CN101392980A - Re-liquefying method for shipping liquefaction ethylene/ethane vaporized gas - Google Patents
Re-liquefying method for shipping liquefaction ethylene/ethane vaporized gas Download PDFInfo
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- CN101392980A CN101392980A CNA2008102188077A CN200810218807A CN101392980A CN 101392980 A CN101392980 A CN 101392980A CN A2008102188077 A CNA2008102188077 A CN A2008102188077A CN 200810218807 A CN200810218807 A CN 200810218807A CN 101392980 A CN101392980 A CN 101392980A
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- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 title claims abstract description 129
- OTMSDBZUPAUEDD-UHFFFAOYSA-N Ethane Chemical compound CC OTMSDBZUPAUEDD-UHFFFAOYSA-N 0.000 title claims abstract description 104
- 239000005977 Ethylene Substances 0.000 title claims abstract description 86
- 238000000034 method Methods 0.000 title claims abstract description 41
- 238000001816 cooling Methods 0.000 claims abstract description 46
- 239000013535 sea water Substances 0.000 claims abstract description 42
- 239000003507 refrigerant Substances 0.000 claims abstract description 41
- 230000006835 compression Effects 0.000 claims abstract description 28
- 238000007906 compression Methods 0.000 claims abstract description 28
- 238000005057 refrigeration Methods 0.000 claims abstract description 17
- 239000007788 liquid Substances 0.000 claims description 28
- 238000007599 discharging Methods 0.000 claims description 21
- 239000012071 phase Substances 0.000 claims description 20
- 239000007791 liquid phase Substances 0.000 claims description 16
- 241000282326 Felis catus Species 0.000 claims description 14
- 238000001704 evaporation Methods 0.000 claims description 9
- 230000008020 evaporation Effects 0.000 claims description 9
- 238000011084 recovery Methods 0.000 abstract description 4
- 230000007613 environmental effect Effects 0.000 abstract description 2
- 238000003860 storage Methods 0.000 abstract description 2
- 239000007789 gas Substances 0.000 description 87
- 238000005516 engineering process Methods 0.000 description 5
- 238000009434 installation Methods 0.000 description 5
- 238000004519 manufacturing process Methods 0.000 description 5
- 239000000203 mixture Substances 0.000 description 5
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 description 4
- 230000008676 import Effects 0.000 description 4
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 4
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 2
- CBENFWSGALASAD-UHFFFAOYSA-N Ozone Chemical compound [O-][O+]=O CBENFWSGALASAD-UHFFFAOYSA-N 0.000 description 2
- 238000005336 cracking Methods 0.000 description 2
- 230000007812 deficiency Effects 0.000 description 2
- 239000003345 natural gas Substances 0.000 description 2
- 239000003208 petroleum Substances 0.000 description 2
- 239000001294 propane Substances 0.000 description 2
- 239000002994 raw material Substances 0.000 description 2
- 238000004064 recycling Methods 0.000 description 2
- VEXZGXHMUGYJMC-UHFFFAOYSA-M Chloride anion Chemical compound [Cl-] VEXZGXHMUGYJMC-UHFFFAOYSA-M 0.000 description 1
- 229910021529 ammonia Inorganic materials 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 229940125368 controlled substance Drugs 0.000 description 1
- 239000000599 controlled substance Substances 0.000 description 1
- 239000002826 coolant Substances 0.000 description 1
- 230000006837 decompression Effects 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 230000003203 everyday effect Effects 0.000 description 1
- 230000002349 favourable effect Effects 0.000 description 1
- 238000002309 gasification Methods 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 231100000252 nontoxic Toxicity 0.000 description 1
- 230000003000 nontoxic effect Effects 0.000 description 1
- 230000000630 rising effect Effects 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 230000002459 sustained effect Effects 0.000 description 1
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Classifications
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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
- F25J1/0002—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
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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
- F25J1/003—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
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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
- F25J1/003—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
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/006—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the refrigerant fluid used
- F25J1/0097—Others, e.g. F-, Cl-, HF-, HClF-, HCl-hydrocarbons etc. or mixtures thereof
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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
- F25J1/0203—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 single-component refrigerant [SCR] fluid in a closed vapor compression cycle
- F25J1/0208—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 single-component refrigerant [SCR] fluid in a closed vapor compression cycle in combination with an internal quasi-closed refrigeration loop, e.g. with deep flash recycle loop
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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
- F25J1/0262—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
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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
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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
- 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)
- Ocean & Marine Engineering (AREA)
- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Separation By Low-Temperature Treatments (AREA)
Abstract
The invention relates to a reliquefying method for shipped liquefied ethylene/ethane vapor. The method comprises the following steps of two stage compression of the ethylene/ethane vapor, successive cooling of the ethylene/ethane vapor by seawater and a refrigerant, phase-change latent heat cooling of ethylene/ethane, and re-liquefied storage of the ethylene/ethane vapor in a tank. The method utilizes phase-change latent heat of the ethylene/ethane and the refrigerant for heat exchange, supplies the cooling capacity through cycle refrigeration of the refrigerant, and re-liquefies and recovers the ethylene/ethane vapor. In the refrigeration cycle of the method, low-temperature return flow is mixed and returned to a cold box so as to cool the refrigerant, so that the method fully utilizes the cooling capacity of the return flow, and improves the recovery utilization rate of energy; and the temperature difference of seawater of the technological method before and after heat exchange accords with the environmental protection rule.
