CN201844655U - Oxygen-containing coal bed methane liquefaction separation device - Google Patents
Oxygen-containing coal bed methane liquefaction separation device Download PDFInfo
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- CN201844655U CN201844655U CN 201020529946 CN201020529946U CN201844655U CN 201844655 U CN201844655 U CN 201844655U CN 201020529946 CN201020529946 CN 201020529946 CN 201020529946 U CN201020529946 U CN 201020529946U CN 201844655 U CN201844655 U CN 201844655U
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Abstract
The utility model discloses an oxygen-containing coal bed methane liquefaction separation device, which comprises a main process system and a refrigeration system. The main process system comprises a primary heat exchanger, a secondary heat exchanger, a tertiary heat exchanger and a rectification column which are sequentially connected in series. The refrigeration system comprises a mixed refrigerant balance tank, a refrigerant compressor, a refrigerant cooler, a refrigerant primary gas-liquid separator and a refrigerant secondary gas-liquid separator. A refrigeration device adopts a mode of combining mixed refrigeration with throttling refrigeration. The oxygen-containing coal bed methane liquefaction separation device changes the existing refrigeration process, sufficiently and reasonably utilizes the cold quantity recovery process and improves the refrigeration efficiency so as to relatively improve the treatment capacity of the device. For coal bed methane with a low well producing rate, the oxygen-containing coal bed methane liquefaction separation device can save the production cost, only utilizes a set of compression equipment and saves power energy.
Description
Technical field
The utility model relates to a kind of device that utilizes the liquefaction principle to separate, and relates in particular to a kind of gas-liquid separation device for oxygenous coal bed.
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 a 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 containing aerobic in coal bed gas, is breakneck combustion-supporting pro-knock agent, has 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.
Along with science and technology development, the liquefaction technology of multiple coalbed methane containing oxygen has appearred.Wherein, the patent disclosure of ZL200610103425.0 cryogenic rectification method be applied to the separation and the liquefaction of coalbed methane containing oxygen, have the separation purity height, the simple advantage of apparatus structure.
But this refrigeration process adopts conventional refrigeration modes such as hybrid refrigeration or swell refrigeration, complex structure, and Aided Machines such as turbine expansion collection, refrigerating efficiency is lower, has reduced the disposal ability of separation and liquefying plant.
Therefore, need the liquefying plant of existing coalbed methane containing oxygen be improved, change existing cooling flow, cold recovery process in the abundant also reasonable use technical process, improve refrigerating efficiency, thereby improve the disposal ability of device relatively, for the not high coal bed gas of well yield, can save production cost.
The utility model content
In view of this, the utility model provides a kind of gas-liquid separation device for oxygenous coal bed, change existing cooling flow, cold recovery process in the abundant also reasonable use technical process, improve refrigerating efficiency, thereby improve the disposal ability of device relatively, for the not high coal bed gas of well yield, can save production cost.
A kind of gas-liquid separation device for oxygenous coal bed of the present utility model comprises main flow system and refrigeration system;
Described main flow system comprises first-class heat exchanger, the secondary heat exchanger of serial connection successively, three grades of heat exchangers and rectifying column, first-class heat exchanger is provided with and purifies back coalbed methane containing oxygen inlet, be positioned at the overhead condenser that the setting of rectifying column cat head is communicated in rectifying tower top nitrogen oxygen outlet, at the bottom of being positioned at tower in the described rectifying Tata reboiler is set, at the bottom of the rectifying Tata condensate outlet is set;
Refrigeration system comprises the mix refrigerant compensator, coolant compressor, refrigerant cooler, gas-liquid separator of cold-producing medium and cold-producing medium secondary gas-liquid separator, the coolant compressor inlet is communicated in the cold-producing medium compensator, the refrigerator compressor outlet is communicated in gas-liquid separator of cold-producing medium by refrigerant cooler, gas-liquid separator gas vent of cold-producing medium is communicated in the secondary gas-liquid separator by first-class heat exchanger, secondary gas-liquid separator gas vent passes through secondary heat exchanger successively, reboiler, three grades of heat exchangers and a choke valve III are communicated in overhead condenser, and the overhead condenser refrigerant outlet is successively through three grades of heat exchangers, secondary heat exchanger and first-class heat exchanger are communicated in the mix refrigerant compensator recycles back flow of refrigerant;
The liquid outlet of a gas-liquid separator is communicated in backflow refrigerant through a first-class heat exchanger and a choke valve I successively between first-class heat exchanger and secondary heat exchanger; The liquid outlet of secondary gas-liquid separator is communicated in backflow refrigerant through a secondary heat exchanger and a choke valve II successively between secondary heat exchanger and three grades of heat exchangers;
Described one-level cooler, secondary coolers, three grades of coolers, reboiler and overhead condensers are the dividing wall type structure that runner is set according to the medium kind.
