AU2021427875A1 - VOC recovery process for LNG dual-fuel vessel based on heat exchange of intermediate media - Google Patents
VOC recovery process for LNG dual-fuel vessel based on heat exchange of intermediate media Download PDFInfo
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- AU2021427875A1 AU2021427875A1 AU2021427875A AU2021427875A AU2021427875A1 AU 2021427875 A1 AU2021427875 A1 AU 2021427875A1 AU 2021427875 A AU2021427875 A AU 2021427875A AU 2021427875 A AU2021427875 A AU 2021427875A AU 2021427875 A1 AU2021427875 A1 AU 2021427875A1
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- 239000000446 fuel Substances 0.000 title claims abstract description 27
- 238000011084 recovery Methods 0.000 title claims abstract description 23
- 239000012855 volatile organic compound Substances 0.000 claims abstract description 76
- 239000007789 gas Substances 0.000 claims abstract description 69
- 239000007788 liquid Substances 0.000 claims abstract description 56
- LYCAIKOWRPUZTN-UHFFFAOYSA-N Ethylene glycol Chemical compound OCCO LYCAIKOWRPUZTN-UHFFFAOYSA-N 0.000 claims abstract description 50
- 239000003949 liquefied natural gas Substances 0.000 claims abstract description 47
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 claims abstract description 44
- 238000009833 condensation Methods 0.000 claims abstract description 41
- 230000005494 condensation Effects 0.000 claims abstract description 41
- WGCNASOHLSPBMP-UHFFFAOYSA-N hydroxyacetaldehyde Natural products OCC=O WGCNASOHLSPBMP-UHFFFAOYSA-N 0.000 claims abstract description 25
- 238000000926 separation method Methods 0.000 claims abstract description 25
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 24
- 239000001294 propane Substances 0.000 claims abstract description 22
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 claims abstract description 15
- 239000005977 Ethylene Substances 0.000 claims abstract description 15
- 238000001816 cooling Methods 0.000 claims abstract description 10
- OTMSDBZUPAUEDD-UHFFFAOYSA-N Ethane Chemical compound CC OTMSDBZUPAUEDD-UHFFFAOYSA-N 0.000 claims abstract description 9
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 10
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims description 8
- 239000011259 mixed solution Substances 0.000 claims description 8
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims description 6
- 239000003507 refrigerant Substances 0.000 claims description 6
- 229910052757 nitrogen Inorganic materials 0.000 claims description 5
- 229910002092 carbon dioxide Inorganic materials 0.000 claims description 4
- 239000001569 carbon dioxide Substances 0.000 claims description 4
- VOPWNXZWBYDODV-UHFFFAOYSA-N Chlorodifluoromethane Chemical compound FC(F)Cl VOPWNXZWBYDODV-UHFFFAOYSA-N 0.000 claims description 3
- 229910021529 ammonia Inorganic materials 0.000 claims description 3
- 239000001273 butane Substances 0.000 claims description 3
- IJDNQMDRQITEOD-UHFFFAOYSA-N n-butane Chemical compound CCCC IJDNQMDRQITEOD-UHFFFAOYSA-N 0.000 claims description 3
- OFBQJSOFQDEBGM-UHFFFAOYSA-N n-pentane Natural products CCCCC OFBQJSOFQDEBGM-UHFFFAOYSA-N 0.000 claims description 3
- 238000000034 method Methods 0.000 abstract description 12
- 230000008569 process Effects 0.000 abstract description 6
- 239000002699 waste material Substances 0.000 abstract description 5
- 230000009977 dual effect Effects 0.000 abstract description 2
- 239000010779 crude oil Substances 0.000 description 12
- 239000000203 mixture Substances 0.000 description 8
- 239000000243 solution Substances 0.000 description 7
- 239000004149 tartrazine Substances 0.000 description 5
- 239000004229 Alkannin Substances 0.000 description 4
- 230000003247 decreasing effect Effects 0.000 description 4
- 229930195733 hydrocarbon Natural products 0.000 description 4
- 150000002430 hydrocarbons Chemical class 0.000 description 4
- 239000004215 Carbon black (E152) Substances 0.000 description 3
- 239000004231 Riboflavin-5-Sodium Phosphate Substances 0.000 description 3
