CN203323490U - Burning and explosion-suppressing low-concentration coal-bed methane cryogenic liquefying device - Google Patents
Burning and explosion-suppressing low-concentration coal-bed methane cryogenic liquefying device Download PDFInfo
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- CN203323490U CN203323490U CN2013203309431U CN201320330943U CN203323490U CN 203323490 U CN203323490 U CN 203323490U CN 2013203309431 U CN2013203309431 U CN 2013203309431U CN 201320330943 U CN201320330943 U CN 201320330943U CN 203323490 U CN203323490 U CN 203323490U
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- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 title claims abstract description 185
- 239000007789 gas Substances 0.000 claims abstract description 149
- 239000003245 coal Substances 0.000 claims abstract description 94
- 238000004880 explosion Methods 0.000 claims abstract description 56
- 238000003860 storage Methods 0.000 claims abstract description 30
- 239000000945 filler Substances 0.000 claims abstract description 14
- 239000000463 material Substances 0.000 claims abstract description 14
- 239000003063 flame retardant Substances 0.000 claims abstract description 10
- 238000005057 refrigeration Methods 0.000 claims abstract description 4
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 69
- 229910052757 nitrogen Inorganic materials 0.000 claims description 36
- 230000001629 suppression Effects 0.000 claims description 29
- DOTMOQHOJINYBL-UHFFFAOYSA-N molecular nitrogen;molecular oxygen Chemical compound N#N.O=O DOTMOQHOJINYBL-UHFFFAOYSA-N 0.000 claims description 25
- 238000002485 combustion reaction Methods 0.000 claims description 20
- 239000003034 coal gas Substances 0.000 claims description 18
- 238000002309 gasification Methods 0.000 claims description 17
- 239000012071 phase Substances 0.000 claims description 17
- 238000004140 cleaning Methods 0.000 claims description 11
- 239000004215 Carbon black (E152) Substances 0.000 claims description 10
- 229930195733 hydrocarbon Natural products 0.000 claims description 10
- 150000002430 hydrocarbons Chemical class 0.000 claims description 10
- 238000001816 cooling Methods 0.000 claims description 7
- 239000000843 powder Substances 0.000 claims description 7
- 238000010992 reflux Methods 0.000 claims description 7
- 238000007789 sealing Methods 0.000 claims description 7
- 238000005507 spraying Methods 0.000 claims description 7
- 238000013022 venting Methods 0.000 claims description 7
- 239000002826 coolant Substances 0.000 claims description 6
- 238000004172 nitrogen cycle Methods 0.000 claims description 6
- 238000005194 fractionation Methods 0.000 claims description 4
- 239000007791 liquid phase Substances 0.000 claims description 4
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 abstract description 16
- 239000001301 oxygen Substances 0.000 abstract description 16
- 229910052760 oxygen Inorganic materials 0.000 abstract description 16
- 238000007906 compression Methods 0.000 abstract description 12
- 238000000926 separation method Methods 0.000 abstract description 11
- 230000006835 compression Effects 0.000 abstract description 10
- 238000000605 extraction Methods 0.000 abstract description 10
- 239000003949 liquefied natural gas Substances 0.000 abstract description 8
- 238000000746 purification Methods 0.000 abstract description 3
- RNFJDJUURJAICM-UHFFFAOYSA-N 2,2,4,4,6,6-hexaphenoxy-1,3,5-triaza-2$l^{5},4$l^{5},6$l^{5}-triphosphacyclohexa-1,3,5-triene Chemical compound N=1P(OC=2C=CC=CC=2)(OC=2C=CC=CC=2)=NP(OC=2C=CC=CC=2)(OC=2C=CC=CC=2)=NP=1(OC=1C=CC=CC=1)OC1=CC=CC=C1 RNFJDJUURJAICM-UHFFFAOYSA-N 0.000 abstract 2
- 238000000034 method Methods 0.000 description 14
- 238000011084 recovery Methods 0.000 description 8
- 230000000694 effects Effects 0.000 description 5
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 4
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 description 4
- 238000010521 absorption reaction Methods 0.000 description 4
- 229910052799 carbon Inorganic materials 0.000 description 4
- QWTDNUCVQCZILF-UHFFFAOYSA-N isopentane Chemical compound CCC(C)C QWTDNUCVQCZILF-UHFFFAOYSA-N 0.000 description 4
- 239000007788 liquid Substances 0.000 description 4
- 230000009102 absorption Effects 0.000 description 3
- 239000000047 product Substances 0.000 description 3
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 2
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 description 2
- 230000009286 beneficial effect Effects 0.000 description 2
- 229910002092 carbon dioxide Inorganic materials 0.000 description 2
- 239000001569 carbon dioxide Substances 0.000 description 2
- 238000006243 chemical reaction Methods 0.000 description 2
- AFABGHUZZDYHJO-UHFFFAOYSA-N dimethyl butane Natural products CCCC(C)C AFABGHUZZDYHJO-UHFFFAOYSA-N 0.000 description 2
- 239000002360 explosive Substances 0.000 description 2
