WO2017222239A1 - Appareil de récupération de composés organiques volatils - Google Patents

Appareil de récupération de composés organiques volatils Download PDF

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Publication number
WO2017222239A1
WO2017222239A1 PCT/KR2017/006267 KR2017006267W WO2017222239A1 WO 2017222239 A1 WO2017222239 A1 WO 2017222239A1 KR 2017006267 W KR2017006267 W KR 2017006267W WO 2017222239 A1 WO2017222239 A1 WO 2017222239A1
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Prior art keywords
gas
heat exchanger
volatile organic
high pressure
liquid
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PCT/KR2017/006267
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English (en)
Korean (ko)
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최성윤
한준희
류시진
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삼성중공업 주식회사
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Publication of WO2017222239A1 publication Critical patent/WO2017222239A1/fr
Priority to NO20181643A priority Critical patent/NO20181643A1/en

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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B65—CONVEYING; PACKING; STORING; HANDLING THIN OR FILAMENTARY MATERIAL
    • B65D—CONTAINERS FOR STORAGE OR TRANSPORT OF ARTICLES OR MATERIALS, e.g. BAGS, BARRELS, BOTTLES, BOXES, CANS, CARTONS, CRATES, DRUMS, JARS, TANKS, HOPPERS, FORWARDING CONTAINERS; ACCESSORIES, CLOSURES, OR FITTINGS THEREFOR; PACKAGING ELEMENTS; PACKAGES
    • B65D90/00—Component parts, details or accessories for large containers
    • B65D90/22—Safety features
    • B65D90/30—Recovery of escaped vapours
    • 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
    • F02M25/00—Engine-pertinent apparatus for adding non-fuel substances or small quantities of secondary fuel to combustion-air, main fuel or fuel-air mixture
    • F02M25/08—Engine-pertinent apparatus for adding non-fuel substances or small quantities of secondary fuel to combustion-air, main fuel or fuel-air mixture adding fuel vapours drawn from engine fuel reservoir
    • 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
    • F25B—REFRIGERATION MACHINES, PLANTS OR SYSTEMS; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS
    • F25B39/00—Evaporators; Condensers
    • F25B39/02—Evaporators
    • 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
    • F25B—REFRIGERATION MACHINES, PLANTS OR SYSTEMS; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS
    • F25B43/00—Arrangements for separating or purifying gases or liquids; Arrangements for vaporising the residuum of liquid refrigerant, e.g. by heat
    • 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
    • F25B—REFRIGERATION MACHINES, PLANTS OR SYSTEMS; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS
    • F25B43/00—Arrangements for separating or purifying gases or liquids; Arrangements for vaporising the residuum of liquid refrigerant, e.g. by heat
    • F25B43/003—Filters
    • 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
    • F25B—REFRIGERATION MACHINES, PLANTS OR SYSTEMS; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS
    • F25B43/00—Arrangements for separating or purifying gases or liquids; Arrangements for vaporising the residuum of liquid refrigerant, e.g. by heat
    • F25B43/02—Arrangements for separating or purifying gases or liquids; Arrangements for vaporising the residuum of liquid refrigerant, e.g. by heat for separating lubricants from the refrigerant
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/0002—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the fluid to be liquefied
    • F25J1/0022—Hydrocarbons, e.g. natural gas
    • 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
    • F25J2205/84—Processes or apparatus using other separation and/or other processing means using filter

Definitions

  • the present invention relates to a device for recovering volatile organic compounds, and more particularly, to a device for recovering volatile organic compounds designed to suppress the emission of volatile organic compounds generated in a crude oil storage tank and to make the best use of available energy. .
  • Volatile organic compounds are organic compounds that evaporate easily due to their low boiling point, and contain various kinds of ingredients depending on their origin. Volatile organic compounds may be toxic or odorous and may contain flammable components. When volatile organic compounds are released into the atmosphere, they pollute the air, and therefore, a technique for treating them is required.
  • Fossil fuels such as crude oil also contribute to the formation of volatile organic compounds. Excessive generation of volatile organic compounds in crude oil carriers and the like for transporting such crude oil is a problem. Volatile organic compounds occur especially during the loading or unloading of liquid cargo such as crude oil, and may be generated inside the tank during the transportation of crude oil to increase the pressure. Therefore, more effective treatment of such volatile organic compounds is required.
