CN111396010B - Clean energy-taking system and method for coal bed gas field - Google Patents
Clean energy-taking system and method for coal bed gas field Download PDFInfo
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- CN111396010B CN111396010B CN202010382214.5A CN202010382214A CN111396010B CN 111396010 B CN111396010 B CN 111396010B CN 202010382214 A CN202010382214 A CN 202010382214A CN 111396010 B CN111396010 B CN 111396010B
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- 239000003245 coal Substances 0.000 title claims abstract description 91
- 238000000034 method Methods 0.000 title claims abstract description 15
- 239000007789 gas Substances 0.000 claims abstract description 226
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 93
- 238000002309 gasification Methods 0.000 claims abstract description 74
- 238000000926 separation method Methods 0.000 claims abstract description 65
- 239000001257 hydrogen Substances 0.000 claims abstract description 58
- 229910052739 hydrogen Inorganic materials 0.000 claims abstract description 58
- 238000004519 manufacturing process Methods 0.000 claims abstract description 54
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims abstract description 52
- 238000001179 sorption measurement Methods 0.000 claims abstract description 32
- 239000007788 liquid Substances 0.000 claims abstract description 28
- 238000000746 purification Methods 0.000 claims abstract description 27
- 238000002347 injection Methods 0.000 claims abstract description 23
- 239000007924 injection Substances 0.000 claims abstract description 23
- 238000002485 combustion reaction Methods 0.000 claims abstract description 16
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims abstract description 12
- 229910052799 carbon Inorganic materials 0.000 claims abstract description 12
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims description 36
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 27
- 229910002091 carbon monoxide Inorganic materials 0.000 claims description 27
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims description 23
- 229910002092 carbon dioxide Inorganic materials 0.000 claims description 18
- 239000001569 carbon dioxide Substances 0.000 claims description 18
- 238000000605 extraction Methods 0.000 claims description 15
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 9
- 238000005516 engineering process Methods 0.000 claims description 9
- 239000001301 oxygen Substances 0.000 claims description 9
- 229910052760 oxygen Inorganic materials 0.000 claims description 9
- 239000002994 raw material Substances 0.000 claims description 8
- 150000002431 hydrogen Chemical class 0.000 claims description 6
- 150000003839 salts Chemical class 0.000 claims description 6
- 239000000126 substance Substances 0.000 claims description 6
- 238000006243 chemical reaction Methods 0.000 claims description 4
- 238000005265 energy consumption Methods 0.000 claims description 4
- 238000010438 heat treatment Methods 0.000 claims description 4
- 239000007787 solid Substances 0.000 claims description 4
- 238000001816 cooling Methods 0.000 claims description 3
- 238000006073 displacement reaction Methods 0.000 claims description 3
- 239000000428 dust Substances 0.000 claims description 3
- 230000000694 effects Effects 0.000 claims description 3
- 239000000203 mixture Substances 0.000 claims description 3
- 238000006057 reforming reaction Methods 0.000 claims description 3
- 238000007789 sealing Methods 0.000 claims description 3
- 238000009628 steelmaking Methods 0.000 claims description 3
- 238000004140 cleaning Methods 0.000 claims 1
- 238000011161 development Methods 0.000 abstract description 8
- 238000012544 monitoring process Methods 0.000 abstract description 3
- 230000018109 developmental process Effects 0.000 description 7
- 230000007547 defect Effects 0.000 description 6
- 239000003034 coal gas Substances 0.000 description 4
- 230000007613 environmental effect Effects 0.000 description 3
- 238000010276 construction Methods 0.000 description 2
- 238000005553 drilling Methods 0.000 description 2
- 230000004075 alteration Effects 0.000 description 1
- 230000033558 biomineral tissue development Effects 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 230000005611 electricity Effects 0.000 description 1
- 238000011065 in-situ storage Methods 0.000 description 1
- 238000005065 mining Methods 0.000 description 1
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- 238000005057 refrigeration Methods 0.000 description 1
- 238000011160 research Methods 0.000 description 1
- 239000002910 solid waste Substances 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
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- E—FIXED CONSTRUCTIONS
- E21—EARTH OR ROCK DRILLING; MINING
- E21B—EARTH OR ROCK DRILLING; OBTAINING OIL, GAS, WATER, SOLUBLE OR MELTABLE MATERIALS OR A SLURRY OF MINERALS FROM WELLS
- E21B43/00—Methods or apparatus for obtaining oil, gas, water, soluble or meltable materials or a slurry of minerals from wells
- E21B43/16—Enhanced recovery methods for obtaining hydrocarbons
- E21B43/24—Enhanced recovery methods for obtaining hydrocarbons using heat, e.g. steam injection
- E21B43/243—Combustion in situ
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- 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
- C10L3/08—Production of synthetic natural gas
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- E—FIXED CONSTRUCTIONS
