CN105783421B - A kind of method and device of natural gas lighter hydrocarbons recovery - Google Patents
A kind of method and device of natural gas lighter hydrocarbons recovery Download PDFInfo
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- CN105783421B CN105783421B CN201610211993.6A CN201610211993A CN105783421B CN 105783421 B CN105783421 B CN 105783421B CN 201610211993 A CN201610211993 A CN 201610211993A CN 105783421 B CN105783421 B CN 105783421B
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/0204—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the feed stream
- F25J3/0209—Natural gas or substitute natural gas
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/0228—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream
- F25J3/0233—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of CnHm with 1 carbon atom or more
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/0228—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream
- F25J3/0242—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of CnHm with 3 carbon atoms or more
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/0228—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream
- F25J3/0247—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of CnHm with 4 carbon atoms or more
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2200/00—Processes or apparatus using separation by rectification
- F25J2200/04—Processes or apparatus using separation by rectification in a dual pressure main column system
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2200/00—Processes or apparatus using separation by rectification
- F25J2200/74—Refluxing the column with at least a part of the partially condensed overhead gas
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2200/00—Processes or apparatus using separation by rectification
- F25J2200/78—Refluxing the column with a liquid stream originating from an upstream or downstream fractionator column
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2270/00—Refrigeration techniques used
- F25J2270/12—External refrigeration with liquid vaporising loop
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2270/00—Refrigeration techniques used
- F25J2270/60—Closed external refrigeration cycle with single component refrigerant [SCR], e.g. C1-, C2- or C3-hydrocarbons
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2270/00—Refrigeration techniques used
- F25J2270/90—External refrigeration, e.g. conventional closed-loop mechanical refrigeration unit using Freon or NH3, unspecified external refrigeration
Abstract
The invention discloses a kind of method and devices of natural gas lighter hydrocarbons recovery, it is therefore intended that the light hydrocarbon recovery rate solved present in existing recovery device of natural gas lighter hydrocarbon is low, and separation accuracy is low, and regulating measure is single, air source problem poor for applicability.It includes the following steps：Unstripped gas enters main heat exchanger, enters first knockout tower after cooling, and first knockout tower top gaseous phase is used as product dry gas, bottom of tower liquid phase to be sent into dethanizer after re-heat；Deethanizer overhead gas phase carries out gas-liquid separation after main heat exchanger cools down, and liquid phase returns to dethanizer, and gas phase enters first knockout tower after further condensation, washed to unstripped gas；Dethanizer tower bottom liquid mutually introduces debutanizing tower；Liquefied petroleum gas product and condensation oil product are respectively obtained from debutanizing tower tower top and bottom of tower；Cold needed for lighter hydrocarbons recovery process is provided by refrigeration system, and refrigeration system uses two-stage throttling refrigeration.There is the present invention regulating measure to enrich, air source is adaptable, low power consumption and other advantages.
Description
Technical field
The present invention relates to natural gas processing field, especially condensation method natural gas lighter hydrocarbons recovery field, specially a kind of days
The method and device of right gas lighter hydrocarbons recovery.
Background technology
The hydrocarbon dew point that natural gas lighter hydrocarbons recovery is on the one hand to control natural gas is kept away with reaching commodity makings figureofmerit
Exempt from gas liquid two-phase flow；On the other hand, the liquid hydrocarbon of recycling has prodigious economic value, can both be directly used as exotic fuels,
It also is used as industrial chemicals.
Currently, methods of light hydrocarbon recovery includes mainly absorption method, oil-absorption process and condensation separation method.Absorption method is to utilize to have
The solid absorbent of porous structure is to the difference of hydrocarbon component adsorption capacity power, and the method for enabling hydrocarbon gas to detach,
Its principle and flow are similar to molecular sieve adsorbing and dewatering.Oil-absorption process is dissolved in absorbing oil based on each component in natural gas
The difference of degree, and the method for enabling different hydrocarbons gas to detach.Condensation separation method is cold using each hydrocarbon component in natural gas
The different feature of solidifying temperature, is cooled to certain temperature by freezing by natural gas, thus by the higher hydro carbons condensation separation of boiling point, and
The method that condensate liquid is fractionated into qualified products.Since there are high energy consumption, operating cost height and products for absorption method and oil-absorption process
The disadvantages such as yield is low, are gradually replaced by more economical and advanced condensation separation method.
