CN103525449A - Recycling process of oilfield associated gas light hydrocarbons - Google Patents
Recycling process of oilfield associated gas light hydrocarbons Download PDFInfo
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Abstract
A recycling process of oilfield associated gas light hydrocarbons comprises the following steps: a factory-outside provided oilfield associated gas successively passes through a raw material settling dehydration and impurity removal process, a skid-mounted unit gas-liquid separation process, a light hydrocarbon refining process, and a process wastewater waste hydrocarbon recovery process to produce purified dry gases, C3 and C4 liquefied gases and liquid hydrocarbons. The recycling process adopts a skid-mounted design and parallel arrangement of multiple skid-mounted units to effectively solve the adaptive capacity to sharp changes of processing amount of a device, and has the operating flexibility of 34 ~ 136%, heavy hydrocarbons and discharged gaseous hydrocarbons in the process wastewater are all recycled, all the process wastewater can be treated by recycling for reuse, all the dry gases can be effectively used, and the recycling process achieves zero emissions.
Description
Technical field
The present invention relates to petrochemical industry, the technique of recycling about hydrocarbon, particularly a kind of associated gas lighter hydrocarbons recovery is utilized technique.
Background technology
From associated gas, reclaim the frequent technique adopting of lighter hydrocarbons lime set and comprise oil-absorption process, absorption method, condensation method.Nearly more than 20 years built condensate recovery device adopt condensation method mostly both at home and abroad.It is exactly by the C2+(in associated gas or C3+ under certain pressure that condensation method reclaims lime set technique) component in the laggard row gas-liquid separation of cryogenic condensation to reach the object that reclaims associated gas lime set.Condensation separation is divided into the large class of shallow cold-peace deep cooling two, and the refrigeration temperature generally condensation process-25 ~-40 ℃ of left and right is shallow cold technique; The refrigeration temperature generally condensation process-90 ~-100 ℃ of left and right is cryogenic technology.In deep cooling retrieving arrangement, using refrigeration agent as auxiliary cold source, expander refrigeration is as the mixing refrigerating method of main low-temperature receiver, its refrigeration temperature is low, and the liquid hydrocarbon rate of recovery is high, to gas source condition conversion strong adaptability, the problems such as investment is large but exist, and energy consumption is high, and economic benefit is not good.
Conventionally the equipment that petrochemical system adopts belongs to main equipment more, and whole technique consists of a plurality of large-scale operating units, and under the prerequisite that can guarantee at raw material, this method can be raised the efficiency, and increases benefit.But when raw material can not reach the requirements for starting construction of large-scale plant, the deposit raw material of just having to stop work, will increase cost while again going into operation, and how to avoid this part expenditure, need to address from technological design.In CN102504860A, although improved technique, between gas-liquid separation and condenser, increase interchanger, also just used a set of compression process, when material gas quantity fluctuates, also have the problems such as malfunction.
The shallow cold recovery process of tradition, the dry gas C3+ component concentration after condensation process is still higher, larger to its further recovery difficult.In process of production, the device bottom such as raw material surge tank, minute flow container, separator all may be discharged waste liquid, and this waste liquid is hydrocarbonaceous waste water.Conventional processing mode is to discharge from sewage network, and this processing mode is the waste to resource.
Along with environmental regulation increasingly stringent, key industry energy-saving and emission-reduction and " zero " discharge gordian technique become the main contents of cleaner production and recycling economy technological development.
Associated gas process for recovering light hydrocarbon technological difficulties are: the adaptive faculty that (1) amount of finish significantly changes; (2) the zero release problem of waste water, useless hydrocarbon, waste gas.
Summary of the invention
The object of the invention is to overcome the deficiencies in the prior art, provide a kind of new associated gas lighter hydrocarbons recovery to utilize technique, can effectively solve associated gas amount of finish and significantly change adaptive faculty problem, and the recovery problem of waste water, useless hydrocarbon.
