BRPI0518529B1 - Process for Separation of a Rich C2 + LNG Fraction - Google Patents
Process for Separation of a Rich C2 + LNG Fraction Download PDFInfo
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- BRPI0518529B1 BRPI0518529B1 BRPI0518529-7A BRPI0518529A BRPI0518529B1 BR PI0518529 B1 BRPI0518529 B1 BR PI0518529B1 BR PI0518529 A BRPI0518529 A BR PI0518529A BR PI0518529 B1 BRPI0518529 B1 BR PI0518529B1
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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
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/0228—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream
- F25J3/0233—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of CnHm with 1 carbon atom or more
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/0204—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
- F25J3/0214—Liquefied natural gas
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/0228—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream
- F25J3/0238—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
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/0228—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream
- F25J3/0242—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of CnHm with 3 carbon atoms or more
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- 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
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2200/00—Processes or apparatus using separation by rectification
- F25J2200/04—Processes or apparatus using separation by rectification in a dual pressure main column system
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2200/00—Processes or apparatus using separation by rectification
- F25J2200/50—Processes or apparatus using separation by rectification using multiple (re-)boiler-condensers at different heights of the column
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- 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
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2200/00—Processes or apparatus using separation by rectification
- F25J2200/72—Refluxing the column with at least a part of the totally condensed overhead gas
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2205/00—Processes or apparatus using other separation and/or other processing means
- F25J2205/02—Processes or apparatus using other separation and/or other processing means using simple phase separation in a vessel or drum
- F25J2205/04—Processes or apparatus using other separation and/or other processing means using simple phase separation in a vessel or drum in the feed line, i.e. upstream of the fractionation step
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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
- F25J2215/00—Processes characterised by the type or other details of the product stream
- F25J2215/62—Ethane or ethylene
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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
- 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
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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
- 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
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- Oil, Petroleum & Natural Gas (AREA)
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- Filling Or Discharging Of Gas Storage Vessels (AREA)
Abstract
processo para separação de uma fração rica em c~ 2+~. de lng. a presente invenção refere-se a um processo para separação de uma fração rica em c~ 2+~ de gás natural liquefeito, que apresenta as seguintes etapas de processo: a) evaporação parcial (e1, e2) do gás natural liquefeito (1, 1'); b) separação (d1) do gás natural liquefeito parcialmente evaporado (2) em uma primeira fração de gás, rica em c~ 1~ (4) e uma primeira fração lí- quida, rica em c~ 2+~ (3); c) separação retificadora (t) da primeira fração de líquido, rica em c~ 2+~ (3), em uma segunda fração de gás, rica em c~ 1~; (8), e uma segunda fração de líquido, rica em c~ 2+~ (10); d) reliquefação (el) da primeira fração de gás, rica em c~ 1~(4; e e) alimentação de pelo menos uma corrente parcial (6) da fração de gás, rica em c~ 1~, reliquefeita (5), como cor- rente de retorno à separação retificadora (t).process for separating a fraction rich in c ~ 2 + ~. from lng. The present invention relates to a process for separating a C 2+ rich fraction of liquefied natural gas, which has the following process steps: a) partial evaporation (e1, e2) of liquefied natural gas (1, 1'); (b) separating (d1) the partially evaporated liquefied natural gas (2) into a first gas fraction rich in c ~ 1 ~ (4) and a first liquid fraction rich in c ~ 2 + ~ (3); c) rectifying separation (t) of the first fraction of liquid rich in c ~ 2 + ~ (3) into a second fraction of gas rich in c ~ 1; (8), and a second fraction of liquid, rich in c ~ 2 + ~ (10); (d) reliquefaction (el) of the first c1- rich gas fraction (4; and e) supplying at least one partial stream (6) of the reliquefied c1- rich gas fraction (5); as the return current to the rectifier separation (t).