Chinese patent CN204661631 U, CN103822438 A etc. disclose condensation separation method process for recovering light hydrocarbon or dress
It sets, is usually that pretreatment, condensed natural gas are introduced into cryogenic separation tank, the gas phase detached in cryogenic separation tank is through re-heat
Afterwards be used as product dry gas outside it is defeated, liquid phase is further detached into dethanizer.However, existing condensation method natural gas methods of light hydrocarbon recovery
In have the disadvantage that：
（1）Light hydrocarbon recovery rate is not high, and the C3 rate of recovery is generally 60% ~ 80%；
（2）Separation accuracy is low, the hydrocarbon liquid inferior quality of separation, and most of technique cannot be by liquefied petroleum gas components（C3
And C4）With condensation oil ingredient（C5~C11+）It efficiently separates；
（3）Existing natural gas methods of light hydrocarbon recovery is only capable of processing C3+（C3+ refers to the hydro carbons of C3 and C3 or more）Content is higher
Moisture, it is difficult to the light hydrocarbon component in recovery channel gas；
（4）Regulating measure is single, and air source is poor for applicability, and the scope of application is limited.
In view of defect existing for existing condensation separation method natural gas process for recovering light hydrocarbon, there is an urgent need to develop a kind of adjusting hands
Duan Fengfu, adaptability to raw material are strong, low energy consumption, C3The methods of light hydrocarbon recovery and/or device of high income.
Invention content
The goal of the invention of the present invention is：It is low for the light hydrocarbon recovery rate present in existing natural gas lighter hydrocarbons recovery, separation
Precision is low, and regulating measure is single, air source problem poor for applicability, provides a kind of method and device of natural gas lighter hydrocarbons recovery.This
There is regulating measure to enrich for invention, adaptability to raw material is strong, low energy consumption, C3The advantages that high income, is worth large-scale promotion and application.
To achieve the goals above, the present invention adopts the following technical scheme that：
A kind of method of natural gas lighter hydrocarbons recovery, includes the following steps：
（1）De- hydrocarbon just detaches
Unstripped gas is entered in first knockout tower by first knockout tower lower part after main heat exchanger cools down, unstripped gas and carrys out autospasy second
The material of alkane overhead separator counter current contacting in first knockout tower, the gaseous phase materials for just detaching column overhead separation are multiple through main heat exchanger
Dry gas output of products is used as after heat；The liquid phase material of first knockout tower bottom of tower is after main heat exchanger re-heat, into dethanizer rectifying；
（2）Deethanization rectifying
From the gaseous phase materials of dethanizer Base top contact after main heat exchanger cools down, carried out into deethanization overhead separator
The gaseous phase materials of gas-liquid separation, the separation of deethanization overhead separator enter just after main heat exchanger condenses from first knockout tower top
In knockout tower, the liquid phase material of deethanization overhead separator separation returns in dethanizer, the liquid drawn from Deethanizer bottom
Phase materials enter debutanizing tower rectifying；
（3）Debutanization rectifying
After the gaseous phase materials of debutanizing tower Base top contact are condensed, part returns to debutanizing tower, partly as liquefaction stone
Oil gas product exports；From debutanizing tower bottom draw liquid phase material after cooling, as condensate output of products；
（4）Cryogen refrigeration recycles
It is recycled by cryogen refrigeration and provides cold for main heat exchanger；
In the step 2, dethanizer is connected with deethanization tower bottom reboiler and deethanization tower bottom reboiler is deethanization
Tower provides rectifying institute calorific requirement；
In the step 3, debutanizing tower is connected with debutanization tower bottom reboiler and debutanization tower bottom reboiler is debutanization
Tower provides rectifying institute calorific requirement.
The main heat exchanger is composed of using a heat exchanger or more heat exchangers.
The main heat exchanger includes evaporator one, evaporator two；
In the step 1, unstripped gas is after the cooling of evaporator two, into first knockout tower；
In the step 2, the gaseous phase materials of dethanizer Base top contact are after the cooling of evaporator one, into deethanization tower top
Separator.
The operation of the step 4 is as follows：The vapor phase refrigerant drawn from two level knockout drum tank deck is freezed through level-one presses
Contracting machine supercharging after, be pressurized to setting pressure into two level refrigeration compressor, through two level refrigeration compressor refrigerant after supercharged according to
It is secondary to be condensed, after level-one throttling, carry out gas-liquid separation into level-one knockout drum；The separation of level-one knockout drum tank deck
Vapor phase refrigerant returns to the supercharging of two level refrigeration compressor；The liquid-phase refrigerant portion of level-one knockout drum tank bottom separation enters master
After heat exchanger provides cold for main heat exchanger high-temperature region, level-one knockout drum is returned to, Partial Liquid Phase refrigerant is through two-step throttle
Enter two level knockout drum afterwards；It is main heat exchanger low temperature that the liquid phase refrigerant of two level knockout drum separation, which enters main heat exchanger,
After area provides cold, two level knockout drum is returned to, the vapor phase refrigerant of two level knockout drum tank deck returns to stage compressor
Supercharging.
