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BRPI1008539B1 - PROCESS TO LIQUEFINE A FRACTION RICH IN HYDROCARBONS - Google Patents

PROCESS TO LIQUEFINE A FRACTION RICH IN HYDROCARBONS Download PDF

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Publication number
BRPI1008539B1
BRPI1008539B1 BRPI1008539-4A BRPI1008539A BRPI1008539B1 BR PI1008539 B1 BRPI1008539 B1 BR PI1008539B1 BR PI1008539 A BRPI1008539 A BR PI1008539A BR PI1008539 B1 BRPI1008539 B1 BR PI1008539B1
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Brazil
Prior art keywords
fraction
mixed refrigerant
rich
liquefied
hydrocarbons
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BRPI1008539-4A
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Portuguese (pt)
Inventor
Heinz Bauer
Rainer Sapper
Daniel Garthe
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Linde Aktiengesellschaft
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Publication of BRPI1008539A2 publication Critical patent/BRPI1008539A2/en
Publication of BRPI1008539B1 publication Critical patent/BRPI1008539B1/en

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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
    • F25B—REFRIGERATION MACHINES, PLANTS OR SYSTEMS; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS
    • F25B9/00—Compression machines, plants or systems, in which the refrigerant is air or other gas of low boiling point
    • F25B9/002—Compression machines, plants or systems, in which the refrigerant is air or other gas of low boiling point characterised by the refrigerant
    • F25B9/006—Compression machines, plants or systems, in which the refrigerant is air or other gas of low boiling point characterised by the refrigerant the refrigerant containing more than one component
    • 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
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/0002—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the fluid to be liquefied
    • F25J1/0022—Hydrocarbons, e.g. natural 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
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
    • F25J1/0047—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using an "external" refrigerant stream in a closed vapor compression cycle
    • F25J1/0052—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using an "external" refrigerant stream in a closed vapor compression cycle by vaporising a liquid refrigerant stream
    • F25J1/0055—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using an "external" refrigerant stream in a closed vapor compression cycle by vaporising a liquid refrigerant stream originating from an incorporated cascade
    • 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
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
    • F25J1/0211—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using a multi-component refrigerant [MCR] fluid in a closed vapor compression cycle
    • F25J1/0212—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using a multi-component refrigerant [MCR] fluid in a closed vapor compression cycle as a single flow MCR cycle
    • 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
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
    • F25J1/0243—Start-up or control of the process; Details of the apparatus used; Details of the refrigerant compression system used
    • F25J1/0244—Operation; Control and regulation; Instrumentation
    • 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
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
    • F25J1/0243—Start-up or control of the process; Details of the apparatus used; Details of the refrigerant compression system used
    • F25J1/0279—Compression of refrigerant or internal recycle fluid, e.g. kind of compressor, accumulator, suction drum etc.
    • F25J1/0291—Refrigerant compression by combined gas compression and liquid pumping
    • 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
    • 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
    • F25B—REFRIGERATION MACHINES, PLANTS OR SYSTEMS; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS
    • F25B1/00—Compression machines, plants or systems with non-reversible cycle
    • F25B1/10—Compression machines, plants or systems with non-reversible cycle with multi-stage compression
    • 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
    • F25J2200/70—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
    • F25J2210/00—Processes characterised by the type or other details of the feed stream
    • F25J2210/06—Splitting of the feed stream, e.g. for treating or cooling in different ways
    • 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
    • F25J2215/04—Recovery of liquid products
    • 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
    • F25J2270/00—Refrigeration techniques used
    • F25J2270/18—External refrigeration with incorporated cascade 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
    • F25J2270/66—Closed external refrigeration cycle with multi component refrigerant [MCR], e.g. 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
    • F25J2270/00—Refrigeration techniques used
    • F25J2270/90—External refrigeration, e.g. conventional closed-loop mechanical refrigeration unit using Freon or NH3, unspecified external refrigeration
    • F25J2270/902—Details about the refrigeration cycle used, e.g. composition of refrigerant, arrangement of compressors or cascade, make up sources, use of reflux exchangers etc.
    • 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
    • F25J2280/00—Control of the process or apparatus
    • F25J2280/02—Control in general, load changes, different modes ("runs"), measurements

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  • Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Mechanical Engineering (AREA)
  • Thermal Sciences (AREA)
  • General Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Separation By Low-Temperature Treatments (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)

