CN113188291A - Carbon dioxide liquefaction system, carbon dioxide liquefaction and liquefied natural gas vaporization combined treatment system and low-carbon-emission ship - Google Patents

Carbon dioxide liquefaction system, carbon dioxide liquefaction and liquefied natural gas vaporization combined treatment system and low-carbon-emission ship Download PDF

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Publication number
CN113188291A
CN113188291A CN202110492550.XA CN202110492550A CN113188291A CN 113188291 A CN113188291 A CN 113188291A CN 202110492550 A CN202110492550 A CN 202110492550A CN 113188291 A CN113188291 A CN 113188291A
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carbon dioxide
heat exchanger
pressure
natural gas
ship
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CN202110492550.XA
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Chinese (zh)
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魏颖
陈世福
何炜
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China Pacific Maritime Technology Shanghai Co ltd
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China Pacific Maritime Technology Shanghai Co ltd
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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/006—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the refrigerant fluid used
    • F25J1/0095—Oxides of carbon, e.g. CO2
    • 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
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B63—SHIPS OR OTHER WATERBORNE VESSELS; RELATED EQUIPMENT
    • B63H—MARINE PROPULSION OR STEERING
    • B63H21/00—Use of propulsion power plant or units on vessels
    • B63H21/38—Apparatus or methods specially adapted for use on marine vessels, for handling power plant or unit liquids, e.g. lubricants, coolants, fuels or the like
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
    • F25J1/0032—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration"
    • F25J1/004—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration" by flash gas recovery
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
    • F25J1/0221—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
    • F25J1/0224—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 internal quasi-closed refrigeration loop
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
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    • F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
    • F25J1/0228—Coupling of the liquefaction unit to other units or processes, so-called integrated processes
    • F25J1/0229—Integration with a unit for using hydrocarbons, e.g. consuming hydrocarbons as feed stock
    • F25J1/023—Integration with a unit for using hydrocarbons, e.g. consuming hydrocarbons as feed stock for the combustion as fuels, i.e. integration with the fuel gas system
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
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    • F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
    • F25J1/0228—Coupling of the liquefaction unit to other units or processes, so-called integrated processes
    • F25J1/0235—Heat exchange integration
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
    • F25J1/0243—Start-up or control of the process; Details of the apparatus used; Details of the refrigerant compression system used
    • F25J1/0244—Operation; Control and regulation; Instrumentation
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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
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
    • F25J1/0243—Start-up or control of the process; Details of the apparatus used; Details of the refrigerant compression system used
    • F25J1/0244—Operation; Control and regulation; Instrumentation
    • F25J1/0254—Operation; Control and regulation; Instrumentation controlling particular process parameter, e.g. pressure, temperature
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    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
    • F25J1/0243—Start-up or control of the process; Details of the apparatus used; Details of the refrigerant compression system used
    • F25J1/0257—Construction and layout of liquefaction equipments, e.g. valves, machines
    • F25J1/0262—Details of the cold heat exchange system
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
    • F25J1/0243—Start-up or control of the process; Details of the apparatus used; Details of the refrigerant compression system used
    • F25J1/0257—Construction and layout of liquefaction equipments, e.g. valves, machines
    • F25J1/0275—Construction and layout of liquefaction equipments, e.g. valves, machines adapted for special use of the liquefaction unit, e.g. portable or transportable devices
    • F25J1/0277—Offshore use, e.g. during shipping
    • 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
    • F25J2205/02—Processes or apparatus using other separation and/or other processing means using simple phase separation in a vessel or drum
    • F25J2205/04—Processes or apparatus using other separation and/or other processing means using simple phase separation in a vessel or drum in the feed line, i.e. upstream of the fractionation 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
    • F25J2205/00—Processes or apparatus using other separation and/or other processing means
    • F25J2205/60—Processes or apparatus using other separation and/or other processing means using adsorption on solid adsorbents, e.g. by temperature-swing adsorption [TSA] at the hot or cold end
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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
    • F25J2210/00—Processes characterised by the type or other details of the feed stream
    • F25J2210/04—Mixing or blending of fluids with 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
    • 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
    • F25J2215/80—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
    • 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
    • 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
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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
    • 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
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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
    • F25J2245/00—Processes or apparatus involving steps for recycling of process streams
    • F25J2245/02—Recycle of a stream in general, e.g. a by-pass 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
    • F25J2245/00—Processes or apparatus involving steps for recycling of process streams
    • F25J2245/90—Processes or apparatus involving steps for recycling of process streams the recycled stream being boil-off gas from storage

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  • Physics & Mathematics (AREA)
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Abstract

The carbon dioxide liquefaction system disclosed in the embodiments of this specification is used for separating the carbon dioxide that catches in ship's tail gas, includes: the buffering and separating device is used for cooling, decompressing and separating carbon dioxide gas from the ship carbon capturing system, and a first input end of the buffering and separating device is connected with the ship carbon capturing system; the pressurizing device is used for pressurizing the carbon dioxide gas output by the buffer separation device, and the input end of the pressurizing device is connected with the output end of the buffer separation device; the first input end of the heat exchanger is connected with the liquefied natural gas fuel storage system, the first output end of the heat exchanger is used for outputting liquefied natural gas after heat exchange, the second input end of the heat exchanger is connected with the output end of the supercharging device, the second output end of the heat exchanger is used for outputting liquid carbon dioxide generated after heat exchange, and the third output end of the heat exchanger is connected with the second input end of the buffer separation device and used for inputting carbon dioxide gas after heat exchange into the buffer separation device.

Description

Carbon dioxide liquefaction system, carbon dioxide liquefaction and liquefied natural gas vaporization combined treatment system and low-carbon-emission ship
Technical Field
The embodiment of the specification relates to the technical field of carbon dioxide liquefaction, in particular to a carbon dioxide liquefaction system, a carbon dioxide liquefaction and liquefied natural gas vaporization combined treatment system and a low-carbon emission ship.
Background
Carbon capture, utilization, and sequestration technologies have attracted attention as one of the key technologies for global warming in recent years, in order to reduce the carbon content of conventional fuels, and to make the fuels clean and practical. Shipping, as the primary means of international transportation, is facing significant challenges in achieving sustainable development in response to global regulations on pollution prevention and environmental protection.
As the industry gradually adapts to the current international maritime organization's enacted 2020 sulfur directive, the international maritime organization will, in turn, plan for new regulations and new challenges to reduce carbon emissions. For the shipping industry, the "zero carbon future" is an ambitious goal, and related regulatory approaches will also evolve with changes in ship design, technology and practice. Importantly, to develop the shipping industry, strategic and overall progress must be made, more efficiently and consistently than is currently possible.
