CN203764088U - System for enriching coal bed gas - Google Patents
System for enriching coal bed gas Download PDFInfo
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- CN203764088U CN203764088U CN201420067986.XU CN201420067986U CN203764088U CN 203764088 U CN203764088 U CN 203764088U CN 201420067986 U CN201420067986 U CN 201420067986U CN 203764088 U CN203764088 U CN 203764088U
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- coal bed
- methane
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- gas
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Abstract
The utility model discloses a system for enriching a coal bed gas. The system comprises an absorption tower, a flashing tower and a low-temperature separation tank which are sequentially connected, wherein the absorption tower is used for an ether solvent to adsorb methane in the coal bed gas; the flashing tower is used for desorbing a solvent-enriching solution adsorbed with the methane so as to separate out the methane; the low-temperature separation tank is used for removing diethyl ether from the methane-enriching gas obtained in a desorption separation mode in the flashing tower; the absorption tower is respectively connected with a first pressurization assembly and a first cooling assembly which are used for pressurizing and cooling the ether solvent and the coal bed gas; and a second pressurization assembly and a second cooling assembly which are used for pressurizing and cooling the methane-enriching gas are arranged between the low-temperature separation tank and the flashing tower. The system is convenient to operate and less in equipment; and the majority of cooling quantity can be recycled by fully utilizing the self heat of the system after the heat is integrated, so that the public engineering loss is less.
Description
Technical field
The utility model relates to Coal Mines layer gas disposal field, a kind of system of coal bed gas being carried out to enrichment of specific design.
Background technology
Coal bed gas, is commonly called as gas, is that a kind of tax is stored in the hydrocarbon gas in coal seam, and main component is CH
4.Coal bed gas comprehensive utilization value is very high, except civilian, also can be used for gas turbine power generation, heat supply, the fuel that is used as power after compressing and liquefying, and also can do the chemical products such as methyl alcohol, synthetic ammonia, is also the basic material of the Organic chemical products such as agricultural chemicals, medicine, dyestuff.Table 1 is 2007～2011 years China's coal bed gas extraction amounts, utilization, emission behaviour table.
Table 1 China's coal bed gas extraction in 2007～2011 years, utilization, discharge capacity information slip
The main cause of a large amount of emptying of current domestic coal bed gas is that methane concentration is low, and it is desirable not enough that coal bed gas is concentrated in security, technology, economic dispatch aspect, hindered the extensive utilization of coal bed gas, causes the gas utilization rate of coal field extraction very low.Therefore, present stage coal bed gas comprehensive utilization on, its key point is how weary low concentration gas enrichment is become to high concentration mineral resources.Its concentration technique mainly contains five kinds of gas separations such as pressure-variable adsorption (PSA) technique, cryogenic separation technology, Mehra technique, Metal Substrate liquid absorption method and membrane separation process.
Pressure-variable adsorption (PSA) technique is the study hotspot of coal bed gas concentration process in recent years, in this technical process, researcher is by the improvement to traditional handicraft, as increase vacuumizing, increase and all press replacement operator, increase adsorption tower number or multiple-hearth absorption etc., all can promote methane adsorption effect, but the main cause of restriction PSA technique large-scale industry is there is no suitable adsorbent, adsorbent determines to the adsorptive selectivity of component complexity and the economic benefit that pressure-variable adsorption separates.
The application of cryogenic separation technology early, is also current CH
4/ N
2separate ripe and the most the most frequently used technology, its general principle is to utilize CH
4with N
2boiling-point difference realize the two separation, utilize cryogenic technique low-concentration methane can be concentrated into more than 90%, but device is complicated, equipment investment is large, and CO
2, the impurity such as water is easy to blocking pipe in the time of low temperature, also only large coal mine had to economic worth.
Mehra technique is to utilize hydrocarbon solvent Physical Absorption CH
4, realize N
2and CH
4the separation of mixture, solvent composition is the mixture of the materials such as alkyl ether, ethylene glycol, 1-METHYLPYRROLIDONE, dimethyl formamide, propylene carbonate fat, sulfolane, although this technique has certain economic value, CH at the nitrogenous natural gas of purifying
4in hydrocarbon solvent, solubility is low, absorbent consumption is large.
