CN108641769A - A kind of recovery method of associated gas - Google Patents
A kind of recovery method of associated gas Download PDFInfo
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- CN108641769A CN108641769A CN201810575982.5A CN201810575982A CN108641769A CN 108641769 A CN108641769 A CN 108641769A CN 201810575982 A CN201810575982 A CN 201810575982A CN 108641769 A CN108641769 A CN 108641769A
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Classifications
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L3/00—Gaseous fuels; Natural gas; Synthetic natural gas obtained by processes not covered by subclass C10G, C10K; Liquefied petroleum gas
- C10L3/12—Liquefied petroleum gas
-
- 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
- F25J3/08—Separating gaseous impurities from gases or gaseous mixtures or from liquefied gases or liquefied gaseous mixtures
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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
- F25J5/00—Arrangements of cold exchangers or cold accumulators in separation or liquefaction plants
Abstract
The present invention provides a kind of recovery methods of associated gas, two level gas-liquid separation, dehydration are carried out after the compressed cooling of gas phase of the raw material after level-one gas-liquid separation, liquid phase after level-one gas-liquid separation is flashed, is dehydrated, is stripped, and the gas phase after the gas phase stripped and flash distillation enters dehydration link after the cooling of 2 second compressions；Gas phase after dehydration and drying first cools down carries out low temperature gas-liquid separation afterwards, rejecting ethane is carried out after liquid phase heating after cryogenic separation, liquid phase after rejecting ethane carries out removing butane after heating, obtain liquid phase LPG products, Partial Liquid Phase condensate after removing butane as the gas phase after cryogenic separation in absorbent and liquefaction step carries out multistage mass transfer, heat transfer after cooling down, and the obtained gas phase after mass transfer, heat transfer is after supercooling, cryogenic separation, decompression and recycling cold as lean gas extraction.The present invention can recycle high value LPG products in associated gas, and using process efficiently, economic, substantially reduce production cost.
Description
Technical field
The invention belongs to Oilfield gas recycling and separation technology fields, more particularly, to a kind of recycling side of associated gas
Method.
Background technology
Traditional casing-head gas recovery method uses high pressure swell refrigeration technique or DHX techniques.
Unstripped gas is high pressure (about 60bar or so) in high pressure swell refrigeration technique, utilizes expansion process Joule Thompson section
It flows effect and generates low temperature, condense C in unstripped gas3、C4Etc. heavy constituents.DHX techniques are further using the precooling of propane ice maker and expanding machine
Refrigeration, wherein dethanizer further recycles C in lean gas using DHX techniques3、C4Component.
It is 20barg or so, C in unstripped gas for raw gas pressure3+C4Content 19% (vt) left and right, lean gas discharge pressure
For 20barg or so, the recycling of defeated pressure and the almost the same casing-head gas of raw gas pressure, swollen according to conventional high-tension outside lean gas
Unstripped gas need to be pressurized to 60bar by swollen refrigeration process by 20barg, and supercharging power consumption is very high, and is pressurized follow-up equipment and is
High-tension apparatus, it is uneconomical.According to DHX techniques, due to C in unstripped gas3Content is higher than 11% (vt), and heavy hydrocarbon can excessively cause to take off
Ethane column overhead temperatures are excessively high to destroy DHX techniques, DHX process advantage unobvious.Moreover, high pressure swell refrigeration technique and
The DHX technique LPG rate of recovery is not high, and generally only 80~90% or so.
Invention content
In view of this, the present invention is directed to propose a kind of recovery method of associated gas, can recycle high in associated gas
LPG products are worth, and using process efficiently, economic, substantially reduce production cost, the LPG rate of recovery is up to 99.8%.
In order to achieve the above objectives, the technical proposal of the invention is realized in this way：
A kind of recovery method of associated gas, raw material pass through following steps successively：Supercharging separation, liquefaction, refines dehydration
It is absorbed with cold oil；
Step 1：Supercharging separation
Raw material first passes through level-one gas-liquid separation, and two level gas-liquid point is carried out after the compressed cooling of gas phase after level-one gas-liquid separation
From the gas phase after two level gas-liquid separation enters dehydration link, and the liquid phase after level-one gas-liquid separation is flashed, the liquid phase after flash distillation
It is stripped after dehydrothermal, the gas phase after the gas phase stripped and flash distillation enters dehydration ring after the cooling of 2 second compressions
Section；
Step 2：Dehydration
Gas phase after two level gas-liquid separation is dehydrated；
Step 3：Liquefaction
Gas phase after dehydration and drying carries out low temperature gas-liquid separation, the liquid after low temperature gas-liquid separation after cooling, partial liquefaction
Mutually cold recovery heating is carried out again；
Step 4：It is refined
Liquid phase after heating up in step 3 carries out the light components such as rejecting ethane, the liquid phase warp after the light components such as rejecting ethane
Removing butane is carried out after crossing heating, then obtains liquid phase LPG products, remaining as condensate, a part of condensate is through cooling
Next step is entered as absorbent, remaining condensate is produced as product；
Step 5：Cold oil absorbs
Condensate carries out multistage mass transfer as the gas phase after cryogenic separation in absorbent and step 3 after supercooling, passes
Heat, the LPG components in gas phase in recycling step three after cryogenic separation,
Obtained gas phase after mass transfer, heat transfer is used as lean gas after supercooling, cryogenic separation, decompression and recycling cold
Extraction, the liquid phase obtained after mass transfer, heat transfer, return to step three.
