CN101915494A - Re-liquefaction method of shipped liquid cargo of ethylene/ethane evaporation gas - Google Patents

Re-liquefaction method of shipped liquid cargo of ethylene/ethane evaporation gas Download PDF

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Publication number
CN101915494A
CN101915494A CN2010102383109A CN201010238310A CN101915494A CN 101915494 A CN101915494 A CN 101915494A CN 2010102383109 A CN2010102383109 A CN 2010102383109A CN 201010238310 A CN201010238310 A CN 201010238310A CN 101915494 A CN101915494 A CN 101915494A
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ethylene
ethane
cold
liquid
refrigerant
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李亚军
金光
李国庆
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South China University of Technology SCUT
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South China University of Technology SCUT
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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
    • F25J1/02—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
    • 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
    • F25J1/0025—Boil-off gases "BOG" from storages
    • 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
    • F25J1/003—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"
    • F25J1/0045—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 vaporising a liquid return 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
    • 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
    • F25J1/0047—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 an "external" refrigerant stream in a closed vapor compression cycle
    • F25J1/0052—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 an "external" refrigerant stream in a closed vapor compression cycle by vaporising a liquid refrigerant 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
    • 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
    • F25J1/0097—Others, e.g. F-, Cl-, HF-, HClF-, HCl-hydrocarbons etc. or mixtures thereof
    • 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
    • F25J1/0211—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 a multi-component refrigerant [MCR] fluid in a closed vapor compression cycle
    • F25J1/0212—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 a multi-component refrigerant [MCR] fluid in a closed vapor compression cycle as a single flow MCR cycle
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • 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
    • F25J1/0211—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 a multi-component refrigerant [MCR] fluid in a closed vapor compression cycle
    • F25J1/0219—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 a multi-component refrigerant [MCR] fluid in a closed vapor compression cycle in combination with an internal quasi-closed refrigeration loop, e.g. using a deep flash recycle 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
    • 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
    • F25J1/0264—Arrangement of heat exchanger cores in parallel with different functions, e.g. different cooling streams
    • F25J1/0265—Arrangement of heat exchanger cores in parallel with different functions, e.g. different cooling streams comprising cores associated exclusively with the cooling of a refrigerant stream, e.g. for auto-refrigeration or economizer
    • 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
    • F25J2215/62—Ethane or ethylene

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  • Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Mechanical Engineering (AREA)
  • Thermal Sciences (AREA)
  • General Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Ocean & Marine Engineering (AREA)
  • Filling Or Discharging Of Gas Storage Vessels (AREA)

Abstract

The invention discloses a re-liquefaction method of shipped liquid cargo of ethylene/ethane evaporation gas. The method comprises an open circulatory system by using a liquid cargo as a refrigerant and a closed-type refrigeration circulatory system by using refrigerant, wherein the open circulatory system by using a liquid cargo as a refrigerant comprises the following steps of: recycling the cold energy of the ethylene/ethane evaporation gas; carrying out two-stage compressing on the ethylene/ethane evaporation gas; cooling the ethylene/ethane evaporation gas; and throttling and cooling the ethylene/ethane evaporation gas and charging into a storage tank; and the closed-type refrigeration circulatory system by using refrigerant comprises the following steps of: cooling the ethylene/ethane evaporation gas with the refrigerant; recycling the cold energy of the low-temperature returning refrigerant; carrying out two-stage- compressing on the refrigerant; cooling the refrigerant; and cooling the critical latent heat of the refrigerant. The invention decreases the total power of process flows and improves the utilization efficiency of the energy; the open circulatory system which uses ethylene as the refrigerant increases an cooing equipment compared with the traditional flows, but decreases a part of equipment for cooling the ethylene; and the cooing equipment has small size and high heat transmission efficiency so that the process flows are simple and easy to operate and have higher efficiency.

Description

A kind of method of re-liquefaction of shipping liquid goods ethylene/ethane boil-off gas
Technical field
The invention belongs to the technical field that the boil-off gas (BOG) of liquid petroleum chemicals liquefies again, be specifically related in a kind of shipping liquid goods ethylene/ethane process, the ethylene/ethane storage tank leaks the method for re-liquefaction of the ethylene/ethane BOG that heat produces because of environment.
Background technology
Ethylene industry is the tap of petrochemical industry, occupies critical role in national economy and social development, along with China's petrochemical industry and fast development of national economy, the demand of ethene is also continued to increase.China's ethene consumption figure was 2,431 ten thousand tons in 2008, and ethylene yield is 999.8 ten thousand tons, and the degree of self-sufficiency only is 41.1%.Estimate that China's ethylene yield in 2015 reaches 2,119 ten thousand tons, ethene equivalent demand reaches 3,895 ten thousand tons, and the ethene equivalent degree of self-sufficiency 54.4% still will rely on a large amount of import ethene to satisfy the demands.
The cracking stock of China's ethene is limited by resource, and based on the naphtha of refinery, the production cost of ethene is up to 530 dollars/t; And the Middle East aboundresources, the price of local ethane is 37.5 dollars/t, ethylene raw 85% adopts ethane and propane, reaches 100 dollars/t thereby its production cost of ethylene is hanged down.Therefore select suitable import ethane as ethylene raw,, alleviate the shortage of petroleum resources, have significant social and economic implications reducing domestic production cost of ethylene.
