CN109847555B - Device and method for recovering multiple gases in catalytic dry gas based on hydrate method - Google Patents
Device and method for recovering multiple gases in catalytic dry gas based on hydrate method Download PDFInfo
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Abstract
The invention belongs to the field of chemical industry, and particularly relates to a device and a method for recovering multiple gases in catalytic dry gas based on a hydrate method. The method of hydration can not only recover hydrogen but also recover C with more value2Component (ethane and ethylene) and can realize CH4、N2Separating and recovering. The gas hydrate forming reaction and the gas hydrate decomposing reaction are separately generated in the reaction tower and the decomposer respectively, the gas hydrate forming and decomposing, the gas mixture separating and the gas component purifying and recovering are realized, a plurality of gases are recovered, and the concentration of the recovered gas is high. Provides a theoretical basis for further realizing the industrial separation of the mixed gas by the hydrate method, and has important practical significance for the popularization and the application of the hydrate separation technology.
Description
Technical Field
The invention belongs to the field of chemical industry, and particularly relates to a device and a method for recovering multiple gases in catalytic dry gas based on a hydrate method.
Background
The catalytic dry gas is a hydrogen-containing gas mixture which is most common in refineries and has the maximum yield (about 5 percent of the mass of raw oil), and is characterized by not only containing a certain amount of hydrogen (the volume fraction is 15 to 40 percent), but also containing C such as ethylene, ethane and the like with higher economic value2The components (volume fraction is about 20-30%), if hydrogen and C can be added2The component recycling can bring objective economic benefit to refineries (according to estimation, the total content of ethylene in the catalytic dry gas produced every year in China exceeds 100 ten thousand tons, and the ethane with the total content equivalent to the ethylene is the best raw material for preparing the ethylene by cracking). For a long time, most of the catalytic dry gas is not well utilized, but is burned as gas. Due to its complex composition, hydrogen and C2The respective concentrations of the components are not too high, although the prior refinery gas comprehensive utilization technology is many, the method also has some limitations, such as the low-temperature condition of a cryogenic separation method can be realized by overlapping refrigeration, the energy consumption is high, the circulating refrigeration process is relatively complex, and the device investment is large; the adsorption technology uses a plurality of devices, the process and program control are complex, frequent switching is needed, and the equipment investment is large; the membrane separation method has the advantages of low recovery rate and product purity, high requirements on membrane materials, short service life of the membrane, high cost and easy loss of gas. In addition, the operating pressure of the membrane separation method is generally 3-15 MPa, and compression and pressure boosting are needed when low-pressure refinery gas is recovered, so that the energy consumption is increased.
The hydrate separation technology is a new separation technology, receives more and more attention at home and abroad, and has unique advantages compared with the existing treatment technology of refinery gas. Compared with the cryogenic separation technology, the hydrate separation technology requires mild conditions (the pressure is 2-6 MPa, the temperature is 0-10 ℃), the mixed gas can be separated and purified at the temperature of more than 0 ℃, and the energy consumption is greatly reduced when the pressure is moderate; secondly, compared with an adsorption separation technology and a membrane separation technology, the application range of the hydrate separation technology is wider, for example, a PSA method and a membrane separation method are generally suitable for raw material gas with higher hydrogen concentration, the recovery rate of the raw material gas with low concentration is too low, the requirement of the hydrate separation technology on the hydrogen concentration in the raw material gas is not high, the recovery rate can reach more than 90 percent generally, and the advantages of small pressure loss and high separation efficiency are achieved; in addition, the hydrate separation technology has the characteristics of short process flow, continuous operation and low equipment investment. The hydrate separation technology has many similarities with the traditional absorption, rectification and adsorption technology, such as single-stage or multi-stage equilibrium separation based on the phase equilibrium difference of different components and according to the requirement of separation precision. Therefore, the hydrate separation technology has good application prospect in the aspect of comprehensive utilization of refinery gas.