- E21—EARTH OR ROCK DRILLING; MINING
- E21B—EARTH OR ROCK DRILLING; OBTAINING OIL, GAS, WATER, SOLUBLE OR MELTABLE MATERIALS OR A SLURRY OF MINERALS FROM WELLS
- E21B43/00—Methods or apparatus for obtaining oil, gas, water, soluble or meltable materials or a slurry of minerals from wells
- E21B43/16—Enhanced recovery methods for obtaining hydrocarbons
- E21B43/24—Enhanced recovery methods for obtaining hydrocarbons using heat, e.g. steam injection
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- E—FIXED CONSTRUCTIONS
- E21—EARTH OR ROCK DRILLING; MINING
- E21B—EARTH OR ROCK DRILLING; OBTAINING OIL, GAS, WATER, SOLUBLE OR MELTABLE MATERIALS OR A SLURRY OF MINERALS FROM WELLS
- E21B43/00—Methods or apparatus for obtaining oil, gas, water, soluble or meltable materials or a slurry of minerals from wells
- E21B43/295—Gasification of minerals, e.g. for producing mixtures of combustible gases
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- E21—EARTH OR ROCK DRILLING; MINING
- E21B—EARTH OR ROCK DRILLING; OBTAINING OIL, GAS, WATER, SOLUBLE OR MELTABLE MATERIALS OR A SLURRY OF MINERALS FROM WELLS
- E21B43/00—Methods or apparatus for obtaining oil, gas, water, soluble or meltable materials or a slurry of minerals from wells
- E21B43/30—Specific pattern of wells, e.g. optimising the spacing of wells
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
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- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P90/00—Enabling technologies with a potential contribution to greenhouse gas [GHG] emissions mitigation
- Y02P90/70—Combining sequestration of CO2 and exploitation of hydrocarbons by injecting CO2 or carbonated water in oil wells
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Abstract
The clean energy-taking system and the clean energy-taking method for the coal-bed gas field are characterized in that two coal-bed gas wells entering a decay phase and one coal-bed gas well still in a production phase are selected from the coal-bed gas field, wherein the two coal-bed gas wells entering the decay phase are a first coal-bed gas well and a second coal-bed gas well respectively, the coal-bed gas well still in the production phase is a third coal-bed gas well, and the depths of the first coal-bed gas well, the second coal-bed gas well and the third coal-bed gas well are sequentially increased, and the clean energy-taking system comprises a first pressure swing adsorption separation device, an air injection pump, a supercritical water gasification hydrogen production device, a gas-solid-liquid separation device, a heat exchange device and a gas separation and purification liquefaction device; the invention effectively implements secondary development and utilization of the coal bed gas field in the decay period, omits various equipment such as gasifier building, combustion control and monitoring, greatly reduces the underground coal gasification cost, has low carbon emission, and obtains new high added value products.
Description
Technical Field
The invention belongs to the technical field of comprehensive development and utilization of coal bed gas and coal underground gasification, and particularly relates to a clean energy taking system and method for coal bed gas.
Background
Coal is fossil energy with the largest existing quantity and the largest exploitation quantity in China, exploitation history reaches hundreds of years, especially high-strength exploitation is improved and opened, shallow coal beds are basically exploited, exploitation difficulty of middle-deep coal beds is high, cost is high, and efficient and low-cost exploitation of abundant middle-deep coal resources becomes a research direction. Through decades of exploratory practice, underground coal gasification has become the most dominant in situ means of mining. Underground coal gasification is carried out by drilling a vertical well/horizontal well, constructing an underground gasifier and a combustion main channel, injecting air into a well A, controllably burning underground to generate raw gas, producing raw gas by a well B, and generating electricity on the ground or purifying and utilizing the raw gas.
In recent years, the development of green economy puts higher demands on environmental protection, coal is used as fossil energy, and the characteristics of complex combustion waste and high carbon are unfavorable for the environment. As an important technical direction for efficiently developing medium-deep coal resources, the underground coal gasification technology has the serious defects of high cost for building a new well and underground gasification furnace, low comprehensive heat efficiency, insufficient deep processing and utilization of raw coal gas, high carbon emission and the like. Although documents and patents innovate the hydrogen production process based on the underground coal gasification technology, the underground gasification process still has important defects of low efficiency, high control difficulty, low comprehensive heat efficiency and the like.
Disclosure of Invention
The invention aims to solve the defects in the prior art, and provides a clean energy-taking system and method for coal bed gas fields, which are mature in technology, controllable in flow, wide in application range, high in thermal efficiency, rich in products and capable of being effectively utilized.