Owing to be about 1/490 of gaseous state volume behind the ethene low-temperature liquefaction under the normal pressure, be approximately 1/435 of gaseous state volume behind the ethane low-temperature liquefaction, under liquefaction so ethene and ethane must can utilize boats and ships to transport economically.The low-temperature liquefied gas carrier is the main means of transportation ethene.
The low-temperature liquefied gas carrier of transportation liquid goods is to approximate greatly under the atmospheric pressure, the temperature of liquid goods ethene is controlled at saturation state loads and transports.In the process of sea-freight because low temperature liquid goods storage tank is subjected to the intrusion of external heat, and in the liquid goods jar during immersed pump operation parts mechanical energy be converted into heat energy, jar interior liquid goods is gasified, i.e. a boil-off gas (BOG, boil-off gas).The generation of BOG makes the interior temperature of liquid goods storage tank raise, and pressure increases, and too high ethene pressure of storage tank can destroy the structure of cargo tank, it is safeguarded also cause danger.If but be discharged into atmosphere, not only very uneconomical, and cause environmental pollution and increase the unsafe factor that discharges inflammable and explosive BOG.Therefore, consider, all need the processing of liquefying again, to reclaim this part BOG to BOG from the security and the economy of boats and ships transportations.
Usually all the BOG reliquefaction installation can be set on the low-temperature liquefaction vessel, the BOG condensation is sent back to liquid tank again.Technology about shipping liquid goods BOG reliquefaction installation has report in document " refrigerating plant-reliquefaction installation of low-temperature liquid gas ship " at present, its device is to adopt the direct kind of refrigeration cycle BOG reliquefaction installation of superposition type technology, be the enclosed kind of refrigeration cycle of cold-producing medium and one with R22 with liquid goods by one promptly is that the open circulation of cold-producing medium is in series.In the cold-producing medium closed cycle of this device, cold-producing medium provides the BOG of cold liquefaction from the evaporation of liquid goods storage tank by compression throttling refrigeration; With liquid goods is in the open circulation of cold-producing medium, and a small part BOG provides cold cooling another part ethene BOG by compression throttling refrigeration, constitutes open circulation.The low temperature BOG that is evaporated from liquid goods storage tank in this technology contains a large amount of colds, directly enters compressor less than reclaiming; Moreover in the cold-producing medium enclosed kind of refrigeration cycle, the backflow cold of cold-producing medium of the low temperature that comes out from air collector does not reclaim yet, but directly advances compressor, causes the waste of cold-producing medium cold, and energy utilization efficiency is low.
Among the patent CN101392980A, a kind of method to above-mentioned flow scheme improvements has been proposed, process chart as shown in Figure 1, technological process is that the open circulation of cold-producing medium is in series by an enclosed kind of refrigeration cycle and one with liquid goods still.Used environment friendly refrigerating fluid R404A in the cold-producing medium circulation, and use an ice chest 12 to reclaim the backflow cold of cold-producing medium of the low temperature that from air collector 22, comes out, having improved is the refrigerating efficiency of the enclosed kind of refrigeration cycle of cold-producing medium with R404A, has improved energy utilization efficiency to a certain extent.But do not have to reclaim the cold of the low temperature BOG that is evaporated from liquid goods storage tank 1 in this flow process, make energy utilization efficiency not high.
Based on above analysis, the present invention proposes a kind of method of re-liquefaction of shipping liquid goods ethylene/ethane boil-off gas, the cold of the low temperature BOG that recovery is evaporated from liquid goods storage tank, and the backflow cold of cold-producing medium of the low temperature that comes out from air collector in the cold-producing medium enclosed kind of refrigeration cycle, be used for cooling off the BOG lime set of high pressure and the cold-producing medium of high pressure respectively, reduce the whole process flow energy consumption to reach, improve the purpose of the liquefaction efficiency again of energy utilization efficiency and ethylene/ethane BOG.
Summary of the invention
In order to solve above-mentioned the deficiencies in the prior art part, primary and foremost purpose of the present invention is to provide the method for re-liquefaction of a kind of liquid of shipping efficiently goods ethylene/ethane boil-off gas (BOG).This method is to improve on the basis of liquefaction technology at the boil-off gas (BOG) on the existing low-temperature liquefied gas carrier again, and its flow process is that open circulation and an enclosed cold-producing medium kind of refrigeration cycle of cold-producing medium is in series by one with liquid goods.Its main feature is to have reclaimed the backflow cold of cold-producing medium of low temperature the cold of the low temperature BOG that is evaporated from the ethylene/ethane storage tank and the kind of refrigeration cycle respectively by two ice chests, improve the efficient of kind of refrigeration cycle, save the consumption of cold-producing medium, made the energy consumption of whole process flow reduce.
