CN111396010A - 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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- 239000003245 coal Substances 0.000 title claims abstract description 151
- 238000000034 method Methods 0.000 title claims abstract description 19
- 239000007789 gas Substances 0.000 claims abstract description 239
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 83
- 238000002309 gasification Methods 0.000 claims abstract description 78
- 238000000926 separation method Methods 0.000 claims abstract description 78
- 239000001257 hydrogen Substances 0.000 claims abstract description 57
- 229910052739 hydrogen Inorganic materials 0.000 claims abstract description 57
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims abstract description 53
- 238000004519 manufacturing process Methods 0.000 claims abstract description 51
- 238000000746 purification Methods 0.000 claims abstract description 34
- 238000001179 sorption measurement Methods 0.000 claims abstract description 31
- 239000007788 liquid Substances 0.000 claims abstract description 25
- 238000002485 combustion reaction Methods 0.000 claims abstract description 20
- 238000002347 injection Methods 0.000 claims abstract description 19
- 239000007924 injection Substances 0.000 claims abstract description 19
- 230000007423 decrease Effects 0.000 claims abstract description 15
- 229910052799 carbon Inorganic materials 0.000 claims abstract description 12
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims abstract description 11
- 238000004140 cleaning Methods 0.000 claims abstract description 6
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims description 36
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims description 36
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 24
- 229910002091 carbon monoxide Inorganic materials 0.000 claims description 24
- 229910002092 carbon dioxide Inorganic materials 0.000 claims description 21
- 239000001569 carbon dioxide Substances 0.000 claims description 18
- 238000005516 engineering process Methods 0.000 claims description 12
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 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 9
- 239000003034 coal gas Substances 0.000 claims description 8
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 6
- 150000003839 salts Chemical class 0.000 claims description 6
- 239000000126 substance Substances 0.000 claims description 6
- 238000000605 extraction Methods 0.000 claims description 5
- 238000005265 energy consumption Methods 0.000 claims description 4
- 150000002431 hydrogen Chemical class 0.000 claims description 4
- 239000007787 solid Substances 0.000 claims description 4
- 238000009833 condensation Methods 0.000 claims description 3
- 230000005494 condensation Effects 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
- 230000008030 elimination Effects 0.000 claims description 3
- 238000003379 elimination reaction Methods 0.000 claims description 3
- 229910052757 nitrogen Inorganic materials 0.000 claims description 3
- 230000009467 reduction Effects 0.000 claims description 3
- 238000006057 reforming reaction Methods 0.000 claims description 3
- 230000009919 sequestration Effects 0.000 claims description 3
- 239000002910 solid waste Substances 0.000 claims description 3
- 238000009628 steelmaking Methods 0.000 claims description 2
- 238000003306 harvesting Methods 0.000 claims 2
- 238000011161 development Methods 0.000 abstract description 11
- 238000012544 monitoring process Methods 0.000 abstract description 3
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- 238000005065 mining Methods 0.000 description 5
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- 229910000831 Steel Inorganic materials 0.000 description 1
- 230000004075 alteration Effects 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000011065 in-situ storage Methods 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000010248 power generation Methods 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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- 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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- 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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- 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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Abstract
The coal bed gas field cleaning energy-taking system and the method thereof select two coal bed gas wells entering a decline period and one coal bed gas well still in a production stage in the coal bed gas field, wherein the two coal bed gas wells entering the decline period are respectively a first coal bed gas well and a second coal bed gas well, the coal bed gas well still in the production stage is a third coal bed gas well, 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 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 decline period, omits various devices such as furnace building of a gasification furnace, combustion control and monitoring, greatly reduces the underground coal gasification cost, realizes low carbon emission, and obtains a new high value-added product.
Description
Technical Field
The invention belongs to the technical field of comprehensive development and utilization of coal bed gas and underground coal gasification, and particularly relates to a clean energy taking system and method for a coal bed gas field.
Background
Coal is the fossil energy with the largest occurrence amount and the largest mining amount in China, the mining history reaches hundreds of years, particularly, the high-strength mining since the development is improved, the shallow coal seam is basically mined, the mining difficulty of the middle and deep coal seams is high, the cost is high, and the high-efficiency and low-cost development of abundant middle and deep coal resources becomes the research direction. After decades of exploration and practice, underground coal gasification becomes the most main in-situ mining means. Underground coal gasification is carried out through drilling of a vertical well/a horizontal well, construction of an underground gasification furnace and a combustion main channel, air injection of a well A, generation of crude gas through underground controllable combustion, crude gas output of a well B, and ground power generation or purification utilization of the crude gas.
