CN202297494U - Device for recycling mixed hydrocarbon from oil associated gas - Google Patents
Device for recycling mixed hydrocarbon from oil associated gas Download PDFInfo
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- CN202297494U CN202297494U CN2011203696238U CN201120369623U CN202297494U CN 202297494 U CN202297494 U CN 202297494U CN 2011203696238 U CN2011203696238 U CN 2011203696238U CN 201120369623 U CN201120369623 U CN 201120369623U CN 202297494 U CN202297494 U CN 202297494U
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Abstract
The utility model provides a device for recycling mixed hydrocarbon from oil associated gas, which comprises a compressor and a first-stage condenser connected with the compressor. The first-stage condenser is connected with a molecular sieve, and a dew point detector is arranged at the outlet of the molecular sieve and connected to a second-stage condenser through a second-stage pre-cooling device. The oil associated gas mixed hydrocarbon recovery device can improve yield of the hydrocarbon reclaimed from associated gas, lowers energy consumption, reduces labor cost, is suitable for associated gas recovery of remote scattered wells, achieves miniaturization and automation, is convenient to install, saves energy for the country, and protects the environment.
Description
Technical field
The utility model relates to petrochemical industry, a kind of specifically recovery system of associated gas hydrocarbon mixture.
Background technology
Associated gas also is oil field gas, is the inflammable gas mixture of in the oil production process, following crude oil to overflow, and its component is generally methane, ethane, propane, butane etc.Because these inflammable gas mixtures can not directly discharge, the technology of recycling is complicated again, so a lot of oil field all is directly with its burning and exhausting.This burning and exhausting both caused severe contamination to environment, had wasted a large amount of inflammable gas energy again.
Traditional associated gas recovery way is to set up lighter hydrocarbons source mill, and this method device is complicated, and the speed of founding the factory is slow, is not easy to resettlement, and for the associated gas that scattered well produces, it is too huge to build the investment of lighter hydrocarbons source mill, is difficult to cost recovery.Therefore on the basis of light ends unit, develop the methods that following several kinds of recovery associated gases:
The expander refrigeration method: its earlier with the free-water of associated gas through separator separates; Gas after the separation gets into compressor, and pressure is compressed to 2.5MPa from about 0.2MPa, and the virgin gas temperature is less than 60 ℃ after air-cooled; Get into the compressor outlet oil-gas separator, get into molecular sieve dehydration equipment again; Separate the mixing low temp gas heat exchange that the back produces again with second-stage separator, the temperature of oil gas drops to about 25 ℃ from 60 ℃.Condensed liquid gets into first step separator; The ice chest that the gas of separating gets into refrigeration module carries out condensation; Temperature is cooled to subzero 40 ℃-subzero 60 ℃ from 25 ℃; Condensed gas gets into the secondary oil-gas separator to be separated, and the liquid that liquid after the separation and first step separator obtain gets into the hydrocarbon mixture storage tank.Discharge behind the heat exchange gas before isolating cryogenic gas of second-stage separator and the refrigeration.Its main flow process is referring to shown in the Figure of description 1.
Traditional ammonia or propane refrigeration method: its earlier with the free-water of associated gas through separator separates, the gas after the separation gets into compressor compresses, pressure is compressed to 1.0MPa from about 0.2MPa; The virgin gas temperature is less than 60 ℃ after air-cooled; Get into the compressor outlet oil-gas separator, get into molecular sieve dehydration equipment again, then separate the mixing low temp gas heat exchange that the back produces with second-stage separator; The temperature of oil gas drops to about 15 ℃ from 60 ℃; Condensed liquid gets into first step separator, and the ice chest that the gas of separating gets into refrigeration module carries out condensation, and temperature is cooled to subzero 40 ℃-subzero 50 ℃ from 15 ℃; Condensed gas gets into the secondary oil-gas separator to be separated, and the liquid that liquid after the separation and first step separator obtain gets into the hydrocarbon mixture storage tank.Behind the preceding heat exchange gas of isolating cryogenic gas of second-stage separator and refrigeration, discharger.Its main flow process is referring to shown in the Figure of description 2.
