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CN101952003A - Separation method - Google Patents

Separation method Download PDF

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Publication number
CN101952003A
CN101952003A CN2008800071052A CN200880007105A CN101952003A CN 101952003 A CN101952003 A CN 101952003A CN 2008800071052 A CN2008800071052 A CN 2008800071052A CN 200880007105 A CN200880007105 A CN 200880007105A CN 101952003 A CN101952003 A CN 101952003A
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China
Prior art keywords
fraction
rich
methane
separation
rectification
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Pending
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CN2008800071052A
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Chinese (zh)
Inventor
H·施密特
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Linde GmbH
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Linde GmbH
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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
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G7/00—Distillation of hydrocarbon oils
    • 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
    • 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
    • F25J3/0238—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 2 carbon atoms or more
    • 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
    • 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
    • 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
    • F25J2200/40—Features relating to the provision of boil-up in the bottom of a column
    • 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
    • F25J2200/70—Refluxing the column with a condensed part of the feed stream, i.e. fractionator top is stripped or self-rectified
    • 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
    • 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
    • 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
    • F25J2205/00—Processes or apparatus using other separation and/or other processing means
    • F25J2205/30—Processes or apparatus using other separation and/or other processing means using a washing, e.g. "scrubbing" or bubble column for purification purposes
    • 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
    • F25J2215/00—Processes characterised by the type or other details of the product stream
    • F25J2215/02—Mixing or blending of fluids to yield a certain product
    • 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
    • F25J2215/00—Processes characterised by the type or other details of the product stream
    • F25J2215/62—Ethane or ethylene
    • 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
    • F25J2220/00—Processes or apparatus involving steps for the removal of impurities
    • F25J2220/60—Separating impurities from natural gas, e.g. mercury, cyclic hydrocarbons
    • F25J2220/66—Separating acid gases, e.g. CO2, SO2, H2S or RSH
    • 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
    • F25J2235/00—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams
    • F25J2235/60—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams the fluid being (a mixture of) hydrocarbons
    • 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
    • F25J2240/00—Processes or apparatus involving steps for expanding of process streams
    • F25J2240/02—Expansion of a process fluid in a work-extracting turbine (i.e. isentropic expansion), e.g. of the feed stream
    • 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
    • F25J2240/00—Processes or apparatus involving steps for expanding of process streams
    • F25J2240/02—Expansion of a process fluid in a work-extracting turbine (i.e. isentropic expansion), e.g. of the feed stream
    • F25J2240/04—Multiple expansion turbines in parallel
    • 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
    • F25J2245/00—Processes or apparatus involving steps for recycling of process streams
    • F25J2245/02—Recycle of a stream in general, e.g. a by-pass stream
    • 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
    • F25J2260/00—Coupling of processes or apparatus to other units; Integrated schemes
    • F25J2260/02—Integration in an installation for exchanging heat, e.g. for waste heat recovery
    • 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
    • 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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  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
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Abstract

本发明描述了从富含烃类的馏份分离出富含C2、C2/CO2、C2+或C3+的馏份的方法，其中对富含烃类的馏份实施一级或多级降压，精馏分离甲烷，并对在甲烷分离中获得的甲烷贫化的馏份实施精馏分离C2、C2/CO2、C2+或C3+。根据本发明，精馏分离甲烷塔(M)的塔底加热装置(E2)经由C3冷却循环(V4，E4，E5，20～27)与精馏分离C2、C2/CO2、C2+或C3+塔(E)的塔顶冷却装置(E3)相连接。

Figure 200880007105

The present invention describes a process for separating a C 2 , C 2 /CO 2 , C 2+ or C 3+ rich fraction from a hydrocarbon rich fraction, wherein the hydrocarbon rich fraction is subjected to a primary Or multi-stage pressure reduction, rectification and separation of methane, and rectification and separation of C 2 , C 2 /CO 2 , C 2+ or C 3+ on the methane-depleted fraction obtained in methane separation. According to the present invention, the bottom heating device (E2) of the rectification separation methane tower (M) is separated from the rectification separation C 2 , C 2 /CO 2 , C The top cooling unit (E3) of the 2+ or C 3+ column (E) is connected.