Further, the liquid phase circulation after two level gas-liquid separation goes back to be flashed.
Further, the gas phase after the light components such as rejecting ethane produces after depressurizing and recycling cold as lean gas.
Further, in step 1, unstripped gas enters level-one gas-liquid separator and carries out gas-liquid separation, level-one gas-liquid separation
Through LPG components in flash tank reclaim liquid phase, flash tank bottom liquid phase is dehydrated liquid phase in device through decanter, dewatered oil phase warp
Enter stripper after pump, the heating of level-one preheater and further recycles LPG, gas phase that stripper top produces and flash drum overhead
Gas phase is pressurized through stage compressor, and stage compressor outlet gas phase enters level-one gas-liquid separator, level-one gas-liquid separation through cooling
The gas phase passed through at the top of device is pressurized through split-compressor, then again after cooling, gas-liquid separation is carried out into two level gas-liquid separator.
Further, stripper bottom oil phase extraction goes to condensate tank field to store after level-one preheater waste heat recovery, and two
The liquid phase of grade gas-liquid separator returns to flash tank.
Further, step 2 includes dewatering unit, and molecular sieve is housed in dewatering unit, dry using 4A molecular sieves
Depth requirements are -40 DEG C of the dew-point temperature of gas.
Further, in step 3, the oil gas after drying enters ice chest partial condensation, subsequently into one grade low-temp gas of downstream
Liquid/gas separator carries out gas-liquid separation, and the top gas phase of level-one low temperature gas-liquid separator goes downstream absorption tower further to recycle in gas phase
LPG components, the bottom liquid phases of level-one low temperature gas-liquid separator enter product purification unit after ice chest recycles cold and carry out essence
System.
Further, in step 4, the light components such as rejecting ethane are carried out in dethanizer, the bottom of tower of dethanizer
Oil phase enters debutanizing tower after secondary heat exchanger heats, and the tower top of debutanizing tower is qualification LPG products, and bottom of tower is condensate group
Divide C5 +。
Further, in step 5, condensate exchanges heat through secondary heat exchanger, and after cooling, pump pressurization, a part, which is used as, to be absorbed
Agent enters in the absorption tower of cold oil absorptive unit, and a part goes to tank field to store as condensation oil product, and absorbent is after cooling
It enters at the top of absorption tower, the gas phase at the top of level-one low temperature gas-liquid separator enters absorb the bottom of the tower, in absorption tower, inhales
It receives agent inversely to be contacted with from the gas phase at the top of level-one low temperature gas-liquid separator, carries out multistage mass transfer, heat transfer, recycle in gas phase
LPG components, absorb the bottom of the tower liquid phase, which enters after ice chest recycles cold in dethanizer recycle, to be refined.
Compared with the existing technology, the recovery method of associated gas of the present invention has the advantage that：
1, the defeated lime set generated in the process, a side are grown in pipe network using flash distillation, decantation and stripping tower process recycling unstripped gas
Face can improve LPG yields, on the other hand can reduce follow-up molecular sieve dehydration energy consumption；
2, setting high pressure supercharger is avoided, device power consumption and equipment investment are reduced；
3, refrigerating part uses pinch technology, level-one low temperature gas-liquid separator top gas phase, bottom liquid phases, deethanization tower top
Gas phase and cold oil are recycled into ice chest and carry out cold recovery, reduce propane ice maker refrigerating capacity, save device consumption；
4, refrigerating part uses ice chest technology, avoids generating gas-liquid two-phase when classification cold recovery, LPG is caused to lose；
5, it is cooled down using first pressurization, rear cold oil absorption technique, relative to traditional deep fat absorption technique, reduces cold oil absorbent
Dosage is recycled, to reduce plant energy consumption；
6, dethanizer is detached using high pressure, on the one hand can be reduced tower top refrigeration and be required, on the other hand can maintain tower
Defeated pressure outside lean gas is pushed up, defeated compressor outside setting lean gas is avoided.