In recent years, environmental protection is required to be improved by green economic development, 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 the efficient development of medium-deep coal resources, the underground coal gasification technology has the major defects of high furnace construction cost, low comprehensive thermal efficiency, insufficient deep processing and utilization of crude gas, high carbon emission and the like of a new drilling and underground gasification furnace. Although documents and patents innovate and propose a hydrogen production process on the basis of an underground coal gasification technology, the underground coal 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 a clean energy taking method for a coalbed methane field, which have the advantages of mature technology, controllable flow, wide application range, high thermal efficiency and abundant products and can be effectively utilized.
In order to solve the technical problems, the invention adopts the following technical scheme: the coal bed gas field cleaning and 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 device, wherein two coal bed gas wells entering a decline period and one coal bed gas well still in a production stage are selected from the coal bed gas field;
the crude oxygen outlet of the first pressure swing adsorption separation device is connected with the well mouth of the first coal bed gas well through a gas injection pipe, a gas injection pump is installed on the gas injection pipe, the well mouth of the second coal bed gas well is connected with the gas inlet of the supercritical water gasification hydrogen production device through a mixed gas exhaust pipe, the well mouth of the third coal bed gas well is connected with the gas inlet of the supercritical water gasification hydrogen production device through a methane gas exhaust pipe, the gas outlet of the supercritical water gasification hydrogen production device is connected with the high-temperature gas inlet of the heat exchange device through a high-temperature mixed gas conveying pipe, the well mouth 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 gas 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 respectively connected with the The gas port is connected, and the combustible gas outlet of the gas separation and purification liquefaction device is connected with the gas inlet of the supercritical water gasification hydrogen production device through a combustible gas pipeline.
The gas separation and purification liquefaction device comprises a second pressure swing adsorption separation device and a cryogenic liquefaction and purification separation device which are connected in series, a carbon dioxide gas outlet of the second pressure swing adsorption separation device is connected with the carbon dioxide liquefaction device, a gas inlet of the second pressure swing adsorption separation device is connected with a gas outlet of the mixed gas pipeline, and combustible gas outlets of the cryogenic liquefaction and purification separation device and the second pressure swing adsorption separation device are connected with the 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 coal bed gas field clean energy-taking system comprises the following steps,
(1) selecting and determining a coal bed gas field in a decline period;
(2) underground coal is gasified by uncontrolled combustion;
(3) hydrogen is produced by the controllable supercritical water gasification on the ground;
(4) the two-stage exchanger takes heat in a cascade way;
(5) two-stage separation and gradient purification and liquefaction.
The step (1) is specifically that the first coal bed gas well and the second coal bed gas well are mined for years, coal bed moisture is drained successively, a coal bed fracturing main channel and fractures are opened, the yield of the gas well is greatly reduced or stopped, a third coal bed gas well with a deeper depth is still in a production stage, coal bed water and CH are produced4Mainly coal bed gas.
Specifically, the step (2) is that air is simply separated and nitrogen is removed through a first pressure swing adsorption separation device with mature technology, low cost and general separation effect to prepare crude oxygen, the crude oxygen and high-temperature steam prepared by a high-temperature heat exchanger are injected into a first coal bed gas well through an air injection pump, uncontrolled combustion gasification is carried out on an underground coal bed between the first coal bed gas well and a second coal bed gas well along a coal bed fracturing main channel and fractures, mixed coal gas is extracted from the second coal bed gas well and is conveyed into a supercritical water gasification hydrogen production device through a mixed coal gas exhaust pipe, and a third coal bed gas well outputs produced gasThe coal bed water and the coal bed gas provide water source and part of methane (CH) for the supercritical water gasification hydrogen production device with underground gasification and ground control4) Raw materials.
The step (3) is specifically that the supercritical water gasification hydrogen production device realizes methane (CH) by adjusting the proportion of mixed coal gas and water vapor raw materials under the control of temperature and pressure of 800 ℃ and over 25MPa4) Water vapor (H)2O), carbon monoxide (CO), carbon dioxide (CO)2) The highest hydrogen (H) with controllable engineering is realized by the chemical reforming reaction of (2)2) Yield.