Abstract

processo para liquefazer um fluxo rico em hidrocarbonetos. a presente invenção refere-se a um processo sendo descrito para liquefazer uma fração rica em hidrocarbonetos com a remoção simultânea de uma fração rica em c2+, em que o resfriamento e a liquefação da fração rica em hidrocarbonetos ocorrem em troca de calor indireta contra o refrigerante misturado de um ciclo de refrigerante misturado no qual o refrigerante misturado é comprimido em pelo menos dois estágios, e a fração rica em c2+ é removida a um nível de temperatura ajustável, em que o refrigerante misturado é separado em uma fração gasosa e uma fração líquida, ambas as frações são subresfriadas, expandidas essencialmente para a pressão de sucção do primeiro estágio de compressor e pelo menos em parte vaporizadas. de acordo com a invenção, pelo menos ocasionalmente, pelo menos um subfluxo (19, 24) da fração gasosa previamente liquefeita do refrigerante misturado (15) é expandida (j, h) e adicionada à fração líquida expandida do refrigerante misturado (21).process to liquefy a hydrocarbon-rich flow. the present invention relates to a process being described for liquefying a fraction rich in hydrocarbons with the simultaneous removal of a fraction rich in c2 +, in which cooling and liquefaction of the fraction rich in hydrocarbons occurs in exchange of indirect heat against the refrigerant mixture from a mixed refrigerant cycle in which the mixed refrigerant is compressed in at least two stages, and the fraction rich in c2 + is removed at an adjustable temperature level, where the mixed refrigerant is separated into a gas fraction and a liquid fraction , both fractions are subcooled, expanded essentially to the suction pressure of the first compressor stage and at least partially vaporized. according to the invention, at least occasionally, at least a subflow (19, 24) of the previously liquefied gas fraction of the mixed refrigerant (15) is expanded (j, h) and added to the expanded liquid fraction of the mixed refrigerant (21).

Description

[0001] A presente invenção refere-se a um processo para liquefazer uma fração rica em hidrocarbonetos com a remoção simultânea de uma fração rica em C2+, em que 0 resfriamento e a liquefação da fração rica em hidrocarbonetos ocorrem em troca de calor indireta contra 0 refrigerante misturado de um ciclo de refrigerante misturado 0 qual 0 refrigerante misturado é comprimido em pelo menos dois estágios, e a fração rica em C2+ é removida a um nível de temperatura ajustável, em que 0 refrigerante misturado é separado em uma fração gasosa e uma fração líquida, ambas as frações são subresfriadas, expandidas essencialmente para a pressão de sucção do primeiro estágio de compressor e pelo menos em parte vaporizadas.[0001] The present invention relates to a process for liquefying a fraction rich in hydrocarbons with the simultaneous removal of a fraction rich in C2 +, in which the cooling and liquefaction of the fraction rich in hydrocarbons occurs in exchange of indirect heat against 0 mixed refrigerant from a mixed refrigerant cycle 0 in which the mixed refrigerant is compressed in at least two stages, and the fraction rich in C2 + is removed at an adjustable temperature level, where the mixed refrigerant is separated into a gas fraction and a fraction liquid, both fractions are subcooled, expanded essentially to the suction pressure of the first compressor stage and at least partially vaporized.

[0002] Um processo do tipo em questão para liquefazer uma fração rica em hidrocarbonetos é conhecido, por exemplo, da DE-A 19722490. Tais processos de liquefação são utilizados, por exemplo, em liquefação de gás natural. Em processos de liquefação do tipo em questão é geralmente necessário remover certos componentes, já que estes precipitariam no estágio sólido nas baixas temperaturas requeridas e/ou prejudicariam a qualidade de produto especificado. No caso mais simples, é suficiente prover somente um separador 0 qual serve para remover os componentes indesejados da fração rica em hidro-carbonetos a qual deve ser liquefeita. A remoção seletiva de componentes de gás natural mais leves, tal como 0 etano, por exemplo, em contraste faz demandas consideravelmente mais altas, tanto do procedimento de processo quanto também da controlabilidade sob condições limites mutáveis.[0002] A process of the type in question to liquefy a fraction rich in hydrocarbons is known, for example, from DE-A 19722490. Such liquefaction processes are used, for example, in liquefaction of natural gas. In liquefaction processes of the type in question, it is generally necessary to remove certain components, as these would precipitate into the solid stage at the required low temperatures and / or impair the specified product quality. In the simplest case, it is sufficient to provide only a separator 0 which serves to remove unwanted components from the hydrocarbon-rich fraction which must be liquefied. The selective removal of lighter natural gas components, such as ethane, for example, in contrast makes considerably higher demands, both on the process procedure and also on controllability under changing limit conditions.

[0003] Nos processos de liquefação de gás natural de pequena a média capacidade - estes são considerados incluir as taxas de produção de 30 000 a 1 milhão t/ano de LNG - os ciclos misturados tendo somente um compressor de ciclo - estes são também denominados processos de Refrigerante Misturado Único (SMR) - são frequentemente utilizados. Estes têm a desvantagem que a fase de refrigerante líquida pode somente ser vaporizada em um nível de pressão. O ajuste determinado e o controle de um perfil de temperatura desejado portanto são difíceis, já que o número de possibilidades para intervenção e/ou graus de liberdade em tais processos é restrito. Perfis de temperatura correspondentes são requeridos, por exemplo, de modo a acelerar a condensação parcial da fração rica em hidrocarbonetos a qual deve ser liquefeita exatamente até uma temperatura definida a qual é requerida pela remoção posterior buscada dos componentes indeseja- dos.[0003] In small to medium capacity natural gas liquefaction processes - these are considered to include production rates of 30,000 to 1 million tonnes / year of LNG - mixed cycles having only one cycle compressor - these are also called Single Mixed Refrigerant (SMR) processes - are often used. These have the disadvantage that the liquid refrigerant phase can only be vaporized at a pressure level. The determined adjustment and the control of a desired temperature profile are therefore difficult, since the number of possibilities for intervention and / or degrees of freedom in such processes is restricted. Corresponding temperature profiles are required, for example, in order to accelerate the partial condensation of the hydrocarbon-rich fraction which must be liquefied exactly to a defined temperature which is required by the subsequent sought removal of unwanted components.

