• 专利附录
  • 专利说明
  • 权利要求
  • 类似技术
  • 同族专利
  • 引用文献
  • 法律状态
  • 优先权
    • 专利摘要:
    1417486 Aerating and circulating liquids IMPERIAL CHEMICAL INDUSTRIES Ltd 3 May 1974 [16 May 1973] 23330/73 Addition to 1353008 Heading B1C [Also in Divisions Cl and C6] Chemical and biochemical reactions involving contacting a liquid and gas, such as the production of aqueous solutions of copper sulphate from copper sulphide-containing mineral ores suspended in aerated aqueous medium, the production of single cell protein by growing micro-organisms upon hydrocarbon or methanolic substrates, or the microbiological production of citric acid, amino acids e.g. lysine, glutamic acid and methionine, enzymes e.g. glucose isomerase and antibiotics e.g. penicillin, are carried out in circulatory apparatus consisting essentially of a riser 1, Fig. 1, a downcomer 5, gas injection spargers 11 and 13, bubble break up devices 16 in the riser and heat exchanger 17. Feed medium containing the elements essential for fermentation enters through line 14 and culture is removed through line 15. Gas bubbles escape from the free surface A-A of the liquid and are vented through line 12. This apparatus and its method of use are broadly described and claimed in the parent Specification 1353008. According to the present Specification, the apparatus is to be at least 20 metres in height e.g. between 40 and 60 metres, the total useful cross-sectional area of the riser is to be greater than, viz. between three and eight times, that of the downcomer, and the circulation of the liquid around the system is to be effected by injecting a gas thereinto in an amount sufficient to impart a mean velocity of at least 15 cms/sec to the liquid in the riser. Between 10% and 100% of the total volume of gas injected into the system may be injected into the liquid in the downcomer at 1 to 5 levels. Typically, the hourly rate of transfer of oxygen into the liquid culture is at least 2 kg. O 2 per cubic metre, and the mean velocity of liquid is between 20 and 80 cm/sec in the riser and between 200 and 500 cms/sec in the downcomer. The apparatus may have 3 to 8 risers and a single downcomer, the cross-sectional area of each riser being the same as that of the downcomer. Figs. 2 to 7 (not shown) depict other constructions of apparatus.
    公开号:SU967278A3
    申请号:SU742029264
    申请日:1974-05-15
    公开日:1982-10-15
    发明作者:Ритчи Гибсон Малькольм；Питер Маслин Франк；Корнелиус Ройслер Франк；Рэймонд Лесли Смит Стюарт
    申请人:Империал Кемикал Индастриз Лимитед (Фирма)；
    IPC主号:
    专利说明:

    The velocity of the fluid in the riser is at least 15 cm / s, the speed of the upward flow is maintained between 20-80 cm / s, and the descending flow is within 2o-500 cm / s, the medium is used as a fluid, containing microorganisms, a nutrient medium containing a hydrocarbon or a partially oxidized hydrocarbon is used as a liquid, an oxygen-containing gas, such as air, is used as a gas.
    In order to intensify the process by increasing the surface, contacting gas and liquid, the device for carrying out the proposed method is equipped with at least one additional pipe for gas supply located in the lowering pipe, and the cross-sectional area of the riser pipe is 3-8 times larger the cross-section of the standpipe, in order to increase productivity, it is equipped with several riser tubes placed around a single descender tube in the form of a polygon, and the riser tube is made in the form of two Ear sections: lower (contact) to upper (upstream flow stabilization), the cross section of the lower section being larger than the upper cross section.
    FIG. 1 schematically shows the proposed device with a separate arrangement of the lifting and downspout, a longitudinal section; in fig. 2 the same, with coaxial arrangement of pipes; in fig. 3, a third embodiment of the device; in fig. - fourths version of the device; in fig. 5 - fifth version of the device; in fig. 6 — Sixth embodiment of the device; in fig. 7 view A in FIG. 6; in fig. 8 - section BB in FIG. 7; in fig. 9 is a sectional view BB in FIG. eight.
