CN102408910A - Method and device for recovering light hydrocarbon through refrigeration using compound refrigerant and secondary dealkylation - Google Patents
Method and device for recovering light hydrocarbon through refrigeration using compound refrigerant and secondary dealkylation Download PDFInfo
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Abstract
The invention discloses a method and a device for recovering light hydrocarbons through refrigeration using a compound refrigerant and secondary dealkylation, wherein the advantages of the traditional natural gas-dealkylation direct heat exchange process are combined with the method of the invention; the precooling of the raw material natural gas, the condensation of a deethanizer top gas, and the cold quantity recovery of the product natural gas and the liquid-phase material of a low-temperature separator are all realized in a main heat exchanger; the cold quantity source of the dealkylation process is provided by a compound refrigerant refrigerating system. The composition, the component contents, the flow rate and the evaporation pressure of the compound refrigerant are adjusted and matched cold quantity and different refrigeration temperatures are provided for the light hydrocarbon condensation process, so that the flexibility of the method in operation and good adaptability of the method to the amount, the pressure and the composition change of the raw material gas; and the method has the characteristics of low energy consumption, high C3 yield and good adaptability to the change of working conditions.
Description
Technical field
The present invention relates to a kind of condensation and separation process of hydrocarbon mixture, especially relate to method and device that a kind of compound cryogen refrigeration degree of depth reclaims lighter hydrocarbons in the Sweet natural gas.
Background technology
Lighter hydrocarbons recovery is meant the process of hydro carbons mixtures such as from Sweet natural gas, reclaiming ethane, propane, butane, pentane, also is called gas reducing liquid and reclaims.According to whether reclaiming ethane, recovery device of natural gas lighter hydrocarbon can be divided into two big types: one type to reclaim C
2Component is a purpose; Another kind of to reclaim C
3And C
3+ component is a purpose.Because the ethane boiling point is lower, be difficult to the liquid form transportation, just consider to reclaim ethane when therefore only near device, ethylene producing device being arranged usually.
At present, the most of light ends unit of domestic fld is to reclaim C
3And C
3+ component is a main purpose, produces products such as LPG liquefied petroleum gas.The process for recovering light hydrocarbon of such device can adopt absorption method, oil-absorption process and condensation separation method, wherein absorption method and oil-absorption process since shortcoming such as energy consumption is high, process cost is high and product yield is low progressively replaced by more economical and advanced condensation separation method.
The condensation separation method is utilized the difference of each component boiling point in the raw natural gas, and after the raw natural gas temperature reduced, the higher hydro carbons condensation separation of boiling point was come out, and the key of this process method is to obtain enough colds to make raw natural gas cooling condensation.According to the difference of cooling method can be divided into the low-temperature receiver method that adds (like propane refrigeration, compound cryogen refrigeration etc.), from refrigerating method (throttling expansion method, turbo-expander method, heat separator method) and use simultaneously and add the low-temperature receiver method and from the combined method of refrigerating method.Since the U.S. in 1964 is used for light ends unit with the turbine expander refrigeration technology; Because this method has advantages such as flow process is simple, easy to operate; The turbine expander refrigeration method has obtained using widely in the light ends unit of newly-built and reconstruction, develops into industrial standards single-stage expansion mechanism cold technology (ISS).
In order to improve C
3Yield, derived on the ISS basis that gas is crossed cold process (GSP), liquid is crossed cold process (LSP) and direct heat exchange method process methodes such as (DHX).Wherein, Direct heat exchange method (DHX) has increased a direct heat exchange tower between decompressor outlet LTS and deethanizing column; Gas phase counter current contact in tower of deethanizing cat head phlegma and LTS outlet; Conduct heat simultaneously and mass transfer, LTS is exported the above C of 80% in the gas phase
3Condensation is got off, thereby has greatly improved the C of device
3Yield.According to document " Process improves C
3+ recovery " (S.A. Khan, Hydrocarbon processing, 1985.5) report, adopt direct heat exchange technology that the existing apparatus of Canadian Esso company is transformed after, the C of this device
3Yield increases to 95% by original 72%, has improved the C of device widely
3Yield.