Description
Technical field
The boil-off gas (BOG) that the present invention relates to liquid petroleum chemicals is the liquefaction technology field again, and when specifically being meant a kind of shipping liquefaction ethene/ethane, processes such as transportation and unloading are because of going into the method for re-liquefaction of thermogenetic BOG.
Background technology
Ethylene industry is to weigh the scale of a national petrochemical industry and the sign of development degree, no matter developed country or developing country, all construction and the development that all can do one's utmost to promote ethylene industry with good conditionsi.Along with the sustained and rapid development of China's Petrochemical and national economy, the demand of ethene is continued to increase.China's ethene consumption figure was 2,169 ten thousand tons in 2007, and ethylene yield is 1,047 ten thousand tons, and the degree of self-sufficiency only is 48.3%; Estimate that China's ethylene production capacity in 2010 will reach 1,600 ten thousand tons, the ethylene requirements equivalent will reach 2,735 ten thousand tons, and equivalent need satisfaction rate is 58.5%, still need rely on a large amount of import ethene to satisfy the demands.
Cracking stock expense proportion is very big in the ethene cost, and cracking stock system ethene is all made with ethane in the natural gas of cheapness and propane in the area of the rich producing natural gas in the world.Middle East (as Saudi Arabia) aboundresources, local ethane price 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.And the ethylene industry of China is limited by resource, and domestic ethylene raw 90% is from the refinery, and raw material is laid particular stress on, and how based on naphtha, production cost of ethylene is up to 530 dollars/t.In order to satisfy the ethylene raw demand, the external interdependency of the oil of China in 2010 further strengthens.Select the deficiency of suitable import ethane,, alleviate the shortage of petroleum resources, have significant social and economic implications reducing domestic production cost of ethylene with the make-up ethylene raw material.
Often adopt the cryostat, ship to carry out ethene commerciality sea-freight in the world, as developed countries such as U.S. import liquid ethylene from middle-east, shipping is come back home.-104 ℃ of liquefied ethylene volumes of the inferior weight of normal pressure are about 1/490 of gas ethene under the normality, and the volume after the liquefaction dwindles greatly, and is comparatively favourable to the storing of ethene.But because the low temperature ethylene storage tank is subjected to the intrusion of external environment heat, part mechanical energy was converted into heat energy when submerged pump moved in the ethene liquid goods jar in the sea-freight process, all can make the gasification of pot liquid ethene produce flashed vapour, also was BOG (boiloff-gas) gas.The generation of boil-off gas can make the liquid goods ethylene temperature of cargo tank raise, thereby causes the rising of cargo hold pressure.Too high cargo tank pressure can destroy the structure of cargo tank, and its maintenance system is caused danger.If but let alone to enter in the air, not only dangerous, also very uneconomical economically.Therefore, consider, all need to the boil-off gas processing of liquefying again, to reclaim this part BOG from the security and the economy of boats and ships transportations.Ethane and ethene character are similar, and under the normal pressure, with the liquid ethane of ethane gas identical weight, temperature is-88 ℃, and volume then has only 1/435.The same existence and the problem of ethene sea-freight in the sea-freight of ethane, also need the ethane gas that the evaporates recycling of liquefying again.