  • the technical problem to be achieved by the present invention is to solve the above problems, to provide a volatile organic compound recovery apparatus designed to suppress the air emissions of volatile organic compounds generated in the crude oil storage tank and to make the best use of the available energy.
  • the volatile organic compound recovery device includes a first compressor for compressing oil vapor supplied from a crude oil storage tank, a first heat exchanger for cooling a high pressure fluid passed through the first compressor, and the first heat exchanger.
  • An expansion valve for depressurizing the first gas separated from the high pressure fluid through a high pressure fluid or a pretreatment unit, the high pressure fluid passing through the expansion valve, or the first gas is separated into a second gas and a second liquid.
  • the second gas is supplied to the combustion engine, the second liquid includes a gas-liquid separator to supply to the storage tank.
  • the apparatus may further include a second heat exchanger installed between the first heat exchanger and the expansion valve to heat exchange the second gas separated from the gas-liquid separator, and the high pressure fluid or the first gas.
  • a third heat exchanger installed between the second heat exchanger and the expansion valve to heat-exchange the second liquid separated from the gas-liquid separator and the high pressure fluid or the first gas.
  • the pretreatment unit may further include a pretreatment separator installed between the first heat exchanger and the second heat exchanger to separate the first gas from the high pressure fluid and to provide the second heat exchanger.
  • the pretreatment unit may further include a water removal unit installed between the first heat exchanger and the pretreatment separator, or between the pretreatment separator and the second heat exchanger.
  • the pretreatment unit may further include a second compressor installed between the pretreatment separator and the second heat exchanger to pressurize the first gas.
  • the apparatus may further include a fourth heat exchanger installed between the second compressor and the second heat exchanger to cool the first gas.
  • the apparatus may further include a branch pipe branched from a conduit through which the first gas flows between the second compressor and the gas-liquid separator, and a high pressure tank connected to the branch pipe to store the first gas.
  • It may further include a pressure reducing valve formed in the branch pipe to control the pressure of the first gas flowing into the high pressure tank.
  • It may further include an evaporator installed between the first heat exchanger and the second heat exchanger to convert the LNG into NG (Natural gas) by heat-exchanging the LNG (Liquefied natural gas), the high pressure fluid or the first gas.
  • NG Natural gas
  • LNG Liquified natural gas
  • the pretreatment separator may be a three-phase separator that separates the first gas, water, and a first liquid comprising a component having a specific gravity smaller than that of the water.
  • It may further include a filtration unit installed between the crude oil storage tank and the first compressor to remove the solid foreign matter and liquid foreign matter contained in the oil vapor.
  • the volatile organic compounds generated in the crude oil storage tank and the like can be treated by a series of continuous treatment processes to minimize the emission of air.
  • FIG. 1 is a block diagram of a volatile organic compound recovery apparatus according to a first embodiment of the present invention.
  • FIG. 2 is a block diagram of a volatile organic compound recovery apparatus according to a second embodiment of the present invention.
  • FIG. 3 is a block diagram of a volatile organic compound recovery apparatus according to a third embodiment of the present invention.
  • FIG. 4 is a configuration diagram of a volatile organic compound recovery apparatus according to a fourth embodiment of the present invention.
  • FIG. 5 is a configuration diagram of a volatile organic compound recovery apparatus according to a fifth embodiment of the present invention.
  • FIG. 6 is a block diagram of a volatile organic compound recovery apparatus according to a sixth embodiment of the present invention.
  • FIGS. 1 to 6 a sixth embodiment of the present invention will be described in detail with reference to FIGS. 1 to 6.
  • the solid arrows connecting the components indicate the 'flow' of the fluid and the 'pipe' through which the fluid flows. Therefore, even if not described with a separate sign it can be understood that the conduit is formed along each solid arrow.
  • 'second gas' and 'second liquid' are defined as fluids generated by separation of a 'gas liquid separator' into a gas phase and a liquid phase.
  • FIG. 1 is a block diagram of a volatile organic compound recovery apparatus according to a first embodiment of the present invention.
  • the volatile organic compound recovery device 1 of the present invention is a continuous series of organic vapors generated in the crude oil storage tank A (which may include volatile organic compounds generated from crude oil and inert gas, etc., filled in the tank). Processing is continuously carried out through the processing step. Treatment steps include pressurization, depressurization, and temperature control of the fluid, phase change, and separation of fluids with different phases, temperature control of fluid through heat exchange between different fluids, and the like.