As shown in Figure 1, the processing unit that " expander refrigeration+DHX technology " relates to comprises: supercharger 18 and direct heat exchange tower 19 etc. behind main heat exchanger 3, LTS 4, deethanizing column reboiler 7, deethanizing column 8, debutanizing tower reboiler 9, debutanizing tower 10, debutanizing tower condensing surface 11, swell refrigeration machine 17, the product gas.
" expander refrigeration+DHX technology " is that the exsiccant Sweet natural gas is delivered to precooling in the main heat exchanger 3; Get into then and carry out in the LTS 4 separating of gaseous phase materials and liquid phase material; Liquid phase material is delivered to the middle part of deethanizing column 8 as its charging; Gaseous phase materials is delivered to and is carried out swell refrigeration in the swell refrigeration machine 17, and the low-temperature material that obtains is delivered to direct heat exchange tower 19.The material of direct heat exchange tower 19 bottoms is delivered to the top of deethanizing column 8.Deethanizing column 8 bottoms have deethanizing column reboiler 7 to improve thermal source for it.The gaseous phase materials at deethanizing column 8 tops is delivered to partial condensation in the main heat exchanger 3, delivers to direct heat exchange tower 19 tops then and refluxes as it, C in the washing gaseous phase materials
3And above component, improved C
3Yield.But because main heat exchanger 3 does not have the outer cooling system of mending, liquefied fraction can't guarantee (usually less than 25%) in this burst backflow material, is difficult to for direct heat exchange tower 19 provides enough colds, and direct heat exchange tower 19 improves C
3The effect of yield is limited.
The virgin gas that process direct heat exchange tower 19 takes off behind the hydrocarbon is product gas, in main heat exchanger 3, is heated the recovery cold.Because in the expander refrigeration process, raw gas pressure reduces, so the product atmospheric pressure may satisfy outer defeated demand, and at this moment, 18 pairs of product gas of supercharger also need be set behind the product gas, and to carry out supercharging defeated outward.The liquid hydrocarbon of deethanizing column 8 bottoms is delivered to the middle part of debutanizing tower 10 as its charging.There is debutanizing tower water cooler 11 at debutanizing tower 10 tops for it provides cold, and there is debutanizing tower reboiler 9 debutanizing tower 10 bottoms for it provides heat, and the top obtains the liquefied gas product after 10 rectifying of charging process debutanizing tower, and the bottom obtains the stable light hydrocarbon product.
This shows, adopt " expander refrigeration+DHX technology ", can improve the C of light ends unit effectively than ISS technology
3Yield.In the light ends unit at home, compressor station is introduced U.S. PRO-QUIP company 100 * 10 in nineteen ninety-five from the oil field, huge port
4m
3After/d the natural gas treatment plant, Yumen Qing Xi arranged successively, tell Ha Wenmi, tell Ha Qiudong, terminal, Weizhou, dawn in spring light ends unit such as terminal adopt this technology.
But still there is following limitation in " expander refrigeration+DHX technology " in application:
1) raw gas pressure reduces or material gas quantity when bigger variations takes place, and decompressor off-design operating mode causes expansion efficiency reduction, fluctuation of service, and decompressor can not provide enough colds, C for device
3Yield descends, and liquid hydrocarbon output reduces.
2) document " efficient of turbine expander refrigeration device and the application of compound cryogen " (mulberry field, " oil and gas chemical industry ", the 13rd volume, the 5th phase) shows, to reclaim C
3+ be in the purpose light ends unit, the more compound cryogen refrigerating of turbine expander refrigeration refrigerating efficiency is low.
3) " expander refrigeration+DHX technology " is applicable to the occasion that virgin gas is poorer, and virgin gas need adopt the cryogen precooling when rich, and facility investment increases.