Description
(54) Título: PROCESSO PARA SEPARAÇÃO DE UMA FRAÇÃO RICA EM C2+ DE LNG (51) Int.CI.: F25J 3/02 (30) Prioridade Unionista: 03/01/2005 DE 10 2005 000 634.5 (73) Titular(es): LINDE AKTIENGESELLSCHAFT (72) Inventor(es): HEINZ BAUER; HUBERT FRANKE; RAINER SAPPER(54) Title: PROCESS FOR SEPARATING A FRACTION RICH IN C2 + LNG (51) Int.CI .: F25J 3/02 (30) Unionist Priority: 03/01/2005 DE 10 2005 000 634.5 (73) ): LINDE AKTIENGESELLSCHAFT (72) Inventor (s): HEINZ BAUER; HUBERT FRANKE; RAINER SAPPER
Relatório Descritivo da Patente de Invenção para PROCESSO PARA SEPARAÇÃO DE UMA FRAÇÃO RICA EM C2+ DE LNG. DESCRIÇÃODescriptive Report of the Invention Patent for PROCESS FOR SEPARATION OF A FRACTION RICH IN C 2+ LNG. DESCRIPTION
A presente invenção refere-se a um processo para separação de 5 uma fração rica em C2+ de gás natural liquefeito (LNG).The present invention relates to a process for separating a C 2 + rich fraction from liquefied natural gas (LNG).
Processos de acordo com a espécie devem ser previstos, por exemplo, quando o valor de aquecimento de gás natural liquefeito não corresponde às especificações desejadas do da rede de tubulações às quais o gás natural deve ser alimentado. Em um caso desse tipo, é adicionado ao gás natural liquefeito um componente redutor do valor de aquecimento, por exemplo, nitrogênio, ou componentes, que causam um aumento do valor de aquecimento, são removidos do gás natural liquefeito. A seguir, é explicada mais detalhadamente a segunda alternativa citada.Processes according to the species should be provided, for example, when the heating value of liquefied natural gas does not correspond to the desired specifications of the pipeline network to which the natural gas must be fed. In such a case, a component that reduces the heating value, for example, nitrogen, or components that cause an increase in the heating value, are added to the liquefied natural gas to the liquefied natural gas. The second alternative mentioned is explained in more detail below.
Do documento US-A 5.114.451 é conhecido um processo de acordo com a espécie, para separação de uma fração rica em C2+ ou em C3+ de LNG, no qual - contrariamente ao processo realizado até o presente uma corrente parcial da fração de gás rica em C1, obtida na separação retificadora do gás natural (liquefeito), é reliquefeita e alimentada à separação retificadora como corrente de retorno. A corrente restante da fração de gás rica em C-ι só é condensada depois da separação da corrente parcial, que forma a corrente de retorno descrita acima, para a pressão de descarga ou da tubulação. O processo descrito no documento US-A 5,114,451 efetivamente possibilita o aumento do rendimento de etano para valores economicamente interessantes, mas isso é obtido pelo uso de pelo menos um con25 densador de alto custo.From US-A 5,114,451, a process according to the species is known for separating a fraction rich in C 2 + or C3 + from LNG, in which - contrary to the process carried out to date, a partial current of the fraction of gas rich in C1, obtained in the rectifying separation of natural gas (liquefied), is re-liquefied and fed to the rectifying separation as a return current. The remaining current of the gas fraction rich in C-ι is only condensed after the separation of the partial current, which forms the return current described above, for the discharge or pipe pressure. The process described in document US-A 5,114,451 effectively makes it possible to increase the ethane yield to economically interesting values, but this is achieved by using at least one high-cost condenser.
Também do documento US-A 3.420.068 é conhecido um processo de acordo com a espécie para separação de uma fração rica de C2+ de LNG. No mesmo, é dispensada uma recondensação da fração de gás rica em metano, obtida na separação retificadora do gás natural parcialmente evaporado, o que tem como consequência o fato de que podem ser obtidos apenas rendimentos de etano médios.Also from US-A 3,420,068 a process according to the species is known for separating a rich fraction of C 2 + from LNG. In it, a recondensation of the fraction of gas rich in methane, obtained in the rectifying separation of partially evaporated natural gas, is dispensed with, which results in the fact that only average ethane yields can be obtained.
