CN101928617B - Gas-liquid separation device for oxygenous coal bed - Google Patents
Gas-liquid separation device for oxygenous coal bed Download PDFInfo
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- CN101928617B CN101928617B CN 201010282233 CN201010282233A CN101928617B CN 101928617 B CN101928617 B CN 101928617B CN 201010282233 CN201010282233 CN 201010282233 CN 201010282233 A CN201010282233 A CN 201010282233A CN 101928617 B CN101928617 B CN 101928617B
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Abstract
The invention discloses a gas-liquid separation device for an oxygenous coal bed, comprising a main process system and a refrigeration system, wherein the main process system comprises a first-stage heat exchanger, a second-stage heat exchanger, a third-stage heat exchanger and a rectification column which are orderly connected in series; and the refrigeration system comprises a mixed refrigerant balance pot, a refrigerant compressor, a refrigerant cooler, a refrigerant primary gas-liquid separator and a refrigerant secondary gas-liquid separator. The refrigeration device of the invention adopts mixed refrigeration and combines throttling refrigeration, changes the traditional refrigeration process, sufficiently and rationally utilizes the refrigeration capacity reclaiming process in the technological process, and improves the refrigeration efficiency, thereby relatively improving the processing capability of the device; for the coal bed gas with low single well output, the production cost can be saved; and only one set of compression equipment is utilized, so that the power energy is saved.
Description
Technical field
The present invention relates to a kind of device that utilizes the liquefaction principle to separate, relate 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 the elementary byproduct that pumps out; Its main component is methane, can find out from its component content, and coal-seam gas is the energy and the industrial chemicals of outbalance.But because its composition is comparatively complicated, particularly containing aerobic in coal-seam 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-seam gas generally enters atmosphere in the coal mining process, causes the profligacy of resource and to environment.
Along with the development of science and technology, the liquefaction technology of multiple coalbed methane containing oxygen has appearred.Wherein, the patent disclosure of ZL200610103425.0 cryogenic rectification method be applied to separation and the liquefaction of coalbed methane containing oxygen, have the separation purity height, the simple advantage of apparatus structure.
But this refrigeration techniques adopts the conventional refrigeration modes such as hybrid refrigeration or swell refrigeration, complex structure, and the auxiliary machinerys such as turbine expansion collection, refrigerating efficiency is lower, has reduced the processing power of separation and liquefying plant.
Therefore, need to the liquefying plant of existing coalbed methane containing oxygen be improved, change existing cooling flow, fully also reasonably utilize the cold recovery process in the technological process, improve refrigerating efficiency, thereby relatively improve the processing power of device, for the not high coal-seam gas of per-well production, can save production cost.
Summary of the invention
In view of this, the invention provides a kind of gas-liquid separation device for oxygenous coal bed, change existing cooling flow, fully also reasonably utilize the cold recovery process in the technological process, improve refrigerating efficiency, thereby relatively improve the processing power of device, for the not high coal-seam gas of per-well production, can save production cost.
A kind of gas-liquid separation device for oxygenous coal bed of the present invention 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 interchanger and rectifying tower, coalbed methane containing oxygen entrance after first-class heat exchanger is provided with and purifies, be positioned at the overhead condenser that the setting of rectifying tower cat head is communicated in rectifying tower top nitrogen oxygen outlet, at the bottom of being positioned at tower in the described rectifying tower reboiler is set, condensate outlet is set at the bottom of the rectifying tower;
Refrigeration system comprises the mix refrigerant surge tank, coolant compressor, refrigerant cooler, gas-liquid separator of refrigeration agent and refrigeration agent secondary gas-liquid separator, the coolant compressor entrance is communicated in the refrigeration agent surge tank, the coolant compressor outlet is communicated in gas-liquid separator of refrigeration agent by refrigerant cooler, gas-liquid separator pneumatic outlet of refrigeration agent is communicated in the secondary gas-liquid separator by first-class heat exchanger, secondary gas-liquid separator pneumatic outlet passes through secondary heat exchanger successively, reboiler, three grades of interchanger and a throttling valve III are communicated in overhead condenser, and the overhead condenser refrigerant outlet is successively through three grades of interchanger, secondary heat exchanger and first-class heat exchanger are communicated in the mix refrigerant surge tank recycles back flow of refrigerant;
Mix refrigerant comprises by mass percentage in the mix refrigerant surge tank: nitrogen 35%, methane 30.65%, ethene 16.81%, propane 3.8%, butane 8.17%, pentane 5.57%;
The liquid exit of a gas-liquid separator is communicated in backflow refrigerant through first-class heat exchanger and a throttling valve I successively between first-class heat exchanger and secondary heat exchanger; The liquid exit of secondary gas-liquid separator is communicated in backflow refrigerant through secondary heat exchanger and a throttling valve II successively between secondary heat exchanger and three grades of interchanger;
Described first-class heat exchanger, secondary heat exchanger, three grades of interchanger, reboiler and overhead condensers are the dividing wall type structure that runner is set according to the medium kind.
