KR20180124348A - An Hydrogen Manufacturing Apparatus and a Method of Producing Hydrogen using Thereof - Google Patents

Abstract

The present invention relates to an apparatus for manufacturing hydrogen from raw material gas containing a large amount of carbon monoxide by using microorganism, and to a method for manufacturing hydrogen using the same. In particular, the present invention does not require to have a heat exchanger for pre-heating feed gas as a biological aqueous gas conversion process using microorganisms and separate steam to reduce construction and operating costs so that the apparatus does not require a catalyst and can achieve the conversion rate of the carbon monoxide of nearly 100% by one reactor.

Description

[0001] The present invention relates to an apparatus for producing hydrogen and a method for producing hydrogen using the same,

More particularly, the present invention relates to a device for producing hydrogen from a gas containing carbon monoxide by using microorganisms and a method for producing hydrogen by using the same. BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a hydrogen production apparatus and a method for producing hydrogen using the same, .

Gas containing carbon monoxide, which is produced in large quantities, includes syngas produced through coal gasification or natural gas reforming, and by-product gas produced as a by-product in steelworks or petrochemical processes.

Coal gasification technology is a technology to produce syngas composed mainly of carbon monoxide and hydrogen through gasification reaction at high temperature and high pressure without directly burning coal. Through this gasification technology, coal can be used efficiently and environmentally clean have.

COG (Coke Oven Gas), BFG (Blast Furnace Gas), LDG (Linze Dnawitz Gas) and converter gas are the by-products of the steelworks. LDG is the most carbon monoxide in the by-product gas of the steelworks.

In order to produce hydrogen by using a gas containing a large amount of carbon monoxide such as syngas or byproduct gas (hereinafter, referred to as 'raw material gas' or BG), a water gas conversion process is performed. Conventionally, a thermochemical water gas conversion process is mainly utilized . FIG. 1 is a simplified schematic diagram of an entire process 100 for producing hydrogen from synthesis gas through common coal gasification.

As shown in FIG. 1, the air separation apparatus 110 first separates the introduced air into oxygen and nitrogen, and then supplies oxygen as an oxidizing agent to the gasification apparatus 120. The gasifier 120 supplied with oxygen from the air separation unit 110 generates synthesis gas (CO, H ₂ , CO ₂ , CH ₄ , H ₂ S, etc.) by incomplete combustion and gasification of coal. The syngas and scrubber 130 cleans impurities of the syngas produced in the gasification unit 120, and provides cooling to the water gas shift unit 140. The water gas shift device 140 provided with the syngas cooled from the syngas cooler 130 converts the carbon monoxide into carbon dioxide and hydrogen through a water gas conversion reaction (CO + H ₂ O? CO ₂ + H ₂ ) And supplies the generated gas to the syngas purification apparatus 150. The syngas purifier 150 purifies carbon dioxide, hydrogen, a product gas mainly composed of methane (CH4), and supplies it to the carbon dioxide separator 160. [ The carbon dioxide separator 160, which receives the generated gas from the syngas purifier 150, separates carbon dioxide from the generated gas and supplies the separated carbon dioxide to a carbon dioxide processor (not shown). Pressure swing adsorption (PSA) 170, which is supplied with purified gas from the carbon dioxide separator 160, is a method of desorbing gas from the adsorbent by increasing the pressure to adsorb the gas to the adsorbent and lowering the pressure Separate the hydrogen. The hydrogen separated from the pressure swing adsorption device 170 can be used for power generation using the gas turbine or the fuel cell or as the raw material itself. Residual gas, other than hydrogen, used as a feedstock is provided to the gas turbine (180). The high-temperature combustion gas discharged from the combustor of the gas turbine 180 is supplied to the waste heat recovering device 181. The waste heat recovering device 181 recovers the waste heat discharged from the combustion gas discharged from the gas turbine 180 and provides it to the steam turbine 182 for generating steam.