The existing CO2 liquefaction technology improves CO through multi-stage compression2Gas pressure and liquefaction temperature, and performing circulation refrigeration with cryogenic fluid such as liquid ammonia, propane or other refrigerant to obtain liquid CO2At the same time, due to liquefied CO2The pressure is higher, and a pressure container is also needed for sealing. Such liquefaction makes the overall system more energy intensive and requires increased storage of intermediate cryogenic cooling media, which in turn results in high construction and operating costs.
Therefore, there is a need for a new carbon dioxide liquefaction system that effectively reduces energy consumption, construction costs, and operational costs.
Disclosure of Invention
In view of this, the present specification provides a carbon dioxide liquefaction system for performing liquefaction separation on carbon dioxide captured in ship exhaust gas, including: the device comprises a buffer separation device, a supercharging device and a heat exchanger;
the buffering and separating device is used for cooling, decompressing and separating carbon dioxide gas from the ship carbon capture system, and a first input end of the buffering and separating device is connected with the ship carbon capture system;
the pressurizing device is used for pressurizing the carbon dioxide gas output by the buffer separation device, and the input end of the pressurizing device is connected with the output end of the buffer separation device;
the heat exchanger is used for heat exchange between liquefied natural gas and pressurized carbon dioxide gas, a first input end of the heat exchanger is connected with a liquefied natural gas fuel storage system, a first output end of the heat exchanger is used for outputting gaseous natural gas generated after heat exchange, a second input end of the heat exchanger is connected with an output end of the supercharging device, a second output end of the heat exchanger is used for outputting liquid carbon dioxide generated after heat exchange,
and the third output end of the heat exchanger is connected with the second input end of the buffer separation device and is used for inputting the heat-exchanged carbon dioxide gas into the buffer separation device so as to mix the heat-exchanged carbon dioxide gas with the cooled and decompressed carbon dioxide gas.
Preferably, the buffering and separating device comprises: the device comprises a first temperature sensor, a throttle valve and a buffer separation tank;
the first temperature sensor is connected with the throttling valve and used for detecting the temperature of the carbon dioxide gas input into the buffer separation tank and generating a first temperature signal;
the input end of the throttle valve is connected with the ship carbon capture system, the throttle valve is used for carrying out temperature reduction and pressure reduction treatment on carbon dioxide gas from the ship carbon capture system according to the first temperature signal,
the output end of the throttling valve is connected with the first input end of the buffer separation tank, so that the cooled and decompressed carbon dioxide is input into the buffer separation tank in a gaseous state;
a second input end of the buffer separation tank is connected with a third output end of the heat exchanger so as to receive the heat-exchanged carbon dioxide gas, so that the heat-exchanged carbon dioxide gas and the cooled and decompressed carbon dioxide gas are mixed in the buffer separation tank;
and a first output end of the buffer separation tank is connected with the supercharging device, and a second output end of the buffer separation tank is connected with the ship carbon capture system so as to return condensed liquid.
Preferably, the buffer separation tank comprises a gas-water separation device;
the gas-water separation device is arranged at the top of the buffer separation tank and used for dehumidifying the carbon dioxide gas output from the buffer separation tank.
Preferably, the apparatus further comprises: a pressure regulating device;
the pressure regulating device comprises a pressure regulating valve and a first pressure sensor connected with the pressure regulating valve,
the first pressure sensor is arranged on the heat exchanger and used for detecting the gas pressure of the carbon dioxide gas in the heat exchanger to generate a first pressure signal;
the pressure regulating valve is respectively connected with the heat exchanger and the buffer separation device and used for regulating the pressure of the carbon dioxide gas input into the heat exchanger according to the first pressure signal.
Preferably, the apparatus further comprises: a low voltage storage device;
and the input end of the low-pressure storage device is connected with the second output end of the heat exchanger and is used for storing the liquid carbon dioxide.
Preferably, the apparatus further comprises: the liquid carbon dioxide output control device is used for controlling the output of the liquid carbon dioxide;
the liquid carbon dioxide output control device comprises a liquid level sensor, a second temperature sensor and a flow control valve;
the liquid level sensor is arranged on the heat exchanger and connected with the flow control valve, and the liquid level sensor is used for detecting the liquid level of liquid carbon dioxide in the heat exchanger and generating a liquid level signal;
the second temperature sensor is connected with the flow control valve and used for detecting the temperature of the liquid carbon dioxide output by the heat exchanger and generating a second temperature signal;
and the flow control valve is respectively connected with the heat exchanger and the low-pressure storage device and is used for controlling the output of the liquid carbon dioxide in the heat exchanger according to the liquid level signal and the second temperature signal.
Preferably, the apparatus further comprises: the cabin pressure control valve and a second pressure sensor are connected with the cabin pressure control valve;
the second pressure sensor is arranged on the low-pressure storage device and used for detecting the air pressure in the low-pressure storage device and generating a second pressure signal;
the low-pressure storage device, the cabin pressure control valve and the buffer separation device are sequentially connected;
the cabin pressure control valve is used for controlling the output of carbon dioxide evaporation gas in the low-pressure storage device according to the second pressure signal, so that the pressure in the low-pressure storage device is controlled.
The embodiment of this specification provides a carbon dioxide liquefaction and liquefied natural gas vaporization combined processing system for utilize the cold energy that produces when liquefied natural gas vaporizes to cool the separation to the carbon dioxide who catches in the ship's tail gas, its characterized in that includes: a carbon dioxide liquefaction system and a liquid natural gas vaporization system;
the carbon dioxide liquefaction system is any one of the carbon dioxide liquefaction systems described above;
the liquefied natural gas vaporization system includes: a fuel pump, a heater, and a temperature control device;
the fuel pump is respectively connected with the liquefied natural gas fuel storage system in the ship and the heat exchanger and is used for inputting liquefied natural gas from the liquefied natural gas fuel storage system in the ship into the heat exchanger;
the heater is used for heating the gaseous natural gas from the heat exchanger through circulating condensed water, and the gaseous natural gas is generated after the liquid natural gas is subjected to heat exchange through the heat exchanger;
a first input end of the heater is connected with a first output end of the heat exchanger, and a first output end of the heater is connected with a power system in the ship;
the temperature control device comprises a temperature control valve and a third temperature sensor connected with the temperature control valve;
the third temperature sensor is used for detecting the temperature of the gaseous natural gas output by the heater and generating a third temperature signal;
the temperature control valve is connected with a second input end of the heater and used for controlling the input of the condensed water according to the third temperature signal, and the second input end of the heater is used for inputting the condensed water.
Preferably, the apparatus further comprises: a control system for controlling the operation of the combined carbon dioxide liquefaction and liquefied natural gas vaporization processing system;
the control system is respectively connected with the first temperature sensor, the throttling valve, the first pressure sensor, the pressure regulating valve, the liquid level sensor, the second temperature sensor, the flow control valve, the second pressure sensor, the cabin pressure control valve, the third temperature sensor and the temperature control valve.