- HDDSHPAODJUKPD-UHFFFAOYSA-N fenbendazole Chemical compound C1=C2NC(NC(=O)OC)=NC2=CC=C1SC1=CC=CC=C1 HDDSHPAODJUKPD-UHFFFAOYSA-N 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- 230000000644 propagated effect Effects 0.000 description 2
- 239000001294 propane Substances 0.000 description 2
- 239000002994 raw material Substances 0.000 description 2
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 description 1
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical group [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 1
- 239000012190 activator Substances 0.000 description 1
- 239000003963 antioxidant agent Substances 0.000 description 1
- 230000003078 antioxidant effect Effects 0.000 description 1
- 239000012298 atmosphere Substances 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 238000006555 catalytic reaction Methods 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 239000000498 cooling water Substances 0.000 description 1
- 235000019628 coolness Nutrition 0.000 description 1
- 238000006392 deoxygenation reaction Methods 0.000 description 1
- 238000006477 desulfuration reaction Methods 0.000 description 1
- 230000023556 desulfurization Effects 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000001704 evaporation Methods 0.000 description 1
- 230000008020 evaporation Effects 0.000 description 1
- 229910000037 hydrogen sulfide Inorganic materials 0.000 description 1
- 239000003317 industrial substance Substances 0.000 description 1
- 238000002386 leaching Methods 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- QSHDDOUJBYECFT-UHFFFAOYSA-N mercury Chemical compound [Hg] QSHDDOUJBYECFT-UHFFFAOYSA-N 0.000 description 1
- 229910052753 mercury Inorganic materials 0.000 description 1
- 238000005065 mining Methods 0.000 description 1
- 239000002808 molecular sieve Substances 0.000 description 1
- QJGQUHMNIGDVPM-UHFFFAOYSA-N nitrogen group Chemical group [N] QJGQUHMNIGDVPM-UHFFFAOYSA-N 0.000 description 1
- 229920006395 saturated elastomer Polymers 0.000 description 1
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 description 1
- 238000001179 sorption measurement Methods 0.000 description 1
- 229910052717 sulfur Inorganic materials 0.000 description 1
- 239000011593 sulfur Substances 0.000 description 1
- 230000026676 system process Effects 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
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Abstract
The utility model discloses a burning and explosion-suppressing low-concentration coal-bed methane cryogenic liquefying device which comprises a coal-bed methane storage system, a coal-bed methane compression system, a coal-bed methane purification system, a coal-bed methane liquification and separation system, an LNG ((Liquefied Natural Gas) storage system and a refrigeration cycle system, wherein active explosion-suppressing devices are respectively arranged on the front side and the rear side of the coal-bed methane storage system; a rectifying tower is filled with filler which is used for fractionating methane in the coal-bed methane and has an explosion suppressing performance; flame-retardant and explosion-suppressing materials are also arranged in the rectifying tower and are fire-retardant screen meshes which are paved in the filler at intervals. The active explosion-suppressing devices can be used for effectively preventing flame from spreading to a gas cabinet and ensuring the safety of the gas cabinet and an underground extraction system of a coal mine. The flame-retardant and explosion-suppressing materials are arranged in the rectifying tower, so that the explosion can be prevented in the liquefying and extraction process of the methane even if the methane enters the range of explosion limit, and the methane with high yield and high purity can be obtained from low-concentration oxygen-containing coal-bed methane under the condition of not deoxidizing the coal-bed methane in advance.
Description
Technical field
The utility model belongs to the technical field that makes gas or admixture of gas be liquefied, solidify or separate by pressurization and cooling processing, is specifically related to a kind of combustion and explosion suppression type low concentration coal-bed gas cryogenic liquefying device.
Background technology
Coalbed methane containing oxygen be colliery in recovery process for preventing gas explosion and outstanding, the elementary byproduct that guarantees Safety of Coal Mine Production and pump out, its main component is methane, from its component content, can find out, coal bed gas is the energy and the industrial chemicals of outbalance.But because its composition is comparatively complicated, particularly in coal bed gas, contain aerobic, it is breakneck combustion-supporting pro-knock agent, restricted the comprehensive utilization of coalbed methane containing oxygen, in practice, for cost-saving, coal bed gas generally enters atmosphere in the coal mining process, causes the profligacy of resource and to environment.
