CN116769522A - Circulating type biological natural gas decarburization system and method - Google Patents
Circulating type biological natural gas decarburization system and method Download PDFInfo
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- CN116769522A CN116769522A CN202310798934.3A CN202310798934A CN116769522A CN 116769522 A CN116769522 A CN 116769522A CN 202310798934 A CN202310798934 A CN 202310798934A CN 116769522 A CN116769522 A CN 116769522A
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- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 title claims abstract description 274
- 239000003345 natural gas Substances 0.000 title claims abstract description 85
- 238000000034 method Methods 0.000 title claims abstract description 24
- 238000005261 decarburization Methods 0.000 title claims abstract description 14
- 239000007789 gas Substances 0.000 claims abstract description 176
- 238000006703 hydration reaction Methods 0.000 claims abstract description 123
- 239000003795 chemical substances by application Substances 0.000 claims abstract description 75
- 230000036571 hydration Effects 0.000 claims abstract description 44
- 238000000354 decomposition reaction Methods 0.000 claims abstract description 28
- 238000011084 recovery Methods 0.000 claims abstract description 27
- 238000005262 decarbonization Methods 0.000 claims abstract description 25
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims description 82
- 238000006243 chemical reaction Methods 0.000 claims description 46
- 229910002092 carbon dioxide Inorganic materials 0.000 claims description 41
- 239000001569 carbon dioxide Substances 0.000 claims description 41
- 230000000887 hydrating effect Effects 0.000 claims description 40
- 239000002002 slurry Substances 0.000 claims description 23
- 238000003860 storage Methods 0.000 claims description 21
- 239000012535 impurity Substances 0.000 claims description 14
- 125000004122 cyclic group Chemical group 0.000 claims description 3
- 238000012544 monitoring process Methods 0.000 claims description 3
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 3
- 238000001816 cooling Methods 0.000 abstract description 7
- 239000012071 phase Substances 0.000 description 64
- 238000000746 purification Methods 0.000 description 20
- 238000000926 separation method Methods 0.000 description 15
- NMJORVOYSJLJGU-UHFFFAOYSA-N methane clathrate Chemical compound C.C.C.C.O.O.O.O.O.O.O.O.O.O.O.O.O.O.O.O.O.O.O.O.O.O.O NMJORVOYSJLJGU-UHFFFAOYSA-N 0.000 description 9
- 239000000047 product Substances 0.000 description 7
- 238000011161 development Methods 0.000 description 5
- 239000007788 liquid Substances 0.000 description 5
- WYURNTSHIVDZCO-UHFFFAOYSA-N Tetrahydrofuran Chemical compound C1CCOC1 WYURNTSHIVDZCO-UHFFFAOYSA-N 0.000 description 4
- 238000010521 absorption reaction Methods 0.000 description 4
- 238000005516 engineering process Methods 0.000 description 4
- 239000002028 Biomass Substances 0.000 description 3
- DBMJMQXJHONAFJ-UHFFFAOYSA-M Sodium laurylsulphate Chemical compound [Na+].CCCCCCCCCCCCOS([O-])(=O)=O DBMJMQXJHONAFJ-UHFFFAOYSA-M 0.000 description 3
- 238000001514 detection method Methods 0.000 description 3
- 235000019333 sodium laurylsulphate Nutrition 0.000 description 3
- 229910052799 carbon Inorganic materials 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 238000005265 energy consumption Methods 0.000 description 2
- 239000007791 liquid phase Substances 0.000 description 2
- 229940083575 sodium dodecyl sulfate Drugs 0.000 description 2
- YLQBMQCUIZJEEH-UHFFFAOYSA-N tetrahydrofuran Natural products C=1C=COC=1 YLQBMQCUIZJEEH-UHFFFAOYSA-N 0.000 description 2
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 239000007795 chemical reaction product Substances 0.000 description 1
- 238000004891 communication Methods 0.000 description 1
- 238000013329 compounding Methods 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000003795 desorption Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 210000003608 fece Anatomy 0.000 description 1
- 238000000855 fermentation Methods 0.000 description 1
- 239000007792 gaseous phase Substances 0.000 description 1
- 239000010806 kitchen waste Substances 0.000 description 1
- 244000144972 livestock Species 0.000 description 1
- 239000010871 livestock manure Substances 0.000 description 1
- 238000005259 measurement Methods 0.000 description 1
- 239000012528 membrane Substances 0.000 description 1
- 239000010815 organic waste Substances 0.000 description 1
- 244000144977 poultry Species 0.000 description 1
- 238000012545 processing Methods 0.000 description 1
- 230000000750 progressive effect Effects 0.000 description 1
- 238000005086 pumping Methods 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 238000001179 sorption measurement Methods 0.000 description 1
- 239000010902 straw Substances 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 230000009466 transformation Effects 0.000 description 1
- 239000002351 wastewater Substances 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L3/00—Gaseous fuels; Natural gas; Synthetic natural gas obtained by processes not covered by subclass C10G, C10K; Liquefied petroleum gas
- C10L3/06—Natural gas; Synthetic natural gas obtained by processes not covered by C10G, C10K3/02 or C10K3/04
- C10L3/10—Working-up natural gas or synthetic natural gas
- C10L3/101—Removal of contaminants
- C10L3/102—Removal of contaminants of acid contaminants
- C10L3/104—Carbon dioxide
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/46—Removing components of defined structure
- B01D53/62—Carbon oxides
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/77—Liquid phase processes
- B01D53/78—Liquid phase processes with gas-liquid contact
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/96—Regeneration, reactivation or recycling of reactants
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- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- General Chemical & Material Sciences (AREA)
- Environmental & Geological Engineering (AREA)
