CN103256786A - Flame-suppression and explosion-suppression cryogenic liquefaction device for low-concentration coal bed gas - Google Patents
Flame-suppression and explosion-suppression cryogenic liquefaction device for low-concentration coal bed gas Download PDFInfo
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- CN103256786A CN103256786A CN2013102283091A CN201310228309A CN103256786A CN 103256786 A CN103256786 A CN 103256786A CN 2013102283091 A CN2013102283091 A CN 2013102283091A CN 201310228309 A CN201310228309 A CN 201310228309A CN 103256786 A CN103256786 A CN 103256786A
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Abstract
The invention discloses a flame-suppression and explosion-suppression cryogenic liquefaction device for low-concentration coal bed gas, which comprises a coal bed gas storage system, a coal bed gas compression system, a coal bed gas purification system, a coal bed gas liquefaction and separation system, an LNG (Liquefied Natural Gas) storage system and a refrigerating circulatory system, wherein driving explosion-suppression devices are arranged on the front side and the rear side of the coal bed gas storage system; a filler used for fractionating methane in the coal bed gas and having the explosion-suppression performance is filled in a rectifying tower; the rectifying tower is internally provided with a fire-retardance and explosion-suppression material; the fire-retardance and explosion-suppression material is a fire-retardance silk screen which is laid in the filler at intervals; and the driving explosion-suppression devices can effectively prevent flame from spreading to a gas holder, and can guarantee the safety of the gas holder and an underground coal mine drainage system. The fire-retardance and explosion-suppression material is arranged in the rectifying tower, so that explosion can be prevented even if the methane enters an explosion limit range in a liquefaction extraction process of the methane, and the high-recovery and high-purity methane can be obtained from the low-concentration oxygenic coal bed gas under the condition that deoxygenation is not performed in advance.
Description
Technical field
The invention belongs to the technical field that makes gas or admixture of gas liquefy, solidify or separate by pressurization and cooling processing, be 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 the colliery in recovery process for preventing gas explosion and outstanding, guarantee Safety of Coal Mine Production and elementary byproduct that pump drainage goes out, its main component is methane, and as can be seen, coal bed gas is the energy and the industrial chemicals of outbalance from its component content.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 the practice, in order to save cost, coal bed gas generally enters atmosphere in the coal mining process, causes the profligacy of resource and environment is polluted.
Because methane content is lower in the low concentration coalbed methane containing oxygen, 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, methane content reduces gradually in the residual gas, just may blast in case enter 5%～15% explosive range, this is that all extract the problem that the methods institute of methane in low concentration coalbed methane containing oxygens must solution.
In the technical method of present report, mainly take following measure to guarantee safety: the one, at first remove oxygen in the low concentration coalbed methane containing oxygen and then extraction methane wherein by means such as catalysis, transformation absorption, film separation, solution absorptions; The 2nd, in whole leaching process, guarantee that methane concentration is higher than UEL everywhere; Perhaps do not mention oxygen in some technical method to Influence on security, only the technical standpoint that separates from gas is described the method for extracting methane.
Though having improved to a certain extent, these methods in the low concentration coalbed methane containing oxygen, extract the methane process safe, but also have the following disadvantages: deoxygenation is formerly extracted in the method for methane again, needing increases deoxidation equipment, has increased equipment investment and operating cost; The control methane content is higher than UEL in whole extraction methane process, has then sacrificed methane recovery to guarantee safe method.
Summary of the invention
In view of this, the object of the present invention is to provide a kind of combustion and explosion suppression type low concentration coal bed gas cryogenic liquefying device, this device can obtain high-recovery and high-purity methane from the low concentration coalbed methane containing oxygen under the situation of not deoxidation in advance.
