CN1952569A - Process and equipment for liquefying air-containing coal-bed gas - Google Patents
Process and equipment for liquefying air-containing coal-bed gas Download PDFInfo
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- CN1952569A CN1952569A CNA2006100808894A CN200610080889A CN1952569A CN 1952569 A CN1952569 A CN 1952569A CN A2006100808894 A CNA2006100808894 A CN A2006100808894A CN 200610080889 A CN200610080889 A CN 200610080889A CN 1952569 A CN1952569 A CN 1952569A
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- 238000000034 method Methods 0.000 title claims abstract description 28
- 239000007789 gas Substances 0.000 claims abstract description 113
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims abstract description 89
- 238000005057 refrigeration Methods 0.000 claims abstract description 60
- 238000000926 separation method Methods 0.000 claims abstract description 36
- 238000007906 compression Methods 0.000 claims abstract description 14
- 230000006835 compression Effects 0.000 claims abstract description 12
- 238000000746 purification Methods 0.000 claims abstract description 6
- 238000005194 fractionation Methods 0.000 claims description 28
- 239000007788 liquid Substances 0.000 claims description 25
- 238000001816 cooling Methods 0.000 claims description 10
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 8
- 239000001301 oxygen Substances 0.000 claims description 8
- 229910052760 oxygen Inorganic materials 0.000 claims description 8
- 239000003507 refrigerant Substances 0.000 claims description 7
- 238000004821 distillation Methods 0.000 claims description 3
- 238000010438 heat treatment Methods 0.000 claims description 3
- 239000012535 impurity Substances 0.000 claims description 2
- 239000002994 raw material Substances 0.000 claims 1
- 239000013589 supplement Substances 0.000 claims 1
- 239000003245 coal Substances 0.000 abstract description 46
- 239000003949 liquefied natural gas Substances 0.000 abstract description 7
- 239000002808 molecular sieve Substances 0.000 description 11
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 description 11
- 238000001035 drying Methods 0.000 description 9
- 238000005516 engineering process Methods 0.000 description 8
- 238000010586 diagram Methods 0.000 description 7
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 6
- 235000019628 coolness Nutrition 0.000 description 5
- 238000004140 cleaning Methods 0.000 description 4
- 238000007599 discharging Methods 0.000 description 4
- 238000001704 evaporation Methods 0.000 description 4
- 230000008020 evaporation Effects 0.000 description 4
- 239000012530 fluid Substances 0.000 description 4
- 229910002092 carbon dioxide Inorganic materials 0.000 description 3
- 239000001569 carbon dioxide Substances 0.000 description 3
- 239000003034 coal gas Substances 0.000 description 3
- 238000002309 gasification Methods 0.000 description 3
- 230000008929 regeneration Effects 0.000 description 3
- 238000011069 regeneration method Methods 0.000 description 3
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 3
- 229910001868 water Inorganic materials 0.000 description 3
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- 238000010521 absorption reaction Methods 0.000 description 2
- 239000003345 natural gas Substances 0.000 description 2
- 239000002671 adjuvant Substances 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000007664 blowing Methods 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 239000000428 dust Substances 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 239000002360 explosive Substances 0.000 description 1
- 238000000605 extraction Methods 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 238000005065 mining Methods 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 238000010992 reflux Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
Images
Classifications
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/0204—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the feed stream
- F25J3/0209—Natural gas or substitute natural gas
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/0228—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream
- F25J3/0233—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of CnHm with 1 carbon atom or more
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/0228—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream
- F25J3/0257—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of nitrogen
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2200/00—Processes or apparatus using separation by rectification
- F25J2200/04—Processes or apparatus using separation by rectification in a dual pressure main column system
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2200/00—Processes or apparatus using separation by rectification
- F25J2200/70—Refluxing the column with a condensed part of the feed stream, i.e. fractionator top is stripped or self-rectified
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2200/00—Processes or apparatus using separation by rectification
- F25J2200/72—Refluxing the column with at least a part of the totally condensed overhead gas
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2210/00—Processes characterised by the type or other details of the feed stream
- F25J2210/40—Air or oxygen enriched air, i.e. generally less than 30mol% of O2