A conventional thermochemical water gas conversion process 10 for producing hydrogen using syngas or by-product gas is shown in detail in FIG. 2, although some detailed configurations may differ depending on the type of source gas BG to be supplied . This corresponds to the detailed configuration of the water gas shift device 140 of FIG.

As shown in FIG. 2, the thermochemical water gas conversion process includes a high temperature water gas conversion reactor 13 operating at a high temperature of 350 to 450 ° C. and a low temperature water gas conversion reactor 15 (low temperature water gas conversion reactor) ). A first cooler 14 such as a cooler or a heat exchanger for cooling the gas temperature to 250 ° C should be installed between the high temperature water gas shift reactor 13 and the low temperature water gas shift reactor 15, A second cooler 16 for cooling the gas temperature reacted at 300 ° C to 350 ° C should also be provided.

The hydrogen production reaction proceeds rapidly through the hot water gas shift reactor 13, but the conversion rate is thermodynamically low. Therefore, it is necessary to convert the remaining carbon monoxide into hydrogen through the low temperature water gas shift reactor (15). The reaction rate of the low temperature water gas conversion reaction is relatively low in comparison with the high temperature water gas conversion reaction, but has a merit that a high conversion rate can be obtained. Thus, in order to obtain hydrogen through the existing thermochemical water gas conversion reaction, two or more reactors (13, 15) operating at high temperature and low temperature are required.

In addition, in order to perform a high-temperature water gas conversion reaction, it is necessary to preheat the temperature of the introduced gas to 250 ° C which is the active temperature of the catalyst (Cu, Fe, Co-Mo, etc.) The device 12 must be installed.

Thus, in the conventional water gas conversion step, the gas preheating device 11 that flows into the high temperature / low temperature water gas conversion reactor and the high temperature water gas conversion reactor 13, the steam supply device 12 necessary for the water gas conversion reaction, A heat exchanger 14 for cooling the gas discharged from the conversion reactor, and the like. In order to adjust the temperature of each reactor, there is a difficulty in the process such as gas preheating or heat exchanger condition must be predetermined.

Recently, the biogas water gas conversion process, which is focused on, is a process for producing hydrogen using a microbial water gas conversion reaction. The biological water gas conversion reaction using microorganisms is different in that the thermochemical water gas conversion reaction and the reaction formula are the same as each other but the microorganism is used instead of the catalyst for the thermochemical water gas conversion reaction.

CO (g) + H ₂ O (1)? H ₂ (g) + CO ₂ (g)? H = 2.8 KJ / mol

The technical contents related to the biological water gas conversion process are described in Patent Documents 1, 2, and 3. Conventional patent documents disclose only the basic contents of the basic process and batch type related to the biological water gas conversion process, and the configuration for improving the overall reaction efficiency by constituting a continuous process using the raw material gas has been studied none.

Patent Registration No. 1401565 Patent Registration No. 1401559 Patent Registration No. 1401563

Disclosure of Invention Technical Problem [8] Accordingly, the present invention is directed to a continuous process for producing hydrogen from carbon monoxide contained in a raw material gas, using hydrogen-producing microorganisms. The present invention eliminates the need for a heat exchanger for preheating the feed gas and reduces the construction cost and operating cost by eliminating the need to supply additional steam, and it is also possible to produce hydrogen that can achieve a conversion rate of carbon monoxide And a method for producing hydrogen using the same.

In order to solve the above problems, a first aspect of the present invention provides a method for producing a fermented milk, comprising: a raw material mixing tank (TK-106) for mixing yeast extract, anaerobic digestion filtrate (AL) and seawater; (R-101, 102, 103) in which a water gas conversion reaction by a microorganism takes place using a raw gas (BG) containing carbon monoxide and a raw material supplied from the raw material mixing tank (TK-106) ; A separator (TK-110) for separating the waste medium generated from the microbial reactors (R-101, 102, 103) into waste solid and waste liquid; A waste liquid discharge tank (TK) for producing an incineration waste gas (PG) from the waste liquid supplied from the separator (TK-110) and the following condensate supplied from the following condenser separator (TK-107) -108); A water gas cooler (E-101) for cooling a water gas containing a large amount of hydrogen generated in the microbial reactors (R-101, 102, 103); (PDG) as a main component from the cooled water gas supplied from the water gas cooler (E-101) to the upper end and a condensate to the waste liquid discharge tank (TK-108) (BG) including a condenser / separator (TK-107) for converting a microbial water gas into a raw gas (BG).