The Metal Substrate liquid absorption method general principle of Bend research institution exploitation is to select to absorb N
2, absorption process is chemical absorbing, 1mol Metal Substrate liquid is to N in theory
2/ CH
4absorption selectivity can reach 5.75, but absorption and regeneration speed is slow, efficiency is low, is only applicable to N in a small amount
2absorption.
Membrane separation technique is a kind of new separation technology, and film was separated in separation of C H in recent years
4/ N
2basic research many, but still larger from industrialized gap, be mainly that the permselective property of film is lower, and the preparation of film is also subject to the restriction of factors.
Above-mentioned five kinds of techniques, some infrastructure device investment is large, and operating cost is higher, and some technology is also immature, complex process, energy consumption is high.Therefore be necessary to provide a kind of technique circuit comparatively simple, easy to operate, the Enriching Coalbed Methane technique that equipment investment is few.
Utility model content
It is a kind of easy to operate that the purpose of this utility model is to provide, the system that coal bed gas is carried out to enrichment that equipment investment is few.
For achieving the above object, the utility model adopts following technical scheme:
A kind of system of coal bed gas being carried out to enrichment, it is characterized in that: this system comprises the absorption tower of the methane of coal bed gas being adsorbed for ether solvent, for being carried out to Desorption separation, the solvent rich solution after adsorbed methane goes out the flash column of methane, and remove the cryogenic separation tank of ether in the methane-rich gas that Desorption separation obtains in flash column, absorption tower, flash column, cryogenic separation tank is sequentially connected, absorption tower respectively with to ether solvent, coal bed gas is pressurizeed, the first cooling pressure-applying unit is connected with the first cooling package, between cryogenic separation tank and flash column, arrange methane-rich gas is pressurizeed, the second cooling pressure-applying unit and the second cooling package.
Concrete scheme is: the bottom on absorption tower arranges respectively coal bed gas entrance and absorbs the solvent-rich outlet after methane, the top on absorption tower arranges respectively coal bed gas outlet and ether solvent entrance, the first described pressure-applying unit comprise to ether solvent carry out the first High pressure feeding pump of forced feed and to coal bed gas pressurize compression compressor bank, the first cooling package comprises to ether solvent is carried out the first cooling cooler and coal bed gas is carried out to cooling cooler unit, the first High pressure feeding pump, the first cooler, between the ether solvent entrance of absorption tower, be communicated with successively connection by pipeline, compressor bank, cooler unit, between the coal bed gas entrance of absorption tower, be communicated with successively connection by pipeline.Bottom, absorption tower methane rich solvent is delivered to flash column through still liquid delivery pump, flash column tower top arranges the discharge mouth of pipe that removes the ether solvent after methane at the bottom of methane-rich gas outlet, tower are set, the second described pressure-applying unit comprises the 4th compressor, the second cooling package comprises the 5th cooler, cryogenic separation tank is provided with methane-rich gas entrance, remove the outlet of methane gas after ether, the ether outlet removing, and flash column methane-rich gas outlet and cryogenic separation tank are provided with and between methane-rich gas entrance, set gradually the 4th compressor and the 5th cooler.
Further scheme is: between the 4th compressor and the 5th cooler, be provided with the second heat exchanger, the low-temperature receiver entrance of the second heat exchanger and the top on absorption tower arrange respectively coal bed gas outlet and are connected and are connected, and the thermal source entrance of the second heat exchanger is connected and is connected with the 4th compressor.Between the 4th compressor and the 5th cooler, be also provided with the 3rd heat exchanger, the low-temperature receiver entrance of the 3rd heat exchanger is connected and is connected with the outlet of methane gas on cryogenic separation tank, and the thermal source entrance of the 3rd heat exchanger is connected and is connected with the 4th compressor.