The embodiment of the present specification provides a low carbon emission ship, which is characterized by comprising: the system comprises a liquefied natural gas fuel storage system, a ship carbon capture system, a carbon dioxide liquefaction and liquefied natural gas vaporization combined processing system and a power system;
the liquefied natural gas fuel storage system is used for providing liquefied natural gas;
the ship carbon capture system is used for capturing carbon dioxide in the low-carbon-emission ship tail gas;
the power system is used for providing power;
the carbon dioxide liquefaction and liquefied natural gas vaporization combined processing system is respectively connected with the liquefied natural gas fuel storage system, the ship carbon capture system and the liquefied natural gas vaporization system;
the carbon dioxide liquefaction and liquefied natural gas vaporization combined treatment system is arranged in a space area formed from a ship centerline to a stern closing plate or from a ship bottom plate to a compass deck along the ship length direction;
the carbon dioxide liquefaction and liquefied natural gas vaporization combined processing system is any one of the carbon dioxide liquefaction and liquefied natural gas vaporization combined processing systems;
the low-pressure storage device is arranged on a deck of the ship or in a compartment below the deck of the ship.
The embodiment of the specification adopts at least one technical scheme which can achieve the following beneficial effects: provided is a carbon dioxide liquefaction system for carrying out liquefaction separation on carbon dioxide captured in ship tail gas, which is characterized by comprising: the device comprises a buffer separation device, a supercharging device and a heat exchanger; the buffering and separating device is used for cooling, decompressing and separating carbon dioxide gas from the ship carbon capture system, and a first input end of the buffering and separating device is connected with the ship carbon capture system; the pressurizing device is used for pressurizing the carbon dioxide gas output by the buffer separation device, and the input end of the pressurizing device is connected with the output end of the buffer separation device; the heat exchanger is used for heat exchange between liquefied natural gas and pressurized carbon dioxide gas, a first input end of the heat exchanger is connected with a liquefied natural gas fuel storage system, a first output end of the heat exchanger is used for outputting gaseous natural gas generated after heat exchange, a second input end of the heat exchanger is connected with an output end of the pressurization device, a second output end of the heat exchanger is used for outputting liquid carbon dioxide generated after heat exchange, and a third output end of the heat exchanger is connected with a second input end of the buffer separation device and used for inputting the carbon dioxide gas after heat exchange into the buffer separation device, so that the carbon dioxide gas after heat exchange is mixed with the carbon dioxide gas after temperature reduction and pressure reduction, and the temperature is reduced. Through this carbon dioxide liquefaction system, when effectively utilizing the cold energy of release when liquefied natural gas vaporizes and the heat energy of release when carbon dioxide gas liquefies, need not to increase new cooling medium again, make full use of current device has reduced the energy consumption, reduces construction cost and operation cost.
Drawings
The accompanying drawings, which are included to provide a further understanding of the embodiments of the specification and are incorporated in and constitute a part of this specification, illustrate exemplary embodiments of the specification and together with the description serve to explain the application and not to limit the application. In the drawings:
fig. 1 is a schematic structural diagram of a carbon dioxide liquefaction system according to an embodiment of the present disclosure.
Fig. 2 is a schematic structural diagram of a carbon dioxide liquefaction system according to an embodiment of the present disclosure.
Fig. 3 is a schematic structural diagram of a carbon dioxide liquefaction and liquefied natural gas vaporization combined processing system according to an embodiment of the present disclosure.
Fig. 4 is a schematic structural diagram of a carbon dioxide liquefaction and liquefied natural gas vaporization combined processing system according to an embodiment of the present disclosure.
Fig. 5 is a schematic structural diagram of a low-carbon-emission ship according to an embodiment of the present disclosure.
Detailed Description
In order to make the objects, technical solutions and advantages of the present application more clear, the technical solutions of the present application will be clearly and completely described below with reference to the specific embodiments of the present specification and the accompanying drawings. It should be apparent that the described embodiments are only some of the embodiments of the present application, and not all of the embodiments. All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the protection scope of the present application.
According to the preliminary strategy of emission reduction of IMO greenhouse gases passed in 2018, the intensity of international shipping carbon is reduced by 40% by 2030, and the ship industry is taken as the traditional transportation industry, and only clean energy and tail gas decarburization can be carried out for realizing carbon emission reduction.
At present, Liquid Natural Gas (LNG) is used as a main fuel of ships, and in the future 20-30 years, LNG powered ships will occupy most markets. The LNG mainly contains methane, and still emits CO after combustion2However, LNG has been counted as a clean fuel compared to traditional fossil fuels.
The carbon dioxide liquefaction system provided by the embodiment of the specification has the core idea that the cold energy generated in the liquid natural gas vaporization process is used for separating the carbon dioxide gas from the carbon dioxide capture system in the LNG ship by adopting a multi-stage circulating cooling mode, and the carbon dioxide gas is generated after the carbon capture system performs carbon capture treatment on the LNG ship tail gas.
The above application scenarios are merely illustrated to facilitate understanding of the present application, and the embodiments of the present specification are not limited in any way in this respect. Rather, embodiments of the present description may be applied to any scenario where applicable.
Hereinafter, a device configuration method, an apparatus, and an electronic device according to the present specification will be described in detail with reference to the accompanying drawings.
Example 1
Fig. 1 is a schematic structural diagram of a carbon dioxide liquefaction system according to an embodiment of the present disclosure.
As shown in fig. 1, a carbon dioxide liquefaction system in the embodiment of the present disclosure is used for separating carbon dioxide captured in ship exhaust gas, and includes: a buffer separation device 11, a pressure boosting device 12 and a heat exchanger 13.
The buffer separation device 11 is used for cooling and decompressing the carbon dioxide gas from the ship carbon capture system.
In the embodiment of the specification, the first input end of the buffering and separating device 11 is connected with the ship carbon capture system through a pipeline.
The carbon dioxide gas from the ship carbon capture system is at a temperature of 30-50 ℃ and a pressure of 50-80 kpa.
In specific implementation, the buffering and separating device 11 may include a self-cooling buffering and separating tank, and after the carbon dioxide gas from the carbon capture system of the ship enters the buffering and separating tank, the temperature is naturally reduced in the tank, so as to separate out a part of condensate, which contains condensate water and other impurities.
The buffer separation device 11 may also include a buffer separation tank having a circulation cooling system, and after the carbon dioxide gas from the ship carbon capture system enters the buffer separation tank, the carbon dioxide gas in the tank is cooled to room temperature by the circulation cooling system, so as to separate a part of condensate, which contains condensed water and other impurities.