- Health & Medical Sciences (AREA)
- Biomedical Technology (AREA)
- Analytical Chemistry (AREA)
- Organic Chemistry (AREA)
- Life Sciences & Earth Sciences (AREA)
- Sustainable Development (AREA)
- Gas Separation By Absorption (AREA)
Abstract
The invention discloses a circulating biological natural gas decarburization system and a method, which relate to the technical field of natural gas decarburization, wherein the system comprises: the air source pretreatment unit is used for pressurizing and pre-cooling the biological natural air source to obtain a pretreated air source; the hydration reaction unit is used for carrying out hydration reaction on the pretreated air source and the hydration agent to generate a gas phase and a hydrate phase; the hydrate decomposition and collection unit is used for collecting a hydrate phase and decomposing the hydrate phase to generate a hydration agent; the hydration agent recovery unit is used for recovering the hydration agent generated by the hydrate decomposition and collection unit and conveying the recovered hydration agent to the hydration reaction unit; a methane collection unit for collecting the gas phase product generated by the hydration reaction unit when the methane concentration detected by the gas analyzer is greater than a set concentration value; and when the concentration of methane is less than or equal to the set concentration value, conveying the gas phase generated by the hydration reaction unit to the gas source pretreatment unit. The invention improves the decarbonization efficiency of the biological natural gas.
Description
Technical Field
The invention relates to the technical field of natural gas decarbonization, in particular to a circulating biological natural gas decarbonization system and method.
Background
Biomass energy is an environmentally friendly renewable energy source, and efficient development and utilization of biomass energy are effective ways to alleviate current environmental and energy problems. The biological natural gas technology is an important mode for realizing the efficient utilization of biomass energy, and is an important substitute energy source of conventional biological natural gas. The biological natural gas is a green low-carbon clean renewable natural gas which is produced by taking various urban and rural organic wastes such as crop straws, livestock and poultry manure, kitchen waste, agricultural and sideline product processing wastewater and the like as raw materials through anaerobic fermentation, purification and purification, and the main component of the natural gas is CH 4 (60%～80%)、CO 2 (20%～40%)、H 2 S (0.5% -2.5%) and some trace gases. The efficient development and large-scale utilization of the biological natural gas play an important role in developing low-carbon economy, realizing energy transformation and sustainable development. However, the purification and purification of biogas is a key issue in achieving efficient utilization of biogas.
At present, the common purification and purification process and method of the biological natural gas mainly comprise a chemical absorption method, a physical absorption method, a membrane separation method, a low-temperature separation method and the like. However, the traditional biological natural gas purification and purification method has the problems of complex process, high cost, unsatisfactory separation effect, inconvenience for industrialization and large scale, and the like, and the development of novel biological natural gas efficient purification and purification technology is urgent. The gas hydrate method for obtaining high-purity methane from the biological natural gas is a very promising separation and purification method for the biological natural gas, and can realize the high-efficiency purification of the biological natural gas.
The existing biological natural gas decarbonization methods comprise a plurality of technologies and methods such as an adsorption method and a low-temperature separation method, but the technologies have the defects of high cost, high energy consumption, low separation efficiency, low speed and the like, and the efficiency of a hydrate method secondary separation method needs to be improved, so that development of a high-efficiency biological natural gas purification system with good safety and strong adaptability is needed to be further improved, and the utilization value of the biological natural gas is further improved.
Disclosure of Invention
The invention aims to provide a circulating type biological natural gas decarbonization system and method, which improve the decarbonization efficiency of biological natural gas.
In order to achieve the above object, the present invention provides the following solutions:
a cyclic biogas decarbonization system comprising:
the air source pretreatment unit is used for sequentially carrying out pressurization treatment and precooling treatment on the biological natural air source to obtain a pretreated air source;
the hydration reaction unit is used for carrying out hydration reaction on the pretreated air source and the hydration agent to generate a gas phase and a hydrate phase;
a hydrate decomposition and collection unit for collecting the hydrate phase and decomposing the hydrate phase to generate a hydrate;
a hydration agent recovery unit for recovering the hydration agent generated by the hydrate decomposition and collection unit and delivering the recovered hydration agent to the hydration reaction unit;
a gas analyzer for detecting the concentration of methane in the gas phase generated by the hydration reaction unit;
a methane collection unit for collecting a gas phase product generated by the hydration reaction unit when the methane concentration detected by the gas analyzer is greater than a set concentration value; and when the methane concentration detected by the gas analyzer is smaller than or equal to a set concentration value, conveying the gas phase generated by the hydration reaction unit to the gas source pretreatment unit.