Further, rectifying column cat head nitrogen oxygen outlet is communicated in the tower overhead gas liquid/gas separator through overhead condenser, and tower overhead gas liquid/gas separator nitrogen oxygen outlet is exported nitrogen oxygen through a finished product cooler, three grades of heat exchangers, secondary heat exchanger and first-class heat exchanger successively; Tower overhead gas liquid/gas separator liquid outlet is communicated in rectifying column; Condensate outlet at the bottom of the described rectifying Tata is communicated in the finished product cooler; Described finished product cooler is the dividing wall type structure;
Further, in the main flow system, between three grades of heat exchangers and the rectifying column choke valve IV is set;
Further, described refrigerator compressor is three grades of compressions.
The beneficial effects of the utility model are: the gas-liquid separation device for oxygenous coal bed of the utility model structure, refrigerating plant adopts hybrid refrigeration and in conjunction with throttling refrigeration, change existing cooling flow, fully also the cold recovery process in the reasonable use technical process improves refrigerating efficiency, thereby improves the disposal ability of device relatively, for the not high coal bed gas of well yield, can save production cost, only utilize a cover compression equipment, save power source.
Description of drawings
Below in conjunction with the drawings and specific embodiments the utility model is described in further detail.
Accompanying drawing is the utility model structural representation.
The specific embodiment
Accompanying drawing is the utility model structural representation, and as shown in the figure: the gas-liquid separation device for oxygenous coal bed of present embodiment comprises main flow system and refrigeration system;
Described main flow system comprises the first-class heat exchanger 1, secondary heat exchanger 2 of serial connection successively, three grades of heat exchangers 4 and rectifying columns 5, first-class heat exchanger 1 is provided with and purifies back coalbed methane containing oxygen inlet, be positioned at the overhead condenser 8 that rectifying column 5 cat head settings are communicated in rectifying tower top nitrogen oxygen outlet, at the bottom of being positioned at tower in described rectifying column 5 towers reboiler 6 is set, at the bottom of rectifying column 5 towers condensate outlet is set;
Refrigeration system comprises mix refrigerant compensator 10, coolant compressor 11, refrigerant cooler 12, gas-liquid separator 13 of cold-producing medium and cold-producing medium secondary gas-liquid separator 15, coolant compressor 11 inlets are communicated in cold-producing medium compensator 10, refrigerator compressor 11 outlets are communicated in gas-liquid separator 13 of cold-producing medium by refrigerant cooler 12, gas-liquid separator 13 gas vents of cold-producing medium are communicated in secondary gas-liquid separator 15 by first-class heat exchanger 1, secondary gas-liquid separator 15 gas vents pass through secondary heat exchanger 2 successively, reboiler 6, three grades of heat exchangers 3 and a choke valve III 17 are communicated in overhead condenser 8, and overhead condenser 8 refrigerant outlets are successively through three grades of heat exchangers 3, secondary heat exchanger 2 and first-class heat exchanger 1 are communicated in mix refrigerant compensator 10 recycles back flow of refrigerant;
The liquid outlet of a gas-liquid separator 13 is communicated in backflow refrigerant through a first-class heat exchanger 1 and a choke valve I 14 successively between first-class heat exchanger 1 and secondary heat exchanger 2; The liquid outlet of secondary gas-liquid separator 15 is communicated in backflow refrigerant through a secondary heat exchanger 2 and a choke valve II 16 successively between secondary heat exchanger 2 and three grades of heat exchangers 3;
Described one-level cooler 1, secondary coolers 2, three grades of coolers 3, reboiler 6 and overhead condensers 8 are the dividing wall type structure that runner is set according to the medium kind; Each by fully independent between the medium and can be mutually between heat-shift.