4) do not have under the situation that pressure more than needed can be able to supply utilize at raw natural gas, virgin gas has increased facility investment after decompressor expansion step-down, also increasing the back topping up compressor.Document " application of DHX technology in the light ends unit " is described to " the defeated pressure P≤1.7MPa of general requirement dry gas " outward in (Zhou Xueshen, " oil planning and design ", 2002.11).
5) be described among SY/T0077-2008 " the gas reducing liquid recovery design specifications " 5.3.8.1: " the direct heat exchange method generally is used for virgin gas and divides C
3Content less than 8%, gas treatment equipment that gas flow is bigger.C
3The amplitude that yield improves depends primarily on C in the virgin gas
1/ C
2Ratio.C in the virgin gas
1/ C
2Ratio more little, low temperature lime set rate is high more in the deethanizer overhead gas phase, DHX technology C
3The yield increase rate is big more, the C in the general requirement virgin gas
1/ C
2Be less than or equal to 7 ".
In view of the ISS technology of using usually improves C
3The yield cost is big, " expander refrigeration+DHX technology " application limitation is big, develops low, the C of a kind of energy consumption
3Yield height, reduced investment, the process for recovering light hydrocarbon that adaptability to raw material is strong are extremely urgent.
Summary of the invention
In order to overcome the above-mentioned shortcoming of prior art, the invention provides a kind of compound cryogen refrigeration secondary and take off hydrocarbon methods of light hydrocarbon recovery and device, in conjunction with the advantage of compound cryogen refrigeration and traditional direct heat exchange technology, low, the C of energy consumption
3Yield height, reduced investment, adaptability to raw material are strong.
The technical solution adopted for the present invention to solve the technical problems is: a kind of compound cryogen refrigeration secondary takes off the hydrocarbon light ends unit, and main heat exchanger, LTS, secondary take off hydrocarbon tower, deethanizing column and debutanizing tower and be connected successively; The liquid phase outlet of LTS inserts the middle part opening for feed of deethanizing column; The gaseous phase outlet of LTS takes off the hydrocarbon tower with secondary and is connected; The liquid hydrocarbon outlet that secondary takes off the hydrocarbon tower bottom is connected with the top opening for feed of deethanizing column; The gaseous phase materials outlet at deethanizing column top inserts main heat exchanger; The product gas outlet that secondary takes off the hydrocarbon tower is connected with main heat exchanger; The liquid hydrocarbon outlet of deethanizing column bottom is connected with the middle part opening for feed of debutanizing tower, is provided with the deethanizing column reboiler in the deethanizing column bottom; Be provided with the debutanizing tower water cooler at the debutanizing tower top; Be provided with the debutanizing tower reboiler in the debutanizing tower bottom; Also being provided with compound cryogen refrigeration system is connected with main heat exchanger.
Said compound cryogen refrigeration system comprises compound cryogen compressor and compound cryogen water cooler; The import of said compound cryogen compressor is connected with the compound cryogen outlet of the gaseous state of main heat exchanger; The outlet of compound cryogen compressor is connected with compound cryogen water cooler, and the outlet of compound cryogen water cooler is connected with main heat exchanger.
The outlet of the inter-stage of said compound cryogen compressor or compound cryogen water cooler is provided with gas-liquid separator, and isolated gas phase and liquid phase material are inserted main heat exchanger respectively.
The liquid phase outlet of said LTS inserts the middle part opening for feed of deethanizing column earlier again through main heat exchanger.
Taking off the hydrocarbon tower with secondary again behind the gaseous phase outlet process J-T throttling valve of said LTS or the swell refrigeration machine is connected.
The gaseous phase materials outlet at said deethanizing column top is earlier through inserting main heat exchanger behind the deethanizing cat head air compressor again.