In the step 4, refrigerant be ethylene, ethane, propylene, propane, butylene, butane, ammonia, one kind in freon or
It is a variety of.
Piece-rate system at the beginning of the device of method for aforementioned natural gas lighter hydrocarbons recovery, including de- hydrocarbon, main heat exchanger, based on change
The cryogen refrigeration circulatory system of hot device offer cold, deethanization distillation system, debutanization distillation system；
Just piece-rate system includes unstripped gas feeding mechanism, first knockout tower, the dry gas for collecting dry gas product to the de- hydrocarbon
Collection device, the unstripped gas feeding mechanism is connected with main heat exchanger, first knockout tower lower part feed inlet successively by pipeline, described
Just separation column overhead discharge port is connected with main heat exchanger, dry gas collection device successively by pipeline；
The deethanization distillation system includes dethanizer, deethanization overhead separator, the de- second being connected with dethanizer
Alkane tower bottom reboiler, the just knockout tower bottom of tower discharge port pass through the pipeline successively feed inlet with main heat exchanger, in the middle part of dethanizer
Be connected, the deethanizer overhead discharge port by pipeline successively on main heat exchanger, deethanization overhead separator, dethanizer
Portion's feed inlet be connected, the deethanization overhead separator top discharge mouth by pipeline successively on main heat exchanger, first knockout tower
Portion's feed inlet is connected, and dethanizer bottom of tower discharge port is connected by pipeline with debutanizing tower；
The debutanization distillation system includes debutanizing tower, debutanization overhead condenser, debutanization tower bottom reboiler, de- fourth
Alkane bottom of tower cooler, liquefied petroleum gas output device, condensate output device, the debutanizing tower, debutanization overhead condenser,
Liquefied petroleum gas output device is sequentially connected by pipeline, and the debutanizing tower, debutanization tower bottom reboiler, debutanizing tower bottom are cold
But device, condensate output device are sequentially connected by pipeline.
The cryogen refrigeration circulatory system include two level knockout drum, level-one refrigeration compressor, two level refrigeration compressor,
Cryogen condenser, level-one throttle valve, level-one knockout drum, two-step throttle valve；
The two level knockout drum, level-one refrigeration compressor, two level refrigeration compressor, cryogen condenser, level-one throttling
Valve, level-one knockout drum, two-step throttle valve, two level knockout drum are sequentially connected by pipeline, the level-one gas-liquid separation
Upper end discharge port is connected by pipeline with two level refrigeration compressor entrance, and level-one knockout drum bottom end discharge port passes through
Pipeline is connected with main heat exchanger, level-one knockout drum feed inlet successively, and two level knockout drum bottom end discharge port passes through
Pipeline is connected with main heat exchanger, two level knockout drum feed inlet successively.
Refrigerant flowing between the level-one knockout drum and main heat exchanger is realized by thermal siphon.
Refrigerant flowing between the two level knockout drum and main heat exchanger is realized by thermal siphon.
For foregoing problems, the present invention provides a kind of method and device of natural gas lighter hydrocarbons recovery.This method includes as follows
Step：De- hydrocarbon just separation, deethanization rectifying, debutanization rectifying, cryogen refrigeration cycle.During de- hydrocarbon just detaches, unstripped gas enters master
Heat exchanger cools down, and enters first knockout tower from tower lower part after cooling；Gaseous phase materials from deethanization overhead separator through cooling,
After condensation from first knockout tower top enter first knockout tower, tower top liquid phase and bottom of tower the gas phase counter current contacting in tower of first knockout tower,
C3+ components in unstripped gas are washed.Gas phase rich in C1, C2 is drawn from first separation column overhead, as dry after re-heat
It is defeated outside gas product；Liquid phase rich in C3, C4 and C5+ component is drawn from bottom of tower, into main heat exchanger re-heat after pump is pressurized, then into
Enter dethanizer.