É tarefa da presente invenção indicar um processo de acordo com a espécie, para separação de uma fração rica em C2+ de gás natural liquefeito (LNG), que possibilita um aumento do rendimento da fração rica em C2+, a uma simultânea redução dos custos de investimento, bem como de operação do processo, particularmente, a dispensa de uma condensação da fração de gás rica em metano.It is the task of the present invention to indicate a process according to the species, for separating a fraction rich in C2 + from liquefied natural gas (LNG), which allows an increase in the yield of the fraction rich in C2 +, while simultaneously reducing investment costs. , as well as the operation of the process, particularly the dispensing of a condensation of the gas fraction rich in methane.
Para solução da tarefa citada acima, é proposto um processo de acordo com a espécie para separação de uma fração rica em C2+ de gás natural liquefeito (LNG), que apresenta as seguintes etapas de processo:To solve the task mentioned above, a process according to the species is proposed to separate a fraction rich in C2 + from liquefied natural gas (LNG), which presents the following process steps:
a) evaporação parcial do gás natural liquefeito,a) partial evaporation of liquefied natural gas,
b) separação do gás natural liquefeito parcialmente evaporado em uma primeira fração de gás rica em C-i e uma primeira fração líquida, rica em C2+,b) separation of the partially evaporated liquefied natural gas into a first fraction of gas rich in C-i and a first liquid fraction, rich in C2 +,
c) separação retificadora da primeira fração de líquido, rica em C2+, em uma segunda fração de gás, rica em C-ι, e uma segunda fração de líquido, rica em C2+,c) rectifying separation of the first fraction of liquid, rich in C 2 +, in a second fraction of gas, rich in C-ι, and a second fraction of liquid, rich in C 2 +,
d) reliquefação da primeira fração de gás, rica em C1, ed) reliquefaction of the first gas fraction, rich in C1, and
e) alimentação de pelo menos uma corrente parcial da fração de gás, rica em C1, reliquefeita, como corrente de retorno à separação retificadora.e) supplying at least a partial current of the gas fraction, rich in C1, re-refined, as a return current to the rectifying separation.
Contrariamente aos procedimentos citados inicialmente, agora a primeira fração de gás, rica em C1( obtida na separação do gás natural parcialmente evaporado, é reliquefeita e pelo menos parcialmente conduzida para separação retificadora como corrente de retorno. O fio necessário para a reliquefação da primeira fração de gás, rica em C1, pode, nesse caso, ser posta à disposição exclusivamente pela corrente de gás natural líquido, que é submetida a um aquecimento até, no máximo, o ponto de ebulição. Como a fração de gás, rica em C-ι, alimentada à separação retificadora como retorno, apresenta um teor de etano comparativamente pequeno, pela mesma é causada uma relavagem de etano e componentes pesados do produto de cabeça das separações retificadoras e, desse modo, o aumento desejado do rendimento de C2+.Contrary to the procedures cited initially, now the first fraction of gas, rich in C 1 ( obtained in the separation of partially evaporated natural gas, is re-liquefied and at least partially conducted for rectifying separation as a return current. The wire necessary for the reliquefaction of the first gas fraction, rich in C1, can, in this case, be made available exclusively by the liquid natural gas stream, which is subjected to heating up to, at most, the boiling point. -ι, fed to the rectifier separation as a return, has a comparatively small ethane content, which causes an ethane overhaul and heavy components of the head product of the rectifier separations, thereby increasing the desired C2 + yield.
O processo de acordo com a invenção possibilita, portanto, que,The process according to the invention therefore allows that,
1° a um procedimento economicamente apropriado, sejam obtidos rendimentos de etano de mais de 90%. Esse valor situa-se no âmbito do rendimento de etano, tal como pode ser obtido com o processo complexo de acordo com o documento US-A 5.114.451, mas nitidamente acima do valor obtido a uma condução de processo de acordo com o documento US-A 3.420.068.1 ° to an economically appropriate procedure, ethane yields of more than 90% are obtained. This value is within the scope of the ethane yield, as can be obtained with the complex process according to US-A 5,114,451, but clearly above the value obtained by conducting a process according to US -A 3,420,068.