- 239000002151 riboflavin Substances 0.000 description 3
- 238000001179 sorption measurement Methods 0.000 description 3
- 239000000126 substance Substances 0.000 description 3
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 2
- 239000004230 Fast Yellow AB Substances 0.000 description 2
- 239000004234 Yellow 2G Substances 0.000 description 2
- 239000007864 aqueous solution Substances 0.000 description 2
- 239000002283 diesel fuel Substances 0.000 description 2
- 230000007613 environmental effect Effects 0.000 description 2
- 238000007710 freezing Methods 0.000 description 2
- 230000008014 freezing Effects 0.000 description 2
- 238000002309 gasification Methods 0.000 description 2
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- 230000009286 beneficial effect Effects 0.000 description 1
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- 238000010276 construction Methods 0.000 description 1
- 238000006477 desulfuration reaction Methods 0.000 description 1
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- 238000003912 environmental pollution Methods 0.000 description 1
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- 238000010257 thawing Methods 0.000 description 1
- 150000003568 thioethers Chemical class 0.000 description 1
Classifications
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F28—HEAT EXCHANGE IN GENERAL
- F28B—STEAM OR VAPOUR CONDENSERS
- F28B7/00—Combinations of two or more condensers, e.g. provision of reserve condenser
-
- 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
- F25D—REFRIGERATORS; COLD ROOMS; ICE-BOXES; COOLING OR FREEZING APPARATUS NOT OTHERWISE PROVIDED FOR
- F25D3/00—Devices using other cold materials; Devices using cold-storage bodies
- F25D3/10—Devices using other cold materials; Devices using cold-storage bodies using liquefied gases, e.g. liquid air
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F28—HEAT EXCHANGE IN GENERAL
- F28B—STEAM OR VAPOUR CONDENSERS
- F28B9/00—Auxiliary systems, arrangements, or devices
- F28B9/04—Auxiliary systems, arrangements, or devices for feeding, collecting, and storing cooling water or other cooling liquid
Landscapes
- Engineering & Computer Science (AREA)
- Mechanical Engineering (AREA)
- General Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Combustion & Propulsion (AREA)
- Physics & Mathematics (AREA)
- Thermal Sciences (AREA)
- Separation By Low-Temperature Treatments (AREA)
- Filling Or Discharging Of Gas Storage Vessels (AREA)
Abstract
The present invention relates to a Volatile Organic Compounds (VOC) recovery process
for a Liquefied Natural Gas (LNG) dual-fuel vessel based on heat exchange of intermediate
media, including a three-stage condensation circulating system. The intermediate media
includes, but not limited to ethane, propane, glycol and water respectively. The LNG cools
ethylene, propane, glycol and water successively. The VOC enters a third condenser first for
first-stage condensation by the cooled glycol and water, and then enters a third separator for
primary gas-liquid separation; the residual gas enters a second condenser for second-stage
condensation by the cooled propane and then enters a second separator for secondary
gas-liquid separation; the residual gas enters a first condenser for third-stage condensation by
the cooled ethane and then enters a first separator for tertiary gas-liquid separation, with
discharged gases being gases consistent with an emission standard. The present invention can
realize condensate recovery of the VOC and cold energy utilization of the LNG, which can
not only reach the emission standard, but also reduce the energy loss, and meanwhile, further
solves the problem of waste of cooling capacity generated in an LNG gasifying process in a
conventional dual power driven vessel.
Description
The present invention belongs to the field of gas treatment, and particularly relates to a Volatile Organic Compounds (VOC) recovery process for a Liquefied Natural Gas (LNG) dual-fuel vessel based on heat exchange of intermediate media.