The second aspect of the present invention is a method for converting a microbial water gas conversion reaction from a raw material gas (BG) to which a seawater heater (E-102) capable of heating seawater is added before mixing seawater into the raw material mixing tank (TK-106) Thereby producing an aqueous gas.

The third aspect of the present invention provides an apparatus for producing a water gas through a microbial water gas conversion reaction from a feed gas (BG) which is Thermococcus onnurineus.

In a fourth aspect of the present invention, the microbial reactor is a microbial reactor having a reactor internal steam pipe and a heat transfer fin extending from the steam pipe so as to maintain the temperature of the zone where the microbial water gas conversion reaction occurs, An apparatus for producing a water gas through a microbial water gas conversion reaction from a gas (BG).

A fifth aspect of the present invention is a method for producing a yeast extract, comprising: 1) preparing a raw material by mixing yeast extract, anaerobic digestion filtrate (AL) and seawater; 2) supplying raw material gas (BG) containing carbon monoxide and the raw material prepared in the step 1) to at least one microbial reactor (R-101, 102, 103) in which a water gas conversion reaction with microorganisms occurs; 3) performing a water gas conversion reaction using microorganisms in the at least one microbial reactor (R-101, 102, 103); 4) separating the waste medium produced from the microbial reactor into a waste solid and a waste liquid; 5) producing an incineration waste gas (PG) from the waste liquid and a condensate generated by cooling the water gas below; 6) cooling a water gas containing a large amount of hydrogen generated in the microbial reactor to generate a water-based gas (PDG) containing hydrogen as a main component and discharging a condensate; and the steps 1) to 6) (BG), which is a continuous process which is carried out at the same time, except for the up-and-down and shut-down processes.

In a sixth aspect of the present invention, there is provided a method for producing a water gas from a raw material gas (BG) compressed and supplied at a pressure of 10 atm or higher by a microbial water gas conversion reaction in a raw material gas (BG) containing carbon monoxide in the step 2) to provide.

A seventh aspect of the present invention provides a method for producing a water gas through a microbial water gas conversion reaction from a raw gas (BG) at a pressure of 70 to 80 atm.

In the eighth aspect of the present invention, in the step 3), the temperature of the zone where the microbial water gas conversion reaction occurs in the microbial reactor is 80 ° C or more and less than 90 ° C, and the microorganism is Thermoglass (Thermococcus onnurineus) To a microbial water-gas conversion reaction.

In a ninth aspect of the present invention, steam is supplied to a steam pipe inside a reactor having a radiating fin extending from the steam pipe so as to maintain the temperature, and water is supplied from the raw gas (BG) Providing a method of producing gas.

The tenth aspect of the present invention provides a method for producing a water gas through a microbial water gas conversion reaction from a raw material gas (BG) in which the yeast extract and the anaerobic digestion filtrate (AL) are mixed at the same volume in the step 1) .

The eleventh aspect of the present invention provides a method for producing a water gas from a raw material gas (BG) having a pH of 6.8 in the microbial reactor (R-101, 102, 103) do.

The present invention relates to a continuous process for producing hydrogen from carbon monoxide contained in a raw material gas, and uses hydrogen-producing microorganisms for the water gas conversion reaction.

The present invention eliminates the need for a heat exchanger to preheat the feed gas, eliminates the need for a separate steam or heating device, reduces construction and operating costs, and allows a single reactor to achieve a conversion rate of carbon monoxide close to 100% without the need for a catalyst.

In contrast to the conventional thermochemical water gas conversion process being an exothermic reaction, the biological water gas conversion process according to the present invention requires only a small amount of energy supply due to a weak endothermic reaction and is thus easy to operate.