O processo de acordo com a invenção, bem como outras configurações do mesmo, que representam objetos das reivindicações de patente dependentes, são explicados mais detalhadamente, a seguir, por meio do exemplo de modalidade representado nas figuras 1 e 2.The process according to the invention, as well as other configurations thereof, which represent objects of the dependent patent claims, are explained in more detail below, by means of the example of embodiment shown in figures 1 and 2.
Tal como representado na figura 1, de um recipiente de armazenamento de LNG S é alimentado ao trocador de calor E1, através da tubulação 1, gás natural liquefeito e sub-refrigerado, que é bombeado por meio da bomba P1 para uma pressão entre 15 e 30 bar. No mesmo, o gás natural é aquecido contra a fração de gás, rica em Ci 4, a ser refrigerada e reliquefeita, que ainda será detalhada abaixo, até pouco antes do ponto de ebulição. A diferença para o ponto de ebulição perfaz, tipicamente, 5°C, no máximo, 20°C.As shown in figure 1, a LNG S storage container is fed to the heat exchanger E1, through the pipeline 1, liquefied and subcooled natural gas, which is pumped through the pump P1 to a pressure between 15 and 30 bar. In it, natural gas is heated against the gas fraction, rich in Ci 4, to be cooled and refined, which will be further detailed below, until just before the boiling point. The difference to the boiling point is typically 5 ° C at most 20 ° C.
Subseqüentemente, o gás natural aquecido é alimentado através da tubulação T a um outro trocador de calor E2 e aquecido no mesmo contra a segunda fração de gás, rica em Ci 8, que ainda será detalhada abaixo, e parcialmente evaporado.Subsequently, the heated natural gas is fed through the T-pipe to another heat exchanger E2 and heated therein against the second fraction of gas, rich in Ci 8, which will still be detailed below, and partially evaporated.
A corrente de gás natural parcialmente evaporada é alimentada através da tubulação 2 a um separador D1. No mesmo, dá-se uma separação da corrente de gás natural parcialmente evaporada para uma primeira fração de gás, rica em C-ι, que é retirada na cabeça do separador D1 através da tubulação 4, e uma primeira fração de líquido, rica em C2+. Esta última é alimentada através da tubulação 3, na qual está prevista uma bomba P3, à coluna de separação T e, desse modo, à separação retificadora.The partially evaporated natural gas stream is fed through piping 2 to a separator D1. In it, there is a separation of the partially evaporated natural gas stream for a first fraction of gas, rich in C-ι, which is removed at the head of separator D1 through piping 4, and a first fraction of liquid, rich in C 2 +. The latter is fed through piping 3, in which a pump P3 is provided, to the separation column T and, thus, to the rectifying separation.
Alternativamente ao retificador D1 representado na figura 1, pode ser prevista uma coluna de retificação, na qual é realizada a separação do gás natural 2 parcialmente evaporado. Nesse caso, a alimentação da corrente de gás natural 2 parcialmente evaporado é feita ao fundo da coluna de retificação. A corrente de retorno da coluna pode ser realizada ou por meio de uma corrente retirada da tubulação 6, ainda a ser descrita, ou de uma corrente, retirada da tubulação 8, ainda a ser descrita, depois do trocador de calor E2 e antes da válvula c. Essa configuração do processo de acordo com a invenção possibilita aumentar substancialmente o rendimento de C2, do que resulta uma redução das perdas no gás de aquecimento.Alternatively to the rectifier D1 shown in figure 1, a rectification column can be provided, in which the separation of the partially evaporated natural gas 2 is carried out. In this case, the partially evaporated natural gas stream 2 is fed to the bottom of the rectification column. The column return current can be carried out either by means of a chain removed from the pipeline 6, yet to be described, or by a chain, removed from the pipeline 8, still to be described, after the heat exchanger E2 and before the valve ç. This configuration of the process according to the invention makes it possible to substantially increase the yield of C2, resulting in a reduction of losses in the heating gas.