Temperature was lower when expander refrigeration was used for gas well gas (dry gas), but was used for C
3The associated gas that+component concentration is higher because a large amount of heavy hydrocarbons condenses into liquid, causes the expansion machine rotor load sharply to increase when decompressor is lowered the temperature, and rotating speed is slack-off, has had a strong impact on efficiency of expander and refrigeration temperature.
Ammonia or propane refrigeration system complex structure, ammonia refrigerant is comparatively huge, is suitable for large-scale refrigerating system.The propane refrigeration system EER is lower, and the propane compressor structure that realizes being equal to refrigerating duty is very huge.Propane and ammonia refrigerant all are inflammable substance, are difficult to realize automatic operating, and processing or misoperation are easy to cause potential safety hazard.
No matter be expander refrigeration or ammonia or propane refrigeration, structure is all comparatively huge, only is fit to on-the-spot the installation, is not easy to realize automatic operating.And traditional technology is paid little attention to molecular sieve dehydration; Be installed on the molecular sieve between feed gas compressor and the refrigeration plant; The virgin gas temperature that gets into molecular sieve receives the influence of envrionment temperature bigger, and drying effect is very unstable, and because of the relation of refrigerated heat exchanger structure; Therefore be prone to cause and freeze stifledly, hydrocarbon mixture production is usually stagnated.Some producers are prone to freeze stifled problem in order to solve interchanger; Adopted the gap bigger; Therefore the shell and tube heat exchanger that heat exchange efficiency is very low causes that the interchanger quality is big, floor space is big, and owing to usually be low-temperature heat exchange during B-grade condensation; Shell and tube heat exchanger need be used the stainless steel that can bear low-temperature impact, so the investment that is used on the interchanger is very big.Illegal producer is more arranged in order to save cost, adopt the not plain carbon stool formula case tube heat exchanger of low-temperature impact-resistant, cause serious potential safety hazard.
When system fails above move under the situation of B-grade condensation temperature in the molecular sieve dehydration degree of depth; Every just need be at a distance from a couple of days to the defrosting that heats up of whole shell and tube heat exchanger, owing to the shell and tube heat exchanger quality is big, thermal capacitance is big; It is slower to heat up; Seriously delay production, hydrocarbon mixture production is difficult to continuous operation, and hydrocarbon mixture output is lower.
Owing to need consume resurgent gases during molecular sieve equipment regeneration; Traditional technology all is that the dried feed gas of molecular sieve outlet itself purges regeneration; Can consume about virgin gas of about 10% like this, under the feed gas compressor of same displacement, the output of hydrocarbon mixture can reduce.
So need a kind of installation, ability automatic operating of being easy to, high associated gas hydrocarbon mixture recovery system and the recovery method of heat exchange efficiency with save energy, reduces environmental pollution simultaneously.
The utility model content
Problem to existing expander refrigeration and ammonia or propane refrigeration; The utility model proposes a kind of associated gas hydrocarbon mixture recovery system; Said equipment comprises compressor, and the first-stage condenser that is connected with said compressor, and said first-stage condenser also is connected with molecular sieve; The outlet of said molecular sieve is provided with the dew point detector, and said dew point detector is connected to secondary condenser through the secondary precooling unit.
Preferably, said recovery system also comprises oil-gas separator, and said oil-gas separator is communicated with said compressor and first-stage condenser respectively; Also be connected with the primary separator that is used to discharge liquid water and liquid hydrocarbon mixture on the said first-stage condenser.
During work, can filter and separate free-water and impurity in the associated gas earlier, get into said compressor again and compress.Pressurized gas after the compression can be earlier after air-cooled, get into the oil-gas separator of said compressor outlet again, to separate liquid water and few part agglomerative hydrocarbon mixture.Gas after separating gets into said first-stage condenser.Condensed material gets into said first separator; Liquid hydrocarbon mixture in the condensing air and liquid water are removed, and said liquid water and liquid hydrocarbon are after said first separator separates, and liquid water is discharged; Liquid hydrocarbon can be kept in separating tank, enters said hydrocarbon mixture product storage tank again.