In addition, the method of producing hydrogen according to the present invention is not only capable of continuous operation, but also uses a plurality of biological reactors to continuously stop the process even in the periodic cleaning and the like necessary for the operation of the biological reactor It is advantageous to be able to operate.

In addition, the present invention has diversified the energy source of the microorganisms used in the biological water gas conversion process. It is possible to further use the anaerobic digestion filtrate in addition to the conventional yeast extract, thereby remarkably reducing the cost due to the hydrogen production, and there is an additional advantage that the environmental waste can be rehabilitated.

Also, by selecting a material suitable for each process, there is a strong resistance to corrosion caused by seawater used in the reaction.

In addition, waste liquid and waste solid generated in the process can be treated at once.

1 is an overall process for producing hydrogen through general coal gasification.
2 is a conventional thermochemical water gas conversion process.
3 is a biological hydrogen production process capable of producing hydrogen from a raw material gas using the microorganism according to the present invention.

Hereinafter, the present invention will be described in detail. Prior to this, terms and words used in the present specification and claims should not be construed as limited to ordinary or dictionary terms, and the inventor may designate the concept of a term appropriately in order to describe its own invention in the best way possible. It should be interpreted as meaning and concept consistent with the technical idea of the present invention. Therefore, it is to be understood that the present invention may be embodied in many other specific forms such as those described in the following embodiments, It should be understood that variations can be made.

DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENTS Hereinafter, preferred embodiments of the present invention will be described in detail with reference to the accompanying drawings. In addition, the following examples can be modified in various forms, and the scope of the present invention is not limited to the following examples.

The apparatus according to the present invention comprises: a raw material gas compressor (C-101) for compressing a raw gas (BG) containing a large amount of carbon monoxide; A yeast extract storage tank (TK-102) capable of storing yeast extract (YEAST) as a primary energy source of microorganisms according to the present invention; A seawater storage tank (TK-104) for receiving and storing seawater (SW); A seawater heater (E-102) for heating seawater of the seawater storage tank (TK-104) before being supplied to the yeast extract tank (TK-103) and the raw material mixing tank (TK-106); A yeast extract tank (TK-103) for mixing yeast extract supplied from the yeast extract storage tank (TK-102) and seawater heated by the seawater heater (E-102); Anaerobic digestion filtrate storage tank (TK-105) for storing anaerobic digestion filtrate (AL); A raw material mixing tank for mixing and storing a yeast extract from the yeast extract tank (TK-103), anaerobic digestion filtrate from the anaerobic digestion filtrate storage tank (TK-105) and seawater heated by a seawater heater (E-103) TK-106); A basic solution storage tank (TK-101) capable of storing a basic solution; A raw material gas is fed from the raw material gas compressor (C-101), a raw material is fed from the raw material mixing tank (TK-106) At least one microbial reactor (R-101, 102, 103) for receiving a basic solution from the basic solution storage tank (TK-101) and performing a water gas conversion reaction by microorganisms; A waste medium storage tank (TK-109) for storing a waste medium (WM) generated from the microbial reactor; A separator (TK-110) for separating the waste medium supplied to the waste media storage tank (TK-109) into waste solid (WS) and waste liquid (WL); A waste solid discharge tank (TK-111) for storing a waste solid (WS) supplied from the separator (TK-110) for discharging; The waste liquid (WL) supplied from the separator (TK-110) and the waste liquid (PG) for incineration from the condensate supplied from the condensate separator (TK-107) A discharge tank (TK-108); A water gas cooler (E-101) for cooling a water gas containing a large amount of hydrogen produced in the microbial reactors (R-101, 102, 103); The condensed water gas supplied from the water gas cooler (E-101) is condensed to discharge the water gas mainly composed of hydrogen gas to the upper end, and the condensate to be supplied to the waste liquid discharge tank (TK-108) Separator (TK-107).

