CN115263466A - Low-temperature carbon capture coupling cold energy and waste heat cascade utilization system of LNG power ship - Google Patents

Low-temperature carbon capture coupling cold energy and waste heat cascade utilization system of LNG power ship Download PDF

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Publication number
CN115263466A
CN115263466A CN202210819925.3A CN202210819925A CN115263466A CN 115263466 A CN115263466 A CN 115263466A CN 202210819925 A CN202210819925 A CN 202210819925A CN 115263466 A CN115263466 A CN 115263466A
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China
Prior art keywords
stage
flue gas
lng
heat
heat exchanger
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CN202210819925.3A
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Chinese (zh)
Inventor
姚寿广
李辰
乔鑫
张�成
金楹杰
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Jiangsu University of Science and Technology
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Jiangsu University of Science and Technology
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Priority to CN202210819925.3A priority Critical patent/CN115263466A/en
Priority to PCT/CN2022/126053 priority patent/WO2024011780A1/en
Publication of CN115263466A publication Critical patent/CN115263466A/en
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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F02—COMBUSTION ENGINES; HOT-GAS OR COMBUSTION-PRODUCT ENGINE PLANTS
    • F02M—SUPPLYING COMBUSTION ENGINES IN GENERAL WITH COMBUSTIBLE MIXTURES OR CONSTITUENTS THEREOF
    • F02M21/00—Apparatus for supplying engines with non-liquid fuels, e.g. gaseous fuels stored in liquid form
    • F02M21/02—Apparatus for supplying engines with non-liquid fuels, e.g. gaseous fuels stored in liquid form for gaseous fuels
    • F02M21/0203—Apparatus for supplying engines with non-liquid fuels, e.g. gaseous fuels stored in liquid form for gaseous fuels characterised by the type of gaseous fuel
    • F02M21/0215—Mixtures of gaseous fuels; Natural gas; Biogas; Mine gas; Landfill gas
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/0002—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the fluid to be liquefied
    • F25J1/0027—Oxides of carbon, e.g. CO2
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    • F01K15/00—Adaptations of plants for special use
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    • F01K23/00—Plants characterised by more than one engine delivering power external to the plant, the engines being driven by different fluids
    • F01K23/02—Plants characterised by more than one engine delivering power external to the plant, the engines being driven by different fluids the engine cycles being thermally coupled
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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    • F01K—STEAM ENGINE PLANTS; STEAM ACCUMULATORS; ENGINE PLANTS NOT OTHERWISE PROVIDED FOR; ENGINES USING SPECIAL WORKING FLUIDS OR CYCLES
    • F01K25/00—Plants or engines characterised by use of special working fluids, not otherwise provided for; Plants operating in closed cycles and not otherwise provided for
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    • F01K25/14—Plants or engines characterised by use of special working fluids, not otherwise provided for; Plants operating in closed cycles and not otherwise provided for using special vapours using industrial or other waste gases
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    • F02G5/00—Profiting from waste heat of combustion engines, not otherwise provided for
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    • F25J1/0222—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using the cold stored in an external cryogenic component in an open refrigeration loop in combination with an intermediate heat exchange fluid between the cryogenic component and the fluid to be liquefied
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    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
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    • F25J1/0228—Coupling of the liquefaction unit to other units or processes, so-called integrated processes
    • F25J1/0229—Integration with a unit for using hydrocarbons, e.g. consuming hydrocarbons as feed stock
    • F25J1/023—Integration with a unit for using hydrocarbons, e.g. consuming hydrocarbons as feed stock for the combustion as fuels, i.e. integration with the fuel gas system
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    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
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    • 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
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    • F25J1/0275—Construction and layout of liquefaction equipments, e.g. valves, machines adapted for special use of the liquefaction unit, e.g. portable or transportable devices
    • F25J1/0277—Offshore use, e.g. during shipping
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    • F25J3/04084—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression of nitrogen
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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2210/00—Processes characterised by the type or other details of the feed stream
    • F25J2210/42—Nitrogen
    • 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
    • F25J2210/50—Oxygen
    • 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
    • F25J2210/58—Argon
    • 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
    • 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
    • F25J2240/90—Hot gas waste turbine of an indirect heated gas for power generation
    • 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
    • F25J2245/00—Processes or apparatus involving steps for recycling of process streams
    • F25J2245/58—Processes or apparatus involving steps for recycling of process streams the recycled stream being argon or crude argon
    • 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
    • F25J2260/00—Coupling of processes or apparatus to other units; Integrated schemes
    • F25J2260/80—Integration in an installation using carbon dioxide, e.g. for EOR, sequestration, refrigeration etc.

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  • Engineering & Computer Science (AREA)
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  • General Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Thermal Sciences (AREA)
  • Chemical & Material Sciences (AREA)
  • Combustion & Propulsion (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Ocean & Marine Engineering (AREA)
  • Engine Equipment That Uses Special Cycles (AREA)

Abstract

The invention discloses a low-temperature carbon capture coupling cold energy and waste heat cascade utilization system for an LNG power ship, which comprises an LNG evaporation side, wherein LNG is used as a cold source of a first two-stage cascade Rankine cycle and forms NG after first-stage pressurization, first-stage heat exchange, second-stage pressurization, second-stage heat exchange and seawater temperature regulation and is sent to an engine; preparing liquid oxygen at the air side by a low-temperature rectification method, reusing cold energy of an air separation product for air cooling and carbon capture, and sending the liquid oxygen to an engine after regasification; on the smoke side, smoke exhausted by the main engine provides heat energy for the second two-stage cascade Rankine cycle after acting through a waste gas turbine, water is separated and shunted after fourth-stage heat exchange and seawater cooling on the smoke side, one path of water is sent to an engine, and the other path of water is collected in a low-temperature liquefaction mode after being pressurized. According to the invention, a host oxygen-enriched combustion system is constructed under the condition of meeting the ship air inlet condition, so that the cold energy and the waste heat of a large ship can be fully recycled, and the carbon dioxide in the exhaust smoke can be efficiently trapped, thereby achieving the purposes of energy conservation and emission reduction.

Description

Low-temperature carbon capture coupling cold energy and waste heat cascade utilization system of LNG power ship
Technical Field
The invention relates to an energy utilization system of an LNG power ship, in particular to a low-temperature carbon capture coupling cold energy and waste heat gradient utilization system of the LNG power ship.
Background
A large amount of cold energy released by LNG in the vaporization process of the existing LNG power ship is almost directly taken away by seawater, energy waste is caused, and harm is caused to marine ecology at the same time, and a large amount of heat energy and kinetic energy of discharged flue gas are not fully utilized. In addition, although the LNG has obvious emission reduction effect as ship power fuel, the CO emitted by the whole ship industry is2The amount is still not insignificant.