For achieving the above object, the invention 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 be used for providing to described coal gas gasification and piece-rate system the cooling cycle system of cold, the both sides, front and back of described coal bed gas storage system are equipped with the active explosion suppression device;
Described coal bed gas compressibility comprises at least one group of supercharging compression unit of connecting mutually that sets gradually along the coal bed gas flow direction, and every group of described supercharging compression unit comprises coal bed gas compressor and coal bed gas cooler;
Described active explosion suppression device comprises controller, the sensor groups that links to each other with controller and the automatic explosion arrestment valve, automatic powder spraying explosion suppression device, the water seal back-fire relief explosion venting device that set gradually and all link to each other with controller along the coal bed gas flow direction, and described sensor groups 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 the 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 cat head arranges overhead condenser, the interior setting of rectifying Tata is positioned at the reboiler at the bottom of the tower, and the nitrogen oxygen outlet that described rectifying column cat head arranges links to each other 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 the 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 the described rectifying column, described back-fire relief explosion-suppressing material is for being laid on the back-fire relief silk screen in the described filler at interval.
Further, described coal bed gas storage system comprises gas holder;
Described coal bed gas cleaning system comprises demercuration tower, absorption tower and the dewater unit that sets gradually along the coal bed gas flow direction;
Described LNG storage system comprises the liquefied methane storage tank, and the entrance of described liquefied methane storage tank links to each other with the condensate outlet of described rectifying column.
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 that sets 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 back is converged with the gas phase azeotrope that refluxes;
Described nitrogen cycle system comprises choke valve V
3With the nitrogen compressor that sets gradually along nitrogen flow of coolant direction, nitrogen cooler, the nitrogen of described nitrogen cooler exports 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, and the nitrogen oxygen outlet of described decompressor enters cleaning procedure by subcooler, three grades of heat exchangers, secondary heat exchanger and first-class heat exchanger after making the re-heat of nitrogen oxygen successively.
Further, described azeotrope is the mixture of nitrogen, methane, ethene, propane, isopentane;
Further, the component of described azeotrope is: 23.5% nitrogen; 38.8% methane; 11% ethene; 14.2% propane; 12.5% isopentane.
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 that every interval 300mm lays the 1-12 layer.
Beneficial effect of the present invention is:
Combustion and explosion suppression type low concentration coal bed gas cryogenic liquefying device of the present invention is used for storage raw material coal bed gas by the coal bed gas storage system is set, and also plays cushioning effect; By the sensor groups 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 the coal mine;
Be used for the cooling coal bed gas to design temperature and make methane liquefaction by coal gas gasification and piece-rate system are set, 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 satisfy 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 microbody product units, the blast chain reaction is cut off, thereby prevents blast; Namely in the low concentration coal bed gas in the rectifying separation process, the methane in the 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 invention can obtain high-recovery and high-purity methane from the low concentration coalbed methane containing oxygen under the situation of not deoxidation in advance;
By many groups supercharging compression unit of mutual series connection is set, can be in coal bed gas supercharging compression process, keep the temperature of coal bed gas below 80 ℃, when the temperature of coal bed gas is about to reach 80 ℃, compress exporting next group supercharging compression unit after the coal bed gas cooling to, can effectively prevent the coal bed gas blast.
Description of drawings
In order to make purpose of the present invention, technical scheme and beneficial effect clearer, the invention provides following accompanying drawing and describe:
Fig. 1 is the structural representation of combustion and explosion suppression type low concentration coal bed gas cryogenic liquefying device of the present invention;
Fig. 2 is the structural representation of rectifying column;
Fig. 3 is the A detail drawing of Fig. 2;
Fig. 4 is for adopting combustion and explosion suppression type low concentration coal bed gas cryogenic liquefying device liquefaction of the present invention and piece-rate system process chart.
Description of reference numerals:
The 1-gas holder; The automatic explosion arrestment valve of 2-; 3-automatic powder spraying explosion suppression device; 4-water seal back-fire relief explosion venting device; The automatic explosion arrestment valve of 5-; 6-automatic powder spraying explosion suppression device; 7-water seal back-fire relief explosion venting device; 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; Three 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, the preferred embodiments of the present invention are described in detail.