The method for producing hydrogen using the apparatus according to the present invention comprises the steps of: 1) compressing a raw material gas (BG) containing carbon monoxide by using a raw material gas compressor (C-101); 2) storing the yeast extract in a yeast extract storage tank (TK-102); 3) storing seawater in a seawater storage tank (TK-104); 4) storing the anaerobic digestion filtrate in the anaerobic digestion filtrate storage tank (TK-105); 5) storing a basic solution in a basic solution storage tank (TK-101); 6) The yeast extract supplied from the yeast extract storage tank (TK-102) and seawater supplied from the seawater storage tank (TK-103) were heated using a heater (E-102) ); 7) While supplying the yeast extract of the yeast extract tank (TK-103) and the anaerobic digestion filtrate of the anaerobic digestion filtrate storage tank (TK-105) to the raw material mixing tank (TK-106) -103) is heated using a seawater heater (E-103) and then supplied to a raw material mixing tank (TK-106); 8) The raw material gas compressed from the raw material gas compressor (C-101) is supplied to the raw material mixing tank (TK-106) Supplying basic solutions from the basic solution storage tank (TK-101) to the at least one microbial reactor (R-101, 102, 103); 9) performing a water gas conversion reaction using microorganisms in the at least one microbial reactor (R-101, 102, 103); 10) discharging a waste medium generated from the microorganism reactor and storing the waste medium in a waste medium storage tank (TK-109); 11) separating the waste medium supplied to the waste media storage tank (TK-109) into waste solid and waste liquid in a separator (TK-110); 12) storing the waste solid in a waste solid waste discharge tank (TK-111) for discharging the waste solid supplied from the separator (TK-110); 13) The waste liquid supplied from the separator TK-110 and the condensate supplied from the condenser separator TK-107 are produced from the waste liquid discharge tank TK-108 to the upper end thereof, Discharging the waste liquid to the lower end; 14) cooling a water gas containing a large amount of hydrogen produced in the microbial reactors (R-101, 102, 103) in a water gas cooler (E-101); 15) Condensate the cooled aqueous gas supplied from the water gas cooler (E-101) in the condenser / separator (TK-107) to discharge the water gas mainly composed of hydrogen gas to the upper end and discharge the condensed liquid to the lower end To the tank (TK-108), wherein the steps 1) to 15) are performed simultaneously except for the start-up and shutdown procedures.

(BG) containing a large amount of carbon monoxide such as syngas produced through coal gasification or natural gas reforming process and byproduct gas generated as a by-product in a steel mill or petrochemical process is stored in a raw material gas reservoir . The raw material gas is compressed in the raw material gas compressor (C-101) at an operating pressure of 10 atm or more, preferably 70 to 80 atm, and supplied to microbial reactors (R-101, R-102 and R-103) . Although three microbial reactors are shown in FIG. 3, one or more of the reactors may be installed for the purpose of reducing the amount of hydrogen to be produced and the efficiency of the process such as reactor washing. In order to periodically clean and manage the bioreactor Three suitable for cycling are preferred.

The microbial reactors (R-101, R-102, R-103) are filled with medium corresponding to 50 to 70% of the total volume. The medium used in this reaction contains appropriate concentrations of substances that act as nutrients for microorganisms such as anaerobic digestion filtrate (AL), yeast extract, and vitamins in seawater. The medium is additionally supplied for continuous operation.

The culture solution for culturing the hydrogen producing microorganism includes a culture medium capable of culturing a microorganism (Thermococcus onnurineus) capable of surviving in seawater at a low temperature of about 80 ° C.

The seawater (SW) is stored in the seawater storage tank (TK-104) and supplied to the raw material mixing tank (TK-106) and the yeast extract tank (TK-103). The anaerobic digestion filtrate (AL) was stored in the anaerobic digestion filtrate storage tank (TK-105) and the yeast extract (YEAST) was continuously stored in the yeast extract tank (TK-102) .

The seawater SW supplied to the raw material mixing tank (TK-106) is heated to 90 DEG C through a seawater heater (E-102) and supplied. The medium stored in the seawater storage tank (TK-104), the anaerobic digestion filtrate storage tank (TK-105) and the yeast extract tank (TK-103) was supplied to the raw material mixing tank (TK-106) (R-101, 102, 103). At this time, the yeast extract and the anaerobic digestion filtrate (AL) can be supplied in the same volume ratio.