Chinese patent publication No. CN113669175A proposes a low-temperature desublimation carbon capture system and method for tail gas of a marine natural gas engine, the system comprises an LNG gas supply system, a marine main engine combustion system, a carbon enrichment system and a low-temperature desublimation carbon capture system, more than 90% of high-concentration carbon-containing tail gas is enriched through an alcohol amine method, and cold energy in the LNG gasification process is combined to realize more than 95% of CO in normal-pressure tail gas2Capture sequestration, but the system employs chemical absorption to enrich CO2Zero carbon emission cannot be realized, and the enrichment efficiency is reduced due to the difficult regeneration of the chemical adsorbentThe whole system consumes much energy and chemicals.
Chinese patent No. CN113738467a proposes an integrated system for power generation with carbon capture by using liquefied natural gas, which integrates LNG gasification, cold energy oxygen generation, oxygen-enriched power generation and carbon capture, so as to greatly reduce the energy consumption of the links of LNG gasification, oxygen generation and carbon capture, improve the utilization rate of LNG cold energy, improve the power generation efficiency, and realize zero-carbon emission power generation by injecting the captured carbon dioxide into the saline water at the bottom of the ground for storage. However, the system is applied to the land, the LNG flow is large enough to provide the cold energy required by the oxygen production and carbon capture processes, and the air intake flow of the LNG on the ship is far less than the flue gas flow, so that the requirement of the cold energy for oxygen production and carbon capture cannot be met, and the system is difficult to apply on the ship.
Disclosure of Invention
In view of the defects of the prior art, the invention aims to provide a low-temperature carbon capture coupling cold energy and waste heat cascade utilization system for an LNG power ship, which reduces low-carbon emission and energy consumption under the condition that the LNG cold quantity of the ship is relatively small.
The technical scheme of the invention is as follows: a LNG power ship low temperature carbon entrapment coupling cold energy and waste heat cascade utilization system includes:
at the LNG evaporation side, the LNG from the LNG storage tank is subjected to primary pressurization, primary LNG heat exchange, secondary pressurization, secondary LNG heat exchange and seawater temperature regulation to form NG, and then the NG is sent to a host;
on the smoke side, smoke discharged by the main machine is subjected to first-stage smoke expansion work, first-stage smoke heat exchange, second-stage smoke expansion work, second-stage smoke heat exchange, third-stage smoke heat exchange and seawater cooling, then water is separated through a first smoke water separator, the water is further divided into two paths, one path of the water is sent to the main machine, the other path of the water is subjected to fourth-stage smoke heat exchange and fifth-stage smoke heat exchange after sequentially passing through a smoke precooler, a second smoke water separator and a smoke compressor to complete low-temperature liquefaction and trapping, and the low-temperature liquefaction and trapping are sent to LCO2A storage tank;
the air side is a flow path for sequentially carrying out multistage cooling pressurization and two-stage rectification on air, waste nitrogen formed after the air is subjected to the two-stage rectification is used for carrying out multistage cooling pressurization on the air, the front-stage cooling except the final-stage cooling is carried out, heat energy is absorbed by a third-stage flue gas heat exchanger and then the air is used for doing work through a waste nitrogen turbine, waste argon formed after the air is subjected to the two-stage rectification is mixed with waste nitrogen discharged from the waste nitrogen turbine, then cold energy is sequentially provided for a flue gas precooler and a carbon capture heat exchanger and then the air is discharged, and liquid oxygen formed after the air is subjected to the two-stage rectification is used for carrying out final-stage cooling on the air and then is regasified in the carbon capture heat exchanger and sent to a host;
the system comprises a first-stage organic Rankine cycle power generation unit, a first-stage LNG heat exchange and re-pressurization loop, a second-stage LNG heat exchange loop and a first-stage organic Rankine cycle power generation unit, wherein a circulation loop of the first-stage organic Rankine cycle power generation unit is a loop which is heated by a second-stage circulating working medium in a first-stage circulating evaporator after being pressurized by a first-stage circulating working medium, and is expanded to work and then is pressurized again through the first-stage LNG heat exchange;
the circulating loop of the second-stage organic Rankine cycle power generation unit is a loop which is formed by pressurizing a second-stage circulating working medium, heating the pressurized second-stage circulating working medium by the flue gas from the flue gas compressor, performing expansion work, and then sequentially exchanging heat and repressurizing the second-stage circulating working medium by the first-stage circulating evaporator and the second-stage circulating seawater cooler;
the circulation loop of the third-stage organic Rankine cycle power generation unit is a loop which is subjected to heat exchange with the flue gas through a third-stage circulation preheater after the third-stage circulation working medium is pressurized, is subjected to second-stage flue gas heat exchange with the flue gas, is subjected to expansion work, and is subjected to heat exchange through a third-stage circulation seawater cooler and is then pressurized again; the system comprises a fourth-stage transcritical Rankine cycle power generation unit, wherein a circulation loop of the fourth-stage transcritical Rankine cycle power generation unit is a loop which is formed by pressurizing a fourth-stage transcritical Rankine cycle working medium, sequentially passing through a high-temperature cylinder sleeve cooling water preheating loop, a fourth-stage circulation heat regenerator for heat regeneration, sequentially carrying out first-stage flue gas heat exchange with flue gas, carrying out expansion and work application, sequentially passing through the fourth-stage circulation heat regenerator, a third-stage circulation preheater and a fourth-stage circulation seawater cooler for heat exchange, and then carrying out repressurization;
the LNG heat exchange of the first stage provides cold energy for LNG to a first stage organic Rankine cycle working medium, the LNG heat exchange of the second stage provides cold energy for LNG to a carbon capture heat exchanger, the flue gas heat exchange of the first stage provides heat energy for flue gas to a fourth stage Rankine cycle working medium, the flue gas heat exchange of the second stage provides heat energy for flue gas to a third stage Rankine cycle working medium, the flue gas heat exchange of the third stage provides heat energy for waste nitrogen after the flue gas is subjected to primary cooling on air, the flue gas heat exchange of the fourth stage releases heat energy to the second stage cycle working medium for flue gas after being compressed by a flue gas compressor, the flue gas heat exchange of the fifth stage releases heat energy to the carbon capture heat exchanger for flue gas, and in the carbon capture heat exchanger, the LNG after being pressurized by the second stage absorbs heat from the flue gas after being subjected to final stage cooling on air and the waste nitrogen and waste argon after being subjected to heat exchange by a flue gas precooler in the same direction as the flue gas after being subjected to heat exchange on the second stage cycle working medium.
The system further comprises a fifth-stage organic Rankine cycle power generation unit, wherein a cycle loop of the fifth-stage organic Rankine cycle power generation unit is a loop which is formed by pressurizing a fifth-stage cycle working medium, exchanging heat through a fifth-stage cycle heat regenerator, heating the fifth-stage cycle working medium by high-temperature cylinder jacket cooling water, performing expansion work, and then sequentially exchanging heat through the fifth-stage cycle heat regenerator and cooling the waste nitrogen and waste argon from the carbon capture heat exchanger for re-pressurization.