The present invention also provides a kind of compound cryogen refrigeration secondary to take off the hydrocarbon methods of light hydrocarbon recovery, comprises the steps:
The first step, compound cryogen refrigeration: by compound cryogen refrigeration system is that main heat exchanger provides insufficient cold;
Second goes on foot, once takes off hydrocarbon:
The exsiccant Sweet natural gas is delivered to precooling in the main heat exchanger, get into then and carry out in the LTS separating of gaseous phase materials and liquid phase material, once take off hydrocarbon thereby accomplish;
The 3rd step, secondary take off hydrocarbon:
Deliver to secondary from the gaseous phase materials of LTS and take off the hydrocarbon tower; Take off in the hydrocarbon tower at secondary; From the overhead condensation liquid of the deethanizing column in the main heat exchanger and gaseous phase materials counter current contact in tower from LTS, the generating gasification refrigeration is with the C that once takes off in the gaseous phase materials that hydrocarbon obtains
3Reach above component and wash, conduct heat simultaneously and mass transfer process; Take off the product gas behind the hydrocarbon through secondary, send into be recovered in the main heat exchanger behind the cold outer defeated;
The 4th step, deethanizing:
Opening for feed gets into deethanizing column from the top of deethanizing column to take off the liquid hydrocarbon that the hydrocarbon tower bottom comes out from secondary; Deliver to heating recovery cold in the main heat exchanger from the liquid phase material of LTS, deliver to of the charging of the middle part of deethanizing column again as deethanizing column; The gaseous phase materials at deethanizing column top is sent into condensation in the main heat exchanger, and the liquid hydrocarbon of deethanizing column bottom is delivered to the middle part of debutanizing tower, as the charging of debutanizing tower;
The 5th step, debutylize:
Liquid hydrocarbon feed from the deethanizing column bottom is distillated in debutanizing tower, obtains the liquefied gas product at the top of debutanizing tower, obtains the stable light hydrocarbon product in the bottom of debutanizing tower.
Said compound cryogen is N
2, methane, ethane, ethene, propane, propylene, butane, pentane, Sweet natural gas, liquefied gas one or more.
The gaseous phase materials at deethanizing column top is earlier through sending into condensation in the main heat exchanger after the supercharging of deethanizing cat head air compressor again.
Compared with prior art, positively effect of the present invention is: the exsiccant Sweet natural gas once takes off hydrocarbon among the present invention in LTS, takes off in the hydrocarbon tower at secondary and takes off the hydrocarbon process with deethanizing cat head phlegma counter current contact completion secondary, thereby improve C
3Yield, the benefit of increase device; Taking off the required cold of hydrocarbon process is provided by compound cryogen refrigeration system, and this system's regulating measure is abundant, can the cold that be complementary be provided for the lighter hydrocarbons condensation process, thereby embodies the present invention in operational handiness with to the flexibility of raw material.Concrete manifestation is following:
1. flexible operation, it is strong to adapt to virgin gas condition changing capability
The cat head charging that secondary among the present invention takes off the hydrocarbon tower is a deethanizing cat head air cooling condensate; Rely on compound cryogen refrigeration system; This system can provide the cold that is complementary as required; Guaranteed that secondary takes off the optimum operation effect of hydrocarbon tower, the adjustable of compound cryogen has strengthened the flexibility that process method of the present invention is formed virgin gas.And the cold of traditional DHX technology utilization DHX overhead gas carries out cooling condensation to deethanizing cat head gas, and this process heat transfer temperature difference is big, and process is decreased big, and cold is difficult to balance, for reaching the preferable operating effect of DHX tower, C in the general requirement virgin gas
1/ C
2Ratio is less than 7.
Compound cryogen refrigeration system among the present invention is an independently system, its technical process and equipment design except that satisfy refrigerant cycle technology required, also have Load Regulation function flexibly.Through regulating compound cryogen composition, component concentration, compound refrigerant cycle amount and compound cryogen refrigerant pressure etc., can be in the variation of pressure, treatment capacity and the composition of endoadaptation virgin gas in a big way.