Figure 200880007105

Description

Separation method
Technical field
The present invention relates to isolate and be rich in C from the fraction that is rich in hydro carbons 2, C 2/ CO 2, C 2+Or C 3+The method of fraction, wherein the fraction that is rich in hydro carbons is implemented one or more levels step-down, rectifying separation of methane, and the fraction of the methane dilution that obtains implemented the rectifying separation of C in methane separation 2, C 2/ CO 2, C 2+Or C 3+
Background technology
Be rich in C isolating from the fraction that is rich in hydro carbons 2, C 2/ CO 2, C 2+Or C 3+The method of fraction in the basic demand that exists be to effectively utilize already present cold supply as far as possible.This takes place under the high situation of raw gas pressure, usually greater than 60 crust, wherein the fraction that is rich in hydro carbons is implemented one or more levels step-down at this pressure.If this uses a plurality of expansion turbines, then can be with their parallel connections and/or arranged in series.
If it is the pressure of the fraction that is rich in hydro carbons to be separated is lower than 40 crust, then not enough usually by the available cold supply of the fraction that is rich in hydro carbons to be separated.This causes cold must additionally be provided.This is for example by means of C 2/3Cool cycles and carrying out, it not only is used for the pre-cooled of the fraction that is rich in hydro carbons to be separated, and is used for the condenser of dethanizer.
For medium raw gas pressure, usually between 70 to 90 crust, there is not on the technology effectively solution at present at this pressure.In this pressure limit, adopt multistage cool cycles at present usually.But this need be than higher cost of investment and operating cost, and make these class methods can't be complicated not obviously.The temperature fluctuation that should be noted that the fraction that is rich in hydro carbons to be separated in addition causes the column bottom temperature of domethanizing column to fluctuate equally, and meanwhile can't provide C according to specification 2Or C 3Product.
Summary of the invention
The object of the present invention is to provide and avoided being used for isolating and being rich in C of above-mentioned shortcoming from the fraction that is rich in hydro carbons 2, C 2/ CO 2, C 2+Or C 3+The method of fraction.
In order to realize this purpose, suggestion is isolated from the fraction that is rich in hydro carbons and is rich in C 2+Or be rich in C 3+The method of fraction, it is characterized in that heater is via C at the bottom of the tower of rectifying separation of methane tower 3Cool cycles and rectifying separation of C 2, C 2/ CO 2, C 2+Or C 3+The cat head cooling device of tower is connected.
According to the present invention, only adopt the C that preferably constitutes now with one-level 3Cool cycles.It is heater and a rectifying separation of C at the bottom of the tower of rectifying separation of methane tower 2, C 2/ CO 2, C 2+Or C 3+" connection " between the cat head cooling device of tower.Therefore, obtain simple on technology, while effective method flow process, its not only with low cost but also energy savings.In addition, the heat of deriving is delivered to this process, and therefore make the demethanation process realize greater flexibility aspect the possible fluctuation of the raw gas temperature of the fraction that is rich in hydro carbons to be separated.
In addition, isolate from the fraction that is rich in hydro carbons according to the present invention and be rich in C 2, C 2/ CO 2, C 2+Or C 3+The method of fraction can be rich in C in discharge 2+/ CO 2The demethanizer of liquid fraction at the bottom of in and at discharge C to be obtained 2, C 2/ CO 2, C 2+Or C 3+On technology, control and regulate product specification in the deethanizer overhead of product fraction simply.
Because in known systems, usually by heating at the bottom of the tower of raw gas enforcement domethanizing column, and implement the cat head cooling of dethanizer by cool cycles, the method according to this invention has then realized separating of heating and raw gas cooling at the bottom of the tower of domethanizing column in contrast to this, and institute is so that the heating control simplification required with the cat head cooling at the bottom of the tower.This also is suitable for the control on technology when startup and operation at part load.
Isolate from the fraction that is rich in hydro carbons according to the present invention and to be rich in C 2+Another advantageous embodiment of method of fraction be characterised in that
-constitute C with one-level 3Cool cycles,
-in the heat exchanger that separates, be implemented in C 3Heat exchange at the bottom of the cooling agent of cool cycles and the tower between the medium of the medium of heater and cat head cooling device,
-will be in the rectifying separation of C 2, C 2/ CO 2, C 2+Or C 3+The part stream of the liquid fraction that obtains in the tower is delivered to rectifying separation of methane tower as backflow.
Below according to the acquisition C shown in the accompanying drawings 2+The method embodiment of product fraction sets forth in more detail according to the present invention to isolate from the fraction that is rich in hydro carbons and is rich in C 2+Or be rich in C 3+The method and the other embodiments thereof of fraction.
Description of drawings
Figure 1 shows that according to embodiment of the present invention.
The specific embodiment
The fraction that is rich in hydro carbons is sent into the first expansion turbine X1 via pipeline 1.This be rich in hydro carbons fraction pressure preferably 70 to 120 the crust between.When needing, the fraction that is rich in hydro carbons is implemented unshowned preliminary treatment in the accompanying drawing, wherein remove non-desired components, as water and glycol.
The fraction that is rich in hydro carbons that reduces pressure in the first expansion turbine X1 is sent into heat exchanger E1 via pipeline 2, relatively cools off with self therein.After heat exchanger E1 discharges, the fraction that is rich in hydro carbons is divided into two bursts of parts flows 3 and 4.First stream 3 is further delivered to the cat head of domethanizing column M after cooling and the total condensation in heat exchanger E1.