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2215/00—Processes characterised by the type or other details of the product stream
- F25J2215/04—Recovery of liquid products
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2215/00—Processes characterised by the type or other details of the product stream
- F25J2215/40—Air or oxygen enriched air, i.e. generally less than 30mol% of O2
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2240/00—Processes or apparatus involving steps for expanding of process streams
- F25J2240/02—Expansion of a process fluid in a work-extracting turbine (i.e. isentropic expansion), e.g. of the feed stream
- F25J2240/10—Expansion of a process fluid in a work-extracting turbine (i.e. isentropic expansion), e.g. of the feed stream the fluid being air
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2270/00—Refrigeration techniques used
- F25J2270/14—External refrigeration with work-producing gas expansion loop
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- Engineering & Computer Science (AREA)
- Physics & Mathematics (AREA)
- Mechanical Engineering (AREA)
- Thermal Sciences (AREA)
- General Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Separation By Low-Temperature Treatments (AREA)
Abstract
本发明公开了一种含空气煤层气的液化工艺，包括压缩净化工艺、制冷工艺和液化分离工艺，该液化分离工艺中采用低温双级精馏方法，其液化和分离都在低温下进行，分离纯度高，安全性能好，其液化天然气的产品纯度可以达到99％以上，排放到空气中甲烷含量仅为1％左右，有效回收了资源；本发明还提供了这种含空气煤层气的液化设备。
The invention discloses a liquefaction process of air-containing coal bed gas, which includes a compression purification process, a refrigeration process and a liquefaction separation process. The liquefaction separation process adopts a low-temperature double-stage rectification method, and its liquefaction and separation are both carried out at low temperature. High purity, good safety performance, the product purity of liquefied natural gas can reach more than 99%, and the content of methane discharged into the air is only about 1%, which effectively recovers resources; the invention also provides the liquefaction equipment of this air-containing coalbed methane .
Description
Technical field
The present invention relates to a kind of gas liquefaction separation equipment and technology, particularly contain the liquefaction process and the equipment of air coal bed gas.
Background technology
Coal bed gas also claims unconventional natural gas or mine gas, and its main component is a methane.It is not only a kind of clean energy resource of preciousness, also is important chemical material.The coal bed gas resource of China is very abundant, but the exploitation fewer, almost do not have industrial application.It is reported, the coal bed gas that China enters atmosphere every year account for the whole world mine discharging the coal bed gas total amount 1/3rd, this has not only caused serious atmosphere pollution, also is the very big wasting of resources.
The characteristics of coal bed gas are that well yield is not really high, and except that using nearby, tubing is defeated outward usually uneconomical.Especially the coal bed gas of extraction in the coal mining process, because pressure is low, methane content is low, and wherein be mixed with air, airborne oxygen is dangerous combustion adjuvant, this has brought difficulty just for the processing and the transportation of coal bed gas, and it is just more serious that emptying is wasted, and this problem never is well solved.If the coal bed gas (mainly being methane) and the air separation that contain in the air coal bed gas are come out, the coal gas gasification after will purifying then, this just is very easy to transportation and utilizes.
The liquefied natural gas technology has the history in three, 40 years so far since the just commercialization of the sixties in last century.China's liquefied natural gas industry is in developing stage, and domestic circulation to various liquefied natural gas is grasped substantially.No matter but be external or domestic, the liquefied natural gas technology all is higher at purity, not aeriferous natural gas.To separation and the liquefaction that contains the air coal bed gas, also do not cause people's attention, the phenomenon that contains air coal bed gas emptying discharging is still very serious.Conventional separation method has absorption process, absorption method, film permeation method and cryogenic rectification method etc.The front several method, the purity of separation is difficult to reach requirement, and therefore what have also needs heating, contains air coal bed gas explosive at high temperature, has potential safety hazard, is not applied.Cryogenic rectification method is applied in the separation that contains the air coal bed gas and the liquefaction, present then yet nobody's proposition, does not more have concrete technology.
Summary of the invention
Technical problem to be solved by this invention provides a kind of liquefaction process that contains the air coal bed gas, adopt low temperature twin-stage rectificating method, the product purity of its liquefied natural gas can reach more than 99%, is discharged into that methane content only is about 1% in the air, has effectively reclaimed resource; The present invention also provides this liquefaction device that contains the air coal bed gas.