The first High pressure feeding pump and the first cooler are provided with First Heat Exchanger, and the low-temperature receiver entrance of First Heat Exchanger is connected and is connected with the outlet of flash column ether solvent, and the thermal source entrance of First Heat Exchanger is connected and is connected with the first High pressure feeding pump.The discharge mouth of pipe place of flash column ether solvent is provided with third high and presses feed pump, third high presses the discharging opening place of feed pump to be provided with a three-way change-over valve, one discharging opening of three-way change-over valve is for being connected and being connected with First Heat Exchanger, and another discharging opening of three-way change-over valve is for being connected and being connected with the ether solvent entrance on absorption tower.
Compressor bank is three-stage blower group, comprises successively first, second and third compressor that serial connection connects, first, second and third compressor outlet arrange respectively second and third, four coolers, second and third, four coolers form cooler units.In absorption tower, be provided with 12 theoretical plates, operating pressure is 1.3MPa.The first, five, six coolers are ammonia cooler, second and third, four coolers are water cooler.
For above-mentioned process system, following control system is set:
The control of High pressure feeding pump adopts the FEEDBACK CONTROL of rate of discharge, controls ether charging conveying capacity, and at pump discharge, pressure-indication means is set, and is used to indicate outlet logistics pressure; The control system that compressor adopts compressor producer to provide, therefore not to repeat here; Heat exchanger is the heat transfer process between process-stream, therefore detects at heat exchanger turnover logistics set temperature; Ammonia cooler and water cooler are the heat transfer process between process-stream and cold public work, and the temperature feedback control of adopting process logistics outlet, regulates the consumption of cold public work to make process-stream outlet temperature reach target setting; Absorption tower arranges pressure difference indicator and temperature indicator, the instruction of tower top setting pressure, and the flow of still liquid delivery pump adopts the control of tower reactor liquid level.
Above-mentioned provide for coal bed gas being carried out to the system of enrichment, easy to operate, equipment is less, heat, after integrated, can make full use of system self heat, reclaims most of cold, public work loss is less; Simultaneously said system process coal bed gas can relatively low at operating pressure (1.3MPa), under the condition of temperature relatively high (30～66 DEG C), implement, methane in coal bed gas can be enriched to 69.9% (mol) by concentration 30%, the rate of recovery is 85.38%.
Brief description of the drawings
Fig. 1 is structural representation of the present utility model.
Wherein: C101/C102/C103-unstripped gas three-stage blower group;
E101/E102/E103-heat exchanger;
L101/L106/L105-ammonia cooler; L102/L103/L104-water cooler;
J101T101 High pressure feeding pump; J102-T101 still liquid delivery pump; J103-T101 cycle of higher pressure feed pump;
V101-triple valve; C104-flash vessel compressor;
T101-absorption tower; T102-adiabatic flash tower; T103-cryogenic separation tank;
PG-pressure visor; TG-temperature visor; LG-liquid level visor; The instruction of PI-pressure; The instruction of PDI-pressure reduction; TT-temperature transmitter; FT-flow transmitter; LT-fluid level transmitter.
Detailed description of the invention
In order to make the purpose of this utility model and advantage clearer, below in conjunction with embodiment, the utility model is further elaborated.Should be appreciated that specific embodiment described herein is only in order to explain the utility model, and be not used in restriction the utility model.
The thought of the whole system that the utility model provides is exactly: utilize ether solvent to adsorb the methane in coal bed gas, then the solvent rich solution after adsorbed methane is carried out to Desorption separation and go out methane, collection obtains methane-rich gas, and methane-rich gas is taken off to ether processing, make methane product.
Specifically as shown in Fig. 1 institute, that is:
A kind of system of coal bed gas being carried out to enrichment, this system comprises the absorption tower T101 methane of coal bed gas being adsorbed for ether solvent, for being carried out to Desorption separation, the solvent rich solution after adsorbed methane goes out the flash column T102 of methane, and remove the cryogenic separation tank T103 of ether in the methane-rich gas that Desorption separation obtains in flash column T102, absorption tower T101, flash column T102, cryogenic separation tank T103 is sequentially connected, absorption tower T101 respectively with to ether solvent, coal bed gas is pressurizeed, the first cooling pressure-applying unit is connected with the first cooling package, between cryogenic separation tank T103 and flash column T102, arrange methane-rich gas is pressurizeed, the second cooling pressure-applying unit and the second cooling package.
