MX2013014870A - Process for liquefaction of natural gas. - Google Patents

Process for liquefaction of natural gas.

Info

Publication number
MX2013014870A
MX2013014870A MX2013014870A MX2013014870A MX2013014870A MX 2013014870 A MX2013014870 A MX 2013014870A MX 2013014870 A MX2013014870 A MX 2013014870A MX 2013014870 A MX2013014870 A MX 2013014870A MX 2013014870 A MX2013014870 A MX 2013014870A
Authority
MX
Mexico
Prior art keywords
gas
heat exchanger
expander
flow
feed
Prior art date
Application number
MX2013014870A
Other languages
Spanish (es)
Other versions
MX346703B (en
Inventor
Anthony Dwight Maunder
Geoffrey Frederick Skinner
Original Assignee
Gasconsult Ltd
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 Gasconsult Ltd filed Critical Gasconsult Ltd
Publication of MX2013014870A publication Critical patent/MX2013014870A/en
Publication of MX346703B publication Critical patent/MX346703B/en

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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
    • F25J5/00—Arrangements of cold exchangers or cold accumulators in separation or liquefaction plants
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/0002—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the fluid to be liquefied
    • F25J1/0022—Hydrocarbons, e.g. natural gas
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
    • F25J1/0032—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration"
    • F25J1/0035—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration" by gas expansion with extraction of work
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
    • F25J1/0032—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration"
    • F25J1/0035—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration" by gas expansion with extraction of work
    • F25J1/0037—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration" by gas expansion with extraction of work of a return 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
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
    • F25J1/0032—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration"
    • F25J1/004—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration" by flash gas recovery
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
    • F25J1/0201—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using only internal refrigeration means, i.e. without external refrigeration
    • F25J1/0202—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using only internal refrigeration means, i.e. without external refrigeration in a quasi-closed internal refrigeration loop
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
    • F25J1/0211—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using a multi-component refrigerant [MCR] fluid in a closed vapor compression cycle
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
    • F25J1/0225—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using other external refrigeration means not provided before, e.g. heat driven absorption chillers
    • F25J1/0227—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using other external refrigeration means not provided before, e.g. heat driven absorption chillers within a refrigeration cascade
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
    • F25J1/0228—Coupling of the liquefaction unit to other units or processes, so-called integrated processes
    • F25J1/0229—Integration with a unit for using hydrocarbons, e.g. consuming hydrocarbons as feed stock
    • F25J1/023—Integration with a unit for using hydrocarbons, e.g. consuming hydrocarbons as feed stock for the combustion as fuels, i.e. integration with the fuel gas 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
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
    • F25J1/0228—Coupling of the liquefaction unit to other units or processes, so-called integrated processes
    • F25J1/0235—Heat exchange integration
    • F25J1/0242—Waste heat recovery, e.g. from heat of compression
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
    • F25J1/0243—Start-up or control of the process; Details of the apparatus used; Details of the refrigerant compression system used
    • F25J1/0244—Operation; Control and regulation; Instrumentation
    • F25J1/0254—Operation; Control and regulation; Instrumentation controlling particular process parameter, e.g. pressure, temperature
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
    • F25J1/0243—Start-up or control of the process; Details of the apparatus used; Details of the refrigerant compression system used
    • F25J1/0279—Compression of refrigerant or internal recycle fluid, e.g. kind of compressor, accumulator, suction drum etc.
    • F25J1/0281—Compression of refrigerant or internal recycle fluid, e.g. kind of compressor, accumulator, suction drum etc. characterised by the type of prime driver, e.g. hot gas expander
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
    • F25J1/0243—Start-up or control of the process; Details of the apparatus used; Details of the refrigerant compression system used
    • F25J1/0279—Compression of refrigerant or internal recycle fluid, e.g. kind of compressor, accumulator, suction drum etc.
    • F25J1/0281—Compression of refrigerant or internal recycle fluid, e.g. kind of compressor, accumulator, suction drum etc. characterised by the type of prime driver, e.g. hot gas expander
    • F25J1/0283—Gas turbine as the prime mechanical driver
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2220/00—Processes or apparatus involving steps for the removal of impurities
    • F25J2220/60—Separating impurities from natural gas, e.g. mercury, cyclic hydrocarbons
    • F25J2220/62—Separating low boiling components, e.g. He, H2, N2, Air
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2220/00—Processes or apparatus involving steps for the removal of impurities
    • F25J2220/60—Separating impurities from natural gas, e.g. mercury, cyclic hydrocarbons
    • F25J2220/64—Separating heavy hydrocarbons, e.g. NGL, LPG, C4+ hydrocarbons or heavy condensates in general
    • 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
    • F25J2240/80—Hot exhaust gas turbine combustion engine
    • F25J2240/82—Hot exhaust gas turbine combustion engine with waste heat recovery, e.g. in a combined cycle, i.e. for generating steam used in a Rankine cycle
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2270/00—Refrigeration techniques used
    • F25J2270/04—Internal refrigeration with work-producing gas expansion loop
    • F25J2270/06—Internal refrigeration with work-producing gas expansion loop with multiple gas expansion loops
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2270/00—Refrigeration techniques used
    • F25J2270/90—External refrigeration, e.g. conventional closed-loop mechanical refrigeration unit using Freon or NH3, unspecified external refrigeration
    • F25J2270/906—External refrigeration, e.g. conventional closed-loop mechanical refrigeration unit using Freon or NH3, unspecified external refrigeration by heat driven absorption chillers

