GB2507109A - Fermenter comprising gas and liquid re-circulation loops - Google Patents

Abstract

A fermenter (100), consisting of a volumetric reactor (115) equipped by a complex of internal devices: an internal cup for removal of re­circulating liquid phase (101), a damper cone (104), a damper-separator of gas and liquid phases providing their effective separation at a top of the reactor (116), a ring bubbler-distributor of methane (102), a ring bubbler-distributor of oxygen or air (103), a pipeline for input of ammonia solution (125) and an external circulating contour for simultaneous re-circulation of gas and liquid phases of the reactor (110), a heat exchanger for removal of fermentation heat (111), an ejector (112) for input and dispergation of re-circulating gas phase in recirculation liquid phase, a pipeline for removal of liquid re-circulating phase from the reactor (107), a pipeline for removal of gas from the reactor (109) and a pipeline for feeding of gas-liquid mix into the reactor (113). Methods of fermentation are also claimed.

Description

FERMENTER AND METHOD OF FERMENTATION

The present invention relates to a fermenter and to a method of affecting a fermentation process.

More specifically, the invention relates to a fermenter and to the method of its operation. The fermentation process described is one with methanotrophic bacteria in which it is necessary to teed one or several gases and other nutritious components in at the liquid phase of the fermenter, the method of the invention can also apply to other similar processes where one or several gases and other nutritious components are feed in at the liquid phase of the fermenter. Mass transport of gas components from the gas phase into the liquid phase of the fermenter should provide an optimum fermentation process due to maintaining required process parameters. The process parameters, where consistency is demanded and desirable, include the concentration of all components in the nutrient solution (i.e. the liquid phase) in the overall volume of the fermenter with simultaneous maintenance of explosion safety, reliability in the fermenter operation, the demanded selective characteristics, good controllability of the fermentation process and as much as possible, the expedient individual capacity of the Fermenter. This results in an economically expedient conversion of hydrocarbon-containing and oxygen-containing gases in a minimal possible period of time.

It may be useful to define terms used below as follows; A fermenter or bio-reactor is defined here as a vessel suitable for conducting fermentation or for employing biocatalysts.

A fermentation process is defined as the growth or maintenance of living bio catalysts under aerobic, anaerobic or partially aerobic conditions such that a desired product is produced, whether that product is the cells themselves or substances produced by the cells or converted by the cells.

Living biocatalysts encompass microbial cells! animal cells, insect cells, plant cells, viruses, phage, prions, amoebae, algae, fungi, bacterial, prokaryotic or eukaryotic cells.

Non living biocatalyst are dead cells or extracts from living or dead cells, e.g. enzymes.

Methanotrophs and methanotrophic bacteria are prokaryotes. They are organisms that are able to metabolize methane as their only source of carbon and energy. They can grow aerobically or anaerobically and require single-carbon compounds to survive. Under aerobic conditions, they combine oxygen and methane to form formaldehyde, which is then incorporated into organic compounds. They also characteristically have a system of internal membranes within which methane oxidation occurs. Methanotrophs occur mostly in soils, and are especially common near environments where methane is produced such as oceans, mud, marshes, underground environments, soils, rice paddies and landfills.

As background to the invention it is understood that biotechnological processes are widely used in a modern practice with use of such biocatalysts as microorganisms or enzymes.

Usually similar biotechnological processes are carried out in installations using a volumetric reactor, either a loop or a U-shaped fermenter in which the water solution of the nutrients, containing compounds of carbons, nitrogen, phosphorus and others macronutrient and micronutrient elements, air or oxygen and the biocatalyst feeds and reacts.

A prominent feature of a biotechnological process is the necessity of a feed in of a gas phase into the liquid phase of the fermenter. The gases including at least a gaseous hydrocarbon-containing substance (for example, methane), air or oxygenated air or oxygen.

It is desirable to provide an improved apparatus and method for fermentation which provides an alternative to the aforementioned fermenter for biotechnological processes.

The invention is defined in the appended claims.

According to a first aspect, the invention comprises a fermenter comprising a volumetric reactor having a liquid re circulation loop and a gas re circulation loop, further comprising an ejector arranged to input re circulating gas into re circulating liquid such that the combined gas-liquid mixture is fed back into a bottom portion of the volumetric reactor.

The cultivation of methane-oxidizing microorganisms both mixed, and also clean cultures of the kinds Methylococcus, Methylosinus, Methylomonas, Methylocystis can be carried out in a periodic, and continuous mode in a mixed aerated water-mineral medium at a process temperature and a growth medium pH, which are optimum for the growth of cultures of microorganisms. Streams of the concentrated nutrient, containing sources of phosphorus, potassium, magnesium and microelements, methane-containing gas and a source of oxygen, and teed are continuously fed into the growth medium. Nitric feed or microorganisms are provided with a feed water solution of ammonia or the gaseous ammonia (used simultaneously for stabilization of growth medium pH) in the growth medium.

There is pressure on the cultivation process in view of the speed of the mass transport of gaseous power supplies from the gas phase in the growth medium to meet demand. In a continuous process of cultivation, a water stream inlet feed, and a suspension containing biomass of a grown culture of microorganisms is selected continuously from the growth medium.

During the fermentation piocess the gas stream divides into two on leaving the growth medium. One of these streams is continuously returned repeatedly into the growth medium.

Thus there is re-circulation and the feed in the growth medium is mixed up all over again with a stream of methane-containing gas, then-with a stream of oxygen source gas. The result is a mixture of a gas stream returned into the growth medium also with streams of methane-containing gas and the gas from an oxygen source that can be carried directly into the giowth medium.

Moisture drops are removed from the second stream of gas and are transported for subsequent burning, and this gas stieam is then distributed between corresponding devices for biomass drying, for production of steam and/or electric power which then are used for the power needs of the process of biomass production.

Moisture, containing cells of microorganisms, removed from the leaving gas stieam of the growth medium is returned into the growth medium, or into the stream of the suspension leaving the growth medium, which is degassed, and the gas stream of the degassing process is united and combined with a part of the stream of the gas leaving from the growth medium and is transpoited for burning. The degassed liquid stream goes to a concentiator.

Then the liquid concentrate from the liquid stream or line goes to be subsequently thermally processed for inactivation of the cells, drying (in particular with a spray or with granulation) and packing, and the waste culture liquid removed by granulation or by drying partially goes to the growth medium after pie-processing or goes to the growth medium without pre-processing.

The cultivation of methane-oxidizing microorganisms at pressures of 0.12-1.0 MPa is intended to lead to an increase in speed of mass transport souices of gas feed. Methane and oxygen from the gas phase enter the fermenter and growth medium in the form of gas streams and hence promote an increase in the growth rate of microorganisms. As energy consumption on mixing of the growth medium does not depend on the cultivation process, this can lead to a deciease in energy consumption from cultivation to product pioduction until a continuous mode of end product production at realisation of the process. Besides, the raised pressure prevents the access of extraneous microflora from the atmosphere during cultivation, promoting increase in cultivation process without additional expense foi maintenance.

Thus sources of oxygen and methane-containing gas should move within the growth medium also at positive pressule, i.e. with pieliminaiy oi initial compression. As the gases heat up to sterilization temperature at compression, during cultivation of microorganisms at the positive pressure the gas streams fed into the growth medium are selected.

The process of cultivation of methane-oxidizing microorganisms can be carried out over a wide range of pressures. The minimal value of the pressure of the process of cultivation is defined first of all by maintenance of transportation of outlet gas fiom the giowth medium for burning together with its preparation, in particular partial drying. Also the pressure of and within the growth medium should provide for transportation of samples of gas and liquid phase to gauges foi controlling the cultivation piocess, in paiticular samples of the gas phase are transported to gas analyzers, samples of the liquid phase are transported to remote devices of a control system, thus reducing the operational expenses associated with the servicing of automatic control systems for the cultivation process.

The maximum value of the pressure of the cultivation process of methane-oxidizing microorganisms is defined by economic parameters, in particular the expense of compiession of a source of oxygen and of a methane-oxidizing gas, the requirements of the feed of liquid streams and the metal consumption iequired for the equipment applied and used in order to realise the method.

The powei input expense required for a cultivation piocess using transportation of output gas and samples at pressures below 0.12 MPa increases by 15-30%. Power inputs increase by 20-30% due to an inclease in the expense of compiession energy iequired foi gas feed sources at work undei piessures above 1.0 MPa.

By the application of natural gas as a methane-oxidizing gas there is an opportunity to exclude the expenses of compression of natural gas due to the use of the energy of the pressure of natural gas in the main pipelines for its feeds.

The concentrated nutrient medium continuously moves into the growth medium for maintenance of methane-oxidizing microorganisms with souices of mineral feed. The concentrated nutrient medium contains sources of phosphorus, potassium, magnesium and microcells or micro organisms with structure, balanced by specific needs of grown microorganisms, this means that the concentration of sources of the mineral feed containing the structure of chemical compounds, when dissolved in a nutrient medium is proportional to needs of the microorganisms to be grown from these feed supplies. The degree of concentration of a nutrient medium is expressed quantitatively in units of concentration of a biomass which could be formed by consumption of all sources of mineral feed in this medium.

The concentrated nutrient medium is prepared in the form of the water solution of the whole complexity of components of a mineral feed of micloorganisms, balanced on their specific need for these components, usually without inclusion of sources of a nitric feed in the structure of a nutrient medium. Use of the concentrated solutions of separate components of a nutrient medium or solutions of the components grouped is possible. In this way a process of proceeding from the technological conditions of the method to the realization is possible. In this case, however, the feed of separate streams is carried out in parity such that a recalculation on the incoipoiated stream of a nutrient medium can be provided. A proportionality calculation is provided between quantities of submitted feed supplies with specific needs of microorganisms for them.

Maintenance of the cultured microorganisms with nitiogen is cairied out by a continuous feed of ammonium nitrogen in the form of water solution of ammonia (ammonium hydroxide) or in the form of gaseous ammonia. It is preferable to use of the feed of ammonium nitrogen for simultaneous stabilization of the pH of the growth medium.

For maintenance of the optimum mode of cultivation of microorganisms the speed of consumption of the corresponding feed supplies streams are monitored. By monitoring the feed supplies it is possible to create an optimum level of concentration of feed supplies in the growth medium that is proportional to the growth rate of the microorganisms. This increases a degree of use of feed components in the nutrient medium during cultivation of micloorganisms. Also the streams of oxygen source and methane-containing gas delivered to the growth medium can be proportional to the speed of consumption of corresponding feed supplies for growing the microorganisms and therefore create an optimum level of concentration of feed supplies in the growth medium. Speed of consumption is defined by one or more of several parameters describing growth of microorganisms! particular examples include; the stream value and volume of the nitric feed source simultaneously used for stabilization of growth medium pH, by speed of carbonic gas formation, by growth rate of microorganisms, by thermal emission of cultivation process.