Because methane content in the low concentration coalbed methane containing oxygen is lower, residual gas is mainly air, so have explosion danger.At normal temperatures and pressures, methane concentration can be blasted 5%～15%, during methane in purification low concentration coalbed methane containing oxygen, along with concentrating of methane, in residual gas, methane content reduces gradually, once enter 5%～15% explosive range, just may blast, this be methane in all extraction low concentration coalbed methane containing oxygens method the problem that must solve.
In the technical method of reporting at present, mainly take following measures to guarantee safety: the one, at first remove the oxygen in the low concentration coalbed methane containing oxygen by means such as catalysis, pressure-variable adsorption, film separation, solution absorptions, and then extract methane wherein; The 2nd, in whole leaching process, guarantee that methane concentration is higher than UEL everywhere; Perhaps in some technical method, do not mention the impact of oxygen on security, the technical standpoint only separated from gas is described the method for extracting methane.
Although having improved to a certain extent, these methods extract the security in the methane process in the low concentration coalbed methane containing oxygen, but also have the following disadvantages: formerly deoxygenation is extracted in the method for methane again, needing increases deoxidation equipment, has increased equipment investment and operating cost; Control methane content higher than UEL in whole extraction methane process, to guarantee safe method, sacrificed methane recovery.
Summary of the invention
In view of this, the purpose of this utility model is to provide a kind of combustion and explosion suppression type low concentration coal-bed gas cryogenic liquefying device, and this device can be in the situation that not deoxidation in advance obtains high-recovery and high-purity methane from the low concentration coalbed methane containing oxygen.
For achieving the above object, the utility model provides following technical scheme:
A kind of combustion and explosion suppression type low concentration coal-bed gas cryogenic liquefying device, comprise coal bed gas storage system, coal bed gas compressibility, coal bed gas cleaning system, coal gas gasification and piece-rate system, LNG storage system and, for the cooling cycle system of cold is provided to described coal gas gasification and piece-rate system, the both sides, front and back of described coal bed gas storage system are equipped with the active explosion suppression device;
Described active explosion suppression device comprises controller, the sensor group be connected with controller and the automatic explosion arrestment valve, automatic powder spraying explosion-suppressing device, the water-sealing fire-retardant explosion venting device that set gradually and all be connected with controller along the coal bed gas flow direction, and described sensor group comprises along the flame sensor and the pressure sensor that are separately positioned in described coal bed gas compressibility, coal bed gas cleaning system, coal gas gasification and piece-rate system;
Described coal gas gasification and piece-rate system comprise along coal bed gas and flow to the first-class heat exchanger set gradually, secondary heat exchanger, three grades of heat exchangers, subcooler, choke valve V
fAnd rectifying column, described rectifying column tower top arranges overhead condenser, the interior setting of rectifying tower is positioned at the reboiler at the bottom of tower, and the nitrogen oxygen outlet that described rectifying column tower top arranges is connected with the nitrogen oxygen outlet of described overhead condenser, and at the bottom of the tower of described rectifying column, condensate outlet is set;
Be filled with in described rectifying column for fractionation coal bed gas methane and filler with datonation-inhibition function, also be provided with the back-fire relief explosion-suppressing material in described rectifying column, described back-fire relief explosion-suppressing material is that interval is laid on the back-fire relief silk screen in described filler.
Further, described refrigeration system comprises the azeotrope circulatory system and nitrogen cycle system;
The described azeotrope circulatory system comprises choke valve V
1, choke valve V
2With the azeotrope compressor set gradually along the azeotrope flow direction, azeotrope cooler, heavy hydrocarbon separator; The gas phase azeotrope outlet of described heavy hydrocarbon separator is communicated in the gas phase azeotrope entrance of described reboiler successively by first-class heat exchanger and secondary heat exchanger, the gas phase azeotrope outlet of described reboiler is successively by choke valve V
2, three grades of heat exchanger, secondary heat exchanger and first-class heat exchanger reflux the gas phase azeotrope and be communicated in the azeotrope entrance of described azeotrope compressor; The liquid phase azeotrope outlet of described heavy hydrocarbon separator is by first-class heat exchanger and choke valve V
1The rear gas phase azeotrope with backflow converges;
Described nitrogen cycle system comprises choke valve V
3With nitrogen compressor, the nitrogen cooler that flow direction along the nitrogen cooling agent sets gradually, the nitrogen outlet of described nitrogen cooler is successively by described first-class heat exchanger, secondary heat exchanger, three grades of heat exchangers, subcooler and choke valve V
3Be communicated in the nitrogen entrance of described overhead condenser, the outlet of the nitrogen of described overhead condenser refluxes the nitrogen cooling agent by subcooler, three grades of heat exchangers, secondary heat exchanger and first-class heat exchanger successively and is communicated in the nitrogen entrance of described nitrogen compressor.
