CN2898737Y - Liquefier containing coal-seam gas - Google Patents
Liquefier containing coal-seam gas Download PDFInfo
- Publication number
- CN2898737Y CN2898737Y CNU2006201158812U CN200620115881U CN2898737Y CN 2898737 Y CN2898737 Y CN 2898737Y CN U2006201158812 U CNU2006201158812 U CN U2006201158812U CN 200620115881 U CN200620115881 U CN 200620115881U CN 2898737 Y CN2898737 Y CN 2898737Y
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- gas
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- liquefaction
- separation
- coal bed
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- 238000005057 refrigeration Methods 0.000 claims abstract description 43
- 238000000926 separation method Methods 0.000 claims abstract description 42
- 230000006835 compression Effects 0.000 claims abstract description 14
- 238000007906 compression Methods 0.000 claims abstract description 14
- 238000004140 cleaning Methods 0.000 claims abstract description 10
- 238000010438 heat treatment Methods 0.000 claims abstract description 5
- 239000003507 refrigerant Substances 0.000 claims abstract description 5
- 239000003245 coal Substances 0.000 claims description 45
- 239000007789 gas Substances 0.000 abstract description 81
- 238000000034 method Methods 0.000 abstract description 13
- 238000005194 fractionation Methods 0.000 abstract description 8
- 239000003949 liquefied natural gas Substances 0.000 abstract description 6
- 238000009434 installation Methods 0.000 abstract 1
- 238000002360 preparation method Methods 0.000 abstract 1
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 39
- 239000007788 liquid Substances 0.000 description 17
- 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
- 238000001816 cooling Methods 0.000 description 7
- 238000010586 diagram Methods 0.000 description 7
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 6
- 238000005516 engineering process Methods 0.000 description 6
- 235000019628 coolness Nutrition 0.000 description 5
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 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
- 239000001301 oxygen Substances 0.000 description 4
- 229910052760 oxygen Inorganic materials 0.000 description 4
- 229910002092 carbon dioxide Inorganic materials 0.000 description 3
- 239000001569 carbon dioxide Substances 0.000 description 3
- 238000000746 purification 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
- 239000003034 coal gas Substances 0.000 description 2
- 238000004821 distillation Methods 0.000 description 2
- 238000002309 gasification 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
- 229910052757 nitrogen Inorganic materials 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
- F25J3/0228—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
- F25J3/0204—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
- F25J3/0257—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
-
- 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
-
- 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
The utility model discloses a liquefier containing coal-seam gas, which comprises a compression cleaning equipment, a refrigeration equipment and a liquefy separation equipment; wherein, the liquefy separation equipment is provided with a heating exchanger; the compression cleaning equipment is connected with the heat medium channel in the heat exchanger of the liquefy separation equipment; the refrigeration equipment is connected with the refrigerant medium channel of the liquefy separation equipment; the liquefy separation equipment comprises an ordinal connected heating exchanger and a two fractionation towers; the first fractionation tower is provided with a condenser; the second fractionation tower is provided with an evaporator; the top part and bottom part of the first fractionation tower are connected with the top part and bottom part of the second fractionation tower through pipeline; and the first fractionation tower is provided with a gas pipe to introduce gas to the refrigeration equipment. The utility model, the liquefier containing coal-seam gas, is designed specifically for the process of separation and liquefying of containing coal-seam gas, the process of liquefying and separation under low temperature, high separation purity, secure performance, and simultaneous separation and preparation of liquefied natural gas. The complete equipment is of convenient installation and connection.
Description
Technical field
The utility model relates to a kind of gas liquefaction separation equipment, particularly contains the liquefaction device 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.
The utility model content
Technical problem to be solved in the utility model provides a kind of liquefaction device that contains the air coal bed gas, adopt low temperature twin-stage rectifying device, contain the air coal bed gas through this device processes, the product purity of its liquefaction coal bed gas can reach more than 99%, be discharged into that methane content only is about 1% in the air, effectively reclaimed resource.
For solving the problems of the technologies described above, technical solution adopted in the utility model is: a kind of liquefaction device that contains the 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, 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 heating pipe line of the evaporimeter of described after-fractionating tower is connected with the unstripped gas pipeline that enters before first fractionating column.
The beneficial effect that the utility model can reach is: the utility model contains air coal gas gasification equipment and 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 utility model embodiment 1 and embodiment 2 compression cleaning equipment schematic diagrames;
Fig. 2 is the utility model embodiment 1 refrigeration plant and liquefaction separation equipment schematic diagram;
Fig. 3 is the utility model embodiment 2 refrigeration plants and liquefaction separation equipment schematic diagram.
The specific embodiment
Consult Fig. 1, Fig. 2, the liquefaction device schematic diagram that contains the air coal bed gas for the utility model embodiment 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, be the utility model compression 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 of this compression cleaning equipment 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 utility model embodiment 1 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 that successively the heat exchanger 15 and two-stage fractionating column 16,17, the first fractionating columns 16 that connect have condenser 19, and the after-fractionating tower has that top of tower is heated up in a steamer with second in evaporimeter 18, the first fractionating column tops, bottom, the bottom links to each other by pipeline.