Information of the Related Art part is merely disclosed to increase the understanding of the overall background of the present invention, but is not necessarily regarded as acknowledging or suggesting, in any form, that the information constitutes the prior art known to a person of ordinary skill in the art. Crude oil transportation vessels or oil tankers are primary marine transportation tools for crude oil. Crude oil is a mixture of various liquid hydrocarbons. Due to strong volatility, hydrocarbon components will generate a lot of VOC in crude oil storage, transportation and loading and unloading processes. The crude oil transportation vessel is provided with a plurality of crude oil cargo tanks, and crude oil stored therein will be evaporated and generate VOC in the transportation process. For the sake of safety, to maintain the pressures of the crude oil cargo tanks, VOC generated in the crude oil cargo tanks needs to be discharged to outside. However, direct emission of VOC gases not only causes a large amount of energy waste, but also leads to severe environmental pollution. Therefore, maritime organizations of various countries and International Maritime Organization put strict requirements on emission standard of VOC. At present, VOC recovery methods widely used are a condensation method and an adsorption method. The adsorption method is mainly used in a case with low heavy hydrocarbon components, which cannot be used continuously (for example, it is non-renewable after activated carbon adsorption) and is relatively narrow in usable range. In comparison, the condensation method is high in adaptability. However, its purification degree is limited by condensation temperature. The recovery rate of VOC can reach the national emission standard provided that the condensation temperature reaches about -110°C. Furthermore, components of VOC gases will vary according to places of production of crude oil. The requirements on refrigerating capacities of corresponding refrigerating systems will change, too. Therefore, the refrigerating system is required to have a certain refrigerating capacity adjusting ability. Moreover, since there have been increasingly strict environmental requirements in recent years, and the emission standard of vessel sulfides is increasingly high, the discharged tail gases can only reach corresponding requirements by adding expensive and bulky desulfurization and denitrification devices. Use of LNG as a fuel is a quite good solution, which can make VOC emission of vessels reach the standard substantially. However, a pure LNG fuel vessel is high in cost, and thus an LNG dual-fuel vessel becomes a better choice, which is a development tendency of vessels. At present, there are real vessels of dual-fuel (LNG and diesel oil) power driven vessels, and meanwhile, the order quantity of such vessels of shipyards is increased year by year. Nonetheless, there are many problems in current VOC condensation recovery systems. Heat exchangers used in conventional VOC condensation systems are common shell-and-tube heat exchangers which are low in heat exchange efficiency and large in size. The major problem is that as VOC is complicated in component and contains water, when VOC is condensed by using a single heat exchanger, there is inevitably a phenomenon that water is frozen at a low temperature and components with high condensation points are condensed to solids when VOC is not condensed completely. The former will cause ice blockage and the latter will be attached to a wall of the heat exchanger. Both of them will reduce the heat exchange efficiency greatly, and make the heat exchanger not work normally. A previous solution is to set two condensation systems working alternately. When one of the systems operates normally, the other one performs defrosting to guarantee that there is always one condensation system working normally. However, this not only increases construction investment cost and operating cost, but also occupies more area on vessel, with economic inefficiency. Besides, when serving as a fuel for vessel, the LNG needs to be gasified. And in the gasifying process, a lot of cooling capacity is often not utilized, which leads to huge resource waste.
Aiming at VOC volatile gases generated by a dual-fuel (LNG and diesel oil) power driven vessel, particularly a large oil tanker in a crude oil storage and transportation process, the objective of the present invention is to provide a VOC condensation liquefying system and method for a vessel, which reliquefies VOC by using the cooling capacity of LNG gasification and uses the VOC as a fuel.