As shown in Figure 1, be the structural representation of combustion and explosion suppression type low concentration coal bed gas cryogenic liquefying device embodiment of the present invention.The combustion and explosion suppression type low concentration coal bed gas cryogenic liquefying device of 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 be used for providing to described coal gas gasification and piece-rate system the cooling cycle system of cold, 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 the outlet pipe comprises controller, the sensor groups that links to each other with controller and the automatic explosion arrestment valve that sets gradually and all link to each other with controller along the coal bed gas flow direction, the automatic powder spraying explosion suppression device, water seal back-fire relief explosion venting device, automatic explosion arrestment valve 2 wherein, automatic powder spraying explosion suppression device 3, water seal back-fire relief explosion venting device 4 is arranged on the air inlet pipeline of gas holder 1, automatically explosion arrestment valve 5, automatic powder spraying explosion suppression device 6, water seal back-fire relief explosion venting device 7 is arranged on the outlet pipe of gas holder 1.Sensor groups 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 the piece-rate system.
The coal bed gas compressibility comprises at least one group of supercharging compression unit of connecting mutually that sets 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, be used for supercharging compression coal bed gas by the coal bed gas compressibility, by many groups supercharging compression unit of mutual series connection is set, can be in coal bed gas supercharging compression process, keep the temperature of coal bed gas below 80 ℃, when the temperature of coal bed gas is about to reach 80 ℃, compress exporting next group supercharging compression unit after the coal bed gas cooling to, can effectively prevent the coal bed gas blast.The coal bed gas compressibility of present embodiment comprises two groups of supercharging compression units, and certainly, the supercharging compression unit also can be set to more than three groups and three groups as required, and its principle is suitable, is not repeated.
The coal bed gas cleaning system comprises demercuration tower 10, absorption tower 11 and the dewater unit that sets gradually along the coal bed gas flow direction, the coal bed gas entrance of demercuration tower 8 links to each other 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 that is arranged in parallel, dehydrating tower I12 and dehydrating tower II13 are standby mutually, and the saturated back of dehydrating tower works on another dehydrating tower therein.Wherein, the preferred sulfur-bearing active carbon of demercuration medium in the demercuration tower 10, the medium in the absorption tower 11 preferably adopts the MEA solution that adds activator and antioxidant, and active carbon or molecular sieve then are set in the dewater unit, can satisfy 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 cat head arranges overhead condenser 19, the interior setting of rectifying Tata is positioned at the reboiler 20 at the bottom of the tower, the nitrogen oxygen outlet that rectifying column 18 cats head arrange links to each other 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, is used for liquified natural gas and flows out.
Be filled with in the 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 the rectifying column 18, the back-fire relief explosion-suppressing material is for being laid on the back-fire relief silk screen 18b in the filler 18a at interval.The mesh size of the back-fire relief silk screen 18b of present embodiment is 80～200 orders, and the laying density of back-fire relief silk screen 18b is that every interval 300mm lays the 1-12 layer, and the laying density of the back-fire relief silk screen 18b of present embodiment is that every interval 300mm lays 5 layers.
The LNG storage system comprises liquefied methane storage tank 21, and the entrance of liquefied methane storage tank 21 links to each other with the condensate outlet of described rectifying column 19.The condensate outlet of the rectifying column 18 of 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.
Present embodiment combustion and explosion suppression type low concentration coal bed gas cryogenic liquefying device is used for storage raw material coal bed gas by the coal bed gas storage system is set, and also plays cushioning effect; By the sensor groups 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 the coal mine.
Be used for the cooling coal bed gas to design temperature and make methane liquefaction by coal gas gasification and piece-rate system are set, then liquefied methane is separated with nitrogen oxygen component, form the LNG product, and can satisfy the rectifying condition by setting in rectifying column 19, 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 microbody product units, the blast chain reaction is cut off, thereby prevents blast; Namely in the low concentration coal bed gas in the rectifying separation process, the methane in the 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 present embodiment can obtain high-recovery and high-purity methane from the low concentration coalbed methane containing oxygen under the situation of not deoxidation in advance.
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 that sets 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
1The back is converged with the gas phase azeotrope that refluxes, and the liquid phase azeotrope converges to reflux by first-class heat exchanger 1 with the gas phase azeotrope and enters azeotrope compressor 8, makes the azeotrope can be recycling.
The azeotrope of present embodiment is the mixture of nitrogen, methane, ethene, propane, isopentane, and is concrete, and the component of azeotrope is: 23.5% nitrogen; 38.8% methane; 11% ethene; 14.2% propane; 12.5% isopentane can satisfy the temperature control requirement in each link of producing at liquefied natural gas, certainly, azeotrope also can adopt the azeotrope of existing other components, the set of dispense of azeotrope can be set to difference than also, and its principle is suitable, is not repeated.