Second portion stream 4 reduces pressure in the second expansion turbine X2, sends into the top region of domethanizing column M subsequently equally via pipeline 5.At this, the input point of second portion stream is preferably placed at the input point below of first's stream.
The expansion turbine X1 and the X2 that also can replace two series connection to be provided with install the expansion turbine more than two, and they can mode in parallel and/or series connection be arranged.
Domethanizing column M preferably moves in the pressure limit between 20 to 35 crust.Discharge the gas fraction that is rich in methane from the top region of domethanizing column M via pipeline 6, fraction that is rich in hydro carbons or part fraction to be cooled in heat exchanger E1 and in pipeline 2 and 3 relatively heat, and are compressed to desirable output pressure subsequently.
In addition, accompanying drawing is depicted as three grades of compression units that are made of compression stage V1, V2 and V3.At this, compressor reducer or compression stage V1 are connected with X2 with expansion turbine X1 with V2, and be shown in dotted line.After being compressed to preferred desired output pressure in the scopes of 50 to 120 crust, the gas fraction that is rich in methane is delivered to its other purposes via pipeline 7.
Heating realizes as follows at the bottom of the tower of domethanizing column M: discharge via pipeline 9 from the territory, tower base area of domethanizing column M and be rich in C 2+Fraction, the cooling agent with the cool cycles that needs to be explained in heat exchanger E2 relatively heats, and sends into domethanizing column M again via pipeline 10 subsequently.
Discharge the fraction of methane dilutions at the bottom of the tower of domethanizing column M via pipeline 8, deliver to dethanizer E.It preferably moves in the pressure limit between 20 to 35 crust.
Discharge the liquid fraction that is rich in propane via pipeline 16 at the bottom of the tower of dethanizer E, be pumped to desired output pressure, and sneak into the gas fraction that is rich in methane that in pipeline 7, is under the high pressure more by pump P.
Cat head at dethanizer E is discharged gaseous state C via pipeline 11 2The product fraction.Cooling agent with the cool cycles that needs to be explained in heat exchanger E3 relatively cools off, and partial condensation, sends into separator D via pipeline 12 subsequently.The liquid fraction that produces in this separator D is sent into pump P2 via pipeline 15, is pumped to the pressure among the dethanizer E in this pump P2 at least, sends into the top region of dethanizer E subsequently via pipeline 15.
Cat head at separator D is discharged gaseous state C via pipeline 13 2The product fraction, and deliver to its other purposes.If C 2The product fraction contains carbon dioxide and expects it from C 2The product fraction is isolated, and unshowned carbon dioxide removal process in the accompanying drawing then is set in dethanizer E downstream.
According to the present invention, the cat head cooling device of heater and above-mentioned dethanizer is via C at the bottom of the tower of above-mentioned domethanizing column 3Cool cycles is connected.This C 3Cool cycles is by duct section 20 to 27, separator D ', storage or tank D ", compressor V4 and two later stage cooler E4 and E5 form.
The cooling agent that is compressed to the desired circulating pressure that is preferably 8 to 16 crust in compressor V4 is sent into the first later stage cooler E4 via pipeline 20, for example relatively cools off with cooling water in this first later stage cooler E4.Be divided into two strands of cooling agents subsequently and partly flow 21 and 22, wherein first's stream is sent into the second cooler E5, relatively carries out condensation in this second cooler E5 with such as the suitable cooling medium of cooling water.
The second above-mentioned cooling agent is partly flowed through and is sent into heat exchanger E2 by pipeline 22, in this heat exchanger E2 with pipeline 9 in liquid to be heated stream relatively carry out condensation, this liquid stream is used to heat at the bottom of the tower of domethanizing column M.
Subsequently this cooling agent is partly flowed through and sneak into first cooling agent of discharging via pipeline 24 by pipeline 23 and partly flow, and guiding is by tank D " from the second later stage cooler E5.This storage or tank D " are used for storing cooling agent under equipment or process halted state.This cooling agent is sent into heat exchanger E3 via pipeline 25 subsequently, and in this heat exchanger E3 and in pipeline 11 C that is rich in to be cooled 2The gas fraction relatively evaporate.
To send into the separator D ' that is arranged on compressor V4 upstream through the cooling agent of heating via pipeline 26 subsequently.From its cat head gaseous coolant is sent into compressor V4 via pipeline 27.
C arranged according to the present invention 3Cool cycles structural configuration as shown in drawings can irrespectively be moved cool cycles with the load separately of the separation process that is realized in domethanizing column M and dethanizer E.
In order to improve the C among the domethanizing column M 2Productive rate, according to an embodiment preferred of the inventive method, at least a portion of discharging the liquid fraction 16 that obtains via pipeline 17 in dethanizer E flows, and is cold excessively in heat exchanger E1, sends into domethanizing column M via pipeline 18 as backflow subsequently.Preferably above the input position of the part of the fraction that is rich in hydro carbons to be separated stream 3, send into this part stream 17/18 at this.
It is emphasized that the method according to this invention not only can be used for isolating from the fraction that is rich in hydro carbons is rich in C 2+Fraction, be rich in C but also can be used for isolating from the fraction that is rich in hydro carbons 2, C 2/ CO 2Or C 3+Fraction.