Optionally, the air source pretreatment unit comprises a first booster pump, a second booster pump and an air pre-cooling device which are sequentially connected; the first booster pump is used for carrying out primary booster on the biological natural gas source, the second booster pump is used for carrying out secondary booster on the biological natural gas source output by the first booster pump, and the gas precooling device is used for carrying out precooling treatment on the biological natural gas source output by the second booster pump;
the methane collection unit is specifically configured to, when the methane concentration detected by the gas analyzer is less than or equal to a set concentration value, convey the gas phase generated by the hydration reaction unit to the second booster pump in terms of conveying the gas phase generated by the hydration reaction unit to the gas source pretreatment unit.
Optionally, the hydration reaction unit comprises a high-pressure reaction kettle and a constant-temperature cold bath device, the high-pressure reaction kettle is connected with the air source pretreatment unit, the high-pressure reaction kettle is arranged in the constant-temperature cold bath device, and the high-pressure reaction kettle is used for carrying out hydration reaction on the pretreated air source and the hydration agent to generate a gas phase and a hydrate phase.
Optionally, a temperature sensor is arranged in the high-pressure reaction kettle, a first pressure sensor is arranged at a gas inlet of the high-pressure reaction kettle, and a second pressure sensor is arranged at a gas outlet of the high-pressure reaction kettle;
the circulating type biological natural gas decarburization system further comprises a data acquisition unit, wherein the data acquisition unit is used for acquiring monitoring data of the temperature sensor, the first pressure sensor and the second pressure sensor.
Optionally, the hydrate decomposition and collection unit comprises a first slurry pump, a hydrate decomposer and a carbon dioxide gas storage tank which are sequentially connected; the first slurry pump is used for conveying the hydrate phase generated by the hydration reaction unit to the hydrate decomposer, the hydrate decomposer is used for decomposing the hydrate phase to generate impurity gas and a hydrating agent, the impurity gas comprises carbon dioxide, and the carbon dioxide gas storage tank is used for collecting the impurity gas.
Optionally, the hydrating agent recovery unit comprises a hydrating agent recovery tank and a second slurry pump which are sequentially connected, wherein the hydrating agent recovery tank is used for recovering the hydrating agent generated by the hydrate decomposition collecting unit, and the second slurry pump is used for conveying the hydrating agent recovered by the hydrating agent recovery tank to the hydration reaction unit.
Optionally, the methane collecting unit includes backpressure valve, buffer tank, hand pump, carbon dioxide absorbing device, methane gas holder, the one end of backpressure valve with hydration unit connects, the other end of backpressure valve respectively with the one end of buffer tank with carbon dioxide absorbing device connects, the other end of buffer tank with hand pump connects, carbon dioxide absorbing device still with methane gas holder connects, carbon dioxide absorbing device is arranged in desorption gaseous phase product's carbon dioxide.
Optionally, the hydrating agent is water.
Alternatively, the set concentration value is 97%.
The invention also discloses a circulating biological natural gas decarbonization method, which comprises the following steps:
the air source pretreatment unit sequentially carries out pressurization treatment and precooling treatment on the biological natural air source to obtain a pretreated air source;
the hydration reaction unit carries out hydration reaction on the pretreated air source and the hydration agent to generate a gas phase and a hydrate phase;
the hydrate decomposition and collection unit collects the hydrate phase and decomposes the hydrate phase to generate a hydrate;
the hydration agent recovery unit is used for recovering the hydration agent generated by the hydrate decomposition and collection unit and conveying the recovered hydration agent to the hydration reaction unit;
detecting the concentration of methane in a gas phase generated by the hydration reaction unit by a gas analyzer;
the methane collecting unit is used for collecting gas phase products generated by the hydration reaction unit when the methane concentration detected by the gas analyzer is larger than a set concentration value; and when the methane concentration detected by the gas analyzer is smaller than or equal to a set concentration value, conveying the gas phase generated by the hydration reaction unit to the gas source pretreatment unit.
According to the specific embodiment provided by the invention, the invention discloses the following technical effects:
according to the invention, the hydration reaction efficiency of the biological natural gas can be further improved through pressurization and pre-cooling pretreatment of the biological natural gas source, so that the decarburization efficiency of the biological natural gas is further realized, the hydration agent after the decomposition of the hydrate can be recycled, the economy of decarburization of the biological natural gas is improved, the residual gas after the hydration separation is subjected to multistage circulation separation, the pressurization cost is further saved, and the biological natural gas can be purified to the specified concentration.
Drawings
In order to more clearly illustrate the embodiments of the present invention or the technical solutions of the prior art, the drawings that are needed in the embodiments will be briefly described below, it being obvious that the drawings in the following description are only some embodiments of the present invention, and that other drawings may be obtained according to these drawings without inventive effort for a person skilled in the art.
Fig. 1 is a schematic structural diagram of a circulating type biological natural gas decarbonization system according to an embodiment of the present invention.