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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)
  • Combustion & Propulsion (AREA)
  • Separation By Low-Temperature Treatments (AREA)

Abstract

A process comprising: cooling natural gas with a heat exchanger and a first expander. The heat exchanger cools the feed natural gas to temperature higher than the outlet temperature of the expander, reheating the expander outlet stream in a first cold passage of the heat exchanger to slightly below the temperature of the feed natural gas to the heat exchanger, passing the cold outlet stream from the heat exchanger into a second expander wherein it is partly liquefied, separating the outlet stream of second expander into liquid and vapour fractions, collecting the liquid fraction for use as LNG product, reheating the vapour fraction in a second cold side passage of the heat exchanger to substantially the same temperature as the temperature of the feed natural gas to the heat exchanger, recycling the reheated vapour fraction partly as feed to the first expander and partly as feed to the heat exchanger.

Description

PROCESS FOR THE LIQUIDATION OF NATURAL GAS Field of the invention The present invention relates to a method for liquefying gas rich in methane and, more specifically but not exclusively, it refers to a method for producing liquefied natural gas (LNG).
BACKGROUND OF THE INVENTION The liquefaction of natural gas can be achieved in a practical way by: the evaporation of liquid refrigerants the work of · expansion of gases in expansion machines (expanders).
The evaporation of liquid refrigerants generates the lowest energy requirements and is the basis of the LNG processes of mixed refrigerant and cascade widely used.
LNG installations based on expanders are simple, compact, lightweight and can prevent the import / preparation / storage of liquid refrigerants. These characteristics are attractive for small-scale applications, particularly in the open sea, where, for safety reasons, a low total amount of hydrocarbons is desired. However, processes with expanders have certain drawbacks: until recently, limited capacity and experience with the expanders Higher energy requirements Higher internal gas flow that requires a larger diameter, etc.
With most expander-based processes, the operating fluid (usually nitrogen) remains in the gas phase at the expander outlet.
By partially liquefying the feed gas itself in an expander and having a two-phase discharge flow, the internal gas flows (recirculation) can be reduced and the energy requirements reduced.
The production of LNG in a liquefaction expander is not a new idea (U.S. Patent No. 2,903,858 - Bocquet).
The present inventors previously described a process (Patent of GB 2393504B, U.S. Patent 7,234,321) with potentially low energy requirements, where a liquefaction expander is combined with a precooling circuit containing a simple mixed refrigerant generated from of the natural gas of feeding.
Other recent presentations include pre-cooling by means of a parallel / recirculation gas expander and then a liquefaction expander: WO 01/44735 (Minta et al.) Describes the production of pressurized liquid natural gas (PGNL, for its English acronym) at -112 ° C from the compressed feed gas to a high pressure "above 1600 psia".
US 2006/0213222 (Whitesell) describes the production of LNG from a feed gas that enters the process at a pressure of "between approximately 1500 psig and approximately 3500 psig" or that is compressed in the process up to said pressure .
Compendium of the invention Related to the two patents mentioned above, an inventive step of the present application consists in the identification of operating conditions for the two expanders (the pre-cooling expander and the liquefaction expander) which allows the practical production of LNG at atmospheric pressure at approximately -161 ° C. In addition, a feed gas at a very high pressure is no longer required, which is characteristic of the patents mentioned above.
This results in a simplified process with improved thermal efficiency having a wide range of potential applications where the raw feed gas has a pressure of only 40 bar (4 MPa).
The present invention facilitates the production of LNG from smaller gas fields, particularly in the open sea, due to its simple flow scheme, low energy consumption and non-dependence on storage and utilization. of liquid refrigerants. The liquefaction process itself generally does not require process columns, for example, for the preparation of the refrigerant, which may be more difficult to operate in operating conditions of this type.