The buffer separation device 11 may further include a buffer separation tank having a pressure reducing valve, and after the carbon dioxide gas from the carbon capture system of the ship enters the buffer separation tank, the pressure of the carbon dioxide gas in the tank is reduced by the pressure reducing device and is reduced to room temperature, so as to separate a part of condensate, which contains condensed water and other impurities.
In the embodiment of the present specification, the output end of the buffer separation device 11 is disposed at the top of the buffer separation device 11, and the carbon dioxide gas after temperature reduction and pressure reduction is output from the top of the buffer separation device 11.
The pressurizing device 12 is used for pressurizing the carbon dioxide gas output by the buffer separation device 11, and the input end of the pressurizing device is connected with the output end of the buffer separation device 11 through a pipeline.
In the embodiment of the present disclosure, the pressurizing device 12 may be a booster fan, or may be other devices that can be used to pressurize the carbon dioxide gas, such as a booster pump, a compressor, and the like.
The carbon dioxide gas input into the heat exchanger 13 is pressurized by the pressurizing device 12, so that the flow rate of the carbon dioxide gas entering the heat exchanger 13 can be controlled, and the heat exchange efficiency is ensured.
The heat exchanger 13 is used for heat exchange between the liquefied natural gas and the pressurized carbon dioxide gas.
The first input end of the heat exchanger 13 is connected with a pipeline of a liquid natural gas fuel storage system, the first output end of the heat exchanger 13 is used for outputting gaseous natural gas generated after heat exchange, the second input end of the heat exchanger 13 is connected with an output end pipeline of the supercharging device 12, the second output end of the heat exchanger 13 is used for outputting liquid carbon dioxide generated after heat exchange, the third output end of the heat exchanger 13 is connected with a second input end pipeline of the buffer separation device 11, and the heat exchange carbon dioxide is input into the buffer separation device 11 so that the heat exchange carbon dioxide is mixed with the temperature-reducing and pressure-reducing carbon dioxide.
In the embodiment of the present specification, the heat exchanger 13 may be a plate heat exchanger, a shell-and-tube heat exchanger, or another heat exchanger suitable for exchanging heat between liquid and gas.
The first input end of the heat exchanger 13 is arranged at the bottom of the heat exchanger 13, and the first output end of the heat exchanger 13 is arranged at the top of the heat exchanger 13, so that the liquefied natural gas is input from the bottom of the heat exchanger 13, and the gaseous natural gas generated after heat exchange is output from the top of the heat exchanger 13.
The second input end of the heat exchanger 13 is arranged at the top of the heat exchanger 13, and the second output end of the heat exchanger 13 is arranged at the bottom of the heat exchanger 13, so that carbon dioxide gas is input through the top of the heat exchanger 13, and liquid carbon dioxide generated after cooling is output through the bottom of the heat exchanger 13.
The temperature of the liquid carbon dioxide generated by cooling is-60 ℃ to-75 ℃.
In the heat exchange process, the liquefied natural gas and the carbon dioxide gas are in reverse contact, so that the contact area of the liquefied natural gas and the carbon dioxide gas is ensured, and the heat exchange efficiency is improved.
Further, in the embodiments of the present disclosure, the contact area between the carbon dioxide gas and the liquefied natural gas may be adjusted by adjusting the number of gas flow channels in the heat exchanger, so as to adjust the heat exchange efficiency.
A third output of the heat exchanger 13 is arranged in the middle of the heat exchanger 13, and the cooled carbon dioxide gas is returned to the buffer separation device 11 through the third output.
The third output end is arranged in the middle of the heat exchanger 13, which not only can ensure that the liquid carbon dioxide does not flow into the buffer separation device 11, but also can ensure that the carbon dioxide gas returning to the buffer separation device 11 is well cooled.
Through mixing the carbon dioxide gas after the heat transfer with the carbon dioxide gas after the cooling decompression for the carbon dioxide gas in the buffering separator 11 can carry out the precooling, thereby reduces the initial temperature of the carbon dioxide gas of input heat exchanger 13, and then improves heat exchange efficiency, reduces the energy consumption.
The carbon dioxide gas from the ship carbon capturing system is cooled and liquefied in a multistage circulating cooling mode, so that the cooling efficiency is improved, the cold energy of the liquefied natural gas is fully utilized, and the energy waste is avoided.
The embodiment of the specification adopts at least one technical scheme which can achieve the following beneficial effects: provided is a carbon dioxide liquefaction system for carrying out liquefaction separation on carbon dioxide captured in ship tail gas, which is characterized by comprising: the device comprises a buffer separation device, a supercharging device and a heat exchanger; the buffering and separating device is used for cooling, decompressing and separating carbon dioxide gas from the ship carbon capture system, and a first input end of the buffering and separating device is connected with the ship carbon capture system; the pressurizing device is used for pressurizing the carbon dioxide gas output by the buffer separation device, and the input end of the pressurizing device is connected with the output end of the buffer separation device; the heat exchanger is used for heat exchange between liquefied natural gas and pressurized carbon dioxide gas, a first input end of the heat exchanger is connected with a liquefied natural gas fuel storage system, a first output end of the heat exchanger is used for outputting gaseous natural gas generated after heat exchange, a second input end of the heat exchanger is connected with an output end of the pressurization device, a second output end of the heat exchanger is used for outputting liquid carbon dioxide generated after heat exchange, and a third output end of the heat exchanger is connected with a second input end of the buffer separation device and used for inputting the carbon dioxide gas after heat exchange into the buffer separation device, so that the carbon dioxide gas after heat exchange is mixed with the carbon dioxide gas after temperature reduction and pressure reduction, and the temperature is reduced. Through this carbon dioxide liquefaction system, when effectively utilizing the cold energy of release when liquefied natural gas vaporizes and the heat energy of release when carbon dioxide gas liquefies, need not to increase new cooling medium again, make full use of current device has reduced the energy consumption, reduces construction cost and operation cost.
Example 2
In embodiment 2, the same method as that in embodiment 1 is used with the same reference numerals and the same description is omitted.
Fig. 2 is a schematic structural diagram of a carbon dioxide liquefaction system according to an embodiment of the present disclosure.
As shown in fig. 2, a carbon dioxide liquefaction system in the embodiment of the present disclosure is used for separating carbon dioxide captured in ship exhaust gas, and includes: the system comprises a first temperature sensor 21, a throttle valve 22, a buffer separation tank 23, a booster fan 24, a heat exchanger 25, a first pressure sensor 26, a pressure regulating valve 27, a low-pressure storage device 28, a liquid level sensor 29, a second temperature sensor 210, a flow control valve 211, a cabin pressure control valve 212 and a second pressure sensor 213.
In the embodiment of the present specification, the buffer separation device includes a first temperature sensor 21, a throttle valve 22, and a buffer separation tank 23.
The first temperature sensor 21 is configured to detect a temperature of the carbon dioxide gas input to the buffer separation tank 23 and generate a first temperature signal.