Further, described coal gas gasification and piece-rate system also comprise decompressor, the nitrogen oxygen outlet of described rectifying column is communicated in the nitrogen oxygen intake of described decompressor by described subcooler, the nitrogen oxygen outlet of described decompressor makes to enter cleaning procedure after the re-heat of nitrogen oxygen by subcooler, three grades of heat exchangers, secondary heat exchanger and first-class heat exchanger successively.
Further, the condensate outlet of described rectifying column is communicated in the liquefied methane storage tank by described three grades of heat exchangers.
Further, the mesh size of back-fire relief silk screen is 80～200 orders.
Further, the laying density of described back-fire relief silk screen is to lay the 1-12 layer at interval of 300mm.
The beneficial effects of the utility model are:
The utility model combustion and explosion suppression type low concentration coal-bed gas cryogenic liquefying device, by the coal bed gas storage system being set for storing the raw material coal bed gas, also play cushioning effect; By the sensor group that the active explosion suppression device is set and safe-guard system is installed at the inlet end of key equipment, as flame sensor, pressure sensor, can effectively stop flame to be propagated to the coal bed gas storage system, ensure the safety of extraction system under gas holder and coal mine;
By arrange coal gas gasification and piece-rate system for cooling coal bed gas to design temperature and make methane liquefaction, then liquefied methane is separated with nitrogen oxygen component, form the LNG product, and by filler and the back-fire relief explosion-suppressing material that can meet the rectifying condition and have datonation-inhibition function is set in rectifying column, in coal bed gas rectifying separation process, extraction along with methane, even enter the explosion limit scope of methane, under the effect of filler and back-fire relief explosion-suppressing material, coal bed gas is split into some micro volumes unit, the blast chain reaction is cut off, thus prevent exploding; At low concentration coal-bed gas in the rectifying separation process, the methane in coal bed gas can be separated as much as possible concentratedly, purity and the rate of recovery of methane are higher; Therefore, combustion and explosion suppression type low concentration coal-bed gas cryogenic liquefying device of the present utility model can be in the situation that not deoxidation in advance obtains high-recovery and high-purity methane from the low concentration coalbed methane containing oxygen.
The accompanying drawing explanation
In order to make the purpose of this utility model, technical scheme and beneficial effect clearer, the utility model provides following accompanying drawing to describe:
The structural representation that Fig. 1 is the utility model combustion and explosion suppression type low concentration coal-bed gas cryogenic liquefying device;
The structural representation that Fig. 2 is rectifying column;
The A detail drawing that Fig. 3 is Fig. 2;
Fig. 4 is for adopting the liquefaction of the utility model combustion and explosion suppression type low concentration coal-bed gas cryogenic liquefying device and piece-rate system process chart.
Description of reference numerals:
The 1-gas holder; The automatic explosion arrestment valve of 2-; The 3-automatic powder spraying explosion-suppressing device; 4-water-sealing fire-retardant explosion venting device; The automatic explosion arrestment valve of 5-; The 6-automatic powder spraying explosion-suppressing device; 7-water-sealing fire-retardant explosion venting device; The 8-coal bed gas compressor; 9-coal bed gas cooler; 10-demercuration tower; The 11-absorption tower; 12-dehydrating tower I; 13-dehydrating tower II; The 14-first-class heat exchanger; The 15-secondary heat exchanger; Tri-grades of heat exchangers of 16-; The 17-subcooler; The 18-rectifying column; The 18a-filler; 18b-back-fire relief silk screen; The 19-overhead condenser; The 20-reboiler; 21-liquefied methane storage tank; 22-azeotrope compressor; 23-azeotrope cooler; 24-heavy hydrocarbon separator; 25-nitrogen compressor; 26-nitrogen cooler; The 27-decompressor.
The specific embodiment
Below in conjunction with accompanying drawing, preferred embodiment of the present utility model is described in detail.
As shown in Figure 1, be the structural representation of the utility model combustion and explosion suppression type low concentration coal-bed gas cryogenic liquefying device embodiment.The combustion and explosion suppression type low concentration coal-bed gas cryogenic liquefying device of the present embodiment, comprise coal bed gas storage system, coal bed gas compressibility, coal bed gas cleaning system, coal gas gasification and piece-rate system, LNG storage system and, for the cooling cycle system of cold is provided to described coal gas gasification and piece-rate system, the both sides, front and back of described coal bed gas storage system are equipped with the active explosion suppression device.