The nitrogen cycle system comprises choke valve V
3With the nitrogen compressor 25 that sets gradually along nitrogen flow of coolant direction, nitrogen cooler 26, the nitrogen of nitrogen cooler 26 exports 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, make the nitrogen can be recycling, 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, and the nitrogen oxygen outlet of decompressor 27 enters cleaning procedure by subcooler 17, three grades of heat exchangers 16, secondary heat exchanger 15 and first-class heat exchanger 14 after making the re-heat of nitrogen oxygen successively.By decompressor 27 is set, make its emptying at normal temperatures and pressures, thereby fully reclaim the energy of the nitrogen oxygen that backflows, reach the purpose of energy-saving and emission-reduction.
Concrete, adopt the method for 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 to be 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 ℃, continue the supercharging compression then, 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 demercuration, desulfurization, carbon dioxide removal and processed successively.In the 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 will purifying is cooled to-140 ℃～-160 ℃, and in the cooled coal gas layer, liquid mole fraction is no more than 15%, and the chilling temperature of coal bed gas is then 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 the coal bed gas is separated, liquefaction separates the methane liquid that obtains and enters the reboiler 20 that is arranged in 18 ends of rectifying column, make the nitrogen and the oxygen evaporation that contain in the methane liquid, liquefaction separates the nitrogen oxygen obtain and enters overhead condenser 19 coolings that are arranged in rectifying column 18 tops, is back in the rectifying column 18 after the methane liquefaction that contains in the nitrogen oxygen is separated.So, after coal bed gas rectifying separation circuit was handled, in the liquefied methane that obtains, methane content was 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 the liquefied methane that obtains be stored in the liquefied methane storage tank 21, liquefied methane storage tank 21 preferred bands force down warm primary and secondary jar.
By being that 25%～40% low concentration coalbed methane containing oxygen is stored in the gas holder 1 with 0.001MPa～0.005MPaG at normal temperatures with methane content, and by air inlet pipeline and the outlet pipe at gas holder initiatively explosion suppression device is set, can have explosion danger; In the coal bed gas compression section, the high pressure-charging pressure of control coal bed gas is 0.35～0.4MPaG, and maximum temperature is no more than 80 ℃, is in a safe condition, no explosion danger; In the coal bed gas purification process, coal bed gas pressure is 0.35～0.4MPaG, and temperature is normal temperature, no 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, methane content is not less than 25% in the gas phase of coal bed gas, and pressure is no more than 0.4MPaG, be safe condition, no explosion danger; In coal bed gas rectifying separation circuit, by being arranged on filler and the back-fire relief explosion-suppressing material that is provided for methane in the fractionation coal bed gas in the rectifying column 18 and has datonation-inhibition function, in coal bed gas rectifying separation circuit, extraction along with methane, methane content reduces gradually in the gas, up to the explosive range that enters 5%～15%, but, under the effect of back-fire relief explosion-suppressing material, can prevent blast, and the content of methane is lower than 0.5%, no explosion danger in the nitrogen oxygen of discharging, the methane content of the liquefied methane that obtains is more than 99%, no explosion danger; In liquefied methane storage operation, the methane content in the liquefied methane is constant, does not have the danger of blast.
To sum up, combustion and explosion suppression type low concentration coal bed gas cryogenic liquefying device of the present invention can be implemented in not under the situation of deoxidation in advance, obtains the methane of high-recovery from the low concentration coalbed methane containing oxygen, can effectively reduce equipment investment and enhances productivity.
Explanation is at last, above preferred embodiment is only unrestricted in order to technical scheme of the present invention to be described, although the present invention 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 claims of the present invention institute restricted portion.