The technology that the steam that liquid goods produces in transportation liquefies again, present document " reliquefying systems mounted on liquefied gas tankships principle and reliquefaction installation general introduction " (Dai Qian, Li Pinyou. reliquefying systems mounted on liquefied gas tankships principle and reliquefaction installation general introduction. cryogenics, 2005 (1): relevant technology report is arranged 6-9).Relevant technologies comprises: the reliquefaction installation on the multipurpose low-temperature liquid gas ship of being mentioned in " reliquefying systems mounted on liquefied gas tankships principle and reliquefaction installation general introduction ", this device is mainly used in liquefied ethylene, oil gas, ammonia, to satisfy the carrying requirement of different goods.This device adopts the direct kind of refrigeration cycle of superposition type, is that the open circulation of refrigerant and the enclosed kind of refrigeration cycle of an employing R22 cold-producing medium are in series by one with liquid goods promptly.In the cold-producing medium closed cycle of this device, refrigerant gas directly enters the refrigerant condenser cooling mix compressed machine compression with the gas that backflows of follow-up flow process after, and entirely by the cooled with seawater cold-producing medium, the heat exchange load is bigger.Cold-producing medium through cooling is divided into two strands, enters heat exchanger after the stock-traders' know-how choke valve decompression, cools off another strand cold-producing medium, and the refrigerant gas after the heat exchange is as backflowing gas.Enter condenser/evaporator cooling BOG gas through cooled another strand cold-producing medium, the refrigerant gas after the heat exchange enters the one-level compressor and constitutes circulation.
In the R22 cold-producing medium enclosed kind of refrigeration cycle in the reliquefaction installation that this article is introduced, employing R22 is a cold-producing medium, R22 has been put into one of controlled substance in the Montreal Protocol because its ozone depletion index is 0.055, chloride cold-producing mediums such as R22, R502 has been stipulated end using time in the world.This device R22 condenser in the liquefaction flow path more in addition, the cooling of cold-producing medium is basic complete in seawater, and the heat exchange load is big, has strengthened investment cost.And, make the refrigerant cools temperature also be restricted owing to be subjected to the restriction of import ocean temperature.
Summary of the invention
Purpose of the present invention is exactly in order to solve above-mentioned the deficiencies in the prior art part, and the process that the BOG of generation liquefies again is provided in a kind of liquefied ethylene/ethane shipping process.This method has utilized the phase change latent heat of ethylene/ethane and cold-producing medium to carry out heat exchange, provides cold by the cold-producing medium circularly cooling, with the ethylene/ethane BOG recovery of liquefying again.In the cold-producing medium R404A of this method kind of refrigeration cycle, low temperature backflowed be back to the agent of ice chest cooling refrigeration again after gas mixes, made full use of the cold of the gas that backflows, improved the recovery utilization rate of energy, and the temperature difference meets environmental regulations before and after the seawater to make heat exchange of this process.
Purpose of the present invention is achieved through the following technical solutions, and a kind of method of re-liquefaction of shipping liquefaction ethene/ethane vaporized gas comprises following concrete steps:
The two stages of compression of first step ethylene/ethane BOG
After the BOG gas that ethylene/ethane liquid goods jar comes out on the ship enters the one-level compressor compresses, mix, enter the split-compressor compression again, obtain HTHP ethylene/ethane gas with the low temperature gas that backflows.
The cooling of the second step ethylene/ethane BOG
HTHP ethylene/ethane gas through two stages of compression is introduced into seawater heat exchanger, by cooling off with seawater to make heat exchange, enters the ethylene/ethane condenser again, by being cooled to lower temperature with the cold-producing medium heat exchange.
The latent heat of phase change cooling of the 3rd step ethylene/ethane
The ethylene/ethane of coming out from the ethylene/ethane condenser is divided into two strands, one enters flash column and carries out adiabatic flash, the ethylene/ethane gas phase discharging of coming out from the flash column cat head is as the low temperature gas that backflows, ethylene/ethane liquid phase discharging at the bottom of the tower is then as low-temperature receiver, enter the latent heat of phase change that heat exchanger utilizes self and cool off another burst ethylene/ethane, make its further cooling, the ethylene/ethane gas after the heat exchange is also as the low temperature gas that backflows.
The 4th step ethylene/ethane BOG liquefies again goes into tank stores
Low temperature ethylene/ethane through the heat exchanger cooling, enter another flash column adiabatic flash, a stage compressor of the first step is returned in the ethylene/ethane gas phase discharging of coming out from the flash column cat head, ethylene/ethane at the bottom of the tower, be the liquid phase discharging after the BOG of liquid goods jar liquefies again, enter ethylene/ethane liquid goods tank stores.
In the first step of the method for re-liquefaction of above-mentioned shipping liquefaction ethene/ethane vaporized gas, described cold-producing medium is R404A.
In the first step of the method for re-liquefaction of above-mentioned shipping liquefaction ethene/ethane vaporized gas, described cold-producing medium is provided by kind of refrigeration cycle, and the workflow of described kind of refrigeration cycle may further comprise the steps:
The two stages of compression of first step refrigerant gas
Refrigerant gas enters seawater heat exchanger after the one-level compressor compresses, by taking away a part of heat with seawater to make heat exchange, and then enter the split-compressor compression, obtains high-temperature high-pressure refrigerant gas.Seawater under the normal pressure is by behind the pump pressure-raising, and separated into two parts provides cold for cold-producing medium.A part enters the seawater heat exchanger of one-level compressor outlet, and another part enters the seawater heat exchanger of split-compressor outlet.