In the present invention, an anaerobic digestion filtrate (AL) was added as an auxiliary nutrient component considering the economical efficiency of the product. The anaerobic digestion filtrate (AL) refers to the digested filtrate generated in the anaerobic digester of a bio treatment facility of various wastes such as food wastes.

In order to regulate the pH of the reactor, the basic solution is supplied from the basic solution storage tank (TK-101), since proper pH control is important for the water gas shift reaction of microorganisms. At this time, a basic solution, preferably an NaOH solution, is supplied so that the pH of the reactor becomes 6.8. In addition, an acidic solution may be supplied depending on the type of seawater to be supplied.

The temperature of the microorganism reactors (R-101, 102, 103) is maintained at 80 DEG C or more and less than 90 DEG C, preferably 82 DEG C or more and less than 88 DEG C, more preferably 83 DEG C, Converted into hydrogen and carbon dioxide and become a water gas and discharged through a water gas cooler (E-101) and a condenser separator (TK-107). When the temperature of the microorganism reactors (R-101, 102, 103) is less than 80 ° C, the water gas conversion reaction by the microorganisms is not smoothly performed. If the temperature exceeds 90 ° C, microorganisms die, More important than that.

The waste medium WM discharged from the microbial reactors R-101, 102 and 103 is stored in the waste medium storage tank TK-109 and the waste solid matter WS through the separator TK- (TK-111), and the waste liquid (WL) is stored in a waste liquid discharge tank (TK-108) and sent to a separate wastewater treatment system.

This process does not include the separation and compression process of the produced gas.

The composition of the inlet / outlet gas of the microbial reactors (R-101, 102, 103) and the gas discharged at the end of the process are summarized in Table 3. Meanwhile, the carbon conversion rate in the hydrogen production reactor according to the present invention is 96.9%, and the energy efficiency of the hydrogen production process is 95.3%.

The apparatus and method for producing hydrogen from syngas using the microorganisms as described above require no heat exchanger by using hydrogen-producing microorganisms, and there is no need for a separate steam or heating device, thereby reducing the construction cost and operating cost. Hydrogen can be sufficiently produced in the reactor.

In addition, while the conventional thermochemical aqueous gas conversion process is an exothermic reaction, the biological aqueous gas conversion process requires only a small amount of energy supply due to a weak endothermic reaction, so that the operation is easy.

It will be apparent to those skilled in the art that various modifications and variations can be made in the present invention without departing from the spirit and scope of the invention. It is.

10: Thermochemical water gas conversion process
11: Gas preheating device
12: Steam supply
13: High temperature water gas conversion reactor
14: First cooler
15: Low temperature water gas conversion reactor
16: second cooler
100: Overall process for producing hydrogen from coal
110: air separator
120: Gasification device
130: Syngas cooling device
140: Water gas conversion device
150: Synthetic gas purifier
160: Carbon dioxide separator
170: pressure swing adsorption device
180: Gas turbine
181: Waste Heat Recovery Unit
182: Steam turbine
AL: anaerobic digestion filtrate
BG: raw material gas
C-101: Raw material gas compressor
E-101: Water gas cooler,
E-102: Seawater heater
NaOH: Sodium hydroxide
PDG: water gas
PG: Incinerator waste gas
R-101, 102, 103: microbial reactor
SW: seawater
TK-101: Basic solution storage tank
TK-102: Yeast extract storage tank
TK-103: yeast extract tank
TK-104: Seawater storage tank
TK-105: Anaerobic digestion filtrate storage tank
TK-106: Raw material mixing tank
TK-107: Condensate separator
TK-108: Waste liquid discharge tank
TK-109: waste medium storage tank
TK-110: Separator
TK-111: Waste solid waste tank
WL: Waste liquid
WM: Waste paper
WS: Waste solid
YEAST: yeast extract

Claims (11)

