AU2008224221A1 - Separation method - Google Patents

Separation method Download PDF

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Publication number
AU2008224221A1
AU2008224221A1 AU2008224221A AU2008224221A AU2008224221A1 AU 2008224221 A1 AU2008224221 A1 AU 2008224221A1 AU 2008224221 A AU2008224221 A AU 2008224221A AU 2008224221 A AU2008224221 A AU 2008224221A AU 2008224221 A1 AU2008224221 A1 AU 2008224221A1
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Australia
Prior art keywords
fraction
hydrocarbon
separation
rich fraction
rectification
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AU2008224221A
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Hans Schmidt
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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
    • F25J2200/02—Processes or apparatus using separation by rectification in a single 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
    • F25J2200/04—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
    • F25J2200/70—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

Description

P07040-DE/AVA = EM-AVA2805 06.03.2007 - Christoph Zahn/bg Description Separation process 5 The invention relates to 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 expanded in a single-stage or multistage process, subjected to methane separation by 10 rectification and the methane-depleted fraction obtained in the methane separation is subjected to separation of C 2 , C 2 /C0 2 , C 2 1 or C 3 , by rectification. In processes of the type in question for separating a 15 C 2 -, C 2
/CO
2 -, C 2 4- or C 3 4-rich fraction from a hydrocarbon-rich fraction, the fundamental requirement is to use the available cold supply as efficiently as possible. In the case of high crude gas pressures pressures of above 60 bar are meant in this case - this 20 is achieved by expanding the hydrocarbon-rich fraction in a single-stage or multistage process. If, for this purpose, a plurality of expansion turbines are used, they can be arranged in parallel and/or series. 25 If the hydrocarbon-rich fraction to be fractionated has a pressure of less than 40 bar, the supply of cold which can be provided by the hydrocarbon-rich fraction to be fractionated is generally not sufficient. This means that cold must be additionally provided. This is 30 achieved, for example, by means of C 2
/
3 refrigerant cycles which are used both in precooling the hydrocarbon-rich fraction which is to be fractionated and for the condenser of the deethanizer. 35 For medium crude gas pressures - pressures between 70 and 90 bar are meant here - there exist to date no P07040-DE/AVA = EM-AVA2805 06.03.2007 - Christoph Zahn/bg - 2 technically efficient solutions. Customarily, multistage refrigeration cycles are used to date in this pressure range also. However, these require comparatively high capital and operating costs and 5 complicate such processes of the type in question not inconsiderably. In addition, attention must be paid to the fact that fluctuations of temperature of the hydrocarbon-rich fraction which is to be fractionated lead to the bottom temperature of the demethanizer 10 likewise fluctuating and, in association with this, the
C
2 product or C 3 product being able to be released not in accordance with specifications. It is an object of the present invention to specify a 15 process of the type in question for separating a C 2 -,
C
2
/CO
2 -, C 2 +- or C 3 +-rich fraction from a hydrocarbon rich fraction, which process avoids the abovementioned disadvantages. 20 To achieve this object, a process of the type in question for separating a C 2 +-rich or C 3 +-rich fraction from a hydrocarbon-rich fraction is proposed which is characterized in that the bottom heating of the methane separation by rectification is connected via a C 3 25 refrigeration cycle to the overhead cooling of the separation of C 2 , C 2
/CO
2 , C 2 + or C 3 , by rectification. According to the invention, now, use is made of only one C 3 refrigeration cycle which is preferably 30 constructed as a single stage. This is a "connection" between the bottom heating of the methane separation by rectification and the overhead cooling of the separation of C 2 , C 2 /C0 2 , C 2 + or C 3 + by rectification. This produces a technically simple and simultaneously 35 efficient process procedure which is both inexpensive P07040-DE/AVA = EM-AVA2805 06.03.2007 - Christoph Zahn/bg - 3 and energy-efficient. In addition, the heat to be removed is given off to the process and a greater flexibility of the demethanizer process is thereby achieved with respect to possible fluctuations of the 5 crude gas temperature of the hydrocarbon-rich fraction which is to be fractionated. The process according to the invention for separating a