To achieve these goals, the present invention is by the following technical solutions: a kind of method of re-liquefaction of shipping liquid goods ethylene/ethane boil-off gas comprises following operating procedure:
(1) with liquid goods is the open-cycle system of cold-producing medium
(1) recovery of ethylene/ethane boil-off gas cold
Low temperature ethylene/the ethane vaporized gas that is evaporated from liquid goods storage tank passes through ice chest A, carries out heat exchange with the high-pressure liquid ethylene/ethane, obtains ethylene/ethane boil-off gas and cryogenic high pressure liquid ethylene/ethane;
(2) two stages of compression of ethylene/ethane boil-off gas
The ethylene/ethane boil-off gas that comes out among step (1) the ice chest A is compressed by two-stage compressor A, and pressure and temperature raises; Intercooler A is arranged between the described two-stage compressor, and intercooler A adopts seawater as low-temperature receiver;
(3) cooling of ethylene/ethane boil-off gas
Will be through the ethylene/ethane boil-off gas behind step (2) the raising pressure, A cools off by seawater heat exchanger, enters the ethylene/ethane condenser then, with the heat exchange of low temperature liquid cold-producing medium, obtains the high-pressure liquid ethylene/ethane; The high-pressure liquid ethylene/ethane enters among the described ice chest A of step (1) and continues to be cooled to cryogenic high pressure liquid ethylene/ethane;
(4) the ethylene/ethane throttling into storage tank of lowering the temperature
Cryogenic high pressure liquid ethylene/ethane is carried out throttling by throttle valve A, pressure and temperature is reduced to the pressure store and the temperature of ethylene/ethane, gaseous ethene/ethane after the throttling and liquid phase ethylene/ethane enter the ethylene/ethane storage tank, and wherein the boil-off gas that is evaporated of gaseous ethene/ethane and ethylene/ethane storage tank is mixed among the ice chest A of step (1) and continues circulation liquefaction again;
(2) enclosed cold-producing medium cooling cycle system
(5) refrigerant cools ethylene/ethane boil-off gas
Low temperature liquid cold-producing medium in the step (3) derives from enclosed cold-producing medium kind of refrigeration cycle, the low temperature liquid cold-producing medium enters in step (3) the ethylene/ethane condenser and the ethylene/ethane boil-off gas heat exchange that improves behind the pressure, the low temperature liquid cold-producing medium undergoes phase transition and becomes gaseous state, obtains refrigerant gas; Refrigerant gas enters in the air collector with from the described gas of step (9) and mixes, and obtains the low temperature cold-producing medium that backflows;
(6) the low temperature recovery of cold-producing medium cold of backflowing
Low temperature in the step (5) cold-producing medium that backflows enters among the ice chest B and to reclaim its cold, and temperature raises and obtains gaseous refrigerant;
(7) two stages of compression of cold-producing medium
With the gaseous refrigerant that comes out among step (6) the ice chest B, B compresses by two-stage compressor, obtains high temperature and high pressure gaseous refrigerant; Intercooler B is arranged between the described two-stage compressor, and intercooler B adopts seawater as low-temperature receiver;
(8) cooling of cold-producing medium
Step (7) gained high temperature and high pressure gaseous refrigerant enters brine cooler B, utilizes cooled with seawater, obtains liquid refrigerant; Liquid refrigerant enters among the ice chest B, with the cold-producing medium heat exchange of backflowing of the described low temperature of step (6), makes liquid refrigerant further cool off, and obtains high-pressure refrigerant;
(9) latent heat of phase change of cold-producing medium cooling
Step (8) gained high-pressure refrigerant, be divided into two strands, one high-pressure refrigerant is by after the choke valve B throttling decrease temperature and pressure, enter flash tank A and carry out adiabatic flash, the gas that comes out from flash tank A top enters the described air collector of step (5), and the liquid refrigerant at the bottom of the flash tank A jar cools off another strand high-pressure refrigerant as low-temperature receiver in Intermediate Heat Exchanger C, obtain the cryogenic high pressure cold-producing medium, liquid refrigerant provides and becomes gaseous state behind the cold and enter the described air collector of step (5); The cryogenic high pressure cold-producing medium is by after the choke valve C throttling decrease temperature and pressure, enter flash tank B and carry out adiabatic flash, the gas that comes out from flash tank B top enters the described air collector of step (5), low temperature liquid cold-producing medium at the bottom of the flash tank B jar enters in the described ethylene/ethane condenser of step (5) and the heat exchange of ethylene/ethane boil-off gas, finishes kind of refrigeration cycle one time.
The temperature range of the described ethylene/ethane boil-off gas of step (1) is-40 ℃～-50 ℃, and the temperature range of cryogenic high pressure liquid ethylene/ethane is-60 ℃～-70 ℃.
The pressure limit that the described ethylene/ethane boil-off gas of step (2) goes out compressor is 0.8MPa～2.0MPa.
The temperature of the described low temperature liquid cold-producing medium of step (3) is-40 ℃～-42 ℃.
The described high-pressure liquid ethylene/ethane of step (3) temperature range-36 ℃～-38 ℃.
The described cold-producing medium of step (5) is R404A; The backflow temperature range of cold-producing medium of described low temperature is-39 ℃～-41 ℃.
The pressure limit that the described gaseous refrigerant of step (7) goes out compressor is 1.5MPa～2.0MPa.
The temperature range of the described liquid refrigerant of step (8) is 28 ℃～38 ℃.