Object of the present invention is achieved by following scheme:
A kind of associated gas lighter hydrocarbons recovery is utilized technique, comprise the steps: associated gas first, processing wastewater useless hydrocarbon refining through raw material deposition dehydrating removing impurities, the gas-liquid separation of skid unit, lighter hydrocarbons reclaim, generate and purify dry gas C3, C4 liquefied gas and liquid hydrocarbon, skid unit adopts many cover skid units to be arranged in parallel, and the liquid, the gas that in the useless hydrocarbon removal process of processing wastewater, discharge all reclaim by hydrocarbon retrieving arrangement and raw material storage device;
Above-mentioned skid unit comprises unstripped gas compression sled, unstripped gas adsorption dry dehydration sled, the cold sled of raw material gas ammonia;
Above-mentioned many cover skid units are to adopt the described skid unit of 1 ~ 4 cover to be arranged in parallel;
Above-mentioned many cover skid units are arranged in parallel technological operation elasticity 34 ~ 136%;
In the useless hydrocarbon removal process of above-mentioned processing wastewater, the liquid of each tank bottom discharge is reclaimed with hydrocarbon retrieving arrangement, and the liquid of middle part discharge send feed-pipe reuse, and top expellant gas returns to raw material storage device;
In the useless hydrocarbon removal process of above-mentioned processing wastewater, the liquid of tank bottom discharge adopts with one-level compressor outlet gas force feed to hydrocarbon retrieving arrangement.
Beneficial effect of the present invention, employing skid design, the small-sized skid unit of many covers is in parallel, can be according to the corresponding amount of finish of associated gas change of production adjustment, compare with tradition list cover main equipment technique, flexibility ratio is higher, and avoiding, because oil and gas production deficiency causes the loss of stopping work and going into operation and causing, has increased the benefit of enterprise in the time of save energy.The isolated hydrocarbonaceous waste water of technological process gives up by waste water, and to realize hydrocarbon water separated for hydrocarbon recovery process, and isolated hydro carbons is delivered to feed-pipe reuse, and the waste water of generation, from being pressed onto circulating water pool, accomplishes that production waste " zero " discharges, and dry gas is all utilized effectively.
Accompanying drawing explanation
Fig. 1 is that a kind of associated gas lighter hydrocarbons recovery of the present invention is utilized technology process schema
Fig. 2 is that a kind of associated gas lighter hydrocarbons recovery of the present invention is utilized technique skid unit gas-liquid separation schema
Fig. 3 is the useless hydrocarbon recovery process schema of waste water
A. unstripped gas in figure, B. purifies dry gas, C. liquefied gas, D. light oil, E. works off one's feeling vent one's spleen from compressor one-level, F. raffinate, G. air-discharging
1-1. raw material surge tank, 1-2a/b/c/d. skid unit, 1-3. raffinate reclaims conveying pot, 1-4. deethanizing column, 1-5. deethanizing tower top ammonia cooler, 1-6. deethanizing tower top return tank, 1-7. deethanizing tower top reflux pump, 1-8. deethanizing bottom reboiler, 1-9. debutanizing tower, 1-10. debutylize tower top reflux pump, 1-11. debutylize tower top watercooler, 1-12. debutylize tower top return tank, 1-13. debutylize bottom reboiler, product pump at the bottom of 1-14. debutanizing tower, 1-15. stablizes light oil water cooler
2-1. one-level air inlet surge tank, 2-2. mono-stage compressor, 2-3. pneumatic press side cooler, minute flow container in the middle of 2-4. pneumatic press, 2-5. pneumatic press one-level outlet recooler, 2-6. pneumatic press one-level outlet secondary divides flow container, 2-7. adsorption dry tower, 2-8. dust filter unit, 2-9. " four plumes " interchanger, 2-10. ammonia evaporator, the cold raw material knockout drum of 2-11. ammonia
1. the unstripped gas after removal of impurities, 2. raffinate at the bottom of raw material surge tank tank, 3. free-water at the bottom of minute flow container tank in the middle of pneumatic press, 4. free-water at the bottom of two minutes flow container tanks, 5. the dry gas that deethanizing tower top return tank is discharged, 6. liquid at the bottom of the cold raw material knockout drum of ammonia tank, the 7. cold raw material knockout drum of ammonia tank deck dry gas
3-1. process spent water is collected and hydrocarbon withdrawing can, and 3-2. reclaims hydrocarbon pump
8. light hydrocarbon gas, 9. the raffinate coming at the bottom of one-level air inlet divides flow container, 10. from one-level, import and export the raffinate of surge tank, 11. divide the raffinate of flow container in the middle of pneumatic press, 12. raffinates that come from the cold raw material knockout drum of ammonia, the raffinate that 13. self-desiccation charging knockout drums come, 14. raffinates that come from coarse filter, 15. raffinates that come from oil removal filter, 16. self-desiccations divide the raffinate of flow container, 17. raffinates that come from dust filter unit, the raffinate that 18. autotomy hydraulic pressure tank sendings are come, 19. reclaim the process water after lighter hydrocarbons, 20. liquid hydrocarbons
Embodiment
Below in conjunction with accompanying drawing, by embodiment, technical scheme of the present invention is described further:
(1) by temperature≤40 ℃ of the external associated gas unstripped gas A of factory, pressure is 0.2～0.3MpaG approximately, flow 80000 ~ 90000Nm
3/ d, access to plant unstripped gas surge tank 1-1 first, the free-water that removes mechanical impurity and may bring into, free-water enters raffinate and reclaims conveying pot 1-3.