[0004] O objetivo da presente invenção é especificar um processo do tipo em questão para liquefazer uma fração rica em hidrocarbonetos com a remoção simultânea de uma fração rica em C2+ 0 qual evita as desvantagens acima descritas. Especificamente, um processo do tipo em questão para liquefazer uma fração rica em hidrocarbonetos deve ser especificado 0 qual seja primeiramente robusto e segundamente torna possível uma remoção eficiente e controlável de etano e hidrocarbonetos mais altos no curso de um processo de liquefação de gás natural. Portanto, a vaporização de um fluxo de refrigerante misturado deve ser disposta de tal modo que esta possa ser utilizada dire-tamente para controlar uma remoção de etano e de hidrocarbonetos mais altos.[0004] The objective of the present invention is to specify a process of the type in question to liquefy a fraction rich in hydrocarbons with the simultaneous removal of a fraction rich in C2 + 0 which avoids the disadvantages described above. Specifically, a process of the type in question to liquefy a hydrocarbon-rich fraction must be specified which is first robust and secondly makes possible an efficient and controllable removal of higher ethane and hydrocarbons in the course of a natural gas liquefaction process. Therefore, the vaporization of a mixed refrigerant stream must be arranged in such a way that it can be used directly to control a removal of higher ethane and hydrocarbons.

[0005] Para atingir este objetivo, um processo do tipo em questão é proposto para liquefazer uma fração rica em hidrocarbonetos com a remoção simultânea de uma fração rica em C2+, 0 qual está caracterizado pelo fato de que pelo menos ocasionalmente, pelo menos um subfluxo da fração gasosa previamente liquefeita do refrigerante misturado seja expandida e adicionada à fração líquida expandida do refrigerante misturado.[0005] To achieve this goal, a process of the type in question is proposed to liquefy a fraction rich in hydrocarbons with the simultaneous removal of a fraction rich in C2 +, 0 which is characterized by the fact that at least occasionally, at least a subflow the previously liquefied gas fraction of the mixed refrigerant is expanded and added to the expanded liquid fraction of the mixed refrigerant.

[0006] Por meio de variação das razões quantitativas da fração líquida e da fração gasosa previamente liquefeita, o perfil de temperatura pode ser influenciado durante a vaporização do refrigerante misturado das duas frações acima mencionadas de tal modo que de acordo com o objetivo a temperatura do refrigerante misturado na região superior do trocador de calor ou trocadores de calor os quais servem para resfriar e para a condensação parcial da fração rica em hidrocarbonetos a ser liquefeita está sempre abaixo da temperatura da fração a ser liquefeita. O procedimento de acordo com a invenção permite uma controlabilidade suficiente da temperatura da fração rica em hidrocarbonetos a ser liquefeita na entrada para o dispositivo de separação ou coluna de separação a ser provido para remover a fração rica em C2+, e assim ajustar uma concentração desejada dos hidrocarbonetos C2+ no produto de liquefação ou Gás Natural Liquefeito (LNG) é possível.[0006] By varying the quantitative ratios of the liquid fraction and the previously liquefied gas fraction, the temperature profile can be influenced during the vaporization of the mixed refrigerant of the two fractions mentioned above in such a way that according to the objective the temperature of the refrigerant mixed in the upper region of the heat exchanger or heat exchangers which serve to cool and for partial condensation of the hydrocarbon-rich fraction to be liquefied is always below the temperature of the fraction to be liquefied. The procedure according to the invention allows sufficient temperature controllability of the hydrocarbon-rich fraction to be liquefied at the entrance to the separation device or separation column to be provided to remove the C2 + rich fraction, and thus adjust a desired concentration of C2 + hydrocarbons in the liquefaction product or Liquefied Natural Gas (LNG) is possible.