The cooling of the second step cold-producing medium
Through the high-temperature high-pressure refrigerant gas of two stages of compression, be introduced into seawater heat exchanger, cooling enters ice chest again, by with the low-temperature refrigerant gas converting heat that backflows, further cooling.
The latent heat of phase change cooling of the 3rd step cold-producing medium
The cold-producing medium that comes out from ice chest, be divided into two strands, one enters flash column and carries out adiabatic flash, the cold-producing medium gas phase discharging of coming out from the flash column cat head is as the low temperature gas that backflows, cold-producing medium liquid phase discharging at the bottom of the tower is then as low-temperature receiver, utilize the evaporation latent heat of self to cool off another strand cold-producing medium, make its further cooling.Refrigerant gas after the heat exchange also as low temperature backflow gas enter ice chest for the compression after cold-producing medium cold is provided.
The cooling of backflowing of the 4th step cold-producing medium
Low-temperature refrigerant by the evaporation latent heat of liquid phase refrigerant self cooling enters another flash column adiabatic flash, and the cold-producing medium gas phase of coming out from the flash column cat head enters the cold-producing medium of ice chest after for compression cold is provided as the low temperature gas that backflows; Cold-producing medium liquid phase discharging at the bottom of the tower enters ethylene/ethane condenser cooled ethylene/ethane BOG.And the cold-producing medium that cold is provided becomes gas phase, also as the low temperature gas that backflows.
After four strands of low temperature of description backflow the gas mixing in the 3rd step and the 4th step, enter ice chest and provide cold for the cold-producing medium after compressing, the gas that backflows after the heat exchange enters a stage compressor again, constitutes enclosed cold-producing medium circulating system.
In the first step, the temperature range of a described stage compressor charging-102 ℃～-85 ℃, pressure limit 0.11MPa～0.12MPa, pressure-raising is to 0.52MPa～0.56MPa; The split-compressor pressure-raising is to 1.72MPa～1.86MPa.
In the 3rd step of the method for re-liquefaction of above-mentioned shipping liquefaction ethene/ethane vaporized gas, the pressure limit of described flash column is 0.52MPa～0.56MPa.
In the 4th step of the method for re-liquefaction of above-mentioned shipping liquefaction ethene/ethane vaporized gas, the pressure limit of described flash column is 0.11MPa～0.12MPa.
The present invention compared with prior art has following advantage and beneficial effect:
1. at ethylene/ethane BOG of the present invention again in the liquefaction system, charging all mixes with the low temperature of the follow-up flow process gas that backflows behind a stage compressor pressure-raising, to reduce the split-compressor inlet temperature, thereby improve the split-compressor compression ratio, reduce the compressor power consumption, save the operating cost of flow process.
2. the preferred R404A of cold-producing medium of the present invention.R404A is that a kind of environment-friendly type ozone depletion index is zero cold-producing medium, and nontoxic, safe, temperature glide is little, belongs to near-azeotrope refrigerant.Pressure and volume refrigerating capacity compressor and R22 have suitable comparativity.
3. in the 4th step of cold-producing medium cooling cycle system of the present invention, multiply low temperature backflowed to be entered the cold-producing medium of ice chest after for compression cold is provided after gas mixes; This operation has made full use of the air cooling amount of backflowing, and refrigerant temperature is further reduced, and has realized the recycling of low-temperature refrigerant energy; Simultaneously also save the circulating refrigerant consumption, thereby saved investment cost.
4. the present invention is according to the present situation of China's ethylene industry, by the ethylene/ethane BOG that will produce in the shipping ethylene/ethane process recovery of liquefying again, not only can improve China's ethylene raw constitutes, reduce energy consumption and production costs, simultaneously also can alleviate the shortage of China's oil resource, thereby have significant social value and economic worth.Ethylene/ethane BOG of the present invention is the reasonable energy utilization of liquefaction process again, so liquefaction efficiency is higher, circulating mass of refrigerant is less simultaneously, and good refrigeration effect, and operating cost is lower.
Description of drawings
Fig. 1 is a process chart of the present invention.
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.