The system further comprises a sixth-stage organic Rankine cycle power generation unit, wherein a circulation loop of the sixth-stage organic Rankine cycle power generation unit is a loop which is heated by the flue gas after heat exchange of the second-stage flue gas after the sixth-stage circulating working medium is pressurized, expanded to do work and then subjected to heat exchange through a sixth-stage seawater cooler and then repressurized; and carrying out third-stage flue gas heat exchange on the flue gas heated by the pressurized sixth-stage circulating working medium.
Further, LNG evaporation side is including LNG storage tank, first order LNG booster pump, LNG heat exchanger, second grade LNG booster pump, carbon capture heat exchanger, sea water thermoregulator and the host computer that connects gradually, the exit linkage of first order LNG booster pump the cold source input of LNG heat exchanger, the cold source output of LNG heat exchanger is connected the input of second grade LNG booster pump, the output of second grade LNG booster pump is connected the first cold source input of carbon capture heat exchanger, the input of sea water thermoregulator is connected to the first cold source output of carbon capture heat exchanger, first order LNG heat transfer is in the LNG heat exchanger goes on.
Further, the flue gas side is including the first order flue gas turbine, first order flue gas heat exchanger, second grade flue gas turbine, second grade flue gas heat exchanger, fourth grade flue gas heat exchanger, third grade flue gas heat exchanger, sea water cooler, first flue gas water separator, the flue gas shunt that connects gradually, the flue gas shunt shunts out is connected to boats and ships host computer directly all the way, and another way is including flue gas precooler, second flue gas water separator, flue gas compressor, second grade circulation evaporator, carbon entrapment heat exchanger and LCO that connect gradually2The storage tank, first order gas heater carries out first order flue gas heat transfer, second level gas heater carries out second level gas heat transfer, the sixth level cycle working medium after the flue gas heating pressure boost in the fourth level gas heater after by the second level gas heat transfer, third level gas heater carries out third level gas heat transfer, the second level circulation evaporimeter carries out the fourth level gas heat transfer, the carbon entrapment heat exchanger carries out the fifth level gas heat transfer.
The air side comprises an air filter, a first-stage cooler, an air-water separator, a second-stage cooler, a first-stage compressor, a third-stage cooler, a second-stage compressor, a fourth-stage cooler, an air throttle valve, a first-stage rectifying tower and a second-stage rectifying tower which are sequentially connected, a waste nitrogen flow path output by an upper tower of the first-stage rectifying tower comprises a third-stage cooler, a second-stage cooler, a first-stage cooler, a third-stage flue gas heat exchanger, a waste nitrogen turbine and a waste nitrogen and waste argon collector which are sequentially connected, the other input end of the waste nitrogen and waste argon collector is connected with the output end of the upper tower of the second-stage rectifying tower, the waste nitrogen and waste argon flow path output by the waste nitrogen and waste argon collector comprises a flue gas precooler and a carbon capture heat exchanger which are sequentially connected, the output end of the flue gas precooler is connected with the third input end of the carbon capture heat exchanger, the fourth-stage flow path of oxygen output by a lower tower of the second-stage rectifying tower comprises a second cooler, an oxygen throttle valve, a carbon capture heat exchanger and a ship cold source which are sequentially connected with the output end of the second-carbon capture heat exchanger.
Further, the working temperature range of the first-stage circulating working medium in the first-stage organic Rankine cycle is-100-70 ℃, the working temperature range of the second-stage circulating working medium in the second-stage organic Rankine cycle is 25-150 ℃, the working temperature range of the third-stage circulating working medium in the third-stage organic Rankine cycle is 25-115 ℃, the working temperature range of the fourth-stage circulating working medium in the fourth-stage transcritical Rankine cycle is 25-261 ℃, the working temperature range of the fifth-stage circulating working medium in the fifth-stage organic Rankine cycle is 0-85 ℃, and the working temperature range of the sixth-stage circulating working medium in the sixth-stage organic Rankine cycle is 25-90 ℃.
Further, the first-stage cycle working medium is R1150, the second-stage cycle working medium is n-Pentane, the third-stage cycle working medium is R600, and the fourth-stage cycle working medium is CO2The fifth-stage cycle working medium is R600, and the sixth-stage cycle working medium is n-Pentane.
Under the condition of meeting the air inlet condition of the main engine, the invention constructs the oxygen-enriched combustion system of the main engine to ensure that the smoke exhaust component is only H2O、CO2And a small amount of Ar, thereby omitting the separation of CO in the prior art scheme2Can efficiently trap CO in exhaust gas2Meanwhile, the invention realizes the dual purposes of energy saving and emission reduction by utilizing the waste heat and cold energy of the ship in a gradient way, and has the advantages compared with the prior art that:
1. the method is applied to a ship application scene, and under the condition that the air intake of the ship is met, the single-stage organic Rankine cycle, the transcritical Rankine cycle and the two-stage cascade Rankine cycle are reasonably constructed between cold sources and heat sources to carry out cascade utilization on the cold energy and the waste heat of the ship based on the principle of temperature contra-aperture and cascade utilization.
2. Constructing an oxygen-enriched combustion system around a ship main engine to obtain CO with high concentration2The flue gas saves the step of separation and purification in the prior art method, and is easier to capture; cooling the air separation productAnd the carbon is recycled for air cooling, flue gas cooling and carbon capture, so that the energy consumption of the whole ship is reduced.
Drawings
Fig. 1 is a schematic structural diagram of a low-temperature carbon capture coupled cold energy and waste heat cascade utilization system of an LNG-powered ship according to an embodiment of the present invention.
Detailed Description
The present invention is further described in the following examples, which are intended to be illustrative only and not to be limiting as to the scope of the invention, which is to be given the full breadth of the appended claims and any and all equivalent modifications within the scope of the following claims.
Referring to fig. 1, a low-temperature carbon capture coupled cold energy and waste heat cascade utilization system for an LNG-powered ship according to an embodiment of the present invention includes:
the LNG evaporation side comprises an LNG storage tank 1, a first-stage LNG booster pump 2, an LNG heat exchanger 3, a second-stage LNG booster pump 4, a carbon capture heat exchanger 5, a seawater thermostat 6 and a marine main engine 7 which are sequentially connected through pipelines, wherein an outlet of the first-stage LNG booster pump 2 is connected with a cold source input end 301 of the LNG heat exchanger 3, a cold source output end 302 of the LNG heat exchanger 3 is connected with an inlet of the second-stage LNG booster pump 4, an outlet of the second-stage LNG booster pump 4 is connected with a first cold source input end 501 of the carbon capture heat exchanger 5, and a first cold source output end 502 of the carbon capture heat exchanger 5 is connected with an input end of the seawater thermostat 6.
