CN103773529A - Pry-mounted associated gas liquefaction system - Google Patents
Pry-mounted associated gas liquefaction system Download PDFInfo
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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 system that Sweet natural gas is produced in liquefaction take Sweet natural gas, coal-seam gas or other high methane gass as raw material production.
Background technology
Sweet natural gas and coal, oil are also called three large pillars of world's primary energy source.Sweet natural gas refers under earth's surface hydro carbons and non-hydrocarbons mixture born in pore formation, normal with crude oil association together with, take methane as main, and comprises than the hydro carbons of methane weight: as ethane, propane, normal butane, Trimethylmethane, Skellysolve A, iso-pentane etc.Except hydrocarbon, also may there is the gases such as a small amount of moisture, nitrogen, carbonic acid gas, hydrogen sulfide, oxygen, argon.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, and oil field emptying natural gas emptying is burnt, and has not only greatly wasted resource, and severe contamination the atmosphere 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, accounting for 13. 4% of national gas field sum, all the other gas fields of 86. 6% are small-sized gas field.For the less scattered gas field of 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 of the market for natural gas of entering.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, China approximately has 1,600,000,000 m every year
3oil field emptying natural gas emptying is burnt.Therefore, economical, reasonably develop side area natural gas source, changes resource is production capacity, reduces field area topsoil, has become the industrial problem anxious to be resolved of development China's natural gas.
The comprehensive utilization of oil-gas field side area associated gas resource is different from large gas utilization, must be based on disperseing internal market and the neighboring markets of well, block of cells well (or working district), 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, oil-gas field is implemented to rolling development.
The recovery method of patent CN1515651A small-sized skid Sweet natural gas lighter hydrocarbons, this patent adopts ammonia refrigeration can produce lighter hydrocarbons, liquefied gas, dry gas etc.But it is not suitable for the recycling without the frontier area natural gas in oil and gas fields of pipe network, and dry gas cannot enter pipe network.The small-sized sledge dress of mono-kind of patent CN03134159.4 Sweet natural gas methods of light hydrocarbon recovery, natural gas via overdraft, cooling, absorb, stable after 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 two processes of cryogenic refrigeration.
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 yield 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 refrigeration agent 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 refrigeration agent separator through refrigeration compressor, refrigeration throttling valve successively, refrigeration agent separator top exit is connected with stage compression unit entrance by liquefied gas interchanger, and refrigeration agent 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 that only has stripping section, gas enters at the bottom of by tower, tower top goes out, overhead gas has partial reflux through compression condensation, by regulating the amount of refrigerant gas and the downstream pressure of refrigeration throttling valve, control ratio and the temperature of withdrawing fluid, guarantee the content value of methane in overhead gas.Washing tower number of theoretical plate is got 5～15, and preferably 8～12, 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 ℃.
In sledge-borne type associated gas liquefaction system of the present invention, described washing tower arranges liquid phase side line extraction mouth, and side line extraction mouth from top to bottom between 4th～8 blocks of column plates, mainly contains C in side line extraction liquid phase at washing tower
2, C
3, C
4component, extraction liquid phase can be used as thick liquefied petroleum gas (LPG) component.
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, preferably two-stage compressor, and stage compression unit top hole pressure is 2～4MPa.Described compressor can adopt liquid-ring compressor, screw compressor or screw-type compressor, preferably 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 device.
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 known contents of 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 entering in refrigeration agent separator is divided into gas-liquid two-phase therein, wherein gas phase is as the refrigeration agent of ice chest, and liquid phase is returned to mass transfer, the liquefaction process that low temperature absorption tower is gaseous fraction in washing tower power is provided, by most C in associated gas
2above components condense separates, and can make the methane concentration in tower top discharge gas 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, has formed refrigeration system of the present invention, and refrigeration system takes full advantage of the compression refrigerating system with current regulator.Thereby can effectively improve cooling power, further reach energy-conservation object.
3, the present invention adopts the direct contact mass transfer of gas-liquid two-phase to conduct heat, and has fully improved the utilization ratio of cold in system, makes C in associated gas
4above components condense separates, and reclaim and obtain raw gasline component, thus the operation energy consumption of reduction apparatus of the present invention and follow-up equipment investment.
4, the present invention has realized effective separation of associated gas different components, associated gas through the inventive method process after, recyclable raw gasline component, liquefied gas component and the highly purified natural gas liquids of obtaining.The advantages such as it is simple that the inventive method has flow process, and 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 refrigeration agent 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 line extraction 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 18 successively, another road is connected with refrigeration agent separator 22 through refrigeration compressor 20, refrigeration throttling valve 21 successively, refrigeration agent separator top exit 24 is connected with stage compression unit entrance 15 by liquefied gas interchanger 6, and refrigeration agent separator bottom goes out 23 mouthfuls and is connected with washing tower top reflux inlet 26 by pipeline.