For solving the problems of the technologies described above, the technical solution used in the present invention is: a kind of liquefaction process that contains the air coal bed gas comprises following processing step:
At first will contain the compression of air coal bed gas unstripped gas and purify, remove impurity in the unstripped gas;
To compress the air coal bed gas feeding heat exchanger that contains that purifies then and carry out heat exchange, temperature will be cooled to-130 ℃～-165 ℃;
The air coal bed gas that contains through refrigeration enters first fractionating column, is liquid by the condenser condenses at fractionating column top, and a liquid part that is condensed enters the further rectifying of after-fractionating top of tower, and another part refluxes;
The evaporimeter that the liquid that is rich in methane that draw first fractionating column bottom enters the after-fractionating tower bottom again is evaporated to gas, as the gas fraction of after-fractionating tower;
The gas fraction of after-fractionating tower bottom contacts further rectifying with the liquid distillate at top, promptly obtains highly purified liquefaction coal bed gas at the after-fractionating tower bottom, and the after-fractionating top of tower obtains containing the pure air of few methane;
The cold of described heat exchanger is provided by a refrigeration system, and described refrigeration system is gas swell refrigeration system or mix refrigerant refrigeration system.
Wherein, in the described gas swell refrigeration system, the gas that draw at the first fractionating column top is introduced into the leakage loss of replenishing refrigeration gas in the refrigeration system;
In the described compression process for purifying step, also can reduce the oxygen content in the coal bed gas in advance, oxygen content is reduced to below 2%;
A part of gas is also drawn at described first fractionating column middle part, after the heat exchanger cooling of after-fractionating top of tower, enters after-fractionating tower middle part and participates in rectifying;
The pure air that described after-fractionating top of tower obtains enters heat exchanger as cold;
The cold of the described first fractionating column condenser is provided by refrigeration system;
The air coal bed gas enters before first fractionating column, and elder generation is through the evaporimeter precooling of after-fractionating tower;
In the gas swell refrigeration system, after the cold heat exchange as the first fractionating column condenser earlier of refrigeration gas, enter the cold junction of heat exchanger again.
The present invention also provides the above-mentioned equipment that contains the liquefaction process of air coal bed gas, comprise the compression cleaning equipment, refrigeration plant and liquefaction separation equipment, the liquefaction separation equipment has heat exchanger, described compression cleaning equipment is connected with the hot media channel of the heat exchanger of liquefaction in the separation equipment, refrigeration plant is connected with the refrigerant passage of liquefaction separation equipment, described liquefaction separation equipment comprises heat exchanger and the two-stage fractionating column that connects successively, first fractionating column has condenser, the after-fractionating tower has evaporimeter, it is characterized in that, the first fractionating column top, top of tower is heated up in a steamer with second in the bottom, the bottom links to each other by pipeline, and the first fractionating column condenser also has gas piping gas is incorporated in the refrigeration plant.
Wherein, pipeline connection is passed through at the middle part of the middle part of described first fractionating column and after-fractionating tower;
Article one, gas piping is connected the after-fractionating top of tower with heat exchanger;
The refrigerant pipeline of the condenser of described first fractionating column is communicated with the refrigeration air pipe of refrigeration plant;
The evaporimeter heating pipe line of described after-fractionating tower is connected with the unstripped gas pipeline that enters before first fractionating column.
The beneficial effect that the present invention can reach is: the present invention contains air coal gas gasification equipment and technology aims at the separation liquefaction process that contains the design of air coal bed gas, its liquefaction is carried out at low temperatures with separating all, the separation purity height, security performance is good, just can produce liquefied natural gas when separating.Complete equipment is installed easy to connect.It has not only effectively utilized aeriferous coal bed gas resource, and the atmosphere pollution of having avoided discharging to cause.
Description of drawings
Fig. 1 is the embodiment of the invention 1 and embodiment 2 compression cleaning equipment schematic diagrames;
Fig. 2 is the embodiment of the invention 1 refrigeration plant and liquefaction separation equipment schematic diagram;
Fig. 3 is the embodiment of the invention 2 refrigeration plants and liquefaction separation equipment schematic diagram.