Use of mineral and gas feed sources by the input streams propoitional to speed of consumption of corresponding feed supplies, provides the maintenance of concentration of feed supplies in the growth medium and, hence, in outlet liquid and gas streams from the growth medium at the set levels corresponding to optimum values for cultivation of micloorganisms. This optimum value is within the limits of, not exceeding 10% from the set level. The level provides an increase in the degree of use of feed supplies during cultivation and allows the process of cultivation to be carried out at higher growth rates and with higher concentrations of biomass of microorganisms.

For maintenance of conformity between speed of consumption of the feed supplies submitted with liquid both gas streams, and volume of the liquid and gas streams submitted to the growth medium a correction factor can be used. The collection of factors of the proportionality between values of the corresponding streams submitted to the growth medium and the parameter or set of parameters, on which the consumption speed of corresponding feed supplies of methane-oxidizing microorganisms is set, is defined in view 205 of the conformity of concentrations of feed supplies of methane-oxidizing microorganisms in the outlet liquid and in the gas streams from the growth medium set to the optimum level.

The preferable range of correction of proportionality factor is 1-10% from the established value. The optimum level of concentration of mineral feed sources in the growth medium is equal to the concentration of these feed supplies in the outlet liquid stream from the growth 210 medium. This is defined by the kinetic laws of consumption of mineral feed sources by methane-oxidizing microorganisms.

The optimum level of oxygen concentration in the stream of outlet gas from the growth medium is defined, on the one hand by the safety requirements of the cultivation process using methane-oxidizing microorganisms and the subsequent transportation of this gas, and 215 on the other hand maintaining maximum process productivity in the cultivation of methane-oxidizing microorganisms, as measured by the quantity of formed biomass.

Maintenance of an optimum level of concentration of feed supplies in the growth medium, submitted with a stream of the nutrient medium, is proportional to speed of their consumption with a correction. The correction is a correction in the proportionality factor between the 220 volume of a stream and parameter on which speed of consumption is defined, by concentration values of these substances in the outlet liquid stream that leads to productivity of process of cultivation is defined by speed of mass transport of gaseous feed supplies from the gas phase into the growth medium for maintenance of cultured microorganisms with the sources of gas teed -methane and oxygen.

225 Speed of mass transport depends on mass exchange characteristics of the apparatuses in which the cultivation process is carried out, and on the driving force of the mass transport, proportional to partial pressure of a corresponding component in the gas phase which is equal to the product of pressure of the growth medium and volumetric concentration of a component in the gas stream which is passing through the growth medium.

By comparing modes of cultivation with the structure and type of the gas stream it is shown, that at iealization of process above the top limit of flammability, higher values of productivity of cultivation process of methane-oxidizing microorganisms are reached, and therefore production expenses per unit decrease at an identical rate to the increase in the power 235 expenses for mixing.

It is possible to accept the maintenance in this mix of oxygen as a parameter of safety of gas mixes in the field of above top limit of flammability of ballasted methane-oxygen mixes. At the content of oxygen less than 10 vol. % ballasted methane-oxygen the mix is always non-flammable irrespective of the content of methane in it and at any pressure. In work 240 situations with mixes having a high volumetric concentration of methane in the structure and with pressures below 0.3-0.4 MPa then the maximal safe content of oxygen can be increased up to 15%. For good safety practice during the cultivation process and also during transportation of the outlet gas stream from the growth medium, the content of oxygen in the outlet gas stream fiom the giowth medium should not be above 10-15 vol. % varying with 245 pressure.

The highest use (degree) value of use of both components of a gas feed -methane and oxygen -is found to be reached at a performance of a condition, that transport rate of both components of the gas feed from a gas phase to the growth medium is equal to speed of theft consumption by micloolganisms. It is experimentally established, that the speed of 250 mass transport of methane from a gas phase to the growth medium is a little below the speed of mass transport of oxygen (around 10-15%) when at an identical partial pressure in a gas phase. This means that for the maintenance of the best modes of cultivation of methane-oxidizing microolganisms the volumetric content in the outlet gas stieam from the growth medium that corresponds to the partial pressure of methane in a gas phase of the 255 growth medium should be above the volumetric content of oxygen in outlet gas stream from the giowth medium and above the ratio of consumption speeds of these feed supplies by methane-oxidizing microorganisms. Thus the absolute content of methane in the outlet gas can be less that the absolute content of oxygen, because it is consumed at a rate more than one volume of oxygen to one volume of methane during the cultivation of methane-oxidizing 260 microorganisms.

Preferable ranges of the excess can be defined as coming from the following reasons. The outlet gas, containing methane from the giowth medium can be considered as low-caloiie fuel which heat of combustion is defined, mainly, by the content of methane in it.

265 In reviewing efficiency and cost effective use of materials for cultivation of methane-oxidising micro organisms the stages of the fermentation process are examined. In connection with expediency of the fullest use of the raw material submitted during cultivation of microorganisms, and considering, that it is economically inexpedient to use it completely during cultivation, also in connection with sharp increase in power expenses with the use of 270 methane from methane-containing gas at more than on 90%, it is necessary to consider an opportunity to use methane-containing gas leaving the growth medium.

Various uses of the outlet gas stream from the growth medium, in particular, as initial raw material for the precipitation of impurities, contained in the supplied or submitted methane-containing gas, or for chemical processing are possible. Another use of the outlet gas 275 stream from the growth medium is for fuel for production for thermal energy. In this connection and use the quantity of methane-containing gas submitted and recirculated to the cultivation process is defined, in particular, and quantity of energy which needs to be produced and burnt at the outlet gas stream from the growth medium is defined. Thus it is expedient to use outlet gas as such fuel, so that additional burning and fuel means is not 280 required.

The minimal content of methane in the outlet gas for use as a possible aid to fuel the production of energy (without use of additional fuel) is 20 vol. %. The use and recirculation depends on the content of oxygen in the gas. The ratio of consumed methane to consumed oxygen during microbe cultivation in the fermenter when compared to the excess input 285 stream methane and recirculated gas (original oxygen source gas, now containing methane) is 1-5% for a minimal use of power. In other words an excess of quantity of submitted methane with the stream of methane-containing gas concerning submitted oxygen with the stream of oxygen source in comparison with ratio of quantity of consumed methane to consumed oxygen on 1-5% at realization of cultivation process of methane-oxidizing 290 microorganisms in a mode of the minimal power expenses for biomass production due to mixing.

The maximum level of excess is defined only by the quantity of energy which is necessary for production due to the burning of the outlet gas stream from the growth medium, but it should not be above 100% as in this case the degree of use of methane sharply decreases 295 during cultivation of methane-oxidizing microorganisms, and it is expensive to supply and recirculate or loop streams of methane-containing gas and oxygen source into the growth medium.

Modes of cultivation of methane-oxidizing microorganisms, corresponding, on the one hand, to optimum consumption of methane and oxygen, and, on the other hand, to safety of the 300 process of cultivation of methane-oxidizing microorganisms and transportation of the outlet gas stream from the growth medium, demand a certain quantity of ballast gases in the outlet gas stream (outlet from the growth medium).

A part of the outlet gas stream from the growth medium returns repeatedly to the growth medium and is re-circulated, and other part is sent direct to recycle the energy contained in 305 it, for maintenance of an adjustable quantity of the gas stream supplied on burning and also a content of ballast gases in it.

An application of the gas phase and the separate feed of streams of methane-containing gas and the oxygen source allow for an expanded area of parities between streams of methane-containing gas and the oxygen source and in such values as correspond to a mode of 310 optimum use of sources of the gas feed. The gases are submitted in the format of a joint stream and as a combustible methane-oxygen mix which for this reason cannot be used for the process of cultivation of methane-oxidizing microorganisms.

The outlet gas stream from the growth medium has the same pressure, as the pressure in the growth medium, and possesses mechanical energy which it would be expedient to use.

315 As well as the potential thermal energy used at its recycling. Energy of the pressure of the outlet gas stream from the growth medium is used at it undergoes transportation, the recycled energy is used to overcome resistance of pipelines and the armature located in them.

Thus, the fermentation process represents aerobic cultivation which is carried out in a liquid 320 nutrient medium of a reactor with gaseous components (for example, methane, air or oxygen-rich air, or oxygen). There is production of a by-product -carbon dioxide which it is necessary to remove from the reactor with an off-gas device.

Microorganisms cannot use gaseous substances directly during fermentation. Gases should be distributed in liquid so that microorganisms can use them for growth of microbial mass.

325 Thus the mass transport speed of substances from the gas phase into the liquid phase as described above, is in the form of more small gas bubbles.

The problem of achieving a uniform distribution of gases in the liquid phase of a fermenter is of the same importance as the problem for an effective fermentation process. In addition simultaneous maintenance of constant (on all volume of a reactor) concentrations of all the 330 nutritional components, the pH of the medium and the selective conditions of fermentation process are required and are connected with it. Other requirements are the mass transport speed from the gas phase in the fermentation liquid phase, the speed and qualitative and quantitative structure of the removed gas from the fermenter, including maintenance and monitoring of the content of carbon dioxide and the residual content of methane and oxygen 335 in it. Further in view of the requirements of the guaranteed maintenance of explosion-proof concentration of oxygen in the removed gas mix, and as a consequence the maintenance of a constancy of speed and all other quantitative characteristics in the fermentation process are required The characteristics of the fermenter and the auxiliary equipment and devices used in its 340 structure have crucial importance for maintenance of economically effective all-round fermentation process. A full account of all above the listed features, laws and requirements of fermentation process is given.

Usual volumetric fermenters are apparatuses with mixers which provide formation of gas bubbles in the liquid phase and their distribution in all parts of a reactor.

345 In a usual volumetric fermenter a part of the gas stream from the outlet gas stream from the growth medium is repeatedly returned to the growth medium and re-circulated for the continuous circulation of a gas phase. This provides regulation of the quantity of the gas submitted and used in burning, and the content of the ballast gases in it, in addition it provides a set of advantages for the realization of a cultivation process for methane - 350 oxidizing microorganisms.

One of the advantages of the application of recycling the outlet gas stream from the growth medium is the opportunity to increase the degree of use of components of the gas feed -for example methane and oxygen components remaining from and during cultivation of methane-oxidizing microorganisms, and especially as its application as a source of oxygen, 355 oxygen-rich air, or pure oxygen.