2. energy consumption is low
For the condensation separation method of lighter hydrocarbons recovery, the principal element that influences energy consumption is the heat transfer temperature difference of refrigeration temperature and refrigeration heat transfer process.Refrigeration temperature is high more, and energy consumption is low more, but C
3Yield is low more; Under identical refrigeration temperature operating mode, heat transfer temperature difference is big more, and the energy consumption of refrigeration system is high more.
After adopting compound cryogen refrigerating method of the present invention, compound cryogen provides the cold that is complementary for the lighter hydrocarbons condensation process in main heat exchanger, and the whole heat transfer process temperature difference is comparatively even, no heat transfer bottleneck, and the available energy loss is little.Simultaneously, adopt secondary of the present invention to take off the hydrocarbon method after, help improving Sweet natural gas lighter hydrocarbons recovery desirable freezing temp, reduce energy consumption for cooling.Therefore, the present invention has the advantage that reduces the light ends unit energy consumption, and energy-saving effect is obvious.
3. flow process is simple, invests lower
Do not have pressure can be able to supply to utilize the time at raw natural gas, also need carry out back supercharging after the raw material natural gas via foam overblow refrigeration in the expander refrigeration technology, and raw natural gas also need increase chilldown system when forming richness insufficient cold is provided with compressor.And the compound cryogen refrigeration techniques among the present invention, raw gas pressure loss is less, need not topping up compressor and chilldown system behind the product gas, and the comprehensive method of investment is comparatively practiced thrift.
See from flow process; Compound cryogen refrigeration techniques has only a compressor; The swell refrigeration scheme has three compressors (one of the refrigeration compressor of two of back topping up compressors and chilldown system) and a swell refrigeration machine, and the flow process of compound cryogen refrigeration techniques is more succinct, operates simpler.
4. C
3Yield is high
After adopting secondary of the present invention to take off the hydrocarbon method, under identical refrigeration temperature, than traditional I SS technology C
3Yield improves more than 10%, its C
3Yield is more than 90%.The reason scale is 150 * 10 somewhere
4m
3Recovery device of natural gas lighter hydrocarbon (the C of/d
3 +Volume content is 4.41%) in, adopt secondary to take off C after the hydrocarbon method
3Yield brings up to 95.47% from 75.11%.
Description of drawings
The present invention will explain through example and with reference to the mode of accompanying drawing, wherein:
Fig. 1 is the device and the process flow diagram of existing " expander refrigeration+DHX ";
Fig. 2 is device of the present invention and process flow diagram.
Embodiment
As shown in Figure 2; A kind of compound cryogen refrigeration secondary takes off the hydrocarbon light ends unit, comprising: compound cryogen compressor 1, compound cryogen water cooler 2, main heat exchanger 3, LTS 4, secondary take off hydrocarbon tower 5, deethanizing cat head air compressor 6, deethanizing column reboiler 7, deethanizing column 8 towers, debutanizing tower reboiler 9, debutanizing tower 10, debutanizing tower condensing surface 11 etc.Wherein:
Main heat exchanger 3, LTS 4, secondary take off hydrocarbon tower 5, deethanizing column 8 and debutanizing tower 10 and are connected successively; The liquid phase outlet of LTS 4 inserts the middle part opening for feed (can directly insert, also can insert through main heat exchanger 3 earlier again, reclaim cold so that liquid phase material is carried out re-heat) of deethanizing column 8; The gaseous phase outlet of LTS 4 and secondary take off hydrocarbon tower 5 and are connected (can directly connect, connect after also can passing through J-T throttling valve or swell refrigeration machine again, so that gaseous phase materials is further freezed, utilize the further cooled natural gas of safety pressure margin of virgin gas); The liquid hydrocarbon outlet that secondary takes off hydrocarbon tower 5 bottoms is connected with the top opening for feed of deethanizing column 8; The gaseous phase materials outlet at deethanizing column 8 tops inserts main heat exchanger 3 (can directly insert, also can so that to the supercharging of deethanizing cat head gas, reduce the deethanizing column working pressure earlier through inserting behind the deethanizing cat head air compressor 6 again); The product gas outlet that secondary takes off hydrocarbon tower 5 is connected with main heat exchanger 3; The liquid hydrocarbon outlet of deethanizing column 8 bottoms is connected with the middle part opening for feed of debutanizing tower 10, is provided with deethanizing column reboiler 7 in deethanizing column 8 bottoms, is used to deethanizing column 8 thermal source is provided; Be provided with debutanizing tower water cooler 11 at debutanizing tower 10 tops, be used to debutanizing tower 10 cold is provided; Be provided with debutanizing tower reboiler 9 in debutanizing tower 10 bottoms, be used to debutanizing tower 10 thermal source is provided.