The coal bed gas storage system comprises gas holder 1, be arranged on the air inlet pipeline of gas holder 1 and the active explosion suppression device on outlet pipe comprises controller, the sensor group be connected with controller and the automatic explosion arrestment valve that sets gradually and all be connected with controller along the coal bed gas flow direction, automatic powder spraying explosion-suppressing device, the water-sealing fire-retardant explosion venting device, automatic explosion arrestment valve 2 wherein, automatic powder spraying explosion-suppressing device 3, water-sealing fire-retardant explosion venting device 4 is arranged on the air inlet pipeline of gas holder 1, automatic explosion arrestment valve 5, automatic powder spraying explosion-suppressing device 6, water-sealing fire-retardant explosion venting device 7 is arranged on the outlet pipe of gas holder 1.The sensor group comprises along the flame sensor and the pressure sensor that are separately positioned in coal bed gas compressibility, coal bed gas cleaning system, coal gas gasification and piece-rate system.
The coal bed gas compressibility comprises at least one group of supercharging compression unit of mutually connecting set gradually along the coal bed gas flow direction, every group of supercharging compression unit comprises coal bed gas compressor 8 and coal bed gas cooler 9, by the coal bed gas compressibility, for supercharging compression coal bed gas, the coal bed gas compressibility of the present embodiment comprises one group of supercharging compression unit.
The coal bed gas cleaning system comprises demercuration tower 10, absorption tower 11 and the dewater unit set gradually along the coal bed gas flow direction, the coal bed gas entrance of demercuration tower 8 is connected with the outlet of the coal bed gas of coal bed gas cooler 7, dewater unit comprises dehydrating tower I12 and the dehydrating tower II13 be arranged in parallel, dehydrating tower I12 and dehydrating tower II13 are mutually standby, and saturated another dehydrating tower of rear use of dehydrating tower works on therein.Wherein, the preferred sulfur-bearing active carbon of demercuration medium in demercuration tower 10, the medium in absorption tower 11 preferably adopts the MEA solution that adds activator and antioxidant, and active carbon or molecular sieve are set in dewater unit, can meet technological requirement.
Coal gas gasification and piece-rate system comprise along coal bed gas and flow to the first-class heat exchanger 14 set gradually, secondary heat exchanger 14, three grades of heat exchangers 16, subcooler 17, choke valve V
fWith rectifying column 18, the rectifying column tower top arranges overhead condenser 19, the interior setting of rectifying tower is positioned at the reboiler 20 at the bottom of tower, the nitrogen oxygen outlet that rectifying column 18 tower tops arrange is connected with the nitrogen oxygen outlet of overhead condenser 19, and at the bottom of the tower of described rectifying column 18, condensate outlet is set, flows out for liquified natural gas.
Be filled with in rectifying column 18 for fractionation coal bed gas methane and filler 18a with datonation-inhibition function, also be provided with the back-fire relief explosion-suppressing material in rectifying column 18, the back-fire relief explosion-suppressing material is that interval is laid on the back-fire relief silk screen 18b in filler 18a.The mesh size of the back-fire relief silk screen 18b of the present embodiment is 80～200 orders, and the laying density of back-fire relief silk screen 18b is that the laying density of the back-fire relief silk screen 18b of the present embodiment is to lay 5 layers at interval of 300mm at interval of 300mm laying 1-12 layer.
The LNG storage system comprises liquefied methane storage tank 21, and the entrance of liquefied methane storage tank 21 is connected with the condensate outlet of described rectifying column 19.The condensate outlet of the rectifying column 18 of the present embodiment is communicated in liquefied methane storage tank 21 after by three grades of heat exchangers 16, makes gas product reach supercooled state, is convenient to store.
The present embodiment combustion and explosion suppression type low concentration coal-bed gas cryogenic liquefying device, by the coal bed gas storage system being set for storing the raw material coal bed gas, also play cushioning effect; By the sensor group that the active explosion suppression device is set and safe-guard system is installed at the inlet end of key equipment, as flame sensor, pressure sensor, can effectively stop flame to be propagated to the coal bed gas storage system, ensure the safety of extraction system under gas holder and coal mine.