In the present embodiment, mix refrigerant comprises by mass percentage in the mix refrigerant compensator 10: nitrogen 35%, methane 30.65%, ethene 16.81%, propane 3.8%, butane 8.17% pentane 5.57%; Each composition is at the gas-liquid composition of each link, the rationally temperature index in the control flow in this proportioning energy reasonable distribution cold-producing medium.
In the present embodiment, rectifying column 5 cat head nitrogen oxygen outlets are communicated in tower overhead gas liquid/gas separator 9 through overhead condenser 8, and tower overhead gas liquid/gas separator 9 nitrogen oxygen outlets are exported nitrogen oxygen through a finished product cooler 7, three grades of heat exchangers 3, secondary heat exchanger 2 and first-class heat exchanger 1 successively; Tower overhead gas liquid/gas separator 9 liquid outlets are communicated in rectifying column 5, are used for condensate liquid and are back to rectifying column; Condensate outlet at the bottom of described rectifying column 5 towers is communicated in finished product cooler 7; Described finished product cooler 7 is the dividing wall type structure; Cross cold product and reclaim cold by finished product cooler 7, make full use of the cold of cryogenic nitrogen oxygen, further improve cooling effectiveness by three grades of heat exchangers 3, secondary heat exchanger 2 and first-class heat exchanger 1.
In the present embodiment, in the main flow system, between three grades of heat exchangers 3 and the rectifying column 5 choke valve IV 4 is set; By the throttling step-down, further reduce temperature, be beneficial to condensation and separation.
In the present embodiment, described refrigerator compressor 11 is three grades of compressions, and inter-stage all is provided with cooling and gas-liquid separator, reduces the single stage compress ratio of Compressed Gas, and the temperature of single-stage outlet, thereby cuts down the consumption of energy.
The utility model comprises when producing:
A. main flow technology: will purify coalbed methane containing oxygen successively by first-class heat exchanger, secondary heat exchanger and three grades of heat exchangers coolings,, form the mixture of condensate liquid and gas, go out heat exchanger and purify coalbed methane containing oxygen and enter rectifying column after through 17 throttlings of choke valve III; Obtain liquefied natural gas at the bottom of the rectifying Tata, the residue condensate liquid is gone out after the cooling of finished product cooler to be the finished product liquefied natural gas by tower bottom flow; Cat head obtains N
2And O
2Gaseous mixture also contains a small amount of CH
4Enter overhead condenser 8;
The N that flow out on rectifying column 5 tops
2And O
2Enter overhead condenser 8 and separate out a small amount of CH that carries out
4Component, have tower overhead gas liquid/gas separator 9 to carry out gas-liquid separation after, liquid state is CH
4Be back to tower by rectifying column 5 tops; Separate liquid CH
4Back N
2And O
2By temperature after reclaiming cold by three grades of heat exchangers 3, secondary heat exchanger 2 and first-class heat exchanger 1 successively behind the liquefied natural gas that comes out at the bottom of the finished product cooler 7 cooling rectifying columns for to export as tail gas.
B. refrigeration process:
B1. the mix refrigerant of cold-producing medium compensator 10 is through coolant compressor 11 compressions, refrigerant cooler 12 coolings; After 13 gas-liquid separations of a gas-liquid separator, gaseous state enters the first-class heat exchanger cooling, after entering the 15 secondary gas-liquid separations of secondary gas-liquid separator, gaseous state enters the reboiler 6 that enters after the secondary heat exchanger cooling at the bottom of the rectifying column, after self is cooled behind the condensate liquid at the bottom of the heating tower, enter 3 coolings of three grades of heat exchangers, enter three grades of heat exchanger coolings again after being introduced into the tower bottom reboiler cooling, can reduce the load of three grades of heat exchangers, guarantee the cooling effect of unstripped gas, heat condensate liquid at the bottom of the tower simultaneously, improved rectifying and refrigerating efficiency, improved the disposal ability of device relatively; Three grades of heat exchanger 3 coolings enter the N of overhead condenser 6 cooling tower top outlets after lower the temperature after the throttling step-down
2And O
2And a small amount of CH
4Component is successively through the heat exchange and be back to compression inlet and recycle gradually of three grades of heat exchangers 6, secondary heat exchanger 2 and first-class heat exchanger 1;
B2. the liquid after the gas-liquid separation enters first-class heat exchanger 1 cooling and refluxes through entering backflow refrigerant between by first-class heat exchanger and secondary heat exchanger after 14 throttlings of choke valve I; Liquid after the secondary gas-liquid separation enters secondary heat exchanger 2 cooling, refluxes through entering backflow refrigerant between by secondary heat exchanger 2 and three grades of heat exchangers 3 after the step-down after 16 throttlings of choke valve II; Thereby reduce the purpose that pressure reaches evaporative cooling by throttling, do not need extra equipment and power, energy savings reduces equipment and takes up an area of to drop into.
