CN103773529B - Pry-mounted associated gas liquefaction system - Google Patents
Pry-mounted associated gas liquefaction system Download PDFInfo
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- CN103773529B CN103773529B CN201210408430.8A CN201210408430A CN103773529B CN 103773529 B CN103773529 B CN 103773529B CN 201210408430 A CN201210408430 A CN 201210408430A CN 103773529 B CN103773529 B CN 103773529B
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Abstract
The invention discloses a pry-mounted associated gas liquefaction system including an inlet compressor set, a purification system, a raw gas heat exchanger, a gas liquid direct-contact heat exchanger, a washing tower, a multistage compressor set, a liquefied gas heat exchanger, a liquefaction throttle valve and a liquefied natural gas storage tank, the components are connected in sequence, wherein the liquefaction system also comprises a refrigeration compressor set, a refrigeration throttle valve and a coolant separator, the multistage compressor set outlet is divided into two paths, one path, after sequential heat transfer and throttling, is connected with a liquefied natural gas storage tank, the other path as a coolant raw material, after compression throttling, enters into the coolant separator, and a bottom outlet of the coolant separator is connected via a pipeline to a washing tower top reflux inlet. The pry-mounted associated gas liquefaction system adopts a washing tower top methane-enriched gas as a coolant of the system itself, and simplifies the process flow. The refrigeration system makes full use of a compression refrigeration system with a throttling device, effectively improves the cooling energy, and is energy-saving.
Description
Technical field
The present invention relates to a kind of associated gas liquefaction system of power-saving technology and field of environment protection, specifically a kind of with Sweet natural gas, coal-seam gas or other high methane gass system for raw material production liquefaction production Sweet natural gas.
Background technology
Sweet natural gas and coal, oil be called three of world's primary energy source large pillars.Sweet natural gas refers to hydro carbons born in pore formation under earth's surface and non-hydrocarbons mixture, normal together with crude oil association, based on methane, and comprises the hydro carbons heavier than methane: as ethane, propane, normal butane, Trimethylmethane, Skellysolve A, iso-pentane etc.In addition to the hydrocarbons, also the gases such as a small amount of moisture, nitrogen, carbonic acid gas, hydrogen sulfide, oxygen, argon may be there is.Sweet natural gas tool has been widely used, and can be used as industrial chemicals and various fuel.
Oil-gas field side area natural gas source can be divided into oil field emptying natural gas, associated gas and gas stringer Sweet natural gas.Associated gas, mainly exists with the form of well head separation gas, Volatile Gas in Oil Tank and stabilization of crude oil gas; Gas stringer Sweet natural gas refers to that tolerance is less than 0.5 ten thousand m
3the low pressure gas gas well gas of/d.The long-term closing well of gas stringer, can not form oil-gas field production capacity, oil field emptying natural gas emptying is burnt, and not only greatly wastes resource, and the severe contamination air of field area.By the statistics in the end of the year 2000, (geologic reserve is greater than 10,000,000,000 m to China's middle-large gas field
3) 56, account for 13. 4% of national gas field sum, all the other gas fields of 86. 6% are small gas fields.The scattered gas field less for reserves and the higher marginal gas field of cost of winning, because the pipeline transportation cost of long distance is higher, industrial scale is uneconomical, does not possess the condition entering market for natural gas.The amount of natural gas in these gas fields does not meet again the liquefaction scale of big-and-middle-sized natural gas liquefaction device simultaneously.For this reason, the scattered gas field of China and outlying gas field Sweet natural gas can not get exploitation for a long time.According to statistics, about there are 1,600,000,000 m in China every year
3oil field emptying natural gas emptying is burnt.Therefore, economy, reasonably exploitation side area natural gas source, change resource is production capacity, reduces field area topsoil, has become the problem that the industry of development China's natural gas is anxious to be resolved.
The comprehensive utilization of oil-gas field side area associated gas resource is different from large gas utilization, must based on the internal market of dispersion well, block of cells well (or working district) and neighboring markets, according to tolerance and the temperament characteristics of natural gas source, adopt little, the less investment for the treatment of capacity and the large sledge-borne type local use technology of turndown ratio, rolling development is implemented to oil-gas field.