Symbol description:
1-a source of biological natural gas; 2-a first valve; 3-a first booster pump; 4-a second booster pump; 5-a second valve; 6-a gas pre-cooling device; 7-a third valve; 8-a high-pressure reaction kettle; 9-a constant temperature cold bath device; 10-fourth valve; 11-a back pressure valve; 12-a buffer tank; 13-hand pump; 14-a fifth valve; 15-a carbon dioxide absorption device; 16-methane storage tank; 17-sixth valve; 18-a first mud pump; a 19-hydrate decomposer; 20-seventh valve; 21-a carbon dioxide storage tank; 22-eighth valve; 23-a hydrating agent recovery tank; 24-ninth valve; 25-a second mud pump; 26-tenth valve; 27-a gas-liquid separator; 28-a vacuum pump; 29-needle valve; 30-eleventh valve; 31-twelfth valve; 32-a data acquisition unit; 33-gas analyzer; 34-a computer; 35-a temperature sensor; 36-a first pressure sensor; 37-a second pressure sensor; 38-a third pressure sensor.
Detailed Description
The following description of the embodiments of the present invention will be made clearly and completely with reference to the accompanying drawings, in which it is apparent that the embodiments described are only some embodiments of the present invention, but not all embodiments. All other embodiments, which can be made by those skilled in the art based on the embodiments of the invention without making any inventive effort, are intended to be within the scope of the invention.
The invention aims to provide a circulating type biological natural gas decarbonization system and method, which improve the decarbonization efficiency of biological natural gas.
In order that the above-recited objects, features and advantages of the present invention will become more readily apparent, a more particular description of the invention will be rendered by reference to the appended drawings and appended detailed description.
Example 1
As shown in fig. 1, the present embodiment provides a circulating type biogas decarbonization system, which includes:
the air source pretreatment unit is used for sequentially carrying out pressurization treatment and precooling treatment on the biological natural air source 1 to obtain a pretreated air source.
And the hydration reaction unit is used for carrying out hydration reaction on the pretreated gas source and the hydration agent to generate a gas phase and a hydrate phase.
And the hydrate decomposition and collection unit is used for collecting the hydrate phase and decomposing the hydrate phase to generate a hydration agent.
And the hydration agent recovery unit is used for recovering the hydration agent generated by the hydrate decomposition and collection unit and conveying the recovered hydration agent to the hydration reaction unit.
And a gas analyzer 33 for detecting the concentration of methane in the gas phase generated by the hydration reaction unit.
A methane collection unit for collecting a gas phase product generated by the hydration reaction unit when the methane concentration detected by the gas analyzer 33 is greater than a set concentration value; when the methane concentration detected by the gas analyzer 33 is less than or equal to a set concentration value, the gas phase generated by the hydration reaction unit is sent to the gas source pretreatment unit.
The air source pretreatment unit comprises a first booster pump 3, a second booster pump 4 and an air pre-cooling device 6 which are sequentially connected; the first booster pump 3 is used for carrying out primary pressurization on the biological natural gas source 1, the second booster pump 4 is used for carrying out secondary pressurization on the biological natural gas source 1 output by the first booster pump 3, and the gas precooling device 6 is used for carrying out precooling treatment on the biological natural gas source 1 output by the second booster pump 4.
The biological natural gas source 1, the first booster pump 3, the second booster pump 4 and the gas precooling device 6 are connected by a one-way pipeline.
The biological natural gas source 1 is pressurized to 3.0 MPa-5.0 MPa after being pressurized for the second time, and the precooling device precools the biological natural gas source 1 to 273K-279K.
In terms of delivering the gas phase generated by the hydration reaction unit to the gas source pretreatment unit when the methane concentration detected by the gas analyzer 33 is less than or equal to a set concentration value, the methane collection unit is specifically configured to deliver the gas phase generated by the hydration reaction unit to the second booster pump 4 when the methane concentration detected by the gas analyzer 33 is less than or equal to a set concentration value.
The hydration reaction unit comprises a high-pressure reaction kettle 8 and a constant-temperature cold bath device 9, wherein the high-pressure reaction kettle 8 is connected with the air source pretreatment unit, the high-pressure reaction kettle 8 is arranged in the constant-temperature cold bath device 9, and the high-pressure reaction kettle 8 is used for carrying out hydration reaction on the pretreated air source and the hydrating agent to generate a gas phase and a hydrate phase. A gas hydrate formation promoter having a predetermined concentration is added to the autoclave 8.
After the reaction in the autoclave 8 is completed, the gas analyzer 33 detects the concentration of each component in the gas phase in the autoclave 8.
A temperature sensor 35 is arranged in the high-pressure reaction kettle 8, a first pressure sensor 36 is arranged at a gas inlet of the high-pressure reaction kettle 8, and a second pressure sensor 37 is arranged at a gas outlet of the high-pressure reaction kettle 8.
