CN115854654A - CRS (Central Standard System) technology-based nitrogen expansion, liquefaction and decarburization system and method - Google Patents
CRS (Central Standard System) technology-based nitrogen expansion, liquefaction and decarburization system and method Download PDFInfo
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- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 title claims abstract description 79
- 229910052757 nitrogen Inorganic materials 0.000 title claims abstract description 39
- 238000000034 method Methods 0.000 title claims abstract description 29
- 238000005261 decarburization Methods 0.000 title claims abstract description 26
- 238000005516 engineering process Methods 0.000 title claims abstract description 20
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims abstract description 90
- 239000003345 natural gas Substances 0.000 claims abstract description 45
- 238000000926 separation method Methods 0.000 claims abstract description 20
- 238000009833 condensation Methods 0.000 claims abstract description 16
- 230000005494 condensation Effects 0.000 claims abstract description 16
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims abstract description 12
- 239000002245 particle Substances 0.000 claims abstract description 12
- 238000005262 decarbonization Methods 0.000 claims abstract description 7
- 229910002092 carbon dioxide Inorganic materials 0.000 claims abstract description 6
- 239000001569 carbon dioxide Substances 0.000 claims abstract description 6
- 239000007788 liquid Substances 0.000 claims description 13
- 239000007789 gas Substances 0.000 claims description 11
- 238000001816 cooling Methods 0.000 claims description 8
- 230000006835 compression Effects 0.000 claims description 7
- 238000007906 compression Methods 0.000 claims description 7
- 230000008569 process Effects 0.000 abstract description 10
- 230000008901 benefit Effects 0.000 abstract description 5
- 238000010521 absorption reaction Methods 0.000 description 3
- 230000008859 change Effects 0.000 description 3
- 238000005265 energy consumption Methods 0.000 description 3
- 239000012528 membrane Substances 0.000 description 3
- 230000009467 reduction Effects 0.000 description 3
- 239000007787 solid Substances 0.000 description 3
- 238000001179 sorption measurement Methods 0.000 description 3
- 238000003860 storage Methods 0.000 description 3
- 238000003795 desorption Methods 0.000 description 2
- 238000007667 floating Methods 0.000 description 2
- 238000010438 heat treatment Methods 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 239000002250 absorbent Substances 0.000 description 1
- 230000002745 absorbent Effects 0.000 description 1
- 230000009471 action Effects 0.000 description 1
- 239000003463 adsorbent Substances 0.000 description 1
- 230000007797 corrosion Effects 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 229910001873 dinitrogen Inorganic materials 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000011156 evaluation Methods 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 239000003208 petroleum Substances 0.000 description 1
- 239000003209 petroleum derivative Substances 0.000 description 1
- 238000012545 processing Methods 0.000 description 1
- 238000011160 research Methods 0.000 description 1
- 239000002904 solvent Substances 0.000 description 1
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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
- 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
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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
- 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
- F25J1/0027—Oxides of carbon, e.g. CO2
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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
- 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
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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
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
- F25J1/0047—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using an "external" refrigerant stream in a closed vapor compression cycle
- F25J1/005—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using an "external" refrigerant stream in a closed vapor compression cycle by expansion of a gaseous refrigerant stream with extraction of work
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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
- 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
- F25J1/0203—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 single-component refrigerant [SCR] fluid in a closed vapor compression cycle
- F25J1/0204—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 single-component refrigerant [SCR] fluid in a closed vapor compression cycle as a single flow SCR cycle
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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
- 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
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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
- 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
- F25J1/0257—Construction and layout of liquefaction equipments, e.g. valves, machines
- F25J1/0275—Construction and layout of liquefaction equipments, e.g. valves, machines adapted for special use of the liquefaction unit, e.g. portable or transportable devices
- F25J1/0277—Offshore use, e.g. during shipping
- F25J1/0278—Unit being stationary, e.g. on floating barge or fixed platform
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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
- F25J2205/10—Processes or apparatus using other separation and/or other processing means using combined expansion and separation, e.g. in a vortex tube, "Ranque tube" or a "cyclonic fluid separator", i.e. combination of an isentropic nozzle and a cyclonic separator; Centrifugal separation
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- 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
- F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
- F25J2230/08—Cold compressor, i.e. suction of the gas at cryogenic temperature and generally without afterstage-cooler
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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
- F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
- F25J2230/30—Compression of the feed stream
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Abstract
The invention discloses a CRS (China railway standard) technology-based nitrogen expansion, liquefaction and decarburization system, which is characterized by comprising a nitrogen expansion system and a natural gas condensation and decarburization system; the nitrogen expansion system comprises a nitrogen pipeline, the nitrogen pipeline is sequentially connected with a first compressor, a first cooler, a second compressor and a second cooler, and an outlet of the second cooler is connected with the first plate type heat exchanger, the first expander, the second plate type heat exchanger and the first plate type heat exchanger; the natural gas condensation decarbonization system comprises a CO-containing system 2 Of natural gas pipelines containing CO 2 The natural gas pipeline is sequentially connected with a first plate heat exchanger, a second expansion machine, a cyclone particle separation device for separating carbon dioxide, a third compressor and a second plate heat exchanger; and the natural gas condensation decarburization system and the nitrogen expansion system are coupled through the first plate heat exchanger and the second plate heat exchanger. The system has the advantages of small occupied area, simple equipment and low cost, and accords with the offshore FPLNG liquefaction process.
