AU2017359435A1 - Bath-type vaporiser-condenser for a method of cryogenically separating a natural gas stream - Google Patents

Bath-type vaporiser-condenser for a method of cryogenically separating a natural gas stream Download PDF

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Publication number
AU2017359435A1
AU2017359435A1 AU2017359435A AU2017359435A AU2017359435A1 AU 2017359435 A1 AU2017359435 A1 AU 2017359435A1 AU 2017359435 A AU2017359435 A AU 2017359435A AU 2017359435 A AU2017359435 A AU 2017359435A AU 2017359435 A1 AU2017359435 A1 AU 2017359435A1
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AU
Australia
Prior art keywords
stage
column
natural gas
liquid product
stream
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Abandoned
Application number
AU2017359435A
Inventor
Paul Terrien
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
Original Assignee
Air Liquide SA
LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Air Liquide SA, LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude filed Critical Air Liquide SA
Publication of AU2017359435A1 publication Critical patent/AU2017359435A1/en
Abandoned legal-status Critical Current

Links

Classifications

    • 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
    • F25J3/0242—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of CnHm with 3 carbon atoms or more
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/04—Processes or apparatus using separation by rectification in a dual pressure main column system
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/74—Refluxing the column with at least a part of the partially condensed overhead gas
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/78—Refluxing the column with a liquid stream originating from an upstream or downstream fractionator column
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2205/00—Processes or apparatus using other separation and/or other processing means
    • F25J2205/02—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
    • 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
    • F25J2235/00—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams
    • F25J2235/60—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams the fluid being (a mixture of) hydrocarbons
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2240/00—Processes or apparatus involving steps for expanding of process streams
    • F25J2240/02—Expansion of a process fluid in a work-extracting turbine (i.e. isentropic expansion), e.g. of the feed stream
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2250/00—Details related to the use of reboiler-condensers
    • F25J2250/02—Bath type boiler-condenser using thermo-siphon effect, e.g. with natural or forced circulation or pool boiling, i.e. core-in-kettle heat exchanger

Abstract

The invention relates to a method for cryogenically separating a natural gas supply stream into a gas which contains the most volatile compounds of the supply stream, and a liquid product which contains the heaviest compounds of the supply stream, at least comprising the following steps: - step a): at least partially condensing a natural gas supply stream in a first heat exchanger system; - step b): introducing the at least partially condensed stream from step a) into an absorption column at an introduction stage in the lower part of said absorption column, said absorption column producing, at the top, a gaseous stream which contains the most volatile compounds and, in the bottom, a liquid product; - step c): introducing the liquid product produced in step b) into a fractionation column in order to obtain, in the bottom of the fractionation column, a liquid product that contains the heaviest compounds of the supply stream and, at the top of the fractionation column, a distillate that is at least partially condensed; - step d): introducing, at a stage in the upper part of the absorption column, the gaseous phase of the condensed distillate produced in step c) as a supply stream for the absorption column; characterised in that the distillate from step c) is condensed in a bath-type vaporiser-condenser installed in a casing mounted on the fractionation column.

