CN217383531U - Gas turbine unit carbon dioxide entrapment liquefaction system based on LNG cold energy - Google Patents

Gas turbine unit carbon dioxide entrapment liquefaction system based on LNG cold energy Download PDF

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CN217383531U
CN217383531U CN202220930402.1U CN202220930402U CN217383531U CN 217383531 U CN217383531 U CN 217383531U CN 202220930402 U CN202220930402 U CN 202220930402U CN 217383531 U CN217383531 U CN 217383531U
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carbon dioxide
cold energy
flue gas
gas
heat exchanger
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Inventor
提梦桃
刘涛
丁予婷
李新林
吴兴栋
许慧萱
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Hebei University of Architecture
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Hebei University of Architecture
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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
    • F25J3/06—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation
    • F25J3/063—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation characterised by the separated product stream
    • F25J3/067—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation characterised by the separated product stream separation of carbon dioxide
    • 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
    • F25J2205/40—Processes or apparatus using other separation and/or other processing means using hybrid system, i.e. combining cryogenic and non-cryogenic separation techniques
    • 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
    • F25J2205/80—Processes or apparatus using other separation and/or other processing means using membrane, i.e. including a permeation step
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2210/00—Processes characterised by the type or other details of the feed stream
    • F25J2210/62—Liquefied natural gas [LNG]; Natural gas liquids [NGL]; Liquefied petroleum gas [LPG]
    • 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
    • F25J2210/00—Processes characterised by the type or other details of the feed stream
    • F25J2210/70—Flue or combustion exhaust 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
    • F25J2215/00—Processes characterised by the type or other details of the product stream
    • F25J2215/04—Recovery of liquid products
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2220/00—Processes or apparatus involving steps for the removal of impurities
    • F25J2220/80—Separating impurities from carbon dioxide, e.g. H2O or water-soluble contaminants
    • F25J2220/82—Separating low boiling, i.e. more volatile components, e.g. He, H2, CO, Air gases, CH4
    • 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
    • F25J2230/04—Compressor cooling arrangement, e.g. inter- or after-stage cooling or condensate removal
    • 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
    • F25J2230/08—Cold compressor, i.e. suction of the gas at cryogenic temperature and generally without afterstage-cooler
    • 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
    • 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
    • F25J2270/904—External refrigeration, e.g. conventional closed-loop mechanical refrigeration unit using Freon or NH3, unspecified external refrigeration by liquid or gaseous cryogen in an open loop

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  • Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Physics & Mathematics (AREA)
  • Mechanical Engineering (AREA)
  • Thermal Sciences (AREA)
  • General Engineering & Computer Science (AREA)
  • Carbon And Carbon Compounds (AREA)

Abstract

The utility model belongs to the technical field of the carbon dioxide entrapment, especially, relate to a gas unit carbon dioxide entrapment liquefaction system based on LNG cold energy, include: the carbon dioxide capturing and liquefying system comprises a flue gas purifying and cooling module, a flue gas drying and compressing module, a carbon dioxide concentrating module, at least two flue gas compressing and cooling modules and a carbon dioxide liquefying module which are connected in sequence; and the LNG cold energy recovery system is used for conveying LNG cold energy to any of the flue gas compression cooling modules in a cascade utilization mode and exchanging heat with the concentrated flue gas in the flue gas compression cooling modules. The utility model discloses in, carbon dioxide entrapment liquefaction system carries out carbon dioxide recovery through coupling membrane filtration method and cryogenic process, and more common carbon dioxide system is more energy-conserving, environmental protection, and LNG cold energy recovery system can realize the step utilization of energy and avoided the production that the cold energy pollutes to a certain extent.

Description

Gas turbine unit carbon dioxide entrapment liquefaction system based on LNG cold energy
Technical Field
The utility model belongs to the technical field of the carbon dioxide entrapment, especially, relate to a gas unit carbon dioxide entrapment liquefaction system based on LNG cold energy.