[0007] Modalidades vantajosas adicionais do processo de acordo com a invenção para liquefazer uma fração rica em hidrocarbonetos com a remoção simultânea de uma fração rica em C2+ as quais são os assuntos das reivindicações dependentes estão caracterizadas pelo fato de que - o subfluxo da fração gasosa previamente liquefeita do refrigerante misturado é retirado na extremidade fria do trocador de calor entre a fração rica em hidrocarbonetos a ser liquefeita e 0 refrigerante misturado e/ou a uma temperatura intermediária adequada, expandida e adicionada à fração líquida expandida do refrigerante misturado, em que uma temperatura intermediária adequada está então presente quando 0 refrigerante misturado tem um subresfriamento de pelo menos 5°C, de preferência de pelo menos 10°C, comparado com 0 estado de ebulição, - a troca de calor entre a fração rica em hidrocarbonetos a ser liquefeita e o refrigerante misturado ocorre em um trocador de calor de múltiplos fluxos, o qual está de preferência construído como um trocador de calor de placa ou um trocador de calor helicoidalmente enrolado, - se a fração rica em C2+ for removida em pelo menos uma coluna de separação, e pelo menos ocasionalmente, um subfluxo da fração rica em hidrocarbonetos a ser liquefeita é alimentado para a região superior e/ou a região inferior da coluna de separação, - se a fração rica em C2+ for removida em pelo menos uma coluna de separação, a temperatura de fundo de coluna de separação é ajustada por meio de um permutador de reaquecimento designado para a coluna de separação.[0007] Additional advantageous modalities of the process according to the invention for liquefying a fraction rich in hydrocarbons with the simultaneous removal of a fraction rich in C2 + which are the subjects of the dependent claims are characterized by the fact that - the underflow of the gas fraction previously liquefied of the mixed refrigerant is removed at the cold end of the heat exchanger between the hydrocarbon-rich fraction to be liquefied and the mixed refrigerant and / or at a suitable intermediate temperature, expanded and added to the expanded liquid fraction of the mixed refrigerant, in which a suitable intermediate temperature is then present when the mixed refrigerant has a subcooling of at least 5 ° C, preferably at least 10 ° C, compared to the boiling state, - the heat exchange between the hydrocarbon-rich fraction to be liquefied and the mixed refrigerant takes place in a multi-flow heat exchanger, which is preferably constructed as a plate heat exchanger or helically wound heat exchanger, - if the C2 + rich fraction is removed in at least one separation column, and at least occasionally, a subflow of the hydrocarbon rich fraction to be liquefied is fed to the upper and / or lower region of the separation column, - if the fraction rich in C2 + is removed in at least one separation column, the bottom temperature of the separation column is adjusted by means of a reheat exchanger designated for the separation column.

[0008] O processo de acordo com a invenção para liquefazer uma fração rica em hidrocarbonetos com a remoção simultânea de uma fração rica em C2+ e também as suas modalidades vantajosas adicionais as quais são os assuntos das reivindicações dependentes serão descritos em mais detalhes daqui em diante com referência às modalidades ilustrativas mostradas nas figuras 1 e 2.[0008] The process according to the invention for liquefying a fraction rich in hydrocarbons with the simultaneous removal of a fraction rich in C2 + and also its additional advantageous modalities which are the subjects of the dependent claims will be described in more detail hereinafter with reference to the illustrative modalities shown in figures 1 and 2.

[0009] Daqui em diante na explicação da modalidade exemplar mostrada na figura 2, somente as diferenças do procedimento mostrado na figura 1 serão consideradas.[0009] Hereinafter in the explanation of the exemplary modality shown in figure 2, only the differences in the procedure shown in figure 1 will be considered.

[00010] As modalidades exemplares do processo de acordo com a invenção as quais estão mostradas nas figuras 1 e 2 para liquefazer uma fração rica em hidrocarbonetos que tem uma coluna de separação T a qual serve para remover uma fração rica em C2+ da fração rica em hidrocarbonetos a ser liquefeita. A fração a ser liquefeita a qual é subsequentemente denominada um fluxo de gás natural, é alimentada através da linha 1 para um trocador de calor de múltiplos fluxos E3.[00010] The exemplary modalities of the process according to the invention which are shown in figures 1 and 2 to liquefy a hydrocarbon-rich fraction that has a separation column T which serves to remove a fraction rich in C2 + from the fraction rich in hydrocarbons to be liquefied. The fraction to be liquefied, which is subsequently called a natural gas flow, is fed through line 1 to a multi-flow heat exchanger E3.

[00011] Este trocador de calor está de preferência construído como um trocador de calor de placa de alumínio soldada. Dependendo do tamanho do sistema, de preferência 1 a 6 unidades de trocador de calor paralelas são providas. Alternativamente, o trocador de calor de múltiplos fluxos E3 pode ser construído como um trocador de calor helicoidalmente enrolado. Neste caso, os trocadores de calor de placa de alumínio são de preferência utilizados para uma capacidade de liquefação de 30 000 a 50 000 t/ano de LNG e os trocadores de calor helicoidalmente enrolado são de preferência utilizados para uma capacidade de liquefação de 100 000 a 1 000 000 t/ano de LNG.[00011] This heat exchanger is preferably constructed as a welded aluminum plate heat exchanger. Depending on the size of the system, preferably 1 to 6 parallel heat exchanger units are provided. Alternatively, the E3 multi-flow heat exchanger can be constructed as a helically wound heat exchanger. In this case, aluminum plate heat exchangers are preferably used for a liquefaction capacity of 30,000 to 50,000 t / year of LNG and helically coiled heat exchangers are preferably used for a liquefaction capacity of 100,000 to 1 000 000 t / year of LNG.