Another advantage of the application of recycling the gases is the opportunity to use high speed submission of gas streams into the growth medium, thus providing a high degree of use of components of the gas feed, which at application of recycling streams is not defined by opportunities of application of apparatuses for cultivation of microorganisms, and 360 requirements on structure of the gas streams, the defined list of conditions of maintenance of optimum conditions of a gas feed of microorganisms, safety issues with conducting the process, transportation of the outlet gas stream from the growth medium and its use as fuel.

Recycling of the gas stream can be used for the removal of part of C02 formed during cultivation, by means of passing of the recycling gas stream through the known devices 365 removing carbonic gas from the gas phase.

Defects of fermenters of the volumetric type include: -Expense of the energy required for mixing great volumes of the reactionary medium by means of a high-speed mixer; -Heating of the reactionary mass due to its mixing by a high-speed mixer and thus the 370 additional heat removal necessitated by this mixing; -Insufficient mass transport from the gas phase to liquid phase; -Poor separation of gas bubbles from liquid in the top pad of the fermenter.

Usual volumetric fementers and ways of production of a biomass of methane-oxidizing microorganisms are shown in the Copyright Certificate of the USSR No. 1349244, the Patent 375 of Russia No. 2064016.

A U-shaped or loop reactor can reduce mechanical mixing to some degree by reducing the mechanical mixing of the liquid reactionary medium, though the pump (more often an axial type) used in the bottom of such a fermenter can give rise to the liquid phase containing bubbles of gases in an ascending part of the fermenter, in essence, also providing a mixing 380 device.

Gases (methane and air or oxygen) move separately usually in a falling part of the U-shaped or loopback rector. This means there may be the possibility of use of the gas at rather low pressure and increases in time of contact of liquid with gas.

As such reactors have the greater total length for maintenance of the necessary time of 385 contact of gas with liquid, the feed of gases carried out in some points and at a variety of entrance points throughout the length of a reactor, and for a decrease in the occurrence of the coalescing of bubbles of gases. Fermenters also establish static or dynamic amalgamators through and along their length and at a falling and ascending part of a reactor after each input of gas.

390 Simultaneously the top part of U-shaped or loop reactor can be expanded for separation of a liquid phase and separation of gases removed from a fermenter.

U-shaped and loopback reactors are intended for realization of fermentation processes basically at atmospheric pressure, though the pressure can be raised slightly in parts of a reactor on the discharge side of pumps or due to a change of diameter of a reactor through 395 its length due to use of pumps.

Some defects of U-shaped and ioop fermenters are: -Variable concentration of components of a liquid nutrient medium and input gas (methane and oxygen) through and along the length of a reactor, considerably reducing the efficiency 400 of the fermentation process; -The difficulty, and impossibility of maintaining a controllable quantity in the optimum size of gas bubbles with diameter 2-5mm in a liquid phase that reduces mass transport from gas to liquid, difficulty in relation to the potentially maximum achievable mass transport with a diameter of bubbles of 2-5mm; 405 -Carrying out the fermentation process at a pressure close to atmospheric pressure due to the difficulty of 002 separation from a liquid phase and the stopping of the fermentation process due to a decrease in the concentration of methane and oxygen. This considerably reduces the product output in relation to the potential output opportunity from the process at a positive pressure; 410 -Carrying out the fermentation process in the field of concentration of oxygen below the low limit of explosivity of methane that leads to serious danger of transition of the process in a zone of explosion hazard due to anticipating an unauthorized increase in the concentration of oxygen in a fermenter (for example, in case of local increase of pressure or failures in a control system); 415 -Necessity of use of the separate compressor for compression of the methane submitted into a fermenter in cases of low pressure of initial methane; -Time of stay and accordingly different concentration of gas in zones of the reactor, submitted to different points through length of fermenter; -Impossibility of qualified use of the off-gas containing the unreacted methane and 420 accordingly the necessary emission into the atmosphere, thus polluting the environment; -Complexity of process control to maintain a suitable pH environment in a fermenter, and the use of alkali for maintenance of pH = 6.0, as in ranges pH = 4-4.5 and 6-7. The addition of alkali does not sharply change the pH environment pH so the additional introduction of ammonia solution is required. This reduces the controllability of the process and leads to the 425 deterioration in the selective properties of the environment and thus leads to an opportunity for the occurrence of pathogenic microbes in the reactor; -Rather small individual capacity of a reactor (up to 3.0-9.0 thousand tons from one reactor per year), defined in particular by the necessary and expedient time of stay of the initial substances in a reactor both for other requirements of technology and opportunities and 430 limitations of the equipment.

Various technical decisions of U-shaped and loop reactors and loop fermenters with the expanded top park and fermentation methods corresponding to them are described in patents US 6,492, 135 B1; WO 031016460 Al; EP 1419234 (Al); WO 2010/0693132.

The defects of U-shaped, loop reactors and loop reactors with an expanded top part upper 435 portion as listed above are defects resulting from the natural shape and structure of these types of reactors, this means that overcoming of the defects can be complicated. In some instances the defects of some fermenters of the volumetric type can be removed or minimised essentially or even practically to eliminate them by a complex set of economically comprehensible technological constructive decisions.

440 The present invention relates to an advanced fermenter with simultaneous gas and liquid phases and with an improved volumetric reactor. The reactor will be described below and has internal devices, and technical features to intensify process of growth of microorganisms and to increase biomass output from 1 M3 of the reactor.

The invention will now be described in further detail with reference to the accompanying 445 drawings in which Figure 1 shows the fermenter apparatus.

The elements shown In Figure 1 include an advanced fermenter 100 comprising a reactor of volumetric type and a liquid recirculation loop and a gas recirculation loop and suitable pump and circulation means for directing and moving the flow of liquid and gas as shown in Figure 1 and represented by the arrows. The reactor 115 is such that the liquid 450 phase is up to lOm high in the reactor. The fermenter apparatus 100 includes re circulating contours in liquid and gas phases simultaneously and ejection apparatus for the circulating gas selected from the top of a reactor, such that the combined gas-liquid mixture is fed back into a bottom portion 105 of the volumetric reactor 100. The liquid phase of the reactor 100 selected from the bottom or base portion 105 of a reactor and submitted and supplied by the 455 pump 110 and ejector 112 with pressure. The pressure is sufficient for ejection of the input of gas-liquid mix (produced in ejector) downstream of the reactor, and maintenance during ejection distributions of gas in liquid in the form of gas bubbles with diameter 2-5 mm. The diameter of 2-5 mm is the most preferable to produce and realize the greatest mass transport from gas to liquid and can achieve the greatest biomass output per time unit. Such 460 design of a fermenter allows for the exclusion of clearing, drying and compression by means of the compressor of re-circulating gas of a reactor and accordingly lowers power consumption considerably.

Simultaneously such design of a fermenter avoids use of high-speed mixer! this in addition reduces power consumption for biomass production, and also excludes the necessity of heat 465 removal at a mixer location and allocated during rotation.

Except for ejection of re-circulating gas of a reactor the liquid phase of a reactor achieves a controllable high degree of distribution of gas in liquid due to the ejector unit proving the formation of a plurality of small diameter bubbles in the liquid phase with optimum diameter 2-5mm. The diameter is set by calculation, and the apparatus is designed to provide bubbles 470 with the best mass transport from gas to liquid and accordingly the best conditions for growth of microbial mass.

The gas-liquid mix from the ejector moves in a vertical reactor tangentially to the vertical orientation and forms the surface of the reactor. The movement of the gas-liquid mix then moves around and under a corner to a vertical axis of a reactor for maintenance of a twisting 475 of gas-liquid mix in a reactor. The twisting increases the time for the interaction of gas and liquid phases and accordingly achieves a more effective mass transport from gas to liquid and a corresponding decrease in the opportunity for coalescence of gas bubbles due to a high speed of a liquid. A twisting action also achieves by a high degree of re-circulating of gas and liquid phases, and also surface-active properties of the reaction medium.

480 In a reactor the fermentation process is preferably carried out at a pressure of 0.12 MPa - 1.0 MPa and a temperature of 42-43°C, and a positive pressure (0.3-0.4 MPa) is preferable.

The parameters provide essentially greater and economically the most favourable speed of process and accordingly greater biomass output per unit time in comparison with fermentation at pressure close to atmospheric pressure or in a loop or U-shaped reactor.

485 A nozzle 124 is used for feed of methane-containing gas carried out in a reactor through the nozzle 124. The feed is carried out through a ring 102 bubbler-distributor of gas downwards of a reactor. Feed of oxygen (air) is carried out in a reactor through the nozzle 123 and through the ring bubbler-distributor of gas 103 also downwards of a reactor, but above the bubbler-distributor of feed of methane-containing gas.

490 Use of static damper 116 of the rotating stream is provided for maintenance of good separation of gas from liquid in the top part of a fermenter. It is executed in the form of a horizontal disk with plates located vertically inside of the disk and in a direction rotating below the gas-liquid stream in its topmost position in a vertical direction upwards already without rotation.

495 Separation of gas from liquid in the top part of a fermenter can also be improved with the use of other static elements, such as horizontal grids, plates with valves or caps and liquid overfalls, installation of return" umbrella 117 feature at the top of a reactor and/or a cyclone or group of cyclones located at the top of a reactor.

In the reactor an internal pipe (a cup) 101 and a cone damper 104 provided on top of the 500 pipe are design features addressing two important problems. The pipe 101 is stipulated in this embodiment for selection of a liquid phase feed from a reactor for its feed in the circulating pump of liquid phase 110: degassing of liquid phase with the purpose of avoiding and excepting cavitation of the circulating pump and simultaneous exception for rotation inside of this pipe (cup) by returned re-circulating liquid phase. The formation of a cone 505 provides rotations of liquid phase inside the reactor around the given pipe (cup), on the one hand, and, on the other hand, high-speed movement of liquid phase downwards inside of the pipe (cup) (with speed of 1.5-2.0 kmls), for prevention of gas inrush through a cone which narrow end is turned downwards into the pipe (cup), to the circulating pump. The installation of a cone damper 104 on top of the internal pipe (cup), to look like a disk with 510 vertical directing streams and stopping rotation of the liquid inside of the pipe (cup) assists in avoiding cavitation.