Because the cold recovery of the precooling of raw natural gas, condensation, product Sweet natural gas and the LTS liquid phase material of deethanizing cat head gas realizes in main heat exchanger 3 that all therefore also being provided with compound cryogen refrigeration system is that main heat exchanger 3 provides insufficient cold.Compound cryogen refrigeration system comprises compound cryogen compressor 1 and compound cryogen water cooler 2.The import of compound cryogen compressor 1 is connected with the compound cryogen outlet of the gaseous state of main heat exchanger 3, and the outlet of compound cryogen compressor 1 is connected with compound cryogen water cooler 2, and the outlet of compound cryogen water cooler 2 is connected with main heat exchanger 3.Refrigerating efficiency for the flow pattern of improving two in the main heat exchanger and the process of raising; Also can gas-liquid separator be set, isolated gas phase and liquid phase material are inserted main heat exchanger respectively at the inter-stage of compound cryogen compressor or the outlet of compound cryogen water cooler.
A kind of compound cryogen refrigeration secondary of said apparatus that utilizes takes off the hydrocarbon methods of light hydrocarbon recovery, comprises the steps:
The first step, compound cryogen refrigeration:
By compound cryogen refrigeration system is that main heat exchanger 3 provides insufficient cold.Compound cryogen refrigeration system comprises compound cryogen compressor 1 and compound cryogen water cooler 2.At first; Get into compression in the compound cryogen compressor 1 from the compound cryogen of the lower gaseous state of the pressure of main heat exchanger 3; Deliver to desuperheating and partial condensation in the compound cryogen water cooler 2 after pressure raises, deliver in the main heat exchanger 3 all condensations again and cross cold after, expenditure and pressure obtains cryogenic compound cryogen; Compound cryogen is sent back in the main heat exchanger 3 to it and is sent back in the compound cryogen compressor 1 after cold is provided, thereby accomplishes compound cryogen process of refrigeration.
Compound cryogen is N
2, methane, ethane, ethene, propane, propylene, butane, pentane, Sweet natural gas, liquefied gas one or more.