The present invention can realize condensate recovery of the VOC and cold energy utilization of the LNG, which can not only reach the emission standard, but also reduce the energy loss, and meanwhile, further solves the problem of waste of cooling capacity generated in an LNG gasifying process in a conventional dual power driven vessel. In order to realize the above technical objectives, the present invention adopts the technical solution as follows: A first aspect of the present invention provides a VOC recovery process for an LNG dual-fuel vessel based on heat exchange of intermediate media. The system is a three-stage condensation circulating system, including a first condenser, a first separator, a first heat exchanger, a second condenser, a second separator, a second heat exchanger, a third condenser, a third separator and a third heat exchange, where a gas inlet of the first heat exchanger is connected to an LNG gas pipeline, and a gas outlet of the first heat exchanger is connected to a gas inlet of the second heat exchanger; a gas outlet of the second heat exchanger is connected to a gas inlet of the third heat exchanger; the VOC pipeline is connected to a gas inlet of the third condenser, a gas outlet of the third condenser is connected to a gas inlet of the third separator, a gas outlet of the third separator is connected to a gas inlet of the second condenser, a gas outlet of the second condenser is connected to a gas inlet of the second separator, a gas outlet of the second separator is connected to a gas inlet of the first condenser, and a gas outlet of the first condenser is connected to a gas inlet of the first separator; and a liquid inlet of the first condenser is connected to a liquid outlet of the first heat exchanger, a liquid inlet of the second condenser is connected to a liquid outlet of the second heat exchanger, and a liquid inlet of the third condenser is connected to a liquid outlet of the third heat exchanger. The present invention researches and develops a VOC condensation recovery system suitable for an LNG dual-fuel vessel, which can condense VOC fully stage by stage so as to avoid the phenomena such as ice blockage, and can utilize a large amount of cooling capacity generated during LNG gasification as well, thereby not only saving resources, but also lowering the investment cost greatly. A second aspect of the present invention provides a VOC recovery process for an LNG dual-fuel vessel based on heat exchange of intermediate media, including: cooling ethylene, propane and a mixed solution of glycol and water successively by LNG to obtain cooled ethylene, propane and mixed solution of glycol and water; contacting the VOC with the cooled mixed solution of glycol and water first for first-stage condensation, and then performing primary gas-liquid separation to obtain the VOC after the primary gas-liquid separation; contacting the VOC after the primary gas-liquid separation with the cooled propane first for second-stage condensation, and then performing secondary gas-liquid separation to obtain the VOC after the secondary gas-liquid separation; contacting the VOC after the secondary gas-liquid separation with the cooled ethylene first for third-stage condensation, and then performing tertiary gas-liquid separation to obtain the VOC. A third aspect of the present invention provides application of any one of the above-mentioned systems in the field of gas treatment. The present invention has the following beneficial effects: (1) The present invention can recover and liquefy VOC evaporated in a petroleum cargo hold during operation for a dual-fuel generator on a vessel. Volatile organic compounds and liquefied natural gas are combined and used as a fuel, which can not only achieve a remarkable environmental benefit of reducing emission of carbon dioxide greatly, but also reduce the loss of crude oil and waste of cooling capacity of LNG greatly. (2) This application features simple operating method, low cost and universality, and is apt to scale production.
The accompanying drawings constituting a part of the present invention are used to provide a further understanding of the present invention. The exemplary embodiments of the present invention and descriptions thereof are used to explain the present invention, and do not constitute an improper limitation of the present invention. FIG. 1 is a schematic structural diagram of a system of this application. In the drawing, E101-first heat exchanger; E102-second heat exchanger; E103-third heat exchanger; E104-first condenser; E105-second condenser; E106-third condenser; E107-preheater; V101-first separator; V102-second separator; V103-third separator; MIXI00-mixer; P100-pump; QI00-electric energy; Q101-cooling capacity.