That as shown in Figure 1, following specific embodiment is described is a 6400M
3The liquid ethylene of capacity/ethane cargo ship adopts the present invention to carry out the method that ethylene/ethane BOG liquefies again.According to the designing requirement that liquid goods is irritated, the BOG evaporation rate of ethylene/ethane liquid goods jar every day of this cargo ship is approximately 0.2～0.38% of liquid goods total amount, the BOG amount that produce will comprise also simultaneously that pipeline, other equipment are gone into heat, ethylene/ethane is loaded or discharging etc.; The BOG of this cargo ship liquefaction system again will possess and can handle 1, and the BOG total amount of 500kg/h is with the constant ability of liquid goods pressure tank on the ship of keeping the 6400M3 capacity; And this BOG liquefaction system temperature rise that also should possess the ethylene/ethane liquid goods in 90 hours in the liquid goods jar again can not surpass 4 ℃, promptly ethene in 90 hours liquid goods jar temperature in the ability of-102 ℃～-98 ℃ of variations.Unit of the present invention comprises sea water pump, BOG compressor and coolant compressor, heat exchanger and flash column.Concrete job step and process conditions are as follows:
Embodiment one: the liquefaction again of liquid ethylene BOG
The two stages of compression of first step ethene BOG
The 1500Kg/hr that ethene liquid goods jar is evaporated from the ship ,-102.0 ℃, the ethene BOG gas of 0.11MPa enter a stage compressor 1, are compressed to 0.52MPa, and temperature rises to-0.7 ℃ by-102 ℃.Mix from backflow gas S3 and the S5 of the ethene BOG of one-level compressor outlet and follow-up flow process, cooled to-13.1 ℃, enter split-compressor 2 compressions, pressure is elevated to 1.72MPa, and temperature is 83.9 ℃.
The cooling of the second step ethene BOG
Cooling device comprises seawater heat exchanger 3 and ethylene condenser 4; HTHP ethylene gas through two stages of compression is introduced into seawater heat exchanger 3, and with seawater to make heat exchange, temperature is reduced to 38 ℃ by 83.9 ℃, and pressure is reduced to 1.69MPa.Enter ethylene condenser 4 and cold-producing medium S12 heat exchange again, temperature drops to-38 ℃ by 38 ℃, and pressure is reduced to 1.59MPa.Seawater 5400Kg/hr under the normal pressure behind 0.50MPa, enters seawater heat exchanger 3 by the pump pressure-raising, and temperature rises to 40.3 ℃ by 32 ℃, and pressure is reduced to 0.30MPa.
The latent heat of phase change cooling of the 3rd step ethene
The ethene that comes out from ethylene condenser 4 enters current divider and is divided into two strands, wherein one S1 enters flash column 5 with 418Kg/hr and carries out adiabatic flash, from the 86Kg/hr that cat head is separated, temperature, pressure are respectively-70 ℃, and the ethylene gas of 0.52MPa is as the low temperature gas S3 that backflows.Ethene liquid phase discharging S4 is 332Kg/hr at the bottom of the tower, enters heat exchanger 6 and utilizes self evaporation latent heat that another strand of 1830Kg/hr ethene BOG S2 is cooled to-66 ℃, and pressure is reduced to 1.52MPa, and the ethylene gas after the heat exchange is also as the low temperature gas S5 that backflows.
The 4th step ethene BOG liquefies again goes into tank stores
The low temperature ethylene of the 1830Kg/hr that process heat exchanger 6 is cooled enters another flash column 7 and carries out adiabatic flash, the gas 330Kg/hr that separates from cat head, temperature, pressure are respectively-102 ℃, 0.11MPa, return the one-level suction port of compressor and mix with ethene BOG gas that ethene liquid goods jar is evaporated and be compressed.Liquid phase discharging 1500Kg/hr enters ethene liquid goods tank stores at the bottom of the tower.
In the said method, the second step cold-producing medium R404A has kind of refrigeration cycle to provide, and the step of kind of refrigeration cycle comprises:
The two stages of compression of first step refrigerant gas
7673Kg/hr, 30.3 ℃, the refrigerant gas of 0.13MPa enter a stage compressor 8, are compressed into 0.59MPa, and temperature rises to 96 ℃ by 30.3 ℃, enters seawater heat exchanger 9 and seawater to make heat exchange, and temperature is reduced to 38 ℃, and pressure is reduced to 0.56MPa.Enter split-compressor 10 then, be compressed to 1.91MPa, temperature is 95.8 ℃.Seawater 56556Kg/hr under the normal pressure, enters current divider and is divided into two strands to 0.50MPa by the pump pressure-raising, and one enters seawater heat exchanger 9, and flow is 13117Kg/hr, and temperature rises to 39.6 ℃ by 32 ℃, and pressure is reduced to 0.30MPa.Another strand enters seawater heat exchanger 11, and flow is 43439Kg/hr.
