WO2016027098A1 - Method of cooling boil off gas and an apparatus therefor - Google Patents
Method of cooling boil off gas and an apparatus therefor Download PDFInfo
- Publication number
- WO2016027098A1 WO2016027098A1 PCT/GB2015/052429 GB2015052429W WO2016027098A1 WO 2016027098 A1 WO2016027098 A1 WO 2016027098A1 GB 2015052429 W GB2015052429 W GB 2015052429W WO 2016027098 A1 WO2016027098 A1 WO 2016027098A1
- Authority
- WO
- WIPO (PCT)
- Prior art keywords
- stream
- cooled
- compressed bog
- bog
- coolant
- Prior art date
Links
- 238000000034 method Methods 0.000 title claims abstract description 102
- 238000001816 cooling Methods 0.000 title claims abstract description 92
- 239000002826 coolant Substances 0.000 claims abstract description 114
- 238000007906 compression Methods 0.000 claims abstract description 98
- 230000006835 compression Effects 0.000 claims abstract description 98
- OTMSDBZUPAUEDD-UHFFFAOYSA-N Ethane Chemical compound CC OTMSDBZUPAUEDD-UHFFFAOYSA-N 0.000 claims abstract description 78
- 238000007667 floating Methods 0.000 claims abstract description 28
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims description 70
- 239000003507 refrigerant Substances 0.000 claims description 62
- 230000008569 process Effects 0.000 claims description 22
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 claims description 20
- 239000013535 sea water Substances 0.000 claims description 12
- 238000004088 simulation Methods 0.000 claims description 12
- 239000007788 liquid Substances 0.000 claims description 11
- 239000001294 propane Substances 0.000 claims description 10
- QQONPFPTGQHPMA-UHFFFAOYSA-N propylene Natural products CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 claims description 5
- 125000004805 propylene group Chemical group [H]C([H])([H])C([H])([*:1])C([H])([H])[*:2] 0.000 claims description 5
- 239000003570 air Substances 0.000 claims description 4
- 239000012080 ambient air Substances 0.000 claims description 3
- 239000007789 gas Substances 0.000 description 50
- 238000009835 boiling Methods 0.000 description 14
- 239000000203 mixture Substances 0.000 description 11
- IJGRMHOSHXDMSA-UHFFFAOYSA-N nitrogen Substances N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 9
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- 238000013461 design Methods 0.000 description 6
- 229930195733 hydrocarbon Natural products 0.000 description 6
- 150000002430 hydrocarbons Chemical class 0.000 description 6
- 239000012071 phase Substances 0.000 description 6
- 229940112112 capex Drugs 0.000 description 5
- FEBLZLNTKCEFIT-VSXGLTOVSA-N fluocinolone acetonide Chemical compound C1([C@@H](F)C2)=CC(=O)C=C[C@]1(C)[C@]1(F)[C@@H]2[C@@H]2C[C@H]3OC(C)(C)O[C@@]3(C(=O)CO)[C@@]2(C)C[C@@H]1O FEBLZLNTKCEFIT-VSXGLTOVSA-N 0.000 description 5
- 229910052757 nitrogen Inorganic materials 0.000 description 5
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 4
- 238000010586 diagram Methods 0.000 description 4
- RWRIWBAIICGTTQ-UHFFFAOYSA-N difluoromethane Chemical compound FCF RWRIWBAIICGTTQ-UHFFFAOYSA-N 0.000 description 4
- MWRWFPQBGSZWNV-UHFFFAOYSA-N Dinitrosopentamethylenetetramine Chemical compound C1N2CN(N=O)CN1CN(N=O)C2 MWRWFPQBGSZWNV-UHFFFAOYSA-N 0.000 description 3
- 238000004519 manufacturing process Methods 0.000 description 3
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- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 3
- 239000004215 Carbon black (E152) Substances 0.000 description 2
- -1 LPG) or similar Chemical compound 0.000 description 2
- 230000009471 action Effects 0.000 description 2
- 229910021529 ammonia Inorganic materials 0.000 description 2
- 230000008859 change Effects 0.000 description 2
- 238000010276 construction Methods 0.000 description 2
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- 230000015572 biosynthetic process Effects 0.000 description 1
- 239000000969 carrier Substances 0.000 description 1
- 150000001875 compounds Chemical class 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 239000010779 crude oil Substances 0.000 description 1
- 230000003247 decreasing effect Effects 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000001704 evaporation Methods 0.000 description 1