(2) the unstripped gas Fen Si road after removal of impurities enters 1 group of unstripped gas compression skid unit through flow control.Unstripped gas, after one-level air inlet surge tank 2-1 dewaters again, enters a stage compressor 2-2, and the gas after boosting is chilled to 40 ℃ of left and right through pneumatic press side cooler 2-3 and enters the middle minute flow container 2-4 of pneumatic press.At the bottom of tank, separate free-water 3, through automatic control, discharge and reclaim, in the middle of pneumatic press, divide the flow container 2-4 raw material vapour that flow out on top to enter pneumatic press one-level outlet recooler 2-5, the low-temperature receiver of this water cooler is " dry gas " that " four plumes " interchanger, the associated gas that separatory tank deck comes in the middle of pneumatic press is cooled to after 28 ℃～32 ℃ again, enter pneumatic press one-level outlet secondary and divide flow container 2-6 to carry out gas-liquid separation, the liquid 4 at the bottom of tank flows out and carries out hydrocarbon and water recovery through leve autocontrol valve.The gas hydrocarbon flowing out from tank deck, contain certain saturated vapor, deliver to charging at the bottom of the adsorption dry tower 2-7 in unstripped gas adsorption dry dehydration skid group, 4A globular molecule sieve is housed in adsorption dry tower, utilizes its strong water-absorbent, remove the minor amount of water in raw material, go out gas dew points at normal pressure≤-60 ℃ of adsorption dry tower, pressure 2.4MPa(a) dew point≤-32 ℃, while adopting 1 cover skid unit, turndown ratio 34%
The unstripped gas that goes out adsorption dry tower enters " four plumes " interchanger 2-9 after dust filter unit 2-8, in " four plumes " interchanger interchanger, thermal source is unstripped gas (one), low-temperature receiver is: bis-strands of the dry gas 5(that deethanizing tower top return tank is discharged), tri-strands of the dry gas 7(of the cold raw material knockout drum of ammonia 2-11 tank deck), tetra-strands of the liquid 6(at the bottom of the cold raw material knockout drum of ammonia).After this four plumes interchanger, unstripped gas temperature is down to approximately 5 ℃～10 ℃, reenter the further condensing cooling of ammonia evaporator 2-10 to-25 ℃, enter the cold raw material knockout drum of ammonia 2-11, at the bottom of tank, liquid 6 is controlled to entering deethanizing column 1-4 middle part after " four plumes " interchanger heat exchange and is carried out fractionation by distillation through liquid level.
(3) lighter hydrocarbons treating process is to carry out in deethanizing column and debutanizing tower, and the in-built High Efficient Standard Packing of filling out of tower adopts total reflux operation.The gas ejecting from deethanizing column 1-4 mainly contains C2, a small amount of C3 and oxygen, nitrogen, carbon dioxide.After deethanizing tower top ammonia cooler 1-5 condensing cooling, enter deethanizing tower top return tank 1-6, carry out gas-liquid separation, gas enters skid unit " four plumes " interchanger 2-9 after voltage-controlled valve, go out heat exchange temperature more than 0 ℃, with go out after the merging from the cold raw material knockout drum of ammonia top dry gas 7 of " four plumes " interchanger, the press one-level of degassing outlet recooler 2-5 makes low-temperature receiver, the dry gas that goes out pneumatic press one-level outlet recooler 2-5 is incorporated to dry gas and goes out device road, in return tank, liquid is extracted out with reflux pump 1-7, all entering deethanizing column 1-4 top refluxes.