    When implementing the proposed method, the fluid is continuously circulated through a system with a height of at least 20 m, which includes at least one upflow chamber (hereinafter referred to as a vertical pipe), and at least one downflow chamber (hereinafter referred to as downspout), the total useful cross-sectional area of the vertical pipe or.
    There is a total useful cross-sectional area of the downcomer or downcomers communicating respectively. . t the upper and lower ends of vertical pipes or vertical pipes; Circulation of the fluid in the system is ensured by introducing sufficient gas into it to give the flow of fluid in the vertical pipe or silt vertical pipes of average speed equal to at least 15 cm / s.
    In addition, a method for introducing a liquid, in contact with a gas, is proposed, in which liquid is continuously circulated in a system with a height of at least 20 m, including at least one upflow chamber (hereinafter referred to as a vertical pipe), and at least one downstream flow chamber (hereinafter referred to as the standpipe), with the total useful cross section of the standpipe or standpipe less than the total useful cross section of the vertical pipe or vertical pipes b and upper and lower ends of the standpipe or standpipe communicate respectively with upper and lower ends of the vertical pipes or riser; Circulation of the fluid in the system is ensured by introducing sufficient gas into it at several points in the system in an amount sufficient to impart to the flow of fluid in a vertical pipe or vertical pipes an average speed equal to at least 15 cm / s; part in the range from 10 to 100, but preferably from 10 to 60% of the total volume of gas introduced into the system, fall into the mass of liquid in the standpipe or downcomers.
    At the beginning of the implementation of the proposed method, it is advantageous to introduce the entire amount or most of the gas into a vertical pipe or vertical pipes for a period of time sufficient to start the circulation of the liquid. This initial stage of the process continues until a uniform circulation of liquid reaches the average velocity of the flow of liquid in the standpipe or standpipes of at least 100 cm / s.
    The invention can be applied to processes requiring homogeneous contact between a liquid and a gas, for example, when preparing solutions of copper sulfate from mineral ores containing copper sulfides in hydrometallurgical processes. In this case, finely ground ore is suspended in an aqueous medium that is circulated in accordance with the proposed method, and the introduced air also serves as an oxygen source for the conversion of sulfides between the ore to copper sulfate, which is in solution in such an environment. Such a transformation may be due to the action of microorganisms present in the medium or by simple chemical exposure in the absence of microorganisms. The invention can be successfully used in the implementation of fermentation processes., In particular, aerobic fermentation processes requiring high-intensity oxygen supply, although using the invention it is possible to carry out anaerobic reactions or fermentation processes by introducing an appropriate gas into the system. Aerob process group. fermentation, where it is possible with great success to apply the invention, including. In particular, the production of unicellular protein by growing microorganisms on hydrocarbon or partially oxidized hydrocarbon (for example, methanol-containing hydrocarbon) substrates; obtaining amino acids (for example, lysine, glutamic acid and methionine); obtaining citric acid and enzymes (for example, glucose isomerase) or obtaining antibiotics (for example, penicillin). In carrying out the method of aerobic fermentation, the invention is carried out. is as follows. The average velocity of the flow of a fluid or liquid nutrient medium in a vertical pipe or vertical pipes or standpipe or standpipes is taken over the entire cross section of the chamber. Because the internal. Cross-section in such chambers, especially in a vertical pipe or. Vertical tubes may not be the same throughout the length; the speed of the flow of a fluid or liquid nutrient medium in any chamber may vary along its length. In the process of aerobic fermentation in accordance with the proposed method of introducing gas into a liquid nutrient medium into a medium of reduced density, consisting of gas bubbles, liquid and the mass of microorganisms, the difference in the volume of voids in the vertical pipe or pipes and the standpipe or pipes as a result of the introduced gas reports to the flow of this medium a rate that is sufficiently high under normal process conditions in order to virtually homogenize the dispersion of the bubbles. In this embodiment, the liquid nutrient medium circulates in the system as a continuous flow, i.e. continuous flow with a certain degree of turbulent mixing. When carrying out this method, the entire volume of the elements of the liquid nutrient medium circulates quickly