- 230000008020 evaporation Effects 0.000 description 1
- 239000007792 gaseous phase Substances 0.000 description 1
- 239000005431 greenhouse gas Substances 0.000 description 1
- 238000009413 insulation Methods 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 239000003345 natural gas Substances 0.000 description 1
- QJGQUHMNIGDVPM-UHFFFAOYSA-N nitrogen group Chemical group [N] QJGQUHMNIGDVPM-UHFFFAOYSA-N 0.000 description 1
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- 238000005057 refrigeration Methods 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 238000012358 sourcing Methods 0.000 description 1
- 238000009834 vaporization Methods 0.000 description 1
- 230000008016 vaporization Effects 0.000 description 1
Classifications
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- F25J1/0002—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the fluid to be liquefied
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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
- F25J2235/00—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams
- F25J2235/60—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams the fluid being (a mixture of) hydrocarbons
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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
- F25J2270/00—Refrigeration techniques used
- F25J2270/90—External refrigeration, e.g. conventional closed-loop mechanical refrigeration unit using Freon or NH3, unspecified external refrigeration
Definitions
- the present invention relates to a method for the cooling, particularly the re-liquefaction, of a boil off gas (BOG) from a liquefied ethane cargo on a floating transportation vessel, and an apparatus therefor.
- a boil off gas BOG
- Floating transportation vessels such as liquefied gas carriers and barges, are capable of transporting a variety of cargoes in the liquefied state.
- a liquefied cargo is wholly or substantially ethane, generally being >90% ethane, or > 95%, or >96%, or >97% or >98% or > 99% ethane.
- Ethane is a useful product source for various industrial processes.
- Ethane can be extracted from natural gas production, fracking, or produced in the refining of crude oil.
- ethane may be associated with a plurality of other components, in particular methane. It is often desirable to liquefy ethane in a liquefaction facility at or near its source, as it can be stored and transported over long distances (generally in excess of normal pipeline distances) more readily as a liquid than in gaseous form because it occupies a smaller volume and may not need to be stored at high pressures.
- the long distance transportation of a liquefied ethane cargo having a boiling point of about -87 °C when measured at 1 atmosphere may be carried out in a suitable liquefied gas carrier, such as an ocean-going tanker having one or more storage tanks to hold the liquefied ethane cargo.
- a suitable liquefied gas carrier such as an ocean-going tanker having one or more storage tanks to hold the liquefied ethane cargo.
- These storage tanks may be insulated and/or pressurized tanks.
- gas may be produced due to the evaporation of the cargo. This evaporated cargo gas is known as boil off gas (BOG).
- a system may be provided on the carrier to re-liquefy the BOG so that it can be returned to the storage tank in a condensed state.
- This can be achieved by the compression and cooling of the BOG against a cold source.
- Ethane has a critical temperature of 32.18 °C at a pressure of 47.7 barg, such that seawater at a similar temperature would be unsuitable as the primary cold source.
- the compressed BOG is cooled and condensed against a secondary refrigerant.
- liquefied cargoes can be defined as 'pure'
- liquefied ethane to be transported as a cargo in a floating transportation vessel can, and increasingly may, comprise concentrations of other components beyond a de minimus level. This is at least partly due to the increasing sourcing of 'non- pure' ethane from new sources or new industrial processes.
- propane has a boiling point of about -40°C when measured at 1 atmosphere, the method and apparatus required to re-liquefy an ethane/propane BOG will inherently achieve re-liquefying of any propane portion of the BOG.