The circulating type biological natural gas decarburization system further comprises a data acquisition unit 32 and a computer 34, wherein the data acquisition unit 32 is used for acquiring monitoring data of the temperature sensor 35, the first pressure sensor 36 and the second pressure sensor 37. The data acquisition unit 32 is used for acquiring and recording temperature and pressure data in the autoclave 8 in real time. When the temperature and pressure data in the autoclave 8 are in accordance with the reaction conditions of the hydration reaction, the gas and the hydrating agent are subjected to the hydration reaction to make the impurity gas (carbon dioxide) generate gas hydrate, and the required gas (methane) does not generate hydrate.
The gas precooling device 6 is embedded with a pressure gauge and a thermometer, and the pressure gauge and the thermometer are connected with the data acquisition unit 32.
The data acquisition unit 32 and the gas analyzer 33 are connected with the computer 34 through electrical signals. The computer 34 is used to monitor the temperature, pressure and concentration of the components of the biogas in the autoclave 8. The communication connection is indicated by the dashed line in fig. 1.
The circulating biological natural gas decarbonization system further comprises a vacuum unit, and the hydration reaction unit is connected with the vacuum unit through a one-way pipeline. The vacuum unit is used for vacuumizing pipelines related to the air source pretreatment unit, the hydration reaction unit, the hydrate decomposition and collection unit, the hydrating agent recovery unit and the methane collection unit before decarbonizing the biological natural gas.
The hydrate decomposition and collection unit comprises a first slurry pump 18, a hydrate decomposer 19 and a carbon dioxide gas storage tank 21 which are sequentially connected; the first slurry pump 18 is used for conveying the hydrate phase generated by the hydration reaction unit to the hydrate decomposer 19, the hydrate decomposer 19 is used for decomposing the hydrate phase to generate impurity gas and a hydrating agent, the impurity gas comprises carbon dioxide, and the carbon dioxide storage tank 21 is used for collecting the impurity gas.
The hydrating agent recovery unit comprises a hydrating agent recovery tank 23 and a second slurry pump 25 which are sequentially connected, wherein the hydrating agent recovery tank 23 is used for recovering the hydrating agent generated by the hydrate decomposition collecting unit, and the second slurry pump 25 is used for conveying the hydrating agent recovered by the hydrating agent recovery tank 23 to the hydration reaction unit.
The methane collecting unit comprises a back pressure valve 11, a buffer tank 12, a hand pump 13, a carbon dioxide absorbing device 15 and a methane gas storage tank 16, wherein one end of the back pressure valve 11 is connected with the hydration reaction unit through a pipeline, the other end of the back pressure valve 11 is respectively connected with one end of the buffer tank 12 and the carbon dioxide absorbing device 15 through a pipeline, the other end of the buffer tank 12 is connected with the hand pump 13 through a pipeline, the carbon dioxide absorbing device 15 is further connected with the methane gas storage tank 16 through a pipeline, and the carbon dioxide absorbing device 15 is used for removing carbon dioxide in gas-phase products. The hand pump 13 is embedded with a pressure gauge.
The invention separates the gas phase and the hydrate phase after hydration reaction, pumps the hydrate phase out to a hydrate decomposer 19 for decomposition by a first slurry pump 18, collects the decomposed gas by a carbon dioxide gas storage tank 21, feeds the decomposed liquid phase to a hydration agent recovery tank 23, and pumps the decomposed liquid phase to a high-pressure reaction kettle 8 by a second slurry pump 25 to realize the recovery cycle of the hydrate phase. The components of the gas phase after the hydration reaction are measured, and when the measurement result does not reach the output concentration, the gas phase enters the second booster pump 4 again through the circulating pipeline to realize gas phase circulating treatment; after the gas phase components reach the required concentration, the gas is controlled to be slowly output through a hand pump 13, and is output to a gas storage tank to store target gas after the residual carbon dioxide is removed through a carbon dioxide absorption device 15.
A first valve 2 is arranged between the first booster pump 3 and the biological natural gas source 1. A second valve 5 is arranged between the second booster pump 4 and the gas precooling device 6. A third valve 7 is arranged between the gas precooling device 6 and the first inlet of the high-pressure reaction kettle 8, the second inlet of the high-pressure reaction kettle 8 is connected with a second slurry pump 25, and a fourth valve 10 is arranged between the gas phase outlet of the high-pressure reaction kettle 8 and the back pressure valve 11. A fifth valve 14 is provided between the back pressure valve 11 and the carbon dioxide absorbing device 15. A sixth valve 17 is arranged between the hydrate phase outlet of the high-pressure reaction kettle 8 and the first slurry pump 18. A seventh valve 20 is provided between the hydrate decomposer 19 and the carbon dioxide gas tank 21. An eighth valve 22 is provided between the hydrate decomposer 19 and the hydrating agent recovery tank 23. A ninth valve 24 is provided between the hydrating agent recovery tank 23 and the second mud pump 25. A tenth valve 26 is provided between the first inlet of the autoclave 8 and the gas analyzer 33, an eleventh valve 30 is provided between the gas phase outlet of the autoclave 8 and the gas-liquid separator 27, and a twelfth valve 31 is provided between the gas phase outlet of the autoclave 8 and the gas analyzer 33.
The gas precooling device 6 in the gas source pretreatment unit is connected with the high-pressure reaction kettle 8 in the hydration reaction unit through a one-way pipeline, and a third valve 7 is arranged on the pipeline.