By arrange coal gas gasification and piece-rate system for cooling coal bed gas to design temperature and make methane liquefaction, then liquefied methane is separated with nitrogen oxygen component, form the LNG product, and by the interior setting of rectifying column 19, meeting the rectifying condition, and filler 19a and back-fire relief explosion-suppressing material with datonation-inhibition function, in coal bed gas rectifying separation process, extraction along with methane, even enter the explosion limit scope of methane, under the effect of filler and back-fire relief explosion-suppressing material, coal bed gas is split into some micro volumes unit, the blast chain reaction is cut off, thereby prevent exploding, at low concentration coal-bed gas in the rectifying separation process, the methane in coal bed gas can be separated as much as possible concentratedly, purity and the rate of recovery of methane are higher, therefore, the combustion and explosion suppression type low concentration coal-bed gas cryogenic liquefying device of the present embodiment can be in the situation that not deoxidation in advance obtains high-recovery and high-purity methane from the low concentration coalbed methane containing oxygen.
Further, refrigeration system comprises the azeotrope circulatory system and nitrogen cycle system;
The described azeotrope circulatory system comprises choke valve V
1, choke valve V
2With the azeotrope compressor 22 set gradually along the azeotrope flow direction, azeotrope cooler 23, heavy hydrocarbon separator 24.The gas phase azeotrope outlet of heavy hydrocarbon separator 24 is communicated in the gas phase azeotrope entrance of reboiler 20 successively by first-class heat exchanger 14 and secondary heat exchanger 15, the gas phase azeotrope outlet of reboiler 20 is successively by choke valve V
2, three grades of heat exchanger 16, secondary heat exchanger 15 and first-class heat exchanger 14 reflux the gas phase azeotrope and be communicated in the azeotrope entrance of azeotrope compressor 22; The liquid phase azeotrope outlet of heavy hydrocarbon separator 24 is by first-class heat exchanger 14 and choke valve V
1Rear with the gas phase azeotrope refluxed, converge, liquid phase azeotrope and gas phase azeotrope converge by refluxing together with first-class heat exchanger 1 and enter azeotrope compressor 8, and azeotrope can be recycled.
The mixture that the azeotrope of the present embodiment is nitrogen, methane, ethene, propane, isopentane, concrete, the component of azeotrope is: 23.5% nitrogen; 38.8% methane; 11% ethene; 14.2% propane; 12.5% isopentane, can meet the temperature control requirement in the links of producing at liquefied natural gas, certainly, azeotrope also can adopt the azeotrope of existing other components, the component proportion of azeotrope also can be set to difference, and its principle is suitable, is not repeated.
The nitrogen cycle system comprises choke valve V
3With nitrogen compressor 25, the nitrogen cooler 26 that flow direction along the nitrogen cooling agent sets gradually, the nitrogen outlet of nitrogen cooler 26 is successively by described first-class heat exchanger 14, secondary heat exchanger 15, three grades of heat exchangers 16, subcooler 17 and choke valve V
3Be communicated in the nitrogen entrance of described overhead condenser 19, the outlet of the nitrogen of overhead condenser 19 refluxes the nitrogen cooling agent by subcooler 17, three grades of heat exchangers 16, secondary heat exchanger 15 and first-class heat exchanger 14 successively and is communicated in the nitrogen entrance of nitrogen compressor 25, nitrogen can be recycled, and provide cold to overhead condenser 19.
Further, coal gas gasification and piece-rate system also comprise decompressor 27, the nitrogen oxygen outlet of rectifying column 18 is communicated in the nitrogen oxygen intake of decompressor 27 by subcooler 17, the nitrogen oxygen outlet of decompressor 27 makes to enter cleaning procedure after the re-heat of nitrogen oxygen by subcooler 17, three grades of heat exchangers 16, secondary heat exchanger 15 and first-class heat exchanger 14 successively.By decompressor 27 is set, make it emptying at normal temperatures and pressures, thereby fully reclaim the energy of the nitrogen oxygen backflowed, reach the purpose of energy-saving and emission-reduction.
Concrete, adopt the method for the present embodiment combustion and explosion suppression type low concentration coal-bed gas cryogenic liquefying device extraction methane as follows, comprise following operation:
1) coal bed gas storage operation: adopt gas holder 1 storage low concentration coalbed methane containing oxygen, and pressure store is 0.001MPa～0.005MPaG.
2) coal bed gas compression section: adopt coal bed gas compressor 8 that the coal bed gas supercharging of gas holder 1 output is compressed to 0.35～0.4MPaG, and, in the supercharging compression process, keep the temperature of coal bed gas lower than 80 ℃.Concrete, in the supercharging compression process, when the temperature of coal bed gas is about to reach 80 ℃, adopt cooling water that coal bed gas is cooled to 40 ℃, then continue the supercharging compression, the coal bed gas after the supercharging compression enters coal bed gas cooler 9 and is cooled to normal temperature.