- One other possible component is nitrogen. As its boiling point is about - 196°C when measured at 1 atmosphere, it is commonly not practical to attempt to re-liquefy any nitrogen in the BOG on a floating transportation vessel. Thus, nitrogen is generally considered to be at least the major component of those parts of the BOG defined as "in-condensable", i.e. it can never (practically) be condensed on a floating transportation vessel. However, nitrogen is a relatively 'safe' gas.
- methane The major other possible component of concern in liquefied ethane cargoes is methane.
- Methane has a boiling point of about -162°C to -163°C when measured at 1 atmosphere. This boiling point is very significantly below the boiling point of ethane when measured at 1 atmosphere.
- methane has hitherto typically been considered as a "non-condensable" component of liquefied cargoes, i.e. it can possibly be condensed (i.e. re-liquefied), but particularly special methods are required which may not be CAPEX and/or OPEX justifiable on a floating transportation vessel.
- methane is considered to be one of the 'greenhouse gasses', such that it is increasingly preferred not to vent it to atmosphere.
- WO2012/143699A relates to a method and apparatus for re-liquefying a BOG stream from a liquefied cargo in a floating transportation vessel, said liquefied cargo having a boiling point of greater than -1 10°C at 1 atmosphere, wherein a cooled vent stream which may comprise non- condensed BOG components is heat exchanged with a portion of the compressed, cooled and then expanded BOG stream.
- This is particularly suitable for liquefied cargos having boiling points of greater than -1 10°C when measured at 1 atmosphere, but a need exists to provide an improved method of cooling, particularly re-liquefying as far as possible under reasonable OPEX and CAPEX, boil off gas from a liquefied ethane cargo, especially such cargoes comprising an increasing proportion of lighter components such as methane.
- the present invention addresses these problems by triple cooling and using a compressed BOG stream.
- the triple cooled stream condense previously non-condensed components, may be re-liquefied and subsequently returned to the liquefied ethane cargo tank in the liquid phase.
- the triple cooled compressed BOG stream provides a source of increased cooling duty compared to heat exchange media such as seawater, allowing the re-liquefaction of lighter components in the BOG stream.
- the method and apparatus disclosed herein allows liquefied ethane cargoes to be transported having an increased content of lighter components such as methane, without the need to add additional stages of compression or increase the venting of previously considered non-condensable
- the method and apparatus described herein allow the extension of a compression system having a given number of stages of compression to cargoes having components which could not normally be re-liquefied or condensed.
- the present invention provides a method of cooling a boil off gas stream from a liquefied ethane cargo in a floating transportation vessel, said method comprising at least the steps of: compressing a boil off gas stream from said liquefied ethane cargo in two or more stages of compression comprising at least a first stage and a final stage to provide a compressed BOG discharge stream, wherein said first stage of compression has a first stage discharge pressure and said final stage of compression has a final stage suction pressure and one or more intermediate, optionally cooled, compressed BOG streams are provided between consecutive stages of compression; cooling the compressed BOG discharge stream against one or more first coolant streams to provide a first cooled compressed BOG stream;
- the first expanded cooled BOG stream is used as the third coolant stream in a heat exchange/exchanger against the second cooled compressed BOG stream, which heat exchange/exchanger provides a third cooled compressed BOG stream and a first expanded heated BOG stream as a heated third coolant stream, which can either indirectly, more preferably directly, be used as the primary or secondary second coolant stream.
- the first expanded heated BOG stream is used as the primary or secondary second coolant stream in heat exchange/exchanger against the first cooled compressed BOG stream, which heat exchange/exchanger provides a second cooled compressed BOG stream and a first expanded further heated BOG stream as a heated second coolant stream.
- first, second, third, “fourth”, etc. as used herein are intended to indicate a connection or relationship, which may or may not be a direct sequence except where explicitly stated. That is, there may be one or more other steps or processes or locations between a "second" and "third” feature.