The processing step of this liquefaction separation equipment 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, the condenser 19 contain air coal bed gas at first fractionating column, 16 tops are condensed into liquid by major part, and temperature is approximately-174 ℃, and pressure is 0.6MPa.
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.
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.
Embodiment 2
Embodiment 2 compression cleaning equipments are identical with embodiment 1.
Consult Fig. 3, for the utility model embodiment 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 processing step of liquefaction separation equipment 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 is on a small quantity passed through pipeline 20 to be 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.
The technological process of above-mentioned refrigeration plant is as follows:
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 is 2.5-5 a times that the liquefaction road contains air coal bed gas flow.
Claims (5)
1, a kind of liquefaction device that contains the 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.
2, a kind of liquefaction device that contains the air coal bed gas according to claim 1 is characterized in that, pipeline connection is passed through at the middle part of the middle part of described first fractionating column and after-fractionating tower.
3, a kind of liquefaction device that contains the air coal bed gas according to claim 1 is characterized in that, a gas piping is connected the after-fractionating top of tower with heat exchanger.
4, a kind of liquefaction device that contains the air coal bed gas according to claim 1 is characterized in that, the refrigerant pipeline of the condenser of described first fractionating column is communicated with the refrigeration air pipe of refrigeration plant.
5, a kind of liquefaction device that contains the air coal bed gas according to claim 1 is characterized in that, the heating pipe line of the evaporimeter of described after-fractionating tower is connected with the unstripped gas pipeline that enters before first fractionating column.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNU2006201158812U CN2898737Y (en) | 2006-04-18 | 2006-05-19 | Liquefier containing coal-seam gas |
Applications Claiming Priority (3)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN200620012499 | 2006-04-18 | ||
| CN200620012499.9 | 2006-04-18 | ||
| CNU2006201158812U CN2898737Y (en) | 2006-04-18 | 2006-05-19 | Liquefier containing coal-seam gas |
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| Publication Number | Publication Date |
|---|---|
| CN2898737Y true CN2898737Y (en) | 2007-05-09 |
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| Application Number | Title | Priority Date | Filing Date |
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| CNU2006201158812U Expired - Lifetime CN2898737Y (en) | 2006-04-18 | 2006-05-19 | Liquefier containing coal-seam gas |
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| Country | Link |
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| CN (1) | CN2898737Y (en) |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101290184B (en) * | 2008-06-05 | 2010-10-13 | 北京国能时代能源科技发展有限公司 | Chemical industry tail gas liquefied separation method and equipment |
| CN101644527B (en) * | 2009-08-26 | 2011-12-28 | 四川空分设备(集团)有限责任公司 | Refrigeration system and liquefaction system for liquefaction process of natural gas |
| CN104697292A (en) * | 2014-05-25 | 2015-06-10 | 刘晓 | Super air purification application system |
| CN105823303A (en) * | 2015-01-23 | 2016-08-03 | 气体产品与化学公司 | Improved separation of heavy hydrocarbons and NGLs from natural gas, and in integration with liquefaction of natural gas |
-
2006
- 2006-05-19 CN CNU2006201158812U patent/CN2898737Y/en not_active Expired - Lifetime
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101290184B (en) * | 2008-06-05 | 2010-10-13 | 北京国能时代能源科技发展有限公司 | Chemical industry tail gas liquefied separation method and equipment |
| CN101644527B (en) * | 2009-08-26 | 2011-12-28 | 四川空分设备(集团)有限责任公司 | Refrigeration system and liquefaction system for liquefaction process of natural gas |
| CN104697292A (en) * | 2014-05-25 | 2015-06-10 | 刘晓 | Super air purification application system |
| CN105823303A (en) * | 2015-01-23 | 2016-08-03 | 气体产品与化学公司 | Improved separation of heavy hydrocarbons and NGLs from natural gas, and in integration with liquefaction of natural gas |
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Owner name: PHYSICAL CHEMISTRY TECHNOLOGY INST., CHINESE ACAD Free format text: FORMER OWNER: BEIJING KERUI SAISI GAS LIQUEFACTION TECHNOLOGY CO., LTD. Effective date: 20080222 |
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Inventor after: Yang Kejian Inventor after: Zhang Wu Inventor after: Ren Xiaokun Inventor before: Yang Kejian |
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Effective date of registration: 20080222 Address after: Beijing, Zhongguancun, Haidian District, No. 2, north, zip code: 100080 Patentee after: Technical Institute of Physics and Chemistry Chinese Academy of Sciences Address before: Beijing, Zhongguancun, Haidian District, No. 2, north, zip code: 100080 Patentee before: Beijing Cryosys Technical Company of Gas Liquefaction Co.,Ltd. |
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