Description

BATH-TYPE VAPORISER-CONDENSER FOR A METHOD OF CRYOGENICALLY
SEPARATING A NATURAL GAS STREAM
The present invention relates to a process for the cryogenic separation of a natural gas feed stream into a gas containing the most volatile compounds of the feed stream and into a liquid product containing the heaviest compounds of the feed stream.
During the exploitation of natural gas deposits, numerous stages may be provided. A relatively conventional stage after the drying and the withdrawal of the impurities is the separation of the liquids associated with the natural gas (NGLs).
It is often desirable to separate the heavy hydrocarbons, or more generally the NGL (Natural Gas Liquids), from the natural gas, for example such as ethane, butane, propane or C5+ and C6+ (that is to say, having at least five carbon atoms and having more than six carbon atoms) hydrocarbons.
This stage can have many advantages but often it is a matter of upgrading various products (ethane, propane, and the like) which are generally sold at a much higher price than the natural gas product. It is in particular common to sell hydrocarbons having a least three carbon atoms as propane, butane and condensate products.
Many industrial installations have been described which make it possible to fractionate gas feedstocks into a residual gas containing the most volatile compounds of the feedstock and into a liquid product containing the heaviest compounds of the feedstock, this being done for the purpose of obtaining, in said liquid product, a given component of the feedstock with a high degree of recovery.
In this regard, mention may be made, for example, of the recovery of liquefied petroleum gas (hydrocarbons therein having three or four carbon atoms) from natural or refinery gas, the recovery of ethane intended in particular to feed steam cracking units, or the desulfurization and the gasoline extraction of natural gases by recovery of the sulfur-comprising compounds, such as carbon oxysulfide and mercaptains
Several technologies exist for producing hydrocarbons having at least three carbon atoms from natural gas.
One of the most effective is a process employing a two-column turboexpander in which the first column is an absorber dedicated to forcing the recovery of as much propane as possible and the second column is a de-ethanizer.
The condensation of the de-ethanizer top stream is often carried out in part with the fluid coming from the absorber bottom.
Such a process is described in the documents US 4 690 702 and US 5 114 450.
Such processes can prove to be complicated to control and require investment in fairly expensive components, such as pumps.
The inventors of the present invention have thus developed a solution which makes it possible to solve the problems raised above.
A subject matter of the present invention is a process as defined in claims 1 to 4.
According to another embodiment, another subject-matter of the invention is an apparatus as defined in claim 5.
The stream of hydrocarbons to be liquefied is generally a stream of natural gas obtained from natural gas fields, oil reservoirs or a domestic gas network in which the gas is distributed via pipelines.
Generally, the natural gas stream is essentially composed of methane. Preferably, the feed stream comprises at least 80 mol% of methane. Depending on the source, the natural gas contains quantities of hydrocarbons heavier than methane, such as, for example, ethane, propane, butane and pentane and also certain aromatic hydrocarbons. The natural gas stream also contains nonhydrocarbon products, such as H2O, N2, CO2, H2S and other sulfur-comprising compounds, mercury and others.
The feed stream containing the natural gas is thus pretreated before being introduced into the heat exchanger making possible the first stage of cooling of the process which is a subject matter of the present invention. This pretreatment comprises the reduction and/or the removal of the undesirable components, such as CO2 and H2S, or other stages, such as the precooling and/or the pressurization.
Given that these measures are well known to a person skilled in the art, they are not described in further detail here.
The expression “natural gas” as used in the present patent application relates to any composition containing hydrocarbons, including at least methane.
This comprises a crude composition (prior to any treatment or scrubbing) and also any composition which has been partially, substantially or completely treated for the reduction and/or removal of one or more compounds, including, but without being limited thereto, sulfur, carbon dioxide, water, mercury and certain heavy and aromatic hydrocarbons.
The heat exchanger can be any heat exchanger, any unit or other arrangement suitable for making possible the passage of a certain number of streams, and thus making possible at least one system for direct or indirect exchange of heat between one or more liquid coolant lines and one or more feed streams.
A bath vaporizer-condenser is, for example, of the type as described in the patent application EP 1 087 194.
The invention will be described in a more detailed manner with reference to the figure.
The figure illustrates the diagram of an embodiment of an implementation of a process according to the invention.
In the figure, a feed stream of natural gas 1 is introduced into a main heat exchanger 2 in order to be cooled. The gas thus cooled 3 is partially condensed and introduced into a phase separator 4. The gas phase 5 at the phase separator 4 top is introduced into a turbine 6 in order to recover the expansion energy and to condense a portion of the stream 5, and is then introduced into an absorption column 7 comprising a lower part 7' and an upper part 7. The liquid phase 8 at the phase separator 4 bottom is introduced after expansion 9 into the absorption column 7. The absorption column produces a liquid 10 at the column bottom and a residual gas 11 at the column top. The liquid 10 is reheated in a heat exchanger 12 in which it is partially evaporated. The stream thus reheated 13 is subsequently introduced into the main exchanger 2; this introduction 13 is thus strongly a twophase introduction.
At the absorption column 7 top, the residual gas 11, which contains only the products more volatile than ethane, is reheated in the main heat exchanger 2; the stream which results therefrom 14 is subsequently compressed and sent to a treatment unit A.
The stream 13’ at the heat exchanger 2 outlet resulting from the bottom of the absorption column 7 is introduced into a fractionation column 15.
This column 15 produces, at the bottom 16, a reboiled liquid product 18 using a reboiler 17 in order to obtain a liquid rich in propane and depleted in ethane.
A gas 20 is produced at the fractionation column 15 top 19. This gas 20 is condensed in the heat exchanger 12 and the product 21 which exits from this exchanger 12 is introduced into a phase separator 22. The gas phase 23 at the top of the phase separator 22 acts as reflux in the absorption column 7. The liquid 25 at the bottom of the phase separator 22 acts as reflux 26 at the top of the fractionation column 15. A pump is not necessary to pump the liquid 25. This arrangement with the use of a bath vaporizer-condenser exhibits the advantage of being very easy to control while integrating the exchanger and the fractionation column and without using a pump (thermosiphon scheme).