The existing methods or devices for recovering various gases by using a hydration method have various defects, such as low combined separation efficiency of the hydration method and other traditional processes; the separated gas is too single; the process is complicated, etc.
Therefore, a device and a method for recovering multiple gases in catalytic dry gas based on a hydrate method are needed.
Disclosure of Invention
The invention aims to provide a method for separating catalytic dry gas and recovering H by using a hydrate method, which has simple process, economy and high efficiency2、CH4、CO2、N2And C2An apparatus and process for the components (ethane and ethylene).
The method for recovering various gases in the catalytic dry gas comprises the following specific steps:
(1) in a first biological decomposition unit, feeding catalytic dry gas in a raw material tank (24) into a first hydrate reaction tower, reacting to obtain two flows, wherein one flow is a gaseous flow which is led out from the top of the reaction tower and consists of hydrogen and enters a hydrogen-rich gas collector (25), and recovering high-concentration hydrogen; the other is slurry formed by the remaining hydrate and unreacted aqueous solution in the reaction device, and the slurry enters a first hydrate decomposer (19) to be decomposed under the conditions of heating and pressure reduction to release CH4、CO2、N2And C2A component and an aqueous solution;
(2) in the second generation decomposition unit, CH obtained in step (1)4、CO2、N2And C2The gas enters the lower part of the second hydrate reaction tower and is in stepwise reverse contact with the water solution containing the kinetic accelerator descending from the first liquid storage tank (5) in the ascending process, C2The component generates hydrate in a second hydrate reaction tower, and CH in gas is removed4、CO2、N2And C2Separating the components; c2The components are converted into hydrate and mixed with aqueous solution to form solid-liquid mixture, the solid-liquid mixture enters a second hydrate decomposer (19) and is decomposed under the condition of heating and pressure reduction, and C is released2Component (a) and an aqueous solution C2The component enters into C2The collector (26) carries out recovery; the aqueous solution returns to the first liquid storage tank (5) for recycling; separated CH4、CO2、N2Discharging the reaction product from the top of the second hydrate reaction tower into a third hydrate reaction tower;
(3) in the third generation decomposition unit, the water enters the other parts of the third hydrate reaction tower and is in stepwise reverse contact with the water solution containing the kinetic accelerator from the second liquid storage tank (5) in the upward process to generate hydrates; CH in gas easy to hydrate4And CO2Converted to hydrate and mixed with aqueous solution to form solid-liquid mixture, remaining N2Discharging from the top of the third hydrate reaction tower and entering a nitrogen collector (28); slurry formed by the hydrate in the third hydrate reaction tower and the unreacted aqueous solution enters a third hydrate decomposer (19) and is decompressed to release CH4Gas and CO2A mixed slurry of hydrate and aqueous solution; feeding the obtained gas to a methane collector (29); the slurry enters a fourth hydrate decomposer (19) for CO2Dissolving and separating the hydrate; CO released by the fourth hydrate decomposer (19)2Into CO2The collector, and the aqueous solution enters a second liquid storage tank (5) for recycling.
Wherein the kinetic accelerator in the first liquid storage tank (5) is Sodium Dodecyl Sulfate (SDS) with the concentration of 300 mg/L; the compound accelerator in the second liquid storage tank (5) is graphite powder (NGP) + SDBS, and the concentration of the aqueous solution is 0.8% + 0.08%.
The reaction pressure of the heating decomposition in the first hydrate decomposer (19) is controlled to be 0.1-0.5 MPa, and the temperature is controlled to be 0.5-1 ℃; the reaction pressure of the heating decomposition in the second hydrate decomposer (19) is controlled to be 0.1-0.5 MPa, and the temperature is controlled to be 4 ℃; the reaction pressure of the heating decomposition in the third hydrate decomposer (19) is controlled at 3.0MPa, and the temperature is controlled at 4 ℃; the reaction pressure of the heating decomposition in the fourth hydrate decomposer (19) is controlled to be 0.1-0.5 MPa, and the temperature is controlled to be 4 ℃.