Description
Technical Field
The invention belongs to the field of gas treatment, and particularly relates to a nitrogen expansion, liquefaction and decarburization system and method based on a CRS (Central processing Unit) technology.
Background
The information in this background section is only for enhancement of understanding of the general background of the invention and is not necessarily to be construed as an admission or any form of suggestion that this information forms the prior art that is already known to a person of ordinary skill in the art.
The marine natural gas resources in China are rich, and according to the third petroleum resource evaluation result, the marine natural gas resources account for 16 billion cubic meters, account for 30 percent of the total amount of the whole country, and are mainly distributed in the Bohai sea and the south sea; for some gas sources, if the traditional modes of ocean fixed platforms or submarine pipelines and the like are adopted, most gas fields cannot be put into exploitation due to cost or technical limitation; in recent years, floating Production Storage and Offloading (FLNG, also known as FPSO-LNG) devices have been proposed in the oceanographic engineering industry, which integrate the liquefaction, storage, loading and unloading of offshore natural gas/petroleum gas, and utilize the easy transportation and Storage characteristics of LNG to reduce the exploitation cost of marginal small gas fields, deep sea natural gas and associated gas resources and realize the development of marginal benefit resources.
At present, the developed decarburization technologies mainly include cryogenic rectification, solvent absorption, adsorption and membrane separation; the application of cryogenic rectification technology in the field of natural gas decarburization is mainly concentrated abroad and is commonly used for separating and recovering CO in associated gas of oil fields 2 However, the application of this aspect in China is rarely reported; physical absorbent with CO 2 Has no obvious chemical action, and has low desorption energy consumption, but the CO and the carbon dioxide are mixed 2 The weaker affinity between the two is also responsible for CO 2 The removal rate is low; the chemical absorption method has high absorption efficiency and good selectivity, but still has many problems to be optimized, such as strong corrosion to equipment, high desorption energy consumption and the like; the research and application of the PSA method in the process and the high-performance adsorbent are advanced to a certain extent, but the large-scale application of the PSA method in the field of natural gas decarburization is still in an exploration stage; moreover, the adsorption process always has the problems of flow dead zone, uneven adsorption and the like; the membrane separation process does not occurPhase change has certain advantages in the aspects of energy consumption, equipment floor area, cost and the like, and a flexible adjustable series process also endows the phase change with greater operation flexibility, but the technology also has the problem of poor stability of a membrane material; storing and transporting (PLNG) at a higher pressure (1-2 MPa) after natural gas liquefaction, wherein the corresponding condensation temperature is obviously increased to-100-120 ℃ from-160 ℃ in the traditional process; CO due to the increase of the condensation temperature 2 The solubility in LNG is also remarkably improved from about 0.01 percent to 1.00 to 3.30 percent, so that the adoption of a floating pressure liquefaction technology is a good choice; the method has the defects of large heat exchange area and low liquefaction rate in the common expansion liquefaction process, can solve the problem by combining the expansion liquefaction process with the pressurized liquefaction process, and adopts a gas-solid separation mode to easily generate solid CO in the prior art for removing the carbon dioxide 2 Thereby plugging the pipe.