and evenly between the high and low hydrostatic pressure sections, respectively, in the lower and upper parts of the system. At the high pressure site, oxygen is required. for the growth of microorganisms, it is absorbed by the nutrient medium, while in the low pressure area the carbon dioxide that is formed during the process is released. In the upper part of the system, the exhaust gas is removed from the circulating fluid of the nutrient medium and removed from the system. The rate of oxygen transfer to the fast-growing nutrient medium, which can be achieved during the aerobic fermentation process, is an important factor, since it determines the rate of microbial production that can be achieved in the fermenter of this volume. The preferred transfer rate. in large-scale production plants, it should be at least 2 kg of oxygen / cubic meter, h, and more preferably, the velocity is in the range of -12 kg / cubic meter. h of oxygen. Since the transfer rate depends, among other things, on the overall height of the system, it is important that the height exceed the minimum value if the acceptable growth rates of microorganisms and the production process are maintained. In the fermentors of the invention, an acceptable transfer rate can be achieved with a total height of 20 m. However, a preferred height is at least 30 m, and a particularly preferred height is in the range of O-B m. The gas introduced into the system during the aerobic process fermentation, which can be used as oxygen, air or some other oxygen-containing gas mixtures, serves for the following purposes: causes the circulation of the nutrient medium in the system; is a source of oxygen required for microorganisms; By appropriately selecting the points of introduction of gas and the amount of gas introduced at these points, a substantial degree of control can be achieved during the process: for example, the flow velocity can be controlled and, consequently, the duration of the medium circulation; in addition, it is possible to regulate the distribution of the concentration of dissolved oxygen; The entire surface area of the bubbles formed by the injected gas is available for desorption of carbon dioxide; the volume and composition of the injected gas can be used to regulate / distribute the distribution of carbon dioxide concentration in a liquid or liquid nutrient medium. The total amount of gas injected, the points at which it is injected, and the proportional amounts of gas injected at different points, vary depending on the needs of the microorganisms and the required circulation rates. Gas can be introduced into the standpipe or pipes at one or several levels, for example at 25 levels. It is preferable to introduce gas into a vertical pipe or pipes at the same level, although it is also to be introduced into a vertical pipe at several levels. The respective points of introduction of gas into each chamber are distributed along the discharge pipe of the sludge pipes, but they are concentrated near the base of the vertical pipe or pipes. The device for contacting gas and liquid contains a circulation loop made in the form of interconnected in the upper and lower parts by re-connecting pipes 1 and 2 of the lifting and lowering pipes. 3 and 4, pipe 5 for gas inlet, located in the lower part lifting pipe 3, and at least one additional pipe 6 for the supply of gas, located in the standpipe pipe t. The cross-sectional area of the riser pipe 3 is larger than the cross-section of the descending pipe. Additionally, the device is equipped with several lifting pipes 3, placed around a single standpipe pipe k in the form of a polygon. Lifting tube 3 can be made up of two sections 7 and 8; the lower (contact) and upper (stabilizing upstream), the cross section of the lower section 7 being larger than the cross section of the upper section 8. For the sake of clarity, the corresponding position of the heat exchanger 9 designed to remove heat from the fermentation, remove or add heat, required for a chemical reaction, shown only in FIG. 1. The devices shown in FIG. 1, 2, 3, and 7, include a vertical pipe or tube in which cylindrical or annular upper and lower sections 8 and 7 are provided; (respectively) communicating with each other by means of a tapered section 10, with the diameter of the lower section 7 being greater than the diameter of the upper section 8. The fermentors shown in FIG. 4-6, include a vertical pipe or pipes 3 in which cylindrical or annular constant cross sections are provided. The upper end of the vertical pipe is connected to the upper end of the standpipe pipe 4 by means of a connecting element 11, which may be a horizontal cylindrical element, as shown in FIG. 1, 6 and 7, or may include a vertical cylindrical section 12 and conical connecting elements 13 and 1, which form extensions of the vertical pipe and standpipe, respectively, as shown in FIG. 2-5. The lower end of the vertical pipe is connected to the lower end of the standpipe by means of the overflow pipe 2 or the connecting element 15 