Description of the drawings
Fig. 1 is the process flow chart of associated gas recycling.
Reference sign：
1- level-one gas-liquid separators；2- flash tanks；3- decanters；5- level-one preheaters；6- strippers；7- one stage of compression
Machine；9- split-compressors；11- two level gas-liquid separators；12- dewatering units；13- ice chests；15- level-one low temperature gas-liquid separators；
16- dethanizers；17- secondary heat exchangers；18- debutanizing towers；The absorption towers 22-；24- two level low temperature gas-liquid separators.
Specific implementation mode
In addition to being defined, technical term used in following embodiment has universal with those skilled in the art of the invention
The identical meanings of understanding.Test reagent used in following embodiment is unless otherwise specified conventional biochemical reagent；It is described
Experimental method is unless otherwise specified conventional method.
With reference to embodiment and attached drawing 1, the present invention will be described in detail.
A kind of recovery method of associated gas includes the following steps：Supercharging separation, dehydration, liquefaction, refined and cold oil are inhaled
It receives：
Step 1：Supercharging separation
Unstripped gas enters level-one gas-liquid separator 1 and carries out gas-liquid separation, and the liquid phase in level-one gas-liquid separator 1 is through flash tank
LPG components in 2 reclaim liquid phases, 2 bottom liquid phases of flash tank are dehydrated through decanter 3, and dewatered oil phase is through pump, level-one preheater 5
Enter the further recycling LPG of stripper 6 after heating, the control of butane content is in 0.3% (Mole percent in 6 bottom oil phase of stripper
Than) within.
The gas phase at 2 top of gas phase and flash tank that the top of stripper 6 produces is pressurized to 20barg through stage compressor 7, and one
Grade compressor 7 exports gas phase and enters level-one gas-liquid separator 1 through cooling, and the gas phase that 1 top of level-one gas-liquid separator passes through is through two level
Compressor 9 is pressurized to 31barg, is then cooled to 45 DEG C again, and gas-liquid separation, stripping are carried out into two level gas-liquid separator 11
6 bottom oil phase extraction of tower goes to condensate tank field to store after 5 waste heat recovery of level-one preheater, the liquid phase of two level gas-liquid separator 11
Flash tank 2 is returned to, wherein flashing pressure is 5barg.
Step 2：Dehydration
The gas phase isolated in two level gas-liquid separator 11 is entered in dewatering unit 12 and is dehydrated, in dewatering unit 12
Equipped with molecular sieve, using 4A molecular sieves, dry depth requirements are -40 DEG C of the dew-point temperature of gas.
Major function is that the moisture of unstripped gas is taken off, and avoids generating icing phenomenon in subsequent liquefaction.
Step 3:Liquefaction
Oil gas after drying enters 13 partial condensation of ice chest, is cooled to -30 DEG C, subsequently into one grade low-temp gas-liquid of downstream point
Gas-liquid separation is carried out from device 15, the top gas phase of level-one low temperature gas-liquid separator 15 goes the further recycling gas phase of downstream absorption tower 22
In LPG components, the bottom liquid phases of level-one low temperature gas-liquid separator 15 enter product purification unit after ice chest 13 recycles cold
It is refined.
Major function is the unstripped gas desuperheat that dehydration comes, and makes major part LPG components condensation (condensation in unstripped gas
While, liquid phase can be also condensed by also having a small amount of light component) become liquid phase, liquid phase removes dethanizer through cold recovery (heating)
It is refined in 16.
Step 4 refines
The light components such as rejecting ethane are carried out in dethanizer 16, and 16 main function of dethanizer is light group of ethane etc.
Divide and C3 points are opened, tower top is exactly the extraction of light component (C1+C2) gas phase, and bottom of tower is heavy constituent extraction (C3+C4).Dethanizer 16
Tower top pressure is controlled in 26barg, and reflux ratio is：1.6.The bottom of tower oil phase of dethanizer 16 heats laggard through secondary heat exchanger 17
Enter debutanizing tower 18, debutanizing tower 18 is mainly opened C4 and C5 points, and tower top produces for LPG (C3+C4), and bottom of tower is condensate
(C5+ or more) is produced.The tower top pressure of debutanizing tower 18 is controlled in 11barg, and reflux ratio is：1.2.The tower top of debutanizing tower 18
For qualified LPG products, bottom of tower is condensation oil ingredient C5 +, the overhead extraction gas phase of dethanizer 16 is decompressed to 20barg through J-T valves
It is used as lean gas to produce after recycling cold by ice chest 13.