Na coluna de separação T dá-se uma separação retificadora da fração de líquido 3, rica em C2+, descrita acima, em uma segunda fração de gás, rica em C1, que é retirada na cabeça da coluna de separação T através da tubulação 8, e em uma segunda fração de líquido, rica em C2+. A coluna T pode apresentar fundos e/ou guarnições.In the separation column T there is a rectifying separation of the liquid fraction 3, rich in C2 +, described above, in a second fraction of gas, rich in C1, which is removed at the head of the separation column T through the pipe 8, and in a second fraction of liquid, rich in C2 +. Column T may have funds and / or trimmings.
A fração de líquido, rica em C2+, citada acima, é retirada através da tubulação 10, na qual está prevista uma válvula de regulagem, do fundo da coluna de separação T é descarrega do processo como uma chamada fração de NGL (Natural Gás Liquids) e, opcionalmente, conduzida para uma utilização adicional. Uma corrente parcial dessa fração é parcialmente evaporada no trocador de calor E3 e alimentada através da tubulação 11 como corrente de reboiler [reebulição] à coluna de separação T.The liquid fraction, rich in C2 +, mentioned above, is removed through the pipe 10, in which a regulating valve is provided, from the bottom of the separation column T is discharged from the process as a so-called NGL fraction (Natural Gas Liquids) and optionally driven for further use. A partial current of this fraction is partially evaporated in the heat exchanger E3 and fed through pipeline 11 as a reboiler current [re-boiling] to the separation column T.
De modo vantajoso, a separação retificadora T dá-se a uma pressão mais alta do que a separação D1 do gás natural 2 parcialmente evaporada em uma primeira fração de gás 4, rica em C-ι, e uma primeira fração de líquido 3, rica em C2+. Nesse caso, na separação ou no separador D1 é realizada, de preferência, uma pressão entre 15 e 25 bar, e na separação retificadora T, de preferência, uma pressão entre 30 e 40 bar. Para superar a diferença de pressão entre separador D1 e coluna de separação T, uma bomba P3 deve ser prevista na tubulação 3.Advantageously, the rectifying separation T occurs at a higher pressure than the separation D1 of the natural gas 2 partially evaporated in a first fraction of gas 4, rich in C-ι, and a first fraction of liquid 3, rich in C 2 +. In this case, in the separation or in the separator D1, a pressure between 15 and 25 bar is preferably carried out, and in the rectifying separation T, preferably a pressure between 30 and 40 bar. To overcome the pressure difference between separator D1 and separation column T, a pump P3 must be provided in piping 3.
A primeira fração de gás, rica em C-ι, obtida na separação da corrente de gás natural 2 parcialmente evaporada, que é retirada da cabeça do separador D1 através da tubulação 4, é reiiquefeita, pelo menos parcialmente, mas, de preferência, totalmente, no trocador de calor E2 contra a corrente de gás natural T a ser aquecida, e alimentada através da tubulação 8', na qual está disposta uma válvula de regulagem c, a um recipiente deThe first fraction of gas, rich in C-ι, obtained by separating the partially evaporated natural gas stream 2, which is removed from the head of the separator D1 through the tubing 4, is re-made, at least partially, but preferably totally , in the heat exchanger E2 against the natural gas stream T to be heated, and fed through the pipe 8 ', in which a regulating valve c is arranged, to a
carga da bomba D2. Ao mesmo é alimentada através da seção de tubulação 7, na qual também está disposta uma válvula de regulagem b, a corrente parcial da primeira fração rica em C-t, reliquefeita, que não é alimentada à coluna de separação T como corrente de retorno.pump load D2. It is fed through the pipe section 7, which also has a regulating valve b, the partial current of the first fraction rich in C-t, re-refined, which is not fed to the separation column T as a return current.
