WO2016156675A1 - Procédé de déazotation du gaz naturel à haut débit - Google Patents
Procédé de déazotation du gaz naturel à haut débit Download PDFInfo
- Publication number
- WO2016156675A1 WO2016156675A1 PCT/FR2015/052632 FR2015052632W WO2016156675A1 WO 2016156675 A1 WO2016156675 A1 WO 2016156675A1 FR 2015052632 W FR2015052632 W FR 2015052632W WO 2016156675 A1 WO2016156675 A1 WO 2016156675A1
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- WO
- WIPO (PCT)
- Prior art keywords
- gas
- denitrogenation
- nitrogen
- natural gas
- stream
- Prior art date
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Classifications
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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
- F25J3/0257—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 nitrogen
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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
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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
- F25J3/0228—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
- 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
- F25J2200/70—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
- F25J2200/78—Refluxing the column with a liquid stream originating from an upstream or downstream fractionator 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
- 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
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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
- 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
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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
- F25J2290/00—Other details not covered by groups F25J2200/00 - F25J2280/00
- F25J2290/50—Arrangement of multiple equipments fulfilling the same process step in parallel
Definitions
- the present invention relates to a method for separating the components of a gaseous mixture containing methane, nitrogen and hydrocarbons heavier than methane.
- the present invention therefore applies to denitrogenation processes of natural gas with or without helium recovery.
- Natural gas is desirable for use as a fuel for use in heating buildings, to provide heat for industrial processes for the generation of electricity, for use as a feedstock for various synthesis processes for produce olefins, polymers and the like.
- Natural gas is found in many areas that are remote from natural gas users. Natural gas typically consists of methane (C1), ethane (C2) and heavier compounds such as hydrocarbons having at least three carbon atoms, such as propane, butane ... (C3 +).
- C2 and C3 + from natural gas may be advantageous to separate C2 and C3 + from natural gas for commercialization as separate co-products. Indeed, their recovery is generally greater than the natural gas itself because they can be used directly for chemical processes (manufacture of ethylene from ethane for example), as fuels (C3 / C4 is a fuel classic called GPL) or for many other applications.
- nitrogen Another component often found in natural gas is nitrogen.
- the presence of nitrogen in natural gas can lead to difficulties in meeting the specifications for natural gas (typically the minimum heating value to be met). This is all the more true when hydrocarbons heavier than methane (C2 and C3 +) are removed because they have a lower heating value than methane, so removing them reduces the lower calorific value than the methane. it may then be necessary to increase by means of nitrogen separation. As a result, considerable effort has been devoted to developing ways to remove nitrogen from natural gas.
- the exploited natural gas fields contain more and more nitrogen. This is particularly due to the depletion and scarcity of fields rich enough that no enrichment treatment is necessary before the marketing of gas.
- Unconventional resources such as shale gas also have the same problem: to make them marketable, it may be necessary to increase their calorific value by means of a treatment that consists in de-gasing the gas.
- cryogenic separation The most widely used method for separating nitrogen and hydrocarbons heavier than methane is "cryogenic separation".
- a cryogenic nitrogen separation process more specifically a method employing a double column, is described in US-A-4778498.
- Natural gas denitrogen units generally treat gases that come directly from wells at high pressure. After denaturing, the treated gas must be returned to the network, often at a pressure close to its inlet pressure.
- NTL natural gas-associated liquids
- NGL unit operates the separation of NGL (later called NGL unit) while a second unit separates nitrogen from natural gas (later called NRU unit).
- This solution has the advantage of flexibility in operation. For example, if the NRU has a refrigeration cycle, the associated machines have limited reliability, and failure of a cycle compressor will cause the NRU to shut down, but without stopping the NGL.
- this stop can not be long since it will then send to the flare production (because of its calorific value too low).
- this scheme is limited in efficiency because all the gas is cooled and then warmed in the NGL unit and then cooled and heated in the NRU.
- the inventors of the present invention have then bridged a solution to solve the problems raised above.
- the present invention relates to a process for separating the components of a gaseous mixture to be treated comprising methane, nitrogen and at least one hydrocarbon having at least two carbon atoms, or a mixture of these hydrocarbons, comprising the steps following:
- the method which is the subject of the present invention comprises at least the following characteristics:
- step d) treating said gas (36) from step c) in a second denitrogenation unit (B) to produce a nitrogen gas stream comprising at most 2 mol% of methane and a methane gas stream comprising at most 5 mol% of nitrogen.