Second goes on foot, once takes off hydrocarbon:
The exsiccant Sweet natural gas is delivered to precooling in the main heat exchanger 3, get into then and carry out in the LTS 4 separating of gaseous phase materials and liquid phase material, once take off hydrocarbon thereby accomplish;
The 3rd step, secondary take off hydrocarbon:
Deliver to secondary from the gaseous phase materials of LTS 4 and take off hydrocarbon tower 5; Take off in the hydrocarbon tower 5 at secondary; From the overhead condensation liquid of the deethanizing column in the main heat exchanger 38 and gaseous phase materials counter current contact in tower, because the C in the overhead condensation liquid of deethanizing column 8 from LTS 4
2C in the component lower temperature separator
2Component concentration is high, thus the generating gasification refrigeration, with the C that once takes off in the gaseous phase materials that hydrocarbon obtains
3Reach above component and wash, conduct heat simultaneously and mass transfer process, improved C
3Yield is secondary and takes off the hydrocarbon process; The virgin gas that takes off behind the hydrocarbon through secondary is product gas, send into be recovered in the main heat exchanger 3 behind the cold outer defeated;
The 4th step, deethanizing:
Opening for feed gets into deethanizing column 8 from the top of deethanizing column 8 to take off the liquid hydrocarbon that comes out hydrocarbon tower 5 bottoms from secondary; Deliver to heating recovery cold in the main heat exchanger 3 from the liquid phase material of LTS 4, deliver to of the charging of the middle part of deethanizing column 8 again as deethanizing column 8; The gaseous phase materials at deethanizing column 8 tops is sent into partial condensation in the main heat exchanger 3 (can directly send into, also can send into through after 6 superchargings of deethanizing cat head air compressor earlier), and the liquid hydrocarbon of deethanizing column 8 bottoms is delivered to the middle part of debutanizing tower 10 as its charging;
The 5th step, debutylize:
Liquid hydrocarbon feed from deethanizing column 8 bottoms is distillated in debutanizing tower 10, obtains the liquefied gas product at the top of debutanizing tower 10, obtains the stable light hydrocarbon product in the bottom of debutanizing tower 10.
Claims (9)
1. a compound cryogen refrigeration secondary takes off the hydrocarbon light ends unit, and it is characterized in that: main heat exchanger, LTS, secondary take off hydrocarbon tower, deethanizing column and debutanizing tower and be connected successively; The liquid phase outlet of LTS inserts the middle part opening for feed of deethanizing column; The gaseous phase outlet of LTS takes off the hydrocarbon tower with secondary and is connected; The liquid hydrocarbon outlet that secondary takes off the hydrocarbon tower bottom is connected with the top opening for feed of deethanizing column; The gaseous phase materials outlet at deethanizing column top inserts main heat exchanger; The product gas outlet that secondary takes off the hydrocarbon tower is connected with main heat exchanger; The liquid hydrocarbon outlet of deethanizing column bottom is connected with the middle part opening for feed of debutanizing tower, is provided with the deethanizing column reboiler in the deethanizing column bottom; Be provided with the debutanizing tower water cooler at the debutanizing tower top; Be provided with the debutanizing tower reboiler in the debutanizing tower bottom; Also being provided with compound cryogen refrigeration system is connected with main heat exchanger.
2. compound cryogen refrigeration secondary according to claim 1 takes off the hydrocarbon light ends unit; It is characterized in that: said compound cryogen refrigeration system comprises compound cryogen compressor and compound cryogen water cooler; The import of said compound cryogen compressor is connected with the compound cryogen outlet of the gaseous state of main heat exchanger; The outlet of compound cryogen compressor is connected with compound cryogen water cooler, and the outlet of compound cryogen water cooler is connected with main heat exchanger.
3. compound cryogen refrigeration secondary according to claim 2 takes off the hydrocarbon light ends unit; It is characterized in that: the outlet of the inter-stage of said compound cryogen compressor or compound cryogen water cooler is provided with gas-liquid separator, and isolated gas phase and liquid phase material are inserted main heat exchanger respectively.
4. compound cryogen refrigeration secondary according to claim 1 takes off the hydrocarbon light ends unit, and it is characterized in that: the liquid phase outlet of said LTS inserts the middle part opening for feed of deethanizing column earlier again through main heat exchanger.
5. compound cryogen refrigeration secondary according to claim 1 takes off the hydrocarbon light ends unit, it is characterized in that: take off the hydrocarbon tower with secondary again behind the gaseous phase outlet process J-T throttling valve of said LTS or the swell refrigeration machine and be connected.
6. compound cryogen refrigeration secondary according to claim 1 takes off the hydrocarbon light ends unit, it is characterized in that: the gaseous phase materials outlet at said deethanizing column top is earlier through inserting main heat exchanger behind the deethanizing cat head air compressor again.