The pressure limit of described flash tank A of step (9) and flash tank B is 0.13MPa～0.14MPa.
The present invention compared with prior art has following outstanding advantage and beneficial effect:
(1) the present invention has reduced the technological process total power consumption, has improved energy utilization efficiency:
By using two ice chests to reclaim the backflow cold of the cold-producing medium that mixes of low temperature the cold of the low temperature BOG that is evaporated from the ethylene/ethane storage tank and the kind of refrigeration cycle respectively, make the consumption of cold-producing medium reduce, the seawater amount of cooling usefulness reduces, and then make that the total power consumption of compressor and sea water pump reduces in the technological process, improved energy utilization efficiency;
(2) technological process becomes simply, is easier to operation:
Be the open-cycle system of cold-producing medium with ethene among the present invention, increased an ice chest equipment though compare existing procedure, but reduced the equipment component of ethene self cooling, saved a separator 7 among Fig. 1, a choke valve 8,10, one blenders 3 of 9, one intercoolers of a flash tank; And, being easier to operation because the ice chest equipment volume is little, and the heat transfer efficiency height makes technological process become simply, efficient is higher.
Description of drawings
Fig. 1 is the prior art processes flow chart, and wherein 1 is the ethylene/ethane storage tank, 2,4 is compressor, and 3 is blender, and 5,15 is seawater heat exchanger, 6 is the ethylene/ethane condenser, and 7,16,24 is separator, and 8,11,17,20 is choke valve, 10,19 is Intermediate Heat Exchanger, and 12 is ice chest, and 13 is two-stage compressor, 14 is intercooler, 9,18,21 is flash tank, and 22 is air collector, and 23 is sea water pump
Fig. 2 is a process chart of the present invention, and wherein 1 is the ethylene/ethane storage tank, and 2,8 is ice chest, 3,9 is two-stage compressor, 4,10 is intercooler, and 5,11 is seawater heat exchanger, and 6 is the ethylene/ethane condenser, 7,13,16 is choke valve, 15 is Intermediate Heat Exchanger, and 12,20 is separator, and 14,17 is flash tank, 18 is air collector, and 19 is sea water pump.
The specific embodiment
The present invention is described in further detail below in conjunction with embodiment and accompanying drawing, but embodiments of the present invention are not limited thereto.
As shown in Figure 2, what following instantiation was described is a liquefied gas carrier that two storage tanks are arranged, and this ship can transport ethene and two kinds of goods of ethane.The useful load of this ship is 10000M 3, the condition of storage of ethene is 0.11MPa (absolute pressure, hereinafter the pressure of Chu Xianing is absolute pressure) ,-102 ℃; The condition of storage of ethane is 0.11MPa ,-87 ℃.Designing requirement according to ethylene/ethane storage tank jar, the ethylene/ethane BOG evaporation rate of ethylene/ethane storage tank every day of this cargo ship is approximately 0.2～0.38% of liquid goods total amount, the BOG amount that will consider also simultaneously that pipeline, other equipment leak heat, ethylene/ethane is loaded or discharging etc. produces; So this ship ethylene/ethane BOG liquefaction system total amount of requiring to possess the BOG of processing again is 2000～3000kg/h, raises and be no more than 4 ℃ to keep on the ship in the constant and ethylene/ethane storage tank of ethylene/ethane tank inner pressure the temperature of liquid goods in 90 hours.The method that this ship adopts the present invention to propose is carried out ethylene/ethane BOG and is liquefied, comprise with the ethylene/ethane and be the open-cycle system of cold-producing medium and be the enclosed cooling cycle system of cold-producing medium with R404A, wherein the amount of the required cold-producing medium R404A that liquefies again of embodiment one liquid goods ethene BOG is 9978kg, and the amount of the required cold-producing medium R404A that liquefies again of embodiment two liquid goods ethane BOG is 9920kg.Concrete processing step and process conditions are as follows:
Embodiment one: the liquefaction again of liquid goods ethene BOG
(1) with ethene is the open-cycle system of cold-producing medium
(1) recovery of ethene BOG cold
Low temperature ethylene BOG (the 2955kg/h that comes out from ethene storage tank 1, pressure is 0.11MPa, temperature is-102 ℃) reclaim its cold by ice chest 2, its cold is used to cool off the high-pressure liquid ethene BOG (2950kg/h, pressure are 1.65MPa, and temperature is-38 ℃) that comes out from ethylene condenser 6, reduce the temperature that liquid ethylene advances choke valve 7, reduce the gasification of ethene in throttling process, improve refrigerating efficiency, obtain ethene BOG and cryogenic high pressure liquid ethylene at last;
(2) two stages of compression of ethene BOG
The ethene BOG temperature of coming out from ice chest 2 in the step (1) is elevated to-45.6 ℃, and by two-stage compressor 3 compressions, pressure is brought up to 1.72MPa then, and temperature is elevated to 133.1 ℃; The power consumption of compressor 3 is 276.2kW, is provided with intercooler 4 between the two-stage compressor, adopts seawater as low-temperature receiver, the temperature that seawater enters intercooler 4 is 25 ℃, and pressure is 0.3MPa, and flow is 3400kg/h, after ethene BOG heat exchange, the temperature of seawater is elevated to 38 ℃.