- the second denitrogenation unit (B) comprises at most N - 1 denitrogenation columns.
- N is greater than or equal to 6.
- the second denitrogenation unit (B) comprises between N - 5 denitrogenation columns and N - 1 denitrogenation columns, preferably N - 4 denitrogenation columns with N - 2.
- steps b) and c) are carried out at a temperature below -50 ° C and the fluid is not heated above -50 ° C between step b) and step c).
- a stream 1 of pretreated natural gas (separation of water, CO 2 , methanol, very heavy hydrocarbons, that is to say having more than six or seven carbon atoms (such as C8 + for example) comprising at least 30 mol% of methane, 0.1 mol% of hydrocarbons heavier than methane (that is to say comprising at least two carbon atoms) and 4 mol% of nitrogen is introduced into a system 2 allowing at least partial condensation of said stream 1.
- the pressure of this stream 1 is between 20 bara (absolute bar) and 100 bara (typically between 30 and 70 bara) and the temperature is close to room temperature, for example between 10 ° C and 30 ° C.
- the system 2 is for example a heat exchanger.
- the mixture 3 leaving this system 2 is in a two-phase state (gas and liquid).
- This mixture 3 is introduced into a phase separator pot 4.
- the operating pressure is between 20 and 100 bara, typically between 30 and 70 bara.
- the temperature of this pot is between -100 ° C and 0 ° C, typically between -80 ° C and -20 ° C.
- the liquid phase 5 from the separator pot 4 is expanded through a valve 6 and then injected at a pressure of between 10 bara and 40 bara and a temperature of, for example, between -10.degree. C. and -30.degree. a demethanization column 7.
- demethanizer column is meant a distillation unit for producing at least two streams of different compositions from feed streams from stream 1 of natural gas to be treated according to the method of the present invention.
- the at least two streams are the following: one gas, depleted in hydrocarbons having at least two carbon atoms, that is to say comprising less than half of the so-called heavy hydrocarbons contained in the feed gas (ethane propane, butane, etc.) and the other, in liquid form, containing less than 5 mol% of the methane initially present in stream 1 of natural gas to be treated.
- demethanization unit any system comprising at least one distillation column to enrich the methane in the overhead gas and to lower the methane tank liquid.
- At least a portion of the gas phase (only a portion typically) 8 from the separator pot 4 is expanded by means of a turbine 9.
- the flow from the turbine 9 is introduced into the column 7 at a higher stage than the stage where the liquid 5 is introduced at the outlet of the valve 6.
- a liquid stream 12 of hydrocarbons heavier than methane is recovered in the lower part 16 of column 7.
- a reboiler 1 1 is placed at a level to reboil the bottom liquid of the column 7 to heat a portion of the liquid of said column in order to adjust the maximum threshold of methane contained in the stream 12 of heavy hydrocarbons .
- At least 50% (typically at least 85%) molar heavy hydrocarbons present in the gaseous mixture 1 to be treated are recovered in this stream 12. Preferably at least 90% is recovered.
- the hydrocarbon liquid stream 12 does not contain more than 1 mol% of methane.
- a gas stream 15 enriched in methane typically containing less than 0.5 mol% of hydrocarbons having more than two carbon atoms (containing at most the half of the amount of heavy hydrocarbons - having more than 2 carbon atoms - present in the feed gas) is extracted.
- the temperature of the gas stream is less than -80 ° C.
- the cold can be recovered by condensing a gas enriched in methane under pressure.
- This condensation is achieved by means of a heat exchanger 17 fed at the same time by a part of the gas stream 8 coming from the separator pot 4 and by the gas stream enriched in methane 15 coming from the head 14 of the demethanization column 7. It does not This is only an example of implementation of the method that is the subject of the invention. But according to a particular embodiment of the invention, a third current to be condensed could be introduced into this exchanger. According to yet another embodiment of the invention, only one of the two described currents would be to condense.
- gas enriched in methane gas mixture containing methane, nitrogen and typically less than 0.5% of hydrocarbons having more than two carbon atoms (containing at most half the amount of heavy hydrocarbons - having more than two carbon atoms - present in the feed gas).
- the stream which has been reheated in the exchanger 17 contains at most half the amount of heavy hydrocarbons - having more than two carbon atoms - present in the feed gas.