Gas in the said first-stage condenser gets in the said molecular sieve and dewaters, the dew point hygrometer that exports through said molecular sieve then; When the dew-point temperature that detects virgin gas when said dew point hygrometer was lower than design temperature T2, system normally supplied dehydrated raw material gas to the back-end.Because the exotherm mechanism of molecular sieve; Behind said molecular sieve dehydration, gas temperature can rise about 10 ℃, so can on said first-stage condenser, connect throttling valve; Earlier dried condensing air and the mixing dry gas heat exchange of from said first-stage condenser, coming out; Be the secondary precooling, dried condensing air temperature is reduced to about 10 ℃, get into said secondary condenser again.Said secondary condenser is controlled at temperature between-40 ℃ to-50 ℃ by two-stage refrigeration unit refrigeration, makes most of C
3+ condensation.
Preferably, be connected with on the said molecular sieve gas is imported second separator that generator generates electricity; Be connected with the 3rd separator on the said secondary condenser, said the 3rd separator separates discharge with the liquid hydrocarbon mixture in the said secondary condenser with dry gas; Also be connected with hydrocarbon mixture product storage tank on said the 3rd separator, said hydrocarbon mixture product storage tank also is communicated with said first separator.
Said secondary condenser makes most of C
3After+the condensation, condensed liquid storage enters said hydrocarbon mixture product storage tank in the bottom of said second-stage separator after a certain amount of.Associated gas heat exchange in said first-stage condenser before isolated cryogenic gas and the refrigeration gets into heat exchange in the said secondary precooling unit then, has utilized to get into generator for electricity generation after remaining cold.
Preferably, be connected with on the said dew point hygrometer and be used to discharge resurgent gases first valve and second valve, said dew point hygrometer is connected with said secondary precooling unit through said second valve.
When the dew-point temperature that detects virgin gas when said dew point hygrometer is lower than design temperature T2, first valve closes, second valve opening, system normally supplies dehydrated raw material gas to the back-end; When the dew-point temperature that detects virgin gas when said dew point hygrometer is higher than design temperature T2, first valve opening, second valve closes, virgin gas is discharged through said first valve.
Because the dehydrating effect of molecular sieve is directly proportional with inlet pressure; Be inversely proportional to temperature in; The molecular sieve of the utility model is installed on after the said first-stage condenser; The temperature that gets into said molecular sieve is controlled between 5 ℃-15 ℃, and the pressure that gets into said molecular sieve is the relatively high pressure after the feed gas compressor compression, has effectively reduced the loading level of said molecular sieve.Simultaneously, the tail gas after the employing of the utility model processing purges molecular sieve, so under the situation of same feed gas compressor, the utility model can be saved 10% purging virgin gas.
Simultaneously; Said molecular sieve and condenser system at different levels form an integral body; Dew point detector and bypath valve are installed in outlet at said molecular sieve; Have only when the outlet dew point of said molecular sieve during far below said B-grade condensation actuator temperature, virgin gas just possibly be lower than 0 ℃ interchanger to the back-end supplies gas, and effectively guarantees not freeze on the cryogenic heat exchanger.So cryogenic heat exchanger can not use traditional anti-freezing tube and shell heat exchanger, and use the higher plate-type heat exchanger of heat exchange efficiency.
The refrigeration system of the utility model adopts the two-shipper compression, and its COP value under-45 ℃ of operating modes can reach 1.22, and the COP value of traditional propane compressor under-35 ℃ of operating modes also is no more than 0.5; Though ammonia machine COP value can be approaching with the utility model, ammonia machine need be installed the additional water refrigerating unit, and with reduction compressor head temperature, and ammonia system is difficult to realize automatic control; Draining simultaneously, oil return, throttling valve etc. much all need professional's manual operation, and cost is higher, so be usually used in large scale system, the sledge-borne type equipment that is not so good as the utility model is convenient.
Description of drawings
Accompanying drawing 1 is the schematic flow sheet of prior art expander refrigeration method;
Accompanying drawing 2 is the schematic flow sheet of prior art ammonia or propane refrigeration method;
Accompanying drawing 3 is the connection synoptic diagram of the utility model recovery system preferred embodiment.
Embodiment
Below in conjunction with Fig. 3 the preferred recovery system of the utility model is done further explanation.