Concrete scheme is: the bottom of absorption tower T101 arranges respectively coal bed gas entrance and absorbs the solvent-rich outlet after methane, the top of absorption tower T101 arranges respectively coal bed gas outlet and ether solvent entrance, the first described pressure-applying unit comprise to ether solvent carry out the first High pressure feeding pump J101 of forced feed and to coal bed gas pressurize compression compressor bank, the first cooling package comprises to ether solvent is carried out the first cooling cooler L101 and coal bed gas is carried out to cooling cooler unit, the first High pressure feeding pump J101, the first cooler L101, between the T101 ether solvent entrance of absorption tower, be communicated with successively connection by pipeline, compressor bank, cooler unit, between the T101 coal bed gas entrance of absorption tower, be communicated with successively connection by pipeline.Flash column T102 tower top arranges the discharge mouth of pipe that removes the ether solvent after methane at the bottom of methane-rich gas outlet, tower are set, the second described pressure-applying unit comprises the 4th compressor C104, the second cooling package comprises the 5th cooler L105, cryogenic separation tank T103 is provided with methane-rich gas entrance, remove the outlet of methane gas after ether, the ether outlet removing, and flash column T102 methane-rich gas outlet and cryogenic separation tank T103 are provided with and between methane-rich gas entrance, set gradually the 4th compressor C104 and the 5th cooler L105.
More preferred scheme is: compressor bank is three-stage blower group, comprise serial connection connects successively first, second and third compressor C101, C102, C103, first, second and third compressor C101, C102, the C103 port of export arrange respectively second and third, four cooler L102, L103, L104, second and third, four cooler L102, L103, L104 form cooler unit.Between the 4th compressor C104 and the 5th cooler L105, be provided with the second heat exchanger E102, the low-temperature receiver entrance of the second heat exchanger E102 and the top of absorption tower T101 arrange respectively coal bed gas outlet and are connected and are connected, and the thermal source entrance of the second heat exchanger E102 is connected and is connected with the 4th compressor C104.Between the 4th compressor C104 and the 5th cooler L105, be also provided with the 3rd heat exchanger E103, the low-temperature receiver entrance of the 3rd heat exchanger E103 is connected and is connected with the outlet of the upper methane gas of cryogenic separation tank T103, and the thermal source entrance of the 3rd heat exchanger E103 is connected and is connected with the 4th compressor C104.The first High pressure feeding pump J101 and the first cooler L101 are provided with First Heat Exchanger E101, the low-temperature receiver entrance of First Heat Exchanger E101 is connected and is connected with the outlet of flash column T102 ether solvent, and the thermal source entrance of First Heat Exchanger E101 is connected and is connected with the first High pressure feeding pump J101.The second High pressure feeding pump J102 is set between absorption tower T101 and flash column T102, the discharge mouth of pipe place of flash column T102 ether solvent is provided with third high and presses feed pump J103, third high presses the discharging opening place of feed pump J103 to be provided with a three-way change-over valve V101, a discharging opening of three-way change-over valve V101 is for being connected and being connected with First Heat Exchanger E101, another discharging opening of three-way change-over valve V101 after the 6th cooler L106 lowers the temperature for being connected and being connected with the ether solvent entrance of absorption tower T101.In the T101 of absorption tower, be provided with 12 theoretical plates, tower top operating pressure is 1.3MPa.The first, five, six coolers are ammonia cooler, second and third, four coolers are water cooler.