The recovery method of the small-sized skid Sweet natural gas lighter hydrocarbons of patent CN1515651A mono-kind, this patent adopts ammonia refrigeration can produce lighter hydrocarbons, liquefied gas, dry gas etc.But it is not suitable for the recycling of the frontier area natural gas in oil and gas fields without pipe network, and dry gas cannot enter pipe network.Patent CN03134159.4 mono-kind small-sized sledge dress Sweet natural gas methods of light hydrocarbon recovery, natural gas via overdraft, cooling, absorption, stable rear separable recovery dry gas, liquefied gas, lighter hydrocarbons and hydrocarbon mixture product, Sweet natural gas recovering effect is good, but plant energy consumption is high, C
2, C
3the rate of recovery not high.Patent CN102115683A discloses a kind of method of producing natural gas liquids, Sweet natural gas obtains natural gas liquids at throttling refrigeration after two-stage heat exchange, natural gas refrigeration technology adopts hybrid refrigeration, and its feature is that hybrid refrigeration is divided into high-temperature refrigeration and cryogenic refrigeration two processes.
At present, associated gas recovery utilization rate in frontier area is very low.In prior art, adopt the device of propane in shallow cold recovery Sweet natural gas, its propane recovering rate is generally 60% ~ 80%; Reclaiming ethane is main device, and the yield of ethane is generally 85%.Therefore, by optimizing operation parameters, change refrigerating method, apply the methods such as new technology, improve light hydrocarbon recovery rate very necessary.Meanwhile, take refrigerating method effectively, reduce the energy consumption of natural gas liquefaction, reduce natural gas processing cost, obtain best economic benefit also very important.
Summary of the invention
The object of this invention is to provide a kind of sledge-borne type associated gas liquefaction system, sledge-borne type associated gas liquefaction system of the present invention has the advantages such as safe and reliable, equipment is simple, process cost is low.
The invention provides a kind of sledge-borne type associated gas liquefaction system, described system comprises imported compressor, purification system, unstripped gas interchanger, gas-liquid direct-contact interchanger, washing tower, stage compression unit, liquefied gas interchanger, liquefaction throttling valve, LNG tank, wherein, raw material associated gas passes through inlet line successively through imported compressor, purification system is connected with gas-liquid direct-contact interchanger unstripped gas entrance with unstripped gas interchanger, gas-liquid direct-contact interchanger gaseous phase outlet is connected with washing tower unstripped gas entrance by pipeline, wash tower bottoms outlet is divided into two-way, one tunnel is connected with gas-liquid direct-contact interchanger spray liquid entrance, another road is connected with the spray liquid entrance of washing tower, washing tower top gaseous phase outlet is connected with stage compression unit entrance by unstripped gas interchanger, it is characterized in that: described liquefaction system also comprises refrigeration compressor, refrigeration throttling valve and refrigerant separator, described stage compression unit outlet is divided into two-way, one tunnel is connected with LNG tank through liquefied gas interchanger, liquefaction throttling valve successively, another road is connected with refrigerant separator through refrigeration compressor, refrigeration throttling valve successively, refrigerant separator top exit is connected with stage compression unit entrance by liquefied gas interchanger, and refrigerant separator outlet at bottom is connected with washing tower top reflux inlet by pipeline.
In sledge-borne type associated gas liquefaction system of the present invention, described washing tower is the rectifying tower only having stripping section, gas by entering at the bottom of tower, tower top goes out, overhead gas has partial reflux through compression condensation, by regulating the downstream pressure of the amount of refrigerant gas and the throttling valve that freezes, control ratio and the temperature of withdrawing fluid, ensure the content value of methane in overhead gas.Washing tower number of theoretical plate gets 5 ~ 15 pieces, preferably 8 ~ 12 pieces, and washing tower spray liquid entrance is at washing tower from top to bottom between 3rd ~ 6 blocks of column plates.The working pressure of washing tower is 0.05 ~ 0.2MPa, and temperature is-100 ~-150 DEG C.
In sledge-borne type associated gas liquefaction system of the present invention, described washing tower arranges liquid phase side take-off mouth, and side take-off mouth from top to bottom between 4th ~ 8 blocks of column plates, mainly contains C in side take-off liquid phase at washing tower
2, C
3, C
4component, extraction liquid phase can be used as thick liquefied petroleum gas components.
In sledge-borne type associated gas liquefaction system of the present invention, described stage compression unit comprises the above compressor of two-stage, water cooler and point flow container, and preferred two-stage compressor, stage compression unit top hole pressure is 2 ~ 4MPa.Described compressor can adopt liquid-ring compressor, screw compressor or screw-type compressor, preferred screw-type compressor.