Claims (4)

1.从富含烃类的馏份分离出富含C2、C2/CO2、C2+或C3+的馏份的方法，其中对富含烃类的馏份实施一级或多级降压，精馏分离甲烷，并对在甲烷分离中获得的甲烷贫化的馏份实施精馏分离C2、C2/CO2、C2+或C3+，其特征在于，精馏分离甲烷塔(M)的塔底加热装置(E2)经由C3冷却循环(V4，E4，E5，20～27)与精馏分离C2、C2/CO2、C2+或C3+塔(E)的塔顶冷却装置(E3)相连接。1. Process for separating a C 2 , C 2 /CO 2 , C 2+ or C 3+ rich fraction from a hydrocarbon rich fraction, wherein the hydrocarbon rich fraction is subjected to one or more Step-down, rectification and separation of methane, and rectification and separation of C 2 , C 2 /CO 2 , C 2+ or C 3+ on the methane-depleted fraction obtained in methane separation, characterized in that rectification The bottom heating device (E2) of the separation methane tower (M) separates C 2 , C 2 /CO 2 , C 2+ or C 3+ via C 3 cooling cycle (V4, E4, E5, 20~27) and rectification The overhead cooling (E3) of column (E) is connected. 2.根据权利要求1的方法，其特征在于，所述C3冷却循环(V4，20～27)以一级构成。2. The method according to claim 1, characterized in that the C3 cooling cycle (V4, 20-27) is constituted in one stage. 3.根据权利要求1或2的方法，其特征在于，在分离的热交换器(E2，E3)中实施在C3冷却循环的冷却剂与塔底加热介质和塔顶冷却介质之间的热交换。3. The method according to claim 1 or 2, characterized in that the heat exchange between the coolant of the C3 cooling cycle and the bottom heating medium and the top cooling medium is carried out in separate heat exchangers (E2, E3). exchange. 4.根据权利要求1至3之一的方法，其特征在于，将在精馏分离C2、C2/CO2、C2+或C3+塔(E)中获得的液体馏份(16)的部分流(17，18)作为回流送至精馏分离甲烷塔(M)。 4. The method according to one of claims 1 to 3, characterized in that the liquid fraction (16 ) part stream (17,18) is sent to rectifying separation methane column (M) as reflux.
CN2008800071052A 2007-03-06 2008-02-21 Separation method Pending CN101952003A (en)

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AU2008224221A1 (en) 2008-09-12
NO20093103L (en) 2009-10-05

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