(3) cooling of ethene BOG
Ethene BOG (pressure 1.72MPa, 133.1 ℃ of temperature) by behind the compressor 3 raising pressure at first enters seawater heat exchanger 5, and the usefulness seawater (10320kg/h, 25 ℃, 0.3MPa) ethene BOG is cooled to 32 ℃, ocean temperature is elevated to 38 ℃; Ethene BOG enters ethylene condenser 6 then, by making ethene BOG be condensed into high-pressure liquid ethene (temperature-38 ℃, pressure 1.65MPa) with low temperature liquid cold-producing medium R404A heat exchange; High-pressure liquid ethene enters ice chest 2 and continues cooling, in ice chest 2 mesohigh liquid ethylenes and the low temperature ethylene BOG heat exchange that is evaporated from ethene storage tank 1, makes that the temperature of liquid ethylene further is reduced to-66 ℃, obtains the cryogenic high pressure liquid ethylene;
(4) the ethene throttling into storage tank of lowering the temperature
The cryogenic high pressure liquid ethylene that comes out from ice chest 2 (66 ℃, 1.65MPa) by choke valve 7 throttlings, make its pressure and temperature all drop to the pressure store of ethene and temperature (102 ℃, 0.11MPa).Gas phase (555kg/h after the throttling,-102 ℃, 0.11MPa) and liquid phase (2400kg/h,-102 ℃, 0.11MPa) ethene all enters ethene storage tank 1, wherein (2400kg/h ,-102 ℃, 0.11MPa) ice chest 2 that is mixed in the step (1) continues circulation liquefaction again to the BOG of gaseous ethene and 1 evaporation of ethene storage tank.
(2) with R404A be the enclosed cooling cycle system of cold-producing medium
(5) refrigerant cools ethene BOG
Low temperature liquid cold-producing medium in the step (3) (7183kg/h, 0.13MPa ,-41.6 ℃) in ethylene condenser 6 with ethene BOG heat exchange, the low temperature liquid cold-producing medium undergoes phase transition and becomes gaseous state (40.8 ℃ 0.13MPa), obtain refrigerant gas; Absorb the heat of ethene BOG in this process, make ethene BOG be condensed into liquid state; The refrigerant gas that comes out from ethylene condenser 6 (40.8 ℃ 0.13MPa) enter air collector 18 and mix with gas from other equipment of step (9), as the low temperature cold-producing medium that backflows.
(6) the low temperature recovery of gaseous mixture cold of backflowing
Low temperature in the step (5) backflow cold-producing medium (9978kg/h ,-40.8 ℃, 0.13MPa) contain a large amount of colds, enter in the ice chest 8 and to reclaim its cold, make the low temperature refrigerant temperature of backflowing be elevated to 14.9 ℃, obtain gaseous refrigerant;
(7) two stages of compression of cold-producing medium
The gaseous refrigerant that step (6) ice chest 8 is come out compresses by two-stage compressor 9, makes its pressure bring up to 1.67MPa, and temperature is elevated to 88.4 ℃, obtains high temperature and high pressure gaseous refrigerant; The power consumption of compressor 9 is 252.2kW, and intercooler 10 is arranged between the two-stage compressor, adopts seawater as low-temperature receiver, the temperature that seawater enters intercooler 10 is 25 ℃, and pressure is 0.3MPa, and flow is 7200kg/h, after the cold-producing medium heat exchange, the temperature of seawater is elevated to 38 ℃.
(8) cooling of cold-producing medium
High temperature and high pressure gaseous refrigerant (88.4 ℃ of temperature, pressure 1.67MPa) from compressor 9 comes out is introduced into brine cooler 11, (35700kg/h, 0.3MPa) is cooled to (32 ℃ of liquid refrigerants by 25 ℃ by seawater, 1.64MPa), ocean temperature is elevated to 38 ℃ simultaneously.Liquid refrigerant enters ice chest 8 then, with the cold-producing medium heat exchange of backflowing of the described low temperature of step (5), makes liquid refrigerant further be cooled to 0 ℃, obtains high-pressure refrigerant.
(9) latent heat of phase change of cold-producing medium cooling
The high-pressure refrigerant that from ice chest 8, comes out, be divided into two strands, one high-pressure refrigerant (flow 2603kg/h, 0 ℃ of temperature, pressure 1.64MPa) (temperature is reduced to-41.5 ℃ by choke valve 13 throttling decrease temperature and pressure, pressure is reduced to 0.13MPa), cold-producing medium after the throttling enters flash tank 14 and carries out adiabatic flash separation gas-liquid phase, (733kg/h, 0.13MPa) enters air collector 18 to the gas that comes out from flash tank 14 tank decks by-41.5 ℃, liquid refrigerant (1870kg/h at the bottom of 14 jars of the flash tanks,-41.5 ℃,, in Intermediate Heat Exchanger 15, utilize the evaporation latent heat of self to cool off another strand high-pressure refrigerant (flow 7375kg/h 0.13MPa) as low-temperature receiver, 0 ℃ of temperature, pressure 1.64MPa), makes it further cool to-38 ℃, obtain the cryogenic high pressure cold-producing medium; Provide the liquid refrigerant of cold then to become gaseous state (temperature-40.5 ℃, pressure 0.13MPa), enter air collector 18; (temperature is reduced to-41.6 ℃ to the low-temperature refrigerant that is cooled by choke valve 16 throttling decrease temperature and pressure, pressure is reduced to 0.13MPa), cold-producing medium after the throttling enters flash tank 17 and carries out adiabatic flash separation gas-liquid phase, (192kg/h, 0.13MPa) enters air collector 18 to the gas that comes out from flash tank 17 tank decks by-41.6 ℃, low temperature liquid cold-producing medium (7183kg/h at the bottom of 17 jars of the flash tanks,-41.6 ℃, 0.13MPa) enter ethylene condenser 6 cooled ethylene BOG, finish kind of refrigeration cycle one time.