Description of the invention According to the invention, a process for the liquefaction of natural gas or other gases rich in methane is provided. The feed gas, normally at a pressure of between 40 (4 MPa) and 100 bar (10 MPa), is liquefied to give an LNG product at approx.1 bar (0.1 MPa) / - 161 ° C through the configuration of the plant based on an expander described above and comprising: cooling the feed gas and the recirculation gas (mentioned above) in a first step by means of a first heat exchanger and in a first work expander; wherein the heat exchanger has an outlet temperature in the range of -50 ° C to -80 ° C, preferably -60 ° C to -70 ° C; where the expander has a lower outlet temperature than that of the heat exchanger; where the expander has its superheated output flow in a cold conduit of said heat exchanger and then it is recompressed to form part of the recirculation gas mentioned above. pass part of the cooled out flow of said first heat exchanger by a hot conduit in a second heat exchanger, where it is essentially condensed, and partly by a second work expander, where said second expander has a lower outlet temperature than the cold outlet of the second heat exchanger, where the outflow of the second expander contains a significant amount of liquid (usually between 10-15% by weight); where the outlet expander is separated into a gaseous fraction and a liquid fraction; wherein the gas fraction is reheated in the cold conduits in said first and second heat exchangers; it is then compressed again and returned to the process inlet as part of the recirculation gas mentioned above. reducing the pressure of the aforementioned separate liquid and condensed liquid from the hot conduit of the second heat exchanger (both typically with an approximate value of -120 ° C) to approximately atmospheric pressure; reheating the evaporated gas that is released in additional cold ducts in the previous heat exchangers; eliminate the liquid for use as an LNG product.
It has been observed that the lower energy requirement of the compression of the recirculation gas is that which results from concentrating the extraction of the mechanical work in the pressure range above 10 bar (1 MPa) approx. at the exit of the second expander. An advantage of this is that the outlet pressures of the two expanders can be balanced to approximately 10 bar (1 MPa), which reduces the first heat exchanger to a three-pipe configuration.
While most of the existing LNG production depends on the evaporation of liquid refrigerants to cool and condense the natural gas so that an LNG product is formed in a heat exchanger, this invention comprises a liquefaction process with energy requirements. Moderates in which the expansion work of the feed gas itself provides, for the most part, the necessary cooling. Therefore, cryogenic liquid refrigerants or other secondary working fluids such as nitrogen are not needed. In this way, the energy is extracted at a temperature level below which results in an improved thermodynamic efficiency. As a result, a significant proportion of the LNG is formed directly in an expander that extracts the work, in addition to that formed by condensation in an exchanger to which the overheating of the cold gas of said work expander cools.
Description of the preferred embodiments The invention will now be described with reference to the accompanying drawings in which the Figures 1 and 2 represent flow diagrams illustrating processes according to the invention.
Figure 1 shows the operating characteristics of the invention. The exact flow diagram will depend on the specification of the feed gas, but will generally contain these basic elements. In all the sites of this application where pressures are indicated as "bar" these are absolute bars.
The natural feed gas (Flow 1) is passed through a pre-treatment stage A in which the components that would otherwise solidify or interfere with the subsequent liquefaction process, such as CO2, H2S, water vapor and mercury vapor, are eliminated as necessary to obtain maximum conventional and appropriate concentrations in the pre-treated gas (Flow 2). Flow 2 is mixed with part (Flow 4) of the recirculation gas (Flow 3) to form Flow 6, which is passed through a conduit of heat exchanger B, and leaves it as Flow 7 at a temperature normally comprised in the range from -20 ° C to -60 ° C, preferably from -30 ° C to -50 ° C. This temperature is normally low enough to condense enough LNG and meet the requirements of the final LNG product. Any hydrocarbons condensed in separator C are removed in the form of Flow 8. The output vapor of C (Flow 9) is further cooled in a conduit of heat exchanger D, and leaves it as Flow 10 at a temperature in the range of -50 ° C to -80 ° C, preferably -60 ° C to -70 ° C. The remaining part of the recirculating gas (Flow 5) is cooled in the gas expander E having an Outflow 11 with a temperature lower than that of the temperature of the Flow 10.
Optionally, all the pre-treated feed gas, or part of it, can leave pre-treatment step A through Flow 2a to join Flow 3 of the recirculation gas before the point at which it is divided into Flows 4 and 5. This option may be convenient when Flow 1 of the natural feed gas has only a small content of heavy hydrocarbons. In this type of case, the pre-treated feed gas can be mixed with the entire recirculation gas, and then the resulting mixture divided to supply the heat exchanger B by Flow 6 and the gas expander E by Flow 5.
The pressure of Flow 11 will normally be about 15 bar (1.5 MPa). The Flow 11 enters a first cold conduit of the heat exchanger D, and leaves it as Flow 12, which then passes through a first cold conduit in the heat exchanger B, and exits (Flow 13) at a temperature just below the Flow temperature 6. The ratio between the flow rate of Flow 4 and the flow rate of Flow 5 is controlled so that the temperature difference between the hot and cold sides composed of the heat exchangers B and D is kept substantially uniform as length of its lengths.