The vacuum unit comprises a gas-liquid separator 27, a vacuum pump 28 and a needle valve 29. The gas-liquid separator 27 is used for preventing liquid from entering the hydration reaction unit, the eleventh valve 30 and the gas phase outlet of the high-pressure reaction kettle 8 are provided with a third pressure sensor 38, and the third pressure sensor 38 is used for judging the vacuum degree of the system.
The hydrating agent is water, and in order to make the reaction efficiency higher, the hydrating agent can be added with a gas hydrate generation accelerant with set concentration, such as an accelerant of compounding sodium dodecyl sulfate (Sodium dodecylsulfate, SDS) and Tetrahydrofuran (THF).
The set concentration value was 97%.
The hydrate decomposition collecting unit, the hydrating agent recovering unit and the hydration reaction unit are connected through a circulation pipeline, more specifically, the high-pressure reaction kettle 8, the sixth valve 17, the first slurry pump 18, the hydrate decomposer 19, the eighth valve 22, the hydrating agent recovering tank 23, the ninth valve 24, the second slurry pump 25 and the high-pressure reaction kettle 8 are sequentially connected through pipelines to form a circulation pipeline.
The generated gas hydrate (hydrate phase) is pumped out of the high-pressure reaction kettle 8 through a first slurry pump 18 to a hydrate decomposer 19 for decomposition, decomposed impurity gas (carbon dioxide) enters a carbon dioxide storage tank 21 for storage, and residual gas in the high-pressure reaction kettle 8 enters the high-pressure reaction kettle 8 again through a circulating pipeline for hydration reaction after being detected by a gas analyzer 33. Thus, the invention completes the separation process of hydration reaction products. The hydrating agent produced in the hydrate decomposer 19 is pumped into the autoclave 8 by the second slurry pump 25 for reuse. The system of the invention finishes the cyclic utilization of the hydrating agent, and further improves the economy of biological natural gas purification.
In the circulating type biological natural gas decarbonization system, a biological natural gas source 1 is subjected to pressurization and precooling pretreatment in sequence, the pretreated biological natural gas can ensure pressure and temperature conditions required by gas hydrate generation before entering a hydration reactor, the pretreated biological natural gas reacts with a hydrating agent to generate gas hydrate after entering the hydration reactor, carbon dioxide gas generates the hydrate and is stored in a solid form in a hydrate phase by controlling the pressure and temperature conditions, and methane gas does not generate the hydrate and exists in the gas phase in a gas form, so that decarbonization treatment of the biological natural gas is realized, and the biological natural gas is purified and purified by a hydrate method, so that the decarbonization efficiency of the biological natural gas is further improved; the gas hydrate generated in the hydration reaction is conveyed into a hydrate decomposer 19 through a slurry pump, the concentration of each component of the residual gas in the hydration reactor is detected through a gas analyzer 33, and when the methane concentration is less than 97%, the residual gas enters the hydration reactor again through a circulating pipeline for hydration reaction; when the methane concentration is more than or equal to 97%, the gas is output to a methane collecting tank for storage.
The specific working flow of the circulating type biological natural gas decarburization system is as follows.
(1) Under the condition that all valves of the circulating type biological natural gas decarbonization system are closed, the back pressure valve 11 is opened, the hand pump 13 is rotated to enable the pressure gauge on the hand pump 13 to be 10MPa, and the back pressure valve 11 is closed, so that the pressure safety protection of the system is realized.
(2) Opening a first valve 2, closing the first valve 2 after the biological natural gas source 1 enters a first booster pump 3 through the first valve 2, pressurizing the biological natural gas source 1 in the first booster pump 3 for the first time, then entering a second booster pump 4 for the second time, pressurizing the biological natural gas to reach the required pressure condition (3.0-5.0 MPa), opening a second valve 5, and leading the pressurized gas to enter a gas precooling device 6 for precooling treatment (precooling the gas source to 273-279K); the second valve 5 is closed.