In order to solve the technical problems, the invention adopts the following technical scheme: the clean energy-taking system of the coal-bed gas field comprises a first pressure swing adsorption separation device, an air injection pump, a supercritical water gasification hydrogen production device, a gas-solid-liquid separation device, a heat exchange device and a gas separation and purification liquefaction device, wherein the first pressure swing adsorption separation device is used for preparing hydrogen from supercritical water;
the crude oxygen outlet of the first pressure swing adsorption separation device is connected with the wellhead of the first coal bed gas well through an air injection pipe, the air injection pump is arranged on the air injection pipe, the wellhead of the second coal bed gas well is connected with the air inlet of the supercritical water gasification hydrogen production device through a mixed gas exhaust pipe, the wellhead of the third coal bed gas well is connected with the air inlet of the supercritical water gasification hydrogen production device through a methane gas exhaust pipe, the air outlet of the supercritical water gasification hydrogen production device is connected with the high-temperature air inlet of the heat exchange device through a high-temperature mixed gas conveying pipe, the wellhead of the third coal bed gas well is connected with the low-temperature water inlet of the heat exchange device through a coal bed water exhaust pipe, the low-temperature air outlet of the heat exchange device is connected with the inlet of the gas-solid-liquid separation device, the high-temperature water outlet of the heat exchange device is connected with the air inlet of the supercritical water gasification hydrogen production device and the air injection pipe respectively through a water vapor pipeline, the air outlet of the gas-solid-liquid separation device is connected with the air inlet of the gas separation and purification liquefaction device through a mixed gas pipeline, and the combustible gas outlet of the gas separation and purification liquefaction device is connected with the air inlet of the supercritical water gasification device through a combustible gas pipeline.
The gas separation and purification liquefying device comprises a second pressure swing adsorption separating device and a cryogenic liquefaction purifying separating device which are connected in series, a carbon dioxide gas outlet of the second pressure swing adsorption separating device is connected with a carbon dioxide liquefying device, a gas inlet of the second pressure swing adsorption separating device is connected with a gas outlet of a mixed gas pipeline, and a combustible gas outlet of the cryogenic liquefaction purifying separating device and a combustible gas outlet of the second pressure swing adsorption separating device are connected with a combustible gas pipeline.
The heat exchange device comprises a low-temperature heat exchanger and a high-temperature heat exchanger which are connected in series, a high-temperature water outlet of the low-temperature heat exchanger is connected with a low-temperature water inlet of the high-temperature heat exchanger, and a high-temperature gas inlet of the low-temperature heat exchanger is connected with a low-temperature gas outlet of the high-temperature heat exchanger.
The clean energy-taking method of the clean energy-taking system of the coal-bed gas field comprises the following steps,
(1) Selecting and determining a coal bed gas field in a decay period;
(2) Underground coal is burnt and gasified in a non-control way;
(3) Ground controllable supercritical water gasification hydrogen production;
(4) Step heat extraction of the two-stage exchanger;
(5) Two-stage separation step purification and liquefaction.
The step (1) is that the first coal-bed gas well and the second coal-bed gas well are mined for years, the water in the coal bed is drained successively, the main coal-bed fracturing channel and the cracks are opened, the yield of the gas well is greatly reduced or stopped, and the third coal-bed gas well with deeper depth is still in the production stage, and the coal-bed water and CH are produced 4 Mainly coal bed gas.
The step (2) is specifically that air is simply separated and removed into crude oxygen through a first pressure swing adsorption separation device with mature technology, low cost and general separation effect, then the crude oxygen and high-temperature steam prepared by a high-temperature heat exchanger are injected into a first coal-bed gas well through a gas injection pipe by a gas injection pump, the underground coal bed between the first coal-bed gas well and a second coal-bed gas well is gasified in a non-controlled combustion manner along a coal-bed fracturing main channel and a crack, mixed gas is extracted from the second coal-bed gas well, the mixed gas is conveyed into a supercritical water gasification hydrogen production device through a mixed gas exhaust pipe, and coal-bed water and coal-bed gas produced by a third coal-bed gas well provide a water source and partial methane (CH) for the supercritical water gasification hydrogen production device with underground gasification and ground control 4 ) Raw materials.
Step (3) is that the supercritical water gasification hydrogen production device realizes methane (CH) by adjusting the mixture ratio of mixed gas and steam raw materials under the control of the temperature and the pressure of more than 25MPa at 800 DEG C 4 ) Steam (H) 2 O), carbon monoxide (CO), carbon dioxide (CO) 2 ) Is subjected to chemical reforming reaction to realize the highest hydrogen (H) 2 ) Yield.