The pipeline 125 illustrated in Figure 1 is introduced inside of the pipe (cup) through the nozzle in a reactor 120 for feed of ammonia solution for regulation of medium pH, which at such way of its feed provides as much as possible operative maintenance of process 515 demanded for technology and maintenance of selective acidities of medium pH (pH = 5.6) in a fermenter.

The pipeline 107 of the re-circulating liquid phase is used also for input of solution of salts and microcells with the set concentration of each component and fresh water in it that allows a substantially and practically constant concentration of all components of a nutrient medium 520 in a fermenter at a frequency rate of circulation of the liquid phase (30-50).

Heat pick up of process of biosynthesis is carried out by cooling the liquid phase in a vertical heat exchanger 111, established on the discharge side of the circulating pump of liquid phase 110 and providing maintenance of optimum temperature in a fermenter for the process of growth of microorganisms (42-43°C).

525 The re-circulating part of the gas phase of a reactor continuously moves in an ejector 112 in which is entrained by the re-circulating stream of the liquid phase with the necessary pressure provided by the circulating pump of the liquid phase 110, and is distributed in the form of a plurality of small bubbles in the liquid phase. The ejector design is made in such a manner that at ejection of gas in the liquid the diameter of the gas bubbles created is 2-5 530 mm. This provides maximal mass transport from gas to liquid during fermentation and accordingly the achievement of the maximal growth rate of microorganisms and the greatest output of biomass per unit time.

In operation, the outlet gas-liquid stieam with gas bubbles distributed inside of it from the ejector moves tangentially in the bottom pad of a leactor thiough the nozzle 114 to vertical 535 forming walls of a reactor and under a corner at an angle of 1O3O0 to a vertical axis of a reactor for twisting of the fermentative medium and course of process of biosynthesis of micloolganisms in a leactor at maximal mass tiansport from gas to liquid, at constant optimum concentration of all of macro-and microcells of a nutrient medium, nitrogen, methane, oxygen and phosphorus, at constant acidity of medium (pH = 5.6), providing 540 selective conditions of fermentation process, at a constant safe concentration of oxygen (10- 15%) -depending on pressure in a fermenter. The safe concentration is one that is safe from the point of view of explosion, at constant selection of produced biomass suspension which is carried out thiough the nozzle 122 in the top part of a leactor, at constant quantity and contents of removed off-gas from a fermenter with constant content of methane (20 vol. 545 %), this amount is the minimum necessary for the possibility of its recycling by burning for generation of thermal energy used by biomass drying.

Pressure in a reactor is supported by pressure of gas in the top part of a reactor, and protection of a reactor against a potential possible excess of pressure in ielation to the design pressure of the system provided due to an explosive membrane (121).

550 Fermenter and fermentation method under the present invention allow to use not less than 90-95% of initial gas (methane) and to produce biomass with the gleatest possible efficiency.

Fermenter and fermentation method under the piesent invention allow to have economically possible much greater individual capacity of a fermenter (not less than 10.0 th.t. of biomass 555 per year from one reactor) from the constructive and technological points of view, than the capacity of a U-shaped either loop fermenter or loop fermenter with an expanded top part (i.e. in 1.3-3.5 times) that essentially reduces quantity of feimenters and accordingly expenses for creation (on 15-40%) and opeiational expenses (on 10-20 %) of plants.

Example:

560 Culture Methylococcus capsulatus strain BCb -874 is grown up in a fermenter in conditions of continuous cultivation. Working volume of the fermenter is 300m3.

Process of cultivation is carried out on the simple mineral mediums consisting of orthophosphoris acid, chlorides of potassium, magnesium, iron and sulphates of copper, manganese, zinc, cobalt, boiic acid and sodium molybdate as micioadclitives. During 565 manufacture natural gas is used as a unique source of carbon and energy. Process is carried out with participation of oxygen.

Process is carried out in a mode of re-circulation of a gas phase.

Medium pH is suppoited by means of ammoniac water which simultaneously is a source of nitrogen, at a pH level of 5.6 + 0.1. A fermenter the temperature is supported at level 42- 570 43°C with use of a remote heat exchanger, located on three contours of re-circulation of liquid medium.

In apparatus pressure is 3 atmg (0,4 MPa (abs)). Outlet gas from the apparatus recycles by means of an ejector in the bottom part of the apparatus in quantity 7500 m3/hour (30000 Nm3/hour). Fiesh natuial gas (95%) and oxygen (95%) in quantity 2440 Nm3/hour and 575 3100 Nm3/F-iour accordingly moves in bubblers of the apparatus. Quantity of the off-gas removed through the nozzle of the top covei of the fermenter is 700 Nni3. Content of methane in off-gas is 20 % oxygen -10%. A degree of use of oxygen is 98%. A degree of use of methane is 95%.

Process of continuous cultivation is caiiied out with a stieam speed 0.25 hi, biomass 580 concentration in the cultivation medium is 20 gIl under dry weight. Hour biomass capacity of the apparatus is 1500 kg/hours.

Suspension leaving the device is decontaminated, concentrates, in activated, dried and packed.

Off-gas is utilized in power installations where it is burnt with addition of additional air.

The following paragraphs further explain the invention.

A fermenter and a method of fermentation in Fermenter (100), consisting of a volumetric reactor (115) equipped by a complex of internal devices: an internal cup for removal of re- 590 circulating liquid phase (101), a damper of cone from rotation and at movement downwards liquids in the reactor (104), a damper-separator of gas and liquid phases providing their effective separation at a top of the reactor (116), a ring bubbler-distributor of methane containing gas fed to the reactor (102), a ring bubbler-distributor of oxygen or air (103), the pipeline for input of ammonia solution (125) and an external circulating contour intended for 595 simultaneous re-circulation of gas and liquid phases of the reactor, including a pump for re-circulation of liquid phase of the reactor (110), a vertical heat exchanger for removal of heat of fermentation process (111), an ejector (112) for input and dispergation of re-circulating gas phase in recirculation liquid phase, a pipeline for removal of liquid re-circulating phase from the reactor (107) through a nozzle in a bottom of the reactor (105), a pipeline for 600 removal of gas re-circulating phase from the reactor (109) through the nozzle at a top of the reactor (106), the pipeline for feeding of gas-liquid mix into the reactor (113) through a nozzle in a bottom of the reactor (114). located tangentially to vertical forming of the reactor shell and under a corner to a vertical axis of the apparatus. In the reactor pressure is supported by pressure of gas in a top part of the reactor, and protection of the reactor 605 against potentially possible excess of pressure in relation to design pressure is provided due to installation of an explosive membrane (121) on a top of the reactor.

The present invention relates to a fermenter and to a method of affecting a fermentation process.

More specifically, the invention relates to the Fermenter and the Method of its operation which correspond to fermentation processes with methanotrophic bacteria and to other similar processes to which it is necessary to feed one or several gases and other nutritious components in the liquid phase of the fermenter. Mass transport of gas components from 615 the gas phase in the liquid phase of the fermenter should provide optimum fermentation process due to maintenance of constancy of demanded parameters of process, concentration of all components in nutrient solution (the liquid phase) on all volume of the fermenter with simultaneous maintenance of explosion safety, reliability of the e operation, demanded selective characteristics, good controllability of fermentation process and 620 achievement of expedient individual capacity of the Fermenter as much as possible and economically expedient conversion hydrocarbon-containing and oxygen-containing gases for minimally possible period of time.

A fermenter or bio-reactor is defined here as a vessel suitable for conducting fermentation or 625 for employing biocatalysts.

A fermentation process is defined as the growth or maintenance of living bio catalysts under aerobic, anaerobic or partially aerobic conditions such that a desired product is produced, whether that product is the cells themselves or substances produced by the cells or 630 converted by the cells.

Living biocatalysts encompass microbial cells! animal cells, insect cells, plant cells, viruses, phage, prions, amoebae, algae, fungi, bacterial, prokaryotic or eukaryotic cells.

635 Non living biocatalyst are dead cells or extracts from living or dead cells, e.g. enzymes.

Biotechnological processes are widely used in a modern practice with use of such biocatalysts as microorganisms or enzymes. Usually similar biotechnological process is carried out on the installations using a volumetric either loop or U-shaped fermenter in which 640 the water solution of the nutrients, containing compounds of carbons, nitrogen, phosphorus and others macronutrient and micronutrient elements, air or oxygen and the biocatalyst feeds.

Prominent feature of biotechnological processes is necessity of teed of the gas phase, 645 including at least gaseous hydrocarbon-containing substance (for example, methane), air or oxygenated air or oxygen, in the liquid phase of the fermenter.

Cultivation of methane-oxidizing microorganisms both mixed, and clean cultures of kinds Methylococcus, Methylosinus, Methylomonas, Methylocystis carry out as in periodic, and 650 continuous mode in the mixed aerated water-mineral medium at process temperature and growth medium pH, which are optimum for grown up culture of microorganisms. Streams of the concentrated nutrient, containing sources of phosphorus, potassium, magnesium and microelements, methane-containing gas and a source of oxygen, feed continuously in the growth medium. Nitric feed or microorganisms is provided with feed water solution of 655 ammonia or the gaseous ammonia (used simultaneously for stabilization of growth medium pH) in the growth medium. Pressure of cultivation process establishes in view of demanded speed of mass transport of gaseous power supplies from the gas phase in the growth medium. In the continuous process of cultivation technological water stream feeds in addition, and the suspension containing biomass of grown up culture of microorganisms 660 select continuously from the growth medium.

During fermentation process of leaving the growth medium the gas stream divides into two.

One of these streams continuously returns repeatedly in the growth medium. Thus before repeated feed in the growth medium it is consecutive can mix up all over again with a stream 665 of methane-containing gas, then-with a stream of oxygen source. Mixture of a gas stream returned in the growth medium with streams of methane-containing gas and oxygen source can be carried out also directly in the growth medium.

Moisture drops are removed from the second stream of gas and are transported for the 670 subsequent burning, distributing this gas stream between corresponding devices for biomass drying, for production of steam and/or the electric power which then are used for power needs of process of biomass production.

Moisture, containing cells of microorganisms, removed from the leaving gas stream of the 675 growth medium is returned or in the growth medium, or in the stream of suspension leaving the growth medium, which is degassed, and the gas stream of degassing process is united with a part of the stream of the gas leaving from the growth medium and is transported for burning, and the degassed liquid stream goes to concentrating.

680 Then concentrate of the liquid stream goes to the subsequent thermal processing for inactivation of cells, drying (in particular spray or with granulation) and packing, and the waste culture liquid partially goes to the growth medium after pre-processing or without it.