At the bottom of deethanizing column 1-4, with vertical reboiler 1-8 heat supply, the effect of reboiler is in order to steam C1, C2, the CO in the oil of deethanizing column bottom
2deng.
Debutanizing tower 1-9 also adopts High Efficient Standard Packing, and the gas ejecting from debutanizing tower 1-9 enters watercooler 1-11 condensation, and the material that goes out watercooler enters debutylize tower top return tank 1-12 carries out gas, liquid is separated.A small amount of C1, C2 and CO
2deng, enter dry gas pipeline after voltage-controlled and go out device.Liquid is extracted out with pump 1-10, and a part is made trim the top of column, and a part is sent the Spherical Tank Area to device as liquefied gas C.
In unstripped gas adsorption dry dehydration skid group, be provided with reprocessing cycle system, flow process trend is: first from unstripped gas, enter the pipeline of moisture eliminator, introduce proper amount of gas and enter dry regeneration forced air cooler.After cooling, enter dry regeneration minute flow container.Remove phlegma (water and a small amount of hydrocarbon), tank deck gas, after recirculation blower supercharging, enters regeneration electric heater, after intensification, entering the tool top of molecular sieve adsorption in dry (has two tools, wherein a tool operation, one tool regeneration, Program alternation carries out), make the molecular sieve desorb dehydration in adsorption dry tower, the resurgent gases that water content is large flows out from adsorption dry tower bottom, enter to be dried regeneration forced air cooler by water condensation, enter bottom and discharge, top gas enters recirculation blower again, continues dehydration cycle.
Drying and dehydrating gas is closed cycle, just introduces first, suitably supplements as required later.
(4) the useless hydrocarbon removal process of processing wastewater: be that the liquid of discharge is concentrated and put into raffinate conveying pot 1-3 at the bottom of unstripped gas surge tank 1-1, one-level air inlet surge tank 2-1, dry regeneration minute flow container tank, then reclaimed with one-level compressor outlet gas force feed to process spent water collection and hydrocarbon withdrawing can 3-1.From compressor one-level work off one's feeling vent one's spleen that E collects raffinate force feed to process spent water and hydrocarbon withdrawing can 3-1 after return in raw material surge tank 1-1, reclaim.
The liquid of discharging at the bottom of other tank, controls through liquid level, and the closed circuit hydrocarbon withdrawing can 3-1 that puts into, is divided into " three-phase " at this tank, and unstripped gas surge tank 1-1 inlet pipe, for the light hydrocarbon gas 8 containing saturation vapour, is returned in top, is reclaimed; Middle part is liquid hydrocarbon 20, and by hydrocarbon recovery pump, 3-2 extracts out, delivers to deethanizing column 1-4 feed-pipe and reclaims; At the bottom of tank, " waste water " does not contain mink cell focus, and in water, institute's hydrocarbon-containifirst amount is few, is certainly depressed into circulating water pool.Because this water is the water of condensation reclaiming, water quality is fine, can be used as the make up water of recirculated water, accomplishes production waste zero release.
(1) by temperature≤40 ℃ of the external associated gas unstripped gas A of factory, pressure is 0.8～1.2MpaG approximately, flow 300000 ~ 360000Nm
3/ d, access to plant unstripped gas surge tank 1-1 first, the free-water that removes mechanical impurity and may bring into, free-water enters raffinate and reclaims conveying pot 1-3.