Background
In recent decades, increasingly serious ecological environmental problems such as acid rain, el nino, raney, marine pollution, ozone layer destruction, haze, global warming and the like frequently occur in the world. Among them, the greenhouse effect caused by carbon dioxide gas (CO2) discharged by the combustion of a large amount of fossil energy is one of the most serious environmental problems facing human beings, and how to effectively reduce the carbon dioxide discharge after the combustion of fossil fuel becomes the focus of attention of relevant scholars at home and abroad. In this context, carbon dioxide capture technology has been developed and developed.
The difficulty in solving the technical problems is as follows: a large amount of carbon dioxide gas can be discharged by burning a large amount of fossil energy, the common carbon dioxide capture technology is difficult to realize energy-saving and environment-friendly recovery, LNG cold energy generated in the using process of a gas unit cannot be reused, then cold energy pollution is easy to generate, and related technical reports about the carbon dioxide capture liquefaction system of the gas unit based on the LNG cold energy are not provided as references at present.
The significance of solving the technical problems is as follows: the LNG cold energy-based gas turbine unit carbon dioxide capture liquefaction system and the method based on the LNG cold energy are designed, can realize energy-saving and environment-friendly carbon dioxide recovery, can realize gradient utilization of energy, and can avoid the generation of cold energy pollution to a certain extent, and have important practical significance.
SUMMERY OF THE UTILITY MODEL
The utility model discloses a solve the problem that exists among the above-mentioned prior art, provide one kind and can realize energy-conserving, the environmental protection the recovery carbon dioxide, can realize again that the step of energy utilizes and avoided the gas unit carbon dioxide entrapment liquefaction system based on LNG cold energy of the production that the cold energy pollutes to a certain extent.
The utility model discloses a solve the technical scheme who takes of this problem and be:
a gas turbine unit carbon dioxide capture liquefaction system based on LNG cold energy includes:
the carbon dioxide capturing and liquefying system comprises a flue gas purifying and cooling module, a flue gas drying and compressing module, a carbon dioxide concentrating module, at least two flue gas compressing and cooling modules and a carbon dioxide liquefying module which are connected in sequence;
and the LNG cold energy recovery system is used for conveying LNG cold energy to any of the flue gas compression cooling modules in a cascade utilization mode and exchanging heat with the concentrated flue gas in the flue gas compression cooling modules.
Preferably, the flue gas purification cooling module comprises a flue gas purification device and a third heat exchanger which are connected in sequence, and an inlet of the flue gas purification device is connected with an outlet flue of the waste heat boiler.
Preferably, the flue gas drying and compressing module comprises a flue gas drying device and a third compressor which are connected in sequence, and a flue gas side outlet of the third heat exchanger is connected with an inlet of the flue gas drying device.
Further preferably, the carbon dioxide concentration module comprises a CO2 concentration device, an inlet of the CO2 concentration device is connected with an outlet of the third compressor, a waste gas outlet of the CO2 concentration device is connected with a smoke exhaust flue, and a carbon dioxide outlet of the CO2 concentration device is connected with the smoke compression cooling module.
Further preferably, the concentrated flue gas in the carbon dioxide capturing and liquefying system passes through each flue gas compression cooling module step by step, the LNG cold energy recovery system comprises LNG and a cold energy pipeline for conveying cold energy, the conveying direction of the cold energy in the LNG cold energy recovery system is opposite to the conveying direction of the concentrated flue gas in the flue gas compression cooling module, and the cold energy in the LNG cold energy recovery system is conveyed in a step utilization manner.
Preferably, when the number of the flue gas compression cooling modules is two, the flue gas compression cooling modules are respectively a first flue gas compression cooling module and a second flue gas compression cooling module which are connected in sequence;
wherein:
the first flue gas compression cooling module comprises a second compressor and a second heat exchanger which are sequentially connected;
the second flue gas compression cooling module comprises a first compressor and a first heat exchanger which are sequentially connected;
and the concentrated flue gas outlet of the second heat exchanger is connected with the inlet of the first compressor.
Further preferably, the carbon dioxide liquefaction module comprises a gas-liquid separator and a CO2 liquid storage tank which are sequentially connected, a concentrated flue gas outlet of the first heat exchanger is connected with a concentrated gas inlet of the gas-liquid separator, a liquefied carbon dioxide outlet of the gas-liquid separator is connected with a CO2 liquid storage tank, and a non-condensable gas outlet of the gas-liquid separator is connected with a non-condensable gas inlet of the second heat exchanger.