Process realisation of cultivation of methane-oxidizing microorganisms at pressure 0.12-1.0 685 MPa is intended for increase in speed of mass transport sources of gas feed, methane and oxygen from the gas phase entering in the form of gas streams in the growth medium and hence promotes increase of the growth rate of microorganisms. Thus as energy consumption on mixing of the growth medium cannot depend on cultivation process lead to decrease in energy consumption at cultivation on production of until of an end product at 690 realisation of process in a continuous mode. Besides, the raised pressure prevents access of extraneous microflora from an atmosphere during cultivation, promoting increase asepsis of cultivation process without additional expenses for its maintenance.

Thus sources of oxygen and methane-containing gas should move in the growth medium 695 also at positive pressure, i.e. preliminary compressed. Considering that gases heat up to sterilization temperature at compression, during cultivation of microorganisms at the positive pressure the gas streams fed into medium are aseptic.

Process of cultivation of methane-oxidizing microorganisms can be carried out in a wide 700 range of pressure. The minimal value of pressure of process of cultivation is defined first of all by maintenance of transpoitation of outlet gas from the growth medium for burning together with its preparation, in particular partial diying. Besides piessure of the growth medium should provide transportation of samples of gas and liquid phase to gauges of control of cultivation process, in particular samples of gas phase to gas analyzers, samples 705 of liquid phase to remote devices of the control, that reducing operational expenses for service of automatic control systems of cultivation process.

The maximal value of pressuie of cultivation piocess of methane-oxidizing micloolganisms is defined by economic parameters, in particular expenses of compression of a source of 710 oxygen and methane-oxidizing gas, feed of liquid streams and metal consumption of the equipment applied to iealization of the method.

Power inputs of cultivation process increase on 15-30% due to expenses for transportation of output gas and samples at work under pressure below 0.12 MPa. Power inputs increase 715 on 20-30% due to increase of expenses of compression eneigy of gas fee sources at woik under pressure above 1.0 MPa.

At application of natural gas as methane-oxidizing gas there is an oppoitunity to exclude expenses of compression of natural gas due to use of energy of pressure of natuial gas in 720 the main pipelines for its feeds.

The concentrated nutrient medium continuously moves into the growth medium for maintenance of methane-oxidizing microorganisms with sources of mineral feed. The concentrated nutlient medium contains sources of phosphorus, potassium, magnesium and 725 miciocells with structure, balanced by specific needs of giown up micloorganisms, that means that concentration of sources of the mineral feed containing structure of chemical compounds, dissolved in a nutrient medium is proportional to needs of grown up micloorganisms foi these feed supplies. Concentrating degiee of a nutlient medium is expressed quantitatively in units of concentration of a biomass which could be formed at all 730 consumption of sources of mineral feed in this medium.

The concentrated nutrient medium is prepared in the form of the water solution of the whole of complex of components of a mineral feed of microorganisms, balanced on theft specific need for these components, usually without inclusion of sources of a nitric feed in structure 735 of a nutrient medium. Use of the concentrated solutions of separate components of a nutrient medium or solutions of the components grouped proceeding from technological conditions of realization of the method is possible. In this case, however, feed of separate streams carry out in such parity that in recalculation on the incorporated stream of a nutrient medium propoitionality was provided between quantities of submitted feed supplies with specific needs of microorganisms for them.

Maintenance of grown up microorganisms with nitrogen is carried out by continuous feed of ammonium nitrogen in the form of watel solution of ammonia (ammonium hydroxide) or in the form of gaseous ammonia. Thus it is preferable to use feed of ammonium nitrogen for 745 simultaneous stabilization of growth medium pH.

For maintenance of optimum modes of cultivation of microolganisms and increases of a degree of use of feed components during cultivation of microorganisms the nutrient medium, and also oxygen source and methane-containing gas move to the growth medium by the 750 streams proportional to speed of consumption of corresponding feed supplies by growing microorganisms for maintenance of growing microorganisms by the feed supplies and creation of an optimum level of concentration of feed supplies in the growth medium. Speed of consumption define on one oi several palameters describing growth of micloolganisms, in particular by stream value of nitric feed source simultaneously used for stabilization of 755 growth medium pH, by speed of carbonic gas formation, by growth rate of microorganisms, by thermal emission of cultivation process.

Use of submission of mineral and gas feed sources by the streams proportional to speed of consumption of coiresponding feed supplies, provides maintenance of concentiation of feed supplies in the growth medium and, hence, in outlet liquid and gas streams from the growth 760 medium at the set levels corresponding optimum values for cultivation of microorganisms within the limits of not exceeding 10% from the set level, that provides increase of degree of use of feed supplies during cultivation and allows to carry out process of cultivation at higher growth rates and concentration of biomass of micloorganisms.

765 For maintenance of conformity between speed of consumption of the feed supplies submitted with liquid both gas streams, and volume of the liquid and gas streams submitted to the growth medium! it is provided correction of factors of proportionality between values of the corresponding streams submitted of the growth medium and parameter or complex of parameters, on which consumption speed of corresponding feed supplies of methane- 770 oxidizing microorganisms is defined in view of conformity of concentrations of reed supplies of methane-oxidizing microorganisms in outlet liquid and gas streams from the growth medium to the set optimum level.

The preferable range of correction of proportionality factor makes 1-10% from the established value. The optimum level of concentration of mineral feed sources in the growth 775 medium equal to concentration of these feed supplies in outlet liquid stream from the growth medium is defined by kinetic laws of consumption of mineral feed sources by methane-oxidizing microorganisms.

Optimum level of oxygen concentration in stream of the outlet gas from the growth medium define, on the one hand, safety condition of conducting cultivation process of methane- 780 oxidizing microorganisms and transportation of this gas, on the other hand maintenance condition of the maximal productivity of cultivation process of methane-oxidizing microorganisms by quantity of formed biomass.

Maintenance of an optimum level of concentration of feed supplies in the growth medium, submitted with a stream of the nutrient medium, is proportional to speed of their consumption 785 with correction of proportionality factor between volume of a stream and parameter on which speed of consumption is defined, by concentration values of these substances in the outlet liquid stream leads to that productivity of process of cultivation is defined by speed of mass transport of gaseous feed supplies from the gas phase into the growth medium for maintenance of grown up microorganisms with sources of gas feed -methane and oxygen.

790 Speed of mass transport depends on mass exchange characteristics of apparatuses in which cultivation process is carried out, and on driving force of mass transport, proportional to partial pressure of a corresponding component in the gas phase which is equal to product of pressure of the growth medium and volumetric concentration of a component in the gas stream which is passing through the growth medium.

At comparison of modes of cultivation with structure of the gas stream it is shown, that at realization of process above the top limit of flammability, higher values of productivity of cultivation process of methane-oxidizing microorganisms are reached, and therefore expenses for production of a unit of production decrease at identical power expenses for 800 mixing.

It is possible to accept the maintenance in this mix of oxygen as a parameter of safety of gas mixes in the field of above top limit of flammability of ballasted methane-oxygen mixes. At the content of oxygen less than 10 vol. % ballasted methane-oxygen mix is always non-flammable irrespective of the content of methane in it and at any pressure. At work with high 805 volumetric concentration of methane in structure of these mixes and pressure below 0.3-0.4 MPa the maximal safe content of oxygen can be raised up to 15%. For good safety process of cultivation and transportation of outlet gas stream from the growth medium the content of oxygen in the outlet gas stream from the growth medium support not above 10-15 vol. % depending on pressure.

810 The highest degree value of use of both components of a gas feed -methane and oxygen -is reached at performance of a condition, that transport rate of both components of the gas feed from a gas phase to the growth medium is equal to speed of their consumption by microorganisms. It is experimentally established, that at identical partial pressure in a gas phase speed of mass transport of methane from a gas phase to the growth medium is a little 815 below speed of mass transport of oxygen (on 10-15%) it means, that for maintenance of the best modes of cultivation of methane-oxidizing microorganisms the volumetric content in the outlet gas stream from the growth medium that corresponds to partial pressure of methane in a gas phase of the growth medium, in relation to the volumetric content of oxygen in outlet gas stream from the growth medium there should be above, than ratio of consumption 820 speeds of these feed supplies by methane-oxidizing microorganisms. Thus the absolute content of methane in the outlet gas can be less that the absolute content of oxygen, because it is consumed more than one volume of oxygen on one volume of methane at cultivation of methane-oxidizing microorganisms.

Preferable ranges of excess define proceeding from following reasons. The outlet gas, 825 containing methane from the growth medium can be considered as low-calorie fuel which heat of combustion is defined, mainly, by content of methane in it In connection with expediency of the fullest use of the raw material submitted during cultivation of microorganisms, and considering, that it is economically inexpedient to use it 830 completely during cultivation, also in connection with sharp increase in power expenses at use of methane from methane-containing gas more than on 90%, it is necessary to consider an opportunity of use of methane-containing gas leaving the growth medium.

Various ways of use of the outlet gas stream from the growth medium, in particular, as initial raw material for the precipitation of impurities, containing in submitted methane-containing 835 gas, or for chemical processing are possible. However the most real is use of the outlet gas stream from the growth medium as fuel for production of thermal energy, in this connection the quantity of methane-containing gas submitted to cultivation process is defined, in particular, and quantity of energy which needs to be produced at burning the outlet gas stream from the growth medium. Thus it is expedient to use outlet gas as such fuel for 840 which burning it is not required additional fuel means.

The minimal content of methane in outlet gas makes 20 vol. %, at which its use is possible as fuel for production of energy without use of additional fuel, depending on content of oxygen in it, that corresponds to excess of quantity of submitted methane with the stream of methane-containing gas concerning submitted oxygen with the stream of oxygen source in 845 comparison with ratio of quantity of consumed methane to consumed oxygen on 1-5% at realization of cultivation process of methane-oxidizing microorganisms in a mode of the minimal power expenses for biomass production due to mixing.

The maximum level of excess is defined only by quantity of energy which is necessary for produced due to burning the outlet gas stream from the growth medium, but should not be 850 above 100% as in this case the degree of use of methane sharply decreases during cultivation of methane-oxidizing microorganisms, and expenses of submission of streams of methane-containing gas and oxygen source of the growth medium.

Modes of cultivation of methane-oxidizing microorganisms, corresponding, on the one hand, to optimum consumption of methane and oxygen, and, on the other hand, safety of process 855 of cultivation of methane-oxidizing microorganisms and transportation of the outlet gas stream from the growth medium, demand, that in structure of the outlet gas stream from the growth medium there was a certain quantity of ballast gases.