Below in conjunction with said system, this utility model is illustrated:
This technique is the object that ether absorption methane reaches enrichment coal bed gas, ether from storage tank through the first High pressure feeding pump J101 by boost in pressure to 1.3MPa, and through getting rid of ether solvent in First Heat Exchanger E101 and flash column T102, to carry out heat exchange cooling and then after the first cooler L101 is cooling, and temperature is down to-25 DEG C of tops that enter absorption tower T101, coal bed gas is mainly made up of methane and nitrogen, molar ratio is 3: 7, after three-stage blower group compression, coal bed gas boost in pressure is entered to absorption tower T101 bottom to 1.3MPa, and in compressor bank, arrange second and third, four cooler L102, L103, L104, prevent from breaking down because excess Temperature causes compressor in compression process, ether solvent and coal bed gas be counter current contacting in the T101 of absorption tower, absorption tower T101 has 12 theoretical plates, operating pressure is 1.3MPa, tower top is low-concentration methane gas 6.4%, and the coal bed gas of the low concentration that absorption tower T101 tower top is got rid of carries out after cold is reclaimed in heat exchange being disposed to torch burning through the second heat exchanger E102 with the methane-rich gas that enters cryogenic separation tank T103, absorption tower T101 tower base solvent rich solution is decompressed to 1atm through adiabatic flash tower T102 and treads a large amount of methane-rich gas, the ether solvent that adiabatic flash bottom column removes after methane presses feed pump J103 pump to promote feed pressure to 1.3MPa through third high, wherein after 95% rich solution and the 6th cooler L106 cooling, circulating, it is interior for absorbing the methane of coal bed gas to be recycled to absorption tower T101, and other 5% ether solvent and fresh ether solvent are transported to after heat exchange in ether retracting device in First Heat Exchanger E101, adiabatic flash tower T102 top methane-rich gas is promoted to 0.3MPa through the 4th compressor C104 by normal pressure, then with the low-concentration methane gas at T101 top, absorption tower in the second heat exchanger E102 after heat exchange, in the 3rd heat exchanger E103, carry out heat exchange with the methane gas of cryogenic separation tank T103 top discharge again, be down to operating temperature-30 DEG C through the 5th cooler L105 (ammonia cooler), enter cryogenic separation tank T103, at 0.3MPa, under adiabatic condition, remove ether a large amount of in methane-rich gas, the ether of cryogenic separation tank T103 bottom removes ether retracting device, methane gas after removing removes methane product storage tank after cold is reclaimed in heat exchange.Said method enrichment to methane product concentration can reach 69.9% (mol), the rate of recovery is 85.38%.
The above is only preferred embodiment of the present utility model; it should be pointed out that for those skilled in the art, do not departing under the prerequisite of the utility model principle; can also make some improvements and modifications, these improvements and modifications also should be considered as protection domain of the present utility model.
Claims (10)
1. one kind is carried out the system of enrichment to coal bed gas, it is characterized in that: this system comprises the absorption tower of the methane of coal bed gas being adsorbed for ether solvent, for being carried out to Desorption separation, the solvent rich solution after adsorbed methane goes out the flash column of methane, and remove the cryogenic separation tank of ether in the methane-rich gas that Desorption separation obtains in flash column, absorption tower, flash column, cryogenic separation tank is sequentially connected, absorption tower respectively with to ether solvent, coal bed gas is pressurizeed, the first cooling pressure-applying unit is connected with the first cooling package, between cryogenic separation tank and flash column, arrange methane-rich gas is pressurizeed, the second cooling pressure-applying unit and the second cooling package.
2. system of coal bed gas being carried out to enrichment as claimed in claim 1, it is characterized in that: the bottom on absorption tower arranges respectively coal bed gas entrance and absorbs the solvent-rich outlet after methane, the top on absorption tower arranges respectively coal bed gas outlet and ether solvent entrance, the first described pressure-applying unit comprise to ether solvent carry out the first High pressure feeding pump of forced feed and to coal bed gas pressurize compression compressor bank, the first cooling package comprises to ether solvent is carried out the first cooling cooler and coal bed gas is carried out to cooling cooler unit, the first High pressure feeding pump, the first cooler, between the ether solvent entrance of absorption tower, be communicated with successively connection by pipeline, compressor bank, cooler unit, between the coal bed gas entrance of absorption tower, be communicated with successively connection by pipeline.
3. system of coal bed gas being carried out to enrichment as claimed in claim 2, it is characterized in that: compressor bank is three-stage blower group, comprise first, second and third compressor that serial connection connects successively, first, second and third compressor outlet arrange respectively second and third, four coolers, second and third, four coolers form cooler units.