Explanation is at last, above embodiment is only unrestricted in order to the explanation the technical solution of the utility model, although the utility model is had been described in detail with reference to preferred embodiment, those of ordinary skill in the art is to be understood that, can make amendment or be equal to replacement the technical solution of the utility model, and not breaking away from the aim and the scope of the technical program, it all should be encompassed in the middle of the claim scope of the present utility model.
Claims (4)
1. a gas-liquid separation device for oxygenous coal bed is characterized in that: comprise main flow system and refrigeration system;
Described main flow system comprises first-class heat exchanger, the secondary heat exchanger of serial connection successively, three grades of heat exchangers and rectifying column, first-class heat exchanger is provided with and purifies back coalbed methane containing oxygen inlet, be positioned at the overhead condenser that the setting of rectifying column cat head is communicated in rectifying tower top nitrogen oxygen outlet, at the bottom of being positioned at tower in the described rectifying Tata reboiler is set, at the bottom of the rectifying Tata condensate outlet is set;
Refrigeration system comprises the mix refrigerant compensator, coolant compressor, refrigerant cooler, gas-liquid separator of cold-producing medium and cold-producing medium secondary gas-liquid separator, the coolant compressor inlet is communicated in the cold-producing medium compensator, the refrigerator compressor outlet is communicated in gas-liquid separator of cold-producing medium by refrigerant cooler, gas-liquid separator gas vent of cold-producing medium is communicated in the secondary gas-liquid separator by first-class heat exchanger, secondary gas-liquid separator gas vent passes through secondary heat exchanger successively, reboiler, three grades of heat exchangers and a choke valve III are communicated in overhead condenser, and the overhead condenser refrigerant outlet is successively through three grades of heat exchangers, secondary heat exchanger and first-class heat exchanger are communicated in the mix refrigerant compensator recycles back flow of refrigerant;
The liquid outlet of a gas-liquid separator is communicated in backflow refrigerant through a first-class heat exchanger and a choke valve I successively between first-class heat exchanger and secondary heat exchanger; The liquid outlet of secondary gas-liquid separator is communicated in backflow refrigerant through a secondary heat exchanger and a choke valve II successively between secondary heat exchanger and three grades of heat exchangers;
Described one-level cooler, secondary coolers, three grades of coolers, reboiler and overhead condensers are the dividing wall type structure that runner is set according to the medium kind.
2. gas-liquid separation device for oxygenous coal bed according to claim 1, it is characterized in that: rectifying column cat head nitrogen oxygen outlet is communicated in the tower overhead gas liquid/gas separator through overhead condenser, and tower overhead gas liquid/gas separator nitrogen oxygen outlet is exported nitrogen oxygen through a finished product cooler, three grades of heat exchangers, secondary heat exchanger and first-class heat exchanger successively; Tower overhead gas liquid/gas separator liquid outlet is communicated in rectifying column; Condensate outlet at the bottom of the described rectifying Tata is communicated in the finished product cooler; Described finished product cooler is the dividing wall type structure.
3. gas-liquid separation device for oxygenous coal bed according to claim 2 is characterized in that: in the main flow system, between three grades of heat exchangers and the rectifying column choke valve IV is set.