Further the ethane in the liquid phase of first knockout tower bottom of tower is removed in dethanizer, needed for dethanizer rectifying
Heat provided by deethanization tower bottom reboiler.From the gaseous phase materials of dethanizer Base top contact through main heat exchanger cooling, part
After condensation, gas-liquid separation is carried out into deethanization overhead separator, the gaseous phase materials of deethanization overhead separator separation are changed through master
Hot device further after cooling, condensation, enters from first knockout tower top in first knockout tower, the liquid phase of deethanization overhead separator separation
Material returns in dethanizer, and the liquid phase material drawn from Deethanizer bottom enters rectifying in debutanizing tower.
In debutanizing tower further in the liquid phase of dethanizer bottom of tower liquefied petroleum gas components and condensation oil ingredient into
Row separation.From the gaseous phase materials of debutanizing tower Base top contact（Main component is C3, C4）After condensed, part returns to debutanization
Tower is partly used as liquefied petroleum gas product to export；The liquid phase material drawn from debutanizing tower bottom（Main component is C5+ hydro carbons）
After cooling, as condensate output of products.
Cold needed for lighter hydrocarbons recovery process is provided by refrigeration system, and refrigeration system uses two-stage throttling refrigeration, cryogen system
SAPMAC method operation is as follows.
The vapor phase refrigerant drawn from two level knockout drum tank deck, after the supercharging of level-one refrigeration compressor, with level-one gas
The vapor phase refrigerant that liquid knockout drum tank deck is drawn is converged, and enters back into two level refrigeration compressor and continues to be pressurized to setting pressure.Supercharging
After rear refrigerant is condensed, level-one throttling is carried out, the gas-liquid mixture after throttling enters level-one knockout drum and carries out gas-liquid
Separation.Gas phase is drawn from tank deck, and into two level refrigeration compressor, liquid phase is drawn from tank bottom, partly enters main heat exchanger, based on change
Hot device high-temperature region provides cold, and two level knockout drum is partly entered after two-step throttle.It is drawn from main heat exchanger high-temperature region
Gaseous refrigerant returns to level-one knockout drum.The liquid phase of two level knockout drum is drawn from tank bottom, into main heat exchanger, based on
Heat exchanger low-temperature space provides cold；The gaseous refrigerant drawn from main heat exchanger low-temperature space returns to two level knockout drum, completes
Refrigeration cycle.
The present invention is capable of the means of enriching gas lighter hydrocarbons recovery, meanwhile, the present invention have preferable adaptability to raw material, compared with
Low energy consumption and higher C3Yield has preferable application prospect.
In conclusion compared with the conventional method, the invention has the advantages that.
1）The present invention can select suitable refrigerant and choke pressure according to air source component feature, and same flow is realized different
Separation condition can have the characteristics that unstripped gas is adaptable in the variation of a wide range of endoadaptation gas source condition.
2）In the present invention, condensed, gas-liquid separation, the liquid phase washing material gas condensed again using deethanizer overhead gas phase
Method, can effectively remove the C3+ components in unstripped gas.Certain treatment scale is 70 × 104Nm3The natural gas lighter hydrocarbons recovery of/d fills
It sets（C3+ volume content is 11.35%）In, using C of the present invention3The rate of recovery be 93%, higher than data 80% disclosed in traditional handicraft,
With significant progress.
3）The refrigeration system of the present invention uses two-step throttle technology, is provided respectively for main heat exchanger high-temperature region and low-temperature space cold
Amount, heat transfer temperature difference is small, has preferable energy-saving effect；In addition, the present invention is classified back according to each cold flow point section difference
Cold energy is received, refrigeration system energy consumption is effectively reduced.
Description of the drawings
Examples of the present invention will be described by way of reference to the accompanying drawings, wherein：
Fig. 1 is the structural schematic diagram of embodiment 1.
In Fig. 1：1 is main heat exchanger, and 2 be first knockout tower, and 3 be dethanizer feed pump, and 4 be dethanizer, and 5 be deethanization
Overhead separator, 6 pump for deethanizer reflux, and 7 be deethanization tower bottom reboiler, and 8 be debutanizing tower, and 9 is cold for debutanization tower top
Condenser, 10 be debutanization overhead separator, and 11 be debutanizing tower reflux pump, and 12 be debutanization tower bottom reboiler, and 13 be debutanization
Bottom of tower cooler, 14 be level-one refrigeration compressor, and 15 be two level refrigeration compressor, and 16 be cryogen condenser, and 17 be level-one gas-liquid
Knockout drum, 18 be two level knockout drum, and I is level-one throttle valve, and II is two-step throttle valve.
Fig. 2 is the structural schematic diagram of embodiment 2.