The specific embodiment
Embodiment 1
Consult Fig. 1, Fig. 2, the liquefaction device schematic diagram that contains the air coal bed gas for the embodiment of the invention 1, comprise the two large divisions, at first contain the compressed purification earlier of air coal bed gas unstripped gas, separate through liquefaction again and can obtain liquified natural gas, the required cold of separation process that wherein liquefies is provided by refrigeration system, and concrete equipment and technology are described below:
Consult Fig. 1, for the present invention compresses the cleaning equipment schematic diagram.Comprise filter 1, gas-liquid separator 2, a stage compressor 3, cooler 5, split-compressor 4, cooler 6, molecular sieve equipment group, described molecular sieve drying equipment group comprises three molecular sieve drying machines 7,8,9.First molecular sieve drying machine 7, second molecular sieve drying machine 8 alternations regeneration, another molecular sieve drying machine 9 coolings are standby, switch once in per 8 hours.This molecular sieve drying equipment is mainly used to remove water, carbon dioxide, and can remove a certain amount of oxygen.
The technological process that compression purifies is as follows:
1, the air coal bed gas unstripped gas that contains that the self-discharging pipeline comes at first removes dust through filter 1;
2, after containing the air coal bed gas and enter gas-liquid separator 2 gas-liquid separations after the dedusting, gas enters the compression of compressor 3 one-levels;
3, compression is after cooler 5 coolings;
4, enter split-compressor 4 and cooler 6 compression coolings again;
5, contain the air coal bed gas and enter molecular sieve drying equipment 7, deviate from water and carbon dioxide, the wherein a part of heater via 11 of regeneration gas and cold blowing gas is heated to 240-250 ℃, be used for the regeneration of mole sieve drier 8, another part directly enters the good drier 9 of having regenerated, the cooling molecular sieve, the temperature that reduces molecular sieve drying machine 9 is standby;
6, remove containing air coal bed gas unstripped gas and can entering refrigeration, liquefaction and separation system through filter 10 again of water, carbon dioxide and oxygen (oxygen content drops to 1.5%) through molecular sieve drying equipment.
Consult Fig. 2,, comprise refrigeration plant and liquefaction separation equipment for the embodiment of the invention 2 contains air coal bed gas refrigeration, liquefaction separation equipment schematic diagram, the cold that refrigeration plant obtains by heat exchanger 15 with its in contain the heat exchange of air coal bed gas.Described liquefaction separation equipment comprises heat exchanger 15 and the two-stage fractionating column 16,17 that connects successively, first fractionating column 16 has condenser 19, the after-fractionating tower has evaporimeter 18, top of tower is heated up in a steamer with second in the first fractionating column top, bottom, the bottom links to each other by pipeline, and the first fractionating column condenser also has gas piping gas is incorporated in the refrigeration plant.
The liquefying separation process step is as follows:
1, the air coal bed gas that contains of compressed purification enters in the heat exchanger 15 and cold Medium Exchange heat wherein, and it is 0.6MPa that temperature reaches-155 ℃, pressure.
2, contain the bottom that the air coal bed gas enters first fractionating column 16, and pass through each piece column plate from bottom to top, condenser 19 contain air coal bed gas at first fractionating column, 16 tops are condensed into liquid by major part, temperature is approximately-174 ℃, pressure is 0.6MPa, and the uncooled gas (being less than 1%) that contains methane is on a small quantity introduced in the refrigeration system by pipeline 20.
3, a liquid part that is condensed in the condenser 19 is passed through pressure-reducing valve 24 (through behind the pressure-reducing valve, fluid temperature is-190 ℃, pressure is 0.15MPa) the further fractionation in top that enters after-fractionating tower 17, another part liquid flows back to first fractionating column 16 as cold, flow through column plate from top to bottom, carry out heat exchange with the unstripped gas that makes progress away; So more upwards, the methane content in the gas is few more, and is downward more, and the methane content in the liquid is many more.
What 4, draw from first fractionating column, 16 bottoms is the liquid that is rich in methane (methane content about 78%), by a pressure-reducing valve 22 (through behind the pressure-reducing valve, fluid temperature is-170 ℃, pressure is 0.15MPa) enter the evaporimeter 18 of the bottom of after-fractionating tower 17 again, be heated evaporation, the gas fraction that becomes after-fractionating tower 17 enters the further rectifying of after-fractionating tower; The distillation process of after-fractionating tower is identical with first fractionating column, and liquid from up to down makes progress under gas, and different is that the after-fractionating tower bottom is to be rich in the liquid of methane in evaporation.