(3) After the biological natural gas is pre-cooled in the gas pre-cooling device 6, the biological natural gas reaches a required temperature condition, and then enters the high-pressure reaction kettle 8 through the third valve 7 for hydration reaction, and the third valve 7 is closed; the reaction conditions are controlled by the pressurizing device, the first pressurizing pump 3, the second pressurizing pump 4 and the gas pre-cooling device 6, the temperature sensor 35, the first pressure sensor 36 and the second pressure sensor 37 monitor the reaction conditions in the high-pressure reaction kettle 8 through the data acquisition unit 32 and the computer 34, so that the impurity gas (carbon dioxide) generates gas hydrate, and the target gas (methane) does not generate hydrate;
(3) The gas phase and the hydrate phase obtained in the high-pressure reaction kettle 8 enter different pipelines through a fourth valve 10 and a sixth valve 17 respectively for further treatment. Opening a sixth valve 17, enabling the decomposed impurity gas (carbon dioxide) to enter a carbon dioxide storage tank 21 for storage under the action of a first slurry pump 18, enabling the decomposed impurity gas (carbon dioxide) to enter a hydrate decomposer 19 for decomposition, closing the sixth valve 17, opening a seventh valve 20, opening an eighth valve 22, enabling a hydrating agent generated in a hydrate decomposer 1919 to enter a hydrating agent recovery tank 23 through the eighth valve 22, closing the eighth valve 22, opening a ninth valve 24, and pumping the hydrating agent into a high-pressure reaction kettle 8 for reuse through a second slurry pump 25;
(4) The gas phase after each hydration reaction in the high-pressure reaction kettle 8 enters a gas analyzer 33 through a tenth valve 26 for component detection, when the detection result does not accord with the output concentration, the fourth valve 10 is opened, the gas phase enters the second booster pump 4 through the fourth valve 10, the fourth valve 10 is closed, the gas enters the gas precooling device 6 through the second valve 5 for precooling treatment after being pressurized, and enters the high-pressure reaction kettle 8 again through the third valve 7; after the gas phase component reaches the required concentration, a twelfth booster pump is opened, so that the gas in the high-pressure reaction kettle 8 enters the gas analyzer 33 through the twelfth booster pump to perform component detection analysis again, the twelfth booster pump is closed, when the gas phase component is consistent with the target concentration, the fourth valve 10 and the fifth valve 14 are opened, the back pressure valve 11 is opened, the hand pump 13 is rotated to slowly output the gas, and after the removal of residual carbon dioxide is realized through the carbon dioxide absorbing device 15, the gas is output to the methane gas storage tank 16 to be stored.
The biological natural gas is treated by links such as a gas buffer tank 12, a gas booster, a gas precooling device 6, a hydration reactor, a hydrate storage tank, a hydrate decomposition collector, a hydrating agent recovery tank 23 and the like through steps (1), (2), (3) and (4), and the unreacted and completely mixed gas enters the hydration reactor again through a circulation pipeline through a tenth valve 26 for hydration reaction, and the purification and purification efficiency of the biological natural gas is further improved through multistage circulation treatment, and the economy of the biological natural gas purification and separation process is improved. According to the components of the biological natural gas, proper hydrate generation conditions are selected for treatment through the steps, so that the efficient purification and purification of the biological natural gas are further realized.
The invention has the following beneficial effects:
(1) According to the invention, the hydration reaction efficiency of the biological natural gas can be further improved by carrying out pressurization and precooling pretreatment on the biological natural gas source, so that the efficient separation and purification of the biological natural gas are realized.
(2) The hydration agent after the hydrate decomposition can be recycled, and the economy of the biological natural gas decarbonization system and method is further improved.
(3) The invention carries out multistage circulation separation on the residual gas after hydration separation, further saves the pressurizing cost, and can purify the biological natural gas to the specified concentration.
(4) According to the components of the biological natural gas, proper hydrate generation conditions are selected for treatment, so that safe and efficient decarbonization of the biological natural gas is realized.
(5) The invention has the advantages of low cost, low energy consumption, high separation efficiency, good safety performance and the like, and has strong adaptability.
Example 2
The embodiment provides a circulating biological natural gas decarbonization method, which comprises the following steps:
step 101: the air source pretreatment unit sequentially carries out pressurization treatment and precooling treatment on the biological natural air source to obtain a pretreated air source.
Step 102: the hydration reaction unit carries out hydration reaction on the pretreated gas source and the hydration agent to generate gas phase and hydrate phase.
Step 103: the hydrate decomposition and collection unit collects the hydrate phase and decomposes the hydrate phase to produce a hydrate.
Step 104: the hydration agent recovery unit recovers the hydration agent generated by the hydrate decomposition collection unit and conveys the recovered hydration agent to the hydration reaction unit.
Step 105: and detecting the concentration of methane in the gas phase generated by the hydration reaction unit by a gas analyzer.
Step 106: the methane collecting unit is used for collecting gas phase products generated by the hydration reaction unit when the methane concentration detected by the gas analyzer is larger than a set concentration value; and when the methane concentration detected by the gas analyzer is smaller than or equal to a set concentration value, conveying the gas phase generated by the hydration reaction unit to the gas source pretreatment unit.
In the present specification, each embodiment is described in a progressive manner, and each embodiment is mainly described in a different point from other embodiments, and identical and similar parts between the embodiments are all enough to refer to each other. For the method disclosed in the embodiment, since it corresponds to the system disclosed in the embodiment, the description is relatively simple, and the relevant points refer to the system part.
The principles and embodiments of the present invention have been described herein with reference to specific examples, the description of which is intended only to assist in understanding the methods of the present invention and the core ideas thereof; also, it is within the scope of the present invention to be modified by those of ordinary skill in the art in light of the present teachings. In view of the foregoing, this description should not be construed as limiting the invention.