  • the volatile organic compound recovery apparatus 1 is composed of a plurality of components organically connected to each other to perform such a process. Through a series of processes by the operation of these components it is possible to minimize the emissions by recovering volatile organic compounds, and also to improve the energy efficiency by recovering the available energy of the volatile organic compounds as much as possible.
  • the volatile organic compound recovery apparatus 1 is configured as follows.
  • the volatile organic compound recovery device (1) is a first heat exchanger for cooling the high pressure fluid (B) passed through the first compressor (10) and the first compressor (10) for compressing the oil vapor supplied from the crude oil storage tank (A). (20), an expansion valve (30) and an expansion valve (30) for depressurizing the first gas separated from the high pressure fluid (B) through the high pressure fluid (B) passing through the first heat exchanger (20) or the pretreatment unit;
  • the high pressure fluid B, or the first gas passed through the gas is separated into a second gas C1 and a second liquid C2, and the second gas C1 is supplied to the combustion engine D, and the second liquid is supplied.
  • the C2 includes a gas-liquid separator 40 for supplying the storage tank 100.
  • the gas-liquid separator 40 may generate the second gas C1 and the second liquid C2 and provide the same to the combustion engine D or store the same in the storage tank 100. .
  • the volatile organic compound recovery device 1 may include a pretreatment unit that separates the first gas from the high pressure fluid B that has passed through the first compressor 10 and participates in the recovery process, or may be formed without the pretreatment unit. Can be.
  • a pretreatment unit that separates the first gas from the high pressure fluid B that has passed through the first compressor 10 and participates in the recovery process
  • Can be In the first embodiment of the present invention, and the second embodiment to be described later, description will be made based on the case where the pretreatment unit is not provided. In this case, the available energy is directly recovered from the high pressure fluid B that has passed through the first compressor 10, and the first gas is not generated and thus does not participate in the energy recovery process.
  • Figure 1 will be described in more detail with respect to each component and operation of the volatile organic compound recovery apparatus 1 according to the first embodiment of the present invention.
  • the first compressor 10 pressurizes and compresses the oil vapor supplied from the crude oil storage tank (A). Crude oil is stored in the crude oil storage tank (A) and the oil vapor may include volatile organic compounds generated from the crude oil and some other substances (such as inert gas injected into the tank).
  • the first compressor 10 converts the high pressure fluid B by pressurizing the oil vapor.
  • the first compressor 10 may be formed to increase the pressure of the fluid using a rotary blade that rotates in the pressure chamber, or may be formed of a reciprocating compressor using a cylinder. However, this does not need to be understood as such an example of the formation method of the compressor.
  • Various types of compressors can be applied by selectively and complexly utilizing various structures within the limit of fluid compression.
  • the high pressure fluid B compressed by the first compressor 10 is supplied to the first heat exchanger 20.
  • the filtration unit 90 is disposed in front of the first compressor 10.
  • the filtration unit 90 may be installed between the crude oil storage tank A and the first compressor 10 to remove solid foreign matter and liquid foreign matter contained in the oil vapor. Unnecessary foreign substances contained in the oil vapor can be removed by the filtration unit 90 and a pure gas containing volatile organic compounds can be supplied to the first compressor 10 to improve the compression ratio and the energy recovery capability.
  • the filtration unit 90 may include a scrubber, a centrifuge, and the like.
  • the filtration unit 90 may be used to remove foreign substances such as soot, liquid droplets, etc. from the oil vapor by using the filtration unit 90. ) Can be supplied.
  • Crude oil storage tank (A) may be installed on a vessel such as a crude oil transport ship, but need not be limited thereto.
  • Crude oil storage tanks (A) include all refineries, transportation facilities, storage facilities, and other types of facilities for storing or importing crude oil.
  • the crude oil storage tank (A) is stored crude oil to generate volatile organic compounds, and the volatile organic compound recovery device (1) of the present invention can effectively recover the volatile organic compounds generated from crude oil and the available energy contained therein.
  • Crude oil storage tank (A) is a facility for storing the substances that cause the generation of volatile organic compounds such as crude oil, and even if not described separately, the object of application of the volatile organic compound recovery device (1) of the present invention is such a crude oil storage tank (A) It is not limited to. That is, the crude oil storage tank (A) is described herein by way of example, but the present invention can be applied to various other facilities in which volatile organic compounds are produced, and the technical concept of the present invention is limited to storage facilities such as crude oil. Need not be interpreted.
