed, after a certain revolution time, into a low-density fluid consisting of gaseous and liquid substances, and on the other hand to keep the speed impressed to said batch at a value high enough for converting this batch, when normal operative conditions and rates are attained, into a substantially homogeneous mass or, in other words, to cause the gas-to-liquid ratio by weight at any point of the vessel to remain substantially constant and to vary along the circuit according to a constant law taking due consideration for the insufflation rate and the higher gas extraction rate.
  • the circulation takes place in a complex enclosure consisting essentially of two chambers disposed externally of each other but interconnected at their upper and lower portions.
  • the circulation takes place through said chambers in succession, the entire batch being involved in the general flow.
  • the said chambers have unequal horizontal cross sections, and the whole or the greater part of the gas is blown in the vicinity of the bottom of the ascending portion of the circuit which has the smallest cross-sectional area, so that a high turbulence and a high rate of flow are imparted to said fluid mass during its upward movement.
  • the mass is subsequently transferred at a lower flow rate into the descending flow chamber having a greater cross-sectional area, whereby the ratio of the times of the ascending and descending movements of said mass considered as having a uniform mean density, ranges from 0.8 to 0.05.
  • the fluid circulation from the smaller chamber to the larger chamber creates for the entire mass of said fluid a substantially horizontal upper surface common to the upper portion of the two chambers and of the means interconnecting them.
  • the ratio of the cross-sectional areas of said two vessels ranges between 0.8 and 0.05.
  • the means provided for blowing gas into said smaller vessel is capable of impressing to the ascending phase a relatively great speed of the order of 0.5 to 2 meters per second and to produce in addition a great turbulence.
  • the communication circuit means between the two vessels are designed with a view to reduce frictional losses, the overflow threshold of the ascending stream into the descending stream lying beneath the upper mean level common to both vessels containing the moving gas-liquid fluid constituting a continuous mass without any discontinuity.
  • FIG. 1 is a diagram for explaining the principle on which this invention is based
  • FIG. 2 is a part-sectional side-elevational view showing a first form of embodiment of the invention
  • FIG. 3 is a plan view thereof
  • FIG. 4 is a view similar to FIG. 2 but showing another form of embodiment
  • FIG. 5 is another plan view of a further modified form of embodiment.
  • FIG. 1 illustrates the mode of circulation of the fluid through a single circuit comparable to that contained in an irregular tore having a vertical plane of symmetry and of which the upper portion c is only partially filled.
  • the vertical portions and b, and the lower portion d have different cross-sectional areas calculated to cause the rates of flow at each point of the circuit to correspond to those found by practical experience with one-vessel fermentation devices.
  • the principal aeration and feed take place at the base of the narrowest portion a, by means of pipe lines 1 and 2.
  • the gas is expelled from the substantially horizontal upper portion 0 connecting, in a substantially horizontal circulation, the ascending phase to the descending phase.
  • the lower portion d connects the descending phase to the ascending phase and in the example illustrated the fluid is extracted at 3 from the lower portion of the descending phase.
  • the continuous or closed circuit illustrated in FIGS. 2 and 3 may thus be constructed, which comprises a vertical vessel a in which the insufflation is carried out, a vessel b parallel to said vessel 11, which may be a simple tank disposed adjacent vessel a and may even be joined or tied thereto, with or without a slight interpenetration.
  • These vessels a and b are notched at 6 and 7 at such a level that the working mass flows from vessel a into vessel b above the base 8 of the upper portion 0, below a level 9 common to the masses to be emulsified, without making it compulsory to raise the mean mass in vessel a at a level substantially higher than that obtaining in vessel b.
  • connection c between vessel a and vessel b enables the entire mass emerging from vessel a to flow into vessel b due to the motion thus created, with the minimum loss of pressure, and the other connection d interconnects the lower portions of these two vessels.
  • the rate of flow of the mass emerging from vessel b is accelerated, if due account is taken of the paths capable of minimizing losses of pressure; it permits mounting either at its inlet at 5, or along said path, or at the outlet thereof, a helical accelerator having the optimum diameter. It also permits mounting a heat exchanger 4 deriving a beneficial effect from the already accelerated flow rates. it also provides the feed points 2 required for the fermentation process as well as the insufflation zones 1.
  • the vessels 0, b and c may be provided with suitably shaped covers for closing the complete fermentation device, these covers being also capable, if desired, to withstand a certain pressure. in this case, the gas is exhausted from the upper portion of the assembly.
  • the flow at c may take place preferably tangentially into the vessel b as shown in FIG. 3, so that a rotary motion can be maintained in said vessel b.