The step (4) is that, because the gas produced by the supercritical water gasification hydrogen production device is high-temperature gas with the temperature of 750-850 ℃, a large amount of heat contained in the gas can prepare the coal bed water produced by the third coal bed gas well into water vapor; the high-temperature gas of the high-temperature gas with the temperature of 750-850 ℃ is cooled to the low-temperature gas with the temperature of 30-50 ℃ through two-stage heat exchange cascade heat taking of the high-temperature heat exchanger and the low-temperature heat exchanger, and the low-temperature gas with the temperature of 30-50 ℃ is introduced into the second pressure swing adsorption separation device; the coal bed water is prepared into high-temperature steam after two-stage heat exchange step heating, and the high-temperature steam is introduced into a first coal bed gas well and a supercritical water gasification hydrogen production device so as to realize the underground coal uncontrolled combustion gasification and supercritical water gasification hydrogen production process and realize the minimum heat loss of the system; along with the step heat taking and cooling of the high-temperature gas through the high-temperature heat exchanger and the low-temperature heat exchanger, the high-temperature gas enters the gas-solid-liquid separation device, tar is condensed into liquid to be produced, salt in high-mineralization coal seam water is crystallized and separated out, mixed salt and dust are safely treated by landfill, and the tar can be used as a high-added-value product to be supplied to the steelmaking industry.
Step (5) is specifically to take the factors of large air flow and minimum energy consumption into consideration in two-stage separation step purification and liquefaction for preparing liquid hydrogen, and to use a mature and low-cost second pressure swing adsorption separation device for CO in high-flow low-temperature gas at 30-50 DEG C 2 、CO、CH 4 Performing primary removal and separation, and performing secondary purification and liquefaction of low-flow crude hydrogen by using a cryogenic liquefaction purification separation device to prepare a high-purity liquid hydrogen product;
carbon dioxide (CO) separated in this step 2 ) Liquid CO prepared by condensing by carbon dioxide liquefying device 2 Or solid CO 2 Can meet the carbon sealing requirement of low-temperature fresh-keeping in food industry and cold chain transportation industry, chemical oil displacement in oil and gas exploitation industry, carbon dioxide fracturing and carbon index trading platform, and separate small amounts of CO and CH 4 And the raw material gas is reintroduced into the supercritical water gasification hydrogen production device to carry out the re-reaction.
By adopting the technical scheme, the invention not only overcomes the five defects of high construction cost, low comprehensive heat efficiency, single effective product, high carbon emission and large process control difficulty of the existing coal underground gasification technology, but also provides a new way for environmental protection treatment of highly mineralized water for coal bed gas field development, and realizes scientific connection of coal bed gas development and coal underground gasification.
Compared with the existing underground coal gasification technology, the invention has the following advantages:
(1) The underground coal gasification is carried out by utilizing the coal bed gas field in the decay period and the coal bed gas field net thereof, so that the defect of excessive cost caused by the need of new drilling, construction of an underground gasification furnace, combustion of a main channel and pre-pumping of water in the existing underground coal gasification is avoided, the coal bed water, a main fracturing channel and cracks of the middle and shallow coal bed of the coal bed gas field in the decay period are opened, the underground coal bed combustion can be efficiently carried out, and the secondary development of the coal bed gas field in the decay period is realized;
(2) The deep gas well of the coal bed gas field can provide a water source for underground gasification of the middle and shallow coal beds, solves the problem of environmental protection treatment cost of high mineralization degree coal bed water, and realizes scientific matching and connection of coal bed gas development and underground coal gasification;
(3) The existing underground coal gasification is renovated into underground coal uncontrolled combustion gasification and ground controllable supercritical water gasification hydrogen production, so that the defects of high technical difficulty, immature process and high equipment cost investment caused by underground coal controlled gasification are avoided, and the hydrogen production efficiency is maximized through the controllability of ground engineering equipment and chemical reaction;
(4) The two-stage heat exchange device of the low-temperature heat exchanger and the high-temperature heat exchanger greatly improves the comprehensive heat efficiency of the system, and realizes the effective recycling of tar;
(5) The pressure swing adsorption primary separation-cryogenic liquefaction separation and purification two-stage separation cascade purification and liquefaction can effectively reduce the scale and investment cost of a cryogenic liquefaction separation device, reduce the refrigeration operation energy consumption, and sequentially separate and scientifically liquefy the effective product components to prepare a high-purity liquid hydrogen product;
(6) Converting carbon sources in coal into liquid or solid C0 through reasonable flow 2 Not only realizing low carbon emission of the clean energy-taking process, but also obtaining new high added value products;
(7) The underground uncontrolled combustion gasification process effectively implements secondary development and utilization of the coal bed gas field in the decay period, omits various equipment such as gasifier building, combustion control and monitoring, and the like, and greatly reduces the underground coal gasification cost.
Drawings
Fig. 1 is a schematic structural view of the present invention.
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.