  • the first heat exchanger 20 cools the high pressure fluid B that has passed through the first compressor 10.
  • the high pressure fluid B having a temperature rise and passing through the first compressor 10 is cooled while passing through the first heat exchanger 20.
  • the first heat exchanger 20 may include one or more flow paths connected to each other to allow heat exchange.
  • the first heat exchanger 20 may have a structure in which a flow path through which the high pressure fluid B flows and a flow path through which the coolant flows contact each other to allow heat exchange.
  • the cooling water supplied to the first heat exchanger 20 may be clear water, distilled water, or the like. When the present invention is applied to a facility such as a ship, sea water may be used as the cooling water. Depending on the situation, it is possible to cool the high pressure fluid (B) by heat exchange with various different types of cooling water.
  • the high pressure fluid B which has passed through the first heat exchanger 20, passes through the expansion valve 30 and is decompressed. That is, the high pressure fluid B pressurized by the first compressor 10 may be expanded by the expansion valve 30 to reduce the pressure and rapidly lower the temperature. Through this it can be supplied by lowering the temperature of the fluid to a temperature that can be easily operated in the gas-liquid separator 40 of the rear end.
  • the expansion valve 30 may be, for example, using a Joule-Thomson effect to depressurize and cool the pressurized fluid through the nozzle.
  • the decompression rate of the expansion valve 30 may be appropriately set or adjusted in consideration of the operating temperature and the pressure of the gas-liquid separator 40.
  • the gas-liquid separator 40 is a second gas through a high pressure fluid (B) (that is, a fluid that is compressed and supplied to the expansion valve at a high pressure state and depressurized while passing through the expansion valve as described above) through the expansion valve (30).
  • B high pressure fluid
  • the separated second gas C1 is supplied to the combustion engine D, and the second liquid C2 is supplied to the storage tank 100.
  • the second gas (C1) and the second liquid (C2) are collected by separating the vapor of the above-mentioned volatile organic compounds into gaseous and liquid phases and contain flammable components, which are directly used as fuel of the combustion engine (D), or It can be converted into gaseous state and used as fuel.
  • Gas-liquid separator 40 may be formed to separate the second gas (C1) and the second liquid (C2) by the difference in density, and discharge the second gas (C1) in the upper portion and the second liquid (C2) in the lower portion ) May be formed in the form of a container or drum for discharging.
  • the fluid provided under the reduced pressure and cooling in the expansion valve 30 to the gas-liquid separator 40 may be separated into a gaseous phase and a liquid phase and used immediately as a fuel or may be stored as a fuel. It may also be used to lower the temperature by heat exchange with the high pressure fluid B before it is used or stored as fuel (see second embodiment 6, described below). That is, the gaseous and liquid components (second gas and second liquid) generated by the cooling process of the expansion valve 30 and the phase separation process of the gas-liquid separator 40 are provided as fuel, so that the available energy is effectively supplied through one or more paths. It is recovered.
  • the second gas C1 is supplied to the combustion engine D after cooling the high pressure fluid B in the second heat exchanger 50 and is consumed.
  • the second liquid C2 is consumed in the second heat exchanger 50.
  • the cooled high pressure fluid B is recooled in the third heat exchanger 60 and then stored in the storage tank 100. In this way, the fluid containing the volatile organic compounds can be treated in a stepwise manner to recover available energy and greatly reduce the amount of emissions.
  • the combustion engine D inflowing and consuming the second gas C1 may include a gas turbine, a gas burner, or the like. If the combustion engine (D) is an engine that generates rotational power, such as a gas turbine, the generator can be combined with the rotary shaft of the gas turbine to produce electric power. The waste heat is recovered at the rear of the gas turbine to generate steam and generate power using the engine. Combined with a heat recovery steam generator (HRSG) that produces energy, energy recovery can be greatly increased.
  • a gas turbine or gas burner may be provided and selectively connected to drive a generator coupled to the gas turbine or to utilize thermal energy generated by the gas burner, and the second liquid C2 stored in the storage tank 100.
  • the volatile organic compound recovery apparatus 1-1 is constructed as follows.