Further preferably, an outlet of the LNGP6 is connected in parallel with a first cold energy pipeline and a second cold energy pipeline, the first cold energy pipeline is provided with a second flow valve, and the second cold energy pipeline is provided with a first flow valve.
Further preferably, a gas inlet of the first heat exchanger is connected with an outlet of the LNG through a first cold energy pipeline, and a gas outlet of the first heat exchanger and a parallel node of the second cold energy pipeline are connected (form a parallel pipeline) and connected with a gas inlet of the second heat exchanger.
Further preferably, a gas outlet of the second heat exchanger is connected with a gas inlet of a third heat exchanger, and a gas outlet of the third heat exchanger is connected with an inlet of the combustion chamber.
Further preferably, the power source of the first compressor, the second compressor and the third compressor is from a main steam pipeline of the waste heat boiler.
The utility model has the advantages and positive effects that:
1. the utility model discloses in, the flue gas that exhaust-heat boiler outlet flue produced carries out carbon dioxide through carbon dioxide entrapment liquefaction system and retrieves, finally obtains liquid carbon dioxide, and this carbon dioxide entrapment liquefaction system carries out carbon dioxide through coupling membrane filtration method and cryogenic process and retrieves, and more energy-conservation, environmental protection of more common carbon dioxide system.
2. The utility model discloses in, the LNG cold energy adopts the cascade utilization formula heat exchange, can fully retrieve the LNG cold energy that produces in the gas unit use, realizes the cascade utilization of energy and has avoided the production that the cold energy pollutes to a certain extent.
Drawings
The technical solution of the present invention will be described in further detail with reference to the accompanying drawings and examples, but it should be understood that these drawings are designed for illustrative purposes only and thus are not intended to limit the scope of the present invention. Furthermore, unless otherwise indicated, the drawings are intended to be illustrative of the structural configurations described herein and are not necessarily drawn to scale.
FIG. 1 is a system connection diagram of the present invention;
fig. 2 is a schematic diagram of the internal structure of a CO2 membrane concentration device.
In the figure: 1.1-a first compressor; 1.2-a second compressor; 1.3-a third compressor; 2-small steam engine; 3.1 — a first heat exchanger; 3.2-a second heat exchanger; 3.3-third heat exchanger; 4-CO2 membrane concentration equipment; 401-carbon dioxide filtration membrane; 402-a gas filtration membrane; 5-flue gas drying equipment; 6.1-first flow valve; 6.2-a second flow valve; 7-gas-liquid separator; 8-a liquid storage tank; 9-a flue gas purification device; p1-main steam pipeline of waste heat boiler; p2-condenser; p3-exhaust-heat boiler outlet flue; p4-combustion engine combustion chamber; p5-unit smoke exhaust flue; P6-LNG.
Detailed Description
First, it should be noted that the specific structures, features, advantages, etc. of the present invention will be described in detail below by way of example, but all the descriptions are only for illustrative purpose and should not be construed as forming any limitation to the present invention. Furthermore, any single feature described or implicit in any embodiment or any single feature shown or implicit in any drawing may still be combined or subtracted between any of the features (or equivalents thereof) to obtain still further embodiments of the invention that may not be directly mentioned herein. In addition, for the sake of simplicity, the same or similar features may be indicated in only one place in the same drawing.
In the present invention, unless otherwise expressly stated or limited, the terms "mounted," "disposed," "connected," "fixed," "screwed" and the like are to be construed broadly, e.g., as meaning fixedly connected, detachably connected, or integrally formed; can be mechanically or electrically connected; they may be directly connected or indirectly connected through an intermediate medium, and may be connected through the inside of two elements or in an interaction relationship between two elements, unless otherwise specifically defined, and the specific meaning of the above terms in the present invention will be understood by those skilled in the art according to specific situations. The present invention will be described in detail with reference to the accompanying drawings.