As shown in fig. 1, the clean energy-taking system for the coal-bed gas field selects two coal-bed gas fields entering a decay phase and one coal-bed gas field still in a production phase from the coal-bed gas field, wherein the two coal-bed gas fields entering the decay phase are a first coal-bed gas field 1 and a second coal-bed gas field 2 respectively, the coal-bed gas field still in the production phase is a third coal-bed gas field 3, the depths of the first coal-bed gas field 1, the second coal-bed gas field 2 and the third coal-bed gas field 3 are sequentially increased, and the system comprises a first pressure swing adsorption separation device 4, a gas injection pump 5, a supercritical water gasification hydrogen production device 6, a gas-solid-liquid separation device 7, a heat exchange device and a gas separation and purification liquefaction device;
the crude oxygen outlet of the first pressure swing adsorption separation device 4 is connected with the wellhead of the first coal-bed gas well 1 through an air injection pipe, the air injection pump 5 is arranged on the air injection pipe 8, the wellhead of the second coal-bed gas well 2 is connected with the air inlet of the supercritical water gasification hydrogen production device 6 through a mixed gas exhaust pipe 9, the wellhead of the third coal-bed gas well 3 is connected with the air inlet of the supercritical water gasification hydrogen production device 6 through a methane gas exhaust pipe 10, the air outlet of the supercritical water gasification hydrogen production device 6 is connected with the high-temperature air inlet of the heat exchange device through a high-temperature mixed gas conveying pipe 11, the wellhead of the third coal-bed gas well 3 is connected with the low-temperature water inlet of the heat exchange device through a coal-bed water discharge pipe 12, the low-temperature air outlet of the heat exchange device is connected with the inlet of the gas-solid-liquid separation device 7, the high-temperature air outlet of the heat exchange device is respectively connected with the air inlet of the supercritical water gasification hydrogen production device 6 and the air injection pipe 8 through a water vapor pipeline 13, the air outlet of the gas-solid-liquid separation device 7 is connected with the air inlet of the gas separation and purification device through a mixed gas pipeline 14, and the combustible gas outlet of the gas separation and liquefaction device is connected with the air inlet of the supercritical water gasification hydrogen production device 6 through a combustible gas pipeline 15.
The gas separation and purification liquefying device comprises a second pressure swing adsorption separating device 16 and a cryogenic liquefying and purifying separating device 17 which are connected in series, a carbon dioxide liquefying device 18 is connected to a carbon dioxide gas outlet of the second pressure swing adsorption separating device 16, a gas inlet of the second pressure swing adsorption separating device 16 is connected with a gas outlet of the mixed gas pipeline 14, and a combustible gas outlet of the cryogenic liquefying and purifying separating device 17 and a combustible gas outlet of the second pressure swing adsorption separating device 16 are connected with the combustible gas pipeline 15.
The heat exchange device comprises a low-temperature heat exchanger 19 and a high-temperature heat exchanger 20 which are connected in series, wherein a high-temperature water outlet of the low-temperature heat exchanger 19 is connected with a low-temperature water inlet of the high-temperature heat exchanger 20, and a high-temperature gas inlet of the low-temperature heat exchanger 19 is connected with a low-temperature gas outlet of the high-temperature heat exchanger 20.
The first pressure swing adsorption separation device 4, the gas injection pump 5, the supercritical water gasification hydrogen production device 6, the gas-solid-liquid separation device 7, the low-temperature heat exchanger 19, the high-temperature heat exchanger 20, the second pressure swing adsorption separation device 16 and the cryogenic liquefaction purification separation device 17 are all of the prior art and are commercially available, so that the specific structure and principle thereof are not repeated.
The clean energy-taking method of the clean energy-taking system of the coal-bed gas field comprises the following steps,
(1) Selecting and determining a coal bed gas field in a decay period;
(2) Underground coal is burnt and gasified in a non-control way;
(3) Ground controllable supercritical water gasification hydrogen production;
(4) Step heat extraction of the two-stage exchanger;
(5) Two-stage separation step purification and liquefaction.
The step (1) is that the first coal-bed gas well 1 and the second coal-bed gas well 2 are mined for years, the water in the coal bed is drained, the main coal-bed fracturing channels and the cracks are opened, the gas well yield is greatly reduced or stopped, and the third coal-bed gas well 3 with deeper depth is still in the production stageCoal seam water and CH 4 Mainly coal bed gas.
The step (1) is specifically that air is simply separated and removed by a first pressure swing adsorption separation device 4 with mature technology, low cost and general separation effect to prepare crude oxygen, high-temperature water vapor prepared by a crude oxygen and a high-temperature heat exchanger 20 is injected into a first coal-bed gas well 1 by an air injection pump 5 through an air injection pipe 8, underground coal beds between the first coal-bed gas well 1 and a second coal-bed gas well 2 are gasified in a non-controlled combustion manner along coal bed fracturing main channels and cracks, mixed coal gas is extracted from the second coal-bed gas well 2, the mixed coal gas is conveyed into a supercritical water gasification hydrogen production device 6 through a mixed coal gas exhaust pipe 9, and coal bed water and coal bed gas produced by a third coal-bed gas well 3 provide a water source and partial methane for the underground gasification and ground-controllable supercritical water gasification hydrogen production device 6 (CH) 4 ) Raw materials. The uncontrolled combustion gasification process omits various equipment such as gasifier building, combustion control and monitoring, and the like, thereby greatly reducing the underground gasification cost.