  • the volatile organic compound recovery device 1-1 is a first compressor 10 for compressing oil vapor supplied from a crude oil storage tank A, and a first compressor for cooling the high pressure fluid B passed through the first compressor 10.
  • Expansion valve 30 for reducing the pressure of the first gas separated from the high pressure fluid B through the heat exchanger 20, the first heat exchanger 20, or the pretreatment unit 30, an expansion valve ( The high pressure fluid B passed through 30 or the first gas is separated into a second gas C1 and a second liquid C2, and the second gas C1 is supplied to the combustion engine D.
  • Second liquid (C2) is installed between the gas-liquid separator 40, the first heat exchanger 20 and the expansion valve 30 to supply to the storage tank 100, the second gas (C1) separated from the gas-liquid separator (40) ), A second heat exchanger 50 for exchanging the high pressure fluid B or the first gas, and the second heat exchanger 50 and the expansion valve 30 are separated from the gas-liquid separator 40.
  • Second liquid (C2), high pressure fluid (B) or the 1 comprises a third heat exchanger 60 to heat the gas.
  • the volatile organic compound recovery apparatus 1-1 includes a second heat exchanger 50 and a third heat exchanger between the first heat exchanger 20 and the expansion valve 30. 60) is installed to cool the fluid in stages.
  • the second heat exchanger 50 and the third heat exchanger 60 are respectively injected into the expansion valve 30 by utilizing the second gas C1 and the second liquid C2 separated from the gas-liquid separator 40 as refrigerant. It is possible to greatly improve the cooling efficiency of the fluid.
  • the second heat exchanger 50 and the third heat exchanger 60 are installed on a flow path through which the high pressure fluid B flows toward the expansion valve 30 as shown.
  • the second heat exchanger (50) is installed between the first heat exchanger (20) and the expansion valve (30), and introduces a second gas (C1) separated from the gas-liquid separator (40) to exchange heat with the high pressure fluid (B). Let's do it.
  • the third heat exchanger (60) is installed between the second heat exchanger (50) and the expansion valve (30) and introduces a second liquid (C2) separated from the gas-liquid separator (40) to supply the high pressure fluid (B). Heat exchange with.
  • the second heat exchanger 50 and the third heat exchanger 60 may also include one or more flow paths connected to each other to enable heat exchange, and each of the flow paths through which the high pressure fluid B flows, and the second gas C1 or the first heat exchanger, respectively.
  • the flow path in which the two liquids C2 flow may be formed in a structure in which the two liquids C2 are in contact with each other to allow heat exchange.
  • the fluid provided under the reduced pressure and cooling in the expansion valve 30 to the gas-liquid separator 40 may be separated into a gaseous phase and a liquid phase and used immediately as a fuel or may be stored as a fuel. It may also be used to lower the temperature by heat exchange with the high pressure fluid (B) before it is used or stored as fuel. That is, the gaseous and liquid components (second gas and second liquid) generated by the cooling process of the expansion valve 30 and the phase separation process of the gas-liquid separator 40 are separated from the high pressure fluid B at the front end of the expansion valve 30. By heat exchange in stages, the cooling efficiency of the high pressure fluid (B) is greatly improved, and then provided as a fuel, the available energy is effectively recovered through various paths.
  • the second gas C1 is supplied to the combustion engine D after cooling the high pressure fluid B in the second heat exchanger 50 and is consumed.
  • the second liquid C2 is consumed in the second heat exchanger 50.
  • the cooled high pressure fluid B is recooled in the third heat exchanger 60 and then stored in the storage tank 100. In this way, the fluid containing the volatile organic compounds can be treated in a stepwise manner to recover available energy and greatly reduce the amount of emissions.
  • FIG. 3 is a block diagram of a volatile organic compound recovery apparatus according to a third embodiment of the present invention.
  • the volatile organic compound recovery apparatus 1-2 separates the first gas from the high pressure fluid B that has passed through the first compressor 10 in the recovery process. And a preprocessing unit 70 for engaging.
  • the high pressure fluid B passing through the first compressor 10 is separated into the first gas B1 and the first liquid B2 in the pretreatment unit 70.
  • the first gas B1 is collected into the second gas C1 and the second liquid C2 through pressure change, heat change, phase change, and the like, and the first liquid B2 is stored in the storage tank 100. Stored.
  • the pretreatment unit 70 By providing the pretreatment unit 70, the fluid handling capacity at the rear end is reduced, so that the energy of each treatment process is reduced and the available energy recovery can be increased.