Do recipiente de carga da bomba D2 , a fração de produto de LNG, reduzida em C2+, é bombeada por meio da bomba P4 para a pressão de alimentação ou de tubulação - a mesma situa-se, em geral, entre 50 e 150 bar - e descarregada do processo através da tubulação 9, na qual também está prevista uma válvula de regulagem a.From the cargo container of pump D2, the fraction of LNG product, reduced by C 2 +, is pumped by means of pump P4 for the supply or piping pressure - it is generally between 50 and 150 bar - and discharged from the process through piping 9, which also includes a regulating valve a.
Caso a segunda fração de líquido, rica em C2+, obtida na separação retificadora T, que é retirada do fundo da coluna de separação T através da tubulação 10, deva ser submetida a uma separação de C2/C3, procede-se, de preferência, tal como representado na figura 2.If the second fraction of liquid, rich in C2 +, obtained in the rectifying separation T, which is removed from the bottom of the separation column T through the pipe 10, should be subjected to a separation of C2 / C3, it is preferable to proceed as shown in figure 2.
Nesse caso, a segunda fração de líquido, rica em C2+, é submetida a uma separação de C2/C3 retificadora na coluna de separação Τ'. Do fundo da coluna de separação Τ' é retirada através da tubulação 18 uma fração de produto de LPG, rica em C3+, e opcionalmente, conduzida a um processamento ou utilização adicional. Uma corrente parcial dessa fração é parcialmente evaporada no trocador de calor E5 e alimentada através da tubulação 19 como corrente de reboiler [reebulição] à coluna de separação T.In this case, the second fraction of liquid, rich in C 2 +, is subjected to a separation of C2 / C3 rectifier in the separation column Τ '. From the bottom of the separation column Τ ', a fraction of LPG product, rich in C 3+ , is removed through the pipe 18 and optionally conducted for further processing or use. A partial current of this fraction is partially evaporated in the E5 heat exchanger and fed through piping 19 as a reboiler [re-boiling] current to the separation column T.
Na cabeça da coluna de separação Τ' é retirada através da tubulação 12 uma fração de gás, rica em C2/C3, pelo menos parcialmente condensada na caldeira lateral E4, e, subseqüentemente, alimentada através da tubulação 14 ao recipiente de carga da bomba D3.At the head of the separation column Τ ', a fraction of gas, rich in C2 / C3, at least partially condensed in the side boiler E4, is drawn through the pipe 12 and subsequently fed through the pipe 14 to the loading container of the pump D3. .
Do recipiente de carga da bomba D3 a fração rica em C2/C3, condensada, é alimentada através da tubulação 15 à bomba P5 e por meio da mesma bombeada para a pressão de alimentação desejada. Uma corrente secundária da fração bombeada é alimentada através da tubulação 16 e da válvula de regulagem f, à cabeça da coluna de separação Τ' como corrente de retorno, enquanto a corrente principal da fração bombeada é descarregada do processo através da tubulação 17 e conduzida, opcionalmente, |3 a uma utilização ou processamento adicional.From the cargo container of pump D3, the fraction rich in C2 / C3, condensed, is fed through pipe 15 to pump P5 and through it pumped to the desired supply pressure. A secondary current from the pumped fraction is fed through the pipe 16 and the regulating valve f, to the head of the separation column Τ 'as a return current, while the main current of the pumped fraction is discharged from the process through the pipe 17 and conducted, optionally, | 3 for additional use or processing.
Altemativamente ao procedimento descrito com base na figura 2, também podem ser realizados, no entanto, outros processos de separação de C2/C3, por exemplo, a retirada de uma fração de produto de cabeça gasosa do recipiente D3.In addition to the procedure described on the basis of figure 2, however, other C2 / C3 separation processes can also be carried out, for example, the removal of a fraction of gaseous head product from container D3.