Step 5, cold oil absorb
Condensate exchanges heat through secondary heat exchanger 17, and after cooling, pump pressurization, a part enters absorption tower 22 as absorbent
In, a part goes to tank field to store as condensation oil product, and absorbent enters 22 top of absorption tower after being cooled to -30 DEG C, come
Enter 22 bottom of absorption tower from the gas phase at the top of level-one low temperature gas-liquid separator 15, in absorption tower 22, absorbent with from level-one
The gas phase at 15 top of low temperature gas-liquid separator is inversely contacted, and is carried out multistage mass transfer, heat transfer, is recycled LPG components in gas phase.It inhales
Receipts 22 bottom liquid phases of tower, which enter after ice chest 13 recycles cold in dethanizer 16, recycle refined, the gas at the top of absorption tower 22
- 30 DEG C are mutually cooled to, condensation oil ingredient in gas phase is recycled, 22 operating pressure of absorption tower is controlled in 30barg.
The foregoing is merely illustrative of the preferred embodiments of the present invention, is not intended to limit the invention, all essences in the present invention
With within principle, any modification, equivalent replacement, improvement and so on should all be included in the protection scope of the present invention god.
Claims (9)
1. a kind of recovery method of associated gas, it is characterised in that：Raw material passes through following steps successively：Supercharging separation, dehydration,
Liquefaction, refined and cold oil absorb；
Step 1：Supercharging separation
Raw material first passes through level-one gas-liquid separation, and two level gas-liquid separation is carried out after the compressed cooling of gas phase after level-one gas-liquid separation,
Gas phase after two level gas-liquid separation enters dehydration link, and the liquid phase after level-one gas-liquid separation is flashed, the liquid phase warp after flash distillation
It is stripped after dehydrothermal, the gas phase after the gas phase stripped and flash distillation enters dehydration link after the cooling of 2 second compressions；
Step 2：Dehydration
Gas phase after two level gas-liquid separation is dehydrated；
Step 3：Liquefaction
Gas phase after dehydration and drying carries out low temperature gas-liquid separation after cooling, partial liquefaction, and the liquid phase after low temperature gas-liquid separation is again
Carry out cold recovery heating；
Step 4：It is refined
Liquid phase after heating up in step 3 carries out the light components such as rejecting ethane, and the liquid phase after the light components such as rejecting ethane is by adding
Removing butane is carried out after heat, then obtains liquid phase LPG products, remaining as condensate, a part of condensate is through the conduct that cools
Absorbent enters next step, and remaining condensate is produced as product；
Step 5：Cold oil absorbs
Condensate carries out multistage mass transfer, heat transfer after supercooling as the gas phase after cryogenic separation in absorbent and step 3, returns
The LPG components in the gas phase in step 3 after cryogenic separation are received,
Obtained gas phase after mass transfer, heat transfer is adopted after supercooling, cryogenic separation, decompression and recycling cold as lean gas
Go out, the liquid phase obtained after mass transfer, heat transfer, return to step three.
2. the recovery method of associated gas according to claim 1, it is characterised in that：Liquid phase after two level gas-liquid separation
It loops back and is flashed.
3. the recovery method of associated gas according to claim 2, it is characterised in that：After the light components such as rejecting ethane
Gas phase after depressurizing and recycling cold as lean gas produce.
4. the recovery method of associated gas according to claim 3, it is characterised in that：In step 1, unstripped gas into
Enter level-one gas-liquid separator (1) and carry out gas-liquid separation, the liquid phase in level-one gas-liquid separator (1) is through flash tank (2) reclaim liquid phase
Middle LPG components, flash tank (2) bottom liquid phases are dehydrated through decanter (3), and dewatered oil phase is heated through pump, level-one preheater (5)
LPG is further recycled into stripper (6) afterwards, the gas phase at the top of the gas phase produced at the top of stripper (6) and flash tank (2) is through one
Grade compressor (7) is pressurized, and stage compressor (7) exports gas phase and enters level-one gas-liquid separator (1), level-one gas-liquid separation through cooling
The gas phase passed through at the top of device (1) is pressurized through split-compressor (9), then again after cooling, into two level gas-liquid separator (11) into
Row gas-liquid separation.