Claims (5)

1. A process for the cryogenic separation of a natural gas feed stream (1) into a gas containing the most volatile compounds (14) of the feed stream (1) and into a liquid product (18) containing the heaviest compounds of the feed stream (1), comprising at least the following stages:
- Stage a): at least partial condensation of a natural gas feed stream (1) in a first heat-exchange system (2);
- Stage b): introduction of the at least partially condensed stream (3) resulting from stage a) into an absorption column (7) at an introduction level located in the lower part of said absorption column, said absorption column producing, at the top, a gas stream (11) containing the most volatile compounds and, at the bottom, a liquid product (10);
- Stage c): introduction of the liquid product resulting from stage b) into a fractionation column (15) in order to obtain, in the fractionation column (15) bottom (16), a liquid product (18) containing the heaviest compounds of the feed stream and, at the fractionation column top (19), an at least partially condensed distillate (21)
- Stage d): introduction, at a level located in the upper part of the absorption column (7), of the gas phase (23) of the condensed distillate (21) resulting from stage c) as feed stream (24) of the absorption column (7); characterized in that the distillate (21) resulting from stage c) is condensed in a bath vaporizer-condenser installed in a shell surrounding the fractionation column (15).
2. The process as claimed in the preceding claim, characterized in that the bath vaporizer-condenser contains at least one heat exchanger (12) fed with refrigerating fluid by the liquid product (10) resulting from stage b).
3. The process as claimed in either one of the preceding claims, characterized in that the liquid phase (25) of the condensed distillate (21) resulting from stage c) is used as reflux (26) at the top of the fractionation column (15).
4. The process as claimed in the preceding claim, characterized in that no pump is necessary for setting up said reflux.
5. A unit for the cryogenic separation of a natural gas feed stream (1) making possible the implementation of the process as defined in one of the preceding claims, characterized in that a pipe connects the top (19) of the fractionation column (15) to a heat exchanger (12) surmounting said fractionation column (15), which heat exchanger is itself placed in a shell provided for a bath formed predominantly of hydrocarbons.
AU2017359435A 2016-11-08 2017-11-08 Bath-type vaporiser-condenser for a method of cryogenically separating a natural gas stream Abandoned AU2017359435A1 (en)

Applications Claiming Priority (3)

Application Number Priority Date Filing Date Title
FR1660780 2016-11-08
FR1660780A FR3058509B3 (en) 2016-11-08 2016-11-08 BATHTUB-CONDENSER FOR A PROCESS FOR CRYOGENIC SEPARATION OF A NATURAL GAS CURRENT
PCT/FR2017/053046 WO2018087472A1 (en) 2016-11-08 2017-11-08 Bath-type vaporiser-condenser for a method of cryogenically separating a natural gas stream

Publications (1)

Publication Number Publication Date
AU2017359435A1 true AU2017359435A1 (en) 2019-06-13

Family

ID=60582615

Family Applications (1)

Application Number Title Priority Date Filing Date
AU2017359435A Abandoned AU2017359435A1 (en) 2016-11-08 2017-11-08 Bath-type vaporiser-condenser for a method of cryogenically separating a natural gas stream

Country Status (5)

Country Link
US (1) US20190277565A1 (en)
AU (1) AU2017359435A1 (en)
FR (1) FR3058509B3 (en)
RU (1) RU2019115689A (en)
WO (1) WO2018087472A1 (en)

Family Cites Families (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR2571129B1 (en) 1984-09-28 1988-01-29 Technip Cie PROCESS AND PLANT FOR CRYOGENIC FRACTIONATION OF GASEOUS LOADS
FR2646166B1 (en) 1989-04-25 1991-08-16 Technip Cie PROCESS FOR RECOVERING LIQUID HYDROCARBONS FROM A GASEOUS LOAD AND PLANT FOR CARRYING OUT SAID PROCESS
FR2798598B1 (en) 1999-09-21 2002-05-24 Air Liquide BATH VAPORIZER-CONDENSER AND CORRESPONDING AIR DISTILLATION APPARATUS
FR2956900B1 (en) * 2010-03-01 2012-06-01 Air Liquide APPARATUS AND METHOD FOR SEPARATING A MIXTURE CONTAINING CARBON DIOXIDE BY DISTILLATION
DE102010035230A1 (en) * 2010-08-24 2012-03-01 Linde Aktiengesellschaft Process for separating nitrogen from natural gas
JP6517497B2 (en) * 2014-11-05 2019-05-22 エア・ウォーター株式会社 Apparatus for producing liquefied natural gas and method for producing liquefied natural gas

Also Published As

Publication number Publication date
FR3058509B3 (en) 2019-02-01
RU2019115689A3 (en) 2020-11-23
US20190277565A1 (en) 2019-09-12
WO2018087472A1 (en) 2018-05-17
FR3058509A3 (en) 2018-05-11
RU2019115689A (en) 2020-11-23

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