Yeast extract, anaerobic digestion filtrate (AL), raw water mixing tank (TK-106) for mixing seawater;
(R-101, 102, 103) in which a water gas conversion reaction by a microorganism takes place using a raw gas (BG) containing carbon monoxide and a raw material supplied from the raw material mixing tank (TK-106) ;
A separator (TK-110) for separating the waste medium generated from the microbial reactors (R-101, 102, 103) into waste solid and waste liquid;
A waste liquid discharge tank (TK) for producing an incineration waste gas (PG) from the waste liquid supplied from the separator (TK-110) and the following condensate supplied from the following condenser separator (TK-107) -108);
A water gas cooler (E-101) for cooling a water gas containing a large amount of hydrogen generated in the microbial reactors (R-101, 102, 103);
(PDG) as a main component from the cooled water gas supplied from the water gas cooler (E-101) to the upper end and a condensate to the waste liquid discharge tank (TK-108) A condensation separator (TK-107)
(BG) containing microorganism water gas. The method according to claim 1,
A device for producing a water gas through a microbial water gas conversion reaction from a raw material gas (BG) to which a seawater heater (E-102) capable of heating seawater is added before mixing the seawater into the raw material mixing tank (TK-106) . The method according to claim 1,
Wherein the microorganism produces a water gas through a microbial water gas conversion reaction from a raw material gas (BG) which is Thermococcus onnurineus. The method according to claim 1,
The microbial reactor may further comprise a microbial water-soluble microbial biomass (BG) from the feed gas (BG) further comprising a steam pipe inside the reactor and a radiating fin extending from the steam pipe to maintain the temperature of the zone where the microbial water- A device for producing a water gas through a gas conversion reaction. 1) preparing a raw material by mixing yeast extract, anaerobic digestion filtrate (AL) and seawater;
2) supplying raw material gas (BG) containing carbon monoxide and the raw material prepared in the step 1) to at least one microbial reactor (R-101, 102, 103) in which a water gas conversion reaction with microorganisms occurs;
3) performing a water gas conversion reaction using microorganisms in the at least one microbial reactor (R-101, 102, 103);
4) separating the waste medium produced from the microbial reactor into a waste solid and a waste liquid;
5) producing an incineration waste gas (PG) from the waste liquid and a condensate generated by cooling the water gas below;
6) cooling a water gas containing a large amount of hydrogen generated in the microbial reactor to generate a water-based gas (PDG) containing hydrogen as a main component and discharging a condensate;
Wherein the steps (1) to (6) are a continuous process which is performed simultaneously with the exception of the start-up and shutdown processes, and wherein the water gas is produced from the feed gas (BG) through a microbial water gas conversion reaction. 6. The method of claim 5,
Wherein the raw gas (BG) containing carbon monoxide in the step (2) is produced by converting microbial water gas from a raw material gas (BG) compressed and supplied to a pressure of 10 atm or higher. The method according to claim 6,
(BG) at a pressure of 70 to 80 atmospheric pressure to produce a water gas through a microbial water gas conversion reaction. 6. The method of claim 5,
In the step 3), the temperature of the zone where the microbial water gas conversion reaction occurs in the microbial reactor is 80 ° C or more and less than 90 ° C, and the microorganism converts the microbial water gas conversion reaction from the feed gas (BG) which is Thermococcus onnurineus ≪ / RTI > 9. The method of claim 8,
A method for producing a water gas from a raw material gas (BG) which regulates temperature by supplying steam to a steam tube inside a reactor having a radiating fin extending from the steam tube so as to maintain the temperature, through a microbial water gas conversion reaction. 6. The method of claim 5,
Wherein the yeast extract and the anaerobic digestion filtrate (AL) are mixed at the same volume in the step (1), and the water gas is produced from the feed gas (BG) through the microbial water gas conversion reaction. 6. The method of claim 5,
Wherein the microorganism reactors (R-101, 102, 103) have a pH of 6.8 to produce a water gas from the raw material gas (BG) through the microbial water gas conversion reaction in the step 3).

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