Disclosure of Invention
In order to solve the problems in the prior art, the invention aims to provide a nitrogen expansion, liquefaction and decarburization system and method based on a CRS technology; CO removal from natural gas 2 A Condensed Rotational Separation (CRS) technique, using a heat exchanger and an expander to enrich the CO 2 Cooling natural gas to promote CO in the natural gas 2 Condensed phase change to generate liquid drops, and high content of CO 2 The liquid-gas mixture of the droplets is introduced into a cyclone particle separator (RPS), and the droplets are separated by centrifugal force generated by high-speed rotation in a microchannel of the RPS, and liquid CO is introduced into the microchannel 2 The natural gas is pressurized by a compressor and then enters a downstream flow after being purified.
In a first aspect of the invention, a nitrogen expansion, liquefaction and decarburization system based on CRS technology is provided, which comprises a natural gas condensation and decarburization system and a nitrogen expansion system;
the nitrogen expansion system comprises a nitrogen pipeline, the nitrogen pipeline is sequentially connected with a first compressor, a first cooler, a second compressor and a second cooler, an outlet of the second cooler is connected with a first heat flow inlet of the first plate heat exchanger, a first heat flow outlet of the first plate heat exchanger is connected with an inlet of the first expander, an outlet of the first expander is connected with a cold flow inlet of the second plate heat exchanger, and a cold flow outlet of the second plate heat exchanger is connected with a cold flow of the first plate heat exchanger;
the natural gas condensation decarbonization system comprises a CO-containing system 2 Of natural gas pipelines containing CO 2 The natural gas pipeline is connected with a second heat flow inlet of the first plate heat exchanger, a second heat flow outlet of the heat exchanger is sequentially connected with a second expander, a cyclone particle separation device for separating carbon dioxide and a third compressor, and an outlet of the third compressor is connected with the second heat flow inlet of the second plate heat exchanger;
and the natural gas condensation decarburization system and the nitrogen expansion system are coupled through the first plate heat exchanger and the second plate heat exchanger.
In a second aspect of the present invention, a method for expanding, liquefying and decarbonizing nitrogen based on a CRS technology is provided, wherein the method comprises:
containing CO 2 The natural gas is condensed and liquefied through the first plate heat exchanger and the second expander in sequence, then is subjected to gas-liquid separation through the cyclone particle separation device, the separated gas phase enters a third compressor for compression, and finally is condensed and liquefied through the second plate heat exchanger;
the nitrogen is subjected to secondary compression to increase the pressure, is subjected to secondary cooler to reduce the temperature, enters the first plate heat exchanger to be further cooled, and cooled N 2 At the time of pressure reduction through the expander, N 2 The natural gas enters the first plate heat exchanger for further deep cooling decarburization after the temperature is reduced, and finally enters the first plate heat exchanger for heat exchange, so that circulation is realized.
One or more technical solutions provided in the embodiments of the present invention have at least the following technical effects or advantages:
(1) The natural gas adopts a pressurized liquefaction process, so that CO can be greatly increased 2 Solubility of (C), reduction of power consumption, CO 2 The content of the LNG is below 0.5 percent, the LNG can be dissolved in the LNG, and the pretreatment for removing CO is not needed 2 ；
(2) The method has the advantages of small occupied area, simple equipment and lower cost, and accords with the offshore FPLNG liquefaction process;
(3) The invention adopts a gas-liquid separation mode, effectively prevents solid CO 2 And the pipeline is prevented from being blocked.
Drawings
The accompanying drawings, which are incorporated in and constitute a part of this application, illustrate embodiments of the application and, together with the description, serve to explain the application and are not intended to limit the application.
FIG. 1 is a schematic diagram of the control system of the present invention;
in fig. 1: 1-a first compressor, 2-a first cooler, 3-a second compressor, 4-a second cooler, 5-a first plate heat exchanger, 6-a first expander, 7-a second plate heat exchanger, 8-a second expander, 9-a cyclone particle separation device and 10-a third compressor; r-round represents N 2 And circulating is carried out.