3) coal bed gas cleaning procedure: the coal bed gas after the supercharging compression is carried out to demercuration, desulfurization, carbon dioxide removal and processed successively.In coal bed gas after purified treatment, mercury content is less than 0.1umg/m
3, hydrogen sulfide content is less than 1ppm, and carbon dioxide content is less than 50ppm, and water content is less than 1ppm.
4) coal bed gas refrigerating work procedure: the coal bed gas after purifying is cooled to-140 ℃～-160 ℃, and, in cooled coal gas layer, liquid mole fraction is no more than 15%, the chilling temperature of coal bed gas is relevant with the component of coal bed gas.
5) coal bed gas rectifying separation circuit: cooled coal bed gas is delivered to rectifying column 18, methane liquefaction in coal bed gas is separated, liquefaction separates the methane liquid obtained and enters the reboiler 20 that is arranged in 18 ends of rectifying column, make the nitrogen and the oxygen evaporation that contain in methane liquid, liquefaction separates the nitrogen oxygen obtained and enters overhead condenser 19 coolings that are arranged in rectifying column 18 tops, after the methane liquefaction separation that makes to contain in nitrogen oxygen, is back in rectifying column 18.So, after coal bed gas rectifying separation circuit is processed, in the liquefied methane obtained, methane content is higher than 99%, and in the nitrogen oxygen of discharge, the content of methane is lower than 0.5%.
6) liquefied methane storage operation: rectifying is separated to the liquefied methane obtained and be stored in liquefied methane storage tank 21, the preferred low temperature primary and secondary tank with pressure of liquefied methane storage tank 21.
By being 25%～40% by methane content, the low concentration coalbed methane containing oxygen is stored in gas holder 1 with 0.001MPa～0.005MPaG at normal temperatures, and, by the active explosion suppression device is set on the air inlet pipeline at gas holder and outlet pipe, can not have explosion danger; In the coal bed gas compression section, the high pressure-charging pressure of controlling coal bed gas is 0.35～0.4MPaG, and maximum temperature is no more than 80 ℃, in a safe condition, without explosion danger; In the coal bed gas purification process, coal bed gas pressure is 0.35～0.4MPaG, and temperature is normal temperature, without explosion danger; In the coal bed gas refrigerating work procedure, coal bed gas makes liquid mole fraction be no more than 15% after being cooled to-140 ℃～-160 ℃, in this state, in the gas phase of coal bed gas, methane content is not less than 25%, and pressure is no more than 0.4MPaG, for safe condition, without explosion danger; In coal bed gas rectifying separation circuit, by being arranged in rectifying column 18 filler and the back-fire relief explosion-suppressing material that is provided for methane in the fractionation coal bed gas and there is datonation-inhibition function, in coal bed gas rectifying separation circuit, extraction along with methane, in gas, methane content reduces gradually, until enter 5%～15% explosive range, but, under the effect of back-fire relief explosion-suppressing material, can prevent exploding, and in the nitrogen oxygen of discharging the content of methane lower than 0.5%, without explosion danger, the methane content of the liquefied methane obtained is more than 99%, without explosion danger; In liquefied methane storage operation, the methane content in liquefied methane is constant, does not have the danger of blast.
To sum up, the utility model combustion and explosion suppression type low concentration coal-bed gas cryogenic liquefying device can realize in the situation that not deoxidation in advance, obtains the methane of high-recovery from the low concentration coalbed methane containing oxygen, can effectively reduce equipment investment and enhance productivity.
Finally explanation is, above preferred embodiment is only unrestricted in order to the technical solution of the utility model to be described, although the utility model is described in detail by above preferred embodiment, but those skilled in the art are to be understood that, can make various changes to it in the form and details, and not depart from the utility model claims limited range.
Claims (6)
1. a combustion and explosion suppression type low concentration coal-bed gas cryogenic liquefying device, comprise coal bed gas storage system, coal bed gas compressibility, coal bed gas cleaning system, coal gas gasification and piece-rate system, LNG storage system and, for the cooling cycle system of cold is provided to described coal gas gasification and piece-rate system, it is characterized in that: the both sides, front and back of described coal bed gas storage system are equipped with the active explosion suppression device;
Described active explosion suppression device comprises controller, the sensor group be connected with controller and the automatic explosion arrestment valve, automatic powder spraying explosion-suppressing device, the water-sealing fire-retardant explosion venting device that set gradually and all be connected with controller along the coal bed gas flow direction, and described sensor group comprises along the flame sensor and the pressure sensor that are separately positioned in described coal bed gas compressibility, coal bed gas cleaning system, coal gas gasification and piece-rate system;
Described coal gas gasification and piece-rate system comprise along coal bed gas and flow to the first-class heat exchanger set gradually, secondary heat exchanger, three grades of heat exchangers, subcooler, choke valve V
fAnd rectifying column, described rectifying column tower top arranges overhead condenser, the interior setting of rectifying tower is positioned at the reboiler at the bottom of tower, and the nitrogen oxygen outlet that described rectifying column tower top arranges is connected with the nitrogen oxygen outlet of described overhead condenser, and at the bottom of the tower of described rectifying column, condensate outlet is set;
Be filled with in described rectifying column for fractionation coal bed gas methane and filler with datonation-inhibition function, also be provided with the back-fire relief explosion-suppressing material in described rectifying column, described back-fire relief explosion-suppressing material is that interval is laid on the back-fire relief silk screen in described filler.