  • the pretreatment unit 70 is disposed between the first heat exchanger 20 and the second heat exchanger 50 as shown.
  • the pretreatment unit 70 separates the high pressure fluid B, which has passed through the first heat exchanger 20, into the first gas B1 and the first liquid B2, and separates the first gas B1 from the second heat exchanger. 50) to the side.
  • the pretreatment unit 70 includes a pretreatment separator 71, and the pretreatment separator 71 is installed between the first heat exchanger 20 and the second heat exchanger 50 so that the first gas (B) B1) is separated and provided to the second heat exchanger (50).
  • the first gas B1 separated from the pretreatment separator 71 is supplied to the expansion valve 30 through additional processing, passes through the expansion valve 30, and is decompressed to thereby greatly reduce the temperature.
  • the reduced pressure and cooled first gas B1 flows into the gas-liquid separator 40 and is separated into the second gas C1 and the second liquid C2, and the second heat exchanger 50 is processed as described above. ) And a third heat exchanger 60 to exchange heat with the first gas B1.
  • the first gas B1 at the rear end of the pretreatment unit 70 passes through the second heat exchanger 50, the third heat exchanger 60, the expansion valve 30, the gas-liquid separator 40, and the like.
  • the fluid B performs substantially the same process as the process performed while passing through the second heat exchanger 50, the third heat exchanger 60, the expansion valve 30, and the gas-liquid separator 40. Therefore, the detailed description thereof will be replaced with the above description. That is, the first gas B1 supplied from the pretreatment unit 70 to the second heat exchanger 50 is cooled by heat exchange with the second gas C1 provided to the second heat exchanger 50, and the second heat exchanger 50.
  • the first gas B1 cooled in this manner is rapidly depressurized while passing through the expansion valve 30, and is rapidly reduced in temperature, and is separated from the gas-liquid separator 40 into the second gas C1 and the second liquid C2. .
  • the second gas C1 and the second liquid C2 are consumed in the combustion engine D after passing through the second heat exchanger 50 and the third heat exchanger 60 or the storage tank 100. ) And used as needed.
  • the volatile organic compound recovery apparatus 1-2 separates the first gas B1 from the high pressure fluid B through the pretreatment unit 70 in the above-described energy recovery process.
  • the first gas B1 separates water and liquid components from the high pressure fluid B by using the pretreatment separator 71.
  • the first gas B1 reduces the fluid treatment capacity by providing the first gas B1, which is a gaseous component, in the post-treatment process. The energy consumed in the process can be saved.
  • the pretreatment unit 70 compresses the first gas B1 to a higher pressure, including a second compressor 73 for additionally pressurizing the first gas B1 at the rear end of the pretreatment separator 71, and expands the expansion valve.
  • the pretreatment unit 70 includes a pretreatment separator 71, a water removal unit 72, a second compressor 73, and a fourth heat exchanger 74.
  • the pretreatment separator 71 is installed between the first heat exchanger 20 and the second heat exchanger 50 as shown in the drawing, and introduces a high pressure fluid B that has passed through the first heat exchanger 20 so as to enter the first heat exchanger. It separates into gas B1, water B3, and the 1st liquid B2.
  • the pretreatment separator (71) is introduced into the high pressure fluid (B) and separated into a first gas (B1) as a gaseous component, water (B3), and a first liquid (B2) composed of a component having a specific gravity smaller than that of water (B3).
  • the separated first gas B1 passes through the water removal unit 72, the second compressor 73, and the fourth heat exchanger 74 to the second heat exchanger 50 as described above. Is provided.
  • the first liquid B2 is stored in the storage tank 100 as shown and used together with the second liquid C2 as necessary.
  • the first liquid B2 and the second liquid C2 may be stored together in the storage tank 100 or may be stored separately from the storage space.
  • Water B3 may be stored in a waste water storage tank, for example a slop tank of a crude oil transport ship.
  • the water removal unit 72 is installed between the pretreatment separator 71 and the second heat exchanger 50 to remove the water of the first gas B1.
  • the first gas B1 is converted into a more pure gaseous phase component and thus is converted into a state where additional compression is easily performed.
  • the second compressor 73 is installed between the pretreatment separator 71 and the second heat exchanger 50 and is disposed at the rear end of the water removal unit 72.
