CN116972598A - Gas turbine unit carbon dioxide capturing and liquefying system and method based on LNG cold energy - Google Patents

Gas turbine unit carbon dioxide capturing and liquefying system and method based on LNG cold energy Download PDF

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Publication number
CN116972598A
CN116972598A CN202210422420.3A CN202210422420A CN116972598A CN 116972598 A CN116972598 A CN 116972598A CN 202210422420 A CN202210422420 A CN 202210422420A CN 116972598 A CN116972598 A CN 116972598A
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China
Prior art keywords
carbon dioxide
flue gas
cold energy
gas
heat exchanger
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CN202210422420.3A
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Chinese (zh)
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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Priority to CN202210422420.3A priority Critical patent/CN116972598A/en
Publication of CN116972598A publication Critical patent/CN116972598A/en
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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
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/0228—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream
    • F25J3/0266—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of carbon dioxide
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/22—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by diffusion
    • B01D53/228—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by diffusion characterised by specific membranes
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES 
    • F23J15/00—Arrangements of devices for treating smoke or fumes
    • F23J15/02—Arrangements of devices for treating smoke or fumes of purifiers, e.g. for removing noxious material
    • F23J15/022—Arrangements of devices for treating smoke or fumes of purifiers, e.g. for removing noxious material for removing solid particulate material from the gasflow
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES 
    • F23J15/00—Arrangements of devices for treating smoke or fumes
    • F23J15/06—Arrangements of devices for treating smoke or fumes of coolers
    • 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
    • F25J2230/08—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
    • F25J2230/20—Integrated compressor and process expander; Gear box arrangement; Multiple compressors on a common shaft
    • 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
    • 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
    • F25J2270/90—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)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Physics & Mathematics (AREA)
  • Thermal Sciences (AREA)
  • Analytical Chemistry (AREA)
  • General Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Carbon And Carbon Compounds (AREA)

Abstract

The invention belongs to the technical field of carbon dioxide capture, and particularly relates to a gas turbine unit carbon dioxide capture liquefaction system and method based on LNG cold energy, wherein the gas turbine unit carbon dioxide capture liquefaction system based on the LNG cold energy comprises: 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 smoke compression cooling module in a gradient mode and is used for carrying out heat exchange with concentrated smoke in the smoke compression cooling module. According to the invention, the carbon dioxide collecting and liquefying system is used for recovering carbon dioxide through a coupling membrane filtration method and a cryogenic method, so that the energy is saved and the environment is protected compared with a common carbon dioxide system, the LNG cold energy recovery system can realize the cascade utilization of energy, and the cold energy pollution is avoided to a certain extent.

Description

Gas turbine unit carbon dioxide capturing and liquefying system and method based on LNG cold energy
Technical Field
The invention belongs to the technical field of carbon dioxide capture, and particularly relates to a carbon dioxide capture liquefaction system and method of a gas turbine unit based on LNG cold energy.
Background
In recent decades, increasingly serious ecological environmental problems such as acid rain, el nino, lanina, marine pollution, ozone layer destruction, haze, global warming and the like have occurred worldwide. Among them, the greenhouse effect caused by carbon dioxide gas (CO 2) discharged from the combustion of fossil energy is one of the most serious environmental problems facing humans, and how to effectively reduce carbon dioxide discharge after the combustion of fossil fuel has become a focus of attention of relevant scholars at home and abroad. In this context, carbon dioxide capture technology has been developed and has been developed.
The difficulty of solving the technical problems is that: the large amount of burning of fossil energy can emit a large amount of carbon dioxide gas, and common carbon dioxide trapping technology hardly realizes energy-saving and environment-friendly recovery, and LNG cold energy produced in the use process of the gas unit can not be secondarily utilized, so that cold energy pollution is easily produced, and no related technical report about a carbon dioxide trapping liquefaction system of the gas unit based on LNG cold energy is available at present as a reference.
The significance of solving the technical problems is that: the gas turbine set carbon dioxide capturing and liquefying system and method based on LNG cold energy, which can realize energy saving and environment protection, realize cascade utilization of energy and avoid cold energy pollution to a certain extent, have important practical significance.