which may be cylindrical, as shown in FIG. 1, 6 and 7, or horizontal with a circular cross section and form the base of the fermentor, as shown in FIG. 2-5Gas, for example air, are introduced into the lower part of the vertical pipe by means of inlet pipes, which causes a continuous circulation of the liquid phase, which occupies the volume of the fermentor to the level of HG. The upper ToijHOMy nozzle 1 is not allowed to fill with liquid, which allows creating a free surface from which gas bubbles escape from the liquid and are removed through the nozzle. An additional amount of gas, such as air, is introduced into the standpipe through one or more inlet pipes 6, two of which are shown in FIG. 1-7. The original medium, which includes elements that are essential for fermentation, is fed into the fermentor through nozzle 16, and the nutrient medium is removed from the fermentor through nozzle 17. Bubble breaker devices, in particular tool 18, are installed in the vertical pipe section. In accordance with FIG. 1, a heat exchanger 9 is shown in the standpipe i, although this heat exchanger can be mounted at any point on the riser and standpipe. In addition, several heat exchangers can be placed in any section of a vertical pipe, in a section of a standpipe, or in one or the other at the same time. It is advantageous to install a vertical pipe or pipes and a standpipe or pipes isolated from each other or completely separate from the connecting pipes, their upper and lower ends, or they can be installed | Vat inside one vessel divided inside. With one or several dividing walls, in the lower and upper part of which holes are provided. As a vertical pipe or pipes and a standpipe or pipes, it is POSSIBLE to use cylinders that are installed in isolation from each other and are connected by pipes that can pass horizontally or (in the case of the bottom connection) have a different shape. In addition, such a system may include In particular, two chambers passing coaxially, with one of THEM, preferably a vertical tube, enclosing the other. This system preferably includes several vertical pipes mounted separately from each other and communicating with one standpipe, in particular from 2 to 8 meters (ethical tubes communicating with one standpipe pipe). I in the latter case the cross-sectional area of each vertical pipe may be equal to the cross-sectional area of the standpipe, as a result of which the total cross-sectional area of the vertical pipes is larger. Such a system can be easily fabricated in advance. The test medium in the standpipe or pipes and in the vertical pipe or pipes, respectively, depend on the cross-sectional areas in such chambers, i.e., their diameters, if they are cylindrical. These chambers need not have the same diameter over their entire length. Indeed, in some cases it is desirable that the vertical pipe or pipes include two sections vertically one above the other, with the lower section characterized by a larger cross-sectional area. In this case, the preferred cross-sectional area of the lower section of a vertical pipe or pipes is 3-8 times larger than the cross-sectional area of the upper section. The length of the lower section is preferably between 30 and 60 times the total length of the vertical pipe. Alternatively, it is possible to permanently reduce the cross-sectional area of the vertical pipe or the pipes in the upward direction along their height. In order to prevent the accumulation of large amounts of carbon dioxide, the liquid nutrient medium must quickly circulate between the high and low pressure areas in the fermentor. The preferred circulation time of the liquid nutrient medium. The entire length of the system is in the range of 0.5-5 minutes, particularly preferably 1-3 minutes. The speed of movement of the liquid nutrient medium in any part of the vertical pipe — or pipes and standpipe or pipes depends on the cross-sectional area in the given section of the chamber. In order to circulate the liquid nutrient medium practically in the form of a continuous flow, the minimum speed allowed for its flow in a vertical pipe or tubes should exceed 10 cm / s. The preferred average velocity is in the range of 20-80 cm / s in a vertical pipe or pipes (in the lower part if this chamber is characterized by a different cross-sectional area in height) and 200-500 cm / s in the standpipe or pipes. In this fermenter can be carried out batch or continuous process. The liquid nutrient medium circulates practically in the form of a continuous current in which a high degree of homogeneity is to be achieved. Almost the entire volume of the fermentor can be -icnonbsoBaTb for the growth of microorganisms, and spaces where the anaerobic conditions are set are excluded. This ensures the possibility of highly efficient control of the parameters of the fermentation yarny, in particular, temperature, pH and concentration of the substrate, which allows to obtain a product of higher quality and greater uniformity. For example, in the case of the implementation of the