  • This vessel b may also be provided in its axial position with a concentric cylinder 10 closed at both ends and suitably streamlined, for the purpose of preventing a privileged flow of the descending mass; this cylinder may also be open at both ends as illustrated in FIG. 4 and receive a secondary insufflation at 11 for restoring a constant ascending flow centrally of the vessel; from the point of view of energy consumption this insufflation is of secondary importance and is not introduced compulsorily into the base of said cylinder.
  • the cross-sectional area of this cylinder will then range from about l/lOth to about l/40th of the total cross-sectional area of the vessel.
  • the general arrangement of the device also permits of bringing certain changes in the general principles set forth hereinabove in connection with homogeneity. It is assumed that the rate of flow actually controls the mean density of the emulsified fluid as well as its homogeneity which it is desired to make constant by weight. By reducing the rate of circulation or flow below a predetermined value one may obtain, as contrasted with what had been contemplated beforehand, a stable operation in which, within certain limits, there is a certain heterogeneity. in this case, as a rule, the mean specific gravity of the fluid at the top vessel b is lower than at the bottom thereof. Therefore, a kind of decantation takes place.
  • the method of this invention by virtue of its properly controlled continuity, will be so effective that it is the density variation, not the density itself, that is regular and constant in the vessel, within the limits preset for the selected rate of circulation.
  • the liquid medium itself consists of a mixture of nonmiscible liquids tending to decant more or less rapidly.
  • This feature may be advantageous; in most cases, the then lighter medium existing at the top of the vessel will have a higher micro-organisms content, this element being effective for selecting the level whereat the micro-organisms are extracted, and the fluid existing at the lower level will have more convenient hydraulic characteristics.
  • a method of continuously fermenting a working liquid and producing micro-organisms which comprises circulating said working liquid in a regular, permanent closed circuit comprising two chambers disposed externally of each other and interconnected at their upper and lower portions, said circulation taking place through said chambers in succession and the entire mass of said working liquid being involved in the general flow, said chambers having unequal effective horizontal cross sections, a chamber of smaller cross section constituting an ascending portion of said circuit, and a chamber of larger cross section constituting a descending portion of said circuit, maintaining the mass of said liquid in said circuit substantially constant by controlling the rates of feed of fluid to said circuit and extraction therefrom said circulation being obtained by blowing gas into said working liquid at a rate sufficient to cause the complete mass of working liquid to be transformed after a predetermined circulation time into a low-density fluid consisting of gaseous and liquid substances and to keep the speed of said mass at a value high enough for converting the mass into a substantially homogeneous mass to cause the gas-to-liquid ratio by weight to remain substantially constant at any selected point of
  • a device for the continuous fermentation and production of any micro-organisms consisting of two vessels having substantially vertical walls and different useful cross-sectional area, means for interconnecting said vessels at the top and bottom thereof, and other means for blowing gas into the lower portion of the smaller vessel'in order to produce the continuous circulation of the working mass, wherein the ratio of the cross-sectional areas of the two vessels ranges from 0.8 to 0.05, said gas blowing means being sufficient for imparting to the ascending phase a relatively high speed of the order of 0.5 to 2 meters/second and producing in addition a great turbulence, the circuits interconnecting the two vessels being arranged with a view to reduce frictional losses, the threshold of overflow of the ascending flow into the descending flow lying above the upper mean level common to both vessels of the gas/liquid circulating mass constituting a continuous mass without any discontinuitty.
  • Micro-organisms ermentation and production device as set forth in claim 12, wherein the outlet for the ascending flow towards the descending flow vessel is deflected with respect to the plane comprising the axes of the two vessels in order to produce an assymetric overflow adapted to maintain the rotation of the mass of fluid during its descending phase, so as to avoid preferential paths in said descending phase.
  • Microorganisms fermentation and production device as set forth in claim 12, wherein a mechanical accelerator is provided in a restricted portion of the fluid circuit in order to accelerate the rate of flow of the fluid in circulation.
  • Microorganisms fermentation and production device as set forth in claim 12, wherein a heat exchange means is installed within the circuit, in said ascending flow smaller vessel.
  • Micro-organisms fermentation and production device as set forth in claim 12, wherein a closed volume is provided in said descending flow vessel, coaxially thereto.
  • Micro-organisms fermentation and production device as set forth in claim 12, wherein a cylindrical enclosure communicating with the descending flow vessel unit is arranged centrally thereof and coaxially thereto, together with means permitting the insufflation of gas from the bottom upwards through said enclosure.
  • Micro-organisms fermentation and production device as set forth in claim 12, wherein a descending flow vessel is common and interconnected with a plurality of ascending flow vessels.
  • Micro-organisms fermentation and production device as set forth in claim 12, wherein said vessels are closed and adapted to operate under pressure.