The invention also provides a method for separating catalytic dry gas and recovering H by using a hydrate method2、CH4、CO2、N2And C2An apparatus for the separation and recovery of components (ethane and ethylene) comprising a first generative decomposition unit for the separation and recovery of hydrogen and a second generative decomposition unit for the separation and recovery of C2Component, third decomposition unit for separating and recovering N2、CH4、CO2And the cooling system, wherein the first generating decomposition unit, the second generating decomposition unit and the third generating decomposition unit are sequentially communicated from front to back according to the process sequence, and the first generating decomposition unit is communicated with the cooling system.
The first biological decomposition unit comprises a first hydrate reaction tower, a raw material tank (24), a hydrogen-rich gas collector (25) and a first hydrate decomposer (19), wherein an inlet of the first hydrate reaction tower is communicated with the raw material tank (24), and a gas pressure regulating valve (10) and a gas flow meter (16) are sequentially arranged on a line of the first hydrate reaction tower communicated with the raw material tank; the top outlet of the first hydrate reaction tower is communicated with a hydrogen-rich gas collector (25); a pressure gauge (17), a backpressure valve (18), a gas flowmeter (16) and a gas pressure regulating valve (10) are sequentially arranged on a line for communicating the first hydrate reaction tower with the hydrogen-rich gas collector; the bottom outlet of the first hydrate reaction tower is communicated with the inlet of a first hydrate decomposer (19); the top outlet of the first hydrate decomposer (19) is communicated with the second hydrate reaction tower; the bottom outlet of the first hydrate decomposer (19) is communicated with a cooling system.
The second generation decomposition unit comprises a first liquid storage tank (5), a second hydrate reaction tower, a second hydrate decomposer (19) and a first hydrate2A collector (26); an inlet at the top of the second hydrate reaction tower is communicated with a first liquid storage tank (5), and an outlet at the top of the second hydrate reaction tower is communicated with a third hydrate reaction tower; a pressure gauge (17), a backpressure valve (18), a gas flowmeter (16) and a gas pressure regulating valve (10) are sequentially arranged on a line for communicating the second hydrate reaction tower with the third hydrate reaction tower; the bottom outlet of the second hydrate reaction tower is communicated with the inlet of a second hydrate decomposer (19), the bottom outlet of the second hydrate decomposer (19) is communicated with a first liquid storage tank (5), and the top outlet of the second hydrate decomposer (19) is communicated with a C2A collector (26) communicated with the second hydrate decomposer2A backpressure valve (18) and a gas flowmeter (16) are sequentially arranged on a line communicated with the collector.
The third biological decomposition unit comprises a second liquid storage tank (5), a third hydrate reaction tower, a third hydrate decomposer (19), a fourth hydrate decomposer (19), a methane collector (27) and N2A gas collector (28) and a carbon dioxide collector (29); the inlet of the third hydrate reaction tower is communicated with a second liquid storage tank (5), and the outlet at the top of the third hydrate reaction tower is communicated with N2A gas collector (28) communicated with the N in the third hydrate reaction tower2A pressure gauge (17), a backpressure valve (18), a gas flowmeter (16) and a gas pressure regulating valve (10) are sequentially arranged on a line communicated with the gas collector (28); an outlet at the bottom of the third hydrate reaction tower is communicated with an inlet of a third hydrate decomposer (19), and an outlet at the upper part of the third hydrate decomposer (19) is communicated with a methane collector (27); an outlet at the bottom of the third hydrate decomposer (19) is communicated with an inlet of a fourth hydrate decomposer (19), an outlet at the upper part of the fourth hydrate decomposer (19) is communicated with a carbon dioxide collector (29), and an outlet at the lower part of the fourth hydrate decomposer (19) is communicated with a second liquid storage tank (5); a back pressure valve (18) and a gas flowmeter (16) are sequentially arranged on the lines of the third hydrate decomposer and the methane collector and the lines of the fourth hydrate decomposer and the carbon dioxide collector.