Step (3) is specifically that the supercritical water gasification hydrogen production device 6 realizes methane (CH) by adjusting the mixture ratio of the mixed gas and steam raw materials under the control of the temperature and the pressure of about 800 ℃ and more than 25MPa 4 ) Steam (H) 2 O), carbon monoxide (CO), carbon dioxide (CO) 2 ) Is subjected to chemical reforming reaction to realize the highest hydrogen (H) 2 ) Yield.
The step (4) is that, because the gas produced by the supercritical water gasification hydrogen production device 6 is high temperature gas with the temperature of 750-850 ℃, a large amount of heat contained in the gas can prepare the coal bed water produced by the third coal bed gas well 3 into water vapor; the high-temperature gas of the high-temperature gas with the temperature of 750-850 ℃ is cooled to the low-temperature gas with the temperature of 30-50 ℃ by two-stage heat exchange cascade heat taking of the high-temperature heat exchanger 20 and the low-temperature heat exchanger 19, and the low-temperature gas with the temperature of 30-50 ℃ is introduced into the second pressure swing adsorption separation device 16; the coal bed water is prepared into high-temperature steam after two-stage heat exchange step heating, and the high-temperature steam is introduced into a first coal bed gas well 1 and a supercritical water gasification hydrogen production device 6 so as to realize the underground coal uncontrolled combustion gasification and supercritical water gasification hydrogen production process and realize the minimum heat loss of the system; along with the step heating and cooling of the high-temperature gas through the high-temperature heat exchanger 20 and the low-temperature heat exchanger 19, the high-temperature gas enters the gas-solid-liquid separation device 7, tar is condensed into liquid to be produced, salt in high-mineralization coal bed water is crystallized and separated out, solid waste with safe mixed salt and dust is buried, and the tar can be used as a high-added-value product for steel making industry and the like.
Step (5) is specifically to take the factors of large air flow and minimum energy consumption into consideration in two-stage separation step purification and liquefaction for preparing liquid hydrogen, and the second pressure swing adsorption separation device 16 with mature technology and low cost is used for purifying CO in high-flow low-temperature gas with the temperature of 30-50 DEG C 2 、CO、CH 4 Performing primary removal and separation, and performing secondary purification and liquefaction of low-flow crude hydrogen by using a cryogenic liquefaction purification separation device 17 again to prepare a high-purity liquid hydrogen product;
carbon dioxide (CO) separated in this step 2 ) Liquid CO produced after condensation by the carbon dioxide liquefying device 18 2 Or solid CO 2 Can meet the carbon sealing requirement of low-temperature fresh-keeping in food industry and cold chain transportation industry, chemical oil displacement in oil and gas exploitation industry, carbon dioxide fracturing and carbon index trading platform, and separate small amounts of CO and CH 4 Is reintroduced into the supercritical water gasification hydrogen production device 6 as the feed gas to carry out the re-reaction.
Although embodiments of the present invention have been shown and described, it will be understood by those skilled in the art that various changes, modifications, substitutions and alterations can be made therein without departing from the principles and spirit of the invention, the scope of which is defined in the appended claims and their equivalents.
Claims (6)
1. The clean energy taking method of the clean energy taking system of the coal bed gas field is characterized by comprising the following steps of: the clean energy-taking system of the coal-bed gas field selects two coal-bed gas fields entering a decay phase and one coal-bed gas field still in a production phase from the coal-bed gas field, wherein the two coal-bed gas fields entering the decay phase are respectively a first coal-bed gas field and a second coal-bed gas field, the coal-bed gas field still in the production phase is a third coal-bed gas field, and the depths of the first coal-bed gas field, the second coal-bed gas field and the third coal-bed gas field are sequentially increased, and the clean energy-taking system is characterized in that: comprises a first pressure swing adsorption separation device, an air injection pump, a supercritical water gasification hydrogen production device, a gas-solid-liquid separation device, a heat exchange device and a gas separation and purification liquefaction device;
the crude oxygen outlet of the first pressure swing adsorption separation device is connected with the wellhead of the first coal bed gas well through an air injection pipe, the air injection pump is arranged on the air injection pipe, the wellhead of the second coal bed gas well is connected with the air inlet of the supercritical water gasification hydrogen production device through a mixed gas exhaust pipe, the wellhead of the third coal bed gas well is connected with the air inlet of the supercritical water gasification hydrogen production device through a methane gas exhaust pipe, the air outlet of the supercritical water gasification hydrogen production device is connected with the high-temperature air inlet of the heat exchange device through a high-temperature mixed gas conveying pipe, the wellhead of the third coal bed gas well is connected with the low-temperature water inlet of the heat exchange device through a coal bed water exhaust pipe, the low-temperature air outlet of the heat exchange device is connected with the inlet of the gas-solid-liquid separation device, the high-temperature water outlet of the heat exchange device is connected with the air inlet of the supercritical water gasification hydrogen production device and the lower part of the air injection pipe respectively through a water vapor pipeline, the air outlet of the gas-solid-liquid separation device is connected with the air inlet of the gas separation and purification liquefaction device through a mixed gas pipeline, and the combustible gas outlet of the gas separation and the purification liquefaction device is connected with the air inlet of the supercritical water gasification device through a combustible gas pipeline;