The first temperature sensor 21 is connected in communication with the throttle valve 22.
The input end of the throttle valve 22 is connected with a pipeline of the ship carbon capture system.
The throttle valve 22 is used for cooling and decompressing carbon dioxide gas from the ship carbon capture system according to the first temperature signal.
The output end of the throttle valve 22 is connected with a first input end pipeline of a buffer separation tank 23 so that the cooled and decompressed carbon dioxide gas is input into the buffer separation tank
Specifically, the gaseous temperature of the carbon dioxide after temperature reduction and pressure reduction is 10-15 ℃, and the pressure is 10-15 kpa.
The buffer separation tank 23 is used for storing the carbon dioxide gas after temperature reduction and pressure reduction.
A first output end of the buffer separation tank 23 is connected with a booster fan 24 through a pipeline.
A second output of the buffer tank 23 is connected to the vessel carbon capture system for returning condensed liquid.
It should be noted that, part of the carbon dioxide gas after being cooled and decompressed by the throttle valve 22 is condensed in the buffer separation tank 23 to generate a condensate, where the condensate contains condensed water and other impurities in the ship tail gas, and in order to ensure the purity of the separated carbon dioxide and improve the subsequent recovery efficiency, the condensate is returned to the ship carbon capture system for re-carbon capture treatment, so as to avoid introducing impurities into the subsequent carbon dioxide liquefaction process.
In one application example, in order to improve the purity of the carbon dioxide gas, the buffer tank 23 includes a gas-water separation device for dehumidifying the carbon dioxide gas output from the buffer tank 23.
The gas-water separation device is arranged at the top of the buffer separation tank 23.
In the embodiment of the present specification, the gas-water separation device may be a molecular sieve dryer, a membrane dryer, or another dryer capable of efficiently dehumidifying gas.
The booster fan 24 is used for pressurizing the carbon dioxide gas output by the buffer separation tank 23, so that the carbon dioxide gas after temperature reduction and pressure reduction can smoothly enter the input heat exchanger 25.
The heat exchanger 25 is used for heat exchange between the liquefied natural gas and the pressurized carbon dioxide gas.
The first input end of heat exchanger 25 and liquefied natural gas fuel storage system pipe connection, the first output end of heat exchanger 25 is used for exporting the gaseous natural gas that generates after the heat transfer, the second input end of heat exchanger 25 and booster fan 24's output end pipe connection, the second output end of heat exchanger 25 is used for exporting the liquid carbon dioxide that generates after the heat transfer, the third output end of heat exchanger 25 and the second input end pipe connection of buffer knockout drum 23, be used for the carbon dioxide gas input buffer knockout drum 23 after with the heat transfer, so that the carbon dioxide gas after the heat transfer mixes with 23 in the carbon dioxide gas buffer knockout drum after the cooling decompression.
In an application example, in order to adjust the circulation rate of the carbon dioxide gas in the heat exchanger 25 and improve the heat exchange efficiency, the carbon dioxide liquefaction system further includes a pressure adjustment device for adjusting the pressure of the carbon dioxide gas fed from the buffer separation tank 23 to the heat exchanger 25.
The pressure regulating means comprises a first pressure sensor 26 and a pressure regulating valve 27 which is connected in communication with the first pressure sensor 26.
A first pressure sensor 26 is disposed on the heat exchanger 25 for sensing the pressure of the carbon dioxide in the heat exchanger 25 to generate a first pressure signal.
The pressure regulating valve 27 is respectively connected with the heat exchanger 25 and the buffer separation tank 23 through pipelines and is used for regulating the pressure of the mixed carbon dioxide gas input into the heat exchanger 25 according to the first pressure signal, so that the pressure of the carbon dioxide gas input into the heat exchanger 25 is kept within a certain range, the carbon dioxide gas can circulate between the heat exchanger 25 and the buffer separation tank 23 at a certain flow speed, and the heat exchange efficiency is improved.
It should be noted that the pressure of the carbon dioxide gas input to the heat exchanger 25 may be adjusted according to actual needs, and is not limited specifically here.
In an application example, in order to ensure stability and safety of the output of the liquid carbon dioxide, the carbon dioxide liquefaction system in the embodiment of the present specification further includes a liquid carbon dioxide output control device for controlling the output of the liquid carbon dioxide in the heat exchanger 25.
Specifically, the liquid carbon dioxide output control means includes the liquid level sensor 29, the second temperature sensor 210, and the flow control valve 211.
The liquid level sensor 29 is disposed on the heat exchanger 25, and is in communication with the flow control valve 211 for detecting the liquid level of the liquid carbon dioxide in the heat exchanger to generate a liquid level signal.
And the second temperature sensor 210 is in communication connection with the flow control valve 211 and is used for detecting the temperature of the liquid carbon dioxide output by the heat exchanger 25 and generating a second temperature signal.
Flow control valve 211 is plumbed to heat exchanger 25 and low pressure storage device 28, respectively, for controlling the output of liquid carbon dioxide in heat exchanger 25 based on the level signal and the second temperature signal.
Specifically, when the liquid level signal indicates that the liquid level of the liquid carbon dioxide in the heat exchanger 25 is too high, the flow control valve 211 adjusts the flow rate of the liquid carbon dioxide, increases the outflow rate, and decreases the liquid level.
When the second temperature signal shows that the temperature of the liquid carbon dioxide is too high, the flow control valve 211 adjusts the flow rate of the liquid carbon dioxide, so as to increase the outflow speed and ensure that the output liquid carbon dioxide is within a preset temperature range.
And a low-pressure storage device 28, the input end of which is connected with the second output end of the heat exchanger 25 through a pipeline, and the low-pressure storage device is used for storing liquid carbon dioxide.
In the illustrated embodiment, the low pressure storage device 28 may be a low pressure carbon dioxide storage tank.
The low-pressure carbon dioxide storage tank comprises at least one of an A-type cabin, a B-type cabin and a film cabin, the storage pressure is below 50kpa, the low-pressure carbon dioxide storage tank is a low-pressure container which is different from a pressure container, and the shape of the low-pressure carbon dioxide storage tank can be linearly matched with the hull shell.
The low pressure storage device 28 uses reinforced polyurethane foam as an insulating material to effectively insulate the carbon dioxide liquid stored therein from vaporization.
The low-pressure storage device is high in integration level, high in storage efficiency and low in energy consumption, reduces storage risks of the high-pressure storage tank, and is suitable for limited space and public resources of ships.
In one application example, in order to enable the shore connection and discharge of the carbon dioxide liquid to be performed quickly and conveniently after the ship is landed, a carbon dioxide transfer pump is included in the low-pressure carbon dioxide storage tank, and the carbon dioxide liquid in the low-pressure carbon dioxide storage tank can be discharged quickly by the carbon dioxide transfer pump.