It should be noted that, the following detailed descriptions are all exemplary, and are intended to provide further descriptions of the present invention. Unless otherwise specified, all technical and scientific terms used herein have the same meanings as those usually understood by a person of ordinary skill in the art to which the present invention belongs. A VOC recovery process for an LNG dual-fuel vessel based on heat exchange of intermediate media includes a three-stage condensation circulating system with an intermediate medium including, but not limited to, ethylene, propane, glycol and water, ethane, butane, ammonia, a refrigerant R22, a refrigerant R410, a refrigerant R44 and carbon dioxide for three-stage condensation of VOC. There are three heat exchangers, three condensers and three separators totally. LNG enters a first heat exchanger to cool ethane, then enters a second heat exchanger to cool propane, finally enters a third heat exchanger to cool glycol and water and is then discharged in a form of gas. The VOC enters a third condenser first for first-stage condensation by the cooled glycol and water, and then enters a third separator for primary gas-liquid separation; the residual gas enters a second condenser for second-stage condensation by the cooled propane and then enters a second separator for secondary gas-liquid separation; the residual gas enters a first condenser for third-stage condensation by the cooled ethane and then enters a first separator for tertiary gas-liquid separation, with discharged gases being gases consistent with an emission standard. In some embodiments, the temperatures of the heat exchangers are decreased progressively, and are usually divided into three stages. A high-temperature heat exchanger is intended to remove water so as to prevent freezing, and the temperature is usually greater than 0°C; the temperature of an intermediate temperate heat exchanger usually ranges from -30°C to -60°C according to composition of VOC; and the temperature of a low-temperature heat exchanger ranges from -80°C to -120°C. If there are no low-boiling-point composition in VOC, the low-temperature heat exchanger can be omitted. In some embodiments, the first heat exchanger, the second heat exchanger and the third heat exchanger are respectively filled with different intermediate media, a condensation point of the intermediate medium in the first heat exchanger is lower than that of the intermediate medium in the second heat exchanger, and the condensation point of the intermediate medium in the second heat exchanger is lower than that of the intermediate medium in the third heat exchanger. In some embodiments, the intermediate media include ethylene, propane, glycol and water. Preferably, in the mixed solution of glycol and water, a volume fraction of glycol is -60%. In some embodiments, a liquid outlet of the first condenser is connected to a liquid inlet ofthe firstheat exchanger. In some embodiments, a liquid outlet of the second condenser is connected to a liquid inlet of the second heat exchanger. In some embodiments, a liquid outlet of the third condenser is connected to a liquid inlet of the third heat exchanger. In some embodiments, a gas mixer and a preheater are further arranged between the VOC pipeline and the gas inlet of the third condenser. In some embodiments, an inlet end of the gas mixer is connected to a nitrogen pipeline and a VOC pipeline respectively. The present invention is further described in detail below with reference to specific embodiments. It should be noted that the specific embodiments are intended to explain rather than limit the present invention. Embodiment 1: LNG: LNG is first subjected to primary heat exchange with ethylene at -90°C, changing the temperature to -93.56°C from -162°C, then subjected to secondary heat exchange with propane at -30°C, changing the temperature to -55.75°C, and finally, exchanged heat with a glycol aqueous solution at 5°C, changing the temperature to 2.817°C. VOC: VOC at 50°C is mixed with nitrogen at 50°C, changing the temperature of the mixture to 13.15°C, then the mixture is heated to 50°C, the heated substance is precooled first, with a cold source from a glycol solution (0°C) passing through a cold end of a heat exchanger, decreasing the temperature to 5°C after precooling, and then gas-liquid separation is performed to remove high condensation point substances therein such as aqueous vapor, the separated gas 1 is condensed, with a cold source from propane (-40°C) passing through the cold end of the heat exchanger, decreasing the temperature of the gas after condensation to -40°C, the gas is then separated to remove hydrocarbon substances therein, the separated gas 2 is then exchanged heat with -100°C ethylene, changing the temperature after heat exchanging to -80°C, and finally, gas-liquid separation is performed. Intermediate media: the intermediate media exchange heat mainly by an intermediate medium heat exchanger, the upper side of which is a cold end and a lower side of