The hydrate reaction tower comprises a high-pressure tower (7) and a high-pressure liquid circulating pump (14), a spray head (11) is arranged at the top end of the interior of the high-pressure tower (7), a high-pressure hydration reactor (12) is arranged in the middle of the interior of the high-pressure tower (7), a refrigerating system (6) is further arranged in the interior of the high-pressure tower (7), and a heat-insulating layer (8) and a cooling coil (9) are arranged on the periphery of the high-pressure tower; the high-pressure liquid circulating pump (14) is communicated with the interior of the high-pressure tower (7);
the liquid storage tank (5) is sequentially communicated with the high-pressure liquid pump (3), the temperature sensor (1) and the safety valve (4), and the stirring motor (2), the refrigerating system (6) and the cooling coil (9) are arranged in the storage tank (5).
The cooling system comprises a cold liquid tank (20), wherein an inlet of the cold liquid tank (20) is communicated with an outlet of the first hydrate decomposer (19), and a refrigeration system (6), a temperature sensor (1) and a liquid pressure regulating valve (15) are sequentially arranged on a line through which the cold liquid tank (20) is communicated with the hydrate decomposer (19); a line for communicating the outlet of the cold liquid tank (20) with the inlet of the first hydrate reaction tower is sequentially provided with a liquid booster flow pump (21), a liquid flow meter (22), a check valve (23) and a liquid pressure regulating valve (15); and a liquid level meter (13) is also arranged outside the cold liquid tank (20).
The invention has the beneficial effects that:
1) the working pressure range of the process adopted by the invention is 0.1-15 MPa, and the temperature range is 273.15-277.65K; because the air source pressure is high, the pressurization is not needed, only a hydration tower and a decomposition device are needed, the investment is not large, and the influence on the industry is avoided.
2) The separation method and the process flow are simple, convenient and efficient, the accelerant is environment-friendly and pollution-free, the equipment cannot be corroded, the reaction rate is high, the production efficiency is high, the energy consumption is low, and the concentration of the obtained separation gas is high (the concentration exceeds 90%); .
3) The invention adopts the hydration method to recover not only hydrogen but also more valuable C2Component (ethane and ethylene) and can realize CH4、N2Separating and recovering. The gas hydrate forming reaction and the gas hydrate decomposing reaction are separately generated in the reaction tower and the decomposer respectively, the gas hydrate forming and decomposing, the gas mixture separating and the gas component purifying and recovering are realized, a plurality of gases are recovered, and the concentration of the recovered gas is high. Provides theoretical basis for further realizing the industrial separation of the mixed gas by the hydrate method and provides a hydrate separation technologyThe popularization and the application have important practical significance.
Drawings
FIG. 1 is a schematic diagram of a recovery device for recovering a plurality of gases in catalytic dry gas by a hydrate method;
description of reference numerals:
1-a temperature sensor, 2-a stirring motor, 3-a high-pressure liquid pump, 4-a safety valve, 5-a liquid storage tank, 6-a refrigeration system, 7-a high-pressure tower, 8-a heat preservation layer, 9-a cooling coil, 10-a gas pressure regulating valve, 11-a spray head, 12-a high-pressure hydration reactor, 13-a liquid level gauge, 14-a high-pressure liquid circulating pump, 15-a liquid pressure regulating valve, 16-a gas flowmeter, 17-a pressure gauge, 18-a back pressure valve, 19-a hydration decomposer, 20-a cold liquid tank, 21-a liquid pressurization flow pump, 22-a liquid flowmeter, 23-a check valve, 24-a raw material tank, 25-a hydrogen-enriched gas collector, 26-C2 collector, 27-a methane collector and 28-a nitrogen collector, 29-carbon dioxide trap.