In an application example, the liquid carbon dioxide stored in the low pressure storage device 28 may cause the liquid carbon dioxide to evaporate to generate gas due to temperature change, so that the pressure inside the low pressure storage device 28 changes, and in order to avoid the influence of the gas generated by evaporation on the stability and safety of storage, the carbon dioxide liquefaction system in the embodiment of the present specification further includes a cabin pressure control valve 212 and a second pressure sensor 213.
A second pressure sensor 213 is disposed on the low pressure storage device 28 and is communicatively coupled to the cabin pressure control valve 212 for sensing the pressure within the low pressure storage device 28 and generating a second pressure signal.
The low-pressure storage device 28, the cabin pressure control valve 212, and the buffer separation tank 23 are connected in sequence by pipes.
Cabin pressure control valve 212 controls the output of gas from low pressure storage device 28 based on the second pressure signal.
Specifically, when the second pressure signal indicates that the pressure in the low pressure storage device 28 is excessive, the cabin pressure control valve 212 controls the gas in the low pressure storage device 28 to be output to the buffer separation tank 23, thereby reducing the pressure in the low pressure storage device 28.
By outputting the gas in the low-pressure storage device 28 to the buffer separation tank 23, the safety of the low-pressure storage device 28 can be effectively ensured, and the carbon dioxide in the BOG gas can be prevented from being recovered, so that the carbon emission is reduced.
The purity of the liquid carbon dioxide separated in the embodiment of the specification is as high as 95-98%, and is close to industrial grade CO2The standard is 99 percent, and the industrial super grade CO can be even achieved after the product is transported to land for simple purification2The gas-tight seal gas can be used for welding seal gas in heavy industries such as shipbuilding industry and the like, and can also be used for gas injection and oil displacement in oil fields and chemical enterprises around wharfs.
Further, for convenience of understanding, the following description will be made schematically on the carbon dioxide liquefaction apparatus provided in the embodiments of the present specification, taking a carbon dioxide gas separation process as an example:
carbon dioxide gas from a ship carbon capturing system is input into a throttle valve 22 for temperature reduction and pressure reduction treatment, the throttle valve 22 adjusts the flow rate of the carbon dioxide gas according to a first temperature signal generated by a first temperature sensor 21, the carbon dioxide gas is input into a buffer separation tank 23 after being reduced to room temperature and low pressure, the carbon dioxide gas is partially condensed after entering the buffer separation tank 23, condensate returns to the ship carbon capturing system through a second output end of the buffer separation tank 23 for carbon capturing treatment again, uncondensed carbon dioxide gas is dehumidified through a gas-water separation device at the top of the buffer separation tank 23, is input into a heat exchanger 25 after being pressurized by a booster fan 24, is subjected to heat exchange with liquefied natural gas in the heat exchanger 25 for temperature reduction, at the moment, a part of the carbon dioxide gas is cooled but not condensed into liquefied carbon dioxide, and the cooled and uncondensed carbon dioxide gas is input into the buffer separation tank 23 through a third output end of the heat exchanger 25, and the carbon dioxide gas is mixed with the carbon dioxide gas in the buffer separation tank 23 for cooling, so that the carbon dioxide gas is circularly cooled between the heat exchanger 25 and the buffer separation tank 23, and the other part of the carbon dioxide gas is condensed to generate liquid carbon dioxide which is output to the low-pressure storage device 28 for storage through a second output end at the bottom of the heat exchanger 25.
Example 3
In embodiment 3, the same method as in embodiment 1 or 2 is used with the same reference numerals and the same description is omitted.
Fig. 3 is a schematic structural diagram of a carbon dioxide liquefaction and liquefied natural gas vaporization combined processing system according to an embodiment of the present disclosure.
As shown in fig. 3, based on the same application concept, a carbon dioxide liquefaction and liquefied natural gas vaporization combined processing system described in the embodiments of the present specification is used for cooling and separating carbon dioxide captured in ship exhaust gas by using cold energy generated when liquefied natural gas is vaporized, and includes: a carbon dioxide liquefaction system 31, a liquid natural gas vaporization system 32, and a control system 33.
The carbon dioxide liquefaction system 31 is the carbon dioxide liquefaction system described in any one of the above.
The lng vaporization system 32 includes: a fuel pump 321, a heater 322, and a temperature control device 323;
the fuel pump 321 is connected to the heat exchangers in the liquefied natural gas system in the ship and the carbon dioxide liquefaction system 31, respectively, and is used for inputting the liquefied natural gas from the liquefied natural gas system in the ship to the heat exchangers.
The liquid natural gas device enters the heat exchanger and exchanges heat with the carbon dioxide gas, absorbs heat generated during liquefaction of the carbon dioxide gas, generates gaseous natural gas and outputs the gaseous natural gas.
The heater 322 is used to heat the gaseous natural gas from the heat exchanger by the circulating condensed water.
In the embodiment of the specification, the used condensed water can be seawater, and the seawater is discharged into the sea after the gas natural device is heated to the temperature (10-32 ℃) required by the engine through seawater circulation.
The used condensed water can also be circulating water used in a ship circulating water system, and the condensed water is returned to the ship circulating water system after the gas natural device is heated to the temperature required by the engine by the circulating water used by the ship.
The existing medium is used for heating the gas and the natural gas, so that the energy consumption of the system is reduced, the energy is saved, the environment is protected, and the cost is effectively reduced.
In the embodiment of the present specification, a first input end of the heater 322 is connected to a first output end of the heat exchanger, and a first output end of the heater 322 is connected to a power system in the ship.
Specifically, the natural gas generator is input into the heater 322 from the first input end, heated to normal temperature, and then enters the power system of the ship through the first output end to provide power for the ship.
The temperature control device 323 includes a temperature control valve and a third temperature sensor connected to the temperature control valve.
The third temperature sensor is disposed on the heater 322 and is configured to detect a temperature of the gaseous natural gas output by the heater 322 and generate a third temperature signal.
The temperature control valve is connected to a second input port of the heater 322 for controlling the input of the condensed water according to a third temperature signal.
And a control system 33 for controlling the operation of the combined carbon dioxide liquefaction and lng vaporization process system.
The control system 33 is respectively connected with a first temperature sensor, an intercepting and cooling valve, a first pressure sensor, a pressure regulating valve, a liquid level sensor, a second temperature sensor, a flow control valve, a second pressure sensor, a cabin control valve, a third temperature sensor and a temperature control valve, and a fuel pump.
Specifically, the control device 33 controls the throttle valve to adjust the flow rate of the carbon dioxide gas in accordance with the first temperature signal generated by the first temperature sensor.
The control device 33 controls the pressure regulating valve to regulate the pressure of the carbon dioxide gas input to the heat exchanger according to the first pressure signal generated by the first pressure sensor.