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  • Chemical & Material Sciences (AREA)
  • Health & Medical Sciences (AREA)
  • Organic Chemistry (AREA)
  • Wood Science & Technology (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Zoology (AREA)
  • Bioinformatics & Cheminformatics (AREA)
  • Sustainable Development (AREA)
  • Microbiology (AREA)
  • Biotechnology (AREA)
  • Biochemistry (AREA)
  • General Engineering & Computer Science (AREA)
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  • Clinical Laboratory Science (AREA)
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US786930A 1967-12-29 1968-12-26 Continuous fermentation method and device Expired - Lifetime US3630848A (en)

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AT (1) AT295447B (ja)
DE (1) DE1817263A1 (ja)
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GB (1) GB1248478A (ja)

Cited By (17)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3793152A (en) * 1971-06-24 1974-02-19 Kanegafuchi Chemical Ind Method of aerobic cultivation of microbes and apparatus therefor
US3847748A (en) * 1970-07-21 1974-11-12 Ici Ltd Fermentation method and apparatus
US3880716A (en) * 1971-04-08 1975-04-29 Wilke Engelbart Process for making optimum chemical conversions and biological fermentations
US3984286A (en) * 1975-03-06 1976-10-05 Phillips Petroleum Company Apparatus and method for conducting fermentation
US3985622A (en) * 1975-01-30 1976-10-12 Phillips Petroleum Company Method and apparatus for conducting fermentation
US4001090A (en) * 1974-05-28 1977-01-04 Societe D'assistance Technique Pour Produits Nestle S.A. Process and apparatus for the culture of microorganisms
US4036699A (en) * 1976-02-02 1977-07-19 Phillips Petroleum Company Fermentation apparatus and method
US4126517A (en) * 1974-09-19 1978-11-21 Giovanola Freres Sa Method of converting liquid micro-biological substrate and apparatus for carrying out the method
JPS5451998U (ja) * 1977-09-19 1979-04-10
US4230806A (en) * 1977-06-07 1980-10-28 Mitsui Engineering & Shipbuilding Co., Ltd. Process for the production of microbial protein and lipid from vegetable carbohydrates by culture of microbes
US4545945A (en) * 1980-12-13 1985-10-08 Hoechst Aktiengesellschaft Process for improving the gas distribution in air-lift loop reactors
US4780415A (en) * 1981-07-29 1988-10-25 Gilbert Ducellier Method of degrading organic products, by-products and scraps in an anaerobic medium
US4935348A (en) * 1984-11-15 1990-06-19 Cooperatieve Vereniging Suiker Unie U.A. Method for the carrying out of a microbiological or enzymatic process
US4992370A (en) * 1982-04-26 1991-02-12 Nestec S.A. Process for the production of alcohol
US5342781A (en) * 1993-07-15 1994-08-30 Su Wei Wen W External-loop perfusion air-lift bioreactor
US20120216680A1 (en) * 2011-02-25 2012-08-30 Southern Company Dispersed Bubble Reactor For Enhanced Gas-Liquid-Solids Contact And Mass Transfer
CN110964625A (zh) * 2019-12-31 2020-04-07 浙江卓尚环保能源有限公司 一种湿式厌氧发酵搅拌与换热方法及湿式厌氧发酵系统