Detailed Description
It is to be understood that the following detailed description is exemplary and is intended to provide further explanation of the invention as claimed. Unless defined otherwise, all technical and scientific terms used herein have the same meaning as commonly understood by one of ordinary skill in the art to which this invention belongs.
It is noted that the terminology used herein is for the purpose of describing particular embodiments only and is not intended to be limiting of example embodiments according to the present application. As used herein, the singular forms "a", "an" and "the" are intended to include the plural forms as well, and it should be understood that when the terms "comprises" and/or "comprising" are used in this specification, they specify the presence of stated features, steps, operations, devices, components, and/or combinations thereof, unless the context clearly indicates otherwise.
Specifically, the invention is realized by the following technical scheme:
in a first aspect of the invention, a nitrogen expansion, liquefaction and decarburization system based on CRS technology is provided, which comprises a natural gas condensation and decarburization system and a nitrogen expansion system;
the nitrogen expansion system comprises a nitrogen pipeline, the nitrogen pipeline is sequentially connected with a first compressor, a first cooler, a second compressor and a second cooler, an outlet of the second cooler is connected with a first heat flow inlet of the first plate heat exchanger, a first heat flow outlet of the first plate heat exchanger is connected with an inlet of the first expander, an outlet of the first expander is connected with a cold flow inlet of the second plate heat exchanger, and a cold flow outlet of the second plate heat exchanger is connected with a cold flow of the first plate heat exchanger;
the natural gas condensation decarbonization system comprises a CO-containing system 2 Natural gas pipeline of (2), containing CO 2 The natural gas pipeline is connected with a second heat flow inlet of the first plate heat exchanger, a second heat flow outlet of the heat exchanger is sequentially connected with a second expander, a cyclone particle separation device for separating carbon dioxide and a third compressor, and an outlet of the third compressor is connected with the second heat flow inlet of the second plate heat exchanger;
and the natural gas condensation decarburization system and the nitrogen expansion system are coupled through the first plate heat exchanger and the second plate heat exchanger.
In some embodiments of the invention, the cold flow outlet of the first plate heat exchanger is connected to the first compressor.
In a second aspect of the present invention, a nitrogen expansion, liquefaction and decarburization method based on CRS technology is provided, where the method includes:
containing CO 2 The natural gas is condensed and liquefied through the first plate heat exchanger and the second expander in sequence, then is subjected to gas-liquid separation through the cyclone particle separation device, the separated gas phase enters a third compressor for compression, and finally is condensed and liquefied through the second plate heat exchanger;
the nitrogen is subjected to secondary compression to increase the pressure, is subjected to secondary cooler to reduce the temperature, enters the first plate heat exchanger to be further cooled, and cooled N 2 At the time of pressure reduction through the expander, N 2 The natural gas enters the first plate heat exchanger for further deep cooling decarburization after the temperature is reduced, and finally enters the first plate heat exchanger for heat exchange, so that circulation is realized.
In some embodiments of the invention, the first plate heat exchanger N 2 The cold flow is respectively connected with N of the first heat flow entering the first plate heat exchanger 2 Second heat flow into the first plate heat exchanger containing CO 2 Is subjected to heat exchange.
Further, N enters the first plate heat exchanger for heat exchange 2 And entering a first compressor for circulation.
Further, a swirling particle separator (RPS) separates condensed liquid droplets by centrifugal force generated by high-speed rotation in a microchannel of the RPS, and liquid CO 2 The purified natural gas is pressurized by a compressor and then enters a downstream flow.
Further, the liquid obtained by condensation and liquefaction through the second plate heat exchanger is decarbonized LNG.
The technical solution of the present application will be described below with specific examples.
Example 1
Natural gas: CO-containing at 50 ℃ 2 And the natural gas is continuously condensed and cooled by the first plate heat exchanger, the temperature is reduced to minus 2 ℃, the natural gas is expanded to 850kPa by the second expander, the temperature is reduced to minus 44.08 ℃, gas-liquid separation is carried out by the cyclone particle separation device, the separated gas phase enters a third compressor for compression, the pressure is increased to 1.364MPa, and then enters the second plate heat exchanger for heat exchange and cooling, and the temperature is reduced to minus 115 ℃.