The associated gas hydrocarbon mixture recovery system of the utility model comprises compressor, and the first-stage condenser that is connected with said compressor, and said first-stage condenser also is connected with molecular sieve; The outlet of said molecular sieve is provided with the dew point detector, and said dew point detector is connected to secondary condenser through the secondary precooling unit.
In this preferred embodiment, said recovery system also comprises oil-gas separator, and said oil-gas separator is communicated with said compressor and first-stage condenser respectively; Also be connected with the primary separator that is used to discharge liquid water and liquid hydrocarbon mixture on the said first-stage condenser.Be connected with on the said molecular sieve gas is imported second separator that generator generates electricity; Be connected with the 3rd separator on the said secondary condenser, said the 3rd separator is discharged liquid hydrocarbon mixture and dry gas in the said secondary condenser respectively; Said the 3rd separator also is connected with hydrocarbon mixture product storage tank, and said hydrocarbon mixture product storage tank also is communicated with said first separator.
During work, filter earlier with separate the associated gas source of the gas in free-water and impurity, get in the compressor again and compress, the scope of the pressure P1 of pressurized gas can be 0.2MPa≤P1≤1.0MPa.Pressurized gas after the compression is after air-cooled, and its temperature gets into the oil-gas separator of said compressor outlet less than 60 ℃.Said oil-gas separator separates the liquid water in the pressurized gas and few part agglomerative hydrocarbon mixture.Associated gas after separating gets into said first-stage condenser, and with the mixing low temp gas heat exchange after the said secondary condenser condensation separation, the temperature of oil gas drops to about 15 ℃ from 60 ℃.The scope of the temperature T 1 of the condensed condensing air of first-stage condenser is 5 ℃≤T1≤15 ℃.Condensed liquid gets into said first separator, removes liquid hydrocarbon mixture and liquid water, and liquid water separates the back discharges with liquid hydrocarbon, and liquid hydrocarbon can enter said hydrocarbon mixture product storage tank after in separating tank, keeping in.
Associated gas after the condensation separation, gets in the said molecular sieve again and dewaters in said first-stage condenser.And dew point hygrometer is set in the outlet of said molecular sieve, and in this preferred embodiment, being connected with on the said dew point hygrometer and being used to discharge the resurgent gases first valve QV1 and the second valve QV2, said dew point hygrometer is connected with said secondary precooling unit through the said second valve QV2.When the dew-point temperature that detects associated gas when said dew point hygrometer was higher than T2, the first valve QV1 opened, and the second valve QV2 closes, and associated gas is discharged by the first valve QV1.When the dew-point temperature that detects associated gas when dew point hygrometer was lower than T2, the first valve QV1 closed, and the second valve QV2 opens, and system is the associated gas after the supply dehydration to the back-end normally.Temperature T 2 can be according to circumstances sets up on their own in-40 ℃≤T2≤-60 ℃, and at this preferred embodiment, T2 is set at-50 ℃.
In the preferred embodiment of the utility model; Also be connected with throttling valve on the said first-stage condenser; Condensed gas in said first-stage condenser gets in the said secondary precooling unit through said throttling valve, and the associated gas that is lower than design temperature T2 with dew-point temperature carries out heat exchange.Because the exotherm mechanism of molecular sieve; Behind said molecular sieve dehydration, the temperature of associated gas can rise about 10 ℃, so earlier dried associated gas and from said one-level condensation, discharge; Through the condensing air heat exchange after said throttling valve throttling and the cooling; Promptly carry out the secondary precooling, the mixed gas temperature after the heat exchange is reduced to about 10 ℃, gets into said secondary condenser again.
Referring to shown in Figure 3, said secondary condenser is by two-stage refrigeration unit refrigeration, and condensing temperature T4 is between-40 ℃≤T4≤-50 ℃, makes most of C
3+ condensation, condensed liquid storage enter said hydrocarbon mixture product storage tank in the bottom of said second-stage separator after a certain amount of.Isolated cryogenic gas and the preceding Sweet natural gas heat exchange in said first-stage condenser of refrigeration; Pass through the throttling valve expenditure and pressure then; Reduce getting into secondary precool heat exchanger device after the temperature and carry out the secondary precooling once more, the scope of the temperature T 3 of secondary precooling is 0 ℃≤T3≤10 ℃.