Disclosure of Invention
The invention aims to solve the problems in the prior art, and provides a liquefied system and a liquefied method for capturing carbon dioxide of a gas turbine set based on LNG cold energy, which can realize energy conservation, environmental protection, cascade utilization of energy and avoid cold energy pollution to a certain extent.
The technical scheme adopted by the invention for solving the problem is as follows:
gas unit carbon dioxide entrapment 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 smoke compression cooling module in a gradient mode and is used for carrying out heat exchange with concentrated smoke in the smoke compression cooling module.
Preferably, the flue gas purifying and cooling module comprises a flue gas purifying device and a third heat exchanger which are sequentially connected, and an inlet of the flue gas purifying device is connected with an outlet flue of the waste heat boiler.
Further preferably, the flue gas drying and compressing module comprises a flue gas drying device and a third compressor which are sequentially connected, 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, an exhaust gas outlet of the CO2 concentration device is connected with the smoke discharging flue, and a carbon dioxide outlet of the CO2 concentration device is connected with the smoke compression cooling module.
Further preferably, concentrated flue gas passes through each flue gas compression cooling module step by step in the carbon dioxide entrapment liquefaction system, LNG cold energy recovery system includes LNG and is used for carrying the cold energy pipeline of cold energy, the direction of delivery of cold energy in 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 the cold energy is cascade utilization type and carries in the LNG cold energy recovery system.
Further preferably, when the number of the flue gas compression cooling modules is two, the first flue gas compression cooling module and the second flue gas compression cooling module are respectively 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;
the concentrated flue gas outlet of the second heat exchanger is connected with the inlet of the first compressor.
Further preferably, the carbon dioxide liquefying module comprises a gas-liquid separator and a CO2 liquid storage tank which are sequentially connected, the concentrated flue gas outlet of the first heat exchanger is connected with the concentrated gas inlet of the gas-liquid separator, the liquefied carbon dioxide outlet of the gas-liquid separator is connected with the CO2 liquid storage tank, and the non-condensable gas outlet of the gas-liquid separator is connected with the non-condensable gas inlet of the second heat exchanger.
Further preferably, the 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, the gas inlet of the first heat exchanger is connected to the LNG outlet through a first cold energy pipe, and the gas outlet of the first heat exchanger and the second cold energy pipe are connected in parallel (form a parallel pipeline) and are connected to the gas inlet of the second heat exchanger.
It is further preferred that the gas outlet of the second heat exchanger is connected to the gas inlet of the third heat exchanger, which gas outlet is connected to the combustion chamber inlet.
Further preferably, the power sources of the first, second and third compressors come from a main steam pipeline of the waste heat boiler.
The second invention of the present invention aims at: the method for utilizing the LNG cold energy-based gas unit carbon dioxide capturing and liquefying system comprises a carbon dioxide capturing and liquefying process and an LNG cold energy recycling process;
wherein: the carbon dioxide capturing and liquefying process comprises the following steps:
step one: removing impurities from the flue gas from the exhaust-heat boiler flue gas by a flue gas purification device, and then cooling the flue gas in a third heat exchanger;
step two: the flue gas cooled by the third heat exchanger enters a flue gas drying device, and the flue gas dried by the flue gas drying device enters a third compressor for compression and pressure boosting;
step three: the flue gas compressed and boosted by the third compressor enters CO2 membrane concentration equipment, the CO2 membrane concentration equipment adopts a permeable membrane component to promote 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 smoke discharging flue of the unit;
step four: the concentrated flue gas after concentration is introduced into a second compressor for further compression, compressed and boosted by the second compressor, and then enters a second heat exchanger for cooling;
step five: the cooled concentrated flue gas is discharged into a first compressor, and the concentrated flue gas compressed and boosted by the first compressor enters a first heat exchanger to be further cooled so that carbon dioxide components in the concentrated flue gas reach a saturated state;
step six: discharging the cooled concentrated flue gas into a gas-liquid separator for gas-liquid separation, and flowing the liquid carbon dioxide obtained by the separation of the gas-liquid separator to a liquid storage tank for storage through a pipeline;
step seven: the gaseous substances obtained by the gas-liquid separator are discharged into a smoke exhaust flue of the unit after the excessive cold energy is recovered by the second heat exchanger;
the LNG cold energy recovery process comprises the following steps:
step one: liquefied natural gas from LNG is respectively fed into a first flow valve and a second flow valve through parallel pipelines, and the liquefied natural gas passing through the second flow valve enters a first heat exchanger to be heated and vaporized;
step two: the liquefied gas after temperature rising is mixed with the liquefied gas passing through the first flow valve, the mixture is introduced into the second heat exchanger, the liquefied gas after temperature rising by the second heat exchanger enters the third heat exchanger for further temperature rising and vaporization, and finally the liquefied gas enters the combustion chamber of the gas turbine.