The flue gas side comprises a first-stage flue gas turbine 8, a first-stage flue gas heat exchanger 9, a second-stage flue gas turbine 10, a second-stage flue gas heat exchanger 11, a fourth-stage flue gas heat exchanger 12, a third-stage flue gas heat exchanger 13, a seawater cooler 14, a first flue gas water separator 15 and a flue gas splitter 16 which are sequentially connected through a pipeline, one path of the split flow of the flue gas splitter 16 is directly connected to a ship host 7, and the other path of the split flow of the flue gas splitter comprises a flue gas precooler 17, a second flue gas water separator 18, a flue gas compressor 19, a second-stage circulating evaporator 20, a carbon capture heat exchanger 5 and an LCO (liquid crystal oxygen demand)2A storage tank 21, wherein the outlet of the first stage flue gas turbine 8 is connected with the heat source input end 903 of the first stage flue gas heat exchanger 9, and the heat source output of the first stage flue gas heat exchanger 9The outlet 904 of the second stage flue gas turbine 10 is connected to the inlet of the second stage flue gas turbine 10, the outlet of the second stage flue gas turbine 10 is connected to the heat source input 1103 of the second stage flue gas heat exchanger 11, the heat source output 1104 of the second stage flue gas heat exchanger 11 is connected to the heat source input 1203 of the fourth stage flue gas heat exchanger 12, the heat source output 1204 of the fourth stage flue gas heat exchanger 12 is connected to the heat source input 1303 of the third stage flue gas heat exchanger 13, the heat source output 1304 of the third stage flue gas heat exchanger 13 is connected to the input of the seawater cooler 14, the gas output of the first flue gas water separator 15 is connected to the input of the flue gas splitter 16, one path of the output of the flue gas splitter 16 is connected to the ship host 7, the other path is connected to the heat source input 1703 of the flue gas precooler 17, the heat source output 1704 of the flue gas precooler 17 is connected to the output of the second flue gas water separator 18, the outlet of the flue gas compressor 19 is connected to the heat source input 2003 of the second stage circulating evaporator 20, the heat source output 2004 of the second stage circulating evaporator 20 is connected to the heat source input 507 of the carbon capture heat exchanger 5, and the heat source output 507 of the carbon capture heat exchanger is connected to the LCO2 A storage tank 21.
The air side comprises an air filter 22, a first-stage cooler 23, an air-water separator 24, a second-stage cooler 25, a first-stage compressor 26, a third-stage cooler 27, a second-stage compressor 28, a fourth-stage cooler 29, an air throttle valve 30, a first-stage rectifying tower 31 and a second-stage rectifying tower 32 which are sequentially connected through pipelines, a flow path of waste nitrogen output by an upper tower of the first-stage rectifying tower 31 comprises the third-stage cooler 27, the second-stage cooler 25, the first-stage compressor 23, a third-stage flue gas heat exchanger 13, a waste nitrogen turbine 33 and a waste nitrogen and waste argon collector 34 which are sequentially connected through pipelines, the other input end of the waste nitrogen and waste argon collector 34 is connected with an upper tower output end of the second-stage rectifying tower 32, the flow path of waste nitrogen and waste argon output by the waste argon collector 34 comprises a flue gas precooler 17, a carbon capture heat exchanger 5 and a fifth-stage circulating condenser 35 which are sequentially connected through pipelines, and a flow path of oxygen output by a lower tower of the second-stage rectifying tower 32 comprises the fourth-stage cooler 29, the oxygen throttle valve 36, the carbon capture heat exchanger 5 and a host 7 which are sequentially connected through pipelines. Wherein the output end of the air filter 22 is connected to the heat source input end 2303 of the first stage cooler 23, the heat source output end 2304 of the first stage cooler 23 is connected to the input end of the air-water separator 24, the gas output end of the air-water separator 24 is connected to the heat source input end 2503 of the second stage cooler 25, the heat source output end 2504 of the second stage cooler 25 is connected to the inlet of the first stage compressor 26, the outlet of the first stage compressor 26 is connected to the heat source input end 2703 of the third stage cooler 27, the heat source output end 2704 of the third stage cooler 27 is connected to the inlet of the second stage compressor 28, the outlet of the second stage compressor 28 is connected to the heat source input end 2903 of the fourth stage cooler 29, the heat source output end 2904 of the fourth stage cooler 29 is connected to the first stage rectifying tower 31 through the air throttle valve 30, the lower tower output end of the first stage rectifying tower 31 is connected to the second stage rectifying tower 32, the upper tower output end of the first-stage rectifying tower 31 is connected with a cold source input end 2701 of a third-stage cooler 27, a cold source output end 2702 of the third-stage cooler 27 is connected with a cold source input end 2501 of a second-stage cooler 25, a cold source output end 2502 of the second-stage cooler 25 is connected with a cold source input end 2301 of a first-stage cooler 23, a cold source output end 2302 of the first-stage cooler 23 is connected with a cold source input end 1301 of a third-stage flue gas heat exchanger 13, a cold source output end 1302 of the third-stage flue gas heat exchanger 13 is connected with an inlet of a waste nitrogen turbine 33, an output end of a waste nitrogen and waste argon current collector 34 is connected with a cold source input end 1701 of a flue gas precooler 17, a cold source output end 1702 of the flue gas precooler 17 is connected with a third cold source input end 505 of a carbon trapping heat exchanger 5, and a cold source output end 506 of the carbon trapping heat exchanger 5 is connected with an input end 3501 of a fifth-stage circulating condenser 35, the lower tower output end of the second stage rectification tower 32 is connected with the cold source input end 2901 of the fourth stage cooler 29, the cold source output end 2902 of the fourth stage cooler 29 is connected with the second cold source input end 503 of the carbon capture heat exchanger 5 through the oxygen throttle valve 36, and the second cold source output end 504 of the carbon capture heat exchanger 5 is connected with the marine main engine 7.
The first-stage organic Rankine cycle power generation unit is a circulation loop formed by connecting a first-stage circulating working medium pump 38, a first-stage circulating evaporator 39, a first-stage circulating turbine 37 and an LNG heat exchanger 3, wherein an outlet of the first-stage circulating working medium pump 37 is connected with a heat source input end 303 of the LNG heat exchanger 3, a heat source output end 304 of the LNG heat exchanger 5 is connected with an inlet of the first-stage circulating working medium pump 38, an outlet of the first-stage circulating working medium pump 38 is connected with a cold source input end 3901 of the first-stage circulating evaporator 39, and a cold source output end 3902 of the first-stage circulating evaporator 39 is connected with an inlet of the first-stage circulating turbine 37.
The second-stage organic Rankine cycle power generation unit is a circulation loop formed by connecting a second-stage circulating working medium pump 42, a second-stage circulating evaporator 20, a second-stage circulating turbine 40, a first-stage circulating evaporator 39 and a second-stage circulating seawater cooler 41, an outlet of the second-stage circulating turbine 40 is connected with a heat source input end 3903 of the first-stage circulating evaporator 39, a heat source output end 3904 of the first-stage circulating evaporator 39 is connected with an input end of the second-stage circulating seawater cooler 41, an outlet of the second-stage circulating working medium pump 42 is connected with a cold source input end 2001 of the second-stage circulating evaporator 20, and a cold source output end 2002 of the second-stage circulating evaporator 20 is connected with an inlet of the second-stage circulating turbine 40.