The amount of the cold-producing medium R404A that liquefaction 2955kg/h ethene BOG need circulate in the above-mentioned example is 9978kg, compares original technology and has reduced 44.9%, and the seawater total amount that needs is 56620kg/h.The total power consumption of compressor is 528.4kW, has reduced 16.2% than original technology.
The liquefaction again of embodiment two liquid goods ethane BOG
(1) with ethane is the open-cycle system of cold-producing medium
(1) recovery of ethane BOG cold
The low temperature ethane BOG (2640kg/h that comes out from ethane storage tank 1, pressure is 0.11MPa, temperature is-87 ℃) reclaim its cold by ice chest 2, its cold is used to cool off the ethane liquid (2640kg/h that comes out from ethane condenser 6, pressure 0.88MPa, temperature-38 ℃), reduce the temperature that liquid ethane is advanced choke valve 7, reduce the gasification of ethane in throttling process, improve refrigerating efficiency; Obtain ethane BOG and cryogenic high pressure liquid ethane at last.
(2) two stages of compression of ethane BOG
The ethane BOG temperature of coming out from ice chest 2 in the step (1) is elevated to-48 ℃, and by two-stage compressor 3 compressions, pressure is brought up to 0.95MPa then, and temperature is elevated to 74 ℃.The power consumption of compressor 3 is 167kW, is provided with intercooler 4 between the two-stage compressor, adopts seawater as low-temperature receiver, the temperature that seawater enters intercooler 4 is 25 ℃, and pressure is 0.3MPa, and flow is 1500kg/h, after ethene BOG heat exchange, the temperature of seawater is elevated to 38 ℃.
(3) cooling of ethane BOG
Ethane BOG (pressure 0.95MPa, 74 ℃ of temperature) by behind the compressor 3 raising pressure at first enters seawater heat exchanger 5, and the usefulness seawater (4000kg/h, 25 ℃, 0.3MPa) ethane BOG is cooled to 32 ℃, ocean temperature is elevated to 38 ℃; Ethane BOG enters ethane condenser 6 then, by making ethane BOG be condensed into high-pressure liquid ethane (temperature-38 ℃, pressure 0.88MPa) with cold-producing medium R404A heat exchange.High-pressure liquid ethane enters ice chest 2 and continues cooling, and liquid ethane and the low temperature ethane BOG heat exchange that is evaporated from ethane storage tank 1 in ice chest 2 make that the temperature of liquid ethane further is reduced to-59.6 ℃, obtain the cryogenic high pressure liquid ethane.
(4) the ethane throttling into storage tank of lowering the temperature
The cryogenic high pressure liquid ethane of coming out from ice chest 2 (59.2 ℃, 0.88MPa) by choke valve 7 throttlings, make its pressure and temperature all drop to the pressure store of ethane and temperature (87 ℃, 0.11MPa).Gas phase (390kg/h after the throttling,-87 ℃, 0.11MPa) and liquid phase (2250kg/h,-87 ℃, 0.11MPa) ethane all enters ethane storage tank 1, wherein (2250kg/h ,-87 ℃, 0.11MPa) ice chest 2 that is mixed in the step (1) continues circulation liquefaction again to the BOG of gas phase ethane and 1 evaporation of ethane storage tank.
(2) with R404A be the enclosed cooling cycle system of cold-producing medium
(5) refrigerant cools ethene BOG
Low temperature liquid cold-producing medium (7141kg/h, 0.13MPa ,-41.6 ℃) in ethylene condenser 6 with ethene BOG heat exchange, cold-producing medium undergoes phase transition and becomes gaseous state (40.7 ℃ 0.13MPa), obtain refrigerant gas; Absorb the heat of ethene BOG in this process, make ethene BOG be condensed into liquid state.The refrigerant gas that comes out from ethylene condenser 6 (40.7 ℃ 0.13MPa) enter air collector 18 and mix with refrigerant gas from other equipment of step (9), as the low temperature cold-producing medium that backflows.
(6) the low temperature recovery of gaseous mixture cold of backflowing
Low temperature in the step (5) backflow cold-producing medium (9920kg/h ,-40.7 ℃, 0.13MPa) contain a large amount of colds, enter in the ice chest 8 and to reclaim its cold, make the low temperature refrigerant temperature of backflowing be elevated to 16.1 ℃, obtain gaseous refrigerant.