- the gas stream 20 heated in the exchanger 17, at a temperature of between -40 ° C. and -70 ° C., preferably of the order of -60 ° C., is then partially condensed by means of, for example, a heat exchanger 21.
- a two-phase (gas-liquid) stream 22 (comprising from 20% to 80% molar of gas) is obtained.
- the diphasic current 22 is, after a possible expansion in a valve or a turbine 23, introduced into a phase separator pot 25.
- the liquid phase 29 coming from the phase separator pot 25 is, after a possible expansion in a valve (not shown in the figure), reheated through the heat exchangers 27 and then 21 and finally 2 in order to join the outlet stream 30 of the gas rich in methane produced at the end of the process.
- the outlet stream contains less than 5 mol% of nitrogen.
- the gaseous phase 26 coming from the separator pot 25 is partially condensed in a heat exchanger 27 and then expanded at the outlet of said exchanger 27 by means of a turbine or a valve before being introduced into a distillation column 31.
- the distillation column 31 is a so-called "stripping" column of nitrogen for the purpose of separating the nitrogen from the liquid enriched in output methane, also called denitrogenation column.
- the methane-enriched liquid comprises less than 5 mol% of nitrogen. This is a distillation column joined to a reboiler 32 but does not have an associated condenser system.
- a stream 33 rich in methane in liquid form is extracted.
- This stream 33 contains less than 5 mol% of nitrogen, preferably less than 4%.
- the liquid stream 33 is then mixed with the liquid phase 29 coming from the phase separator pot 25 and follows the same path to the outlet stream 30.
- a portion 32 of the mixed stream containing partly the liquid phase 29 and the liquid 33 and heated through the heat exchanger 27 is recycled to the lower portion 34 of the denitrogenation column 31.
- a nitrogen-rich gas stream 36 at a temperature below -1 10 ° C is produced.
- Said stream 36 rich in nitrogen comprises at least 20 mol% of nitrogen.
- the nitrogen-rich stream 36 is heated through the successive exchangers 27, 21 and then 2. It can also be a single exchanger according to a particular embodiment of the invention. And according to another particular embodiment of the invention, more than three exchangers can be implemented.
- the denitrogenation system B aims to produce a gaseous flow even richer in nitrogen than the stream 37.
- This system B may for example include at least one separator pot and a denitrogenation column. If the nitrogen specification at the outlet of system B is strict (typically ⁇ 100 ppm), it may be necessary to add a cycle compressor, for example a nitrogen compressor, to system B to bring reflux. necessary to obtain nitrogen purity at the top of the B system denazaction column.
- the method that is the subject of the present invention makes it possible to:
- denitrogenation system B if a failure occurs on the denitrogenation system B, it will still be possible to continue the implementation of the process and to produce a large part, typically at least 80%, of the desired products (denitrogenated methane) thanks to denitrogenation system A. Indeed, the proposed solution is to partially integrate the denitrogenation system with the extraction system of products from the "NGL part".
- This partial integration consists in integrating at least one first separator pot following the demethanization column of the "NGL process". From this first separator pot will be recovered, in liquid form, at least a portion of the natural gas product. This product will be denoted at least partially, allowing in certain cases to reach the specification in terms of calorific value of the product.
- a first denitrogenation column can be integrated into the "NGL part", this makes it possible to increase the proportion of product to the specification directly produced from the denitrogenation system.
- NNL part is meant all the steps of the process according to the invention prior to step c).
- a failure of the refrigeration cycle will then stop the denitrogenation but may maintain part of the production of nitrogen-containing natural gas and the production of products from the "NGL part".
- the implementation of the method according to the invention makes it possible, in addition to improving the reliability of the plant, to optimize the total investment cost by optimizing the number of elements constituting the different units of implementation. said process with respect to the flow rate entering each unit.
- the use of at least one less train on the NRU portion than on the NGL portion eg, seven trains for the NGL portion and three trains for the NGL portion.
- NRU part makes it possible, in addition to improving the reliability of the plant, to optimize the total investment cost by optimizing the number of trains with respect to the flow rate entering each unit.
- a train is a processing unit generally comprising a single equipment for each function of the process (a turbine 9, a separator pot 4 ). It can however happen to specifically double one or more equipment within the same train. When the flow is too high it is necessary to use several identical trains, namely several processing units operating in parallel and with the same equipment.