Preferably, the carbon dioxide capturing and liquefying process and the LNG cold energy recycling process are synchronously carried out, and the power sources of the compressors in the flue gas drying and compressing module and the flue gas compressing and cooling module come from a main steam pipeline of the waste heat boiler.
The invention has the advantages and positive effects that:
1. in the invention, the flue gas generated by the outlet flue of the waste heat boiler is subjected to carbon dioxide recovery through the carbon dioxide capturing and liquefying system, and finally liquid carbon dioxide is obtained.
2. According to the invention, LNG cold energy adopts cascade utilization type heat exchange, LNG cold energy generated in the using process of the gas unit can be fully recovered, cascade utilization of energy is realized, and cold energy pollution is avoided to a certain extent.
Drawings
The technical solution of the present invention will be described in further detail below with reference to the accompanying drawings and examples, but it should be understood that these drawings are designed for the purpose of illustration only and thus are not limiting the scope of the present invention. Moreover, unless specifically indicated otherwise, the drawings are intended to conceptually illustrate 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 flow diagram of a carbon dioxide capture liquefaction process;
FIG. 3 is a schematic flow diagram of an LNG cold energy recovery process;
fig. 4 is a schematic diagram of the internal structure of the CO2 membrane concentration device.
In the figure: 1.1-a first compressor; 1.2-a second compressor; 1.3-a third compressor; 2-a small steam turbine; 3.1-a first heat exchanger; 3.2-a second heat exchanger; 3.3-a third heat exchanger; 4-CO2 membrane concentration equipment; 401-a carbon dioxide filtration membrane; 402-a gas filtration membrane; 5-flue gas drying equipment; 6.1-a first flow valve; 6.2-a second flow valve; 7-a gas-liquid separator; 8-a liquid storage tank; 9-a flue gas purifying device; p1-a main steam pipeline of the waste heat boiler; p2-condenser; p3-exhaust-heat boiler outlet flue; p4-combustion chamber of combustion engine; p5-a smoke exhaust flue of the unit; P6-LNG.
Detailed Description
First, it should be noted that the following detailed description of the specific structure, characteristics, advantages, and the like of the present invention will be given by way of example, however, all descriptions are merely illustrative, and should not be construed as limiting the present invention in any way. Furthermore, any single feature described or implied in the embodiments mentioned herein, or any single feature shown or implied in the figures, may nevertheless be continued in any combination or pruning between these 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 of the drawing, identical or similar features may be indicated at one point in the same drawing.
In the present invention, unless explicitly specified and limited otherwise, the terms "mounted," "configured," "connected," "secured," "screwed," and the like are to be construed broadly and may be, for example, fixedly connected, detachably connected, or integrally formed; can be mechanically or electrically connected; either directly or indirectly through intermediaries, or in communication with each other or in interaction with each other, unless explicitly defined otherwise, the meaning of the terms described above in this application will be understood by those of ordinary skill in the art in view of the specific circumstances. The present invention will be described in detail with reference to the accompanying drawings.
Example 1:
gas unit carbon dioxide entrapment 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 smoke compression cooling module in a gradient mode and is used for carrying out heat exchange with concentrated smoke in the smoke compression cooling module.