The third-stage organic Rankine cycle power generation unit comprises a circulation loop formed by connecting a third-stage circulating working medium pump 55, a third-stage circulating preheater 49, a second-stage flue gas heat exchanger 11, a third-stage circulating turbine 53 and a third-stage seawater cooler 54, wherein an outlet of the third-stage circulating turbine 53 is connected with an input end of the third-stage circulating seawater cooler 54, an output end of the third-stage circulating seawater cooler 54 is connected with an inlet of the third-stage circulating working medium pump 55, an outlet of the third-stage circulating working medium pump 55 is connected with a cold source input end 4901 of the third-stage circulating preheater 49, a cold source output end 4902 of the third-stage circulating preheater 49 is connected with a cold source input end 1101 of the second-stage flue gas heat exchanger 11, and a cold source output end 1102 of the second-stage flue gas heat exchanger 11 is connected with an inlet of the third-stage circulating turbine 53.
The fourth-stage transcritical Rankine cycle power generation unit comprises a fourth-stage circulating working medium pump 51, a fourth-stage circulating preheater 52, a fourth-stage circulating heat regenerator 48, a first-stage flue gas heat exchanger 9, a fourth-stage circulating turbine 47, a third-stage circulating preheater 49 and a fourth-stage circulating seawater cooler 50 which are connected to form a circulating loop, an outlet of the fourth-stage circulating turbine 47 is connected with a heat source input end 4803 of the fourth-stage circulating heat regenerator 48, a heat source output end 4804 of the fourth-stage circulating heat regenerator 48 is connected with a heat source input end 4903 of the third-stage circulating preheater 49, a heat source output end 4904 of the third-stage circulating preheater 49 is connected with an input end of the fourth-stage circulating seawater cooler 50, an output end of the fourth-stage circulating seawater cooler 50 is connected with an inlet of the fourth-stage circulating working medium pump 51, an outlet of the fourth-stage circulating working medium pump 51 is connected with a cold source input end 5201 of the fourth-stage circulating preheater 52, a cold source output end 5202 of the fourth-stage circulating heat regenerator 52 is connected with an input end 4801 of the fourth-stage circulating heat regenerator 48, an output end 4802 of the fourth-stage circulating heat regenerator 48 is connected with an inlet end 901 of the fourth-stage flue gas cold source of the fourth-stage circulating heat exchanger 902 of the fourth-stage circulating heat regenerator 47.
The fifth-stage organic Rankine cycle power generation unit is a circulation loop formed by connecting a fifth-stage circulating working medium pump 45, a fifth-stage circulating heat regenerator 44, a fifth-stage circulating evaporator 46, a fifth-stage circulating turbine 43 and a fifth-stage circulating condenser 35, wherein an outlet of the fifth-stage circulating turbine 43 is connected with a heat source input end 4403 of the fifth-stage circulating heat regenerator 44, a heat source output end 4404 of the fifth-stage circulating heat regenerator 44 is connected with a heat source input end 3503 of the fifth-stage circulating condenser 35, a heat source output end 3504 of the fifth-stage circulating condenser 35 is connected with an inlet of the fifth-stage circulating working medium pump 45, an outlet of the fifth-stage circulating working medium pump 45 is connected with a cold source input end 4401 of the fifth-stage circulating heat regenerator 44, a cold source output end 4402 of the fifth-stage circulating evaporator 44 is connected with an input end 4601 of the fifth-stage circulating evaporator 46, and a cold source output end 4602 of the fifth-stage circulating evaporator 46 is connected with an inlet of the fifth-stage circulating turbine 43.
The sixth-stage organic Rankine cycle power generation unit is a circulation loop formed by connecting a sixth-stage circulating working medium pump 58, a fourth-stage flue gas heat exchanger 12, a sixth-stage circulating turbine 56 and a sixth-stage circulating seawater cooler 57, an outlet of the sixth-stage circulating turbine 56 is connected with an inlet of the sixth-stage circulating seawater cooler 57, an outlet of the sixth-stage circulating seawater cooler 57 is connected with an inlet of the sixth-stage circulating working medium pump 58, an outlet of the sixth-stage circulating working medium pump 58 is connected with a cold source input end 1201 of the fourth-stage flue gas heat exchanger 12, and a cold source output end 1202 of the fourth-stage flue gas heat exchanger 12 is connected with an inlet of the sixth-stage circulating turbine 56.
The working process of each part in the low-temperature carbon capture coupling cold energy and waste heat cascade utilization system of the LNG power ship is further described by combining 296600 tons of VLCC-LNG power ships. The LNG components in the LNG storage tank are 95% of methane, 3% of ethane and 2% of propane. The air comprises 78.1% of nitrogen, 20.9% of oxygen, 0.94% of argon, 0.03% of carbon dioxide and 0.03% of water vapor. The oxygen (non-pure oxygen) component introduced into the engine is 98.35 percent of oxygen and 1.65 percent of argon. As the oxygen introduced in the embodiment is not pure oxygen, the CO is recycled to realize zero carbon emission of the system2The components are regulated to be carbon dioxide 94.31%, argon 2.82% and water vapor 2.87%.
Description of process parameters:
LNG flow path: LNG (3000 kg/h,600kPa, -162 ℃) is discharged from an LNG storage tank 1, is pressurized to 15MPa (-154.3 ℃) for the first time by a first-stage LNG booster pump 2, and then exchanges heat with a first-stage circulating working medium (R1150, 150kPa, -51.43 ℃) to-91.08 ℃ in an LNG heat exchanger 3. Then the LNG is pressurized for the second time to 30Mpa (-75.82) by the second-stage LNG booster pump 4, and then enters the low-temperature carbon capture heat exchanger 5 for heat exchange and temperature rise to 0 ℃, and the LNG can utilize cold
Figure BDA0003743814960000081
And less, directly exchanging heat to 15 ℃ through a seawater temperature regulator 6 and sending to a ship main engine 7.
Flue gas flow: the flue gas (350 ℃,500kPa, 196070kg/h) discharged by the ship main engine 7 does work through a first-stage flue gas turbine 8 (the pressure at the outlet of the turbine is limited to be more than 150 kPa), and the flue gas (150kPa, 266 ℃) after doing work is in a first-stage flue gas heat exchanger 9 and a fourth-stage circulating working medium (CO) discharged by a fourth-stage circulating heat regenerator 482And the temperature is 126.9 ℃, the flue gas (150kPa, 144.4 ℃) after heat exchange is expanded by the second-stage flue gas turbine 10 to do work to 110kPa (123.6 ℃), and then the flue gas is subjected to heat exchange with a fifth-stage circulating working medium (R600, 80 ℃) discharged from a fifth-stage circulating preheater 49 in a second-stage flue gas heat exchanger 11 and cooled to 94.07 ℃.And then, providing heat for a sixth-stage Rankine cycle working medium (n-Pentane, 25.16 ℃) in a fourth-stage flue gas heat exchanger 12, cooling to 77.63 ℃, exchanging heat with waste nitrogen (623kPa, 8.114 ℃) in a third-stage flue gas heat exchanger 13 to 73.08 ℃, then exchanging heat to 25 ℃ through a seawater cooler 14, separating out most of water through a first flue gas water separator 15, dividing the water into two parts through a flue gas splitter 16, using one part as circulating flue gas to be sent to a ship host 7, and using the other part to carry out carbon capture on the circulating flue gas.