In Fig. 2：1 is unstripped gas heat exchanger, and 2 be evaporator two, and 3 be first knockout tower, and 4 be first knockout tower top heat exchanger, and 5 are
Dethanizer feed pump, 6 be dethanizer, and 7 be evaporator one, and 8 be deethanization overhead separator, and 9 pump for deethanizer reflux,
10 be deethanization tower bottom reboiler, and 11 be debutanizing tower, and 12 be debutanization overhead condenser, and 13 be debutanization overhead separator,
14 be debutanizing tower reflux pump, and 15 be debutanization tower bottom reboiler, and 16 be debutanizing tower bottom cooler, and 17 be level-one refrigerant compression
Machine, 18 be two level refrigeration compressor, 19 be cryogen condenser, 20 be level-one knockout drum, 21 be two level knockout drum, I
It is two-step throttle valve for level-one throttle valve, II.
Specific implementation mode
All features disclosed in this specification or disclosed all methods or in the process the step of, in addition to mutually exclusive
Feature and/or step other than, can combine in any way.
Any feature disclosed in this specification unless specifically stated can be equivalent or with similar purpose by other
Alternative features are replaced.That is, unless specifically stated, each feature is an example in a series of equivalent or similar characteristics
.
Embodiment 1
The flow diagram of the present embodiment is as shown in Figure 1, the workflow of the present embodiment is as follows.
Unstripped gas enters the cooling of main heat exchanger 1, and unstripped gas after cooling enters first knockout tower 2 from 2 lower part of first knockout tower
In.Gas phase from deethanization overhead separator 5（Main component is C1 and C2）After the cooling of main heat exchanger 1, from first knockout tower 2
Top enters in first knockout tower 2, tower top liquid phase and bottom of tower the gas phase counter current contacting in first knockout tower 2, by the C3+ groups in unstripped gas
Divide and washs.
Gaseous phase materials rich in C1, C2 are drawn from 2 tower top of first knockout tower, after 1 re-heat of main heat exchanger, as product dry gas
It is outer defeated；Liquid phase material rich in C3, C4 and C5+ is drawn from 2 bottom of tower of first knockout tower, after the supercharging of dethanizer feed pump 3, warp
1 re-heat of main heat exchanger enters back into 4 rectifying of dethanizer.
The gaseous phase materials drawn from 4 tower top of dethanizer are after the cooling of main heat exchanger 1, into deethanization overhead separator 5
Carry out gas-liquid separation.The gaseous phase materials that deethanization overhead separator 5 detaches return to first point after main heat exchanger 1 is further cooling
From tower 2, unstripped gas is washed.The liquid phase material that deethanization overhead separator 5 detaches is through 6 supercharging of deethanizer reflux pump
Afterwards, dethanizer 4 is returned.The liquid phase material drawn from 4 bottom of tower of dethanizer enters rectifying in debutanizing tower 8.
The gaseous phase materials drawn from 8 tower top of debutanizing tower（Main component is C3 and C4）It is cold through debutanization overhead condenser 9
But after, into debutanization overhead separator 10, on-condensible gas（If any）It is discharged by diffusion system, from debutanization overhead separator
For 10 liquid phase materials drawn after the supercharging of debutanizing tower reflux pump 11, part returns to debutanizing tower 8, and part is drawn as liquefaction stone
It is defeated outside oil gas product.The liquid phase material drawn from 8 bottom of tower of debutanizing tower（Main component is C5+）Through debutanizing tower bottom cooler 13
After cooling, as defeated outside condensation oil product.
The heat of 8 rectifying of dethanizer 4 and debutanizing tower is boiled by deethanization tower bottom reboiler 7 and debutanizing tower bottom again respectively
Device 12 provides.
Cold needed for the present embodiment light hydrocarbon recovery system is provided by refrigeration system（Use refrigeration system for main heat exchanger
1 provides cold）, refrigeration system is using two-step throttle Refrigeration Technique.Workflow is as follows：Draw from 18 tank deck of two level knockout drum
After the vapor phase refrigerant gone out enters the supercharging of level-one refrigeration compressor 14, then the gas phase system with the extraction of 17 tank deck of level-one knockout drum
After cryogen converges, continue to be pressurized to setting pressure into two level refrigeration compressor 15.Refrigerant after supercharged is through cryogen condenser
It after 16 coolings, condensation, then depressurizes and throttles through level-one throttle valve I, finally enter in level-one knockout drum 17.Level-one gas-liquid separation
The gas phase of tank 17 is drawn from tank deck, returns to two level refrigeration compressor 15.The liquid phase of level-one knockout drum 17 is drawn from tank bottom divides
Make two strands, wherein one liquid phase enters main heat exchanger 1, and cold is provided for 1 high-temperature region of main heat exchanger；Another burst of liquid phase is through two level section
It flows valve II and carries out second depressurized.The gaseous refrigerant drawn from 1 high-temperature region of main heat exchanger returns to level-one knockout drum 17, through two
Refrigerant after grade decompression enters two level knockout drum 18.The gas phase of two level knockout drum 18 is drawn from tank deck, into one
Grade refrigeration compressor 14；The liquid phase of two level knockout drum 18 is drawn from tank bottom, is 1 low temperature of main heat exchanger into main heat exchanger 1
Area provides cold, and the gaseous refrigerant drawn from 1 low-temperature space of main heat exchanger returns to two level knockout drum 18, completes refrigeration and follows
Ring.