The cooling of the second step cold-producing medium
Cooling device comprises seawater heat exchanger 11 and ice chest 12.High-temperature high-pressure refrigerant gas through two stages of compression is introduced into seawater heat exchanger 11 and seawater to make heat exchange, and temperature is reduced to 38 ℃ by 95.8 ℃, and pressure is reduced to 1.88MPa.The temperature of seawater then rises to 39.6 ℃ by 32 ℃, and pressure is reduced to 0.30MPa.Cold-producing medium through cooled with seawater enters ice chest 12 again, and by the low-temperature refrigerant gas S13 heat exchange of backflowing in going on foot with the 4th, temperature is reduced to 2 ℃.
The latent heat of phase change cooling of the 3rd step cold-producing medium
The cold-producing medium that comes out from ice chest 12 enters current divider and is divided into two strands, and one S6 enters flash column 13 with 2087Kg/hr and carries out adiabatic flash.From the gas 610Kg/hr that cat head is separated, temperature, pressure are respectively-41.5 ℃, 0.13MPa, as the low temperature gas S8 that backflows.Cold-producing medium liquid phase discharging S9 is 1477Kg/hr at the bottom of the tower, enters heat exchanger 14, utilizes self evaporation latent heat that the cold-producing medium S7 of another gang 5586Kg/hr is cooled to-38 ℃, and pressure is reduced to 1.78MPa.Refrigerant gas after the heat exchange is as the low temperature gas S10 that backflows.
The cooling of backflowing of the 4th step cold-producing medium
The low-temperature refrigerant of the 5586Kg/hr that is cooled through heat exchanger 14 enters another flash column 15 and carries out adiabatic flash, and from the gas 144Kg/hr that the flash column cat head comes out, temperature, pressure are respectively-41.62 ℃, 0.13MPa, as the low temperature gas S11 that backflows.Cold-producing medium liquid phase discharging 5442Kg/hr at the bottom of the tower utilizes self evaporation latent heat that the ethene BOG of compression is cooled to-38 ℃ at heat exchanger 4 by 38 ℃, and the refrigerant gas after the heat exchange is as the low temperature gas S14 that backflows.Above-mentioned four strands of low temperature backflow and are the low-temperature refrigerant gas S13 that backflows after gas S8, S10, S11 and S14 mix, temperature, pressure are respectively-40.8 ℃, 0.13MPa enter ice chest, as the refrigerant gas after the low-temperature receiver cooled compressed, provide the refrigerant gas temperature of cold to rise to 30.3 ℃ by-40.8 ℃, enter one-level compressor compresses 8 again, constitute the cold-producing medium circulating system.
Embodiment two: the liquefaction again of liquid ethane BOG
The two stages of compression of first step ethane gas
The 1480Kg/hr that ethane liquid goods jar is evaporated from the ship ,-85.0 ℃, the ethane BOG of 0.12MPa enter a stage compressor 1, are compressed to 0.56MPa, and temperature rises to 2.8 ℃ by-85.0 ℃.Mix from backflow gas S3 and the S5 of the ethane BOG of one-level compressor outlet and follow-up flow process, cooled to-6.1 ℃, enter split-compressor 2, pressure is elevated to 1.86MPa, and temperature is 75.4 ℃.
The cooling of the second step ethane BOG
Cooling device comprises seawater heat exchanger 3 and ethane condenser 4; HTHP ethane gas through two stages of compression is introduced into seawater heat exchanger 3, and with seawater to make heat exchange, temperature is reduced to 40 ℃ by 75.4 ℃, and pressure is reduced to 1.82MPa.Enter ethane condenser 4 again, with cold-producing medium S12 heat exchange, temperature drops to-20 ℃ by 40 ℃, and pressure is reduced to 1.75MPa.Seawater 5044Kg/hr under the normal pressure behind 0.50MPa, enters seawater heat exchanger 3 by the pump pressure-raising, and temperature rises to 40 ℃ by 32 ℃, and pressure is reduced to 0.30MPa.
The latent heat of phase change cooling of the 3rd step ethane
The ethane that comes out from ethane condenser 4 enters current divider and is divided into two strands, wherein a stream gang S1 enters flash column 5 with 400Kg/hr and carries out adiabatic flash, from the 80Kg/hr that cat head is separated, temperature, pressure are respectively-49.7 ℃, and the ethane gas of 0.56MPa is as the low temperature gas S3 that backflows.Ethane liquid phase discharging S4 is 320Kg/hr at the bottom of the tower, enters heat exchanger 6 and utilizes self evaporation latent heat that another strand ethane BOG S2 of 1877Kg/hr is cooled to-45 ℃, and pressure is reduced to 1.69MPa, and the ethane gas after the heat exchange is also as the low temperature gas S5 that backflows.