Desenvolvendo adicionalmente o processo de acordo com a invenção para separação de uma fração rica em C2+, propõe-se que a refrigeração de correntes de processo, que resultam da separação Τ' da segunda fração de líquido, rica em C2+, contra a primeira fração de líquido, rica em C2+ e/ou contra pelo menos uma fração de líquido, que é retirada da separação retificadora, se dê abaixo da alimentação da primeira fração de líquido, rica em C2+.Further developing the process according to the invention to separate a fraction rich in C 2 +, it is proposed that the cooling of process currents, which result from the separation Τ 'of the second fraction of liquid, rich in C 2 +, against the first fraction of liquid, rich in C 2 + and / or against at least one fraction of liquid, which is removed from the rectifying separation, occurs below the feed of the first fraction of liquid, rich in C 2+ .
Particularmente se a segunda fração de líquido 10, rica em C2+, for submetida a uma separação de C2/C3 retificadora, recomenda-se que a fração de gás, rica em C2/C3 12, obtida na separação de C2/C3 Τ' retificadora, seja refrigerada no trocador de calor contra a primeira fração de líquido 3, rica em C2+, de preferência, para uma temperatura de armazenamento sem pressão.Particularly if the second fraction of liquid 10, rich in C 2 +, is subjected to a separation of C 2 / C3 rectifier, it is recommended that the gas fraction, rich in C 2 / C3 12, obtained in the separation of C 2 / C3 Τ 'rectifier, be cooled in the heat exchanger against the first fraction of liquid 3, rich in C 2+ , preferably to a pressure-free storage temperature.
O trocador de calor necessário para esse fim, pode estar previsto, por exemplo, entre a bomba P3 e a coluna de separação T. Para que pode ser realizado um armazenamento sem pressão, no caso de uma fração de gás, que consiste predominantemente em etano, obtida na cabeça da separação de C2/C3 Τ', é necessária uma temperatura de cerca de -100°C. Nessa condução de processo, é vantajoso que em todo o processo pode ser dispensada uma refrigeração externa - portanto, uma refrigeração abaixo da temperatura ambiente - ou uma condensação - termodinamicamente equivalente.The heat exchanger required for this purpose may be provided, for example, between the P3 pump and the separation column T. So that pressure-free storage can be carried out in the case of a gas fraction, which consists predominantly of ethane , obtained at the head of the separation of C 2 / C3 Τ ', a temperature of about -100 ° C is required. In this process conduction, it is advantageous that in the whole process external cooling - therefore, cooling below room temperature - or thermodynamically equivalent condensation - can be dispensed with.
Quando todas as correntes de processo, tal como explicado no processo representado por meio das figuras 1 e 2, entram em estado líquido (corrente 1) e são novamente descarregadas em estado líquido (correntes 9 e 10 ou 9, 17 e 18), a refrigeração dá-se, finalmente, da sub-refrigeração do LNG usado.When all process currents, as explained in the process represented by figures 1 and 2, enter a liquid state (current 1) and are again discharged into a liquid state (currents 9 and 10 or 9, 17 and 18), the cooling occurs, finally, from the sub-cooling of the used LNG.
O processo de acordo com a invenção para separação de uma fração rica em C2+ de gás natural liquefeito (LNG) possibilita a obtenção de altos rendimentos de etano, a uma dispensa simultânea de condensadores de alto custo.The process according to the invention for separating a fraction rich in C2 + from liquefied natural gas (LNG) makes it possible to obtain high ethane yields, while simultaneously dispensing high-cost condensers.