A trapping process: one path of trapped flue gas (9108 kg/h,110kPa,25 ℃) shunted by the flue gas shunt 16 exchanges heat with waste nitrogen (110 kPa, -70.45 ℃) discharged from a waste nitrogen and waste argon current collector 34 in the flue gas precooler 17 and is cooled to-52 ℃, the trapped flue gas (8995 kg/h) obtained after water is separated by the second flue gas water separator 18 is pressurized to 1950kPa (202.9 ℃) through a flue gas compressor 19, then exchanges heat with the second circulating working fluid (25.75 ℃) through the second circulating evaporator 20 and is cooled to 67.59 ℃, finally the trapped flue gas exchanges heat with oxygen (-110.8 ℃) through the carbon trapping heat exchanger 5, exchanges heat with the waste nitrogen (-50.19 ℃) and LNG (-75.82 ℃), and is liquefied at-36.5 ℃ and 1950kPa and is sent to LCO2 A storage tank 21.
And (3) air separation flow: air (25 ℃,110kPa, 52250kg/h) is filtered to remove impurities through an air filter 22, exchanges heat with waste nitrogen (-87.94 ℃,623 kPa) from a second-stage cooler 25 in a first-stage cooler 23, separates water through an air-water separator 24 after the temperature is reduced to-52 ℃, then exchanges heat with the waste nitrogen (-175.9 ℃,623kPa, vapor fraction 0.7356) from a third-stage cooler 27 in the second-stage cooler 25, reduces the temperature to-162 ℃, then is pressurized to 570kPa (-69.38 ℃) for one time through a first-stage compressor 26, and exchanges heat with the waste nitrogen (-176.1 ℃,623kPa, liquid fraction 1) from a fourth-stage cooler 29 in the third-stage cooler 27, and reduces the temperature to-162 ℃. Further pressurizing to 1600kPa (-109.5 ℃) in the second stage compressor 28 for the second time, then exchanging heat between the air and liquid oxygen (-182.7 ℃,112 kPa) discharged from the lower tower of the second stage rectifying tower 32 in a fourth stage cooler 29 to reduce the temperature to-157 ℃, and then passing through an air throttle valve 30 to reduce the pressure to 1200kPa, and reducing the temperature to-162 ℃. The air flowing out of the air throttle valve 30 enters a first-stage rectifying tower 31 for separation, and liquid oxygen (625 kPa, -1) flows out from the bottom61.7℃，O2The mole fraction 0.9546) and the waste nitrogen flowing out of the top (623 kPa, liquid phase fraction 1-176.1 ℃) are used as cold sources and sequentially enter a third-stage cooler 27, a second-stage cooler 25, a first-stage cooler 23 and a third-stage flue gas heat exchanger 13 to exchange heat and raise the temperature to 27 ℃, and then enter a waste nitrogen turbine 33 to expand and do work to 110kPa (-68.04 ℃). After the waste nitrogen after acting is mixed with waste argon discharged from the upper tower of the second-stage rectifying tower 32 through a waste nitrogen and waste argon current collector 34, the waste nitrogen and the collected flue gas (25 ℃) exchange heat in a flue gas precooler 17 and are heated to-50.19 ℃, the waste nitrogen enters a low-temperature carbon collection heat exchanger 5 to provide cold energy, and the discharged waste nitrogen (-17.89) is discharged after the cold energy is provided for a fifth-stage circulating working medium (R600, 8 ℃) in a fifth-stage circulating condenser 35 of the heat exchanger. Liquid oxygen discharged from the lower tower of the first-stage rectifying tower 31 enters a second-stage rectifying tower 32 for further separation and purification, waste argon (110 kPa, -192 ℃) flowing out of the top is mixed with the waste nitrogen through a waste nitrogen and waste argon collector 34, oxygen (112 kPa, -182.3 ℃, O2 mole fraction 0.9835, liquid fraction 1) flowing out of the bottom enters a fourth-stage cooler 29 to be used as a cold source for heat exchange, the temperature is increased to-110.8 ℃, the pressure is reduced to 110kPa through an oxygen throttle valve 36, and then the temperature is increased to 20 ℃ as the cold source for heat exchange in a carbon capture heat exchanger 5 and is sent to a ship host 7.
A first stage organic Rankine cycle: the first-stage circulating working medium (R1150, -51.43 ℃,150kPa, 1210kg/h) after the exhaust steam is processed by the first-stage circulating turbine 37 to perform heat exchange with LNG (-154.3) in an LNG heat exchanger 3 to-100 ℃, then is pressurized to 2000kPa (-98.69 ℃) by a first-stage circulating working medium pump 38, is subjected to heat exchange with a second-stage circulating working medium (94.25 ℃) in a first-stage circulating evaporator 39 to heat to 66 ℃, and finally is processed by the first-stage circulating turbine 37 to perform work, thereby completing a cycle.
A second-stage organic Rankine cycle: the second-stage circulating working medium (n-Pentane, 94.25 ℃,110kPa,2100 kg/h) after the exhaust steam which does work by the second-stage circulating turbine 40 exchanges heat with the first-stage circulating working medium (98.69 ℃) in the first-stage circulating evaporator 39 and is cooled to 36.87 ℃, then exchanges heat to 25 ℃ through the first-stage circulating seawater cooler 41, is pressurized to 1400kPa (25.75 ℃) through the second-stage circulating working medium pump 42, exchanges heat with the trapped flue gas (202.9 ℃) which is compressed by the flue gas compressor 19 in the second-stage circulating evaporator 20 and is heated to 150 ℃, and finally does work through the second-stage circulating turbine 40 to finish a cycle.
A third-stage organic Rankine cycle: after the exhaust steam is acted by the third stage circulation turbine 53, the fifth stage circulation working medium (R600, 66.54 ℃,250kPa, 15600kg/h) exchanges heat to 25 ℃ through the third stage circulation seawater cooler 54, is pressurized to 1500kPa (25.93 ℃) through the third stage circulation working medium pump 55, exchanges heat with the fourth stage circulation working medium (90 ℃) in the third stage circulation preheater 49, is heated to 80 ℃, further exchanges heat with the flue gas (123.6 ℃) in the second stage flue gas heat exchanger 11, is heated to 115 ℃, and finally acts through the third stage circulation turbine 53 to finish a cycle.