  • the first gas B1 from which water is removed by passing through the water removal unit 72 is compressed to a higher pressure while passing through the second compressor 73. That is, the high pressure fluid (B) is generated by passing through the first compressor (10) described above, and passed through the pretreatment separator (71) to separate gas phase components (first gas), and the separated first gas (B1).
  • the second compressor 73 may be formed to increase the fluid pressure by using a rotary blade that rotates in the pressure chamber, or may be formed of a reciprocating compressor using a cylinder.
  • this also does not need to be limited to understand the formation method of the compressor as an example, it is possible to apply a variety of compressors by selectively and complex use of various structures within the limit of the fluid compression.
  • the second compressor 73 compresses the first gas B1 from which the liquid component is separated from the high pressure fluid B, so that the driving energy consumption is small and the capacity is relatively small.
  • the first gas B1 passing through the second compressor 73 passes through the fourth heat exchanger 74 and is preferentially cooled.
  • the fourth heat exchanger 74 is installed between the second compressor 73 and the second heat exchanger 50 and includes the first gas B1 together with the second heat exchanger 50 and the third heat exchanger 60 in the rear stage. To form a multi-stage cooling structure. Through this, the temperature of the first gas B1 compressed at high pressure can be easily cooled to a more suitable temperature.
  • the fourth heat exchanger 74 may also include a flow path structure connected to allow heat exchange, and the fourth heat exchanger 74 may have a structure in which the flow path through which the first gas B1 flows and the flow path through which the coolant flows contact each other to allow heat exchange. .
  • Clear water, distilled water, or the like may be used as the cooling water.
  • sea water may be used as the cooling water.
  • various types of cooling water may be provided to the fourth heat exchanger 74 to cool the first gas B1.
  • the high pressure state of the first gas B1 is provided to the second heat exchanger 50 from the pretreatment unit 70 configured as described above.
  • the first gas B1 is cooled and decompressed through the above-described process, and is rapidly depressurized under high pressure to be provided to the gas-liquid separator 40 at a sufficiently low temperature.
  • a lower temperature of the second gas C1 and the second liquid C2 may be generated, and as described above, the second gas C1 and the second liquid C2 may be transferred to the second heat exchanger 50 and After passing through the third heat exchanger 60, it may be supplied to the combustion engine D or stored in the storage tank 100, and may be used as needed.
  • first liquid (B2) may also be stored in the storage tank 100 together with the second liquid (C2) or stored separately and used as necessary.
  • the available energy of the volatile organic compound may be recovered more effectively, thereby increasing energy efficiency and minimizing the emission of the volatile organic compound.
  • FIG. 4 is a configuration diagram of a volatile organic compound recovery apparatus according to a fourth embodiment of the present invention.
  • the volatile organic compound recovery apparatus 1-3 is a conduit through which the first gas B1 flows between the second compressor 73 and the gas-liquid separator 40. It is connected to the branch pipe 111 and branch pipes 111 branched from the high-pressure tank 110 for storing the first gas (B1).
  • the high pressure tank 110 may be configured to introduce and store the first gas B1 compressed in a multi-stage state under a high pressure state through the branch pipe 111 and discharge and use it as necessary.
  • the branch pipe 111 may be formed to adjust the pressure of the first gas B1 introduced into the high pressure tank 110 by installing a control valve 120. Branch pipe 111 may be branched in the conduit connecting the fourth heat exchanger 74 and the second heat exchanger 50 as shown.
  • the first gas B1 stored in the high pressure tank 110 may be provided to the combustion engine D, for example.
  • a supply pipe (not shown) connecting the high pressure tank 110 and the combustion engine D is formed, and a valve capable of reducing pressure is added to the front of the combustion engine D of the supply pipe so that the first gas ( The pressure of B1) can be adjusted and provided to the combustion engine (D).
  • the combustion engine (D) is formed of a gas turbine or the like through this configuration to respond to the load fluctuations of the turbine and quickly provide the first gas (B1) stored in the high-pressure tank 110 to the combustion engine (D). can do.
  • the high-pressure tank 110 may be configured to recover available energy and more effectively utilize the same.
  • FIG. 5 is a configuration diagram of a volatile organic compound recovery apparatus according to a fifth embodiment of the present invention.
  • the volatile organic compound recovery apparatus 1-4 is installed between the first heat exchanger 20 and the second heat exchanger 50, and has a LNG (Liquefied natural gas).