Families Citing this family (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR2209837A1 (en) * 1972-12-13 1974-07-05 Baranovsky Vladimir Tubular appts. for microorganism growing - medium being moved by propel-lers through froth dampers and heat exchangers
CH578618A5 (ja) * 1973-08-30 1976-08-13 Mueller Hans Maennedorf
DE2511038C2 (de) * 1974-03-18 1982-04-01 Hans Dr.-Ing. Männedorf Müller Vorrichtung zum Kühlen und Belüften der Substratflüssigkeit in Reaktoren für mikrobiologische Stoffumsetzungen.
FR2404045A1 (fr) * 1977-09-23 1979-04-20 Proizv Ob Gid Appareil destine a la culture de micro-organismes
BG32191A1 (en) * 1980-07-11 1982-06-15 Kostadinov Method and apparatus for cultivation of aerobic microorganisms

Citations (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2983652A (en) * 1958-02-21 1961-05-09 Bertrams Ag Hch Fermenter

Patent Citations (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2983652A (en) * 1958-02-21 1961-05-09 Bertrams Ag Hch Fermenter

Cited By (20)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3847748A (en) * 1970-07-21 1974-11-12 Ici Ltd Fermentation method and apparatus
US3880716A (en) * 1971-04-08 1975-04-29 Wilke Engelbart Process for making optimum chemical conversions and biological fermentations
US3793152A (en) * 1971-06-24 1974-02-19 Kanegafuchi Chemical Ind Method of aerobic cultivation of microbes and apparatus therefor
US4001090A (en) * 1974-05-28 1977-01-04 Societe D'assistance Technique Pour Produits Nestle S.A. Process and apparatus for the culture of microorganisms
US4126517A (en) * 1974-09-19 1978-11-21 Giovanola Freres Sa Method of converting liquid micro-biological substrate and apparatus for carrying out the method
US3985622A (en) * 1975-01-30 1976-10-12 Phillips Petroleum Company Method and apparatus for conducting fermentation
US3984286A (en) * 1975-03-06 1976-10-05 Phillips Petroleum Company Apparatus and method for conducting fermentation
US4036699A (en) * 1976-02-02 1977-07-19 Phillips Petroleum Company Fermentation apparatus and method
US4230806A (en) * 1977-06-07 1980-10-28 Mitsui Engineering & Shipbuilding Co., Ltd. Process for the production of microbial protein and lipid from vegetable carbohydrates by culture of microbes
JPS5621272Y2 (ja) * 1977-09-19 1981-05-20
JPS5451998U (ja) * 1977-09-19 1979-04-10
US4545945A (en) * 1980-12-13 1985-10-08 Hoechst Aktiengesellschaft Process for improving the gas distribution in air-lift loop reactors
US4780415A (en) * 1981-07-29 1988-10-25 Gilbert Ducellier Method of degrading organic products, by-products and scraps in an anaerobic medium
US4992370A (en) * 1982-04-26 1991-02-12 Nestec S.A. Process for the production of alcohol
US4935348A (en) * 1984-11-15 1990-06-19 Cooperatieve Vereniging Suiker Unie U.A. Method for the carrying out of a microbiological or enzymatic process
US5342781A (en) * 1993-07-15 1994-08-30 Su Wei Wen W External-loop perfusion air-lift bioreactor
US20120216680A1 (en) * 2011-02-25 2012-08-30 Southern Company Dispersed Bubble Reactor For Enhanced Gas-Liquid-Solids Contact And Mass Transfer
WO2012121886A1 (en) * 2011-02-25 2012-09-13 Southern Company Dispersed bubble reactor for enhanced gas-liquid-solids contact and mass transfer
US9242220B2 (en) * 2011-02-25 2016-01-26 Southern Company Dispersed bubble reactor for enhanced gas-liquid-solids contact and mass transfer
CN110964625A (zh) * 2019-12-31 2020-04-07 浙江卓尚环保能源有限公司 一种湿式厌氧发酵搅拌与换热方法及湿式厌氧发酵系统

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GB1248478A (en) 1971-10-06
FR1556397A (ja) 1969-02-07
DE1817263A1 (de) 1969-07-17
AT295447B (de) 1972-01-10

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