7. a compound cryogen refrigeration secondary takes off the hydrocarbon methods of light hydrocarbon recovery, it is characterized in that: comprise the steps:
The first step, compound cryogen refrigeration: by compound cryogen refrigeration system is that main heat exchanger provides insufficient cold;
Second goes on foot, once takes off hydrocarbon:
The exsiccant Sweet natural gas is delivered to precooling in the main heat exchanger, get into then and carry out in the LTS separating of gaseous phase materials and liquid phase material, once take off hydrocarbon thereby accomplish;
The 3rd step, secondary take off hydrocarbon:
Deliver to secondary from the gaseous phase materials of LTS and take off the hydrocarbon tower; Take off in the hydrocarbon tower at secondary; From the overhead condensation liquid of the deethanizing column in the main heat exchanger and gaseous phase materials counter current contact in tower from LTS, the generating gasification refrigeration is with the C that once takes off in the gaseous phase materials that hydrocarbon obtains
3Reach above component and wash, conduct heat simultaneously and mass transfer process; Take off the product gas behind the hydrocarbon through secondary, send into be recovered in the main heat exchanger behind the cold outer defeated;
The 4th step, deethanizing:
Opening for feed gets into deethanizing column from the top of deethanizing column to take off the liquid hydrocarbon that the hydrocarbon tower bottom comes out from secondary; Deliver to heating recovery cold in the main heat exchanger from the liquid phase material of LTS, deliver to of the charging of the middle part of deethanizing column again as deethanizing column; The gaseous phase materials at deethanizing column top is sent into condensation in the main heat exchanger, and the liquid hydrocarbon of deethanizing column bottom is delivered to the middle part of debutanizing tower, as the charging of debutanizing tower;
The 5th step, debutylize:
Liquid hydrocarbon feed from the deethanizing column bottom is distillated in debutanizing tower, obtains the liquefied gas product at the top of debutanizing tower, obtains the stable light hydrocarbon product in the bottom of debutanizing tower.
8. compound cryogen refrigeration secondary according to claim 7 takes off the hydrocarbon methods of light hydrocarbon recovery, and it is characterized in that: said compound cryogen is N
2, methane, ethane, ethene, propane, propylene, butane, pentane, Sweet natural gas, liquefied gas one or more.
9. compound cryogen refrigeration secondary according to claim 7 takes off the hydrocarbon methods of light hydrocarbon recovery, it is characterized in that: the gaseous phase materials at deethanizing column top is earlier through sending into condensation in the main heat exchanger after the supercharging of deethanizing cat head air compressor again.
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| CN104194852A (en) * | 2014-08-20 | 2014-12-10 | 四川科比科油气工程有限公司 | High-yield light hydrocarbon recovery method from low-pressure natural gas |
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| CN107163975A (en) * | 2017-05-27 | 2017-09-15 | 中国石油集团工程设计有限责任公司 | The device and method that a kind of lighter hydrocarbons depth is reclaimed |
| CN107163975B (en) * | 2017-05-27 | 2019-02-19 | 中国石油工程建设有限公司 | A kind of device and method of lighter hydrocarbons depth recycling |
| CN111164187A (en) * | 2017-08-08 | 2020-05-15 | 沙特阿拉伯石油公司 | Simultaneous conversion of natural gas condensate fractionation plant waste heat to electricity and cooling capacity using an organic-based integrated compressor-ejector-expander three cycle system |
| CN114479905A (en) * | 2020-10-27 | 2022-05-13 | 中国石油化工股份有限公司 | Light hydrocarbon recovery system and light hydrocarbon recovery process |
| CN114479905B (en) * | 2020-10-27 | 2023-04-25 | 中国石油化工股份有限公司 | Light hydrocarbon recovery system and light hydrocarbon recovery process |
| CN114073863A (en) * | 2021-11-23 | 2022-02-22 | 江苏永诚装备科技有限公司 | Multiple dealkylation device of light hydrocarbon recovery device |
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