2. combustion and explosion suppression type low concentration coal-bed gas cryogenic liquefying device according to claim 1, it is characterized in that: described refrigeration system comprises the azeotrope circulatory system and nitrogen cycle system;
The described azeotrope circulatory system comprises choke valve V
1, choke valve V
2With the azeotrope compressor set gradually along the azeotrope flow direction, azeotrope cooler, heavy hydrocarbon separator; The gas phase azeotrope outlet of described heavy hydrocarbon separator is communicated in the gas phase azeotrope entrance of described reboiler successively by first-class heat exchanger and secondary heat exchanger, the gas phase azeotrope outlet of described reboiler is successively by choke valve V
2, three grades of heat exchanger, secondary heat exchanger and first-class heat exchanger reflux the gas phase azeotrope and be communicated in the azeotrope entrance of described azeotrope compressor; The liquid phase azeotrope outlet of described heavy hydrocarbon separator is by first-class heat exchanger and choke valve V
1The rear gas phase azeotrope with backflow converges;
Described nitrogen cycle system comprises choke valve V
3With nitrogen compressor, the nitrogen cooler that flow direction along the nitrogen cooling agent sets gradually, the nitrogen outlet of described nitrogen cooler is successively by described first-class heat exchanger, secondary heat exchanger, three grades of heat exchangers, subcooler and choke valve V
3Be communicated in the nitrogen entrance of described overhead condenser, the outlet of the nitrogen of described overhead condenser refluxes the nitrogen cooling agent by subcooler, three grades of heat exchangers, secondary heat exchanger and first-class heat exchanger successively and is communicated in the nitrogen entrance of described nitrogen compressor.
3. combustion and explosion suppression type low concentration coal-bed gas cryogenic liquefying device according to claim 2, it is characterized in that: described coal gas gasification and piece-rate system also comprise decompressor, the nitrogen oxygen outlet of described rectifying column is communicated in the nitrogen oxygen intake of described decompressor by described subcooler, the nitrogen oxygen outlet of described decompressor makes to enter cleaning procedure after the re-heat of nitrogen oxygen by subcooler, three grades of heat exchangers, secondary heat exchanger and first-class heat exchanger successively.
4. combustion and explosion suppression type low concentration coal-bed gas cryogenic liquefying device according to claim 2, it is characterized in that: the condensate outlet of described rectifying column is communicated in the liquefied methane storage tank by described three grades of heat exchangers.
5. according to the described combustion and explosion suppression type of claim 1-4 any one low concentration coal-bed gas cryogenic liquefying device, it is characterized in that: the mesh size of back-fire relief silk screen is 80～200 orders.
6. combustion and explosion suppression type low concentration coal-bed gas cryogenic liquefying device according to claim 5 is characterized in that: the laying density of described back-fire relief silk screen is for laying the 1-12 layer at interval of 300mm.
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103256786A (en) * | 2013-06-08 | 2013-08-21 | 中煤科工集团重庆研究院 | Flame-suppression and explosion-suppression cryogenic liquefaction device for low-concentration coal bed gas |
| CN105296038A (en) * | 2015-11-27 | 2016-02-03 | 中煤科工集团重庆研究院有限公司 | Oxygen-bearing coal-bed gas low-temperature concentration method and device for implementing method |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103256786A (en) * | 2013-06-08 | 2013-08-21 | 中煤科工集团重庆研究院 | Flame-suppression and explosion-suppression cryogenic liquefaction device for low-concentration coal bed gas |
| CN103256786B (en) * | 2013-06-08 | 2015-09-09 | 中煤科工集团重庆研究院有限公司 | Combustion and explosion suppression type low concentration coal-bed gas cryogenic liquefying device |
| CN105296038A (en) * | 2015-11-27 | 2016-02-03 | 中煤科工集团重庆研究院有限公司 | Oxygen-bearing coal-bed gas low-temperature concentration method and device for implementing method |
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