(2) the unstripped gas Fen Si road after removal of impurities enters 1 group of unstripped gas compression skid unit through flow control.Unstripped gas, after one-level air inlet surge tank 2-1 dewaters again, enters a stage compressor 2-2, and the gas after boosting is chilled to 40 ℃ of left and right through pneumatic press side cooler 2-3 and enters the middle minute flow container 2-4 of pneumatic press.At the bottom of tank, separate free-water 3, through automatic control, discharge and reclaim, in the middle of pneumatic press, divide the flow container 2-4 raw material vapour that flow out on top to enter pneumatic press one-level outlet recooler 2-5, the low-temperature receiver of this water cooler is " dry gas " that " four plumes " interchanger, the associated gas that separatory tank deck comes in the middle of pneumatic press is cooled to after 28 ℃～32 ℃ again, enter pneumatic press one-level outlet secondary and divide flow container 2-6 to carry out gas-liquid separation, the liquid 4 at the bottom of tank flows out and carries out hydrocarbon and water recovery through leve autocontrol valve.The gas hydrocarbon flowing out from tank deck, contain certain saturated vapor, deliver to charging at the bottom of the adsorption dry tower 2-7 in unstripped gas adsorption dry dehydration skid group, 4A globular molecule sieve is housed in adsorption dry tower, utilizes its strong water-absorbent, remove the minor amount of water in raw material, go out gas dew points at normal pressure≤-60 ℃ of adsorption dry tower, pressure 2.4MPa(a) dew point≤-32 ℃, while adopting 4 cover skid unit, turndown ratio 136%
The unstripped gas that goes out adsorption dry tower enters " four plumes " interchanger 2-9 after dust filter unit 2-8, in " four plumes " interchanger interchanger, thermal source is unstripped gas (one), low-temperature receiver is: bis-strands of the dry gas 5(that deethanizing tower top return tank is discharged), tri-strands of the dry gas 7(of the cold raw material knockout drum of ammonia 2-11 tank deck), tetra-strands of the liquid 6(at the bottom of the cold raw material knockout drum of ammonia).After this four plumes interchanger, unstripped gas temperature is down to approximately 5 ℃～10 ℃, reenter the further condensing cooling of ammonia evaporator 2-10 to-25 ℃, enter the cold raw material knockout drum of ammonia 2-11, at the bottom of tank, liquid 6 is controlled to entering deethanizing column 1-4 middle part after " four plumes " interchanger heat exchange and is carried out fractionation by distillation through liquid level.
(3) lighter hydrocarbons treating process is to carry out in deethanizing column and debutanizing tower, and the in-built High Efficient Standard Packing of filling out of tower adopts total reflux operation.The gas ejecting from deethanizing column 1-4 mainly contains C2, a small amount of C3 and oxygen, nitrogen, carbon dioxide.After deethanizing tower top ammonia cooler 1-5 condensing cooling, enter deethanizing tower top return tank 1-6, carry out gas-liquid separation, gas enters skid unit " four plumes " interchanger 2-9 after voltage-controlled valve, go out heat exchange temperature more than 0 ℃, with go out after the merging from the cold raw material knockout drum of ammonia top dry gas 7 of " four plumes " interchanger, the press one-level of degassing outlet recooler 2-5 makes low-temperature receiver, the dry gas that goes out pneumatic press one-level outlet recooler 2-5 is incorporated to dry gas and goes out device road, in return tank, liquid is extracted out with reflux pump 1-7, all entering deethanizing column 1-4 top refluxes.
At the bottom of deethanizing column 1-4, with vertical reboiler 1-8 heat supply, the effect of reboiler is in order to steam C1, C2, the CO in the oil of deethanizing column bottom
2deng.
Debutanizing tower 1-9 also adopts High Efficient Standard Packing, and the gas ejecting from debutanizing tower 1-9 enters watercooler 1-11 condensation, and the material that goes out watercooler enters debutylize tower top return tank 1-12 carries out gas, liquid is separated.A small amount of C1, C2 and CO
2deng, enter dry gas pipeline after voltage-controlled and go out device.Liquid is extracted out with pump 1-10, and a part is made trim the top of column, and a part is sent the Spherical Tank Area to device as liquefied gas C.