Specifically, the gas produced by the supercritical water gasification hydrogen production device is high-temperature gas with the temperature of 750-850 ℃, and a large amount of heat contained in the gas can prepare coal bed water produced by a third coal bed gas well into steam; the heat is taken in a two-stage heat exchange cascade mode through a high-temperature heat exchanger and a low-temperature heat exchanger, the high-temperature gas of the high-temperature gas with the temperature of 750-850 ℃ is cooled to be low-temperature gas with the temperature of 30-50 ℃, and the low-temperature gas with the temperature of 30-50 ℃ is introduced into a second pressure swing adsorption separation device; the coal bed water is subjected to two-stage heat exchange and gradient heat increment to prepare high-temperature steam, 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 supply the uncontrolled combustion gasification and supercritical water gasification hydrogen production processes of underground coal, and realize the minimum heat loss of the system; the tar is condensed into liquid to be output along with the high-temperature gas which is subjected to step heat extraction and temperature reduction through the high-temperature heat exchanger and the low-temperature heat exchanger and then enters the gas-solid-liquid separation device, salt in the high-salinity coal bed water is crystallized and separated out, the mixed salt and the dust are safe, solid waste is buried, and the tar can be used as a high-value-added product to be supplied to the steel making industry.
The step (5) is specifically that the two-stage separation and gradient purification and liquefaction take the factors of large gas flow and minimum energy consumption for preparing liquid hydrogen into consideration, and a second pressure swing adsorption separation device with mature technology and low cost is used for separating CO in large-flow low-temperature gas at the temperature of 30-50 DEG C2、CO、CH4Performing primary elimination and separation, and performing secondary purification and liquefaction on the 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 step2) Liquid CO prepared after condensation by a carbon dioxide liquefying device2Or solid CO2Can meet the requirements of low-temperature fresh-keeping in the food industry and the cold chain transportation industry, chemical oil displacement in the oil and gas exploitation industry, carbon dioxide fracturing and carbon sequestration of a carbon index trading platform, and a small amount of separated CO and CH4And the raw material gas is introduced into the supercritical water gasification hydrogen production device again to react again.
By adopting the technical scheme, the invention not only overcomes the five defects of high construction cost, low comprehensive thermal efficiency, single effective product, high carbon emission, large process control difficulty and the like of the existing underground coal gasification technology, but also provides a new way for the environment-friendly treatment of high-salinity water in coal bed gas field development, and realizes the scientific connection between the coal bed gas development and the underground coal gasification.
Compared with the prior underground coal gasification technology, the invention has the following advantages:
(1) the method has the advantages that the coal bed gas field and the coal bed gas well network in the decline period are utilized to develop underground coal gasification, so that the defect that the cost is too high due to the fact that new drilling, construction of an underground gasification furnace, combustion of a main channel and pre-pumping are needed in the existing underground coal gasification is overcome, the middle and shallow coal beds of the coal bed gas field in the decline period are drained of coal bed water, a main fracturing channel and cracks are opened, underground coal bed combustion can be efficiently carried out, and secondary development of the coal bed gas field in the decline period is also achieved;
(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, so that the problem of the environmental protection treatment cost of the high-salinity coal bed water is solved, and scientific matching and connection of coal bed gas development and underground coal gasification are realized;
(3) the current underground coal gasification is reformed into 'underground coal uncontrolled combustion gasification + 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 overcome, 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 preliminary separation-cryogenic liquefaction separation purification two-stage separation and cascade purification and liquefaction can effectively reduce the scale and the investment cost of a cryogenic liquefaction separation device, reduce the energy consumption of refrigeration operation, sequentially separate and scientifically liquefy effective product components and prepare a high-purity liquid hydrogen product;
(6) the carbon source in the coal is converted into liquid or solid C0 through a reasonable process2The low-carbon emission of the clean energy-taking process is realized, and a new product with high added value is obtained;
(7) the underground uncontrolled combustion gasification process effectively implements secondary development and utilization of the coal bed gas field in the decline period, omits various devices such as furnace building, combustion control and monitoring of a gasification furnace and the like, and greatly reduces the underground coal gasification cost.
Drawings
FIG. 1 is a schematic structural diagram of the present invention.
Detailed Description
The technical solutions in the embodiments of the present invention will be clearly and completely described below with reference to the drawings in the embodiments of the present invention, and it is obvious that the described embodiments are only a part of the embodiments of the present invention, and not all of the embodiments. All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the protection scope of the present invention.