In the present embodiment, unstripped gas treatment scale is 70 × 104Nm3/ d, C in unstripped gas3+ volume content be 11.35%,
Using C of the present invention3The rate of recovery be 93%.
Embodiment 2
The flow diagram of the present embodiment is as shown in Figure 2.
In the present embodiment, main heat exchanger is composed of more heat exchangers, and the workflow of the present embodiment is as follows.
Unstripped gas enters the cooling of unstripped gas heat exchanger 1, after unstripped gas after cooling enters the further cooling of evaporator 22,
Enter in first knockout tower 3 from tower lower part.Gas phase from deethanization overhead separator 8（Main component is C1 and C2）Successively through steaming
After sending out device 22, the cooling of first knockout tower top heat exchanger 4, enter first knockout tower 3, tower top liquid phase and bottom of tower gas from 3 top of first knockout tower
The mutually counter current contacting in 3 tower of first knockout tower, the C3+ components in unstripped gas are washed.
Gaseous phase materials rich in C1, C2 are drawn from 3 tower top of first knockout tower, first recycle cold through first knockout tower top heat exchanger 4
Afterwards, unstripped gas heat exchanger 1 is entered back into, as defeated outside product dry gas after re-heat；Liquid phase rich in C3, C4 and C5+ is from first knockout tower
3 bottoms of tower are drawn, and after the supercharging of dethanizer feed pump 5, into 1 re-heat of unstripped gas heat exchanger, enter back into 6 rectifying of dethanizer.
The gaseous phase materials drawn from 6 tower top of dethanizer are after the cooling of evaporator 1, into deethanization overhead separator 8
Carry out gas-liquid separation.The gaseous phase materials that deethanization overhead separator 8 detaches are cold through evaporator 22 and first knockout tower top heat exchanger 4
But after, enter first knockout tower 3 from 3 top of first knockout tower, unstripped gas is washed.The liquid that deethanization overhead separator 8 detaches
Phase materials return to dethanizer 6 after 9 supercharging of deethanizer reflux pump.The liquid phase material drawn from 6 bottom of tower of dethanizer enters
Rectifying in debutanizing tower 11.
The gaseous phase materials drawn from 11 tower top of debutanizing tower（Main component is C3 and C4）Through debutanization overhead condenser 12
After cooling, into debutanization overhead separator 13, on-condensible gas（If any）It is discharged by diffusion system, is detached from debutanization tower top
For the liquid phase material that device 13 is drawn after the supercharging of debutanizing tower reflux pump 14, part returns to debutanizing tower 11, and part, which is drawn, is used as liquid
It is defeated outside lpg product.The liquid phase material drawn from 11 bottom of tower of debutanizing tower（Main component is C5+）It is cold through debutanizing tower bottom
But after device 16 cools down, as defeated outside condensation oil product.
The heat of 11 rectifying of dethanizer 6 and debutanizing tower respectively by deethanization tower bottom reboiler 10 and debutanizing tower bottom again
Device 15 is boiled to provide.