The 4th step ethane BOG liquefies again goes into tank stores
The low temperature ethane of the 1877Kg/hr that process heat exchanger 6 is cooled enters another flash column 7 and carries out adiabatic flash, the gas 397Kg/hr that separates from cat head, temperature, pressure are respectively-85 ℃, 0.12MPa, return the one-level suction port of compressor and mix with ethane BOG gas that ethane liquid goods jar is evaporated and be compressed.Liquid phase discharging 1480Kg/hr enters ethane liquid goods tank stores at the bottom of the tower.
In the said method, the second step cold-producing medium R404A has kind of refrigeration cycle to provide, and the step of kind of refrigeration cycle is identical with kind of refrigeration cycle step among the embodiment one.
The above-mentioned specific embodiment is the preferred embodiments of the present invention; can not limit claim of the present invention; other any change or other equivalent substitute mode that does not deviate from technical scheme of the present invention and made is included within protection scope of the present invention.
Claims (6)
1, a kind of method of re-liquefaction of shipping liquefaction ethene/ethane vaporized gas is characterized in that may further comprise the steps:
The two stages of compression of first step ethylene/ethane boil-off gas
After the ethylene/ethane boil-off gas that ethylene/ethane liquid goods jar comes out on the ship enters the one-level compressor compresses, mix, enter the split-compressor compression again, obtain HTHP ethylene/ethane gas with the low temperature gas that backflows;
The cooling of the second step ethylene/ethane boil-off gas
HTHP ethylene/ethane gas through two stages of compression is introduced into seawater heat exchanger, by cooling off with seawater to make heat exchange, enters the ethylene/ethane condenser again, by being cooled to lower temperature with the cold-producing medium heat exchange;
The latent heat of phase change cooling of the 3rd step ethylene/ethane
The ethylene/ethane gas that comes out from the ethylene/ethane condenser is divided into two strands, one enters flash column and carries out adiabatic flash, the ethylene/ethane gas phase discharging of coming out from the flash column cat head is as the low temperature gas that backflows, ethylene/ethane liquid phase discharging at the bottom of the tower is then as low-temperature receiver, enter the latent heat of phase change that heat exchanger utilizes self and cool off another burst ethylene/ethane, make its further cooling, the ethylene/ethane gas after the heat exchange is also as the low temperature gas that backflows;
The 4th step ethylene/ethane boil-off gas liquefies again goes into tank stores
Low temperature ethylene/ethane through the heat exchanger cooling, enter another flash column adiabatic flash, a stage compressor of the first step is returned in the ethylene/ethane gas phase discharging of coming out from the flash column cat head, ethylene/ethane at the bottom of the tower is the liquid phase discharging after the boil-off gas of liquid goods jar liquefies again, enters ethylene/ethane liquid goods tank stores.
2, the method for re-liquefaction of shipping liquefaction ethene/ethane vaporized gas according to claim 1, it is characterized in that: in the described first step, the temperature range of a described stage compressor charging-102 ℃～-85 ℃, pressure limit 0.11MPa～0.12MPa, pressure-raising is to 0.52MPa～0.56MPa; Described split-compressor pressure-raising is to 1.72MPa～1.86MPa.
3, the method for re-liquefaction of shipping liquefaction ethene/ethane vaporized gas according to claim 1 is characterized in that: in described second step, described cold-producing medium is R404A.
4, the method for re-liquefaction of shipping liquefaction ethene/ethane vaporized gas according to claim 1 is characterized in that: in described second step, described cold-producing medium is provided by kind of refrigeration cycle, and described kind of refrigeration cycle is realized by following steps:
The two stages of compression of first step refrigerant gas
Refrigerant gas enters seawater heat exchanger after the one-level compressor compresses, by taking away a part of heat with seawater to make heat exchange, and then enter the split-compressor compression, obtains high-temperature high-pressure refrigerant gas; Seawater under the normal pressure is by behind the pump pressure-raising, and separated into two parts provides cold for cold-producing medium; A part enters the seawater heat exchanger of one-level compressor outlet, and another part enters the seawater heat exchanger of split-compressor outlet;
The cooling of the second step cold-producing medium
Through the high-temperature high-pressure refrigerant gas of two stages of compression, be introduced into seawater heat exchanger, cooling enters ice chest again, by with the low-temperature refrigerant gas converting heat that backflows, further cooling;
The latent heat of phase change cooling of the 3rd step cold-producing medium
The cold-producing medium that comes out from ice chest, be divided into two strands, one enters flash column and carries out adiabatic flash, the cold-producing medium gas phase discharging of coming out from the flash column cat head is as the low temperature gas that backflows, cold-producing medium liquid phase discharging at the bottom of the tower is then as low-temperature receiver, utilize the evaporation latent heat of self to cool off another strand cold-producing medium, make its further cooling; Refrigerant gas after the heat exchange also as low temperature backflow gas enter ice chest for the compression after cold-producing medium cold is provided;
The cooling of backflowing of the 4th step cold-producing medium
Low-temperature refrigerant by the evaporation latent heat of liquid phase refrigerant self cooling enters another flash column adiabatic flash, and the cold-producing medium gas phase of coming out from the flash column cat head enters the cold-producing medium of ice chest after for compression cold is provided as the low temperature gas that backflows; Cold-producing medium liquid phase discharging at the bottom of the tower enters ethylene/ethane condenser cooled ethylene/ethane vaporized gas; And the cold-producing medium that cold is provided becomes gas phase, also as the low temperature gas that backflows;
Four strands of low temperature in the 3rd step and the 4th step backflow after gas mixes, and enter ice chest and provide cold for the cold-producing medium after compressing, and the gas that backflows after the heat exchange enters a stage compressor again, constitutes enclosed cold-producing medium circulating system.