The control device 33 controls the flow control valve to adjust the output of the liquid carbon dioxide according to the liquid level signal generated by the liquid level sensor and the second temperature signal generated by the second temperature sensor.
The control device 33 controls the cabin pressure control valve to regulate the gas output from the low pressure storage device according to a second pressure signal generated by the second pressure sensor.
The control device 33 controls the temperature control valve to regulate the input of the condensed water and the fuel pump to regulate the flow rate of the liquefied natural gas based on the third temperature signal generated by the third temperature sensor.
Fig. 4 is a schematic structural diagram of a carbon dioxide liquefaction and liquefied natural gas vaporization combined processing system according to an embodiment of the present disclosure.
As shown in fig. 4, in the embodiment of the present specification, the fuel pump 41 is connected to the heat exchangers in the liquefied natural gas system and the carbon dioxide liquefaction system in the ship, respectively, and is configured to input the liquefied natural gas from the liquefied natural gas system in the ship to the heat exchangers.
The liquid natural gas enters the heat exchanger and then exchanges heat with the carbon dioxide gas, the heat generated when the carbon dioxide gas is liquefied is absorbed, and the generated gaseous natural gas is output to a power system in the ship.
The heater 42 is used to heat the gaseous natural gas from the heat exchanger by the circulating condensed water.
In the embodiment of the present disclosure, the heater 42 uses the circulating water in the ship circulating water system, and after the gas natural generator is heated to the temperature required by the engine by the circulating water used by the ship itself, the condensed water is returned to the ship circulating water system.
The third temperature sensor 43 is provided on the heater.
The temperature control valve 44 is connected in communication with the temperature control valve, and the temperature control valve 44 is connected to the second inlet pipe of the heater 42 for controlling the input of the condensed water according to the third temperature signal.
In the embodiment of the specification, LNG is vaporized by using heat released by liquefaction of carbon dioxide, the vaporized gaseous natural gas is used for combustion of an engine, heat required by vaporization of LNG is saved, and CO is used2The liquefaction and the LNG vaporization are jointly processed, and the liquefied and the LNG vaporization are manufactured into modules to be arranged in a fuel preparation room of the LNG, so that the installation space is saved, and the construction and operation cost is reduced.
Example 4
In example 5, the same reference numerals are used for the same methods as in examples 1 to 3, and the same descriptions are omitted.
Fig. 5 is a schematic structural diagram of a low-carbon-emission ship according to an embodiment of the present disclosure.
As shown in fig. 5, based on the same application concept, the embodiment of the present specification describes a low-carbon-emission ship including: a liquefied natural gas fuel storage system, a ship carbon capture system, a combined carbon dioxide liquefaction and liquefied natural gas vaporization processing system 51, and a power system.
A natural gas liquid fuel storage system is used to provide natural gas liquid.
The ship carbon capture system is used for capturing carbon dioxide in low-carbon emission ship tail gas.
The carbon dioxide liquefaction and liquefied natural gas vaporization combined processing system 51 is respectively connected with a liquefied natural gas fuel storage system, a ship carbon capture system and a power system.
The combined carbon dioxide liquefaction and liquefied natural gas vaporization processing system 51 includes a carbon dioxide liquefaction system and a liquefied natural gas vaporization system.
The combined processing system for carbon dioxide liquefaction and liquefied natural gas vaporization is installed in a space area formed from a ship center line to a stern transom and from a ship bottom plate to a compass deck along the ship length direction.
Carbon dioxide liquefaction and liquefied natural gas vaporization combined processing system any one of the carbon dioxide liquefaction and liquefied natural gas vaporization combined processing system described above.
The low-pressure storage device 511 in the carbon dioxide liquefaction system is provided on the deck of the ship or in a compartment below the deck of the ship.
The low-pressure storage device is arranged in a mode that the ship structure cargo tank is transformed, the transformation cost can be reduced, and the storage space is improved.
Such an arrangement reduces the amount of heat generated by radiation, and thus liquid CO2The evaporation rate of (c).
The power system is used for providing power for the low-carbon emission ship.
While certain embodiments of the present disclosure have been described above, other embodiments are within the scope of the following claims. In some cases, the actions or steps recited in the claims may be performed in a different order than in the embodiments and still achieve desirable results. In addition, the processes depicted in the accompanying figures do not necessarily have to be in the particular order shown or in sequential order to achieve desirable results. The embodiments in the present specification are described in a progressive manner, and the same and similar parts among the embodiments are referred to each other, and each embodiment focuses on the differences from the other embodiments.
It should also be noted that the terms "comprises," "comprising," or any other variation thereof, are intended to cover a non-exclusive inclusion, such that a process, method, article, or apparatus that comprises a list of elements does not include only those elements but may include other elements not expressly listed or inherent to such process, method, article, or apparatus. Without further limitation, an element defined by the phrase "comprising an … …" does not exclude the presence of other identical elements in the process, method, article, or apparatus that comprises the element.
The above description is only an example of the present specification, and is not intended to limit the present application. Various modifications and changes may occur to those skilled in the art. Any modification, equivalent replacement, improvement, etc. made within the spirit and principle of the present application should be included in the scope of the claims of the present application.

Claims (10)

1. A carbon dioxide liquefaction system for carrying out liquefaction separation on carbon dioxide captured in ship tail gas, characterized by comprising: the device comprises a buffer separation device, a supercharging device and a heat exchanger;
the buffering and separating device is used for cooling, decompressing and separating carbon dioxide gas from the ship carbon capture system, and a first input end of the buffering and separating device is connected with the ship carbon capture system;
the pressurizing device is used for pressurizing the carbon dioxide gas output by the buffer separation device, and the input end of the pressurizing device is connected with the output end of the buffer separation device;
the heat exchanger is used for heat exchange between liquefied natural gas and pressurized carbon dioxide gas, a first input end of the heat exchanger is connected with a liquefied natural gas fuel storage system, a first output end of the heat exchanger is used for outputting gaseous natural gas generated after heat exchange, a second input end of the heat exchanger is connected with an output end of the supercharging device, a second output end of the heat exchanger is used for outputting liquid carbon dioxide generated after heat exchange,
and the third output end of the heat exchanger is connected with the second input end of the buffer separation device and is used for inputting the heat-exchanged carbon dioxide gas into the buffer separation device so as to mix the heat-exchanged carbon dioxide gas with the cooled and decompressed carbon dioxide gas.