As shown in fig. 1, in the clean energy-taking system for the coal bed gas field, two coal bed gas wells entering a decline period and one coal bed gas well still in a production stage are selected from the coal bed gas field, the two coal bed gas wells entering the decline period are respectively a first coal bed gas well 1 and a second coal bed gas well 2, the coal bed gas well still in the production stage is a third coal bed gas well 3, the depths of the first coal bed gas well 1, the second coal bed gas well 2 and the third coal bed gas well 3 are sequentially increased, and the system comprises a first pressure swing adsorption separation device 4, a supercritical water 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 well mouth of the first coal-bed gas well 1 through a gas injection pipe, a gas injection pump 5 is installed on the gas injection pipe 8, the well mouth of the second coal-bed gas well 2 is connected with the gas inlet of the supercritical water gasification hydrogen production device 6 through a mixed gas exhaust pipe 9, the well mouth of the third coal-bed gas well 3 is connected with the gas inlet of the supercritical water gasification hydrogen production device 6 through a methane gas exhaust pipe 10, the gas outlet of the supercritical water gasification hydrogen production device 6 is connected with the high-temperature gas inlet of the heat exchange device through a high-temperature mixed gas conveying pipe 11, the well mouth 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 gas outlet of the heat exchange device is connected with the inlet of the gas-solid-, the gas outlet of the gas-solid-liquid separation device 7 is connected with the gas inlet of the gas separation and purification liquefaction device through a mixed gas pipeline 14, and the combustible gas outlet of the gas separation and purification liquefaction device is connected with the gas inlet of the supercritical water gasification hydrogen production device 6 through a combustible gas pipeline 15.
The gas separation and purification liquefaction device comprises a second pressure swing adsorption separation device 16 and a cryogenic liquefaction and purification separation device 17 which are connected in series, a carbon dioxide gas outlet of the second pressure swing adsorption separation device 16 is connected with a carbon dioxide liquefaction device 18, a gas inlet of the second pressure swing adsorption separation device 16 is connected with a gas outlet of the mixed gas pipeline 14, and combustible gas outlets of the cryogenic liquefaction and purification separation device 17 and the second pressure swing adsorption separation 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 in the invention are all the existing mature technologies and are commercially available in the market, so the specific construction and principle thereof are not described again.
The clean energy-taking method of the coal bed gas field clean energy-taking system comprises the following steps,
(1) selecting and determining a coal bed gas field in a decline period;
(2) underground coal is gasified by uncontrolled combustion;
(3) hydrogen is produced by the controllable supercritical water gasification on the ground;
(4) the two-stage exchanger takes heat in a cascade way;
(5) two-stage separation and gradient purification and liquefaction.
The step (1) is specifically that the first coal bed gas well 1 and the second coal bed gas well 2 have been mined for years, coal bed moisture is drained successively, coal bed fracturing main channels and fractures are opened, the yield of the gas wells is greatly reduced or stopped, and a third coal bed gas well 3 with a deeper depth is still in a production stage, and coal bed water and CH are produced4Mainly coal bed gas.
Specifically, the step (1) is that air is simply separated and nitrogen is removed through a first pressure swing adsorption separation device 4 with mature technology, low cost and general separation effect to prepare crude oxygen, the crude oxygen and high-temperature steam prepared by a high-temperature heat exchanger 20 are injected into a first coal-bed gas well 1 through a gas injection pipe 8 by a gas injection pump 5, underground coal seams between the first coal-bed gas well 1 and a second coal-bed gas well 2 are subjected to uncontrolled combustion gasification along a coal-bed fracturing main channel and cracks, mixed coal gas is extracted from the second coal-bed gas well 2 and is conveyed into a supercritical water gasification hydrogen production device 6 through a mixed coal gas exhaust pipe 9, coal-bed water and coal-bed gas produced by a third coal-bed gas well 3 provide water sources and partial methane (CH) for the underground gasification and ground-controllable supercritical water gasification hydrogen production device 64) Raw materials. The uncontrolled combustion gasification process omits various devices such as furnace building, combustion control and monitoring of the gasification furnace, and greatly reduces the underground gasification cost.
The step (3) is specifically that the supercritical water gasification hydrogen production device 6 adjusts the mixed coal under the control of temperature and pressure of about 800 ℃ and over 25MPaThe mixture ratio of gas and steam raw materials realizes the methane (CH)4) Water vapor (H)2O), carbon monoxide (CO), carbon dioxide (CO)2) The highest hydrogen (H) with controllable engineering is realized by the chemical reforming reaction of (2)2) Yield.