Example 1:
a gas turbine unit carbon dioxide capture liquefaction system based on LNG cold energy includes: the carbon dioxide capturing and liquefying system comprises a flue gas purifying and cooling module, a flue gas drying and compressing module, a carbon dioxide concentrating module, at least two flue gas compressing and cooling modules and a carbon dioxide liquefying module which are connected in sequence; and the LNG cold energy recovery system is used for conveying LNG cold energy to any of the flue gas compression cooling modules in a cascade utilization mode and exchanging heat with the concentrated flue gas in the flue gas compression cooling modules.
In this embodiment, as shown in fig. 1, flue gas generated by the exhaust-heat boiler outlet flue P3 is subjected to carbon dioxide recovery by a carbon dioxide capture liquefaction system, and the carbon dioxide capture liquefaction system includes a flue gas purification cooling module, a flue gas drying and compression module, a carbon dioxide concentration module, at least two flue gas compression cooling modules, and a carbon dioxide liquefaction module, which are connected in sequence. Wherein: the flue gas purification cooling module is used for purifying and cooling flue gas; the flue gas drying and compressing module is used for drying and compressing flue gas; the flue gas after compression and pressure rise enters a carbon dioxide concentration module, and the concentration of carbon dioxide in the flue gas is improved by adopting a permeable membrane module under the action of osmotic pressure difference; the at least two flue gas compression and cooling modules are used for compressing and cooling the concentrated flue gas for multiple times to enable the carbon dioxide component in the concentrated flue gas to reach a saturated state, and in the compression and cooling processes, different gases are separated by utilizing the difference of different gas boiling points, so that the principle of recycling the carbon dioxide by adopting a cryogenic method is adopted; the carbon dioxide liquefaction module is used for carrying out gas-liquid separation on the concentrated flue gas and storing the obtained liquid carbon dioxide. The carbon dioxide capture liquefaction system recovers carbon dioxide by a coupling membrane filtration method and a cryogenic method, and is more energy-saving and environment-friendly than a common carbon dioxide system.
When the carbon dioxide gathering liquefaction system carries out carbon dioxide recovery, LNG cold energy recovery system carries the LNG cold energy cascade utilization formula for wantonly flue gas compression cooling module for the cold energy carries out the heat exchange with concentrated flue gas among the flue gas compression cooling module, can fully retrieve the LNG cold energy that produces in the gas unit use, realizes the cascade utilization of energy and has avoided the production of cold energy pollution to a certain extent.
Furthermore, it can be considered in this embodiment that the flue gas cleaning and cooling module includes a flue gas cleaning device 9 and a third heat exchanger 3.3 connected in sequence, and an inlet of the flue gas cleaning device 9 is connected to the exhaust-heat boiler outlet flue P3.
Furthermore, it can be considered in this embodiment that the flue gas drying and compressing module includes a flue gas drying device 5 and a third compressor 1.3 connected in sequence, and a flue gas side outlet of the third heat exchanger 3.3 is connected to an inlet of the flue gas drying device 5.
Furthermore, it is also considered in this embodiment that the carbon dioxide concentration module includes a CO2 concentration device 4, an inlet of the CO2 concentration device 4 is connected to an outlet of the third compressor 1.3, an exhaust gas outlet of the CO2 concentration device 4 is connected to a smoke exhaust flue P5, and a carbon dioxide outlet of the CO2 concentration device 4 is connected to the smoke compression cooling module.
It should be noted that the CO2 concentration device 4 is a double-layer barrel-shaped structure, the inner-layer barrel structure is used for installing a permeable membrane module, the permeable membrane module includes a carbon dioxide filter membrane 401 and a gas filter membrane 402, wherein the carbon dioxide filter membrane 401 only allows carbon dioxide to pass through, the gas filter membrane 402 allows gases except carbon dioxide to pass through, and the flue gas entering the CO2 concentration device realizes a gas separation effect under the pressure effect.
Furthermore, it can be considered in this embodiment that the concentrated flue gas in the carbon dioxide capturing and liquefying system passes through each flue gas compression and cooling module step by step, the LNG cold energy recovery system includes LNGP6 and a cold energy pipeline for transporting cold energy, a transporting direction of the cold energy in the LNG cold energy recovery system is opposite to a transporting direction of the concentrated flue gas in the flue gas compression and cooling module, and the cold energy in the LNG cold energy recovery system is transported in a cascade manner.