In this embodiment, as shown in fig. 1, the flue gas generated by the exhaust-heat boiler outlet flue P3 is subjected to carbon dioxide recovery through a carbon dioxide capturing and liquefying system, and 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 sequentially connected. Wherein: the flue gas purifying and 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 compressed and boosted flue gas enters a carbon dioxide concentration module, and the concentration of carbon dioxide in the flue gas is improved by adopting a permeable membrane component under the action of osmotic pressure difference; the at least two flue gas compression cooling modules are used for compressing and cooling the concentrated flue gas for a plurality of times, so that carbon dioxide components in the concentrated flue gas reach a saturated state, and in the compression and cooling processes, different gases are separated by utilizing the difference of boiling points of the different gases, so that the principle of recycling carbon dioxide by a cryogenic method is adopted; the carbon dioxide liquefying module is used for carrying out gas-liquid separation on the concentrated flue gas and storing the obtained liquid carbon dioxide. The carbon dioxide capturing and liquefying system is used for recycling carbon dioxide by coupling the membrane filtration method and the cryogenic method, and is more energy-saving and environment-friendly than a common carbon dioxide system.
When carbon dioxide is recovered by the carbon dioxide capturing and liquefying system, LNG cold energy is transmitted to any smoke compression cooling module by the LNG cold energy recycling system in a gradient mode, so that cold energy and concentrated smoke in the smoke compression cooling module are subjected to heat exchange, LNG cold energy generated in the using process of the gas turbine unit can be fully recycled, gradient utilization of energy is achieved, and cold energy pollution is avoided to a certain extent.
Furthermore, it may be considered in this embodiment that the flue gas purifying and cooling module includes a flue gas purifying device 9 and a third heat exchanger 3.3 that are sequentially connected, an inlet of the flue gas purifying device 9 is connected with an outlet flue P3 of the waste heat boiler, a flue gas outlet pressure of the gas-steam combined cycle waste heat boiler is substantially normal pressure, and a temperature is generally not more than 180 ℃.
Still further, it is also contemplated 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.
Still further, it is also contemplated 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 the smoke exhaust path 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 structure, the inner-layer barrel structure is used for installing a permeable membrane module, the permeable membrane module comprises a carbon dioxide filtering membrane 401 and a gas filtering membrane 402, wherein the carbon dioxide filtering membrane 401 only allows carbon dioxide to pass through, the gas filtering membrane 402 allows gases except carbon dioxide to pass through, and flue gas entering the CO2 concentration device realizes gas separation under the action of pressure.
Still further, it may 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 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 and cooling module, and the cold energy in the LNG cold energy recovery system is conveyed in a step utilization mode.
In the embodiment, at least two flue gas compression and cooling modules are arranged in the carbon dioxide capturing and liquefying 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 the LNGP6 is connected with at least two cold energy pipelines in parallel, the number of the cold energy pipelines is the same as that 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 capturing and liquefying system is provided with a 1 st, a 2 … … N-1 and an N flue gas compression and cooling module, an outlet of the LNGP6 is connected with a 1 st, a 2 … … N-1 and an N cold energy pipeline in parallel, the 1 st cold energy pipeline of the LNGP6 is connected with a gas inlet of the 1 st heat exchanger, a gas outlet of the 1 st heat exchanger and the 2 nd cold energy pipeline form a parallel pipeline to be connected with a gas inlet of the 2 nd heat exchanger … …, and the gas outlet of the N-1 st heat exchanger and the N cold energy pipeline form a parallel pipeline to be connected with the gas inlet of the N heat exchanger, so that the gradient utilization of energy is realized, and the generation of cold energy pollution is avoided to a certain extent.
Example 2:
example 2 of the present invention is further modified on the basis of example 1 so as to fully exert technical advantages of the present invention, which will be exemplified below.
For example: when the number of the smoke compression cooling modules is two, the smoke compression cooling modules are respectively a first smoke compression cooling module and a second smoke compression cooling module which are connected in sequence;
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 connected in sequence; the concentrated flue gas outlet of the second heat exchanger 3.2 is connected with the inlet of the first compressor 1.1.
Still further, it may be considered in this embodiment that the carbon dioxide liquefying module includes a gas-liquid separator 7 and a CO2 liquid storage tank 8 that are sequentially connected, the concentrated flue gas outlet of the first heat exchanger 3.1 is connected to the concentrated gas inlet of the gas-liquid separator 7, the liquefied carbon dioxide outlet of the gas-liquid separator 7 is connected to the CO2 liquid storage tank 8, and the non-condensable gas outlet of the gas-liquid separator 7 is connected to the non-condensable gas inlet of the second heat exchanger 3.2.