the gas separation and purification liquefying device comprises a second pressure swing adsorption separating device and a cryogenic liquefaction purifying separating device which are connected in series, a carbon dioxide gas outlet of the second pressure swing adsorption separating device is connected with a carbon dioxide liquefying device, a gas inlet of the second pressure swing adsorption separating device is connected with a gas outlet of a mixed gas pipeline, and a combustible gas outlet of the cryogenic liquefaction purifying separating device and a combustible gas outlet of the second pressure swing adsorption separating device are connected with a combustible gas pipeline;
the heat exchange device comprises a low-temperature heat exchanger and a high-temperature heat exchanger which are connected in series, a high-temperature water outlet of the low-temperature heat exchanger is connected with a low-temperature water inlet of the high-temperature heat exchanger, and a high-temperature gas inlet of the low-temperature heat exchanger is connected with a low-temperature gas outlet of the high-temperature heat exchanger;
the cleaning energy-taking method comprises the following steps:
(1) Selecting and determining a coal bed gas field in a decay period;
(2) Underground coal is burnt and gasified in a non-control way;
(3) Ground controllable supercritical water gasification hydrogen production;
(4) Step heat extraction of the two-stage exchanger;
(5) Two-stage separation step purification and liquefaction.
2. The clean energy extraction method of the clean energy extraction system of the coal-bed gas field of claim 1, wherein the clean energy extraction method comprises the following steps: the step (1) is that the first coal-bed gas well and the second coal-bed gas well are mined for years, the water in the coal bed is drained successively, the main coal-bed fracturing channel and the cracks are opened, the yield of the gas well is greatly reduced or stopped, and the third coal-bed gas well with deeper depth is still in the production stage, and the coal-bed water and CH are produced 4 Mainly coal bed gas.
3. The clean energy extraction method of the clean energy extraction system of the coal-bed gas field of claim 2, wherein the clean energy extraction method is characterized by comprising the following steps: the step (2) is specifically that air is simply separated and removed into crude oxygen through a first pressure swing adsorption separation device with mature technology, low cost and general separation effect, then the crude oxygen and high-temperature steam prepared by a high-temperature heat exchanger are injected into a first coal-bed gas well through a gas injection pipe by a gas injection pump, the underground coal bed between the first coal-bed gas well and a second coal-bed gas well is gasified in a non-controlled combustion manner along a coal-bed fracturing main channel and a crack, mixed gas is extracted from the second coal-bed gas well, the mixed gas is conveyed into a supercritical water gasification hydrogen production device through a mixed gas exhaust pipe, and coal-bed water and coal-bed gas produced by a third coal-bed gas well provide a water source and partial methane (CH) for the supercritical water gasification hydrogen production device with underground gasification and ground control 4 ) Raw materials.
4. A method of clean energy capture for a clean energy capture system for a coal bed gas field as claimed in claim 3, wherein: the step (3) is that the supercritical water gasification hydrogen production device is at 800 ℃ and above 25MPaUnder the control of temperature and pressure, the mixture ratio of the mixed gas and the steam raw materials is adjusted to realize methane (CH) 4 ) Steam (H) 2 O), carbon monoxide (CO), carbon dioxide (CO) 2 ) Is subjected to chemical reforming reaction to realize the highest hydrogen (H) 2 ) Yield.
5. The clean energy extraction method of the clean energy extraction system of the coal-bed gas field of claim 4, wherein the clean energy extraction method comprises the following steps: the step (4) is that, because the gas produced by the supercritical water gasification hydrogen production device is high-temperature gas with the temperature of 750-850 ℃, a large amount of heat contained in the gas can prepare the coal bed water produced by the third coal bed gas well into water vapor; the high-temperature gas of the high-temperature gas with the temperature of 750-850 ℃ is cooled to the low-temperature gas with the temperature of 30-50 ℃ through two-stage heat exchange cascade heat taking of the high-temperature heat exchanger and the low-temperature heat exchanger, and the low-temperature gas with the temperature of 30-50 ℃ is introduced into the second pressure swing adsorption separation device; the coal bed water is prepared into high-temperature steam after two-stage heat exchange step heating, and the high-temperature steam is introduced into a first coal bed gas well and a supercritical water gasification hydrogen production device so as to realize the underground coal uncontrolled combustion gasification and supercritical water gasification hydrogen production process and realize the minimum heat loss of the system; along with the step heat taking and cooling of the high-temperature gas through the high-temperature heat exchanger and the low-temperature heat exchanger, the high-temperature gas enters the gas-solid-liquid separation device, tar is condensed into liquid to be produced, salt in high-mineralization coal seam water is crystallized and separated out, mixed salt and dust are safely treated by landfill, and the tar can be used as a high-added-value product to be supplied to the steelmaking industry.