In the embodiment, at least two flue gas compression and cooling modules are arranged in the carbon dioxide capture liquefaction system, and concentrated flue gas passes through each flue gas compression and cooling module step by step to be compressed and cooled for multiple times, so that carbon dioxide components in the concentrated flue gas reach a saturated state; the outlet of LNGP6 is connected in parallel with at least two cold energy pipelines, the number of the cold energy pipelines is the same as the number of the smoke compression cooling modules, and each cold energy pipeline is provided with a flow valve. LNG cold energy adopts cascade utilization formula transportation, and is specific: the carbon dioxide capture liquefaction system is provided with a 1 st, 2 … … th N-1 st and N flue gas compression cooling module, an outlet of the LNGP6 is connected with a 1 st, 2 … … th N-1 st and N cold energy pipelines in parallel, the 1 st cold energy pipeline of the LNGP6 is connected with a fuel gas inlet of the 1 st heat exchanger, a fuel gas outlet of the 1 st heat exchanger and the 2 nd cold energy pipeline form a parallel pipeline which is connected with a fuel gas inlet of the 2 nd heat exchanger … …, a fuel gas outlet of the N-1 st heat exchanger and the N th cold energy pipeline form a parallel pipeline which is connected with a fuel gas inlet of the N th heat exchanger, the cascade utilization of energy is realized, and the generation of cold energy pollution is avoided to a certain extent.
Example 2:
embodiment 2 of the present invention is further improved on the basis of embodiment 1 so as to fully exert the technical advantages of the present invention, and this is exemplified below.
For example: when the number of the flue gas compression cooling modules is two, the flue gas compression cooling modules are respectively a first flue gas compression cooling module and a second flue gas compression cooling module which are sequentially connected;
wherein: the first flue gas compression cooling module comprises a second compressor 1.2 and a second heat exchanger 3.2 which are connected in sequence; the second flue gas compression cooling module comprises a first compressor 1.1 and a first heat exchanger 3.1 which are sequentially connected; and the concentrated flue gas outlet of the second heat exchanger 3.2 is connected with the inlet of the first compressor 1.1.
Furthermore, it can be considered in this embodiment that the carbon dioxide liquefaction module includes a gas-liquid separator 7 and a CO2 liquid storage tank 8 that are connected in sequence, the concentrated flue gas outlet of the first heat exchanger 3.1 is connected with the concentrated gas inlet of the gas-liquid separator 7, the liquefied carbon dioxide outlet of the gas-liquid separator 7 is connected with the CO2 liquid storage tank 8, and the non-condensable gas outlet of the gas-liquid separator 7 is connected with the non-condensable gas inlet of the second heat exchanger 3.2.
Furthermore, it can be considered in this embodiment that the outlet of the LNGP6 is connected in parallel to a first cold energy pipeline and a second cold energy pipeline, the first cold energy pipeline is provided with a second flow valve 6.2, and the second cold energy pipeline is provided with a first flow valve 6.1.
Furthermore, it can be considered in this embodiment that the gas inlet of the first heat exchanger 3.1 is connected to the outlet of the LNG P6 through a first cold energy pipeline, the gas outlet of the first heat exchanger 3.1 and the parallel connection node of the second cold energy pipeline (forming a parallel pipeline) are connected to each other and to the gas inlet of the second heat exchanger 3.2, the gas outlet of the second heat exchanger 3.2 is connected to the gas inlet of the third heat exchanger 3.3, and the gas outlet of the third heat exchanger 3.3 is connected to the combustion chamber inlet P4.