[00012] O fluxo de gás natural é resfriado dentro do trocador de calor E3 parcialmente condensado e sequencialmente expandido através de uma válvula a para dentro da região superior da coluna de separação T. No topo da coluna de separação T uma fração de gás rica em metano é retirada através da linha 2, liquefeita e também subresfriada no trocador de calor E3 e subsequentemente, através da linha 3, na qual uma válvula de controle e está provida, retirada e suprida para sua utilização adicional ou armazenamento intermediário. Esta fração é o produto de liquefação (LNG). Uma fração rica em C2+ é retirada do fundo da coluna de separação T através da linha 4, a qual do mesmo modo tem uma válvula de controle d, e suprida para sua utilização adicional.[00012] The flow of natural gas is cooled inside the E3 heat exchanger partially condensed and sequentially expanded through a valve into the upper region of the separation column T. At the top of the separation column T a fraction of gas rich in methane is removed via line 2, liquefied and also subcooled on the E3 heat exchanger and subsequently via line 3, in which a control valve is provided, removed and supplied for further use or intermediate storage. This fraction is the product of liquefaction (LNG). A fraction rich in C2 + is removed from the bottom of the separation column T via line 4, which likewise has a control valve d, and supplied for further use.

[00013] Por meio de uma alimentação de um subfluxo do fluxo de gás natural através da linha 5 e da válvula de controle b, a temperatura de topo da coluna de separação T e portanto a composição da fração de gás rica em metano retirada através da linha 2 são influenciadas. A temperatura de fundo da coluna de separação T também, e também a composição da fração líquida retirada através da linha 4 podem ser influenciadas pelo permutador de reaquecimento E4 e/ou a adição de um subfluxo do fluxo de gás natural através da linha 6 e da válvula de expansão c.[00013] By supplying a subflow of the natural gas flow through line 5 and the control valve b, the top temperature of the separation column T and therefore the composition of the methane-rich gas fraction removed through the line 2 are influenced. The bottom temperature of the separation column T as well, and also the composition of the liquid fraction removed through line 4 can be influenced by the reheating exchanger E4 and / or the addition of a subflow of the natural gas flow through line 6 and the expansion valve c.

[00014] O ciclo de refrigerante misturado consiste em uma unidade de compressor de dois estágios que consiste em um primeiro estágio de compressor e um segundo estágio de compressor C1 e C2, respectivamente. A Jusante de ambos os estágios de compressor está conectado em cada caso um resfriador, E1 e E2, respectivamente. Além disso, um separador de baixa pressão D1, um separador de média pressão D2, e também um separador de alta pressão D3 estão providos.[00014] The mixed refrigerant cycle consists of a two-stage compressor unit that consists of a first compressor stage and a second compressor stage C1 and C2, respectively. Downstream of both compressor stages, a chiller, E1 and E2, is connected in each case, respectively. In addition, a low pressure separator D1, a medium pressure separator D2, and also a high pressure separator D3 are provided.

[00015] Do topo do separador de baixa pressão D1 o qual serve para a segurança do primeiro estágio de compressor C1, o refrigerante misturado que circula no ciclo de refrigeração é alimentado através da linha 11 para o primeiro estágio de compressor C1. Neste, o refrigerante misturado é comprimido para uma pressão intermediária desejada - esta é costumeiramente entre 0,7 MPa e 3,5 MPa (7 e 35 bar), de preferência entre 1 MPa e 2,5 MPa (10 e 25 bar) - subsequentemente resfriado no resfriador E1, parcialmente condensado e alimentado através da linha 12 para o separador de média pressão D2. Enquanto a fração líquida é retirada do mesmo através da linha 20, cuja fração líquida será considerada em mais detalhes daqui em diante, a fase de gás do refrigerante misturado a qual é retirada através da linha 13 do topo do separador D2 é alimentada para o segundo estágio de compressor C2 e neste comprimida para a pressão final desejada - esta é costumeiramente entre 3 MPa e 8 MPa (30 e 80 bar), de preferência entre 4 MPa e 6 MPa (40 e 60 bar). Subsequentemente, o refrigerante misturado é resfriado no resfriador E2, parcialmente condensado e alimentado através da linha 14 para o separador de alta pressão D3. A fração líquida que ocorre no fundo do separador D3 é recirculada através da linha 16, na qual uma válvula de expansão k está provida, a montante do separador de média pressão D2.[00015] From the top of the low pressure separator D1 which serves for the safety of the first compressor stage C1, the mixed refrigerant circulating in the refrigeration cycle is fed through line 11 to the first compressor stage C1. In this, the mixed refrigerant is compressed to a desired intermediate pressure - this is usually between 0.7 MPa and 3.5 MPa (7 and 35 bar), preferably between 1 MPa and 2.5 MPa (10 and 25 bar) - subsequently cooled in the cooler E1, partially condensed and fed through line 12 to the medium pressure separator D2. While the liquid fraction is removed from it via line 20, the liquid fraction of which will be considered in more detail hereinafter, the gas phase of the mixed refrigerant which is removed via line 13 from the top of separator D2 is fed to the second compressor stage C2 and compressed to the desired final pressure - this is usually between 3 MPa and 8 MPa (30 and 80 bar), preferably between 4 MPa and 6 MPa (40 and 60 bar). Subsequently, the mixed refrigerant is cooled in the cooler E2, partially condensed and fed through line 14 to the high pressure separator D3. The liquid fraction that occurs at the bottom of the separator D3 is recirculated through line 16, in which an expansion valve k is provided, upstream of the medium pressure separator D2.