Further, rectifying tower cat head nitrogen oxygen outlet is communicated in the overhead gas liquid/gas separator through overhead condenser, and overhead gas liquid/gas separator nitrogen oxygen outlet is exported nitrogen oxygen through a finished product water cooler, three grades of interchanger, secondary heat exchanger and first-class heat exchanger successively; Overhead gas liquid/gas separator liquid exit is communicated in rectifying tower; Condensate outlet at the bottom of the described rectifying tower is communicated in the finished product water cooler; Described finished product water cooler is the dividing wall type structure;
Further, in the main flow system, between three grades of interchanger and the rectifying tower throttling valve IV is set;
Further, described coolant compressor is three grades of compressions.
Beneficial effect of the present invention is: the gas-liquid separation device for oxygenous coal bed of structure of the present invention, refrigeration plant adopts hybrid refrigeration and in conjunction with throttling refrigeration, change existing cooling flow, fully also reasonably utilize the cold recovery process in the technological process, improve refrigerating efficiency, thereby relatively improve the processing power of device, for the not high coal-seam gas of per-well production, can save production cost, only utilize a cover compression equipment, save power source.
Description of drawings
The present invention is further detailed explanation below in conjunction with the drawings and specific embodiments.
Accompanying drawing is structural representation of the present invention.
Embodiment
Accompanying drawing is structural representation of the present invention, 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 first-class heat exchanger 1, the secondary heat exchanger 2 of serial connection successively, three grades of interchanger 3 and rectifying tower 5, coalbed methane containing oxygen entrance after first-class heat exchanger 1 arranges and purifies, be positioned at the overhead condenser 8 that rectifying tower 5 cat head settings are communicated in rectifying tower top nitrogen oxygen outlet, at the bottom of being positioned at tower in described rectifying tower 5 towers reboiler 6 is set, at the bottom of rectifying tower 5 towers condensate outlet is set;
Refrigeration system comprises mix refrigerant surge tank 10, coolant compressor 11, refrigerant cooler 12, gas-liquid separator 13 of refrigeration agent and refrigeration agent secondary gas-liquid separator 15, coolant compressor 11 entrances are communicated in refrigeration agent surge tank 10, coolant compressor 11 outlets are communicated in gas-liquid separator 13 of refrigeration agent by refrigerant cooler 12, gas-liquid separator 13 pneumatic outlets of refrigeration agent are communicated in secondary gas-liquid separator 15 by first-class heat exchanger 1, secondary gas-liquid separator 15 pneumatic outlets pass through secondary heat exchanger 2 successively, reboiler 6, three grades of interchanger 3 and a throttling valve III 17 are communicated in overhead condenser 8, and overhead condenser 8 refrigerant outlets are successively through three grades of interchanger 3, secondary heat exchanger 2 and first-class heat exchanger 1 are communicated in mix refrigerant surge tank 10 recycles back flow of refrigerant;
Mix refrigerant surge tank 10 interior mix refrigerants comprise by mass percentage: 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 links, the rationally temperature index in the control flow in this proportioning energy properly distributed refrigeration agent;
The liquid exit of a gas-liquid separator 13 is communicated in backflow refrigerant through first-class heat exchanger 1 and a throttling valve I 14 successively between first-class heat exchanger 1 and secondary heat exchanger 2; The liquid exit of secondary gas-liquid separator 15 is communicated in backflow refrigerant through secondary heat exchanger 2 and a throttling valve II 16 successively between secondary heat exchanger 2 and three grades of interchanger 3;
Described first-class heat exchanger 1, secondary heat exchanger 2, three grades of interchanger 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, rectifying tower 5 cat head nitrogen oxygen outlets are communicated in overhead gas liquid/gas separator 9 through overhead condenser 8, and overhead gas liquid/gas separator 9 nitrogen oxygen outlets are exported nitrogen oxygen through a finished product water cooler 7, three grades of interchanger 3, secondary heat exchanger 2 and first-class heat exchanger 1 successively; Overhead gas liquid/gas separator 9 liquid exits are communicated in rectifying tower 5, are used for phlegma and are back to rectifying tower; Condensate outlet at the bottom of described rectifying tower 5 towers is communicated in finished product water cooler 7; Described finished product water cooler 7 is the dividing wall type structure; Cross cold product and reclaim cold by three grades of interchanger 3, secondary heat exchanger 2 and first-class heat exchanger 1 by finished product water cooler 7, take full advantage of the cold of cryogenic nitrogen oxygen, further improve cooling efficiency.