In this embodiment, the device flow is:
an outlet flue P3 of the waste heat boiler is connected with an inlet of a flue gas purification device 9, an outlet of the flue gas purification device 9 is connected with a flue gas side inlet of a third heat exchanger 3.3, a flue gas side outlet of the third heat exchanger 3.3 is connected with an inlet of a flue gas drying device 5, an outlet of the flue gas drying device 5 is connected with an inlet of a third compressor 1.3, an outlet of the third compressor 1.3 is connected with an inlet of a CO2 concentration device 4, a waste gas outlet of the CO2 concentration device 4 is connected with a flue gas exhaust flue P5, a carbon dioxide outlet of the CO2 concentration device 4 is connected with a concentrated flue gas inlet of a second heat exchanger 3.2, a concentrated flue gas outlet of the second heat exchanger 3.2 is connected with an inlet of a first compressor 1.1, an outlet of the first compressor 1.1 is connected with a concentrated flue gas inlet of the first heat exchanger 3.1, a concentrated flue gas outlet of the first heat exchanger 3.1 is connected with a concentrated gas inlet of a gas-liquid separator 7, a liquefied carbon dioxide outlet of the gas-liquid storage tank 7 is connected with a CO2 liquid storage tank, a non-condensable gas outlet of the gas-liquid separator 7 is connected with a non-condensable gas inlet of the second heat exchanger 3.2, a non-condensable gas outlet of the second heat exchanger 3.2 is connected with a unit smoke exhaust flue P5, a gas inlet of the first heat exchanger 3.1 is connected with an outlet of the second flow valve 6.2, an inlet of the second heat exchanger 3.2 is formed by connecting an outlet of the first flow valve 6.1 and a gas outlet of the first heat exchanger 3.1 in parallel, a gas outlet of the second heat exchanger 3.2 is connected with a gas inlet of the third heat exchanger 3.3, a gas outlet of the third heat exchanger 3.3 is connected with an inlet of the combustion chamber P4, and the first flow valve 6.1 and the second flow valve 6.2 are connected with an outlet of the LNGP6 in parallel.
Furthermore, it can be considered in this embodiment that the power source of the first compressor 1.1, the second compressor 1.2 and the third compressor 1.3 is from the main steam pipeline P1 of the waste heat boiler, the compressors are driven by the rotational kinetic energy generated by the work of the waste heat boiler main steam pipeline P1 through the small steam turbine 2, and the steam after the work is discharged into the condenser P2.
Example 3:
the method for utilizing the LNG cold energy-based gas unit carbon dioxide capture liquefaction system comprises a carbon dioxide capture liquefaction process and an LNG cold energy recovery process;
wherein: the carbon dioxide capture liquefaction process comprises the steps of:
the method comprises the following steps: the flue gas from the exhaust flue P3 of the waste heat boiler enters the third heat exchanger 3.3 for cooling after impurities are removed by the flue gas purification device 9;
step two: the flue gas cooled by the third heat exchanger 3.3 enters the flue gas drying device 5, and the flue gas dried by the flue gas drying device 5 enters the third compressor 1.3 for compression and pressure boosting;
step three: the flue gas compressed and boosted by the third compressor 1.3 enters a CO2 membrane concentration device 4, the CO2 membrane concentration device 4 adopts a permeable membrane module to increase the concentration of carbon dioxide in the flue gas under the action of osmotic pressure difference, and other gases generated in the process are discharged into a unit smoke exhaust flue P5;
step four: the concentrated flue gas after concentration is introduced into a second compressor 1.2 for further compression, and the concentrated flue gas after concentration is compressed and boosted by the second compressor 1.2 and then enters a second heat exchanger 3.2 for cooling;
step five: the cooled concentrated flue gas is discharged into a first compressor 1.1, the concentrated flue gas compressed and boosted by the first compressor 1.1 enters a first heat exchanger 3.1 for further cooling and temperature reduction, so that the carbon dioxide component in the concentrated flue gas reaches a saturated state;
step six: discharging the cooled concentrated flue gas into a gas-liquid separator 7 for gas-liquid separation, and allowing liquid carbon dioxide obtained by separation by the gas-liquid separator 7 to flow to a liquid storage tank 8 through a pipeline for storage;
step seven: the gaseous substance obtained by the gas-liquid separator 7 is discharged into a unit smoke exhaust flue P5 after surplus cold energy is recovered by the second heat exchanger 3.2;
the LNG cold energy recovery process comprises the following steps:
the method comprises the following steps: liquefied natural gas from LNGP6 is respectively led into a first flow valve 6.1 and a second flow valve 6.2 through parallel pipelines, and the liquefied natural gas passing through the second flow valve 6.2 enters a first heat exchanger 3.1 for temperature rise and vaporization;
step two: the heated liquefied gas and the liquefied gas passing through the first flow valve 6.1 are mixed, the temperature of the mixture is adjusted, the mixture is introduced into the second heat exchanger 3.2, the liquefied gas heated by the second heat exchanger 3.2 enters the third heat exchanger 3.3 for further heating and vaporization, and finally the liquefied gas enters a combustion engine combustion chamber P4.