In sledge-borne type associated gas liquefaction system of the present invention, described imported compressor and refrigeration compressor can adopt liquid-ring compressor, screw compressor or screw-type compressor.Described imported compressor top hole pressure is 0.1 ~ 0.2MPa, and refrigeration compressor top hole pressure is 4 ~ 6MPa.Described refrigeration throttling valve downstream pressure is 0.1 ~ 3.5MPa, preferably 0.3 ~ 2.5MPa.
In sledge-borne type associated gas liquefaction system of the present invention, described gas-liquid direct-contact interchanger can be vertical, horizontal, preferably vertical.
In sledge-borne type associated gas liquefaction system of the present invention, described purification system is membrane separation unit, molecular sieve adsorption device or chemical absorption arrangement.
In sledge-borne type associated gas liquefaction system of the present invention, gas converting heat technology, natural gas conditioning technology, expenditure and pressure method and associated viscera are the contents known by technician.
Compared with prior art, sledge-borne type associated gas liquefaction system tool of the present invention has the following advantages.
1, in liquefaction system of the present invention, the high methane gas entered in refrigerant separator is divided into gas-liquid two-phase wherein, wherein gas phase is as the refrigeration agent of ice chest, and liquid phase returns mass transfer that low temperature absorption tower is gaseous fraction in washing tower, liquefaction process provides power, by C most in associated gas
2above components condense is separated, and the methane concentration in tower top discharge gas can be made to be greater than 95%, and simplify the technical process of this device.
2, in the present invention, refrigeration agent, through overdraft, cooling, throttling sepn process, constitutes refrigeration system of the present invention, and refrigeration system takes full advantage of the compression refrigerating system of band current regulator.Thus effectively can improve cooling power, reach energy-conservation object further.
3, the present invention adopts the direct contact mass transfer heat transfer of gas-liquid two-phase, substantially increases the utilization ratio of cold in system, makes C in associated gas
4above components condense is separated, and reclaims and obtains raw gasline component, thus reduces operation energy consumption and the follow-up equipment investment of apparatus of the present invention.
4, present invention achieves effective separation of associated gas different components, associated gas, after the inventive method process, recyclablely obtains raw gasline component, liquefied gas component and highly purified natural gas liquids.It is simple that the inventive method has flow process, the advantages such as system energy consumption is low, reduced investment.
Accompanying drawing explanation
Fig. 1 is a kind of detailed process schematic flow sheet of sledge-borne type associated gas liquefaction system of the present invention.
Embodiment
Further illustrate particular case of the present invention below by specific embodiment, but be not limited to following embodiment.
The invention provides a kind of sledge-borne type associated gas liquefaction system, described system comprises imported compressor 2, purification system 3, unstripped gas interchanger 4, gas-liquid direct-contact interchanger 5, washing tower 8, stage compression unit 14, liquefied gas interchanger 16, liquefaction throttling valve 17, LNG tank 18, refrigeration compressor 20, refrigeration throttling valve 21 and refrigerant separator 22, wherein, raw material associated gas passes through inlet line 1 successively through imported compressor 2, purification system 3 is connected with gas-liquid direct-contact interchanger unstripped gas entrance 6 with unstripped gas interchanger 4, gas-liquid direct-contact interchanger gaseous phase outlet 7 is connected with washing tower unstripped gas entrance 12 by pipeline, wash tower bottoms outlet is divided into two-way, one tunnel is connected with gas-liquid direct-contact interchanger spray liquid entrance 10, another road is connected with the spray liquid entrance 11 of washing tower, washing tower top gaseous phase outlet 13 is connected with stage compression unit entrance 15 by unstripped gas interchanger 4, described washing tower is also provided with side take-off mouth, stage compression unit outlet 19 is divided into two-way, one tunnel is connected with LNG tank 18 through liquefied gas interchanger 16, liquefaction throttling valve 17 successively, another road is connected with refrigerant separator 22 through refrigeration compressor 20, refrigeration throttling valve 21 successively, refrigerant separator top exit 24 is connected with stage compression unit entrance 15 by liquefied gas interchanger 16, goes out 23 mouthfuls and be connected with washing tower top reflux inlet 26 by pipeline bottom refrigerant separator.