C
2 -, C 2 /C0 2 -, C 2 +- or C 3 +-rich fraction from a 10 hydrocarbon-rich fraction in addition makes possible technically simple control and setting of product specifications, not only in the bottom of the demethanizer - from which a C 2 4/CO 2 -rich liquid fraction is taken off - but also in the head of the deethanizer 15 - from which the C 2 , C 2 /C0 2 , C 2 , or C 3 1 product fraction which is to be obtained is taken off. Since, compared with the known prior art, in which the bottom heating of the demethanizer is generally carried 20 out via the crude gas and the overhead cooling of the deethanizer via a refrigeration cycle, the process according to the invention implements decoupling of demethanizer bottom heating and crude gas cooling, the required control of the bottom heating and also 25 overhead cooling is simplified. The same also applies to the technical control during startup and also partial load operation. Further advantageous embodiments of the process 30 according to the invention for separating a C 2 4-rich fraction from a hydrocarbon-rich fraction which are subject matter of the dependent claims are characterized in that P07040-DE/AVA = EM-AVA2805 06.03.2007 - Christoph Zahn/bg -4 - the C 3 refrigeration cycle is constructed as a single stage, - the heat exchange between the refrigerant of the 5 C 3 refrigeration cycle and the bottom heating medium and also the overhead cooling medium proceeds in separate heat exchangers and - a substream of the liquid fraction obtained in the 10 separation of C 2 , C 2 /C0 2 , C 2 + or C 3 1 by rectification is applied as reflux to the methane separation by rectification. The process according to the invention for separating a 15 C 2 4-rich or C 3 +-rich fraction from a hydrocarbon-rich fraction and also further embodiments of the same will be described in more detail hereinafter on the basis of the process example shown in the figure which shows a
C
2 1 product fraction being obtained. 20 Via line 1, a hydrocarbon-rich fraction is fed to a first expansion turbine X1. This hydrocarbon-rich fraction preferably has a pressure between 70 and 120 bar. The hydrocarbon-rich fraction is - where 25 necessary - subjected to a pretreatment which is not shown in the figure and in which unwanted components such as water and glycol, for example, are removed. The hydrocarbon-rich fraction which is expanded in the 30 first expansion turbine X1 is fed via line 2 to a heat exchanger El and in this cooled against itself. After take-off from the heat exchanger El, the hydrocarbon rich fraction is divided into two substreams 3 and 4. The first-mentioned substream 3, after further cooling P07040-DE/AVA = EM-AVA2805 06.03.2007 - Christoph Zahn/bg -5 and total condensation in the heat exchanger El, is applied to the head of the demethanizer M. The second substream 4 is expanded in the second 5 expansion turbine X2 and subsequently fed via line 5 likewise to the head region of the demethanizer M. The feed point of the second substream in this case is preferably below the feed point of the first substream. Instead of the two series-connected expansion turbines 10 X1 and X2, more than two expansion turbines can also be provided, wherein these can be arranged in parallel and/or in series. The demethanizer M is preferably operated in a pressure 15 range between 20 and 35 bar. From the head region of the demethanizer M, via line 6, a methane-rich gas fraction is taken off, warmed in heat exchanger El against the hydrocarbon-rich fraction or subfraction in lines 2 and 3 which is to be cooled and subsequently 20 compressed to the desired delivery pressure. For this, in the figure a three-stage compressor unit is shown which consists of the compressor stages V1, V2 and V3. The compressors or compressor stages V1 and V2 25 in this case are coupled to the expansion turbines X1 and X2 - shown by the dashed line. After the compression to the desired delivery pressure - this is preferably in the range between 50 and 120 bar - the methane-rich gas fraction is fed via line 7 to its 30 further use. The demethanizer M has bottom heating which is implemented by a C 2 1-rich fraction being taken off from the bottom region of the demethanizer M via line 9, P07040-DE/AVA = EM-AVA2805 06.03.2007 - Christoph Zahn/bg - 6 warmed in the heat exchanger E2 against the refrigerant of the refrigeration cycle which is still to be described, and then subsequently fed via line 10 back to the demethanizer M. 5 From the bottom of the demethanizer M, via line 8 a methane-depleted fraction is taken off and delivered to a deethanizer E. This is preferably operated in a pressure range between 20 and 35 bar. 10 From the bottom of the deethanizer E, via line 16, a propane-rich liquid fraction is taken off, pumped by means of the pump P to the desired delivery pressure and added to the higher-pressure methane-rich gas 15 fraction in the line 7. At the head of the deethanizer E, via line 11 a gaseous
C
2 product fraction is taken off. In the heat exchanger E3, it undergoes cooling and partial condensation 20 against the refrigerant of the refrigeration cycle which is still to be described and is subsequently fed via line 12 to a separator D. The liquid fraction produced in this is fed via line 15 to a pump P2, pumped in this at least to the pressure prevailing in 25 the deethanizer E and subsequently fed via line 15 to the deethanizer E in the head region thereof. At the head of the separator D, via line 13, the gaseous C 2 product fraction is taken off and fed to its 30 further use. If the C 2 product fraction contains carbon dioxide and its separation from the C2 product fraction is desired, a carbon dioxide removal process, which is not shown in the figure, must be connected downstream of the deethanizer E.
P07040-DE/AVA = EM-AVA2805 06.03.2007 - Christoph Zahn/bg -7 According to the invention, the above-described demethanizer bottom heating and also the above described deethanizer overhead cooling are coupled via a C 3 refrigeration cycle. This C 3 refrigeration cycle 5 consists of the line sections 20 to 27, the separator D', the storage or reservoir vessel D", the compressor V4 and also the two aftercoolers E4 and E5. The refrigerant which is compressed in the compressor 10 V4 to the desired circulation pressure - this is preferably between 8 and 16 bar - is fed via line 20 to the first aftercooler E4 and cooled in this, for example against cooling water. Subsequently division into two refrigerant substreams 21 and 22 proceeds, 15 wherein the first-mentioned substream is fed to a second cooler E5 and in this condensed against a suitable cooling medium such as, for example, cooling water. 20 The abovementioned second refrigerant substream is fed via line 22 to the heat exchanger E2 and in this condensed against the fluid stream in line 9 which is to be warmed and which serves for heating the bottom of the demethanizer M. 25 Subsequently thereto, this refrigerant substream is added via line 23 to the first refrigerant substream which is removed from the second aftercooler E5 via line 24 and passed through the reservoir vessel D". 30 This storage or reservoir vessel D" serves for storing the refrigerant during plant or process stoppage. The refrigerant is subsequently fed via line 25 to the heat exchanger E3 and in this vaporized against the C 2 -rich gas fraction in line 11 which is to be cooled.
P07040-DE/AVA = EM-AVA2805 06.03.2007 - Christoph Zahn/bg - 8 Via line 26, the warmed refrigerant is subsequently fed to a separator D' which is connected upstream of the compressor V4. From the head of said separator D', gaseous refrigerant is fed via line 27 to the 5 compressor V4. The structural design shown in the figure of the C 3 refrigeration cycle which is to be provided according to the invention enables the refrigeration cycle also 10 to be operated independently of the respective load of the separation process implemented in the demethanizer M and deethanizer E. For increasing the C 2 yield in the demethanizer M 15 according to an advantageous embodiment of the process according to the invention - via line 17 at least a substream of the liquid fraction 16 obtained in the deethanizer E can be taken off, subcooled in the heat exchanger El and subsequently fed as reflux via line 18 20 to the demethanizer M. This substream 17/18 in this case is preferably fed in above the feed point of the substream 3 of the hydrocarbon-rich fraction which is to be fractionated. 25 It must be stressed that the procedure according to the invention can serve not solely for separating a C 2 4-rich fraction from a hydrocarbon-rich fraction, but also for separating a C 2 -, C 2
/CO
2 - or C 3 ,-rich fraction from a hydrocarbon-rich fraction.