which is a hot end. Ethylene at -90°C first exchanges heat with LNG at -162°C at the cold end, changing the temperature to -100°C, and then exchanges heat with the gas 2 at -40°C at the hot end, changing the temperature to -90°C, and this cycle is repeated. Propane at -30°C first exchanges heat with LNG (-93.56°C) heated once, changing the temperature after heat exchange to -40°C, and then exchanges heat with the gas 1 at 5°C, changing the temperature after heat exchange to -30°C, and this cycle is repeated. The glycol aqueous solution at 5°C first exchanges heat with LNG (-55.75°C) heated twice, changing the temperature after heat exchange to 0°C, and then exchanges heat with the mixture of nitrogen heated to 50°C and VOC, changing the temperature after heat exchange to 5°C, then the solution is transported to the cold end of the heat exchanger by a pump, and this cycle is repeated. Embodiment 2 A VOC recovery process for an LNG dual-fuel vessel based on heat exchange of intermediate media includes a three-stage condensation circulating system. The intermediate media includes, but not limited to, ethylene, propane, glycol and water, ethane, propane, butane, ammonia, a refrigerant R22, a refrigerant R410, a refrigerant R44 and carbon dioxide for three-stage condensation of VOC. There are three heat exchangers, three condensers and three separators totally. LNG enters a first heat exchanger E1O to cool ethane, then enters a second heat exchanger E102 to cool propane, and finally enters a third heat exchanger E103 to cool glycol and water and is discharged in a form of gas. The VOC enters a third condenser E106 first for first-stage condensation by the cooled glycol and water, and then enters a third separator V103 for primary gas-liquid separation; the residual gas enters a second condenser E105 for second-stage condensation by the cooled propane and then enters a second separator V102 for secondary gas-liquid separation; the residual gas enters a first condenser E104 for third-stage condensation by the cooled ethane and then enters a first separator ViO for tertiary gas-liquid separation, with discharged gases being gases consistent with an emission standard. In some implementations, the temperatures of the heat exchangers are decreased progressively, and are usually divided into three stages. A high-temperature heat exchanger is intended to remove water so as to prevent freezing, and the temperature is usually greater than 0°C; the temperature of an intermediate temperate heat exchanger usually ranges from °C below zero to 60°C below zero according to composition of VOC; and the temperature of a low-temperature heat exchanger ranges from 80°C below zero to 120°C below zero. If there are no low-boiling-point compositions in VOC, the low-temperature heat exchanger can be omitted. In some implementations, the first heat exchanger E101, the second heat exchanger E102 and the third heat exchanger E103 are respectively filled with different intermediate media, a condensation point of the intermediate medium in the first heat exchanger E101 is lower than that of the intermediate medium in the second heat exchanger E102, and the condensation point of the intermediate medium in the second heat exchanger E102 is lower than that of the intermediate medium in the third heat exchanger E103. In some implementations, the intermediate media include ethylene, propane, glycol and water. Preferably, in the mixed solution of glycol and water, a volume fraction of glycol is -60%. In some implementations, a liquid outlet of the first condenser E104 is connected to a liquid inlet of the first heat exchanger E101. In some implementations, a liquid outlet of the second condenser E105 is connected to a liquid inlet of the second heat exchanger E102. In some implementations, a liquid outlet of the third condenser E106 is connected to a liquid inlet of the third heat exchanger E103. In some implementations, a gas mixer MIX100 and a preheater E107 are further arranged between the VOC pipeline and the gas inlet of the third condenser E106. In some embodiments, an inlet end of the gas mixer MIX100 is connected to a nitrogen pipeline and a VOC pipeline respectively. In some embodiments, Q100 and QIO are energy flows. For example, a pump P100 needs to power consumption Q101, and the preheater E107 needs cooling capacity Q100. It should be finally noted that the foregoing descriptions are merely preferred embodiments of the present invention, but are not intended to limit the present invention. Although the present invention has been described in detail with reference to the foregoing embodiments, for a person of ordinary skill in the art, modifications can be made to the technical solutions described in the foregoing embodiments, or equivalent replacements can be made to some technical features in the technical solutions. Any modification, equivalent replacement, or improvement made within the spirit and principle of the present invention shall fall within the protection scope of the present invention.