As shown in Figure 1, the concrete technology flow process of the inventive method is as follows: raw material associated gas enters imported compressor by inlet line, enters purification system 3 process by imported compressor 2 after being compressed to 0.1 ~ 0.2MPa; Raw material associated gas after purification carries out heat exchange with the overhead gas from washing tower 8 in unstripped gas interchanger 4, associated gas temperature is reduced to-10 DEG C ~-30 DEG C, then enter in gas-liquid direct-contact interchanger 5, with from the lime set countercurrent heat-transfer mass transfer at the bottom of washing tower tower, associated gas is cooled to-50 DEG C ~-80 DEG C further, meanwhile, C in associated gas
4above most of heavy constituent is condensed separations, and by the discharge of gas-liquid direct-contact interchanger 5 outlet at bottom, isolated lime set can be used as raw gasline component.Raw material associated gas enters washing tower 8 after twice cooling down, washings countercurrent heat-transfer mass transfer in tower that associated gas enters in washing tower 8 and by washing tower spray liquid entrance 11, after washing, tower top obtains high methane gas, wherein the content of methane is greater than 95%, and the temperature of tower top high methane gas is reduced to-120 ~-150 DEG C.Washing tower stage casing arranges side take-off mouth, main containing C in side take-off liquid phase
2, C
3, C
4component, extraction liquid phase can be used as thick liquefied petroleum gas components.Lime set at the bottom of washing tower tower is divided into two portions after condensate pump 9 promotes, wherein a part enters gas-liquid direct-contact interchanger 5 as the spray liquid of gas-liquid direct-contact interchanger 5 through the spray liquid entrance 10 of direct-contact heat-exchanger, a part as washing tower spray liquid through washing tower spray liquid entrance 11 times washing towers 8, stage compression is carried out after washing tower tower top high methane gas and the heat exchange of raw material associated gas, be compressed to after pressure is 2 ~ 4MPa through stage compression unit and be divided into two-way, wherein, one tunnel is through liquefied gas interchanger 16 heat exchange, then after the throttling of liquefaction throttling valve 17, natural gas liquids is obtained, and send into storage in LNG tank 18, another road is compressed to 4 ~ 6MPa through refrigeration compressor 20, then to be reduced pressure throttling refrigeration by refrigeration throttling valve 21, control downstream pressure is 0.1 ~ 3.5MPa, gas is gas-liquid two-phase after throttling, two-phase fluid realizes two-phase laminated flow in refrigerant separator 22, wherein gas phase is as the heat-eliminating medium of liquefied gas interchanger 16, enter in stage compression unit 14 through heat exchange Posterior circle, the liquid obtained bottom refrigerant separator is back in washing tower by washing tower top reflux inlet 26 as the tower top washings of washing tower 8.
Embodiment 1
In the present embodiment, the stabilization of crude oil gas composition of certain joint station, in table 1, adopts the composition of natural gas liquids, washing tower overhead gas, thick liquefied petroleum gas components and the raw gasline component product obtained in native system production liquefied gas process in table 2.
In the present embodiment, described stage compression unit comprises two-stage compressor, described gas-liquid direct-contact interchanger is vertical, described column plate of washing column number is 10 pieces, side take-off mouth is positioned at washing tower from top to bottom on the 5th block of column plate, and washing tower spray liquid entrance is positioned at washing tower from top to bottom on the 3rd block of column plate.
Raw material associated gas through imported compressor compression after pressure to 0.1MPa, associated gas temperature after the heat exchange of gas-liquid direct-contact interchanger is down to-70 DEG C, then cold washing tower bottom is entered, the working pressure of cold washing tower is 0.05MPa, temperature is-120 ~-150 DEG C, overhead gas is after heat exchange, temperature is down to-150 DEG C, then stage compression unit is entered, 1.9MPa is compressed to through stage compressor, 3.8 MPa are compressed to again through two stage compressor, then two-way is divided into, wherein a road is through liquefied gas interchanger heat exchange extremely-140 DEG C, 0.103 MPa is depressurized to further through liquefaction throttling valve, temperature is reduced to-162 DEG C, now obtain natural gas liquids, send in LNG tank, another road is compressed to 5MPa through refrigeration compressor, through refrigeration throttling valve reducing pressure by regulating flow to 0.103 MPa, in gas-liquid two-phase after throttling, two-phase fluid realizes two-phase laminated flow in refrigerant separator 22, wherein gas phase is as the heat-eliminating medium of liquefied gas interchanger 16, enter in stage compression unit 14 through heat exchange Posterior circle, the liquid obtained bottom refrigerant separator is back in washing tower by washing tower top reflux inlet 26 as the tower top washings of washing tower 8.Associated gas, after the process of this device, can obtain natural gas liquids, thick liquefied petroleum gas components and raw gasline component.