Claims (10)
1. A cyclic biogas decarbonization system comprising:
the air source pretreatment unit is used for sequentially carrying out pressurization treatment and precooling treatment on the biological natural air source to obtain a pretreated air source;
the hydration reaction unit is used for carrying out hydration reaction on the pretreated air source and the hydration agent to generate a gas phase and a hydrate phase;
a hydrate decomposition and collection unit for collecting the hydrate phase and decomposing the hydrate phase to generate a hydrate;
a hydration agent recovery unit for recovering the hydration agent generated by the hydrate decomposition and collection unit and delivering the recovered hydration agent to the hydration reaction unit;
a gas analyzer for detecting the concentration of methane in the gas phase generated by the hydration reaction unit;
a methane collection unit for collecting a gas phase product generated by the hydration reaction unit when the methane concentration detected by the gas analyzer is greater than a set concentration value; and when the methane concentration detected by the gas analyzer is smaller than or equal to a set concentration value, conveying the gas phase generated by the hydration reaction unit to the gas source pretreatment unit.
2. The circulating type biological natural gas decarburization system of claim 1, wherein the gas source pretreatment unit comprises a first booster pump, a second booster pump and a gas precooling device which are sequentially connected; the first booster pump is used for carrying out primary booster on the biological natural gas source, the second booster pump is used for carrying out secondary booster on the biological natural gas source output by the first booster pump, and the gas precooling device is used for carrying out precooling treatment on the biological natural gas source output by the second booster pump;
the methane collection unit is specifically configured to, when the methane concentration detected by the gas analyzer is less than or equal to a set concentration value, convey the gas phase generated by the hydration reaction unit to the second booster pump in terms of conveying the gas phase generated by the hydration reaction unit to the gas source pretreatment unit.
3. The circulating type biological natural gas decarburization system of claim 1, wherein the hydration reaction unit comprises a high-pressure reaction kettle and a constant-temperature cold bath device, the high-pressure reaction kettle is connected with the gas source pretreatment unit, the high-pressure reaction kettle is arranged in the constant-temperature cold bath device, and the high-pressure reaction kettle is used for carrying out hydration reaction on the pretreated gas source and the hydration agent to generate gas phase and hydrate phase.
4. The circulating type biological natural gas decarburization system according to claim 3, wherein a temperature sensor is arranged in the high-pressure reaction kettle, a first pressure sensor is arranged at a gas inlet of the high-pressure reaction kettle, and a second pressure sensor is arranged at a gas outlet of the high-pressure reaction kettle;
the circulating type biological natural gas decarburization system further comprises a data acquisition unit, wherein the data acquisition unit is used for acquiring monitoring data of the temperature sensor, the first pressure sensor and the second pressure sensor.
5. The circulating type biological natural gas decarburization system of claim 1, wherein the hydrate decomposition collection unit comprises a first slurry pump, a hydrate decomposer and a carbon dioxide gas storage tank which are sequentially connected; the first slurry pump is used for conveying the hydrate phase generated by the hydration reaction unit to the hydrate decomposer, the hydrate decomposer is used for decomposing the hydrate phase to generate impurity gas and a hydrating agent, the impurity gas comprises carbon dioxide, and the carbon dioxide gas storage tank is used for collecting the impurity gas.
6. The circulating type biogas decarbonization system of claim 1, wherein the hydrating agent recovery unit comprises a hydrating agent recovery tank and a second slurry pump which are sequentially connected, the hydrating agent recovery tank is used for recovering the hydrating agent generated by the hydrate decomposition collecting unit, and the second slurry pump is used for conveying the hydrating agent recovered by the hydrating agent recovery tank to the hydration reaction unit.
7. The circulating type biological natural gas decarbonization system according to claim 1, wherein the methane collecting unit comprises a back pressure valve, a buffer tank, a hand pump, a carbon dioxide absorbing device and a methane gas storage tank, one end of the back pressure valve is connected with the hydration reaction unit, the other end of the back pressure valve is respectively connected with one end of the buffer tank and the carbon dioxide absorbing device, the other end of the buffer tank is connected with the hand pump, the carbon dioxide absorbing device is further connected with the methane gas storage tank, and the carbon dioxide absorbing device is used for removing carbon dioxide in gas phase products.
8. The circulating biogas decarbonization system of claim 1, wherein the hydrating agent is water.
9. The circulating biogas decarbonization system of claim 1, wherein the set concentration value is 97%.
10. A method for decarbonizing a circulating biogas, comprising:
the air source pretreatment unit sequentially carries out pressurization treatment and precooling treatment on the biological natural air source to obtain a pretreated air source;
the hydration reaction unit carries out hydration reaction on the pretreated air source and the hydration agent to generate a gas phase and a hydrate phase;
the hydrate decomposition and collection unit collects the hydrate phase and decomposes the hydrate phase to generate a hydrate;
the hydration agent recovery unit is used for recovering the hydration agent generated by the hydrate decomposition and collection unit and conveying the recovered hydration agent to the hydration reaction unit;
detecting the concentration of methane in a gas phase generated by the hydration reaction unit by a gas analyzer;
the methane collecting unit is used for collecting gas phase products generated by the hydration reaction unit when the methane concentration detected by the gas analyzer is larger than a set concentration value; and when the methane concentration detected by the gas analyzer is smaller than or equal to a set concentration value, conveying the gas phase generated by the hydration reaction unit to the gas source pretreatment unit.
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