A part of the outlet gas stream from the growth medium return repeatedly to the growth 860 medium, and other part direct to recycling of energy containing in it, for maintenance of adjustable quantity of the gas stream submitted on burning and content of ballast gases in it.

Application of iecalculating of the gas phase and separate feed of streams of methane-containing gas and oxygen source allows to expand area of parities between streams of methane-containing gas and oxygen source on such values which correspond to a mode of 865 optimum use of sources of gas feed, but at their submission by joint stream form combustible methane-oxygen mixes which foi this ieason cannot be used for process of cultivation of methane-oxidizing microorganisms.

The outlet gas stieam from the giowth medium has the same piessure, as pressure in the growth medium has the same pressure, as pressure in the growth medium, and possesses, 870 hence, besides the potential thermal energy used at its recycling, mechanical energy which is expedient foi using. Energy of pressure of outlet gas stream from the growth medium is used at its transportation to recycling for overcoming resistance of pipelines and the armature located in them.

Thus, fermentation process represents aerobic cultivation which is carried out in a liquid 875 nutrient medium of a reactor in which gaseous components (for example, methane, air or oxygen-rich aft, oi oxygen) with production of a by-product -caibon dioxide which is necessary to remove from a reactor with off-gas.

Micioorganisms cannot use gaseous substances directly during feimentation. Gases should be distributed in liquid that microorganisms could use them for growth of microbial mass.

880 Thus mass transport speed of substances from the gas phase in the liquid phase is above, than more small gas bubbles.

Therefore uniform distribution of gases in the liquid phase of a fermenter is the same important problem for effective carrying out of fermentation process as well as simultaneous maintenance of constancy (on all volume of a leactor) of concentration of all nutritious 885 components, medium pH and selective conditions of fermentation process, connected with it, and mass transport speed from the gas phase in the fermentation liquid phase, speed and qualitative and quantitative structure of removed gas from a feimenter, including content of caibon dioxide and the residual content of methane and oxygen in it, in view of lequirements of the guaranteed maintenance of explosion-proof concentration of oxygen in removed gas 890 mix, and as consequence, maintenance of constancy of speed and all other quantitative characteristics of fermentation process.

Characteristics of fermenter and complex of auxiliary equipment and devices used in its structure have crucial importance for maintenance of economically effective all-round and full account of all above the listed features, laws and requirements of fermentation process.

895 Usual volumetric fermenters are apparatuses with mixers which provide formation of gas bubbles in the liquid phase and their distribution in all parts of a reactor.

In usual volumetric fermenter return of a part of the gas stream the outlet gas stream from the growth medium is repeated to the growth medium or continuous circulation of a gas phase besides regulation of quantity of the gas submitted on burning, and content of ballast 900 gases in it, provides set of advantages at realization of cultivation process of methane -oxidizing microorganisms.

One of advantages of application of recycling of the outlet gas stream from the growth medium is the opportunity of increase in a degree of use of components of the gas feed -methane and oxygen during cultivation of methane-oxidizing microorganisms, especially at 905 its application as source of oxygen, oxygen-rich air, or pure oxygen.

Other advantage of application of recycling is the opportunity of use of high speeds of submission of gas streams in the growth medium, thus providing a high degree of use of components of the gas feed, which at application of recycling streams is not defined by opportunities of application of apparatuses for cultivation of microorganisms, and 910 requirements on structure of the gas streams, the defined listed conditions of maintenance of optimum conditions of a gas feed of microorganisms, safety of conducting process, transportation of the outlet gas stream from the growth medium and its use as fuel.

Recycling of gas stream can be used for the removal of part of C02 formed during cultivation, by means of passing of recycling gas stream through the known devices 915 removing carbonic gas from the gas phase.

Defects of fermenters of volumetric type are: -High expenses of energy for mixing of great volumes of the reactionary medium by means of a high-speed mixer; 920 -Hearing of reactionary mass due to its mixing by a high-speed mixer and of additional heat removal in this connection necessity; -Insufficient mass transport from the gas phase to liquid; -Bad separation of gas bubbles from liquid in the top pad of a fermenter.

Usual volumetric fomenters and ways of production of biomass of methane-oxidizing 925 microorganisms are shown in the Copyright Certificate of the USSR No. 1349244, the Patent of Russia No. 2064016.

u-shaped or loop reactor in the certain degree reduce mechanical mixing of the liquid reactionary medium, though the pump (more often axial type) used in the bottom of such fermenter for rise of the liquid phase containing bubbles of gases by an ascending pad of the 930 fermenter, in essence, also is the mixing device.

Gases (methane and air or oxygen) move separately usually in a falling part of the U-shaped or loopback rector for possibility of use of gas at rather low pressure and increases in time of contact of liquid with gas.

As such reactors have the greater total length for maintenance of necessary time of contact 935 of gas with liquid, feed of gases carry out in some points through length of a reactor, and for decrease in coalescing of bubbles of gases in addition establish static or dynamic amalgamators through length of a falling and ascending pad of a reactor after each input of gas.

Simultaneously the top part of U-shaped or loop reactor can be expanded for separation of a 940 liquid phase and gases removing from a fermenter.

U-shaped and loopback reactors are intended for realization of fermentation process basically at atmospheric pressure, though pressure can slightly raise in parts of a reactor on the discharge side of pumps or due to change of diameter of a reactor through its length due to use of pumps.

Defects of U-shaped and ioop fermenters are: -Variable concentration of components of a liquid nutrient medium and entered gas (methane and oxygen) through length of a reactor, that considerably reduces efficiency of fermentation process; 950 -Impossibility of maintenance of controllable quantity and the optimum size of gas bubbles with diametei 2-5mm in a liquid phase that reduces mass tiansport from gas to liquid in relation to potentially achievable mass tiansport at diameter of bubbles 2-5mm; -Carrying out of fermentation process at piessure close to atmospheric because of difficulty of CO2 separation from a liquid phase and stopping of process due to decrease in 955 concentration of methane and oxygen, that considerably reduces product output in relation to potential opportunities of process at the positive pressure; -Carrying out of fermentation process in the field of concentration of oxygen below the low limit of explosibility of methane that leads to selious danger of tiansition of process in a zone of explosion hazard due to not authoriz3ed increase of concentration of oxygen in a 960 fermenter (for example, in case of local increase of pressure or failures in a control system); -Necessity of use of the separate compiessor foi compression of the methane submitted in a fermenter in cases of low pressure of initial methane; -Time of stay and accoidingly different concentration of gas in zones of the reactor, submitted to different points through length of feimenter; 965 -Impossibility of qualified use of the off-gas containing the rests of not reacted methane and accordingly necessity of its emission in an atmosphere that pollutes an envilonment; -Complexity of piocess control of maintenance of environment pH in a fernienter at use of alkali for maintenance of pH = 6.0, as in ranges pH = 4-4.5 and 6-7 addition of alkali not sharply changes environment pH and additional introduction of ammonia solution for 970 updating pH is required. It reduces controllability of piocess and leads to deterioration of selective properties of environment and an opportunity of occurrence of pathogenic microbes in a reactol; -Rather small individual capacity of a reactor (up to 3.0-9.0 thousand tons from one reactor per year), defined in particular necessary and expedient time of stay of initial substances in a 975 reactor both other requirements of technology and opportunities of the equipment.

Various technical decisions of U-shaped and oop reactors and ioop fermenters with the expanded top park and fermentation methods corresponding to them are resulted in patents USA US 6,492, 135 Bl; World Intellectual Property Organization WIPO WO 03/016460 Al; 980 ECEP 1419234 (Al); WIPO WO 2010/0693132.

As the defects of U-shaped, loop reactor and loop reactor with the expanded top pad listed above are natural defects of these types of reactors and their overcoming is rather complicated, and defects of fermenters of volumetric type can be lowered essentially or even practically to eliminate due to a complex of economically comprehensible technological 985 constructive decisions. In the present invention is developed an advanced fermenter with simultaneous gas and liquid phases and with the volumetric reactor having a complex of special internal devices, allowing due to some technical decisions considerably to intensify process of growth or microorganisms and to increase biomass output from 1 M3 of the reactor.

990 According to the invention (see Fig.1) an advanced fermenter (100) consists of a reactor of volumetric type (115) with height of a liquid phase in a reactor up to lOm with remote circulating contours on liquid and gas phases simultaneously with use of ejection of the circulating gas selected from the top of a reactor, the liquid phase of a reactor selected from the bottom of a reactor and submitted by the pump (110) in ejector (112) with pressure, 995 which sufficient for ejection of input of gas-liquid mix (produced in ejector) downwards of a reactor, and maintenance during ejection distributions of gas in liquid in the form of gas bubbles with diameter 2-5 mm which is the most preferable to realization as much as possible effective mass transport from gas to liquid and achievements of the greatest biomass output per time unit. Such design of a ferment allows to exclude clearing, drying 1000 and compression by means of the compressor of re-circulating gas of a reactor and accordingly to lower considerably a power consumption considerably.

Simultaneously such design of a fermenter allows refusing use of high-speed mixer that in addition reduces power consumption at biomass production, and also excludes necessity of heat removal allocated at mixer rotation.

1005 Except for it at ejection of re-circulating gas of a reactor the liquid phase of a reactor reaches an opportunity of a controllable high degree of distribution of gas in liquid due to ejector of formation of a plenty small bubbles with optimum diameter 2-5mm set by calculation, that provides the best mass transport from gas to liquid and accordingly the best conditions for growth of microbial mass.

Gas-liquid mix from ejector moves in a vertical reactor tangentially to vertical forming surface of a reactor and under a corner to a vertical axis of a reactor for maintenance of a twisting of gas-liquid mix in a reactor and increases in time of interaction of gas and liquid phases and accordingly achievements of more effective mass transport from gas to liquid and decrease 1015 in an opportunity of coalescence of gas bubbles due to high speed of liquid, achieved by a high degree of re-circulating of gas and liquid phases, and also surface-active properties of the reaction medium.

In a reactor fermentation process carry out at pressure 0.12 MPa -1.0 MPa and temperature 42-43°C, and the positive pressure (0.3-0.4 MPa) is preferable, that provides 1020 essentially greater and economically the most favourable speed of process and accordingly greater biomass output per unit time in comparison with fermentation at pressure close to atmospheric in a loop or U-shaped reactor.

Feed of methane-containing gas is carried out in a reactor through the nozzle (124) and through the ring bubbler-distributor of gas (102) downwards of a reactor. Feed of oxygen r 1025 air is carried out in a reactor through the nozzle (123) and through the ring bubbler-distributor of gas (103) also downwards of a reactor, but above the bubbler-distributor of feed of methane-containing gas.

