CN102504859A - Method and equipment for recovery of oilfield associated gas hydrocarbon mixture - Google Patents
Method and equipment for recovery of oilfield associated gas hydrocarbon mixture Download PDFInfo
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Abstract
The invention relates to a method for recovery of oilfield associated gas hydrocarbon mixture, which includes steps: firstly, delivering associated gas into a compressor for compression to form compressed gas with a pressure P1; secondly, subjecting the compressed gas to primary condensation at a temperature T1 to form condensed gas and liquid; thirdly, delivering the condensed gas to a molecular sieve for dewatering; fourthly, subjecting the dewatered condensed gas to dew point detection; fifthly, exhausting the dewatered condensed gas as recovered gas if the dew point temperature of the dewatered condensed water is higher than a temperature T2, and performing following steps if the dew point temperature of the dewatered condensed water is lower than the temperature T2; sixthly, subjecting the dewatered condensed gas to secondary precooling at a certain temperature T3; seventhly, subjecting the gas subjected to secondary precooling to secondary condensation at a certain temperature T4; and eighthly, separating and storing a product of secondary condensation to generate recovered hydrocarbon mixture.
Description
Technical field
The present invention relates to petrochemical industry, a kind of specifically recovery system of associated gas hydrocarbon mixture and recovery method.
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 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 the liquid after the separation and first 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 machine 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 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 the liquid after the separation and first 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.
But so need a kind of automatic operating that is easy to install, high associated gas hydrocarbon mixture recovery method and the recovery system of heat exchange efficiency with save energy, reduces environmental pollution simultaneously.
Summary of the invention
To the problem of existing expander refrigeration and ammonia or propane refrigeration method, the present invention proposes a kind of associated gas hydrocarbon mixture recovery method, said method comprising the steps of:
Step 1: associated gas is delivered in the compressor and compresses, and makes it to form the pressurized gas that pressure is P1;
Step 2: said pressurized gas carries out the one-level condensation 1 time in temperature T, forms condensing air and fluent meterial;
Step 3: said condensing air is delivered in the molecular sieve and dewaters;
Step 4: the condensing air after will dewatering carries out dew point and detects;
Step 5:, then discharge and form reclaiming gas if the condensing air dew-point temperature after the said dehydration is higher than temperature T 2.
In said step 5, if the condensing air dew-point temperature after the said dehydration is lower than temperature T 2, then said recovery method further may further comprise the steps:
Step 6: the condensing air after the said dehydration is carried out the secondary precooling under certain temperature T3;
Step 7: the gas after the secondary precooling is carried out B-grade condensation under certain temperature T4;
Step 8:, form the hydrocarbon mixture product that reclaims with separating substances behind the B-grade condensation and storage.
Preferably, further comprise step 11 before the said step 1: filter and separate free-water and impurity in the associated gas source of the gas; Further comprise step 21 before the said step 2: said pressurized gas is carried out gas-oil separation, separate liquid water and part agglomerative hydrocarbon mixture.
The concrete removal process of above-mentioned each step is: filter and separate associated gas behind free-water and the impurity and get into compressor and compress.Pressurized gas after the compression can be earlier after air-cooled, get into the oil-gas separator of said compressor outlet again, separate liquid water and few part agglomerative hydrocarbon mixture.Gas after separating gets into first-stage condenser, forms condensing air and fluent meterial.Said fluent meterial is mainly liquid hydrocarbon mixture and liquid water, and it separates after getting into first separator, and the water of separating is directly discharged, and the liquid hydrocarbon mixture of separating enters hydrocarbon mixture product storage tank after can in separating tank, keeping in.
After step 2 was carried out the one-level condensation, fluent meterial was drained through said first separator, and remaining condensing air gets in the molecular sieve and dewaters, and discharged through the dew point hygrometer of said molecular sieve outlet then.The dew-point temperature that detects said condensing air when said dew point hygrometer is lower than necessarily can temperature T 2 time, and system continues the condensing air after the supply dehydration to the back-end.Because the exotherm mechanism of said molecular sieve; Behind said molecular sieve dehydration; The temperature of condensing air can rise about 10 ℃, so can carry out heat exchange to condensing air after the said molecular sieve drying and the condensing air that comes out from first-stage condenser, i.e. secondary precooling earlier; The degree of said condensing air is reduced to about 10 ℃, gets into secondary condenser again.Said secondary condenser makes most of C
3+ condensation, condensed liquid storage can enter said hydrocarbon mixture product storage tank in the bottom of said second-stage separator after a certain amount of.