Furthermore, it can be considered in this embodiment that the carbon dioxide capture liquefaction process and the LNG cold energy recovery process are performed synchronously, and the power source of the compressor in the flue gas drying and compressing module and the flue gas compression and cooling module comes from the waste heat boiler main steam pipeline P1.
In this embodiment, the process flow is as follows:
the method comprises the steps that the smoke from the exhaust flue P3 of the waste heat boiler enters a third heat exchanger 3.3 for cooling after impurities are removed by a smoke purification device 9, the smoke cooled by the third heat exchanger 3.3 enters a smoke drying device 5, the smoke dried by the smoke drying device 5 enters a third compressor 1.3, the smoke is compressed and boosted by the third compressor 1.3 and then enters a CO2 membrane concentration device 4, a permeable membrane module or a CO2 separation membrane is arranged in the CO2 membrane concentration device 4, the concentration of carbon dioxide in the smoke is increased by the permeable membrane module under the action of osmotic pressure difference, and other gases generated in the process are discharged into the exhaust flue P5 of a unit. The concentrated flue gas is introduced into a second compressor 1.2 for further compression, the concentrated flue gas is compressed and boosted by the second compressor 1.2 and then enters a second heat exchanger 3.2 for cooling, the cooled concentrated flue gas is discharged into a first compressor 1.1, the concentrated flue gas compressed and boosted by the first compressor 1.1 enters a first heat exchanger 3.1 for further cooling and temperature reduction so that carbon dioxide components in the concentrated flue gas reach a saturated state, the cooled concentrated flue gas is discharged into a gas-liquid separator 7 for gas-liquid separation, liquid carbon dioxide obtained by the separation of the gas-liquid separator 7 flows to a liquid storage tank 8 through a pipeline for storage, gaseous substances obtained by the gas-liquid separator 7 are discharged into a unit smoke exhaust flue P4 after surplus cold energy is recovered by the second heat exchanger 3.2, the compressor adopts a main steam pipeline P1 of the waste heat boiler, the compressor is driven by the rotational kinetic energy generated by the small steam turbine 2, and the steam after acting is discharged into a condenser P2.
The LNG cold energy recovery system adopts cold energy from a gasification process of LNG P6 in a gas turbine power plant, liquefied natural gas from LNG P6 is respectively introduced into a first flow valve 6.1 and a second flow valve 6.2 through parallel pipelines, the liquefied natural gas passing through the second flow valve 6.2 enters a first heat exchanger 3.1 for temperature rise and vaporization, the heated liquefied gas and the liquefied gas passing through the first flow valve 6.1 are mixed for temperature regulation and then are introduced into a second heat exchanger 3.2, the temperature is further raised for vaporization of the second heat exchanger 3.2, and the heated liquefied gas enters a third heat exchanger 3.3 for further temperature rise and vaporization after being heated by the second heat exchanger 3.2 and then enters a gas turbine combustor P4.
The above embodiments are described in detail, but the above description is only for the preferred embodiments of the present invention, and should not be construed as limiting the scope of the present invention. All the equivalent changes and improvements made according to the application scope of the present invention should still fall within the patent coverage of the present invention.

Claims (10)

1. The utility model provides a gas unit carbon dioxide entrapment liquefaction system based on LNG cold energy which characterized in that: the method comprises the following steps:
the carbon dioxide capturing and liquefying system comprises a flue gas purifying and cooling module, a flue gas drying and compressing module, a carbon dioxide concentrating module, at least two flue gas compressing and cooling modules and a carbon dioxide liquefying module which are connected in sequence;
and the LNG cold energy recovery system is used for conveying LNG cold energy to any of the flue gas compression cooling modules in a cascade utilization mode and exchanging heat with the concentrated flue gas in the flue gas compression cooling modules.
2. The LNG cold energy-based gas turbine unit carbon dioxide capture liquefaction system of claim 1, characterized in that: the flue gas purification cooling module comprises a flue gas purification device (9) and a third heat exchanger (3.3) which are connected in sequence, and an inlet of the flue gas purification device (9) is connected with an outlet flue (P3) of the waste heat boiler.