Still further, it may be considered in this embodiment that the 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 6.2, and the second cold energy pipeline is provided with a first flow valve 6.1.
Still further, it is also contemplated 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 pipe, and the gas outlet of the first heat exchanger 3.1 is connected to the gas inlet of the second heat exchanger 3.2 through a parallel node (forming a parallel pipeline), 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 combustor inlet P4.
In this embodiment, the device flow is:
the exhaust-heat boiler outlet flue P3 is connected with an inlet of the flue gas purification device 9, an outlet of the flue gas purification device 9 is connected with a flue gas side inlet of the third heat exchanger 3.3, a flue gas side outlet of the third heat exchanger 3.3 is connected with an inlet of the flue gas drying device 5, an outlet of the flue gas drying device 5 is connected with an inlet of the third compressor 1.3, an outlet of the third compressor 1.3 is connected with an inlet of the CO2 concentration device 4, an exhaust gas outlet of the CO2 concentration device 4 is connected with the flue gas P5, a carbon dioxide outlet of the CO2 concentration device 4 is connected with a concentrated flue gas inlet of the second heat exchanger 3.2, a concentrated flue gas outlet of the second heat exchanger 3.2 is connected with an inlet of the first compressor 1.1, an outlet of the first heat exchanger 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 flue gas inlet of the third heat exchanger 1.3, a liquefied carbon dioxide outlet of the gas separator 7 is connected with the CO2 reservoir 8, a non-gas outlet of the gas separator 7 is connected with a non-heat exchanger 3.2 inlet of the second heat exchanger 6.2, a gas outlet of the first heat exchanger 6.6 is connected with a gas inlet of the second heat exchanger 3.6.2, and a gas outlet of the first heat exchanger 6.6 is connected with a gas inlet of the first heat exchanger 6.6.1, and a gas flow rate of the gas exchange valve is connected with the first heat exchanger 6.6.6, and the gas flow of the gas exchange valve is connected with the first heat exchanger 2 is connected with the inlet of the gas 2.
Furthermore, in this embodiment, it may be considered that the power sources of the first compressor 1.1, the second compressor 1.2 and the third compressor 1.3 come from the main steam pipeline P1 of the waste heat boiler, the compressors are driven by the rotational kinetic energy generated by the main steam pipeline P1 of the waste heat boiler through the small steam turbine 2, and the steam after working is discharged into the condenser P2.
Example 3:
the method for utilizing the LNG cold energy-based gas turbine set carbon dioxide capturing and liquefying system comprises a carbon dioxide capturing and liquefying process and an LNG cold energy recycling process;
wherein: as shown in fig. 2, fig. 2 is a schematic flow chart of a carbon dioxide capturing and liquefying process in the present embodiment, the carbon dioxide capturing and liquefying process includes the steps of:
step one (S210): the flue gas from the exhaust-heat boiler flue P3 enters a third heat exchanger 3.3 for cooling after removing impurities through a flue gas purifying device 9;
step two (S220): the flue gas cooled by the third heat exchanger 3.3 enters the flue gas drying equipment 5, and the flue gas dried by the flue gas drying equipment 5 enters the third compressor 1.3 for compression and pressure boosting;
step three (S230): the flue gas compressed and boosted by the third compressor 1.3 enters the CO2 membrane concentration equipment 4, the CO2 membrane concentration equipment 4 adopts a permeable membrane component to promote 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 (S240): 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 (S250): the cooled concentrated flue gas is discharged into a first compressor 1.1, and the concentrated flue gas compressed and boosted by the first compressor 1.1 enters a first heat exchanger 3.1 for further cooling to enable carbon dioxide components in the concentrated flue gas to reach a saturated state;
step six (S260): discharging the cooled concentrated flue gas into a gas-liquid separator 7 for gas-liquid separation, and flowing the liquid carbon dioxide separated by the gas-liquid separator 7 to a liquid storage tank 8 for storage through a pipeline;
step seven (S270): the gaseous substances obtained by the gas-liquid separator 7 are discharged into a unit smoke exhaust flue P5 after the excessive cold energy is recovered by the second heat exchanger 3.2;
as shown in fig. 3, fig. 3 is a schematic flow chart of an LNG cold energy recovery process in the present embodiment, and the LNG cold energy recovery process includes the following steps:
step one (S310): liquefied natural gas from the LNGP6 is respectively introduced into the first flow valve 6.1 and the second flow valve 6.2 through parallel pipelines, and the liquefied natural gas through the second flow valve 6.2 enters the first heat exchanger 3.1 for heating and vaporization;
step two (S320): the liquefied gas after temperature rising is mixed with the liquefied gas passing through the first flow valve 6.1 for temperature regulation and then is introduced into the second heat exchanger 3.2, the liquefied gas after temperature rising through the second heat exchanger 3.2 enters the third heat exchanger 3.3 for further temperature rising and vaporization, and finally enters the combustion chamber P4 of the gas turbine.