Claims (10)
1. A Volatile Organic Compounds (VOC) recovery system for a Liquefied Natural Gas (LNG) dual-fuel vessel based on heat exchange of intermediate media, the system being a three-stage condensation circulating system, comprising a first condenser, a first separator, a first heat exchanger, a second condenser, a second separator, a second heat exchanger, a third condenser, a third separator and a third heat exchange, wherein a gas inlet of the first heat exchanger is connected to an LNG gas pipeline, and a gas outlet of the first heat exchanger is connected to a gas inlet of the second heat exchanger; a gas outlet of the second heat exchanger is connected to a gas inlet of the third heat exchanger; the VOC pipeline is connected to a gas inlet of the third condenser, a gas outlet of the third condenser is connected to a gas inlet of the third separator, a gas outlet of the third separator is connected to a gas inlet of the second condenser, a gas outlet of the second condenser is connected to a gas inlet of the second separator, a gas outlet of the second separator is connected to a gas inlet of the first condenser, and a gas outlet of the first condenser is connected to a gas inlet of the first separator; and a liquid inlet of the first condenser is connected to a liquid outlet of the first heat exchanger, a liquid inlet of the second condenser is connected to a liquid outlet of the second heat exchanger, and a liquid inlet of the third condenser is connected to a liquid outlet of the third heat exchanger.
2. The VOC recovery system for an LNG dual-fuel vessel based on heat exchange of intermediate media according to claim 1, wherein the first heat exchanger, the second heat exchanger and the third heat exchanger are respectively filled with different intermediate media, a condensation point of the intermediate medium in the first heat exchanger is lower than that of the intermediate medium in the second heat exchanger, and the condensation point of the intermediate medium in the second heat exchanger is lower than that of the intermediate medium in the third heat exchanger.
3. The VOC recovery system for an LNG dual-fuel vessel based on heat exchange of intermediate media according to claim 1, wherein the intermediate media comprise ethylene, propane, glycol and water, ethane, butane, ammonia, a refrigerant R22, a refrigerant R410, a refrigerant R44 and carbon dioxide.
4. The VOC recovery system for an LNG dual-fuel vessel based on heat exchange of intermediate media according to claim 1, wherein a liquid outlet of the first condenser is connected to a liquid inlet of the first heat exchanger; or the temperature of the intermediate medium in the first heat exchanger ranges from -80°C to -120°C.
5. The VOC recovery system for an LNG dual-fuel vessel based on heat exchange of intermediate media according to claim 1, wherein a liquid outlet of the second condenser is connected to a liquid inlet of the second heat exchanger.
6. The VOC recovery process for an LNG dual-fuel vessel based on heat exchange of intermediate media according to claim 1, wherein a liquid outlet of the third condenser is connected to a liquid inlet of the third heat exchanger; the temperature of the intermediate medium in the third heat exchanger is higher than °C.
7. The VOC recovery system for an LNG dual-fuel vessel based on heat exchange of intermediate media according to claim 1, wherein a gas mixer and a preheater are further arranged between the VOC pipeline and the gas inlet of the third condenser.
8. The VOC recovery system for an LNG dual-fuel vessel based on heat exchange of intermediate media according to claim 1, wherein a gas inlet of the gas mixer is connected to a nitrogen pipeline and a VOC pipeline respectively; or there are no first condenser, first separator and first heat exchanger.