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, is compressed to and is entered purification system 3 after 0.1～0.2MPa and process by imported compressor 2; Raw material associated gas after purifying carries out heat exchange in unstripped gas interchanger 5 Yu from the overhead gas of washing tower 8, associated gas temperature is reduced to-10 ℃～-30 ℃, then enter in gas-liquid direct-contact interchanger 5, with the lime set countercurrent heat-transfer mass transfer from the bottom of washing tower tower, associated gas is further cooled to-50 ℃～-80 ℃, meanwhile, C in associated gas
4separations that be condensed of above most of heavy constituent, by the 5 outlet at bottoms discharges of gas-liquid direct-contact interchanger, isolated lime set can be used as raw gasline component.Raw material associated gas enters washing tower 8 after twice cooling down, associated gas in washing tower 8 with washings countercurrent heat-transfer mass transfer in tower of being entered 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 ℃.Washing tower stage casing arranges side line extraction mouth, in side line extraction liquid phase, mainly contains C
2, C
3, C
4component, extraction liquid phase can be used as thick liquefied petroleum gas (LPG) component.At the bottom of washing tower tower, lime set is divided into two portions after condensate pump 9 promotes, wherein a part enter 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 11 times washing towers 8 of washing tower spray liquid entrance, after washing tower tower top high methane gas and the heat exchange of raw material associated gas, carry out stage compression, be compressed to after pressure is 2～4MPa and be divided into two-way through stage compression unit, wherein, one tunnel is through 16 heat exchange of liquefied gas interchanger, then after 18 throttlings of liquefaction throttling valve, obtain natural gas liquids, and send in LNG tank 18 and to store, another road is compressed to 4～6MPa through refrigeration compressor 20, then by refrigeration throttling valve 21 throttling refrigeration that reduces pressure, control downstream pressure is 0.1 ~ 3.5MPa, gas is gas-liquid two-phase after throttling, two-phase fluid is realized two and is separated in refrigeration agent separator 22, wherein gas phase is as the heat-eliminating medium of liquefied gas interchanger 16, after heat exchange, circulate and enter in stage compression unit 14, the liquid that refrigeration agent separator bottom obtains 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 of certain joint station forms in table 1, adopts the composition of the natural gas liquids, washing tower overhead gas, thick liquefied petroleum gas (LPG) component and the raw gasline component product that obtain 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, side line extraction 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 after imported compressor compression pressure to 0.1MPa, associated gas temperature after the heat exchange of gas-liquid direct-contact interchanger is down to-70 ℃, then enter cold washing tower bottom, the working pressure of cold washing tower is 0.05MPa, temperature is-120～-150 ℃, overhead gas is after heat exchange, temperature is down to-150 ℃, then enter stage compression unit, through one-level compressor compresses to 1.9MPa, be compressed to 3.8 MPa through two stage compressor again, then be divided into two-way, wherein a road is through extremely-140 ℃ of liquefied gas interchanger heat exchange, further be depressurized to 0.103 MPa through liquefaction throttling valve, temperature is reduced to-162 ℃, 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, after throttling, be gas-liquid two-phase, two-phase fluid is realized two and is separated in refrigeration agent separator 22, wherein gas phase is as the heat-eliminating medium of liquefied gas interchanger 16, after heat exchange, circulate and enter in stage compression unit 14, the liquid that refrigeration agent separator bottom obtains is back in washing tower by washing tower top reflux inlet 24 as the tower top washings of washing tower 8.Associated gas, after this device is processed, can obtain natural gas liquids, thick liquefied petroleum gas (LPG) component and raw gasline component.
Table 1 raw material associated gas composition
| 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 composition
| 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 set, refrigeration throttling valve and refrigeration agent 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 refrigeration agent separator through refrigeration compressor set, refrigeration throttling valve successively, refrigeration agent separator top exit is connected with stage compression unit entrance by liquefied gas interchanger, and refrigeration agent separator outlet at bottom is connected with washing tower top reflux inlet by pipeline.
2. according to system claimed in claim 1, it is characterized in that: described cold washing tower is the rectifying tower that only has stripping section, washing tower theoretical plate number is 5～15.
3. according to system claimed in claim 1, it is characterized in that: described washing tower arranges side line extraction mouth, side line extraction mouth is at washing tower from top to bottom between 4th～8 blocks of column plates.
4. according to system claimed in 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 claimed in claim 1, it is characterized in that: the working pressure of described washing tower is 0.05～0.2MPa, temperature is-100～-150 ℃.
6. according to system claimed in 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 claimed in 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 set top hole pressure is 4～6MPa, and refrigeration throttling valve downstream pressure is 0.1～3.5MPa.
8. according to system claimed in claim 7, it is characterized in that: refrigeration throttling valve downstream pressure is 0.3～2.5MPa.
9. according to system claimed in 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 claimed in claim 1, it is characterized in that: described purification system is membrane separation unit, molecular sieve adsorption device or chemical absorption device.
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN104941231A (en) * | 2015-06-16 | 2015-09-30 | 浙江省天正设计工程有限公司 | Non-condensable gas containing rectification exhaust gas recovery technology and device |
| CN107664265A (en) * | 2016-07-29 | 2018-02-06 | 北京航天动力研究所 | A kind of skid-mounted type pressure regulating system |
| CN113387364A (en) * | 2021-05-08 | 2021-09-14 | 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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| CN107664265B (en) * | 2016-07-29 | 2023-07-14 | 北京航天动力研究所 | Skid-mounted pressure regulating system |
| CN113387364A (en) * | 2021-05-08 | 2021-09-14 | 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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| Publication number | Publication date |
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| CN103773529B (en) | 2015-05-13 |
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