Said secondary condenser makes most of C
3After+the condensation, condensed liquid storage enters said hydrocarbon mixture product storage tank in the bottom of said second-stage separator after a certain amount of.Sweet natural gas heat exchange in said first-stage condenser before isolated cryogenic gas and the refrigeration gets into heat exchange in the said secondary precooling unit then, has utilized to get into generator for electricity generation after remaining cold.
The main recovery path of the utility model recovery system has two; One of which is: after associated gas said compressor of process and the first-stage condenser; Part condensing air is through said molecular sieve; Carry out the secondary precool heat exchanger with another part without the condensing air of said molecular sieve, get into condensation in the said secondary condenser again; The liquid that condenses is as the hydrocarbon mixture product that reclaims, and dry gas gets in the said first-stage condenser again and circulates.It two is: the low temperature dry gas of separating in the secondary condenser; In first-stage condenser, carry out heat exchange with refrigerating associated gas pressurized gas not, and then expenditure and pressure, get in the secondary precooling unit; Through the said molecular sieve and second separator separates, get in the generator again as power generation energy resource.Also have one to reclaim the path and be: associated gas through said first-stage condenser and molecular sieve after directly discharge.
The molecular sieve of the utility model is installed on after the said first-stage condenser; Because the dehydrating effect of molecular sieve is directly proportional with inlet pressure; Be inversely proportional to temperature in; The temperature that gets into said molecular sieve is controlled between 5 ℃-15 ℃, and the pressure that gets into said molecular sieve is the relatively high pressure after the feed gas compressor compression, has reduced the loading level of molecular sieve effectively.After 4-5, when said molecular sieve lost efficacy, the solid waste that enters environment in the molecular sieve reduced greatly.Traditional technology or be loaded on the import of feed gas compressor to molecular sieve, or be loaded on the outlet of compressor, molecular sieve and feed gas compressor group sled, increased the consumption of molecular sieve, and the molecular sieve dehydration effect can not get effective assurance.
Molecular sieve of the utility model and condenser system form an integral body; In the outlet of said molecular sieve online dew point detector is installed; The bypass first valve QV1 and the second valve QV2 are set simultaneously; Have only when molecular sieve outlet dew point during far below the temperature of secondary condenser, virgin gas just possibly be lower than 0 ℃ interchanger to the back-end supplies gas, and effectively guarantees on the cryogenic heat exchanger icing; So cryogenic heat exchanger can not use traditional anti-freezing tube and shell heat exchanger, and use the higher plate-type heat exchanger of heat exchange efficiency.Traditional tube and shell heat exchanger heat transfer coefficient has only the 1/3-1/5 of plate-type heat exchanger, and when reaching identical heat exchange effect, the metal consumption of shell and tube heat exchanger is quite big.
The refrigeration system of the utility model preferred embodiment adopts the two-shipper compression; Refrigeration agent adopts the R404A of environmental protection, and its COP value under-45 ℃ of operation conditions reaches 1.22, and the COP value of traditional propane compressor under-35 ℃ of operation conditions also is no more than 0.5; Though ammonia machine COP value and R404A twin-stage machine are approaching; But the ammonia machine need be installed the additional water refrigerating unit, and with reduction compressor head temperature, and ammonia system is difficult to realize automatic control; Draining simultaneously, oil return, throttling valve etc. much all need professional's manual operation, so be usually used in large scale system.
Because it is all remote to produce the scattered well of associated gas; Water source and traffic are all not convenient; Hydrocarbon mixture for scattered well reclaims the increase that the use ammonia system can cause operator's quantity; Average every cover adopts the equipment of ammonia machine to increase about 4 people than the two-stage refrigeration with automatic control, and cost of labor is very high, causes investor's minimizing of getting a profit.And the association source of the gas of scattered well reduces, and when needing resettlement ammonia machine, the sledge-borne type equipment that can not show a candle to the utility model is convenient.