When the gas after said step 8 is with B-grade condensation separates; Virgin gas before isolated cryogenic gas and the refrigeration is in the heat exchange of one-level condensation in-process; Expenditure and pressure then gets into secondary precool heat exchanger device after reducing temperature once more, has utilized can get into generator for electricity generation after remaining cold.
The invention allows for a kind of associated gas hydrocarbon mixture recovery system, said equipment comprises compressor, and with the first-stage condenser of said compressor through pipe connection, said first-stage condenser also is connected with molecular sieve; The outlet of said molecular sieve is provided with the dew point detector, is connected with two valves on the said dew point detector; One of them valve is connected to the secondary precooling unit, is connected with secondary condenser on the said secondary precooling unit.
Preferably, also be connected with first separator on the said first-stage condenser, be connected with second separator on the said molecular sieve, be connected with the 3rd separator on the said secondary condenser.
Molecular sieve of the present invention is installed on after the said first-stage condenser; The temperature that gets into said molecular sieve is controlled between 5 ℃-15 ℃; The pressure that gets into said molecular sieve is the relatively high pressure after the associated gas compressor compresses; And the dehydrating effect of molecular sieve is directly proportional with inlet pressure, is inversely proportional to temperature in, so the present invention has effectively reduced the loading level of said molecular sieve.Simultaneously, the tail gas after the employing processing of the present invention purges molecular sieve, so under the situation of same feed gas compressor, the present invention can save 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.
Refrigeration system of the present invention 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 present invention, 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, it is convenient to be not so good as sledge-borne type equipment of the present invention.
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 schematic flow sheet of hydrocarbon mixture recovery method preferred embodiment of the present invention.
Embodiment
Below in conjunction with Fig. 3 preferred recovery method of the present invention and recovery system are done further explanation.
Associated gas hydrocarbon mixture recovery method of the present invention may further comprise the steps:
Step 1: associated gas is delivered in the compressor and compresses, and makes it to form the pressurized gas that pressure is P1;
Step 2: said pressurized gas carries out the one-level condensation 1 time in temperature T, forms condensing air and fluent meterial;
Step 3: said condensing air is delivered in the molecular sieve and dewaters;
Step 4: the condensing air after will dewatering carries out dew point and detects;
Step 5:, then discharge and form reclaiming gas if the condensing air dew-point temperature after the said dehydration is higher than temperature T 2.
In said step 5, if the condensing air dew-point temperature after the said dehydration is lower than temperature T 2, then said recovery method further may further comprise the steps:
Step 6: the condensing air after the said dehydration is carried out the secondary precooling under certain temperature T3;
Step 7: the gas after the secondary precooling is carried out B-grade condensation under certain temperature T4;
Step 8:, form the hydrocarbon mixture product that reclaims with separating substances behind the B-grade condensation and storage.
In a preferred embodiment of the invention, also comprise step 11 before the said step 1: filter and separate free-water and impurity in the associated gas source of the gas; Also comprise step 21 before the said step 2: said pressurized gas is carried out gas-oil separation, separate liquid water and part agglomerative hydrocarbon mixture.
During use, filter and separate free-water and impurity in the associated gas source of the gas earlier, get in the compressor 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 first-stage condenser, and the scope of the temperature T 1 of condensation is 5 ℃≤T1≤15 ℃.Condensed liquid gets into first separator, and wherein liquid hydrocarbon mixture is separated with liquid water, and after the separation, said liquid water is discharged, said liquid hydrocarbon in separating tank temporary after, can enter hydrocarbon mixture product storage tank.
After step 2 was carried out the one-level condensation, fluent meterial was drained through said first separator, and remaining condensing air gets in the molecular sieve and dewaters.The outlet of said molecular sieve is provided with dew point hygrometer, the first valve QV1 and the second valve QV2.When the dew-point temperature that detects condensing air when said dew point hygrometer was higher than design temperature T2, the first valve QV1 opened, and the second valve QV2 closes, and condensing air is discharged by the QV1 valve.When the dew-point temperature that detects condensing air when said dew point hygrometer was lower than design temperature 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 ℃.