Claims (9)
1. 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 be used for providing to described coal gas gasification and piece-rate system the cooling cycle system of cold, 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 coal bed gas compressibility comprises at least one group of supercharging compression unit of connecting mutually that sets gradually along the coal bed gas flow direction, and every group of described supercharging compression unit comprises coal bed gas compressor and coal bed gas cooler;
Described active explosion suppression device comprises controller, the sensor groups that links to each other with controller and the automatic explosion arrestment valve, automatic powder spraying explosion suppression device, the water seal back-fire relief explosion venting device that set gradually and all link to each other with controller along the coal bed gas flow direction, and described sensor groups 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 the 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 cat head arranges overhead condenser, the interior setting of rectifying Tata is positioned at the reboiler at the bottom of the tower, and the nitrogen oxygen outlet that described rectifying column cat head arranges links to each other 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 the 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 the described rectifying column, described back-fire relief explosion-suppressing material is for being laid on the back-fire relief silk screen in the described filler at interval.
2. combustion and explosion suppression type low concentration coal bed gas cryogenic liquefying device according to claim 1 is characterized in that:
Described coal bed gas storage system comprises gas holder;
Described coal bed gas cleaning system comprises demercuration tower, absorption tower and the dewater unit that sets gradually along the coal bed gas flow direction;
Described LNG storage system comprises the liquefied methane storage tank, and the entrance of described liquefied methane storage tank links to each other with the condensate outlet of described rectifying column.
3. 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 that sets 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 back is converged with the gas phase azeotrope that refluxes;
Described nitrogen cycle system comprises choke valve V
3With the nitrogen compressor that sets gradually along nitrogen flow of coolant direction, nitrogen cooler, the nitrogen of described nitrogen cooler exports 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.
4. combustion and explosion suppression type low concentration coal bed gas cryogenic liquefying device according to claim 3, 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, and the nitrogen oxygen outlet of described decompressor enters cleaning procedure by subcooler, three grades of heat exchangers, secondary heat exchanger and first-class heat exchanger after making the re-heat of nitrogen oxygen successively.
5. combustion and explosion suppression type low concentration coal bed gas cryogenic liquefying device according to claim 4, it is characterized in that: described azeotrope is the mixture of nitrogen, methane, ethene, propane, isopentane.
6. combustion and explosion suppression type according to claim 5 also is used for extracting the device of low concentration coalbed methane containing oxygen methane, and it is characterized in that: the component of described azeotrope is: 23.5% nitrogen; 38.8% methane; 11% ethene; 14.2% propane; 12.5% isopentane.
7. combustion and explosion suppression type low concentration coal bed gas cryogenic liquefying device according to claim 3, 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.
8. according to each described combustion and explosion suppression type low concentration coal bed gas cryogenic liquefying device of claim 1-7, it is characterized in that: the mesh size of back-fire relief silk screen is 80～200 orders.
9. combustion and explosion suppression type low concentration coal bed gas cryogenic liquefying device according to claim 8 is characterized in that: the laying density of described back-fire relief silk screen is that every interval 300mm lays the 1-12 layer.
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| CN201310228309.1A CN103256786B (en) | 2013-06-08 | 2013-06-08 | Combustion and explosion suppression type low concentration coal-bed gas cryogenic liquefying device |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105806040A (en) * | 2016-04-28 | 2016-07-27 | 北京中科瑞奥能源科技股份有限公司 | System and method for preparing liquefied natural gas through carbon black tail gas |