Detailed Description
Example 1
(1) The catalytic dry gas enters a first hydrate reaction tower through a gas flowmeter (16) and a gas pressure regulating valve (10), two flows are obtained through the reaction of the first hydrate reaction tower, one flow is a gaseous material flow which is led out from the top of the reaction tower and consists of hydrogen, the gaseous material flow passes through a pressure gauge (17) and a back pressure valve (18), the gas flowmeter (16) enters a hydrogen-rich gas collector (25) through the gas pressure regulating valve (10), and high-concentration hydrogen is recycled (the gas concentration is about 95%); the residual water and the hydrate form slurry, the slurry enters a first hydrate decomposer (19) through a liquid pressure regulating valve (15), the decomposition is carried out under the conditions of heating and pressure reduction (the pressure is controlled to be 0.1-0.5 MPa, the temperature is controlled to be 0.5-1 ℃), and CH is released4、CO2、N2And C2A component and an aqueous solution;
(2) CH obtained in step (1)4、CO2、N2And C2The gas enters the lower part of the second hydrate reaction tower and is in stepwise reverse contact with a descending aqueous solution containing a kinetic accelerator (the concentration of SDS is 300mg/L, the pressure is 4.0MPa, and the temperature is 4.5 ℃) from a first liquid storage tank (5) in the ascending process, and C2The components being hydratedHydrate is generated in the reactant reaction tower, and CH in the gas is removed4、CO2、N2And C2Separating the components; c2The components are converted into hydrates and mixed with aqueous solution to form a solid-liquid mixture, the solid-liquid mixture enters a second hydrate decomposer (19) and is decomposed under the conditions of heating and pressure reduction (the pressure is controlled to be 0.1-0.5 MPa, the temperature is controlled to be 4 ℃), and C is released2Component (a) and an aqueous solution C2The component (concentration 98.98%) enters C2The collector (26) carries out recovery; the aqueous solution returns to the first liquid storage tank (5) for recycling; separated CH4、CO2、N2And the gas is discharged from the top of the second hydrate reaction tower, sequentially passes through a back pressure valve (18), a gas flowmeter (16) and a gas pressure regulating valve (10) and enters a third hydrate reaction tower.
(3) Gas enters a third hydrate reaction tower from the lower part, and is in stepwise reverse contact with a water solution (graphite powder NGP + SDBS, the concentration of the water solution is 0.8% + 0.08%, the pressure is 7.5MPa, and the temperature is 4 ℃) containing a kinetic accelerator from a second liquid storage tank (5) in the ascending process of the gas to generate a hydrate (compared with a pure water system, the efficiency is improved to 116.3%); component (CH) in gas liable to hydrate4、CO2Component) is converted to hydrate and mixed with an aqueous solution to form a solid-liquid mixture, the remaining gas (N)2) Discharging from the top of the third hydrate reaction tower and entering a nitrogen collector (28); slurry formed by the hydrate in the third hydrate reaction tower and the unreacted aqueous solution enters a third hydrate decomposer (19) and is heated and decomposed in the third hydrate decomposer (the reaction pressure is controlled at 3.0MPa, the temperature is controlled at 4 ℃), and CH is released4Gas and CO2A mixed slurry of hydrate and aqueous solution; feeding the obtained gas to a methane (91% concentration) collector (27); the slurry enters a fourth hydrate decomposer (19) for CO2Dissolving and separating the hydrate (the pressure is controlled to be 0.1-0.5 MPa, and the temperature is controlled to be 4 ℃); CO released by the fourth hydrate decomposer (19)2The CO enters the gas flow meter (16) through the gas pressure regulating valve (10) through the pressure gauge (17), the back pressure valve (18) and the gas flow meter (16)2A collector (29) (60% concentration, e.g. 96% concentration if the second separation is performed) and an aqueous solutionReturning to the second liquid storage tank (5) for recycling.