Specifically, the gas produced by the supercritical water gasification hydrogen production device 6 is high-temperature gas at 750-850 ℃, and a large amount of heat contained in the gas can prepare coal bed water produced by the third coal bed gas well 3 into steam; the heat is taken in a two-stage heat exchange cascade mode through the high-temperature heat exchanger 20 and the low-temperature heat exchanger 19, the high-temperature gas of the high-temperature gas with the temperature of 750-850 ℃ is cooled to be low-temperature gas with the temperature of 30-50 ℃, 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 subjected to two-stage heat exchange and gradient heat increment to prepare high-temperature steam, and the high-temperature steam is introduced into the first coal bed gas well 1 and the supercritical water gasification hydrogen production device 6 so as to supply the uncontrolled combustion gasification and supercritical water gasification hydrogen production processes of underground coal, and realize the minimum heat loss of the system; after high-temperature gas is subjected to step heat extraction and temperature reduction through the high-temperature heat exchanger 20 and the low-temperature heat exchanger 19 and enters the gas-solid-liquid separation device 7, tar is condensed into liquid to be output, salt in high-salinity coal bed water is crystallized and separated out, mixed salt and dust are safely buried in solid waste, and the tar serving as a high-value-added product can be supplied to the steel industry and the like.
The step (5) is specifically that the two-stage separation and gradient purification and liquefaction take the factors of large gas flow and minimum energy consumption into consideration to prepare liquid hydrogen, and a second pressure swing adsorption separation device 16 with mature technology and low cost is used for treating CO in large-flow 30-50 ℃ low-temperature gas2、CO、CH4Performing primary elimination and separation, and performing secondary purification and liquefaction of the low-flow crude hydrogen by using the cryogenic liquefaction purification separation device 17 again to prepare a high-purity liquid hydrogen product;
carbon dioxide (CO) separated in this step2) Liquid CO produced after condensation by the carbon dioxide liquefaction device 182Or solid CO2Can be used for low-temperature fresh-keeping of food industry and cold-chain transportation industry, chemical oil displacement of oil and gas exploitation industry, carbon dioxide fracturing and carbon sequestration of carbon index transaction platformObtaining small amount of separated CO and CH4The raw material gas is introduced into the supercritical water gasification hydrogen production device 6 again for secondary reaction.
Although embodiments of the present invention have been shown and described, it will be appreciated by those skilled in the art that changes, modifications, substitutions and alterations can be made in these embodiments without departing from the principles and spirit of the invention, the scope of which is defined in the appended claims and their equivalents.
Claims (9)
1. The clean energy taking system for the coal bed gas field is characterized in that two coal bed gas wells entering a decline period and one coal bed gas well still in a production stage are selected from the coal bed gas field, the two coal bed gas wells entering the decline period are respectively a first coal bed gas well and a second coal bed gas well, the coal bed gas well still in the production stage 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: 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 well mouth of a first coal-bed gas well through a gas injection pipe, a gas injection pump is arranged on the gas injection pipe, the well mouth of a second coal-bed gas well is connected with the gas inlet of a supercritical water gasification hydrogen production device through a mixed gas exhaust pipe, the well mouth of a third coal-bed gas well is connected with the gas inlet of the supercritical water gasification hydrogen production device through a methane gas exhaust pipe, the gas outlet of the supercritical water gasification hydrogen production device is connected with the high-temperature gas inlet of a heat exchange device through a high-temperature mixed gas conveying pipe, the well mouth of a 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 gas outlet of the heat exchange device is connected with the inlet of the gas-, the gas outlet of the gas-solid-liquid separation device is connected with the gas 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 gas inlet of the supercritical water gasification hydrogen production device through a combustible gas pipeline.
2. The coalbed methane field cleaning and energy-taking system of claim 1, wherein: the gas separation and purification liquefaction device comprises a second pressure swing adsorption separation device and a cryogenic liquefaction and purification separation device which are connected in series, a carbon dioxide gas outlet of the second pressure swing adsorption separation device is connected with the carbon dioxide liquefaction device, a gas inlet of the second pressure swing adsorption separation device is connected with a gas outlet of the mixed gas pipeline, and combustible gas outlets of the cryogenic liquefaction and purification separation device and the second pressure swing adsorption separation device are connected with the combustible gas pipeline.