Nitrogen gas: n at 5.061 ℃ under 108kPa 2 Compressing with a first compressor to 300kPa, heating to 172.7 deg.C, cooling with a first condenser to 30 deg.C, compressing with a second compressor to 800kPa, heating to 163.9 deg.C, cooling with a second condenser to 20 deg.C, cooling with a first plate heat exchanger to-66 deg.C, and condensing to obtain N 2 The temperature is expanded to 113kPa, the temperature is reduced to-134.6 ℃, the natural gas enters a second plate heat exchanger for heat exchange, the temperature is increased to-90.84 ℃, and finally the natural gas enters a first plate heat exchanger for heat exchange, the temperature is increased to 5.061 ℃, and the circulation is carried out.
The above description is only a preferred embodiment of the present invention and is not intended to limit the present invention, and various modifications and changes may be made by those skilled in the art. Any modification, equivalent replacement, or improvement made within the spirit and principle of the present invention should be included in the protection scope of the present invention.
Claims (7)
1. A nitrogen expansion, liquefaction and decarburization system based on a CRS technology is characterized by comprising a nitrogen expansion system and a natural gas condensation and decarburization system;
the nitrogen expansion system comprises a nitrogen pipeline, the nitrogen pipeline is sequentially connected with a first compressor, a first cooler, a second compressor and a second cooler, an outlet of the second cooler is connected with a first heat flow inlet of the first plate heat exchanger, a first heat flow outlet of the first plate heat exchanger is connected with an inlet of the first expander, an outlet of the first expander is connected with a cold flow inlet of the second plate heat exchanger, and a cold flow outlet of the second plate heat exchanger is connected with a cold flow of the first plate heat exchanger;
the natural gas condensation decarbonization system comprises a CO-containing system 2 Of natural gas pipelines containing CO 2 The natural gas pipeline is connected with a second heat flow inlet of the first plate heat exchanger, a second heat flow outlet of the heat exchanger is sequentially connected with a second expander, a cyclone particle separation device for separating carbon dioxide and a third compressor, and an outlet of the third compressor is connected with the second plate heat exchanger in a heat flow manner;
and the natural gas condensation decarburization system and the nitrogen expansion system are coupled through the first plate heat exchanger and the second plate heat exchanger.
2. The CRS technology-based nitrogen expansion, liquefaction and decarbonization system of claim 1, wherein the cold flow outlet of the first plate heat exchanger is connected with a first compressor.
3. A nitrogen expansion, liquefaction and decarburization method based on a CRS technology is characterized by comprising the following steps:
containing CO 2 The natural gas is condensed and liquefied through the first plate heat exchanger and the second expander in sequence, then is subjected to gas-liquid separation through the cyclone particle separation device, the separated gas phase enters a third compressor for compression, and finally is condensed and liquefied through the second plate heat exchanger;
the nitrogen is subjected to secondary compression to increase the pressure, is subjected to secondary cooler to reduce the temperature, enters the first plate heat exchanger to be further cooled, and cooled N 2 While reducing the pressure through the expander, N 2 The natural gas enters the first plate heat exchanger for further deep cooling decarburization after the temperature is reduced, and finally enters the first plate heat exchanger for heat exchange, so that circulation is realized.
4. The CRS technology-based nitrogen expansion, liquefaction and decarbonization method of claim 3, wherein the first plate heat exchanger N is 2 N of cold flow and first hot flow entering first plate heat exchanger 2 Second heat flow into the first plate heat exchanger containing CO 2 Is subjected to heat exchange.
5. The CRS technology-based nitrogen expansion, liquefaction and decarburization method as recited in claim 3, wherein N after entering the first plate heat exchanger for heat exchange is 2 And entering a first compressor for circulation.
6. The CRS technology-based nitrogen expansion, liquefaction and decarburization method as claimed in claim 3, wherein the separation of condensed liquid droplets and liquid CO is realized by centrifugal force generated by high-speed rotation in the micro-channel of the cyclone particle separation device 2 The purified natural gas is pressurized by a compressor and then enters a downstream flow.
7. The CRS technology-based nitrogen expansion, liquefaction and decarbonization method of claim 3, wherein the liquid obtained by the final condensation and liquefaction through the second plate heat exchanger is decarbonized LNG.
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