Claims (6)
1. A method for recovering multiple gases in catalytic dry gas is characterized in that: the method comprises the following specific steps:
(1) in a first biological decomposition unit, feeding catalytic dry gas in a raw material tank (24) into a first hydrate reaction tower, reacting to obtain two flows, wherein one flow is a gaseous flow which is led out from the top of the reaction tower and consists of hydrogen and enters a hydrogen-rich gas collector (25), and recovering high-concentration hydrogen; the other is slurry formed by the remaining hydrate and unreacted aqueous solution in the reaction device, and the slurry enters a first hydrate decomposer (19) to be decomposed under the conditions of heating and pressure reduction to release CH4、CO2、N2And C2A component and an aqueous solution;
(2) in the second generation decomposition unit, CH obtained in step (1)4、CO2、N2And C2The gas enters the lower part of the second hydrate reaction tower and is in stepwise reverse contact with the water solution containing the kinetic accelerator descending from the first liquid storage tank (5) in the ascending process, C2The component generates hydrate in a second hydrate reaction tower, and CH in gas is removed4、CO2、N2And C2Separating the components; c2The components are converted into hydrate and mixed with aqueous solution to form solid-liquid mixture, the solid-liquid mixture enters a second hydrate decomposer (19) and is decomposed under the condition of heating and pressure reduction, and C is released2Component (a) and an aqueous solution C2The component enters into C2The collector (26) carries out recovery; the aqueous solution returns to the first liquid storage tank (5) for recycling; separated CH4、CO2、N2Discharging the reaction product from the top of the second hydrate reaction tower into a third hydrate reaction tower;
(3) in the third generation decomposition unit, gas entering a third hydrate reaction tower is in stepwise reverse contact with an aqueous solution containing a kinetic accelerator from a second liquid storage tank (5) in the upward process to generate a hydrate; CH in gas easy to hydrate4And CO2Is converted into hydrate and is mixed with waterMixing the solution to form a solid-liquid mixture, and adding the remaining N2Discharging from the top of the third hydrate reaction tower and entering a nitrogen collector (28); slurry formed by the hydrate in the third hydrate reaction tower and the unreacted aqueous solution enters a third hydrate decomposer (19) and is decompressed to release CH4Gas and CO2A mixed slurry of hydrate and aqueous solution; feeding the obtained gas to a methane collector (29); the slurry enters a fourth hydrate decomposer (19) for CO2Dissolving and separating the hydrate; CO released by the fourth hydrate decomposer (19)2Into CO2The collector, and the aqueous solution enters the second liquid storage tank (5), recycle;
the reaction pressure of the heating decomposition in the first hydrate decomposer (19) is controlled to be 0.1-0.5 MPa, and the temperature is controlled to be 0.5-1 ℃; the reaction pressure of the heating decomposition in the second hydrate decomposer (19) is controlled to be 0.1-0.5 MPa, and the temperature is controlled to be 4 ℃; the reaction pressure of the heating decomposition in the third hydrate decomposer (19) is controlled at 3.0MPa, and the temperature is controlled at 4 ℃; the reaction pressure of the heating decomposition in the fourth hydrate decomposer (19) is controlled to be 0.1-0.5 MPa, and the temperature is controlled to be 4 ℃;
the device for recovering a plurality of gases in the catalytic dry gas based on the hydrate method comprises a first generating and decomposing unit for separating and recovering hydrogen and a second generating and decomposing unit for separating and recovering C2Component, third decomposition unit for separating and recovering N2、CH4、CO2The first generating decomposition unit, the second generating decomposition unit and the third generating decomposition unit are communicated in sequence from front to back according to the process sequence, and the first generating decomposition unit is communicated with the cooling system;
the first biological decomposition unit comprises a first hydrate reaction tower, a raw material tank (24), a hydrogen-rich gas collector (25) and a first hydrate decomposer (19), wherein the bottom inlet of the first hydrate reaction tower is communicated with the raw material tank (24); the top outlet of the first hydrate reaction tower is communicated with a hydrogen-rich gas collector (25); the bottom outlet of the first hydrate reaction tower is communicated with the inlet of a first hydrate decomposer (19); the top outlet of the first hydrate decomposer (19) is communicated with the second hydrate reaction tower; the bottom outlet of the first hydrate decomposer (19) is communicated with a cooling system;
the cooling system comprises a cold liquid tank (20), wherein an inlet of the cold liquid tank (20) is communicated with an outlet of the first hydrate decomposer (19), and a refrigeration system (6), a temperature sensor (1) and a liquid pressure regulating valve (15) are sequentially arranged on a line through which the cold liquid tank (20) is communicated with the hydrate decomposer (19); a line for communicating the outlet of the cold liquid tank (20) with the inlet of the first hydrate reaction tower is sequentially provided with a liquid booster flow pump (21), a liquid flow meter (22), a check valve (23) and a liquid pressure regulating valve (15); and a liquid level meter (13) is also arranged outside the cold liquid tank (20).