Cold needed for the present embodiment light hydrocarbon recovery system is provided by refrigeration system, and refrigeration system is freezed using two-step throttle
Technique.Workflow is as follows：The vapor phase refrigerant drawn from 21 tank deck of two level knockout drum, into level-one refrigeration compressor 17
After supercharging, then with 20 tank deck of level-one knockout drum draw vapor phase refrigerant converge after, into two level refrigeration compressor 18 after
It is continuous to be pressurized to setting pressure.Refrigerant after supercharged is cooled down, after condensation through cryogen condenser 19, then is depressurized through level-one throttle valve I
After throttling, subsequently into level-one knockout drum 20.The gas phase of level-one knockout drum 20 is drawn from tank deck, into two-stage system
Cold compressor 18.The liquid phase that level-one knockout drum 20 detaches is allocated as two strands from tank bottom extraction, and wherein one liquid phase enters evaporation
Device 1 evaporates cooling, and another burst of liquid phase carries out second depressurized through two-step throttle valve II.The gaseous refrigerant drawn from evaporator 1
Agent returns to level-one knockout drum 20, and the refrigerant after second depressurized enters two level knockout drum 21.Two level gas-liquid separation
The gas phase of tank 21 is drawn from tank deck, into level-one refrigeration compressor 17；The liquid phase of two level knockout drum 21 is drawn from tank bottom, into
Enter evaporator 22 and evaporate cooling, the gaseous refrigerant drawn from evaporator 22 returns to two level knockout drum 21, completes refrigeration
Cycle.
In the present embodiment, unstripped gas treatment scale is 50 × 104Nm3/ d, C in unstripped gas3+ volume content be 18.55%,
Using C of the present invention3The rate of recovery be 95.4%.
The invention is not limited in specific implementation modes above-mentioned.The present invention, which expands to, any in the present specification to be disclosed
New feature or any new combination, and disclose any new method or process the step of or any new combination.
Claims (9)
1. a kind of method of natural gas lighter hydrocarbons recovery, which is characterized in that include the following steps：
（1）De- hydrocarbon just detaches
Unstripped gas after main heat exchanger cools down, by first knockout tower lower part enter first knockout tower in, unstripped gas with come from dethanizer
The material of top separator counter current contacting in first knockout tower just detaches the gaseous phase materials of column overhead separation after main heat exchanger re-heat
As dry gas output of products；The liquid phase material of first knockout tower bottom of tower is after main heat exchanger re-heat, into dethanizer rectifying；
（2）Deethanization rectifying
From the gaseous phase materials of dethanizer Base top contact after main heat exchanger cools down, gas-liquid is carried out into deethanization overhead separator
Separation, the gaseous phase materials of deethanization overhead separator separation enter just separation after main heat exchanger condenses, from first knockout tower top
In tower, the liquid phase material of deethanization overhead separator separation returns in dethanizer, the liquid phase object drawn from Deethanizer bottom
Material enters debutanizing tower rectifying；
（3）Debutanization rectifying
After the gaseous phase materials of debutanizing tower Base top contact are condensed, part returns to debutanizing tower, is partly used as liquefied petroleum gas
Output of products；From debutanizing tower bottom draw liquid phase material after cooling, as condensate output of products；
（4）Cryogen refrigeration recycles
It is recycled by cryogen refrigeration and provides cold for main heat exchanger；
In the step 2, dethanizer is connected with deethanization tower bottom reboiler and deethanization tower bottom reboiler carries for dethanizer
For rectifying institute calorific requirement；
In the step 3, debutanizing tower is connected with debutanization tower bottom reboiler and debutanization tower bottom reboiler carries for debutanizing tower
For rectifying institute calorific requirement.
2. the method for natural gas lighter hydrocarbons recovery according to claim 1, which is characterized in that the main heat exchanger is changed using one
Hot device is composed of more heat exchangers.
3. the method for natural gas lighter hydrocarbons recovery according to claim 2, which is characterized in that the main heat exchanger includes evaporator
One, evaporator two；
In the step 1, unstripped gas is after the cooling of evaporator two, into first knockout tower；
In the step 2, the gaseous phase materials of dethanizer Base top contact detach after the cooling of evaporator one into deethanization tower top
Device.
4. according to the method for any one of the claim 1 ~ 3 natural gas lighter hydrocarbons recovery, which is characterized in that the behaviour of the step 4
Make as follows：The vapor phase refrigerant drawn from two level knockout drum tank deck is after the supercharging of level-one refrigeration compressor, into two-stage system
Cold compressor is pressurized to setting pressure, is condensed successively through two level refrigeration compressor refrigerant after supercharged, after level-one throttling,
Gas-liquid separation is carried out into level-one knockout drum；The vapor phase refrigerant of level-one knockout drum tank deck separation returns to two level refrigeration
Compressor boost；It is main heat exchanger high-temperature region that the liquid-phase refrigerant portion of level-one knockout drum tank bottom separation, which enters main heat exchanger,
After cold is provided, level-one knockout drum is returned to, Partial Liquid Phase refrigerant enters two level knockout drum after two-step throttle；Two
The liquid phase refrigerant of grade knockout drum separation enters after main heat exchanger provides cold for main heat exchanger low-temperature space, return two level gas
The vapor phase refrigerant of liquid knockout drum, two level knockout drum tank deck returns to stage compressor supercharging.