Use of static damper of the rotating stream (116) is provided for maintenance of good separation of gas from liquid in the top part of a fermenter. It is executed in the form of a 1030 horizontal disk with plates located vertically inside of the disk and directing rotating below gas-liquid stream in its most top in a vertical direction upwards already without rotation.

Separation of gas from liquid in the top part of a fermenter can improve also due to use of other static elements, such as horizontal grids, plates with valves or caps and liquid overfall, installation of "return" umbrella (117) at the top of a reactor and/or the cyclone or group of 1035 cyclones located at the top of a reactor.

In the reactor the internal pipe (a cup) (101), which design provides the decision of two important problems, is stipulated for selection from a reactor of liquid phase for its feed in the circulating pump of liquid phase (110): degassing of liquid phase with the purpose of exception of cavitation of the circulating pump and simultaneous exception of rotation inside 1040 of this pipe (cup) returned re-circulating liquid phase with a formation of a cone in it because of rotations of liquid phase inside of a reactor around the given pipe (cup), on the one hand, and, on the other hand, high-speed movement of liquid phase downwards inside of the pipe (cup) (with speed of 1.5-2.0 km/s), for prevention of gas inrush through a cone which narrow end is turned downwards into the pipe (cup), to the circulating pump, due to installation of a 1045 cone damper (104) on top of the internal pip (cup), looking like disk with vertical directing streams and stopping rotation of liquid inside of the pipe (cup).

The pipeline (125) is introduced inside of the pipe (cup) through the nozzle in a reactor (120) for feed of ammonia solution for regulation medium pH, which at such way of its feed provides as much as possible operative maintenance of process demanded for technology 1050 and maintenance of selective acidities of medium (pH = 5.6) in a fermenter.

The pipeline of re-circulating liquid phase (107) is used also for input of solution of salts and microcells with the set concentration of each component and fresh water in it that allows providing practically constant concentration of all components of a nutrient medium in a fermenter at used frequency rate of circulation of liquid phase (30-50).

1055 Heat pick up of process of biosynthesis is carried out by cooling liquid phase in a vertical heat exchanger (111), established on the discharge side of the circulating pump of liquid phase (110) and providing maintenance of optimum temperature in a fermenter for process of growth of microorganisms (42-43°C).

The re-circulating part of gas phase of a reactor continuously moves in an ejector (112) in 1060 which is entrained by the re-circulating stream of liquid phase with the necessary pressure provided by the circulating pump of liquid phase (110), and is distributed in the form of a plenty small bubbles in liquid phase. The ejector design is made in such a manner that at ejection of gas in liquid diameter of gas bubbles makes 2-5 mm that provides maximal mass transport from gas to liquid during fermentation and accordingly achievement of the maximal 1065 growth rate microorganisms and the greatest output of biomass per unit time.

Outlet gas-liquid stream with gas bubbles distributed inside of it from ejector moves tangentially in the bottom part of a reactor through the nozzle (114) to vertical forming walls of a reactor and under corner 10-30° to a vertical axis of a reactor for twisting of the 1070 fermentative medium and course of process of biosynthesis of microorganisms in a reactor at maximal mass transport from gas to liquid, at constant optimum concentration of all of macro-and microcells of a nutrient medium, nitrogen, methane, oxygen and phosphorus, at constant acidity of medium (pH = 5.6), providing selective conditions of fermentation process, at constant safe concentration of oxygen (1 0-1 5%) -depending on pressure in a 1075 fermenter) from the point of view of explosion, at constant selection of produced biomass suspension which is carried out through the nozzle (122) in the top part of a reactor, at constant quantity and contents of removed off-gas from a fermenter with constant content of methane (20 vol. %), minimally necessary for possibility of its recycling by burning for generation of thermal energy used by biomass drying.

1080 Pressure in a reactor is supported by pressure of gas in the top part of a reactor, and protection of a reactor against potentially possible excess of pressure in relation to design pressure is provided due to an explosive membrane (121).

Fermenter and fermentation method under the present invention allow to use not less than 90-95% of initial gas (methane) and to produce biomass with the greatest possible 1085 efficiency.

Fermenter and fermentation method under the present invention allow to have economically possible much greater individual capacity of a fermenter (not less than 10.0 th.t. of biomass per year from one reactor) from the constructive and technological points of view, than capacity of U-shaped either loop fermenter or loop fermenter with the expanded top part (i.e. 1090 in 1.3-3.5 times) that essentially reduces quantity of fermenters and accordingly expenses for creation (on 15-40%) and operational expenses (on 10-20%) of plants.

Example:

Culture Methylococcus capsulatus strain BCb -874 is grown up in a fermenter in conditions of continuous cultivation. Working volume of the fermenter is 300m3.

Process of cultivation is carried out on the simple mineral mediums consisting from orthophosphoris acid, chlorides of potassium, magnesium, iron and sulphates of copper, manganese, zinc, cobalt, boric acid and sodium molybdate as microadditives. During manufacture natural gas is used as a unique source of carbon and energy. Process is 1100 carried out with participation of oxygen.

Process is carried out in a mode of re-circulation of a gas phase.

Medium pH is supported by means of ammoniac water which simultaneously is a source of nitrogen, at level 5.6 + 0.1. in a fermenter the temperature is supported at level 42-43°C with use of a remote heat exchanger, located on three contours of re-circulation of liquid 1105 medium.

In apparatus pressure is 3 atmg (0,4 MPa (abs)). Outlet gas from the apparatus recycles by means of an ejector in the bottom part of the apparatus in quantity 7500 m3/hour (30000 Nm3/hour). Fresh natural gas (95%) and oxygen (95%) in quantity 2440 Nm3/hour and 3100 Nm3/hour accordingly moves in bubblers of the apparatus. Quantity of the off-gas 1110 removed through the nozzle of the top cover of the fermenter is 700 Nni3. Content of methane in off-gas is 20% oxygen -10%. A degree of use of oxygen is 98%. A degree of use of methane is 95%.

Process of continuous cultivation is carried out at stream speed 0.25 hr, biomass concentration in the cultivation medium is 20 gIl under dry weight. Hour biomass capacity of 1115 the apparatus is 1500 kg/hours.

Suspension leaving the device is decontaminated, concentrates, in activated, dried and packed.

Off-gas is utilized in power installations where it is burnt with addition of additional air.

1120 Features of the invention * Fermenter (100), consisting of a volumetric reactor (115) equipped by a complex of internal devices; an internal cup for removal of re-circulating liquid phase (101), a damper of cone from rotation and at movement downwards liquids in the reactor (104), a damper-separator of gas and liquid phases providing their effective 1125 separation at a top of the reactor (116), a ring bubbler-distributor of methane-containing gas (102), a ring bubbler-distributor of oxygen or air (103), the nozzle for output of biomass suspension from the fermenter (122), the nozzle (118) for input of a nutrient medium in the pipeline of outlet of re-circulating liquid phase (107) of the reactor, the nozzle (119) for input of fresh water in the same pipeline 1130 and an external circulating contour, including a pump for re-circulation of liquid phase of the reactor (110), a vertical heat exchanger for removal of heat of fermentation process (111), an ejector (112) for input of re-circulating gas in re-circulating liquid and dispergation of re-circulating gas phase in the form of gas bubbles with diameter 2-5mm in re-circulating liquid phase, a pipeline for removal 1135 of liquid re-circulating phase from the reactor (107) through a nozzle in a bottom of the reactor (105), a pipeline for removal of gas re-circulating phase from the reactor (109) through the nozzle at a top of the reactor (106), the pipeline for feeding of gas liquid mix into the reactor (113) thorough a nozzle in a bottom of the reactor (114), located tangentially to vertical forming of the reactor shell under 1140 a corner to a vertical axis of the apparatus for maintenance of rotation of gas liquid mix in the reactor upwards. In the reactor pressure is controlled by the measuring device established in the nozzle (127), located in the top part of the fermenter in off gas stream, and content of off-gas of the reactor and, in particular content of oxygen in it is controlled by the analyzer of continuous action, which sample 1145 device is established in the nozzle (126) located in the pipeline (128) of off-gas from the fermenter.

* Fermenter under item 1 characterized that two and more external circulating contour are used for one reactor for simultaneous recirculation of gas and liquid 1150 phases of the reactor.

* Fermenter under item 1 characterized that the sample device for the analyzer for the control of control of off-gas, in particular content of oxygen in it, and the measuring device for control of pressure in fermenter are established directly in 1155 nozzles on the top cover of the reactor.

* Fermenter under item 1 characterized that a horizontal grid or a plate with valves or caps with overflow of liquid or a cyclone or group of cyclones are used as the 1160 device for effective separation of gas and liquid phases at the top of the reactor (116).

* Fermenter under item 1 characterized that input of ammonia solution in the reactor, is carried out through the nozzle in addition established in the pipeline of 1165 outlet of re-circulating liquid phase from the reactor (107).

* Fermenter under item 1 characterized that for feed of fresh methane-containing gas having low pressure which is not enough for its direct input in the reactor through the nozzle in the reactor (124) and the ring bubbler-distributor of 1170 submitted gas (102), feed of fresh methane containing gas is carried out similarly to input of re-circulating gas in the reactor with use of an additional separate external contour of re-circulation of liquid phase of the reactor into which methane-containing gas of low pressure is entered through the ejector.

1175 * Fermentation method in which process is carried out input in the liquid nutrient medium containing water solution of salts and microcells with maintenance of constant medium pH due to input of ammonia solution in it, and submitted in Fermnenter, with a reactor of volumetric type with a complex intemal devices and external re-circulating contour in which gas and liquid phases of methane- 1180 containing gas, gaseous oxygen or oxygen enriched air or air and at presence of methane-oxidizing microorganisms, characterized that re-circulation of gas and liquid phases is carried out simultaneously with separate outlet of these phases from top and bottom of the reactor accordingly, and their joint input in the bottom of the reactor due to ejection of gas phase of the reactor in the ejector (112) of 1185 liquid phase of the reactor which pressure preliminary rises by the circulating pump (110) of external circulating contour.

* Fermentation method under item 7 characterized that the ejector (112) of external circulating contour of fermenter provide dispergation of re-circulating gas phase of 1190 the reactor in liquid phase of the reactor with controllable formation of gas bubbles with diameter 2-5mm, providing maximal mass transport from gas to liquid during fermentation.

* Fermentation method under item 7, characterized that fermentation process in the 1195 reactor of volumetric type (115) is carried out in gas liquid medium rotating inside of the reactor due to input of gas liquid mix from ejector (112) into the bottom of the reactor tangentially to vertical forming (shell) of the reactor under a corner to a vertical axis of the reactor.