In unstripped gas adsorption dry dehydration skid group, be provided with reprocessing cycle system, flow process trend is: first from unstripped gas, enter the pipeline of moisture eliminator, introduce proper amount of gas and enter dry regeneration forced air cooler.After cooling, enter dry regeneration minute flow container.Remove phlegma (water and a small amount of hydrocarbon), tank deck gas, after recirculation blower supercharging, enters regeneration electric heater, after intensification, entering the tool top of molecular sieve adsorption in dry (has two tools, wherein a tool operation, one tool regeneration, Program alternation carries out), make the molecular sieve desorb dehydration in adsorption dry tower, the resurgent gases that water content is large flows out from adsorption dry tower bottom, enter to be dried regeneration forced air cooler by water condensation, enter bottom and discharge, top gas enters recirculation blower again, continues dehydration cycle.
Drying and dehydrating gas is closed cycle, just introduces first, suitably supplements as required later.
(4) the useless hydrocarbon removal process of processing wastewater: be that the liquid of discharge is concentrated and put into raffinate conveying pot 1-3 at the bottom of unstripped gas surge tank 1-1, one-level air inlet surge tank 2-1, dry regeneration minute flow container tank, then reclaimed with one-level compressor outlet gas force feed to process spent water collection and hydrocarbon withdrawing can 3-1.From compressor one-level work off one's feeling vent one's spleen that E collects raffinate force feed to process spent water and hydrocarbon withdrawing can 3-1 after return in raw material surge tank 1-1, reclaim.
The liquid of discharging at the bottom of other tank, controls through liquid level, and the closed circuit hydrocarbon withdrawing can 3-1 that puts into, is divided into " three-phase " at this tank, and unstripped gas surge tank 1-1 inlet pipe, for the light hydrocarbon gas 8 containing saturation vapour, is returned in top, is reclaimed; Middle part is liquid hydrocarbon 20, and by hydrocarbon recovery pump, 3-2 extracts out, delivers to deethanizing column 1-4 feed-pipe and reclaims; At the bottom of tank, " waste water " does not contain mink cell focus, and in water, institute's hydrocarbon-containifirst amount is few, is certainly depressed into circulating water pool.Because this water is the water of condensation reclaiming, water quality is fine, can be used as the make up water of recirculated water, accomplishes production waste zero release.
Claims (6)
1. an associated gas lighter hydrocarbons recovery is utilized technique, comprise the steps: associated gas first, processing wastewater useless hydrocarbon refining through raw material deposition dehydrating removing impurities, the gas-liquid separation of skid unit, lighter hydrocarbons reclaim, generate and purify dry gas C3, C4 liquefied gas and liquid hydrocarbon, is characterized in that: described skid unit adopts many cover skid units to be arranged in parallel; The liquid, the gas that in the useless hydrocarbon removal process of described processing wastewater, discharge all reclaim by hydrocarbon retrieving arrangement and raw material storage device.
2. a kind of associated gas lighter hydrocarbons recovery according to claim 1 is utilized technique, it is characterized in that: described skid unit comprises unstripped gas compression sled, unstripped gas adsorption dry dehydration sled, the cold sled of raw material gas ammonia.
3. a kind of associated gas lighter hydrocarbons recovery according to claim 1 is utilized technique, it is characterized in that: described many cover skid units are to adopt the described skid unit of 1 ~ 4 cover to be arranged in parallel.
4. a kind of associated gas lighter hydrocarbons recovery according to claim 1 is utilized technique, it is characterized in that: adopt described many cover skid units to be arranged in parallel technological operation elasticity 34 ~ 136%.
5. a kind of associated gas lighter hydrocarbons recovery according to claim 1 is utilized technique, it is characterized in that: in the useless hydrocarbon removal process of described processing wastewater, the liquid of each tank bottom discharge send hydrocarbon retrieving arrangement to be reclaimed, the liquid of middle part discharge send feed-pipe reuse, and top expellant gas returns to raw material storage device.
6. a kind of associated gas lighter hydrocarbons recovery according to claim 5 is utilized technique, it is characterized in that: in the useless hydrocarbon removal process of described processing wastewater, the liquid of tank bottom discharge adopts one-level compressor outlet gas force feed to hydrocarbon retrieving arrangement.
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Cited By (1)
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| CN107746146A (en) * | 2017-11-28 | 2018-03-02 | 北京合众思流体技术有限公司 | Handle high-salt wastewater skid-mounted unit, its evaporation and concentration structure and method of wastewater treatment |
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Application publication date: 20140122 |