The molecular sieve outlet that the conventional hybrid hydrocarbon reclaims is generally water cooling, can run into very big difficulty in arid relatively place production.And behind molecular sieve in the utility model and the condensation module group sled, utilize the high pressure dry gas throttling cooling refrigeration of producing discharge, and the molecular sieve temperature out is reduced, reduced dry gas pressure simultaneously, for getting into generator for electricity generation, dry gas gets ready.
The utility model is compared with traditional mixing hydrocarbon recovery system, and output can increase 10%-50%; Also have the following advantages simultaneously:
1. energy consumption reduces greatly.Owing to adopted Two-stage refrigerating system, made the refrigerator power consumption lower; Adopt reliable molecular sieve dehydration technology, adopt the scheme heat exchange of light weight, plate-type heat exchanger that heat transfer coefficient is high, also reduced energy consumption.
2. the molecular sieve of traditional mixing hydrocarbon recovery system, ammonia refrigeration system are all manual control, and the utility model molecular sieve and dew point detection, refrigeration system etc. are control automatically all, and every covering device lacks than legacy equipment uses 4 people;
3. molecular sieve filled minimizing; Legacy equipment is because the installation site of molecular sieve etc. are undesirable, in order to reach separating effect, is example with the equipment of treatment capacity 10,000 side's associated gases every day, usually need fill molecular sieve 1-2 ton, and the utility model only needs filling molecular sieve 500kg.
4. can save the purging dry gas.In the technology of existing ammonia machine and decompressor, because the installation site of its molecular sieve and the problem of technical process, generally need export 10% dry gas and purge said molecular sieve with molecular sieve, caused the waste of virgin gas.And the tail gas after the processing adopted of the utility model purges, so under the situation of same feed gas compressor, the utility model can be saved 10% purging dry gas.
5. expander refrigeration system and ammonia system all need on-the-spot the installation, and installation period is long, and field erected quality is also uneven, but and the skid system complete production in the utility model, the quality of its production rate and equipment improves greatly.
6. because existing installation uses is large-scale decompressor and ammonia machine refrigerating scheme; The investor is general to select broad-minded place to set up the hydrocarbon mixture recovery system, simultaneously, source of the gas that originally can the inlet pipe net is contracted to oneself has; Increase the income of oneself with this, but brought loss to country.And the device miniaturization of the utility model, robotization, be beneficial to construction, and can the associated gas of the outlying scattered well that is in emptying and burns be reclaimed, for country has practiced thrift the energy, protect environment.
7. ammonia refrigerant is inflammable, and is harmful, and the propane refrigerant EER is low, and is inflammable; The utility model adopts the scheme of environmental protection refrigerant R4040A two-stage refrigeration, and is safe and efficient.
The refrigeration system of the utility model adopts the two-shipper compression; Refrigeration agent adopts the R404A of environmental protection; Its COP value under-45 ℃ of operation conditions reaches 1.22; And traditional propane compressor ground COP value under-35 ℃ of operation conditions also is no more than 0.5, though ammonia refrigerant COP value and R404A twin-stage machine are approaching, need to install the additional water refrigerating unit and reduces the compressor head temperature; And ammonia system is difficult to realize automatic control, and draining, oil return, throttling valve etc. much all need professional's manual operation, so be usually used in large scale system.Because it is all remote to produce the scattered well of associated gas, water source and traffic are all not convenient, reclaim for the hydrocarbon mixture of scattered well and use ammonia system can cause operator's quantity to increase, and cost of labor is very high, cause investor's minimizing of getting a profit.During resettlement, it is convenient that the ammonia machine also can not show a candle to the sledge-borne type equipment of the utility model.
Traditional molecular sieve outlet that is used for the hydrocarbon mixture recovery is generally water cooling, can run into very big difficulty in arid relatively place production.And behind molecular sieve in the utility model and the refrigeration system group sled, utilize and produce the high pressure dry gas throttling cooling refrigeration of discharging, the molecular sieve temperature out is reduced, reduced dry gas pressure simultaneously, for getting into generator for electricity generation, dry gas gets ready.
Last institute should be noted that; Above embodiment is only in order to the technical scheme of explanation the utility model but not to the restriction of the utility model protection domain; Although the utility model has been done detailed description with reference to preferred embodiment; Those of ordinary skill in the art should be appreciated that and can make amendment or be equal to replacement the technical scheme of the utility model, and do not break away from the essence and the scope of the utility model technical scheme.