2. The method for recovering a plurality of gases from a catalytic dry gas according to claim 1, wherein the kinetic accelerator in the first liquid storage tank (5) is Sodium Dodecyl Sulfate (SDS) and the concentration of the aqueous solution is 300 mg/L; the compound accelerator in the second liquid storage tank (5) is graphite powder (NGP) + SDBS, and the concentration of the aqueous solution is 0.8% + 0.08%.
3. Method for recovering gases from catalytic dry gas according to claim 1, characterized in that the second generation decomposition unit comprises a first liquid storage tank (5), a second hydrate reaction tower, a second hydrate decomposer (19) and C2A collector (26); an inlet at the top of the second hydrate reaction tower is communicated with a first liquid storage tank (5), and an outlet at the top of the second hydrate reaction tower is communicated with a third hydrate reaction tower; the bottom outlet of the second hydrate reaction tower is communicated with the inlet of a second hydrate decomposer (19), the bottom outlet of the second hydrate decomposer (19) is communicated with a first liquid storage tank (5), and the top outlet of the second hydrate decomposer (19) is communicated with a C2The collectors (26) are communicated.
4. A method for recovering gases from catalytic dry gas according to claim 1, wherein the third biological decomposition unit comprises a second liquid storage tank (5), a third hydrate reaction tower, a third hydrate decomposer (19), a fourth hydrate decomposer (19), a methane collector (27)、N2A gas collector (28) and a carbon dioxide collector (29); the top inlet of the third hydrate reaction tower is communicated with a second liquid storage tank (5), and the top outlet of the third hydrate reaction tower is communicated with N2The gas collector (28) is communicated; an outlet at the bottom of the third hydrate reaction tower is communicated with an inlet of a third hydrate decomposer (19), and an outlet at the upper part of the third hydrate decomposer (19) is communicated with a methane collector (27); an outlet at the bottom of the third hydrate decomposer (19) is communicated with an inlet of a fourth hydrate decomposer (19), an outlet at the upper part of the fourth hydrate decomposer (19) is communicated with a carbon dioxide collector (29), and an outlet at the lower part of the fourth hydrate decomposer (19) is communicated with a second liquid storage tank (5).
5. The method for recovering multiple gases in catalytic dry gas according to claim 1, 3 or 4, wherein the hydrate reaction tower comprises a high-pressure tower (7) and a high-pressure liquid circulating pump (14), a spray head (11) is arranged at the top end of the interior of the high-pressure tower (7), a high-pressure hydration reactor (12) is arranged in the middle of the interior of the high-pressure tower (7), a refrigerating system (6) is further arranged in the interior of the high-pressure tower (7), and an insulating layer (8) and a cooling coil (9) are arranged on the periphery of the high-pressure tower; the high-pressure liquid circulating pump (14) is communicated with the interior of the high-pressure tower (7).
6. The method for recovering a plurality of gases in catalytic dry gas according to claim 3 or 4, characterized in that the liquid storage tank (5) is communicated with a high-pressure liquid pump (3), a temperature sensor (1) and a safety valve (4) in sequence, and the stirring motor (2), the refrigerating system (6) and the cooling coil (9) are arranged in the storage tank (5).
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