5, the method for re-liquefaction of shipping liquefaction ethene/ethane vaporized gas according to claim 4 is characterized in that: in described the 3rd step, the pressure limit of described flash column is 0.52MPa～0.56MPa.
6, the method for re-liquefaction of shipping liquefaction ethene/ethane vaporized gas according to claim 4 is characterized in that: in described the 4th step, the pressure limit of described flash column is 0.11MPa～0.12MPa.
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Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101915494A (en) * | 2010-07-27 | 2010-12-15 | 华南理工大学 | Re-liquefaction method of shipped liquid cargo of ethylene/ethane evaporation gas |
| CN103608632A (en) * | 2011-05-30 | 2014-02-26 | 瓦锡兰油气系统公司 | Utilization of LNG used for fuel to liquefy LPG boil off |
| CN104976862A (en) * | 2015-05-21 | 2015-10-14 | 潜江永安药业股份有限公司 | Low-temperature refrigeration process in ethylene storing process |
| CN105837715A (en) * | 2015-01-13 | 2016-08-10 | 青岛海晶化工集团有限公司 | Method for cooling water through utilization of cold energy of low-temperature ethylene and process unit |
| US9823014B2 (en) | 2011-04-19 | 2017-11-21 | Babcock Ip Management (Number One) Limited | Method of cooling boil off gas and an apparatus therefor |
| CN109099640A (en) * | 2018-08-21 | 2018-12-28 | 中国寰球工程有限公司 | Ethylene BOG gas comprehensive reutilization system and method |
| CN110537065A (en) * | 2017-04-20 | 2019-12-03 | 巴布科克知识产权管理（第一）有限公司 | The method and device thereof of cooling boil-off gas |
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2008
- 2008-10-31 CN CN2008102188077A patent/CN101392980B/en not_active Expired - Fee Related
Cited By (11)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101915494A (en) * | 2010-07-27 | 2010-12-15 | 华南理工大学 | Re-liquefaction method of shipped liquid cargo of ethylene/ethane evaporation gas |
| US9823014B2 (en) | 2011-04-19 | 2017-11-21 | Babcock Ip Management (Number One) Limited | Method of cooling boil off gas and an apparatus therefor |
| CN103608632A (en) * | 2011-05-30 | 2014-02-26 | 瓦锡兰油气系统公司 | Utilization of LNG used for fuel to liquefy LPG boil off |
| CN103608632B (en) * | 2011-05-30 | 2016-03-16 | 瓦锡兰油气系统公司 | Utilize the LNG being used for fuel with the system and method for the LPG boil-off gas that liquefies |
| CN105837715A (en) * | 2015-01-13 | 2016-08-10 | 青岛海晶化工集团有限公司 | Method for cooling water through utilization of cold energy of low-temperature ethylene and process unit |
| CN105837715B (en) * | 2015-01-13 | 2018-03-02 | 青岛海湾集团有限公司 | A kind of method and process unit using low temperature ethylene cold energy cooling water |
| CN104976862A (en) * | 2015-05-21 | 2015-10-14 | 潜江永安药业股份有限公司 | Low-temperature refrigeration process in ethylene storing process |
| CN104976862B (en) * | 2015-05-21 | 2017-08-25 | 潜江永安药业股份有限公司 | A kind of cryogenic refrigeration technique in ethene storage process |
| CN110537065A (en) * | 2017-04-20 | 2019-12-03 | 巴布科克知识产权管理（第一）有限公司 | The method and device thereof of cooling boil-off gas |
| CN110537065B (en) * | 2017-04-20 | 2021-10-22 | Lge知识产权管理有限公司 | Method and apparatus for cooling boil-off gas |
| CN109099640A (en) * | 2018-08-21 | 2018-12-28 | 中国寰球工程有限公司 | Ethylene BOG gas comprehensive reutilization system and method |
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