A fourth-stage transcritical rankine cycle: fourth-stage circulating working medium (CO) after dead steam is applied by the fourth-stage circulating turbine 472165.1 ℃,6750kPa, 126000kg/h) firstly exchanges heat to 90 ℃ in a fourth stage circulating heat regenerator 48, then exchanges heat with a third stage circulating working medium (R600, 25.93 ℃) pressurized by a third stage circulating working medium pump 55 in a third stage circulating preheater 49, reduces the temperature to 76.53 ℃, then exchanges heat to 25 ℃ through a fourth stage circulating seawater cooler 50, and then is pressurized to 20000kPa (53.7 ℃) by a fourth stage circulating working medium pump 51. Then, the fourth-stage circulating working medium exchanges heat with water cooled by high-temperature cylinder sleeve water (90 ℃) in a fourth-stage circulating preheater 52 to heat to 85 ℃, then regenerates heat to 126.9 ℃ in a fourth-stage circulating regenerator 48, finally exchanges heat with flue gas (266 ℃) in a first-stage flue gas heat exchanger 9 to heat to 260.5 ℃, and then works through a fourth-stage circulating turbine 47 to finish a cycle.
A fifth stage of organic Rankine cycle: after the exhaust steam is applied by the fifth-stage circulating turbine 43, the fifth-stage circulating working medium (R600, 27.95 ℃,110kPa, 2190kg/h) is subjected to heat exchange and temperature reduction by the fifth-stage circulating heat regenerator 44 to 8 ℃, then is subjected to heat exchange and temperature reduction by the fifth-stage circulating condenser 35 and waste nitrogen (-17.82) to 0 ℃, is pressurized to 1100kPa (0.63 ℃) by the fifth-stage circulating working medium pump 45, enters the fifth-stage circulating heat regenerator 44 to be subjected to heat regeneration to 15.26 ℃, is further subjected to heat exchange with high-temperature cylinder sleeve water cooling water (90 ℃) in the fifth-stage circulating evaporator 46 to heat up to 85 ℃, and finally is applied by the fifth-stage circulating turbine 43 to complete a cycle.
A sixth stage of organic rankine cycle: after the exhaust steam is applied by the sixth-stage circulating turbine 56, the sixth-stage circulating working medium (n-Pentane, 64.97 ℃,110kPa, 6500kg/h) is subjected to heat exchange to 25 ℃ through the sixth-stage circulating seawater cooler 57, then is pressurized to 390kPa (25.16 ℃) through the sixth-stage circulating working medium pump 58, is subjected to heat exchange with the flue gas (94.07 ℃) in the fourth-stage flue gas heat exchanger 12, is heated to 88 ℃, and finally is applied by the sixth-stage circulating turbine 56 to complete a cycle.

Claims (10)

1. The utility model provides a LNG power ship low temperature carbon entrapment coupling cold energy and waste heat cascade utilization system which characterized in that includes:
at the LNG evaporation side, the LNG from the LNG storage tank is subjected to primary pressurization, primary LNG heat exchange, secondary pressurization, secondary LNG heat exchange and seawater temperature regulation to form NG, and then the NG is sent to a host;
on the smoke side, smoke discharged by the main machine is subjected to first-stage smoke expansion work, first-stage smoke heat exchange, second-stage smoke expansion work, second-stage smoke heat exchange, third-stage smoke heat exchange and seawater cooling, then water is separated through a first smoke water separator, the water is further divided into two paths, one path of the water is sent to the main machine, the other path of the water is subjected to fourth-stage smoke heat exchange and fifth-stage smoke heat exchange after sequentially passing through a smoke precooler, a second smoke water separator and a smoke compressor to complete low-temperature liquefaction and trapping, and the low-temperature liquefaction and trapping are sent to LCO2A storage tank;
the air side comprises a flow path for sequentially carrying out multistage cooling pressurization and two-stage rectification on air, waste nitrogen formed after the air is subjected to the two-stage rectification is used for carrying out multistage cooling pressurization on the air, the front-stage cooling except the final-stage cooling is carried out, heat energy is absorbed by a third-stage flue gas heat exchanger and then the air is used for doing work through a waste nitrogen turbine, waste argon formed after the air is subjected to the two-stage rectification is mixed with waste nitrogen discharged from the waste nitrogen turbine, then cold energy is sequentially provided for a flue gas precooler and a carbon capture heat exchanger and then the air is discharged, and liquid oxygen formed after the air is subjected to the two-stage rectification is used for carrying out final-stage cooling on the air and then is regasified in the carbon capture heat exchanger and sent to a host;
the system comprises a first-stage organic Rankine cycle power generation unit, wherein a circulation loop of the first-stage organic Rankine cycle power generation unit is a loop which is heated by a second-stage circulating working medium in a first-stage circulating evaporator after being pressurized by a first-stage circulating working medium, and is subjected to expansion work and then is repressurized through first-stage LNG heat exchange;
the circulating loop of the second-stage organic Rankine cycle power generation unit is a loop which is formed by pressurizing a second-stage circulating working medium, heating the pressurized second-stage circulating working medium by the flue gas from the flue gas compressor, performing expansion work, and then sequentially exchanging heat and repressurizing the second-stage circulating working medium by the first-stage circulating evaporator and the second-stage circulating seawater cooler;
the circulation loop of the third-stage organic Rankine cycle power generation unit is a loop which is subjected to heat exchange with the flue gas through a third-stage circulation preheater after the third-stage circulation working medium is pressurized, is subjected to second-stage flue gas heat exchange with the flue gas, is subjected to expansion work, and is subjected to heat exchange through a third-stage circulation seawater cooler and is then pressurized again;
and a fourth-stage transcritical Rankine cycle power generation unit, wherein a circulation loop of the fourth-stage transcritical Rankine cycle power generation unit is a loop in which a fourth-stage transcritical Rankine cycle working medium is pressurized, then sequentially passes through a high-temperature cylinder sleeve cooling water preheating mode, a fourth-stage circulation heat regenerator for heat regeneration, then sequentially performs first-stage flue gas heat exchange with flue gas, performs expansion and work, and then sequentially passes through a fourth-stage circulation heat regenerator, a third-stage circulation preheater and a fourth-stage circulation seawater cooler for heat exchange and then is pressurized again.
Wherein the first-stage LNG heat exchange provides cold energy for LNG to a first-stage organic Rankine cycle working medium, the second-stage LNG heat exchange provides cold energy for LNG to a carbon capture heat exchanger, the first-stage flue gas heat exchange provides heat energy for flue gas to a fourth-stage Rankine cycle working medium, the second-stage flue gas heat exchange provides heat energy for flue gas to a third-stage Rankine cycle working medium, and the third-stage flue gas heat exchange provides heat energy for the flue gas to waste nitrogen after primary cooling of air, the fourth stage of flue gas heat exchange is that the flue gas compressed by the flue gas compressor releases heat energy to the second stage of circulating working medium, the fifth stage of flue gas heat exchange is that the flue gas releases heat energy to the carbon capture heat exchanger, and in the carbon capture heat exchanger, the LNG subjected to secondary pressurization, the oxygen subjected to final-stage cooling on the air and the waste nitrogen and waste argon subjected to heat exchange by the flue gas precooler absorb heat in the same direction with the flue gas subjected to heat exchange by the second stage of circulating working medium.