5, through after 17 rectifying of after-fractionating tower, what emit from the top of second rectifying column is to contain the few pure air of methane, enters heat exchanger 15, reclaims cold.
What 6, emit from after-fractionating tower 17 bottoms is exactly the very high liquefaction coal bed gas of purity.
Heat exchanger 15 needed colds are provided by refrigeration system in the above-mentioned liquefaction separation process, and refrigeration system comprises refrigeration machine 12 and compressor 13.
In the refrigeration system loop, the flow of gas approximately is 2.5-5 a times that the liquefaction road contains air coal bed gas flow.
Consult Fig. 3, for the embodiment of the invention 2 contains air coal bed gas refrigeration plant and liquefaction separation equipment schematic diagram.The liquefaction separation equipment comprises two-stage heat exchanger 35,36, first fractionating column 37,38, first fractionating column 37 has condenser 34, after-fractionating tower 38 has evaporimeter 39, the first fractionating column top, middle part, bottom and second are heated up in a steamer top of tower, middle part, bottom and are linked to each other by pipeline, and the first fractionating column condenser also has gas piping gas is incorporated in the refrigeration plant.
The liquefying separation process step is as follows:
1, the air coal bed gas unstripped gas that contains of compressed purification enters heat-shift in the heat exchanger 35,36, and the evaporimeter 39 that enters after-fractionating tower 38 further reduces temperature, and to reach-160 ℃, pressure be 0.6MPa.
2, contain air coal bed gas flash-pot 39 and come out after, enter the bottom of first fractionating column 37, and pass through each piece column plate from bottom to top, unstripped gas is condensed into liquid by major part in the condenser 34 (cold of condenser 34 is provided by refrigeration system) at first fractionating column, 37 tops, temperature is approximately-174 ℃, pressure is 0.6MPa, and the uncooled gas (being less than 1%) that contains methane on a small quantity is introduced in the refrigeration system.
3, a liquid part that is condensed in the condenser 34 is passed through pressure-reducing valve 43 (through behind the pressure-reducing valve, fluid temperature is-190 ℃, pressure is 0.15MPa) the further fractionation in top that enters after-fractionating tower 38, another part liquid flows back to first fractionating column 37 as cold, flow through column plate from top to bottom, carry out heat exchange with the unstripped gas that makes progress away; So more upwards, the methane content in the gas is few more, and is downward more, and the methane content in the liquid is many more.
What 4, draw from first fractionating column, 37 bottoms is the liquid that is rich in methane (methane content about 78%), by a pressure-reducing valve 45 (through behind the pressure-reducing valve, fluid temperature is-170 ℃, pressure is 0.15MPa) enter the evaporimeter 39 of the bottom of after-fractionating tower 38 again, be heated evaporation, the gas fraction that becomes after-fractionating tower 38 enters the further rectifying of after-fractionating tower; The distillation process of after-fractionating tower is identical with first fractionating column, and liquid from up to down makes progress under gas, and different is that the after-fractionating tower bottom is to be rich in the liquid of methane in evaporation.
5, through after 38 rectifying of after-fractionating tower, what emit from the top of second rectifying column is to contain the few pure air of methane, (this portion gas is to draw for improving rectification effect to the gas that 40 coolings are drawn from first fractionating column middle part through a heat exchanger again, be cooled to-170 ℃ through heat exchanger 40 and pressure-reducing valve 23, pressure is 0.15MPa) gas go out heat exchanger after temperature be-93 ℃, pressure is 0.15MPa, enter heat exchanger 35, reclaim cold.
What 6, emit from after-fractionating tower 17 bottoms is exactly the very high liquefaction coal bed gas of purity.
Heat exchanger 35,36 and condenser 34 needed colds are provided by refrigeration system in the above-mentioned liquefaction separation process, described refrigeration plant is provided with cooler 44,45 after comprising two-stage compressor 27, the 28 every stage compressors that connect successively, connect cooler 33 behind two stage turbine supercharger 29,30, the turbine supercharger, and connect first heat exchanger 35, first heat exchanger 35 further connects two stage turbine decompressor 32,31, and turbo-expander is introduced into condenser 34 and further with the cold medium channel of second heat exchanger is communicated with.