proposed method in the process. the production of unicellular protein, the microorganisms produced show a high degree of morphological homogeneity and an improved degree of conversion of the carbon of the substrate to cellular carbon is achieved. The invention allows for efficient circulation and eliminates the need for external circulation bypass lines to remove the heat of reaction and fermentation. In an aerobic fermentation process, the application of the invention gives good results with respect to the achieved rate of oxygen transfer and energy consumption. The volumetric rate of oxygen transfer and the degree of energy transfer that can be achieved in fermenters of different heights are calculated theoretically for fermentors, the design of which is shown in phi 1. The volume transfer rate of oxygen is the rate expressed in kilograms of oxygen per hour and in a cubic meter of liquid that dissolves in a liquid nutrient medium. The degree of energy transfer is the ratio between the rate of oxygen transfer and the energy expended, expressed in kilograms of oxygen in a liquid nutrient medium per kilowatt-hour of work produced by compressing air before it is introduced into a single nutrient medium. The degree of energy transfer increases with an increase in the rate of transfer of oxygen, due to which, in order to increase the efficiency of the process, it is desirable to maximize both parameters as much as possible. liquid nutrient medium, as well as by calculating pressure changes between different points in the system. The energy required to compress the gas is calculated from the following assumptions: the pressure in the upper part of the system (where the gas is released from the liquid) is 1.5 bar (absolute); the pressure loss between the compressor and the entrance to the enzymeOp is 1 bar; air is supposedly used as the oxygen-containing gas. in its original state under a pressure of 1 bar and temperature. It is suggested that the compression process is adiabatic (isentropic) and to achieve a pressure increase sufficient to overcome the established 1 bar loss and to introduce air into the fermentor under pressure (or pressure) existing at the point of injection (or points of injection). These assumptions allow us to calculate the compression work that is valid in terms of the shaft power requirement of large axial compressors with intermediate cooling between two stages. It is assumed that up to 45% of the gas must be introduced into the standpipe at points whose number reaches 3. The results obtained are presented in the table.
    The results presented in the table are calculated with preservation of the assumptions about the coefficient of mass transfer and average sizes of bubbles. This indicates that the volumetric rate of oxygen transfer increases with increasing height of the fermentor. The best of the previously known results obtained using conventional enzymes include a transfer rate of approximately 3 kg / cubic meter of liquid nutrient medium, and they are achieved with a lower degree of energy transfer than that achieved in according to the invention. Thus, the implementation of the invention makes it possible to significantly improve the known results, and the height of the fermentor is of great importance for achieving such an improvement.
    The method of enrichment of oxygen-containing gas using pure oxygen or a mixture of pure oxygen with air allows, when it is carried out, to achieve even higher transfer rates. The 3Tof method does not fall within the scope of the invention, but it can easily be used in combination with the latter. Similarly, the transfer rate can be increased by constructing the entire fermenter as an elevated pressure vessel, causing the pressure in it to exceed atmospheric pressure at any point. This method can also be used in conjunction with the invention. However, both of these well-known methods for increasing the speed of production, namely methods of using frequent oxygen.
    And the creation of increased pressure throughout the space also suffers from known deficiencies. The great advantage of the invention is that the transfer rate of the same high value as indicated in the table can be achieved by using air as oxygen-containing gas, which is combined with a good degree of energy transfer without increasing the concentration of carbon dioxide dissolved in the liquid nutrient medium. to a high level.
    权利要求:
    Claims (6)
    [1]
    1. A method of contacting gas and liquid in aerobic fermentation processes by introducing gas into a liquid and creating circulating upward and downward flows of the gas-liquid mixture, so that, in order to intensify the process , at least 10 of the total amount of gas is injected into the liquid .8 the standpipe and the average velocity of the liquid in the riser is at least 15 cm / s.
    [2]
    2. The method according to claim G, about tl and h and y and the fact that the speed of the upward flow is maintained within 20-80 cm / s, and the downstream - within 200-500 cm / s.