[00016] No topo do separador D3 a fração de refrigerante gasosa é retirada através da linha 15, liquefeita e também subresfriada no trocador de calor E3 e retirada do mesmo através da linha 17. Esta fração ou um subfluxo desta fração é expandida na válvula de expansão g para a pressão de ciclo mais baixa antes desta ser alimentada através da linha 18 através do trocador de calor E3 e sendo completamente vaporizada. Através da linha 10, a fração completamente vaporizada é subsequentemente alimentada para o separador D1.[00016] At the top of the D3 separator the fraction of gaseous refrigerant is removed via line 15, liquefied and also subcooled in the heat exchanger E3 and removed from it via line 17. This fraction or a subflow of this fraction is expanded in the expansion g to the lowest cycle pressure before it is fed through line 18 through heat exchanger E3 and completely vaporized. Via line 10, the fully vaporized fraction is subsequently fed to the separator D1.

[00017] No procedimento mostrado na figura 1, a fração de refrigerante líquida é retirada através da linha 20 do fundo do separador D2, alimentada para o trocador de calor E3 e subresfriada no mesmo. Através da linha 21, a fração líquida subresfriada é retirada do trocador de calor E3, expandida na válvula F para a pressão de ciclo mais baixa e subsequentemente alimentada através da linha 22 de volta para o trocador de calor E3. A fração vaporizada no mesmo é adicionada através da linha 23 à fração vaporizada acima mencionada na linha 10.[00017] In the procedure shown in figure 1, the liquid refrigerant fraction is removed through line 20 at the bottom of separator D2, fed to the heat exchanger E3 and subcooled in it. Through line 21, the subcooled liquid fraction is removed from the heat exchanger E3, expanded on valve F to the lowest cycle pressure and subsequently fed through line 22 back to the heat exchanger E3. The vaporized fraction in it is added via line 23 to the vaporized fraction mentioned above in line 10.

[00018] Nas válvulas f e g, costumeiramente uma expansão prossegue para uma pressão a qual corresponde, à parte de quedas de pressão inevitáveis, para a pressão de sucção do primeiro estágio de compressor C1. Por meio de uma escolha adequada da composição, a quantidade e/ou a pressão de vaporização do refrigerante misturado, não somente a temperatura final mas também a taxa de fluxo da fração rica em hidrocarbonetos a ser liquefeita ou do fluxo de gás natural a ser liquefeito podem ser ajustadas.[00018] In valves f and g, an expansion usually proceeds to a pressure which corresponds, in the part of inevitable pressure drops, to the suction pressure of the first compressor stage C1. Through an appropriate choice of composition, the amount and / or vaporization pressure of the mixed refrigerant, not only the final temperature but also the flow rate of the hydrocarbon-rich fraction to be liquefied or the flow of natural gas to be liquefied can be adjusted.

[00019] Em contraste com o procedimento mostrado na figura 1, na modalidade exemplar mostrada na figura 2, a fração líquida do refrigerante misturado a ser alimentada para o trocador de calor E3 ainda não foi retirada do separador D2, mas do separador D3 através da linha 20'. A fração líquida que ocorre no fundo do separador D2 é portanto alimentada através da linha 16', na qual uma bomba P está disposta, para o separador D3.[00019] In contrast to the procedure shown in figure 1, in the exemplary mode shown in figure 2, the liquid fraction of the mixed refrigerant to be fed to the heat exchanger E3 has not yet been removed from separator D2, but from separator D3 through line 20 '. The liquid fraction that occurs at the bottom of the separator D2 is therefore fed through line 16 ', on which a pump P is arranged, to the separator D3.

[00020] O procedimento de processo mostrado na figura 2 é um pouco mais eficiente comparado com o procedimento de processo mostrado na figura 1 - este torna possível um aperfeiçoamento em eficiência de 1 a 5% - mas requer uma bomba a qual dá origem a custos de capital aumentados e um maior gasto em manutenção. O procedimento de processo de acordo com a figura 1 é portanto de preferência utilizado em capacidades de sistema relativamente pequenas (30 000 a 500 000 t/ano de LNG) enquanto que o procedimento de processo mostrado na figura 2 é de preferência implementado em capacidades de sistema relativamente grandes (100 000 a 1 000 000 t/ano de LNG).[00020] The process procedure shown in figure 2 is slightly more efficient compared to the process procedure shown in figure 1 - this makes possible an improvement in efficiency of 1 to 5% - but requires a pump which gives rise to costs capital and increased maintenance expenses. The process procedure according to figure 1 is therefore preferably used in relatively small system capacities (30,000 to 500,000 t / year of LNG) while the process procedure shown in figure 2 is preferably implemented in capacities of relatively large systems (100,000 to 1,000,000 t / year of LNG).