Table 1 raw material associated gas forms
| Composition | C 1 | C 2 | C 3 | iC 4 | nC 4 | iC 5 | nC 5 | C 6 | C 6 + | N 2 | CO 2 |
| mol% | 50.7 | 18.9 | 14.5 | 2.4 | 6.1 | 1.1 | 1.1 | 0.8 | 1.2 | 2.1 | 1.1 |
Table 2 product forms
| Logistics content, mol% | C 1 | C 2 | C 3 | iC 4 | nC 5 | iC 5 | nC 5 | C 6 | C 6 + |
| Raw gasline component | 5 | 24 | 25.2 | 17.5 | 28.3 | ||||
| Washing tower overhead gas | 96.5 | 2.3 | 1.2 | ||||||
| Natural gas liquids | 96.5 | 2.3 | 1.2 | ||||||
| Thick liquefied petroleum gas (LPG) | 1.5 | 62 | 10.4 | 25.1 | 1 |
Claims (10)
1. a sledge-borne type associated gas liquefaction system, described liquefaction system comprises imported compressor group, purification system, unstripped gas interchanger, gas-liquid direct-contact interchanger, washing tower, stage compression unit, liquefied gas interchanger, liquefaction throttling valve, LNG tank, wherein, raw material associated gas passes through inlet line successively through imported compressor group, purification system is connected with gas-liquid direct-contact interchanger unstripped gas entrance with unstripped gas interchanger, gas-liquid direct-contact interchanger gaseous phase outlet is connected with washing tower unstripped gas entrance by pipeline, wash tower bottoms outlet is divided into two-way, one tunnel is connected with gas-liquid direct-contact interchanger spray liquid entrance, another road is connected with the spray liquid entrance of washing tower, washing tower top gaseous phase outlet is connected with stage compression unit entrance by unstripped gas interchanger, it is characterized in that: described liquefaction system also comprises refrigeration compressor, refrigeration throttling valve and refrigerant separator, described stage compression unit outlet is divided into two-way, one tunnel is connected with LNG tank through liquefied gas interchanger, liquefaction throttling valve successively, another road is connected with refrigerant separator through refrigeration compressor, refrigeration throttling valve successively, refrigerant separator top exit is connected with stage compression unit entrance by liquefied gas interchanger, and refrigerant separator outlet at bottom is connected with washing tower top reflux inlet by pipeline.
2. according to system according to claim 1, it is characterized in that: described washing tower is the rectifying tower only having stripping section, washing tower theoretical plate number is 5 ~ 15 pieces.
3. according to system according to claim 1, it is characterized in that: described washing tower arranges side take-off mouth, side take-off mouth is at washing tower from top to bottom between 4th ~ 8 blocks of column plates.
4. according to system according to claim 1, it is characterized in that: described washing tower spray liquid entrance is at washing tower from top to bottom between 3rd ~ 6 blocks of column plates.
5. according to system according to claim 1, it is characterized in that: the working pressure of described washing tower is 0.05 ~ 0.2MPa, and temperature is-100 ~-150 DEG C.
6. according to system according to claim 1, it is characterized in that: described stage compression unit comprises the above compressor of two-stage, and compressor can adopt liquid-ring compressor, screw compressor or screw-type compressor.
7. according to system according to claim 1, it is characterized in that: described imported compressor group top hole pressure is 0.1 ~ 0.2MPa, stage compression unit top hole pressure is 2 ~ 4MPa, and refrigeration compressor top hole pressure is 4 ~ 6MPa, and refrigeration throttling valve downstream pressure is 0.1 ~ 3.5MPa.
8. according to system according to claim 7, it is characterized in that: refrigeration throttling valve downstream pressure is 0.3 ~ 2.5MPa.
9. according to system according to claim 1, it is characterized in that: it is characterized in that: described gas-liquid direct-contact interchanger is vertical or horizontal.
10. according to system according to claim 1, it is characterized in that: described purification system is membrane separation unit, molecular sieve adsorption device or chemical absorption arrangement.
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| CN104941231B (en) * | 2015-06-16 | 2017-03-22 | 浙江省天正设计工程有限公司 | Non-condensable gas containing rectification exhaust gas recovery technology and device |
| CN107664265B (en) * | 2016-07-29 | 2023-07-14 | 北京航天动力研究所 | Skid-mounted pressure regulating system |
| CN113387364B (en) * | 2021-05-08 | 2023-02-28 | 内蒙古新特硅材料有限公司 | Method and system for treating cold hydrogenation synthesis gas |
| CN114484279A (en) * | 2022-03-21 | 2022-05-13 | 广东肯富来泵业股份有限公司 | Oil field associated gas recovery liquid ring multi-stage compressor system and method |
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