3. The coalbed methane field cleaning and energy-taking system of claim 2, wherein: 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.
4. A method of clean energy extraction using the coal bed methane field clean energy extraction system of claim 3, wherein: comprises the following steps of (a) carrying out,
(1) selecting and determining a coal bed gas field in a decline period;
(2) underground coal is gasified by uncontrolled combustion;
(3) hydrogen is produced by the controllable supercritical water gasification on the ground;
(4) the two-stage exchanger takes heat in a cascade way;
(5) two-stage separation and gradient purification and liquefaction.
5. The coalbed methane field cleaning and energy-taking system of claim 4, wherein: the step (1) is specifically that the first coal bed gas well and the second coal bed gas well are mined for years, coal bed moisture is drained successively, a coal bed fracturing main channel and fractures are opened, the yield of the gas wells is greatly reduced or stopped, and the depth is deepThe third more deep coal bed gas well is still in the production stage, and produces coal bed water and CH4Mainly coal bed gas.
6. The method of claim 5, wherein: specifically, the step (2) is that air is simply separated and nitrogen is removed through a first pressure swing adsorption separation device with mature technology, low cost and general separation effect to prepare crude oxygen, the crude oxygen and high-temperature steam prepared by a high-temperature heat exchanger are injected into a first coal-bed gas well through an air injection pump, uncontrolled combustion gasification is carried out on an underground coal bed between the first coal-bed gas well and a second coal-bed gas well along a coal-bed fracturing main channel and fractures, mixed coal gas is extracted from the second coal bed and is conveyed into a supercritical water gasification hydrogen production device through a mixed coal gas exhaust pipe, 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 control4) Raw materials.
7. The coalbed methane field cleaning and energy-taking method according to claim 6, characterized in that: the step (3) is specifically that the supercritical water gasification hydrogen production device realizes methane (CH) by adjusting the proportion of mixed coal gas and water vapor raw materials under the control of temperature and pressure of 800 ℃ and over 25MPa4) Water vapor (H)2O), carbon monoxide (CO), carbon dioxide (CO)2) The highest hydrogen (H) with controllable engineering is realized by the chemical reforming reaction of (2)2) Yield.
8. The clean energy harvesting method of claim 7, wherein: specifically, the gas produced by the supercritical water gasification hydrogen production device is high-temperature gas with the temperature of 750-850 ℃, and a large amount of heat contained in the gas can prepare coal bed water produced by a third coal bed gas well into steam; the heat is taken in a two-stage heat exchange cascade mode through a high-temperature heat exchanger and a low-temperature heat exchanger, the high-temperature gas of the high-temperature gas with the temperature of 750-850 ℃ is cooled to be low-temperature gas with the temperature of 30-50 ℃, and the low-temperature gas with the temperature of 30-50 ℃ is introduced into a second pressure swing adsorption separation device; the coal bed water is subjected to two-stage heat exchange and gradient heat increment to prepare high-temperature steam, 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 supply the uncontrolled combustion gasification and supercritical water gasification hydrogen production processes of underground coal, and realize the minimum heat loss of the system; the tar is condensed into liquid to be output along with the high-temperature gas which is subjected to step heat extraction and temperature reduction through the high-temperature heat exchanger and the low-temperature heat exchanger and then enters the gas-solid-liquid separation device, salt in the high-salinity coal bed water is crystallized and separated out, the mixed salt and the dust are safe, solid waste is buried, and the tar can be used as a high-value-added product to be supplied to the steel making industry.
9. The clean energy harvesting method of claim 8, wherein: the step (5) is specifically that the two-stage separation and gradient purification and liquefaction take the factors of large gas flow and minimum energy consumption for preparing liquid hydrogen into consideration, and a second pressure swing adsorption separation device with mature technology and low cost is used for separating CO in large-flow low-temperature gas at the temperature of 30-50 DEG C2、CO、CH4Performing primary elimination and separation, and performing secondary purification and liquefaction on the 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 step2) Liquid CO prepared after condensation by a carbon dioxide liquefying device2Or solid CO2Can meet the requirements of low-temperature fresh-keeping in the food industry and the cold chain transportation industry, chemical oil displacement in the oil and gas exploitation industry, carbon dioxide fracturing and carbon sequestration of a carbon index trading platform, and a small amount of separated CO and CH4And the raw material gas is introduced into the supercritical water gasification hydrogen production device again to react again.
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