Because the exotherm mechanism of said molecular sieve; Behind said molecular sieve dehydration; The temperature of condensing air can rise about 10 ℃, so can carry out heat exchange to condensing air after the said molecular sieve drying and the condensing air that comes out from first-stage condenser, i.e. secondary precooling earlier; The degree of said condensing air is reduced to about 10 ℃, gets into secondary condenser again.Said secondary condenser makes most of C
3+ condensation, condensed liquid storage can enter said hydrocarbon mixture product storage tank in the bottom of said second-stage separator after a certain amount of.
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 carries out the one-level condensation with the preceding virgin gas of refrigeration in first-stage condenser; Pass through expenditure and pressure then; Reduce after the temperature getting in the said secondary precool heat exchanger device once more, carry out the secondary precooling, the scope of the temperature T 3 of secondary precooling is 0 ℃≤T3≤10 ℃.
The invention allows for a kind of associated gas hydrocarbon mixture recovery system, said equipment comprises compressor, and with the first-stage condenser of said compressor through pipe connection, said first-stage condenser also is connected with molecular sieve; The outlet of said molecular sieve is provided with the dew point detector, is connected with two valves on the said dew point detector; One of them valve is connected to the secondary precooling unit, is connected with secondary condenser on the said secondary precooling unit.
In the preferred embodiment of invention, also be connected with first separator on the said first-stage condenser, be used for the liquid water of pressurized gas is separated with few part agglomerative hydrocarbon mixture; Be connected with second separator on the said molecular sieve, be used for the tail gas of molecular sieve sent in the generator and generate electricity; Be connected with the 3rd separator on the said secondary condenser; Be used to separate gas and liquid behind the B-grade condensation; Isolated liquid gets in the hydrocarbon mixture product storage tank and stores; Sweet natural gas heat exchange in first-stage condenser before the cryogenic gas of separating and the refrigeration, expenditure and pressure then gets into secondary precool heat exchanger device after reducing temperature once more.
Because the dehydrating effect of molecular sieve is directly proportional with inlet pressure; Be inversely proportional to temperature in; Molecular sieve of the present invention 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 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 present invention 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 preferred embodiment of the present invention 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, it is convenient to can not show a candle to sledge-borne type equipment of the present invention.
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 among the present invention 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 present invention compares 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 molecular sieve of the present invention 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 present invention 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 of the present inventionly adopt the tail gas after the processing to purge, so under the situation of same feed gas compressor, the present invention can save 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 among the present invention, 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 device miniaturization of the present invention, 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 present invention adopts the scheme of environmental protection refrigerant R4040A two-stage refrigeration, and is safe and efficient.
Last institute should be noted that; Above embodiment is only in order to technical scheme of the present invention to be described but not to the restriction of protection domain of the present invention; Although the present invention 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 technical scheme of the present invention, and do not break away from the essence and the scope of technical scheme of the present invention.
Claims (10)
1. associated gas hydrocarbon mixture recovery method is characterized in that: said method comprising the steps of:
Step 1: associated gas is delivered in the compressor and compresses, and makes it to form the pressurized gas that pressure is P1;
Step 2: said pressurized gas carries out the one-level condensation 1 time in temperature T, forms condensing air and fluent meterial;
Step 3: said condensing air is delivered in the molecular sieve and dewaters;
Step 4: the condensing air after will dewatering carries out dew point and detects;
Step 5:, then discharge and form reclaiming gas if the condensing air dew-point temperature after the said dehydration is higher than temperature T 2.
2. recovery method as claimed in claim 1 is characterized in that: in said step 5, if the condensing air dew-point temperature after the said dehydration is lower than temperature T 2, then said recovery method further may further comprise the steps:
Step 6: the condensing air after the said dehydration is carried out the secondary precooling under certain temperature T3;
Step 7: the gas after the secondary precooling is carried out B-grade condensation under certain temperature T4;
Step 8:, form the hydrocarbon mixture product that reclaims with separating substances behind the B-grade condensation and storage.
3. recovery method as claimed in claim 1 is characterized in that: further comprise step 11 before the said step 1: filter and separate free-water and impurity in the associated gas source of the gas.
4. recovery method as claimed in claim 1 is characterized in that: further comprise step 21 before the said step 2: said pressurized gas is carried out gas-oil separation, separate liquid water and part agglomerative hydrocarbon mixture.
5. recovery method as claimed in claim 1 is characterized in that: the scope of the pressure P1 in the said step 1 is 0.2MPa≤P1≤1.0MPa.
6. recovery method as claimed in claim 1 is characterized in that: the scope of the temperature T 1 in the said step 2 is 5 ℃≤T1≤15 ℃; The scope of the temperature T 2 in the said step 5 is-40 ℃≤T2≤-60 ℃.