4. system of coal bed gas being carried out to enrichment as claimed in claim 2, it is characterized in that: flash column tower top arranges methane-rich gas outlet, the discharge mouth of pipe that removes the ether solvent after methane is set at the bottom of tower, the second described pressure-applying unit comprises the 4th compressor, the second cooling package comprises the 5th cooler, cryogenic separation tank is provided with methane-rich gas entrance, remove the outlet of methane gas after ether, the ether outlet removing, flash column methane-rich gas outlet and cryogenic separation tank are provided with and between methane-rich gas entrance, set gradually the 4th compressor and the 5th cooler.
5. system of coal bed gas being carried out to enrichment as claimed in claim 4, it is characterized in that: between the 4th compressor and the 5th cooler, be provided with the second heat exchanger, the low-temperature receiver entrance of the second heat exchanger and the top on absorption tower arrange respectively coal bed gas outlet and are connected and are connected, and the thermal source entrance of the second heat exchanger is connected and is connected with the 4th compressor.
6. the system that coal bed gas is carried out to enrichment as described in claim 4 or 5, it is characterized in that: between the 4th compressor and the 5th cooler, be also provided with the 3rd heat exchanger, the low-temperature receiver entrance of the 3rd heat exchanger is connected and is connected with the outlet of methane gas on cryogenic separation tank, and the thermal source entrance of the 3rd heat exchanger is connected and is connected with the 4th compressor.
7. system of coal bed gas being carried out to enrichment as claimed in claim 4, it is characterized in that: the first High pressure feeding pump and the first cooler are provided with First Heat Exchanger, the low-temperature receiver entrance of First Heat Exchanger is connected and is connected with the outlet of flash column ether solvent, and the thermal source entrance of First Heat Exchanger is connected and is connected with the first High pressure feeding pump.
8. system of coal bed gas being carried out to enrichment as claimed in claim 7, it is characterized in that: the discharge mouth of pipe place of flash column ether solvent is provided with third high and presses feed pump, third high presses the discharging opening place of feed pump to be provided with a three-way change-over valve, one discharging opening of three-way change-over valve is for being connected and being connected with First Heat Exchanger, and another discharging opening of three-way change-over valve is for being connected and being connected with the ether solvent entrance on absorption tower.
9. system of coal bed gas being carried out to enrichment as claimed in claim 7, is characterized in that: in absorption tower, be provided with 12 theoretical plates, operating pressure is 1.3MPa.
10. the system that coal bed gas is carried out to enrichment as described in claim 3 or 5, is characterized in that: the first, five, six coolers are ammonia cooler, second and third, four coolers are water cooler.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201420067986.XU CN203764088U (en) | 2014-02-14 | 2014-02-14 | System for enriching coal bed gas |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201420067986.XU CN203764088U (en) | 2014-02-14 | 2014-02-14 | System for enriching coal bed gas |
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| Publication Number | Publication Date |
|---|---|
| CN203764088U true CN203764088U (en) | 2014-08-13 |
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ID=51281336
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201420067986.XU Expired - Fee Related CN203764088U (en) | 2014-02-14 | 2014-02-14 | System for enriching coal bed gas |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105771560A (en) * | 2016-04-27 | 2016-07-20 | 西安科技大学 | Refined filtration system for low-concentration coal-bed methane |
| CN111747816A (en) * | 2019-03-29 | 2020-10-09 | 中国石油大学(北京) | System and process for recovering ethane from mixed gas |
-
2014
- 2014-02-14 CN CN201420067986.XU patent/CN203764088U/en not_active Expired - Fee Related
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105771560A (en) * | 2016-04-27 | 2016-07-20 | 西安科技大学 | Refined filtration system for low-concentration coal-bed methane |
| CN111747816A (en) * | 2019-03-29 | 2020-10-09 | 中国石油大学(北京) | System and process for recovering ethane from mixed gas |
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| C14 | Grant of patent or utility model | ||
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| CF01 | Termination of patent right due to non-payment of annual fee |
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