[00021] Devido à expansão acima descrita da fração gasosa sub- resfriada líquida e também previamente liquefeita do refrigerante misturado nas válvulas f e g para uma pressão de vaporização essencialmente idêntica, o curso de temperatura do fluxo de refrigerante dentro do trocador de calor E3 a jusante da válvula f não é livremente se- lecionável. As composições das frações de refrigerante gasosa e líquida por sua vez estão acopladas pelos equilíbrios nos separadores D2 e D3. Portanto, o ajuste de válvula da válvula f não pode influenciar a um grau suficiente o perfil de temperatura na parte superior ou mais quente do trocador de calor E3.[00021] Due to the aforementioned expansion of the sub-cooled liquid gas fraction and also previously liquefied refrigerant mixed in the f and g valves to an essentially identical vaporization pressure, the temperature flow of the refrigerant flow inside the E3 heat exchanger downstream of the valve f is not freely selectable. The compositions of the gas and liquid refrigerant fractions are in turn coupled by the equilibria in the separators D2 and D3. Therefore, the valve setting of valve f cannot sufficiently influence the temperature profile at the top or the hotter part of the E3 heat exchanger.

[00022] De acordo com a invenção, portanto, pelo menos ocasionalmente, pelo menos um subfluxo da fração gasosa previamente líquida do refrigerante misturado 15 é expandida e adicionada à fração líquida expandida do refrigerante misturada na linha 22. Nas figuras, dois subfluxos de refrigerante misturados possíveis 19 e 24 estão mostrados os quais, após a expansão na válvula h ou j, respectivamente, podem ser adicionados ao refrigerante misturado expandido na linha 22. Na prática, na maioria dos casos, ou a válvula h ou a j está provida. A princípio, no entanto, os subfluxos de refrigerante misturado 19 e 24 podem ser utilizados separadamente ou juntamente para controlar a temperatura ou perfil de temperatura.[00022] According to the invention, therefore, at least occasionally, at least a subflow of the previously liquid gas fraction of the mixed refrigerant 15 is expanded and added to the expanded liquid fraction of the mixed refrigerant in line 22. In the figures, two subflows of refrigerant possible mixtures 19 and 24 are shown which, after expansion in valve h or j, respectively, can be added to the expanded mixed refrigerant in line 22. In practice, in most cases, either the h or aj valve is provided. In principle, however, mixed refrigerant subflows 19 and 24 can be used separately or together to control the temperature or temperature profile.

[00023] Neste caso, os subfluxos de refrigerante misturado 19 e/ou 24 é ou são retirados na extremidade fria do trocador de calor E3 e/ou a uma temperatura intermediária adequada através da linha 19 ou 24, expandidos na válvula h ou j e adicionados à fração líquida expandida do refrigerante misturado 22. Uma temperatura intermediária adequada está presente quando o refrigerante misturado 15 tem um subres- friamento de pelo menos 5°C, de preferência pelo menos 10°C, comparado com o estado de ebulição.[00023] In this case, the subflows of mixed refrigerant 19 and / or 24 are either removed at the cold end of the heat exchanger E3 and / or at a suitable intermediate temperature via line 19 or 24, expanded in the h or j valve added to the expanded liquid fraction of the mixed refrigerant 22. A suitable intermediate temperature is present when the mixed refrigerant 15 has a subcooling of at least 5 ° C, preferably at least 10 ° C, compared to the boiling state.

[00024] Por meio do procedimento de acordo com a invenção, uma controlabilidade suficiente da temperatura da fração rica em hidrocarbonetos ou do fluxo de gás natural 1 o qual deve ser liquefeito na entrada para a coluna de separação T está provida, e é requerida para ajustar uma concentração desejada dos hidrocarbonetos C2+ no produto de liquefação ou no LNG.[00024] By means of the procedure according to the invention, sufficient controllability of the temperature of the hydrocarbon-rich fraction or the flow of natural gas 1 which must be liquefied at the entrance to the separation column T is provided, and is required for adjust a desired concentration of C2 + hydrocarbons in the liquefaction product or LNG.

Claims (7)