Furthermore, in this embodiment, it may be considered that the carbon dioxide capturing and liquefying process and the LNG cold energy recovering process are performed simultaneously, and the power sources of the compressors in the flue gas drying and compressing module and the flue gas compressing and cooling module come from the main steam pipeline P1 of the waste heat boiler.
In this embodiment, the process flow is as follows:
the flue gas from exhaust-heat boiler flue P3 gets into third heat exchanger 3.3 after getting rid of impurity through flue gas purification device 9 and cools down, and flue gas after the cooling of third heat exchanger 3.3 gets into flue gas drying equipment 5, and flue gas after the drying of flue gas drying equipment 5 gets into third compressor 1.3, gets into CO2 membrane concentration equipment 4 after the compression of third compressor 1.3 is risen, is equipped with osmotic membrane module or CO2 separation membrane in the CO2 membrane concentration equipment 4, adopts osmotic membrane module to promote the carbon dioxide concentration in the flue gas under osmotic pressure difference effect, and other gases that this process produced are discharged into unit flue gas P5. 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 the first heat exchanger 3.1 for further cooling, 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 separated by the gas-liquid separator 7 flows into a liquid storage tank 8 for storage through a pipeline, gaseous substances obtained by the gas-liquid separator 7 are discharged into a unit smoke exhaust flue P4 after redundant cold energy is recovered by the second heat exchanger 3.2, and the compressor is driven by rotational kinetic energy generated by working of a waste heat boiler main steam pipeline P1 and is discharged into a condenser P2 after working.
LNG cold energy recovery system adopts cold energy to come from the LNG P6 gasification process of gas turbine power plant, and the liquefied natural gas that comes from LNG P6 is through parallelly connected pipeline respectively lets in first flow valve 6.1 and second flow valve 6.2, and the liquefied natural gas that goes through second flow valve 6.2 gets into first heat exchanger 3.1 and heats vaporization, and the liquefied gas after the intensification is mixed with the liquefied gas that goes through first flow valve 6.1 and is transferred into second heat exchanger 3.2 after the temperature adjustment, further heats vaporization second heat exchanger 3.2, gets into third heat exchanger 3.3 after the second heat exchanger 3.2 heats up and further heats vaporization and gets into gas turbine combustion chamber P4.
The foregoing examples illustrate the invention in detail, but are merely preferred embodiments of the invention and are not to be construed as limiting the scope of the invention. All equivalent changes and modifications within the scope of the present invention are intended to be covered by the present invention.

Claims (10)

1. Gas unit carbon dioxide entrapment liquefaction system based on LNG cold energy, its characterized in that: comprising 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 smoke compression cooling module in a gradient mode and is used for carrying out heat exchange with concentrated smoke in the smoke compression cooling module.
2. The LNG cold energy based gas turbine train carbon dioxide capture liquefaction system of claim 1, wherein: the flue gas purifying and cooling module comprises a flue gas purifying device (9) and a third heat exchanger (3.3) which are sequentially connected, and an inlet of the flue gas purifying device (9) is connected with an outlet flue (P3) of the waste heat boiler.
3. The LNG cold energy based gas turbine train carbon dioxide capture liquefaction system of claim 2, wherein: 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 train carbon dioxide capture liquefaction system of claim 3, wherein: the carbon dioxide concentration module comprises CO2 concentration equipment (4), an inlet of the CO2 concentration equipment (4) is connected with an outlet of the third compressor (1.3), an exhaust gas outlet of the CO2 concentration equipment (4) is connected with an exhaust flue (P5), and a carbon dioxide outlet of the CO2 concentration equipment (4) is connected with the flue gas compression cooling module.