5. the recovery method of associated gas according to claim 4, it is characterised in that：Stripper (6) bottom oil phase is adopted
Condensate tank field is gone to store after going out level-one preheater (5) waste heat recovery, the liquid phase of two level gas-liquid separator (11) returns to flash tank
(2)。
6. the recovery method of associated gas according to claim 3, it is characterised in that：Step 2 includes dewatering unit
(12), molecular sieve is housed, using 4A molecular sieves, dry depth requirements are -40 DEG C of the dew-point temperature of gas in drain sump (12).
7. the recovery method of associated gas according to claim 3, it is characterised in that：In step 3, the oil after drying
Gas enters ice chest (13) partial condensation, carries out gas-liquid separation subsequently into downstream level-one low temperature gas-liquid separator (15), level-one is low
The top gas phase of wet liquid/gas separator (15) goes downstream absorption tower (22) further to recycle the LPG components in gas phase, a grade low-temp
The bottom liquid phases of gas-liquid separator (15) are refined after ice chest (13) recycles cold into product purification unit.
8. the recovery method of associated gas according to claim 3, it is characterised in that：In step 4, rejecting ethane
Etc. light components be to carry out in the dethanizer (16), the bottom of tower oil phase of dethanizer (16) heats laggard through secondary heat exchanger (17)
Enter debutanizing tower (18), the tower top of debutanizing tower (18) is qualification LPG products, and bottom of tower is condensation oil ingredient C5 +。
9. the recovery method of associated gas according to claim 3, it is characterised in that：In step 5, condensate is through two
Grade heat exchanger (17) exchanges heat, and after cooling, pump pressurization, a part enters the absorption tower (22) of cold oil absorptive unit as absorbent
In, a part goes to tank field to store as condensation oil product, and absorbent is entered after cooling at the top of absorption tower (22), comes from level-one
Gas phase at the top of low temperature gas-liquid separator (15) enters absorption tower (22) bottom, in absorption tower (22), absorbent with from level-one
Gas phase at the top of low temperature gas-liquid separator (15) is inversely contacted, and is carried out multistage mass transfer, heat transfer, is recycled LPG components in gas phase,
Absorption tower (22) bottom liquid phases, which enter after ice chest (13) recycles cold in dethanizer (16) recycle, to be refined.
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| CN109653716A (en) * | 2018-10-29 | 2019-04-19 | 中国石油天然气集团有限公司 | Super-viscous oil is handled up development block closed gathering method and device |
| CN110093197A (en) * | 2019-05-23 | 2019-08-06 | 中国石油化工股份有限公司 | A kind of denitrogenation method and denitrification system for associated gas |
| CN111004657A (en) * | 2019-12-11 | 2020-04-14 | 中国天辰工程有限公司 | Method for comprehensively utilizing oilfield associated gas |
| CN111717915A (en) * | 2019-03-19 | 2020-09-29 | 中石化石油工程技术服务有限公司 | Method and device capable of improving capture rate of carbon dioxide in carbon dioxide flooding produced gas of oil field |
| CN112745974A (en) * | 2020-12-14 | 2021-05-04 | 中海石油(中国)有限公司 | Membrane separation method oilfield associated gas purification process and system based on adsorption dehydration pretreatment |
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| CN111717915A (en) * | 2019-03-19 | 2020-09-29 | 中石化石油工程技术服务有限公司 | Method and device capable of improving capture rate of carbon dioxide in carbon dioxide flooding produced gas of oil field |
| CN110093197A (en) * | 2019-05-23 | 2019-08-06 | 中国石油化工股份有限公司 | A kind of denitrogenation method and denitrification system for associated gas |
| CN110093197B (en) * | 2019-05-23 | 2024-04-26 | 中国石油化工股份有限公司 | Denitrification method and denitrification system for oilfield associated gas |
| CN111004657A (en) * | 2019-12-11 | 2020-04-14 | 中国天辰工程有限公司 | Method for comprehensively utilizing oilfield associated gas |
| CN111004657B (en) * | 2019-12-11 | 2021-04-27 | 中国天辰工程有限公司 | Method for comprehensively utilizing oilfield associated gas |
| CN112980489A (en) * | 2019-12-16 | 2021-06-18 | 天津深蓝化工技术有限公司 | Process method for recycling associated gas light hydrocarbon of open refrigeration oil field |
| CN112980489B (en) * | 2019-12-16 | 2023-08-08 | 天津深蓝化工技术有限公司 | Process method for recycling light hydrocarbons of associated gas of open refrigeration oilfield |
| CN112745974A (en) * | 2020-12-14 | 2021-05-04 | 中海石油(中国)有限公司 | Membrane separation method oilfield associated gas purification process and system based on adsorption dehydration pretreatment |
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