7. recovery method as claimed in claim 2 is characterized in that: the secondary precooling in the said step 6 for the condensing air after the said molecular sieve drying with carry out heat exchange from the condensing air of said one-level condensation.
8. recovery method as claimed in claim 2 is characterized in that: the scope of the temperature T 3 in the said step 6 is 0 ℃≤T3≤10 ℃; The scope of the temperature T 4 in the said step 7 is-40 ℃≤T4≤-50 ℃.
9. associated gas hydrocarbon mixture recovery system, it is characterized in that: said equipment comprises compressor, and with the first-stage condenser of said compressor through pipe connection, said first-stage condenser also is connected with molecular sieve; The outlet of said molecular sieve is provided with the dew point detector, is connected with two valves on the said dew point detector; One of them valve is connected to the secondary precooling unit, is connected with secondary condenser on the said secondary precooling unit.
10. recovery system as claimed in claim 9 is characterized in that: also be connected with first separator on the said first-stage condenser, be connected with second separator on the said molecular sieve, be connected with the 3rd separator on the said secondary condenser.
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| CN102925194A (en) * | 2011-08-12 | 2013-02-13 | 王建基 | Recovery technology of stable mixed hydrocarbons of associated gases of scattered oil and gas wells in oilfield |
| CN103146450A (en) * | 2013-03-29 | 2013-06-12 | 四川金科深冷设备工程有限公司 | Natural gas recovery process |
| CN103965942A (en) * | 2014-05-09 | 2014-08-06 | 宁夏宝塔石化科技实业发展有限公司 | Light hydrocarbon recovery process technology for oil field associated gas |
| CN105444524A (en) * | 2015-01-30 | 2016-03-30 | 张登峰 | Portable mixed hydrocarbon extraction equipment and extraction method |
| CN109444307A (en) * | 2018-09-29 | 2019-03-08 | 福建和盛高科技产业有限公司 | A kind of oil gas isolating device and its working method |
| CN110452730A (en) * | 2019-09-02 | 2019-11-15 | 上海优华系统集成技术股份有限公司 | The recovery system and its method of heavy constituent in lighter hydrocarbons dry gas |
| CN111852404A (en) * | 2020-07-27 | 2020-10-30 | 青岛科技大学 | Associated gas recovery processing device and method |
| WO2023087507A1 (en) * | 2021-11-17 | 2023-05-25 | 烟台杰瑞石油装备技术有限公司 | Gas treatment apparatus and method for treating gas using same |
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| CN102925194A (en) * | 2011-08-12 | 2013-02-13 | 王建基 | Recovery technology of stable mixed hydrocarbons of associated gases of scattered oil and gas wells in oilfield |
| CN103146450A (en) * | 2013-03-29 | 2013-06-12 | 四川金科深冷设备工程有限公司 | Natural gas recovery process |
| CN103965942A (en) * | 2014-05-09 | 2014-08-06 | 宁夏宝塔石化科技实业发展有限公司 | Light hydrocarbon recovery process technology for oil field associated gas |
| CN105444524A (en) * | 2015-01-30 | 2016-03-30 | 张登峰 | Portable mixed hydrocarbon extraction equipment and extraction method |
| CN105444524B (en) * | 2015-01-30 | 2018-04-13 | 张登峰 | A kind of portable mixed hydrocarbon extraction equipment and extracting method |
| CN109444307A (en) * | 2018-09-29 | 2019-03-08 | 福建和盛高科技产业有限公司 | A kind of oil gas isolating device and its working method |
| CN110452730A (en) * | 2019-09-02 | 2019-11-15 | 上海优华系统集成技术股份有限公司 | The recovery system and its method of heavy constituent in lighter hydrocarbons dry gas |
| CN110452730B (en) * | 2019-09-02 | 2021-08-06 | 上海优华系统集成技术股份有限公司 | System and method for recovering heavy components in light hydrocarbon dry gas |
| CN111852404A (en) * | 2020-07-27 | 2020-10-30 | 青岛科技大学 | Associated gas recovery processing device and method |
| CN111852404B (en) * | 2020-07-27 | 2021-07-27 | 青岛科技大学 | Associated gas recovery processing device and method |
| WO2023087507A1 (en) * | 2021-11-17 | 2023-05-25 | 烟台杰瑞石油装备技术有限公司 | Gas treatment apparatus and method for treating gas using same |
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