6. The clean energy extraction method of the clean energy extraction system of the coal-bed gas field of claim 5, wherein the clean energy extraction method comprises the following steps: step (5) is specifically to take the factors of large air flow and minimum energy consumption into consideration in two-stage separation step purification and liquefaction for preparing liquid hydrogen, and to use a mature and low-cost second pressure swing adsorption separation device for CO in high-flow low-temperature gas at 30-50 DEG C 2 、CO、CH 4 Performing primary removal and separation, and performing secondary purification and liquefaction of low-flow crude hydrogen by using a cryogenic liquefaction purification and separation device to prepare high-purity liquid hydrogenIs a product of (a);
carbon dioxide (CO) separated in this step 2 ) Liquid CO prepared by condensing by carbon dioxide liquefying device 2 Or solid CO 2 Can meet the carbon sealing requirement of low-temperature fresh-keeping in food industry and cold chain transportation industry, chemical oil displacement in oil and gas exploitation industry, carbon dioxide fracturing and carbon index trading platform, and separate small amounts of CO and CH 4 And the raw material gas is reintroduced into the supercritical water gasification hydrogen production device to carry out the re-reaction.
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Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106640007A (en) * | 2016-12-30 | 2017-05-10 | 中国海洋石油总公司 | Multisource and multielement thermal fluid generating and method |
| CN109252842A (en) * | 2018-10-29 | 2019-01-22 | 邓晓亮 | Overcritical underground coal gasification(UCG) output mixed gas trilogy supply electricity generation system |
Family Cites Families (12)
| Publication number | Priority date | Publication date | Assignee | Title |
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| SU1390238A1 (en) * | 1984-11-27 | 1988-04-23 | Институт Геологии И Геохимии Горючих Ископаемых Ан Усср | Method of underground gasification of coal |
| BRPI0512499A (en) * | 2004-06-23 | 2008-03-11 | Harry B Curlett | methods of extracting thermal energy from a rock formation, completing geothermal production wells, drilling deep wells, developing a high temperature hot dry geothermal reservoir, developing geothermal reservoirs in hot dry rock formations , completing geothermal production wells, generating geothermal production wells and processing chemical reactions |
| AU2011200090B2 (en) * | 2008-06-12 | 2016-01-07 | Winwick Business Solutions Pty Ltd | System for cultivation and processing of microorganisms, processing of products therefrom, and processing in drillhole reactors |
| CN102418476A (en) * | 2011-10-24 | 2012-04-18 | 国鼎(大连)投资有限公司 | Deep coal and coal bed gas combined mining method |
| CN103670338B (en) * | 2012-09-21 | 2016-06-15 | 新奥气化采煤有限公司 | A kind of coal bed gas and coal mining method altogether |
| CN103589472A (en) * | 2013-11-19 | 2014-02-19 | 煤科集团沈阳研究院有限公司 | Mobile low-concentration coal bed gas concentration device and concentration method thereof |
| CH710999A2 (en) * | 2015-04-27 | 2016-10-31 | Von Düring Man Ag | Method for utilizing the internal energy of an aquifer fluid in a geothermal plant. |
| US10920152B2 (en) * | 2016-02-23 | 2021-02-16 | Pyrophase, Inc. | Reactor and method for upgrading heavy hydrocarbons with supercritical fluids |
| CN106630287B (en) * | 2016-12-30 | 2019-06-18 | 西安理工大学 | The overcritical hydro-thermal burning processing of oil recovery waste liquid, steam injection system |
| CN109138952B (en) * | 2018-10-29 | 2024-04-19 | 邓晓亮 | System and method for generating power by underground gasification of supercritical coal |
| CN110187011B (en) * | 2019-07-03 | 2024-04-16 | 新疆维吾尔自治区煤田地质局煤层气研究开发中心 | Simulation experiment device and simulation method for dynamic adsorption and desorption research |
| CN212177118U (en) * | 2020-05-08 | 2020-12-18 | 新疆维吾尔自治区煤田地质局煤层气研究开发中心 | Clean energy-taking system for coal bed gas field |
-
2020
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Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106640007A (en) * | 2016-12-30 | 2017-05-10 | 中国海洋石油总公司 | Multisource and multielement thermal fluid generating and method |
| CN109252842A (en) * | 2018-10-29 | 2019-01-22 | 邓晓亮 | Overcritical underground coal gasification(UCG) output mixed gas trilogy supply electricity generation system |
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