  • the evaporator 130 may include a flow path structure interconnected to allow heat exchange.
  • the evaporator 130 may flow through the first gas B1 into one flow path and introduce LNG (E1) into the other flow path. It can heat-exchange with (B1).
  • the cryogenic LNG E1 is vaporized by heat exchange with the first gas B1, converted into NG E2, and provided to the consumer F.
  • a pipeline connected between the evaporator 130 and the high pressure fluid B may be introduced into the evaporator 130 and heat exchanged with the LNG E1 to convert NG (E2).
  • the cryogenic LNG (E1) is used as a refrigerant.
  • the consumer F does not need to additionally install a vaporizer or the like for vaporizing the LNG E1, which is efficient in terms of device configuration.
  • the LNG E1 may be provided to the evaporator 130 by a pump 140 connected between the evaporator 130 and the LNG storage tank E, and the NG E2 vaporized in the evaporator 130 may be a consumer F. Can be supplied and used.
  • the consumer F includes an internal combustion engine capable of using NG (E2) as a fuel, a boiler, a turbine, and the like, and controls the pump 140 and adjusts the NG (E2) supply amount in response to these load variations.
  • NG NG
  • the volatile organic compound recovery apparatus 1-4 can be easily applied to a facility equipped with the LNG storage tank E.
  • FIG. 6 is a block diagram of a volatile organic compound recovery apparatus according to a sixth embodiment of the present invention.
  • the water removal unit 72 is disposed in front of the pretreatment separator 71. That is, the water removal unit 72 is disposed between the first heat exchanger 20 and the pretreatment separator 71 so that the water contained in the high pressure fluid B introduced into the pretreatment separator 71 is pretreated separator 71. It can be pretreated before entering the furnace. Therefore, it is not necessary to form the pretreatment separator 71 as the three-phase separator as described above, and pretreatment with a gas-liquid separator in which the high pressure fluid B is introduced into the first gas B1 and the first liquid B2. Separator 71 can be configured. Through this, it is possible to minimize the generation of unnecessary additives and to improve the device configuration, and it is possible to recover the available energy of the volatile organic compound and minimize the emission more efficiently through the process as described above.

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  • Engineering & Computer Science (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Thermal Sciences (AREA)
  • Physics & Mathematics (AREA)
  • Analytical Chemistry (AREA)
  • Power Engineering (AREA)
  • Combustion & Propulsion (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • General Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Separation By Low-Temperature Treatments (AREA)
  • Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)

Abstract

La présente invention concerne un appareil de récupération de composé organique volatil conçu pour supprimer l'émission d'un composé organique volatil dans l'atmosphère et maximiser l'utilisation d'énergie disponible. L'appareil de récupération comprend : un premier compresseur pour comprimer une vapeur d'huile fournie depuis un réservoir de stockage de pétrole brut ; un premier échangeur de chaleur pour refroidir un fluide à haute pression passé à travers le premier compresseur ; un détendeur pour décompresser le fluide à haute pression passé à travers le premier échangeur de chaleur ou un premier gaz séparé du fluide à haute pression par l'intermédiaire d'une unité de prétraitement ; et un séparateur gaz-liquide pour séparer le fluide à haute pression passé à travers le détendeur, ou le premier gaz dans un deuxième gaz et un deuxième liquide et distribuer le deuxième gaz dans un moteur à combustion et le deuxième liquide dans un réservoir de stockage.
PCT/KR2017/006267 2016-06-22 2017-06-15 Appareil de récupération de composés organiques volatils WO2017222239A1 (fr)

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KR1020160078203A KR101741834B1 (ko) 2016-06-22 2016-06-22 휘발성유기화합물 회수장치

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CN112469624A (zh) * 2018-01-25 2021-03-09 韩国造船海洋株式会社 挥发性有机化合物处理系统和船舶

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NO20171222A1 (en) * 2017-07-21 2019-01-22 Waertsilae Gas Solutions Norway As Low emission SVOC fueled oil tanker
CN109916109A (zh) * 2019-01-28 2019-06-21 珠海格力电器股份有限公司 一种热泵系统和空调器
CN117516065B (zh) * 2024-01-08 2024-05-03 连云港市拓普科技发展有限公司 一种低压风冷组合式VOCs气体收集处理装置

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