2. The apparatus of claim 1, the buffer separation apparatus comprising: the device comprises a first temperature sensor, a throttle valve and a buffer separation tank;
the first temperature sensor is connected with the throttling valve and used for detecting the temperature of the carbon dioxide gas input into the buffer separation tank and generating a first temperature signal;
the input end of the throttle valve is connected with the ship carbon capture system, the throttle valve is used for carrying out temperature reduction and pressure reduction treatment on carbon dioxide gas from the ship carbon capture system according to the first temperature signal,
the output end of the throttling valve is connected with the first input end of the buffer separation tank, so that the cooled and decompressed carbon dioxide is input into the buffer separation tank in a gaseous state;
a second input end of the buffer separation tank is connected with a third output end of the heat exchanger so as to receive the heat-exchanged carbon dioxide gas, so that the heat-exchanged carbon dioxide gas and the cooled and decompressed carbon dioxide gas are mixed in the buffer separation tank;
and a first output end of the buffer separation tank is connected with the supercharging device, and a second output end of the buffer separation tank is connected with the ship carbon capture system so as to return condensed liquid.
3. The apparatus of claim 2, the buffer separation tank comprising a gas-water separation device;
the gas-water separation device is arranged at the top of the buffer separation tank and used for dehumidifying the carbon dioxide gas output from the buffer separation tank.
4. The apparatus of claim 1, further comprising: a pressure regulating device;
the pressure regulating device comprises a pressure regulating valve and a first pressure sensor connected with the pressure regulating valve,
the first pressure sensor is arranged on the heat exchanger and used for detecting the gas pressure of the carbon dioxide gas in the heat exchanger to generate a first pressure signal;
the pressure regulating valve is respectively connected with the heat exchanger and the buffer separation device and used for regulating the pressure of the carbon dioxide gas input into the heat exchanger according to the first pressure signal.
5. The apparatus of claim 1, further comprising: a low voltage storage device;
and the input end of the low-pressure storage device is connected with the second output end of the heat exchanger and is used for storing the liquid carbon dioxide.
6. The apparatus of claim 5, further comprising: the liquid carbon dioxide output control device is used for controlling the output of the liquid carbon dioxide;
the liquid carbon dioxide output control device comprises a liquid level sensor, a second temperature sensor and a flow control valve;
the liquid level sensor is arranged on the heat exchanger and connected with the flow control valve, and the liquid level sensor is used for detecting the liquid level of liquid carbon dioxide in the heat exchanger and generating a liquid level signal;
the second temperature sensor is connected with the flow control valve and used for detecting the temperature of the liquid carbon dioxide output by the heat exchanger and generating a second temperature signal;
and the flow control valve is respectively connected with the heat exchanger and the low-pressure storage device and is used for controlling the output of the liquid carbon dioxide in the heat exchanger according to the liquid level signal and the second temperature signal.
7. The apparatus of claim 5, further comprising: the cabin pressure control valve and a second pressure sensor are connected with the cabin pressure control valve;
the second pressure sensor is arranged on the low-pressure storage device and used for detecting the air pressure in the low-pressure storage device and generating a second pressure signal;
the low-pressure storage device, the cabin pressure control valve and the buffer separation device are sequentially connected;
the cabin pressure control valve is used for controlling the output of carbon dioxide evaporation gas in the low-pressure storage device according to the second pressure signal, so that the pressure in the low-pressure storage device is controlled.
8. A carbon dioxide liquefaction and liquefied natural gas vaporization combined processing system is used for cooling and separating carbon dioxide captured in ship tail gas by using cold energy generated in the process of vaporizing liquefied natural gas, and is characterized by comprising the following components: a carbon dioxide liquefaction system and a liquid natural gas vaporization system;
the carbon dioxide liquefaction system of any of claims 1 to 8;
the liquefied natural gas vaporization system includes: a fuel pump, a heater, and a temperature control device;
the fuel pump is respectively connected with the liquefied natural gas fuel storage system in the ship and the heat exchanger and is used for inputting liquefied natural gas from the liquefied natural gas fuel storage system in the ship into the heat exchanger;
the heater is used for heating the gaseous natural gas from the heat exchanger through circulating condensed water, and the gaseous natural gas is generated after the liquid natural gas is subjected to heat exchange through the heat exchanger;
a first input end of the heater is connected with a first output end of the heat exchanger, and a first output end of the heater is connected with a power system in the ship;
the temperature control device comprises a temperature control valve and a third temperature sensor connected with the temperature control valve;
the third temperature sensor is used for detecting the temperature of the gaseous natural gas output by the heater and generating a third temperature signal;
the temperature control valve is connected with a second input end of the heater and used for controlling the input of the condensed water according to the third temperature signal, and the second input end of the heater is used for inputting the condensed water.
9. The apparatus of claim 8, further comprising: a control system for controlling the operation of the combined carbon dioxide liquefaction and liquefied natural gas vaporization processing system;
the control system is respectively connected with the first temperature sensor, the throttling valve, the first pressure sensor, the pressure regulating valve, the liquid level sensor, the second temperature sensor, the flow control valve, the second pressure sensor, the cabin pressure control valve, the third temperature sensor and the temperature control valve.
10. A low carbon emission vessel, comprising: the system comprises a liquefied natural gas fuel storage system, a ship carbon capture system, a carbon dioxide liquefaction and liquefied natural gas vaporization combined processing system and a power system;
the liquefied natural gas fuel storage system is used for providing liquefied natural gas;
the ship carbon capture system is used for capturing carbon dioxide in the low-carbon-emission ship tail gas;
the power system is used for providing power;
the carbon dioxide liquefaction and liquefied natural gas vaporization combined processing system is respectively connected with the liquefied natural gas fuel storage system, the ship carbon capture system and the power system;
the carbon dioxide liquefaction and liquefied natural gas vaporization combined treatment system is arranged in a space area formed from a ship centerline to a stern closing plate or from a ship bottom plate to a compass deck along the ship length direction;
the combined processing system for carbon dioxide liquefaction and liquefied natural gas vaporization is the combined processing system for carbon dioxide liquefaction and liquefied natural gas vaporization of any one of claims 8 to 9;
the low-pressure storage device is arranged on a deck of the ship or in a compartment below the deck of the ship.
CN202110492550.XA 2021-05-06 2021-05-06 Carbon dioxide liquefaction system, carbon dioxide liquefaction and liquefied natural gas vaporization combined treatment system and low-carbon-emission ship Pending CN113188291A (en)

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Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN114877619A (en) * 2022-06-07 2022-08-09 上海齐耀螺杆机械有限公司 System and method for liquefying carbon dioxide
WO2024011780A1 (en) * 2022-07-13 2024-01-18 江苏科技大学 Low-temperature carbon capture coupling cold energy and waste heat gradient utilization system for lng-powered vessel

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN114877619A (en) * 2022-06-07 2022-08-09 上海齐耀螺杆机械有限公司 System and method for liquefying carbon dioxide
WO2024011780A1 (en) * 2022-07-13 2024-01-18 江苏科技大学 Low-temperature carbon capture coupling cold energy and waste heat gradient utilization system for lng-powered vessel

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