(7) two stages of compression of cold-producing medium
The gaseous refrigerant that comes out from ice chest 8 compresses by two-stage compressor 9, makes its pressure bring up to 1.67MPa, and temperature is elevated to 88.4 ℃, obtains high temperature and high pressure gaseous refrigerant.The power consumption of compressor 9 is 251kW, and intercooler 10 is arranged between the two-stage compressor, adopts seawater as low-temperature receiver, the temperature that seawater enters intercooler 10 is 25 ℃, and pressure is 0.3MPa, and flow is 7000kg/h, after the cold-producing medium heat exchange, the temperature of seawater is elevated to 38 ℃.
(8) cooling of cold-producing medium
High temperature and high pressure gaseous refrigerant (88.4 ℃ of temperature, pressure 1.67MPa) from compressor 9 comes out is introduced into brine cooler 11, (35000kg/h, 0.3MPa) is cooled to (32 ℃ of liquid refrigerants by 25 ℃ by seawater, 1.64MPa), ocean temperature is elevated to 38 ℃ simultaneously.Liquid refrigerant enters ice chest 8 then, with the cold-producing medium heat exchange of backflowing of the described low temperature of step (5), makes liquid refrigerant further be cooled to 0 ℃, obtains high-pressure refrigerant.
(9) latent heat of phase change of cold-producing medium cooling
The high-pressure refrigerant that from ice chest 8, comes out, be divided into two strands, one high-pressure refrigerant (flow 2588kg/h, 0 ℃ of temperature, pressure 1.64MPa) (temperature is reduced to-41.5 ℃ by choke valve 13 throttling decrease temperature and pressure, pressure is reduced to 0.13MPa), cold-producing medium after the throttling enters flash tank 14 and carries out adiabatic flash separation gas-liquid phase, (729kg/h, 0.13MPa) enters air collector 18 to the gas that comes out from flash tank 14 tank decks by-41.5 ℃, liquid refrigerant (1859kg/h at the bottom of 14 jars of the flash tanks,-41.5 ℃,, in Intermediate Heat Exchanger 15, utilize the evaporation latent heat of self to cool off another strand high-pressure refrigerant (flow 7332kg/h 0.13MPa) as low-temperature receiver, 0 ℃ of temperature, pressure 1.64MPa), makes it further cool to-38 ℃, obtain the cryogenic high pressure cold-producing medium; Provide the cold-producing medium of cold then to become gaseous state (temperature-40.5 ℃, pressure 0.13MPa), enter air collector 18.(temperature is reduced to-41.6 ℃ to the low-temperature refrigerant that is cooled by choke valve 16 throttling decrease temperature and pressure, pressure is reduced to 0.13MPa), cold-producing medium after the throttling enters flash tank 17 and carries out adiabatic flash separation gas-liquid phase, gas (the 191kg/h that comes out from flash tank 17 tank decks,-41.6 ℃, 0.13MPa) enter air collector 18, low temperature liquid cold-producing medium (7141kg/h at the bottom of 17 jars of the flash tanks,-41.6 ℃, 0.13MPa) enter the ethylene condenser 6 cooled ethylene BOG in the step (5), finish kind of refrigeration cycle one time.
The foregoing description is a preferred implementation of the present invention; but embodiments of the present invention are not restricted to the described embodiments; other any do not deviate from change, the modification done under spiritual essence of the present invention and the principle, substitutes, combination, simplify; all should be the substitute mode of equivalence, be included within protection scope of the present invention.

Claims (9)

1. the method for re-liquefaction of a shipping liquid goods ethylene/ethane boil-off gas is characterized in that comprising following operating procedure:
(1) with liquid goods is the open-cycle system of cold-producing medium
(1) recovery of ethylene/ethane boil-off gas cold
Low temperature ethylene/the ethane vaporized gas that is evaporated from liquid goods storage tank passes through ice chest A, carries out heat exchange with the high-pressure liquid ethylene/ethane, obtains ethylene/ethane boil-off gas and cryogenic high pressure liquid ethylene/ethane;
(2) two stages of compression of ethylene/ethane boil-off gas
The ethylene/ethane boil-off gas that comes out among step (1) the ice chest A is compressed by two-stage compressor A, and pressure and temperature raises; Be provided with intercooler A between the described two-stage compressor A, intercooler A adopts seawater as low-temperature receiver;
(3) cooling of ethylene/ethane boil-off gas
Will be through the ethylene/ethane boil-off gas behind step (2) the raising pressure, A cools off by seawater heat exchanger, enters the ethylene/ethane condenser then, with the heat exchange of low temperature liquid cold-producing medium, obtains the high-pressure liquid ethylene/ethane; The high-pressure liquid ethylene/ethane enters among the described ice chest A of step (1) and continues to be cooled to cryogenic high pressure liquid ethylene/ethane;
(4) the ethylene/ethane throttling into storage tank of lowering the temperature
Cryogenic high pressure liquid ethylene/ethane is carried out throttling by throttle valve A, pressure and temperature is reduced to the pressure store and the temperature of ethylene/ethane, gaseous ethene/ethane after the throttling and liquid phase ethylene/ethane enter the ethylene/ethane storage tank, and wherein the boil-off gas that is evaporated of gaseous ethene/ethane and ethylene/ethane storage tank is mixed among the ice chest A of step (1) and continues circulation liquefaction again;