Claims (1)

  1. 06.03.2007 - Christoph Zahn/bg - 9 Claims 1. Process for separating a C 2 -, C 2 /CO 2 -, C 2 +- or C 3 + rich fraction from a hydrocarbon-rich fraction, 5 wherein the hydrocarbon-rich fraction is expanded in a single-stage or multistage process, subjected to methane separation by rectification and the methane-depleted fraction obtained in the methane separation is subjected to separation of C 2 , 10 C 2 /CO 2 , C 2 + or C 3 + by rectification, characterized in that the bottom heating (E2) of the methane separation (M) by rectification is connected via a C 3 refrigeration cycle (V4, E4, E5, 20-27) to the overhead cooling (E3) of the separation of C 2 , 15 C 2 /CO 2 , C 2 + or C 3 + by rectification (E) . 2. Process according to Claim 1, characterized in that the C 3 refrigeration cycle (V4, 20-27) is constructed as a single stage. 20 3. Process according to Claim 1 or 2, characterized in that the heat exchange between the refrigerant of the C 3 refrigeration cycle and the bottom heating medium and also the overhead cooling 25 medium proceeds in separate heat exchangers (E2, E3). 4. Process according to one of the preceding Claims 1 to 3, characterized in that a substream (17, 18) 30 of the liquid fraction (16) obtained in the separation of C 2 , C 2 /CO 2 , C 2 + or C 3 + by rectification is applied as reflux to the methane separation (M) by rectification.
AU2008224221A 2007-03-06 2008-02-21 Separation method Abandoned AU2008224221A1 (en)

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IT1400370B1 (en) * 2010-05-31 2013-05-31 Nuova Pignone S R L METHOD AND DEVICE FOR RECOVERING NATURAL LIQUEFIED NGL GAS
DE102012020469A1 (en) * 2012-10-18 2014-04-24 Linde Aktiengesellschaft Method for separating methane from methane-containing synthesis gas in separation unit, involves feeding capacitor with secondary portion of refrigerant of outlet temperature to intermediate temperature and cooling to lower temperature
DE102015001858A1 (en) * 2015-02-12 2016-08-18 Linde Aktiengesellschaft Combined separation of heavy and light ends from natural gas
DE102015009254A1 (en) * 2015-07-16 2017-01-19 Linde Aktiengesellschaft Process for separating ethane from a hydrocarbon-rich gas fraction
EP3315773A1 (en) * 2016-10-25 2018-05-02 Linde Aktiengesellschaft Pump feed tank, rectification system and method of low temperature rectification
CN110801639B (en) * 2019-11-11 2021-06-01 杭州快凯高效节能新技术有限公司 Method for recovering carbon dioxide by multistage liquefaction and fractional refrigeration of industrial tail gas

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DE1268162B (en) * 1965-07-28 1968-05-16 Linde Ag Method for separating a gas mixture
DE3511636A1 (en) * 1984-12-17 1986-07-10 Linde Ag, 6200 Wiesbaden METHOD FOR OBTAINING C (DOWN ARROW) 2 (DOWN ARROW) (DOWN ARROW) + (DOWN ARROW) - OR FROM C (DOWN ARROW) 3 (DOWN ARROW) (DOWN ARROW) + (DOWN ARROW) CARBON
IT1222733B (en) * 1987-09-25 1990-09-12 Snmprogetti S P A FRACTIONING PROCESS OF HYDROCARBON GASEOUS MIXTURES WITH HIGH CONTENT OF ACID GASES
US4869740A (en) * 1988-05-17 1989-09-26 Elcor Corporation Hydrocarbon gas processing
US5675054A (en) * 1995-07-17 1997-10-07 Manley; David Low cost thermal coupling in ethylene recovery
US5881569A (en) * 1997-05-07 1999-03-16 Elcor Corporation Hydrocarbon gas processing
US6755965B2 (en) * 2000-05-08 2004-06-29 Inelectra S.A. Ethane extraction process for a hydrocarbon gas stream
CN1195717C (en) * 2000-08-18 2005-04-06 成都华西化工科技股份有限公司 Process for separating and recovering ethylene, ethane, propylene and hydrogen from gas mixture containing hydrocarbons
WO2004076946A2 (en) * 2003-02-25 2004-09-10 Ortloff Engineers, Ltd Hydrocarbon gas processing
US7311813B2 (en) * 2003-03-20 2007-12-25 Ineos Usa Llc Distillation sequence for the purification and recovery of hydrocarbons
EP1734027B1 (en) * 2005-06-14 2012-08-15 Toyo Engineering Corporation Process and Apparatus for Separation of Hydrocarbons from Liquefied Natural Gas
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WO2008107079A3 (en) 2014-02-27
RU2009136693A (en) 2011-04-20

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