3. The LNG cold energy-based gas turbine unit carbon dioxide capture liquefaction system of claim 2, characterized in that: the flue gas drying and compressing module comprises a flue gas drying device (5) and a third compressor (1.3) which are sequentially connected.
4. The LNG cold energy-based gas turbine unit carbon dioxide capture liquefaction system of claim 3, characterized in that: the carbon dioxide concentration module comprises CO2 concentration equipment (4), the inlet of the CO2 concentration equipment (4) is connected with the outlet of the third compressor (1.3), the exhaust gas outlet of the CO2 concentration equipment (4) is connected with a smoke exhaust flue (P5), and the carbon dioxide outlet of the CO2 concentration equipment (4) is connected with the smoke compression cooling module.
5. The LNG cold energy-based gas turbine carbon dioxide capture liquefaction system of any one of claims 1-4, wherein: concentrated flue gas in the carbon dioxide gathering liquefaction system passes through each flue gas compression cooling module step by step, LNG cold energy recovery system includes LNG (P6) and is used for carrying the cold energy pipeline of cold energy, the direction of delivery of cold energy among the LNG cold energy recovery system is opposite with the direction of delivery of concentrated flue gas in the flue gas compression cooling module, and cold energy is the cascade utilization formula transport among the LNG cold energy recovery system.
6. The LNG cold energy-based gas turbine unit carbon dioxide capture liquefaction system of claim 5, characterized in that: when the number of the flue gas compression cooling modules is two, the flue gas compression cooling modules are respectively a first flue gas compression cooling module and a second flue gas compression cooling module which are sequentially connected;
wherein:
the first flue gas compression cooling module comprises a second compressor (1.2) and a second heat exchanger (3.2) which are sequentially connected;
the second flue gas compression cooling module comprises a first compressor (1.1) and a first heat exchanger (3.1) which are sequentially connected;
and the concentrated flue gas outlet of the second heat exchanger (3.2) is connected with the inlet of the first compressor (1.1).
7. The LNG cold energy-based gas turbine unit carbon dioxide capture liquefaction system of claim 6, characterized in that: the carbon dioxide liquefaction module is including the vapour and liquid separator (7) and the CO2 liquid storage pot (8) that connect gradually, the concentrated exhanst gas outlet of first heat exchanger (3.1) links to each other with the concentrated gas entry of vapour and liquid separator (7), the liquefied carbon dioxide export of vapour and liquid separator (7) links to each other with CO2 liquid storage pot (8), the noncondensable gas row mouth of vapour and liquid separator (7) links to each other with second heat exchanger (3.2) noncondensable gas entry.
8. The LNG cold energy-based gas turbine unit carbon dioxide capture liquefaction system of claim 7, characterized in that: the export of LNG (P6) is parallelly connected to have first cold energy pipeline and second cold energy pipeline, be equipped with second flow valve (6.2) on the first cold energy pipeline, be equipped with first flow valve (6.1) on the second cold energy pipeline.
9. The LNG cold energy-based gas turbine unit carbon dioxide capture liquefaction system of claim 8, characterized in that: the gas inlet of the first heat exchanger (3.1) is connected with the outlet of LNG (P6) through a first cold energy pipeline, the gas outlet of the first heat exchanger (3.1) is connected with the parallel connection node of the second cold energy pipeline and is connected with the gas inlet of the second heat exchanger (3.2), the gas outlet of the second heat exchanger (3.2) is connected with the gas inlet of the third heat exchanger (3.3), and the gas outlet of the third heat exchanger (3.3) is connected with the inlet (P4) of the combustion chamber.
10. The LNG cold energy-based gas turbine unit carbon dioxide capture liquefaction system of claim 6, characterized in that: the power source of the first compressor (1.1), the second compressor (1.2) and the third compressor (1.3) is from a main steam pipeline (P1) of the waste heat boiler.
CN202220930402.1U 2022-04-21 2022-04-21 Gas turbine unit carbon dioxide entrapment liquefaction system based on LNG cold energy Active CN217383531U (en)

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