5. The LNG cold energy based gas turbine train carbon dioxide capture liquefaction system of any one of claims 1-4, wherein: concentrated flue gas in the carbon dioxide entrapment 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 in the LNG cold energy recovery system is opposite with the direction of delivery of concentrated flue gas in the flue gas compression cooling module.
6. The LNG cold energy based gas turbine train carbon dioxide capture liquefaction system of claim 5, wherein: when the number of the smoke compression cooling modules is two, the smoke compression cooling modules are respectively a first smoke compression cooling module and a second smoke compression cooling module which are connected in sequence;
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 connected in sequence;
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 train carbon dioxide capture liquefaction system of claim 6, wherein: the carbon dioxide liquefying module comprises a gas-liquid separator (7) and a CO2 liquid storage tank (8) which are sequentially connected, a concentrated flue gas outlet of the first heat exchanger (3.1) is connected with a concentrated gas inlet of the gas-liquid separator (7), and a liquefied carbon dioxide outlet of the gas-liquid separator (7) is connected with the CO2 liquid storage tank (8).
8. The LNG cold energy based gas turbine train carbon dioxide capture liquefaction system of claim 7, wherein: the export of LNG (P6) has parallelly connected 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, the gas entry of first heat exchanger (3.1) links to each other with the export of LNG (P6) through first cold energy pipeline, the gas export of first heat exchanger (3.1) and the parallelly connected node connection of second cold energy pipeline and link to each other with the gas entry of second heat exchanger (3.2).
9. The method for capturing and liquefying a gas turbine set carbon dioxide based on LNG cold energy by using the LNG cold energy as claimed in claim 8, which is characterized in that: the method comprises a carbon dioxide capturing and liquefying process and an LNG cold energy recycling process;
wherein: the carbon dioxide capturing and liquefying process comprises the following steps:
step one: the flue gas from the exhaust-heat boiler flue (P3) enters a third heat exchanger (3.3) for cooling after impurities are removed by a flue gas purifying device (9);
step two: the flue gas cooled by the third heat exchanger (3.3) enters the flue gas drying equipment (5), and the flue gas dried by the flue gas drying equipment (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 CO2 membrane concentration equipment (4), the CO2 membrane concentration equipment (4) adopts a permeable membrane component to promote 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 enters a second heat exchanger (3.2) for cooling after being compressed and boosted by the second compressor (1.2);
step five: the cooled concentrated flue gas is discharged into a first compressor (1.1), and the concentrated flue gas compressed and boosted by the first compressor (1.1) enters a first heat exchanger (3.1) for further cooling to enable carbon dioxide components in the concentrated flue gas to reach a saturated state;
step six: discharging the cooled concentrated flue gas into a gas-liquid separator (7) for gas-liquid separation, and flowing the liquid carbon dioxide separated by the gas-liquid separator (7) to a liquid storage tank (8) for storage through a pipeline;
step seven: the gaseous substances obtained by the gas-liquid separator (7) are discharged into a smoke exhaust flue (P5) of the unit after the excessive cold energy is recovered by the second heat exchanger (3.2);
the LNG cold energy recovery process comprises the following steps:
step one: 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, and the liquefied natural gas which passes through the second flow valve (6.2) enters a first heat exchanger (3.1) for heating and vaporization;
step two: the liquefied gas after temperature rising is mixed with the liquefied gas passing through the first flow valve (6.1) for temperature regulation and then is introduced into the second heat exchanger (3.2), the liquefied gas after temperature rising through the second heat exchanger (3.2) enters the third heat exchanger (3.3) for further temperature rising and vaporization, and finally enters the combustion chamber (P4) of the gas turbine.
10. The method according to claim 9, wherein: the carbon dioxide capturing and liquefying process and the LNG cold energy recycling process are synchronously carried out, and the power sources of the compressors in the flue gas drying and compressing module and the flue gas compressing and cooling module come from a main steam pipeline (P1) of the waste heat boiler.
CN202210422420.3A 2022-04-21 2022-04-21 Gas turbine unit carbon dioxide capturing and liquefying system and method based on LNG cold energy Pending CN116972598A (en)

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