Claims (10)
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DE102005000634A DE102005000634A1 (en) | 2005-01-03 | 2005-01-03 | Process for separating a C2 + -rich fraction from LNG |
DE102005000634.5 | 2005-01-03 | ||
PCT/EP2005/013748 WO2006072390A1 (en) | 2005-01-03 | 2005-12-21 | Method for separating a fraction rich in c2+ from liquefied natural gas |
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BRPI0518529A2 BRPI0518529A2 (en) | 2008-11-25 |
BRPI0518529B1 true BRPI0518529B1 (en) | 2018-06-26 |
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EP (1) | EP1834144B1 (en) |
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CN (1) | CN101095023B (en) |
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US7603867B2 (en) * | 2006-09-11 | 2009-10-20 | Cryogenic Group, Inc. | Process and system to produce multiple distributable products from source, or imported LNG |
US8820096B2 (en) | 2007-02-12 | 2014-09-02 | Daewoo Shipbuilding & Marine Engineering Co., Ltd. | LNG tank and operation of the same |
US7644676B2 (en) | 2008-02-11 | 2010-01-12 | Daewoo Shipbuilding & Marine Engineering Co., Ltd. | Storage tank containing liquefied natural gas with butane |
KR20090107805A (en) | 2008-04-10 | 2009-10-14 | 대우조선해양 주식회사 | Method and system for reducing heating value of natural gas |
JP5686989B2 (en) * | 2010-05-13 | 2015-03-18 | エア・ウォーター株式会社 | Production of liquefied natural gas for automobiles |
DE102012021637A1 (en) * | 2012-11-02 | 2014-05-08 | Linde Aktiengesellschaft | Process for cooling a hydrocarbon-rich fraction |
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FR1501013A (en) | 1966-09-13 | 1967-11-10 | Air Liquide | Process for the production of a gas rich in methane under high pressure from liquid natural gas under low pressure |
US5114451A (en) | 1990-03-12 | 1992-05-19 | Elcor Corporation | Liquefied natural gas processing |
US6116050A (en) * | 1998-12-04 | 2000-09-12 | Ipsi Llc | Propane recovery methods |
US6742358B2 (en) * | 2001-06-08 | 2004-06-01 | Elkcorp | Natural gas liquefaction |
FR2831656B1 (en) * | 2001-10-31 | 2004-04-30 | Technip Cie | METHOD AND PLANT FOR SEPARATING A GAS CONTAINING METHANE AND ETHANE WITH TWO COLUMNS OPERATING UNDER TWO DIFFERENT PRESSURES |
US6941771B2 (en) * | 2002-04-03 | 2005-09-13 | Howe-Baker Engineers, Ltd. | Liquid natural gas processing |
US6564579B1 (en) * | 2002-05-13 | 2003-05-20 | Black & Veatch Pritchard Inc. | Method for vaporizing and recovery of natural gas liquids from liquefied natural gas |
US7051553B2 (en) * | 2002-05-20 | 2006-05-30 | Floor Technologies Corporation | Twin reflux process and configurations for improved natural gas liquids recovery |
US6907752B2 (en) * | 2003-07-07 | 2005-06-21 | Howe-Baker Engineers, Ltd. | Cryogenic liquid natural gas recovery process |
US7155931B2 (en) * | 2003-09-30 | 2007-01-02 | Ortloff Engineers, Ltd. | Liquefied natural gas processing |
US7278281B2 (en) * | 2003-11-13 | 2007-10-09 | Foster Wheeler Usa Corporation | Method and apparatus for reducing C2 and C3 at LNG receiving terminals |
DE05856782T1 (en) * | 2004-07-01 | 2007-10-18 | Ortloff Engineers, Ltd., Dallas | PROCESSING OF LIQUEFIED GAS |
EP1789739B1 (en) * | 2004-09-14 | 2020-03-04 | Exxonmobil Upstream Research Company | Method of extracting ethane from liquefied natural gas |
AU2005316515B2 (en) * | 2004-12-16 | 2010-02-18 | Fluor Technologies Corporation | Configurations and methods for LNG regasification and BTU control |
CA2653610C (en) * | 2006-06-02 | 2012-11-27 | Ortloff Engineers, Ltd. | Liquefied natural gas processing |
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ES2665688T3 (en) | 2018-04-26 |
JP2008527287A (en) | 2008-07-24 |
CN101095023B (en) | 2010-12-22 |
EP1834144A1 (en) | 2007-09-19 |
US20090211296A1 (en) | 2009-08-27 |
WO2006072390A1 (en) | 2006-07-13 |
DE102005000634A1 (en) | 2006-07-13 |
EP1834144B1 (en) | 2018-02-28 |
KR20070100760A (en) | 2007-10-11 |
CN101095023A (en) | 2007-12-26 |
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BRPI0518529A2 (en) | 2008-11-25 |
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