A large part of Flow 10 (Flow 14) is then passed through a second gas expander F, from which it emerges as Flow 15 at a pressure of between 3 bar (0.3 MPa) and 20 bar (2 MPa), preferably between 5 bar (0.5 MPa) and 15 bar (1.5 MPa) and in a partially liquefied state. The Flow 15 then enters the vapor-liquid separator G. The liquid phase of the separator G (Flow 16) is then normally reduced in a pressure reducing device H such as a valve or a turbine. The outflow of H (Flow 17), which is normally at atmospheric pressure, or close to it, is supplied to Tank I of LNG. If it is desired to reduce the nitrogen content of the LNG product, a conventional nitrogen separation column (not shown) can be used, which normally uses the sensible heat of Flow 16 for reheating to boiling.
Optionally and preferably, a part of the Flow 10 circulates as Flow 23 through a conduit of the hot side in a heat exchanger J, where it is liquefied by an indirect heat exchange with the steam of the separator G (Flow 18), and emerges as Flow 24. Normally, the pressure of the latter is then reduced by means of a pressure reducing device K, such as a valve or a turbine. The outflow of K is well channeled to a vapor-liquid separator G, which is shown with a dotted line as Flow 25a, or preferably as Flow 25b to tank I of LNG. This second option helps reduce the accumulation of nitrogen in the recirculation gas. The Flow 18, which has been heated in a first cold conduit of the heat exchanger J, emerges as Flow 19. It is then further heated in a second cold conduit of the heat exchanger D, and emerges as Flow 20, which is heated further then in a second cold conduit of heat exchanger B, and emerges as Flow 21 at a temperature slightly lower than the temperature of Flow 6.
Flows 13 and 21 are compressed in the recirculation compressor N, whose outlet flow 34 is normally cooled with cooling water in a refrigerator O. The compressor N can consist of more than one stage with intermediate coolers. Flows 13 and 21 will not have the same pressure and can enter different stages of the compressor. The outflow of O forms the Flow 3 of the recirculation gas mentioned above.
The instantaneous vaporization of Flow 16 through H and the instantaneous vaporization of Flow 24 through K results in the evolution of vapor comprising mainly methane together with most of the nitrogen content of the feed gas. Typically, this vapor (Flow 26), optionally combined with the evaporated vapor portion resulting from the heat loss to tank I, is heated in a first cold conduit in a heat exchanger J to form Flow 27, below in a second cold conduit in a heat exchanger D to obtain Flow 28 and finally in a third conduit cooled in heat exchanger B, and emerges as Flow 29 at a temperature slightly lower than the temperature of Flow 6. It can be provided a conventional booster compressor (also not shown) in Flow 26 to ensure that Flow 29 pressure does not fall below atmospheric pressure. Flow 29 can normally be used as fuel gas.
All Flow 29, or part thereof, (Flow 30) can optionally be compressed for its return to recirculation gas in a low pressure compressor L, which leaves as Flow 31. This flow is cooled in an M refrigerant, whose flow outlet (Flow 32) joins Flow 21 to form Flow 22, which then enters the suction of recirculation compressor N instead of Flow 21 only if this option is not used. An additional option it consists in removing the recirculating gas (Flow 33) from the compressor N at a convenient point normally for use as a gas turbine fuel. It may be convenient to use Flow 29 or Flow 33 as a separation gas for the regeneration of adsorbents in the pre-treatment stage A, before their final combustion as fuels.
Figure 2 shows a preferred embodiment of the invention in which the expanders E and F have essentially the same outlet pressure of between 3 bar (0.3 MPa) and 20 bar (2 MPa), preferably between 5 bar (0.5 MPa) and 15 bar (1.5 MPa). The output flow of the expander E (Flow 11) is then combined with the Flow 19 to form the Flow 19a, which enters the heat exchanger D instead of the Flow 19 in Fig. 1. The heat exchangers B and D later have only three ducts, which simplifies the construction of the exchanger and the operation of the plant.
Although in most applications it is expected that Flows 2 and 3 have temperatures close to room temperature, it may be convenient to cool below this level. It is feasible to cool these flows, and optionally the outflows of the intermediate refrigerants and the subsequent refrigerants of the compressor, by means of a mechanical refrigeration cycle or by means of of an absorption refrigeration system, which normally uses lithium bromide (LiBr), which can receive its heat supply from the exhaust gas of a gas turbine, gas machine or combined cycle or any other suitable element.
It is noted that in relation to this date, the best method known to the applicant to carry out the aforementioned invention, is that which is clear from the present description of the invention.