9. A VOC (Volatile Organic Compounds) recovery process for an LNG (Liquefied Natural Gas) dual-fuel vessel based on heat exchange of intermediate media, comprising: cooling ethylene, propane and a mixed solution of glycol and water successively by LNG to obtain cooled ethylene, propane and mixed solution of glycol and water; contacting the VOC with the cooled mixed solution of glycol and water first for first-stage condensation, and then performing primary gas-liquid separation to obtain the VOC after the primary gas-liquid separation; contacting the VOC after the primary gas-liquid separation with the cooled propane first for second-stage condensation, and then performing secondary gas-liquid separation to obtain the VOC after the secondary gas-liquid separation; contacting the VOC after the secondary gas-liquid separation with the cooled ethylene first for third-stage condensation, and then performing tertiary gas-liquid separation to obtain the VOC.
10. Application of the system according to any one of claims 1-8 in the field of gas treatment.
Applications Claiming Priority (3)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2021109897173 | 2021-08-26 | ||
| CN202110989717.3A CN113654373A (en) | 2021-08-26 | 2021-08-26 | LNG dual-fuel ship VOC recovery system and process based on intermediate medium heat exchange |
| PCT/CN2021/133647 WO2023024301A1 (en) | 2021-08-26 | 2021-11-26 | Lng dual-fuel ship voc recycling system and process based on intermediate medium heat exchange |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| AU2021427875A1 true AU2021427875A1 (en) | 2023-03-16 |
| AU2021427875B2 AU2021427875B2 (en) | 2023-11-09 |
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| AU2021427875A Active AU2021427875B2 (en) | 2021-08-26 | 2021-11-26 | VOC recovery process for LNG dual-fuel vessel based on heat exchange of intermediate media |
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| CN113654373A (en) * | 2021-08-26 | 2021-11-16 | 中国石油大学(华东) | LNG dual-fuel ship VOC recovery system and process based on intermediate medium heat exchange |
| CN115265095A (en) * | 2022-08-01 | 2022-11-01 | 中国石油大学(华东) | System and process for decarbonizing tail gas by using LNG cold energy based on LNG power ship |
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| KR20160086254A (en) * | 2015-01-09 | 2016-07-19 | 삼성중공업 주식회사 | Fuel gas supplying system in ships |
| WO2016111500A1 (en) * | 2015-01-09 | 2016-07-14 | 삼성중공업 주식회사 | System for supplying fuel gas in ship |
| CN205330749U (en) * | 2016-01-25 | 2016-06-22 | 辽宁石油化工大学 | LNG cold energy cascade utilization device |
| US20190112008A1 (en) * | 2016-03-31 | 2019-04-18 | Daewoo Shipbuilding & Marine Engineering Co., Ltd. | Boil-off gas re-liquefying device and method for ship |
| NL1042097B1 (en) * | 2016-10-11 | 2018-04-18 | Van Der Bogt Perry | Energy saving method for electrical (green) power supply with the EmNa power technology's. |
| NO20171222A1 (en) * | 2017-07-21 | 2019-01-22 | Waertsilae Gas Solutions Norway As | Low emission SVOC fueled oil tanker |
| CN109268095B (en) * | 2018-08-15 | 2021-09-07 | 江苏科技大学 | LNG fuel cold energy comprehensive utilization method and system for dual-fuel power ship |
| KR20210012795A (en) * | 2019-07-26 | 2021-02-03 | 대우조선해양 주식회사 | Crude Oil Eco-Carrier and Noncombustible Treatment Method for Crude Oil Cargo Tank of the Crude Oil Eco-Carrier |
| CN111141107B (en) * | 2020-01-03 | 2021-04-06 | 江苏科技大学 | Marine VOC (volatile organic compound) and BOG (boil off gas) comprehensive liquefaction system and method |
| CN113018891B (en) * | 2021-05-24 | 2021-10-15 | 潍坊石大昌盛能源科技有限公司 | Method for carrying out step-by-step condensation on oil gas recovery by utilizing LNG cold energy |
| CN113654373A (en) * | 2021-08-26 | 2021-11-16 | 中国石油大学(华东) | LNG dual-fuel ship VOC recovery system and process based on intermediate medium heat exchange |
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| WO2023024301A1 (en) | 2023-03-02 |
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