In the present embodiment, in the main flow system, between three grades of interchanger 3 and the rectifying tower 5 throttling valve IV 4 is set; By reducing pressure by regulating flow, further reduce temperature, be beneficial to condensation and separation.
In the present embodiment, described coolant compressor 11 is three grades of compressions, and inter-stage all arranges cooling and gas-liquid separator, reduces the single-stage compression ratio of pressurized gas, and the temperature of single-stage outlet, thereby reduces energy consumption.
The present invention comprises when producing:
A. main flow technique: will purify coalbed methane containing oxygen successively by first-class heat exchanger, secondary heat exchanger and three grades of interchanger coolings,, form the mixture of phlegma and gas, go out interchanger and purify coalbed methane containing oxygen and enter rectifying tower after through 17 throttlings of throttling valve III; Obtain natural gas liquids at the bottom of the rectifying tower, the residue phlegma is gone out after the cooling of finished product water cooler to be the finished product natural gas liquids by tower bottom flow; Cat head obtains N
2And O
2Gas mixture also contains a small amount of CH
4Enter overhead condenser 8;
The N that flow out on rectifying tower 5 tops
2And O
2Enter overhead condenser 8 and separate out a small amount of CH that carries out
4Component, have overhead gas liquid/gas separator 9 to carry out gas-liquid separation after, liquid state is CH
4Be back to tower by rectifying tower 5 tops; Separate liquid CH
4Rear N
2And O
2Temperature is to export as tail gas behind the cold by reclaiming by three grades of interchanger 3, secondary heat exchanger 2 and first-class heat exchanger 1 successively behind out the natural gas liquids at the bottom of the finished product water cooler 7 cooling rectifying tower.
B. refrigeration techniques:
B1. the mix refrigerant of refrigeration agent surge tank 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 tower, after self is cooled behind the phlegma at the bottom of the heating tower, enter 3 coolings of three grades of interchanger, enter again three grades of interchanger coolings after being introduced into the tower bottom reboiler cooling, can reduce the load of three grades of interchanger, guarantee the cooling performance of unstripped gas, heat simultaneously phlegma at the bottom of the tower, improved rectifying and refrigerating efficiency, relatively improved the processing power of device; 3 coolings of three grades of interchanger enter N2 and O2 and a small amount of CH4 component of the outlet of overhead condenser 6 cooling tower tops by cooling behind the reducing pressure by regulating flow, successively through the gradually heat exchange and be back to the compression entrance and recycle of three grades of interchanger 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 throttling 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 interchanger 3 after the step-down after 16 throttlings of throttling valve II; Thereby reduce the purpose that pressure reaches evaporative cooling by throttling, do not need extra equipment and power, save energy reduces equipment and takes up an area to drop into.
Explanation is at last, above embodiment is only unrestricted in order to technical scheme of the present invention to be described, although with reference to preferred embodiment the present invention is had been described in detail, those of ordinary skill in the art is to be understood that, can make amendment or be equal to replacement technical scheme of the present invention, and not breaking away from aim and the scope of the technical program, it all should be encompassed in the middle of the claim scope of the present invention.