| CN107219255A (en) * | 2016-03-22 | 2017-09-29 | 中国石油化工股份有限公司 | Oxidation reactor fires risk assessment device |
| CN107219256A (en) * | 2016-03-22 | 2017-09-29 | 中国石油化工股份有限公司 | The appraisal procedure on oxidation reactor reaction temperature safety operation border |
| CN107219253A (en) * | 2016-03-22 | 2017-09-29 | 中国石油化工股份有限公司 | The appraisal procedure on oxidation reactor residence time safety operation border |
| CN107219254A (en) * | 2016-03-22 | 2017-09-29 | 中国石油化工股份有限公司 | The appraisal procedure of oxidation reactor highest combustible gas concentration |
| CN107219252A (en) * | 2016-03-22 | 2017-09-29 | 中国石油化工股份有限公司 | The appraisal procedure of oxidation reactor maximum pressure |
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Citations (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5232467A (en) * | 1992-06-18 | 1993-08-03 | Texaco Inc. | Process for producing dry, sulfur-free, CH4 -enriched synthesis or fuel gas |
| JPH09133430A (en) * | 1995-11-10 | 1997-05-20 | Ishikawajima Harima Heavy Ind Co Ltd | Air conditioner using lng plant equipment |
| CN1908559A (en) * | 2006-07-03 | 2007-02-07 | 北京科瑞赛斯气体液化技术有限公司 | Air-contained coal gas gasification and separation process and equipment |
| CN201199120Y (en) * | 2007-10-12 | 2009-02-25 | 北京国能时代能源科技发展有限公司 | Separated liquefaction equipment of air conditioner back heating type mine gas |
| CN201202974Y (en) * | 2008-05-28 | 2009-03-04 | 煤炭科学研究总院重庆研究院 | Low concentration mash gas safe conveying device |
| CN101591579A (en) * | 2009-05-13 | 2009-12-02 | 赵昱 | Method for deoxidizing and concentrating mine gas |
| CN101929788A (en) * | 2010-09-15 | 2010-12-29 | 中国科学院理化技术研究所 | Device for preparing liquefied natural gas by oxygen-bearing coal mine methane |
| CN203323490U (en) * | 2013-06-08 | 2013-12-04 | 中煤科工集团重庆研究院 | Burning and explosion-suppressing low-concentration coal-bed methane cryogenic liquefying device |
-
2013
- 2013-06-08 CN CN201310228309.1A patent/CN103256786B/en active Active
Patent Citations (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5232467A (en) * | 1992-06-18 | 1993-08-03 | Texaco Inc. | Process for producing dry, sulfur-free, CH4 -enriched synthesis or fuel gas |
| JPH09133430A (en) * | 1995-11-10 | 1997-05-20 | Ishikawajima Harima Heavy Ind Co Ltd | Air conditioner using lng plant equipment |
| CN1908559A (en) * | 2006-07-03 | 2007-02-07 | 北京科瑞赛斯气体液化技术有限公司 | Air-contained coal gas gasification and separation process and equipment |
| CN201199120Y (en) * | 2007-10-12 | 2009-02-25 | 北京国能时代能源科技发展有限公司 | Separated liquefaction equipment of air conditioner back heating type mine gas |
| CN201202974Y (en) * | 2008-05-28 | 2009-03-04 | 煤炭科学研究总院重庆研究院 | Low concentration mash gas safe conveying device |
| CN101591579A (en) * | 2009-05-13 | 2009-12-02 | 赵昱 | Method for deoxidizing and concentrating mine gas |
| CN101929788A (en) * | 2010-09-15 | 2010-12-29 | 中国科学院理化技术研究所 | Device for preparing liquefied natural gas by oxygen-bearing coal mine methane |
| CN203323490U (en) * | 2013-06-08 | 2013-12-04 | 中煤科工集团重庆研究院 | Burning and explosion-suppressing low-concentration coal-bed methane cryogenic liquefying device |
Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107219255A (en) * | 2016-03-22 | 2017-09-29 | 中国石油化工股份有限公司 | Oxidation reactor fires risk assessment device |
| CN107219256A (en) * | 2016-03-22 | 2017-09-29 | 中国石油化工股份有限公司 | The appraisal procedure on oxidation reactor reaction temperature safety operation border |
| CN107219253A (en) * | 2016-03-22 | 2017-09-29 | 中国石油化工股份有限公司 | The appraisal procedure on oxidation reactor residence time safety operation border |
| CN107219254A (en) * | 2016-03-22 | 2017-09-29 | 中国石油化工股份有限公司 | The appraisal procedure of oxidation reactor highest combustible gas concentration |
| CN107219252A (en) * | 2016-03-22 | 2017-09-29 | 中国石油化工股份有限公司 | The appraisal procedure of oxidation reactor maximum pressure |
| CN105806040A (en) * | 2016-04-28 | 2016-07-27 | 北京中科瑞奥能源科技股份有限公司 | System and method for preparing liquefied natural gas through carbon black tail gas |
| CN109002156A (en) * | 2018-10-11 | 2018-12-14 | 郑州云海信息技术有限公司 | A kind of novel closed-type phase-change type liquid cooled server system |
| CN109002156B (en) * | 2018-10-11 | 2023-09-15 | 郑州云海信息技术有限公司 | Novel closed phase-change liquid cooling server system |
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