    [3]
    3. The method according to claim 1 is also characterized in that a nutrient medium containing microorganisms is used as a liquid.
    [4]
    . Method-po.PP 1 and 3i about tl and cha. This is because a nutrient medium containing a hydrocarbon or a partially oxidized hydrocarbon is used as a liquid.
    [5]
    5. The method according to claim 1, wherein the gas has an oxygen-containing gas, for example, air.
    [6]
    6. A device for carrying out the method according to claim 1, comprising a circulating circuit made in the form of interconnected in the upper and lower parts by the overflow branch pipes of the lifting and lowering pipes, and a branch pipe for introducing the g-ase, 1; 1 h in the lower part the lifting pipe, p., tl, and the fact that in order to intensify the process by increasing the surface of contact of gas and liquid, it provides) at least one additional pipe / P1P gas supply located in the standpipe j and the cross-sectional area The first pipe is times the cross section of the standpipe. 7- The device according to claim 6, characterized in that, in order to increase productivity, it is equipped with several lifting tubes placed around one standpipe in the form of a polygon. 9 816 8. The device, on PP. 6-7, about the fact that the lifting pipe is made in the form of two sections; lower (contact) and upper (stabilization of the rising flow), with the cross section of the lower section being larger than the cross section of the upper one. Sources of information taken into account in the examination 1. French patent number 1228011, cl. At 01h, 08.26.60.
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    同族专利:
    公开号 | 公开日
    NO741770L|1974-11-19|
    NO143668B|1980-12-15|
    BR7403976D0|1974-11-26|
    BE815151R|1974-11-18|
    NO143668C|1981-03-25|
    DE2423766A1|1975-02-06|
    ES426381A2|1976-11-16|
    NL7406510A|1974-11-19|
    JPS5051972A|1975-05-09|
    GB1417486A|1975-12-10|
    DE2423766C2|1986-09-18|
    JPS5496868A|1979-07-31|
    引用文献:
    公开号 | 申请日 | 公开日 | 申请人 | 专利标题
    DE637728C|1930-12-23|1936-11-03|Svenska Jaestfabriks Aktiebola|Method and device for yeast production|
    DE752360C|1942-06-24|1953-06-22|Eugen Georg Stich|Circuit fermentation process and device for its implementation|GB1525930A|1974-12-04|1978-09-27|Ici Ltd|Circulation of gas/liquid mixtures|
    NZ183731A|1976-04-02|1980-04-28|Ici Ltd|Process for culturing cells dependent on the relationship between cycle time and biomass efficiency ratio|
    GB1573907A|1976-05-14|1980-08-28|Ici Ltd|Method and apparatus for the aerobic treatment of waste water|
    FR2359081B1|1976-07-22|1983-02-04|Dunlop Plantations Ltd|
    GB2002417B|1977-08-09|1982-05-26|Ici Ltd|Gas-liquid circulating and contacting apparatus|
    JPS6225347B2|1980-09-26|1987-06-02|Hitachi Ltd|
    US4752564A|1983-07-12|1988-06-21|Phillips Petroleum Company|Fermentation method and apparatus|
    GB8527335D0|1985-11-06|1985-12-11|Ici Plc|Fermentation process|
    GB8615059D0|1986-06-20|1986-07-23|Boc Group Plc|Oxygen using|
    DE102008041652A1|2008-08-28|2010-03-04|Evonik Oxeno Gmbh|Apparatus and method for the continuous reaction of a liquid with a gas|
    JP2010131590A|2008-10-30|2010-06-17|Shinshu Univ|Chemical reaction apparatus and stirring mechanism|
    JP5985270B2|2012-06-26|2016-09-06|新日本技研株式会社|Gas dissolver for liquid|
    CA2885803C|2012-10-08|2021-01-26|Calysta, Inc.|Gas-fed fermentation systems|
    JP2019129726A|2018-01-29|2019-08-08|長瀬産業株式会社|OTR simulator|
    法律状态:
    优先权:
    申请号 | 申请日 | 专利标题
    GB2333073A|GB1417486A|1973-05-16|1973-05-16|Liquid circulation and gas contacting device|
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