Claims (3)
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 interchanger and rectifying tower, coalbed methane containing oxygen entrance after first-class heat exchanger is provided with and purifies, be positioned at the overhead condenser that the setting of rectifying tower cat head is communicated in rectifying tower top nitrogen oxygen outlet, at the bottom of being positioned at tower in the described rectifying tower reboiler is set, condensate outlet is set at the bottom of the rectifying tower;
Refrigeration system comprises the mix refrigerant surge tank, coolant compressor, refrigerant cooler, gas-liquid separator of refrigeration agent and refrigeration agent secondary gas-liquid separator, the coolant compressor entrance is communicated in the refrigeration agent surge tank, the coolant compressor outlet is communicated in gas-liquid separator of refrigeration agent by refrigerant cooler, gas-liquid separator pneumatic outlet of refrigeration agent is communicated in the secondary gas-liquid separator by first-class heat exchanger, secondary gas-liquid separator pneumatic outlet passes through secondary heat exchanger successively, reboiler, three grades of interchanger and a throttling valve III are communicated in overhead condenser, the overhead condenser refrigerant outlet is successively through three grades of interchanger, secondary heat exchanger and first-class heat exchanger are communicated in the mix refrigerant surge tank recycles back flow of refrigerant, and described coolant compressor is three grades of compressions;
Mix refrigerant comprises by mass percentage in the mix refrigerant surge tank: nitrogen 35%, methane 30.65%, ethene 16.81%, propane 3.8%, butane 8.17%, pentane 5.57%;
The liquid exit of a gas-liquid separator is communicated in backflow refrigerant through first-class heat exchanger and a throttling valve I successively between first-class heat exchanger and secondary heat exchanger; The liquid exit of secondary gas-liquid separator is communicated in backflow refrigerant through secondary heat exchanger and a throttling valve II successively between secondary heat exchanger and three grades of interchanger;
Described first-class heat exchanger, secondary heat exchanger, three grades of interchanger, 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 tower cat head nitrogen oxygen outlet is communicated in the overhead gas liquid/gas separator through overhead condenser, and overhead gas liquid/gas separator nitrogen oxygen outlet is exported nitrogen oxygen through a finished product water cooler, three grades of interchanger, secondary heat exchanger and first-class heat exchanger successively; Overhead gas liquid/gas separator liquid exit is communicated in rectifying tower; Condensate outlet at the bottom of the described rectifying tower is communicated in the finished product water cooler; Described finished product water cooler is the dividing wall type structure.
3. gas-liquid separation device for oxygenous coal bed according to claim 1 is characterized in that: in the main flow system, between three grades of interchanger and the rectifying tower throttling valve IV is set.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 201010282233 CN101928617B (en) | 2010-09-15 | 2010-09-15 | Gas-liquid separation device for oxygenous coal bed |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 201010282233 CN101928617B (en) | 2010-09-15 | 2010-09-15 | Gas-liquid separation device for oxygenous coal bed |
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| CN101928617A CN101928617A (en) | 2010-12-29 |
| CN101928617B true CN101928617B (en) | 2013-03-20 |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN103361138B (en) * | 2013-07-24 | 2015-02-18 | 开封黄河空分集团有限公司 | Method for preparing liquefied natural gas and synthesis ammonia raw material gases by use of hydrogen extraction desorption gas |
| CN109210867B (en) * | 2018-08-28 | 2021-03-19 | 中国科学院理化技术研究所 | System for retrieve methane in follow oxygen-bearing coal bed gas |
| CN109439375A (en) * | 2018-10-25 | 2019-03-08 | 杨昌玮 | A kind of method of heat exchange type purification and liquefaction coalbed or coal mine gas |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1572863A (en) * | 2003-05-22 | 2005-02-02 | 气体产品与化学公司 | Nitrogen rejection from condensed natural gas |
| CN201212765Y (en) * | 2008-06-05 | 2009-03-25 | 北京国能时代能源科技发展有限公司 | Liquefaction separation device for chemical industrial exhaust |
| CN201503189U (en) * | 2009-08-26 | 2010-06-09 | 四川空分设备(集团)有限责任公司 | Refrigeration system and liquefaction system of natural gas liquefaction process |
| CN201844655U (en) * | 2010-09-15 | 2011-05-25 | 煤炭科学研究总院重庆研究院 | Oxygen-containing coal bed methane liquefaction separation device |
Family Cites Families (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2008081018A2 (en) * | 2007-01-04 | 2008-07-10 | Shell Internationale Research Maatschappij B.V. | Method and apparatus for liquefying a hydrocarbon stream |
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Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1572863A (en) * | 2003-05-22 | 2005-02-02 | 气体产品与化学公司 | Nitrogen rejection from condensed natural gas |
| CN201212765Y (en) * | 2008-06-05 | 2009-03-25 | 北京国能时代能源科技发展有限公司 | Liquefaction separation device for chemical industrial exhaust |
| CN201503189U (en) * | 2009-08-26 | 2010-06-09 | 四川空分设备(集团)有限责任公司 | Refrigeration system and liquefaction system of natural gas liquefaction process |
| CN201844655U (en) * | 2010-09-15 | 2011-05-25 | 煤炭科学研究总院重庆研究院 | Oxygen-containing coal bed methane liquefaction separation device |
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| CN101928617A (en) | 2010-12-29 |
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