* Fermentation method under item 7, characterized that outlet of recirculation liquid 1200 phase is carried out from the bottom of the reactor with preliminary degassing and lamination of the steam of this liquid phase inside of the reactor due to the device of an internal cup (101) in the reactor with a damper of cone (104) from rotation of the reactionary medium around of the cup and movement of liquid downwards in the top park of the glass in the reactor.

1205 * Fermentation method under item 7, characterized that effective separation of gas and liquid phases at the top of the reactor is carried out due to the damper separator of gas and liquid phases in the top part of gas liquid mix in the reactor (116) in the form of a horizontal disk with vertical guides inside of it.

* Fermentation method under item 7,1 characterized that (a return umbrella) (117) 1210 with a drain aperture in the middle of a plate with valves or caps and a drain pipe or a cyclone or group of cyclones is installed for prevention of liquid loss with departing and re-circulating gas in the top part of the reactor.

* Fermentation method under item 7, characterized that maintenance of constant temperature in fermenter (42-43°C) is carried out due to remove heat of 1215 fermentation process in heat exchanger (11 1), installed in a remote circulating contour, as a rule, on the party of discharge of the circulating pump (110) of liquid phases.

* Fermentaqtion method under item 7, characterized that fermentation process is carried out ant concentration of oxygen in off-gas not above 10-15 vol. % 1220 depending on fermentation pressure and maintenance of concentration of methane in off-gas of 20-25 vol. % for a possibility of explosion safety of the process qualified use of off-gas for generation of thermal energy and prevention of emissions of the rests of hydrocarbons from fermenter in an environment.

* Fermentation method under item 7, characterized that input fresh methane- 1225 containing gas and oxygen or air in the reactor is carried out in the bottom part of the reactor through the ring bubbler-distributors of gases, and a ring for distribution of oxygen is installed above a ring for distribution of methane.

* Fermentation method under item 7, characterized that fermentation process in carried out at the optimal positive pressure (0.3-0.4 MPa) for achievement of 1230 economically expedient maximal fermentation speed.

* Fermentation method under item 7, characterized that fermentation process in fermenter (100) is carried out at maintenance of all constant optimal values of all transport from gas to liquid, maintenance of explosion-proof concentration of oxygen in gas phase, maintenance of content of components of off-gas providing 1235 its qualified use and preventing emissions of hydrocarbons in an environment with maintenance of the maximal speed of process, use of methane up to 95% reaching of the maximal output of biomass per unit time, a possibility of economically expedient and possible use of fermenters with the big individual capacity of 10.0 thousand tons per year and more) and decrease of cost of 1240 manufactures on 15-40% and decrease of operational expenses on 20-25%.

Claims (18)

1. Claims 1. A fermenter comprising a volumetric reactor having a liquid re circulation loop and a gas re circulation loop, further comprising an ejector arranged to input re circulating gas into re circulating liquid such that the combined gas-liquid mixture is fed back into 1245 a bottom portion of the volumetric reactor.
2. 2. A fermenter (100), comprising a volumetric reactor (115), arranged to provide gas and liquid phases of the reactor, an internal pipe arranged to remove a re-circulating liquid phase (101), a cone damper (104) located on top of the internal pipe arranged to stop 1250 rotation of the liquid inside the pipe in the reactor, a damper-separator (116) arranged to provide effective separation of gas and liquid phases at the top of the reactor, a ring bubbler-distributor (102) for methane-containing gas, a ring bubbler-distributor (103) for oxygen or air, an output nozzle (122) for output of a biomass suspension from the fermenter (122), a first input nozzle (118) for input of a nutrient medium into a pipeline 1255 at an outlet (107) of a re-circulating liquid phase of the reactor, a second nozzle (119) for input of fresh water in the pipeline and an external circulating loop, including a pump (110) for re-circulation of liquid phase of the reactor, a vertical heat exchanger (111) for removal of heat from the fermentation process, an ejector (112) for the addition of a re-circulating gas into the re-circulating liquid such that the gas is 1260 distributed in the form of small bubbles in the re-circulating liquid phase, a pipeline (107) for removal of liquid from the re-circulating phase from the reactor through a nozzle (105) in a bottom of the reactor, a pipeline (109) for removal of gas re-circulating phase from the reactor through the nozzle (106) at a top of the reactor, the pipeline (113) for feeding of gas liquid mix into the reactor thorough a nozzle (114) in 1265 a bottom of the reactor, the pipeline located tangentially to vertical axis forming the reactor shell under a corner of the apparatus arranged to maintain rotation of gas liquid mix in the reactor upwards, wherein the reactor pressure is controlled by a measuring device established in the nozzle (127), located in the top part of the fermenter in off gas stream, and whereby the content of the off-gas of the reactor and, 1270 in particular the content of the oxygen in it is sampled with a sampling device in the nozzle (126) located in the pipeline (128) of the off-gas from the fermenter and is controlled by the continuous analyzer action.
3. 3. A fermenter as claimed in claim 2 characterised in that two or more external 1275 circulating loops are used in one reactor for simultaneous recirculation of gas and liquid phases of the reactor.
4. 4. A fermenter as claimed in claim 2 characterised in that the sampling device for the analyzer for the control of control of off-gas, in particular content of oxygen in it, and 1280 the measuring device for control of pressure in fermenter are established directly in nozzles on the top cover of the reactor.
5. 5. A fermenter as claimed in claim 2 characterised in that a horizontal grid or a plate with valves or caps is provided with an overflow of liquid or a cyclone or group of 1285 cyclones are used as a device for effective separation of gas and liquid phases at the top of the reactor (116).
6. 6. A fermenter as claimed in claim 2 characterised in that the input of ammonia solution in the reactor is carried out through the nozzle and further comprising a 1290 pipeline at the outlet of re-circulating liquid phase from the reactor (107).
7. 7. A fermenter as claimed in claim 2 characterised in that for feed of fresh methane-containing gas having low pressure which is not enough for its direct input in the reactor through the nozzle in the reactor (124) and the ring bubbler-distributor of 1295 submitted gas (102), feed of fresh methane containing gas is carried out similarly to input of re-circulating gas in the reactor with use of an additional separate external contour of re-circulation of liquid phase of the reactor into which methane-containing gas of low pressure is entered through the ejector.

   1300
8. 8. A fermentation method in which the process carried out is input in the liquid nutrient medium containing water solution of salts and microcells with maintenance of constant medium pH due to input of ammonia solution in it, and submitted in Fermenter, with a reactor of volumetiic type with a complex internal devices and external re-circulating contour in which gas and liquid phases of methane-containing 1305 gas, gaseous oxygen or oxygen enriched air or air and at presence of methane-oxidizing microorganisms, characterized that re-circulation of gas and liquid phases is carried out simultaneously with separate outlet of these phases from top and bottom of the reactor accordingly, and their joint input in the bottom of the reactor due to ejection of gas phase of the reactor in the ejector (112) of liquid phase of the 1310 reactor which pressure preliminary rises by the circulating pump (110) of external circulating contour.
9. 9. Fermentation method as claimed in claim 8 characterized that the ejector (112) of external circulating contour of fermenter provide dispergation of re-circulating gas 1315 phase of the reactor in liquid phase of the reactor with controllable formation of gas bubbles with diameter 2-5mm, providing maximal mass transport from gas to liquid during fermentation.
10. 10. Fermentation method as claimed in claim 8, characterized that fermentation 1320 process in the reactor of volumetric type (115) is carried out in gas liquid medium rotating inside of the reactor due to input of gas liquid mix from ejector (112) into the bottom of the reactor tangentially to vertical forming (shell) of the reactor under a corner to a vertical axis of the reactor.
11. 11. Fermentation method as claimed in claim 8, characterized that outlet of 1325 recirculation liquid phase is carried out from the bottom of the reactor with preliminary degassing and lamination of the steam of this liquid phase inside of the reactor due to the device of an internal cup (101) in the reactor with a damper of cone (104) from rotation of the reactionary medium around of the cup and movement of liquid downwards in the top park of the glass in the reactor.

    1330
12. 12. Fermentation method as claimed in claim 8, characterized that effective separation of gas and liquid phases at the top of the reactor is carried out due to the damper separator of gas and liquid phases in the top part of gas liquid mix in the reactor (116) in the form of a horizontal disk with vertical guides inside of it.
13. 13. Fermentation method as claimed in claim 8, characterized that (a return umbrella) 1335 (117) with a drain aperture in the middle of a plate with valves or caps and a drain pipe or a cyclone or group of cyclones is installed for prevention of liquid loss with departing and re-circulating gas in the top part of the reactor.
14. 14. Fermentation method as claimed in claim 8, characterized that maintenance of constant temperature in fermenter (42-43°C) is carried out due to remove heat of 1340 fermentation process in heat exchanger (111), installed in a remote circulating contour, as a rule, on the party of discharge of the circulating pump (110) of liquid phases.
15. 15. Fermentation method as claimed in claim 8, characterized that fermentation process is carried out ant concentration of oxygen in off-gas not above 10-15 vol. % 1345 depending on fermentation pressure and maintenance of concentration of methane in off-gas of 20-25 vol. % for a possibility of explosion safety of the process qualified use of off-gas for generation of thermal energy and prevention of emissions of the rests of hydrocarbons from fermenter in an environment.
16. 16. Fermentation method as claimed in claim 8, characterized that input fresh 1350 methane-containing gas and oxygen or air in the reactor is carried out in the bottom part of the reactor through the ring bubbler-distributors of gases, and a ring for distribution of oxygen is installed above a ring for distribution of methane.
17. 17. Fermentation method as claimed in claim 8, characterized that fermentation process in carried out at the optimal positive pressure (0.3-0.4 MPa) for achievement 1355 of economically expedient maximal fermentation speed.
18. 18. Fermentation method as claimed in claim 8, characterized that fermentation process in fermenter (100) is carried out at maintenance of all constant optimal values of all transport from gas to liquid, maintenance of explosion-proof concentration of oxygen in gas phase, maintenance of content of components of off- 1360 gas providing its qualified use and preventing emissions of hydrocarbons in an environment with maintenance of the maximal speed of process, use of methane up to 95% reaching of the maximal output of biomass per unit time, a possibility of economically expedient and possible use of fermenters with the big individual capacity of 10.0 thousand tons per year and more) and decrease of cost of 1365 manufactures on 15-40% and decrease of operational expenses on 20-25%.