Claims (8)

1. A process for the liquefaction of natural gas or other gases rich in methane, comprising: - cooling the natural feed gas (9) to a pressure between 40 and 100 bar (between 4 and 10 mPa) up to a temperature between -50 ° C and -80 ° C by means of a heat exchanger (D) and a first gas expander (E), where the heat exchanger receives the natural gas feed (9) and has an outlet temperature higher than the exit temperature of the expander; reheating the output flow of the expander (11) in a first cold conduit of said heat exchanger (D) to just below the inlet temperature of the natural gas supply (9) of said heat exchanger, compress and recielar; - passing the entire cold outlet flow (14) of said heat exchanger (D), or part thereof, through a second expander (F) in which it is partially liquefied; - separating the outflow (15) of said second expander (F) into liquid and gaseous fractions; - collect the liquid fractions (16) for use as LNG product, - reheating the gas fraction (19) in a second conduit of the cold side of said heat exchanger (D) to just below the inlet temperature of the natural gas feed (9) of said heat exchanger; - recieling said reheated gas fraction after compression, in part (5), in said first expander and, in part (4), in said heat exchanger; CHARACTERIZED BY the outflow (15) of the second expander (F) is at a pressure between 5 and 15 bar (0.5 and 1.5 MPa).
2. A process as claimed in Claim 1 in which the heat exchanger receives all of the natural feed gas.
3. A process as claimed in Claim 1 in which the heat exchanger receives a large part, at least 30%, of the natural feed gas.
4. A process as claimed in any preceding claim in which the natural feed gas is cooled to a temperature between -60 ° C and -70 ° C.
5. A modification of the claimed process in any preceding claim wherein said first and second gas expanders (E, F) have essentially the same outlet pressure of between 5 bar and 15 bar (0.5 and 1.5 MPa), and the outflows of both expanders are combined (19a) before final reheating, compression and recirculation.
6. A process as claimed in any preceding claim wherein all of the recirculation and / or feed and / or discharge flows of the compressor, or any part thereof, are cooled, typically by the use of refrigeration cycles by absorption, such as with lithium bromide (LiBr).
7. A process as claimed in any preceding claim in which the heat demand for an absorption cooling system is supplied by the heat of the exhaust gases of a gas turbine or gas machine, such as turbines or gas machines. gas which can be used to supply power to the compressors of the process.
8. A process as claimed in any preceding claim wherein this type of cooling of the feed and / or recirculation flows is combined with the removal of carbon dioxide and / or other impurities from the feed gas.
MX2013014870A 2011-06-15 2012-06-11 Process for liquefaction of natural gas. MX346703B (en)

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AU2012270148B2 (en) 2017-12-07
JP2014522477A (en) 2014-09-04
JP5984192B2 (en) 2016-09-06
GB2486036A (en) 2012-06-06
KR101820560B1 (en) 2018-01-19
EP2721358A2 (en) 2014-04-23
AU2012270148A1 (en) 2013-11-28
CA2836628A1 (en) 2012-12-20
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US20140083132A1 (en) 2014-03-27
MY172653A (en) 2019-12-09
GB2486036B (en) 2012-11-07
GB201110096D0 (en) 2011-07-27
WO2012172281A3 (en) 2013-12-05
WO2012172281A4 (en) 2014-01-09
MX346703B (en) 2017-03-28
WO2012172281A2 (en) 2012-12-20
CA2836628C (en) 2019-06-25

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