5. the method for natural gas lighter hydrocarbons recovery according to claim 4, which is characterized in that in the step 4, refrigerant is second
It is one or more in alkene, ethane, propylene, propane, butylene, butane, ammonia, freon.
6. the device for any one of preceding claims 1 ~ 5 natural gas methods of light hydrocarbon recovery, which is characterized in that including de-
The first piece-rate system, main heat exchanger, the cryogen refrigeration circulatory system that cold is provided for main heat exchanger, deethanization distillation system, de- of hydrocarbon
Butane rectification system；
Just piece-rate system includes unstripped gas feeding mechanism, first knockout tower, is collected for collecting the dry gas of dry gas product the de- hydrocarbon
Device, the unstripped gas feeding mechanism are connected with main heat exchanger, first knockout tower lower part feed inlet successively by pipeline, described just to divide
It is connected successively with main heat exchanger, dry gas collection device by pipeline from column overhead discharge port；
The deethanization distillation system includes dethanizer, deethanization overhead separator, the dethanizer being connected with dethanizer
Bottom reboiler, the just knockout tower bottom of tower discharge port are connected with feed inlet in the middle part of main heat exchanger, dethanizer successively by pipeline,
The deethanizer overhead discharge port by pipeline successively with main heat exchanger, deethanization overhead separator, dethanizer top into
Material mouth be connected, the deethanization overhead separator top discharge mouth by pipeline successively with main heat exchanger, first knockout tower top into
Material mouth is connected, and dethanizer bottom of tower discharge port is connected by pipeline with debutanizing tower；
The debutanization distillation system includes debutanizing tower, debutanization overhead condenser, debutanization tower bottom reboiler, debutanizing tower
Bottom cooler, liquefied petroleum gas output device, condensate output device, the debutanizing tower, debutanization overhead condenser, liquefaction
Oil gas output device is sequentially connected by pipeline, the debutanizing tower, debutanization tower bottom reboiler, the cooling of debutanizing tower bottom
Device, condensate output device are sequentially connected by pipeline.
7. device according to claim 6, which is characterized in that the cryogen refrigeration circulatory system includes two level gas-liquid separation
Tank, level-one refrigeration compressor, two level refrigeration compressor, cryogen condenser, level-one throttle valve, level-one knockout drum, two level section
Flow valve；
The two level knockout drum, level-one refrigeration compressor, two level refrigeration compressor, cryogen condenser, level-one throttle valve, one
Grade knockout drum, two-step throttle valve, two level knockout drum are sequentially connected by pipeline, the level-one gas-liquid separation upper end
Discharge port is connected by pipeline with two level refrigeration compressor entrance, level-one knockout drum bottom end discharge port by pipeline according to
It is secondary to be connected with main heat exchanger, level-one knockout drum feed inlet, two level knockout drum bottom end discharge port by pipeline according to
It is secondary to be connected with main heat exchanger, two level knockout drum feed inlet.
8. device according to claim 7, which is characterized in that the refrigeration between the level-one knockout drum and main heat exchanger
Agent flowing is realized by thermal siphon.
9. device according to claim 7, which is characterized in that the refrigeration between the two level knockout drum and main heat exchanger
Agent flowing is realized by thermal siphon.
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| CN107760355A (en) * | 2017-12-01 | 2018-03-06 | 四川中油乐仪能源装备制造股份有限公司 | A kind of stable light hydrocarbon recovery system and its recovery method |
| CN108165333A (en) * | 2017-12-27 | 2018-06-15 | 四川杰瑞恒日天然气工程有限公司 | A kind of azeotrope refrigeration liquefying natural gas co-production lighter hydrocarbons technique |
| CN111849573A (en) * | 2019-04-26 | 2020-10-30 | 中国石油化工股份有限公司 | Light hydrocarbon recovery system |
| CN110759821A (en) * | 2019-11-23 | 2020-02-07 | 张家港市华昌新材料科技有限公司 | Neopentyl glycol production raw material recovery system and recovery method thereof |
| CN112980490B (en) * | 2019-12-16 | 2023-08-29 | 天津深蓝化工技术有限公司 | Light hydrocarbon recovery system for dry gas low-pressure expansion oilfield associated gas and use method |
| CN113897213A (en) * | 2021-11-15 | 2022-01-07 | 福建福海创石油化工有限公司 | Grading separation device and process method for independently processing condensate oil |
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