2. The LNG powered ship low-temperature carbon capture coupling cold energy and waste heat cascade utilization system as claimed in claim 1, comprising a fifth-stage organic Rankine cycle power generation unit, wherein a circulation loop of the fifth-stage organic Rankine cycle power generation unit is a loop in which a fifth-stage circulating working medium is pressurized, then the fifth-stage circulating working medium is subjected to heat exchange through a fifth-stage circulating heat regenerator, then the fifth-stage circulating heat regenerator is used for heating by high-temperature cylinder jacket cooling water, and after expansion work is performed, the fifth-stage circulating heat regenerator is sequentially subjected to heat exchange and waste nitrogen and waste argon from the carbon capture heat exchanger are cooled and then repressurized.
3. The LNG powered ship low-temperature carbon capture coupling cold energy and waste heat cascade utilization system as claimed in claim 2, comprising a sixth-stage organic Rankine cycle power generation unit, wherein a circulation loop of the sixth-stage organic Rankine cycle power generation unit is a loop in which a sixth-stage circulating working medium is pressurized, heated by flue gas after heat exchange with second-stage flue gas, expanded to work, and then subjected to heat exchange and re-pressurization through a sixth-stage seawater cooler; and carrying out third-stage flue gas heat exchange on the flue gas heated by the pressurized sixth-stage circulating working medium.
4. The LNG power ship low-temperature carbon capture coupling cold energy and waste heat cascade utilization system of claim 1, wherein the LNG evaporation side comprises an LNG storage tank, a first-stage LNG booster pump, an LNG heat exchanger, a second-stage LNG booster pump, a carbon capture heat exchanger, a seawater temperature regulator and a ship host which are connected in sequence, an outlet of the first-stage LNG booster pump is connected with a cold source input end of the LNG heat exchanger, a cold source output end of the LNG heat exchanger is connected with an input end of the second-stage LNG booster pump, an output end of the second-stage LNG booster pump is connected with a first cold source input end of the carbon capture heat exchanger, a first cold source output end of the carbon capture heat exchanger is connected with an input end of the seawater temperature regulator, and the first-stage LNG heat exchange is carried out at the LNG heat exchanger.
5. The LNG powered ship low-temperature carbon capture coupling cold energy and waste heat cascade utilization system as claimed in claim 3, wherein the flue gas side comprises a first stage flue gas turbine, a first stage flue gas heat exchanger, a second stage flue gas turbine, a second stage flue gas heat exchanger, a fourth stage flue gas heat exchanger, a third stage flue gas heat exchanger, a seawater cooler, a first flue gas water separator and a flue gas flow divider which are sequentially connected, one path of split flow of the flue gas flow divider is directly connected to a ship host, and the other path of split flow of the flue gas flow divider comprises a flue gas precooler, a second flue gas water separator, a flue gas compressor, a second stage circulating evaporator, a carbon capture heat exchanger and an LCO which are sequentially connected2The system comprises a storage tank, wherein the first-stage flue gas heat exchanger carries out first-stage flue gas heat exchange, the second-stage flue gas heat exchanger carries out second-stage flue gas heat exchange, a sixth-stage circulating working medium which is heated and pressurized by flue gas after the second-stage flue gas heat exchange in the fourth-stage flue gas heat exchanger, the third-stage flue gas heat exchanger carries out third-stage flue gas heat exchange, the second-stage circulating evaporator carries out fourth-stage flue gas heat exchange, and the carbon capture heat exchanger carries out fifth-stage flue gas heat exchange.
6. The LNG powered ship low-temperature carbon capturing coupling cold energy and waste heat cascade utilization system as claimed in claim 1, wherein the air side comprises an air filter, a first-stage cooler, an air-water separator, a second-stage cooler, a first-stage compressor, a third-stage cooler, a fourth-stage cooler, an air throttle valve, a first-stage rectifying tower and a second-stage rectifying tower which are sequentially connected, the flow path of waste nitrogen output by the upper tower of the first-stage rectifying tower comprises a third-stage cooler, a second-stage cooler, a first-stage cooler, a third-stage flue gas heat exchanger, a waste nitrogen turbine and a waste nitrogen and waste argon current collector which are sequentially connected, the other input end of the waste nitrogen and waste argon current collector is connected with the output end of the upper tower of the second-stage rectifying tower, the flow path of waste nitrogen and waste argon output by the waste nitrogen and waste argon current collector comprises a flue gas precooler and a carbon capturing heat exchanger which are sequentially connected, the cold source output end of the flue gas capturing heat exchanger is connected with the third cold source input end of the carbon capturing heat exchanger, the flow path of oxygen output by the lower tower of the second-stage rectifying tower comprises a third-stage cooler, an oxygen throttling valve and an oxygen capturing heat exchanger which are sequentially connected with the second-carbon capturing host machine, and the cold source output end of the second-carbon capturing heat exchanger which are connected with the cold source input end of the ship host.
7. The LNG powered ship low-temperature carbon capture coupling cold energy and waste heat cascade utilization system as claimed in claim 1, wherein the working temperature range of a first-stage circulating working medium in the first-stage organic Rankine cycle is-100-70 ℃, the working temperature range of a second-stage circulating working medium in the second-stage organic Rankine cycle is 25-150 ℃, the working temperature range of a third-stage circulating working medium in the third-stage organic Rankine cycle is 0-85 ℃, and the working temperature range of a fourth-stage circulating working medium in the fourth-stage transcritical Rankine cycle is 25-261 ℃.
8. The LNG powered ship low-temperature carbon capture coupling cold energy and waste heat cascade utilization system as claimed in claim 3, wherein the working temperature range of a fifth-stage circulating working medium in the fifth-stage organic Rankine cycle is 25-115 ℃, and the working temperature range of a sixth-stage circulating working medium in the sixth-stage organic Rankine cycle is 25-90 ℃.
9. The LNG powered vessel cryogenic carbon capture coupling cold energy and waste heat cascade utilization system of claim 7, wherein the first stage cycle fluid is R1150, the second stage cycle fluid is n-Pentane, the third stage cycle fluid is R600, and the fourth stage cycle fluid is CO2。
10. The LNG powered vessel cryogenic carbon capture coupled cold energy and waste heat cascade utilization system of claim 8, wherein the fifth stage cycle fluid is R600, and the sixth stage cycle fluid is n-Pentane.
CN202210819925.3A 2022-07-13 2022-07-13 Low-temperature carbon capture coupling cold energy and waste heat cascade utilization system of LNG power ship Pending CN115263466A (en)

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