Claims (10)
1. associated gas hydrocarbon mixture recovery system, it is characterized in that: said equipment comprises compressor, and the first-stage condenser that is connected with said compressor, said first-stage condenser also is connected with molecular sieve; The outlet of said molecular sieve is provided with the dew point detector, and said dew point detector is connected to secondary condenser through the secondary precooling unit.
2. recovery system as claimed in claim 1 is characterized in that: it also comprises oil-gas separator, and said oil-gas separator is communicated with said compressor and first-stage condenser respectively.
3. recovery system as claimed in claim 1 is characterized in that: also be connected with the primary separator that is used to discharge liquid water and liquid hydrocarbon mixture on the said first-stage condenser.
4. recovery system as claimed in claim 1 is characterized in that: also be connected with throttling valve on the said first-stage condenser, condensed gas gets in the said secondary precooling unit through said throttling valve in said first-stage condenser.
5. recovery system as claimed in claim 1 is characterized in that: be connected with on the said molecular sieve gas is imported second separator that generator generates electricity.
6. recovery system as claimed in claim 1 is characterized in that: be connected with on the said dew point hygrometer and be used to discharge resurgent gases first valve and second valve, said dew point hygrometer is connected with said secondary precooling unit through said second valve.
7. recovery system as claimed in claim 1 is characterized in that: be connected with the 3rd separator on the said secondary condenser, it separates the liquid hydrocarbon mixture in the said secondary condenser and discharges with dry gas.
8. recovery system as claimed in claim 6 is characterized in that: said the 3rd separator also is connected with hydrocarbon mixture product storage tank, and said hydrocarbon mixture product storage tank also is communicated with said first separator.
9. recovery method as claimed in claim 1 is characterized in that: the scope of the pressure P1 in the said compressor is 0.2MPa≤P1≤1.0MPa.
10. recovery method as claimed in claim 1 is characterized in that: the condensing air temperature T 1 in the said first-stage condenser is 5 ℃≤T1≤15 ℃, and the gas temperature T3 in the said secondary precooling unit is 0 ℃≤T3≤10 ℃; The temperature T 4 of the gas in the said secondary condenser is-40 ℃≤T4≤-50 ℃.
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| CN2011203696238U CN202297494U (en) | 2011-09-30 | 2011-09-30 | Device for recycling mixed hydrocarbon from oil associated gas |
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| CN2011203696238U CN202297494U (en) | 2011-09-30 | 2011-09-30 | Device for recycling mixed hydrocarbon from oil associated gas |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102504859A (en) * | 2011-09-30 | 2012-06-20 | 上海森鑫新能源科技有限公司 | Method and equipment for recovery of oilfield associated gas hydrocarbon mixture |
| CN103497804A (en) * | 2013-10-09 | 2014-01-08 | 重庆耐德工业股份有限公司 | Method for removing heavy hydrocarbon in natural gas through low-temperature capillary condensation |
| CN104132504A (en) * | 2014-07-17 | 2014-11-05 | 西安长庆科技工程有限责任公司 | System and method for recycling mixed hydrocarbon from well site natural gas |
-
2011
- 2011-09-30 CN CN2011203696238U patent/CN202297494U/en not_active Expired - Lifetime
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102504859A (en) * | 2011-09-30 | 2012-06-20 | 上海森鑫新能源科技有限公司 | Method and equipment for recovery of oilfield associated gas hydrocarbon mixture |
| CN103497804A (en) * | 2013-10-09 | 2014-01-08 | 重庆耐德工业股份有限公司 | Method for removing heavy hydrocarbon in natural gas through low-temperature capillary condensation |
| CN103497804B (en) * | 2013-10-09 | 2015-08-26 | 重庆耐德工业股份有限公司 | The method of heavy hydrocarbon in Sweet natural gas is deviate from a kind of low temperature capillary condensation |
| CN104132504A (en) * | 2014-07-17 | 2014-11-05 | 西安长庆科技工程有限责任公司 | System and method for recycling mixed hydrocarbon from well site natural gas |
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