4. gas-liquid separation device for oxygenous coal bed according to claim 3 is characterized in that: described refrigerator compressor is three grades of compressions.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 201020529946 CN201844655U (en) | 2010-09-15 | 2010-09-15 | Oxygen-containing coal bed methane liquefaction separation device |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 201020529946 CN201844655U (en) | 2010-09-15 | 2010-09-15 | Oxygen-containing coal bed methane liquefaction separation device |
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| Publication Number | Publication Date |
|---|---|
| CN201844655U true CN201844655U (en) | 2011-05-25 |
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| CN 201020529946 Expired - Fee Related CN201844655U (en) | 2010-09-15 | 2010-09-15 | Oxygen-containing coal bed methane liquefaction separation device |
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101928617A (en) * | 2010-09-15 | 2010-12-29 | 中国科学院理化技术研究所 | Gas-liquid separation device for oxygenous coal bed |
| CN102374754A (en) * | 2011-09-24 | 2012-03-14 | 辽宁哈深冷气体液化设备有限公司 | Equipment and method for preparing liquid natural gas and carbon oxide from coke oven gas |
| CN104130812A (en) * | 2013-05-02 | 2014-11-05 | 中国石油天然气股份有限公司 | Constant-temperature dew-point controlling skid-mounted device specially used for coalbed methane and based on methanol gas-state recovery |
| CN117072268A (en) * | 2023-10-12 | 2023-11-17 | 浙江博旭新能源科技有限公司 | Comprehensive utilization energy storage system and method for LNG cold energy and compressor inter-stage cooling water |
-
2010
- 2010-09-15 CN CN 201020529946 patent/CN201844655U/en not_active Expired - Fee Related
Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101928617A (en) * | 2010-09-15 | 2010-12-29 | 中国科学院理化技术研究所 | Gas-liquid separation device for oxygenous coal bed |
| CN101928617B (en) * | 2010-09-15 | 2013-03-20 | 中国科学院理化技术研究所 | Gas-liquid separation device for oxygenous coal bed |
| CN102374754A (en) * | 2011-09-24 | 2012-03-14 | 辽宁哈深冷气体液化设备有限公司 | Equipment and method for preparing liquid natural gas and carbon oxide from coke oven gas |
| CN102374754B (en) * | 2011-09-24 | 2015-08-19 | 辽宁哈深冷气体液化设备有限公司 | The Apparatus and method for of liquified natural gas and carbon monoxide is produced from coke-stove gas |
| CN104130812A (en) * | 2013-05-02 | 2014-11-05 | 中国石油天然气股份有限公司 | Constant-temperature dew-point controlling skid-mounted device specially used for coalbed methane and based on methanol gas-state recovery |
| CN104130812B (en) * | 2013-05-02 | 2016-03-09 | 中国石油天然气股份有限公司 | The constant temperature dew-point control sled assembling device reclaimed based on methyl alcohol gaseous state that coal-seam gas is special |
| CN117072268A (en) * | 2023-10-12 | 2023-11-17 | 浙江博旭新能源科技有限公司 | Comprehensive utilization energy storage system and method for LNG cold energy and compressor inter-stage cooling water |
| CN117072268B (en) * | 2023-10-12 | 2024-01-19 | 浙江博旭新能源科技有限公司 | Comprehensive utilization energy storage system and method for LNG cold energy and compressor inter-stage cooling water |
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Legal Events
| Date | Code | Title | Description |
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| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| C56 | Change in the name or address of the patentee |
Owner name: CHINA COAL TECHNOLOGY ENGINEERING GROUP CHONGQING Free format text: FORMER NAME: CHINA COAL SCIENCE AND INDUSTRY GROUP CHONGQING RESEARCH INSTITUTE Owner name: CHINA COAL SCIENCE AND INDUSTRY GROUP CHONGQING RE Free format text: FORMER NAME: COAL SCIENTIFIC RESEARCH INSTITUTE CHONGQING INSTITUTE |
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| CP01 | Change in the name or title of a patent holder |
Address after: 400037, No. three village, 55 bridge, Shapingba District, Chongqing Patentee after: Chongqing Research Institute of China Coal Technology & Engineering Group Corp. Address before: 400037, No. three village, 55 bridge, Shapingba District, Chongqing Patentee before: Chongqing Institute of Coal Science Research Institute |
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| CP03 | Change of name, title or address |
Address after: 400039 Chongqing Jiulongpo Branch City Road No. 6 Patentee after: CHONGQING RESEARCH INSTITUTE CO., LTD. OF CHINA COAL TECHNOLOGY & ENGINEERING Group Address before: 400037, No. three village, 55 bridge, Shapingba District, Chongqing Patentee before: Chongqing Research Institute of China Coal Technology & Engineering Group Corp. |
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| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20110525 Termination date: 20160915 |
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| CF01 | Termination of patent right due to non-payment of annual fee |