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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)
- Gas Separation By Absorption (AREA)
Abstract
Description
Claims
Priority Applications (4)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
US15/563,117 US20180087833A1 (en) | 2015-04-01 | 2015-10-01 | Process for removing nitrogen from high-flow natural gas |
AU2015388736A AU2015388736B2 (en) | 2015-04-01 | 2015-10-01 | Process for removing nitrogen from high-flow natural gas |
MX2017012611A MX2017012611A (es) | 2015-04-01 | 2015-10-01 | Procedimiento de desnitrogenacion del gas natural de alto caudal. |
EA201792037A EA035250B1 (ru) | 2015-04-01 | 2015-10-01 | Способ удаления азота из быстротекущего природного газа |
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
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FR1552781 | 2015-04-01 | ||
FR1552781A FR3034428B1 (fr) | 2015-04-01 | 2015-04-01 | Procede de desazotation du gaz naturel a haut debit |
Publications (1)
Publication Number | Publication Date |
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WO2016156675A1 true WO2016156675A1 (fr) | 2016-10-06 |
Family
ID=53177676
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
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PCT/FR2015/052632 WO2016156675A1 (fr) | 2015-04-01 | 2015-10-01 | Procédé de déazotation du gaz naturel à haut débit |
Country Status (6)
Country | Link |
---|---|
US (1) | US20180087833A1 (fr) |
AU (1) | AU2015388736B2 (fr) |
EA (1) | EA035250B1 (fr) |
FR (1) | FR3034428B1 (fr) |
MX (1) | MX2017012611A (fr) |
WO (1) | WO2016156675A1 (fr) |
Cited By (1)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
CN117889612A (zh) * | 2024-03-12 | 2024-04-16 | 新疆凯龙清洁能源股份有限公司 | 含氮甲烷气脱氮液化的方法及系统 |
Citations (5)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US4195979A (en) * | 1978-05-12 | 1980-04-01 | Phillips Petroleum Company | Liquefaction of high pressure gas |
US4778498A (en) | 1986-09-24 | 1988-10-18 | Union Carbide Corporation | Process to produce high pressure methane gas |
DE10106484A1 (de) * | 2001-02-13 | 2002-08-14 | Linde Ag | Verfahren zum gleichzeitigen Gewinnen einer Helium- und einer Stickstoff-Reinfraktion |
US20070193303A1 (en) * | 2004-06-18 | 2007-08-23 | Exxonmobil Upstream Research Company | Scalable capacity liquefied natural gas plant |
US20090248174A1 (en) * | 2008-03-28 | 2009-10-01 | Saudi Arabian Oil Company | Control method of refrigeration systems in gas plants with parallel trains |
Family Cites Families (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US4687499A (en) * | 1986-04-01 | 1987-08-18 | Mcdermott International Inc. | Process for separating hydrocarbon gas constituents |
US7234322B2 (en) * | 2004-02-24 | 2007-06-26 | Conocophillips Company | LNG system with warm nitrogen rejection |
DE102008056196A1 (de) * | 2008-11-06 | 2010-05-12 | Linde Ag | Verfahren zum Abtrennen von Stickstoff |
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2015
- 2015-04-01 FR FR1552781A patent/FR3034428B1/fr active Active
- 2015-10-01 AU AU2015388736A patent/AU2015388736B2/en active Active
- 2015-10-01 MX MX2017012611A patent/MX2017012611A/es unknown
- 2015-10-01 WO PCT/FR2015/052632 patent/WO2016156675A1/fr active Application Filing
- 2015-10-01 EA EA201792037A patent/EA035250B1/ru not_active IP Right Cessation
- 2015-10-01 US US15/563,117 patent/US20180087833A1/en not_active Abandoned
Patent Citations (5)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US4195979A (en) * | 1978-05-12 | 1980-04-01 | Phillips Petroleum Company | Liquefaction of high pressure gas |
US4778498A (en) | 1986-09-24 | 1988-10-18 | Union Carbide Corporation | Process to produce high pressure methane gas |
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AU2015388736B2 (en) | 2021-05-13 |
FR3034428A1 (fr) | 2016-10-07 |
EA201792037A1 (ru) | 2017-12-29 |
EA035250B1 (ru) | 2020-05-20 |
US20180087833A1 (en) | 2018-03-29 |
AU2015388736A1 (en) | 2017-11-09 |
FR3034428B1 (fr) | 2020-01-10 |
MX2017012611A (es) | 2018-01-09 |
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