(2) enclosed cold-producing medium cooling cycle system
(5) refrigerant cools ethylene/ethane boil-off gas
Low temperature liquid cold-producing medium in the step (3) derives from enclosed cold-producing medium kind of refrigeration cycle, the low temperature liquid cold-producing medium enters in step (3) the ethylene/ethane condenser and the ethylene/ethane boil-off gas heat exchange that improves behind the pressure, the low temperature liquid cold-producing medium undergoes phase transition and becomes gaseous state, obtains refrigerant gas; Refrigerant gas enters in the air collector with from the described gas of step (9) and mixes, and obtains the low temperature cold-producing medium that backflows;
(6) the low temperature recovery of cold-producing medium cold of backflowing
Low temperature in the step (5) cold-producing medium that backflows enters among the ice chest B and to reclaim its cold, and temperature raises and obtains gaseous refrigerant;
(7) two stages of compression of cold-producing medium
With the gaseous refrigerant that comes out among step (6) the ice chest B, B compresses by two-stage compressor, obtains high temperature and high pressure gaseous refrigerant; Be provided with intercooler B between the described two-stage compressor B, intercooler B adopts seawater as low-temperature receiver;
(8) cooling of cold-producing medium
Step (7) gained high temperature and high pressure gaseous refrigerant enters brine cooler B, utilizes cooled with seawater, obtains liquid refrigerant; Liquid refrigerant enters among the ice chest B, with the cold-producing medium heat exchange of backflowing of the described low temperature of step (6), makes liquid refrigerant further cool off, and obtains high-pressure refrigerant;
(9) latent heat of phase change of cold-producing medium cooling
Step (8) gained high-pressure refrigerant, be divided into two strands, one high-pressure refrigerant is by after the choke valve B throttling decrease temperature and pressure, enter flash tank A and carry out adiabatic flash, the gas that comes out from flash tank A top enters the described air collector of step (5), and the liquid refrigerant at the bottom of the flash tank A jar cools off another strand high-pressure refrigerant as low-temperature receiver in Intermediate Heat Exchanger C, obtain the cryogenic high pressure cold-producing medium, liquid refrigerant provides and becomes gaseous state behind the cold and enter the described air collector of step (5); The cryogenic high pressure cold-producing medium is by after the choke valve C throttling decrease temperature and pressure, enter flash tank B and carry out adiabatic flash, the gas that comes out from flash tank B top enters the described air collector of step (5), low temperature liquid cold-producing medium at the bottom of the flash tank B jar enters in the described ethylene/ethane condenser of step (5) and the heat exchange of ethylene/ethane boil-off gas, finishes kind of refrigeration cycle one time.
2. the method for re-liquefaction of a kind of shipping liquid goods ethylene/ethane boil-off gas according to claim 1, it is characterized in that: the temperature range of the described ethylene/ethane boil-off gas of step (1) is-40 ℃～-50 ℃, and the temperature range of cryogenic high pressure liquid ethylene/ethane is-60 ℃～-70 ℃.
3. the method for re-liquefaction of a kind of shipping liquid goods ethylene/ethane boil-off gas according to claim 1 is characterized in that: the pressure limit that the described ethylene/ethane boil-off gas of step (2) goes out compressor is 0.8MPa～2.0MPa.
4. the method for re-liquefaction of a kind of shipping liquid goods ethylene/ethane boil-off gas according to claim 1 is characterized in that: the temperature of the described low temperature liquid cold-producing medium of step (3) is-40 ℃～-42 ℃.
5. the method for re-liquefaction of a kind of shipping liquid goods ethylene/ethane boil-off gas according to claim 1 is characterized in that: the described high-pressure liquid ethylene/ethane of step (3) temperature range-36 ℃～-38 ℃.
6. the method for re-liquefaction of a kind of shipping liquid goods ethylene/ethane boil-off gas according to claim 1 is characterized in that: the described cold-producing medium of step (5) is R404A; The backflow temperature range of cold-producing medium of described low temperature is-39 ℃～-41 ℃.
7. the method for re-liquefaction of a kind of shipping liquid goods ethylene/ethane boil-off gas according to claim 1 is characterized in that: the pressure limit that the described gaseous refrigerant of step (7) goes out compressor is 1.5MPa～2.0MPa.
8. the method for re-liquefaction of a kind of shipping liquid goods ethylene/ethane boil-off gas according to claim 1 is characterized in that: the temperature range of the described liquid refrigerant of step (8) is 28 ℃～38 ℃.
9. the method for re-liquefaction of a kind of shipping liquid goods ethylene/ethane boil-off gas according to claim 1 is characterized in that: the pressure limit of described flash tank A of step (9) and flash tank B is 0.13MPa～0.14MPa.
CN2010102383109A 2010-07-27 2010-07-27 Re-liquefaction method of shipped liquid cargo of ethylene/ethane evaporation gas Pending CN101915494A (en)

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Application publication date: 20101215