1, before refrigeration system starts, be full of nitrogen in the system as refrigeration gas, temperature is 30 ℃, and pressure is 0.15Mpa;
2, start refrigeration system, earlier compressed machine 27, the 28 compression coolings of refrigeration gas through turbine supercharger 29,30 superchargings cooling, enter 35 precoolings of first heat exchanger again;
3, refrigeration gas is introduced into condenser 34 again through turbo-expander 32,31 swell refrigerations, and temperature drops to-166 ℃, promptly enters the cold junction of heat exchanger 36;
3, the gas of drawing in the liquefying separation process step 2 is introduced in the refrigeration pipe behind the decompressor, to replenish the refrigeration gas that leaks;
4, after refrigeration gas enters the re-heat of heat exchanger gas, recompression, supercharging, refrigeration, swell refrigeration, so circulation.
In the refrigeration system loop, the flow of gas approximately be liquefaction contain air coal bed gas flow in the pipeline 2.5-5 doubly.
Claims (12)
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Cited By (9)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN101948707A (en) * | 2010-09-15 | 2011-01-19 | 煤炭科学研究总院重庆研究院 | Oxygen-containing coalbed methane purification device |
| CN101476813B (en) * | 2009-01-21 | 2011-06-15 | 成都蜀远煤基能源科技有限公司 | Feed gas separation method and apparatus of coal gasification apparatus |
| CN102538398A (en) * | 2012-02-09 | 2012-07-04 | 杭州杭氧股份有限公司 | Process and system for purifying, separating and liquefying nitrogen-and-oxygen-containing coal mine methane (CMM) |
| CN102634395A (en) * | 2012-04-24 | 2012-08-15 | 中国五环工程有限公司 | Process and system for purifying and refining coal-bed gas |
| CN101445755B (en) * | 2008-12-22 | 2012-11-28 | 中国石油集团长城钻探工程有限公司 | Method for purifying and liquefying coalbed gas |
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| CN103205297A (en) * | 2013-04-15 | 2013-07-17 | 西南化工研究设计院有限公司 | Method for separating and purifying coal mine methane (CMM) in mine areas by using pressure swing adsorption (PSA) process |
| CN104359286A (en) * | 2014-11-12 | 2015-02-18 | 辽宁哈深冷气体液化设备有限公司 | Method for removing acidic gas from natural gas |
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| CN101476813B (en) * | 2009-01-21 | 2011-06-15 | 成都蜀远煤基能源科技有限公司 | Feed gas separation method and apparatus of coal gasification apparatus |
| CN101948707A (en) * | 2010-09-15 | 2011-01-19 | 煤炭科学研究总院重庆研究院 | Oxygen-containing coalbed methane purification device |
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| CN102634395A (en) * | 2012-04-24 | 2012-08-15 | 中国五环工程有限公司 | Process and system for purifying and refining coal-bed gas |
| CN103148678A (en) * | 2013-02-25 | 2013-06-12 | 中煤科工集团重庆研究院 | Device for producing LNG (liquefied natural gas) through PSA (pressure swing adsorption) deepening cold liquefying purification of CBM (coalbed methane) with low concentration |
| CN103148678B (en) * | 2013-02-25 | 2016-04-27 | 中煤科工集团重庆研究院有限公司 | Device for preparing LNG through low-concentration coal bed gas pressure swing adsorption, deepening cold liquefaction and purification |
| CN103205297A (en) * | 2013-04-15 | 2013-07-17 | 西南化工研究设计院有限公司 | Method for separating and purifying coal mine methane (CMM) in mine areas by using pressure swing adsorption (PSA) process |
| CN104359286A (en) * | 2014-11-12 | 2015-02-18 | 辽宁哈深冷气体液化设备有限公司 | Method for removing acidic gas from natural gas |
| CN104359286B (en) * | 2014-11-12 | 2017-01-04 | 辽宁中集哈深冷气体液化设备有限公司 | A kind of remove the method for sour gas in natural gas |
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