1. Processo para liquefazer uma fração rica em hidrocarbo-netos com a remoção simultânea de uma fração rica em C2+, em que 0 resfriamento e a liquefação da fração rica em hidrocarbonetos ocorrem em troca de calor indireta contra 0 refrigerante misturado de um ciclo de refrigerante misturado no qual 0 refrigerante misturado é comprimido em pelo menos dois estágios, e a fração rica em C2+ é removida a um nível de temperatura ajustável, em que 0 refrigerante misturado é separado em uma fração gasosa e uma fração líquida, ambas as frações são subresfriadas, expandidas essencialmente para a pressão de sucção do primeiro estágio de compressor e pelo menos em parte vaporizadas, caracterizado pelo fato de que pelo menos ocasionalmente, pelo menos um subfluxo (19, 24), que é liquefeito contra ele mesmo, da fração gasosa previamente liquefeita do refrigerante misturado (15) é expandida (j, h) e adicionada à fração líquida expandida do refrigerante misturado (21).1. Process for liquefying a fraction rich in hydrocarbons with the simultaneous removal of a fraction rich in C2 +, where cooling and liquefaction of the fraction rich in hydrocarbons occurs in exchange of indirect heat against the mixed refrigerant of a refrigerant cycle mixed in which the mixed refrigerant is compressed in at least two stages, and the fraction rich in C2 + is removed at an adjustable temperature level, where the mixed refrigerant is separated into a gas fraction and a liquid fraction, both fractions are subcooled , expanded essentially to the suction pressure of the first compressor stage and at least partially vaporized, characterized by the fact that at least occasionally, at least a subflow (19, 24), which is liquefied against itself, of the gas fraction previously liquefied of the mixed refrigerant (15) is expanded (j, h) and added to the expanded liquid fraction of the mixed refrigerant (21). 2. Processo de acordo com a reivindicação 1, caracterizado pelo fato de que 0 subfluxo (19, 24) da fração gasosa previamente li-quefeita do refrigerante misturado (15) é retirado na extremidade fria do trocador de calor (E3) entre a fração rica em hidrocarbonetos a ser liquefeita (1, 2) e 0 refrigerante misturado (15, 17, 18, 20, 20', 22) e/ou a uma temperatura intermediária adequada, expandida (j, h) e adicionada à fração líquida expandida do refrigerante misturado (21), em que uma temperatura intermediária adequada está então presente quando 0 refrigerante misturado (15) tem um subresfriamento de pelo menos 5°C, comparado com 0 estado de ebulição.2. Process according to claim 1, characterized in that the subflow (19, 24) of the previously liquefied gas fraction of the mixed refrigerant (15) is removed at the cold end of the heat exchanger (E3) between the fraction rich in hydrocarbons to be liquefied (1, 2) and 0 mixed refrigerant (15, 17, 18, 20, 20 ', 22) and / or at a suitable intermediate temperature, expanded (j, h) and added to the expanded liquid fraction of the mixed refrigerant (21), where a suitable intermediate temperature is then present when the mixed refrigerant (15) has a subcooling of at least 5 ° C, compared to the boiling state. 3. Processo, de acordo com a reivindicação 2, caracterizado pelo fato de que 0 refrigerante misturado (15) tem um subresfriamento de pelo menos 10°C comparado com 0 estado de ebulição.3. Process according to claim 2, characterized by the fact that the mixed refrigerant (15) has a subcooling of at least 10 ° C compared to the boiling state. 4. Processo, de acordo com qualquer uma das reivindicações precedentes, caracterizado pelo fato de que a troca de calor entre a fração rica em hidrocarbonetos a ser liquefeita (1, 2) e o refrigerante misturado (15, 17, 18, 20, 20', 22) ocorre em um trocador de calor de múltiplos fluxos (E3), o qual está construído como um trocador de calor de placa ou um trocador de calor helicoidalmente enrolado.4. Process according to any of the preceding claims, characterized by the fact that the heat exchange between the hydrocarbon-rich fraction to be liquefied (1, 2) and the mixed refrigerant (15, 17, 18, 20, 20 ', 22) occurs in a multi-flow heat exchanger (E3), which is constructed as a plate heat exchanger or helically wound heat exchanger. 5. Processo, de acordo com qualquer uma das reivindicações precedentes, em que a fração rica em C2+ é removida em pelo menos uma coluna de separação, caracterizado pelo fato de que, pelo menos ocasionalmente, um subfluxo (5) da fração rica em hidrocarbonetos a ser liquefeita é alimentado para a região superior da coluna de separação (T).Process according to any one of the preceding claims, wherein the fraction rich in C2 + is removed in at least one separation column, characterized by the fact that, at least occasionally, a subflow (5) of the fraction rich in hydrocarbons to be liquefied is fed to the upper region of the separation column (T). 6. Processo, de acordo com qualquer uma das reivindicações precedentes, em que a fração rica em C2+ é removida em pelo menos uma coluna de separação, caracterizado pelo fato de que, pelo menos ocasionalmente, um subfluxo (6) da fração rica em hidrocarbonetos a ser liquefeita é alimentado para a região inferior da coluna de separação (T).Process according to any one of the preceding claims, wherein the fraction rich in C2 + is removed in at least one separation column, characterized by the fact that, at least occasionally, a subflow (6) of the fraction rich in hydrocarbons to be liquefied is fed to the lower region of the separation column (T). 7. Processo, de acordo com qualquer uma das reivindicações precedentes , em que a fração rica em C2+ é removida em pelo menos uma coluna de separação, caracterizado pelo fato de que a temperatura de fundo de coluna de separação é ajustada por meio de um permutador de reaquecimento (E4) designado para a coluna de separação (T).Process according to any one of the preceding claims, in which the fraction rich in C2 + is removed in at least one separation column, characterized by the fact that the bottom temperature of the separation column is adjusted by means of an exchanger reheating (E4) designated for the separation column (T).
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