- the terms are used to clarify a different nature or presence of an associated feature in or of a stream, and the present invention is not limited by these terms.
- the second coolant stream i.e. first expanded heated BOG stream
- the third coolant stream i.e. first expanded cooled BOG stream
- the third coolant stream is at a lower temperature than the second coolant stream.
- the method further comprises:
- first expanded heated BOG stream as a heated second coolant stream
- intermediate compressed BOG stream such as a first or a second intermediate compressed BOG stream, preferably with a first intermediate compressed BOG stream.
- the step of cooling the compressed BOG discharge stream against one or more first coolant streams to provide a first cooled compressed BOG stream may comprise:
- a first refrigerant stream is used as one of the one or more first coolant streams in a heat exchange/exchanger against the compressed BOG discharge stream, which heat exchange/exchanger provides a first cooled compressed BOG stream and a heated first refrigerant stream as a heated first coolant stream.
- the step of cooling the compressed BOG discharge stream against one or more first coolant streams to provide a first cooled compressed BOG stream may comprise:
- a pre-cooling coolant stream is used as one of the one or more first coolant streams in a heat exchange/exchanger against the
- a first refrigerant stream is used as one of the one or more first coolant streams in a heat exchange/exchanger against the pre-cooled compressed BOG stream, which heat exchange/exchanger provides a first cooled compressed BOG stream and a heated first refrigerant stream as a heated first coolant stream.
- the pre-cooling coolant stream may be part of an open pre-cooling coolant system or a closed pre-cooling coolant system.
- the pre-cooling coolant stream may be selected from a water stream, an air stream or a pre-cooling refrigerant stream, with a water or air stream being preferred.
- the pre-cooling coolant stream may be selected from a seawater stream and an ambient air stream.
- the pre-cooling coolant stream may be selected from a pre-cooling refrigerant stream.
- the cooling of the pre-cooled compressed discharge stream against the pre-cooling coolant stream is carried out in a pre-cooling heat exchanger such as a shell and tube heat exchanger or a plate heat exchanger.
- the one or more first coolant streams comprise a first refrigerant stream, such as a first refrigerant comprising a single refrigerant or mixture of refrigerants.
- the first refrigerant should be capable of condensing ethane (i) at the discharge pressure of the compression system and the discharge temperature of the compression system or (ii) at the discharge pressure of the compression system and the temperature of the pre-cooled
- the first refrigerant may comprise one or more organic compounds, ammonia, and particularly hydrocarbons and fluorinated hydrocarbons such as propane, propylene, difluoromethane and pentafluoromethane, including the fluorinated hydrocarbon mixture R- 41 OA.
- the cooling of the compressed BOG discharge stream or the pre-cooled compressed discharge stream against the first refrigerant stream is carried out in a discharge heat exchanger such as a shell and tube heat exchanger, a plate heat exchanger or an economiser.
- a discharge heat exchanger such as a shell and tube heat exchanger, a plate heat exchanger or an economiser.
- all the compressed BOG discharge stream is cooled against the one or more first coolant streams.
- the liquefied ethane cargo comprises >0.1 mol% methane.
- the liquefied ethane cargo may comprise > 0.4 mol% methane, including >0.5 mol%, 0.6 mol%, >0.7 mol%, >0.8 mol%, >0.9 mol% and >1 .0 mol% methane.
- the present invention extends to a liquefied ethane cargo having 1 -5 mol% methane, optionally >5 mol% methane.
- the number of stages of compression is not a limiting factor of the present invention.
- the method comprises three or four stages of compression
- it is desired to provide a fully condensed boil off gas as the first cooled compressed BOG stream but the present invention extends to a method wherein the boil off gas is not fully condensed after cooling against the one or more first coolant streams.
- the present invention overcomes the difficulty of using certain types of heat exchange, in particular certain types of heat exchanger, and more particularly conventional shell & coil economisers, where the temperature approach is limited by the composition of the fluid in the shell. Where the composition of the fluid in the shell may be a single component, i.e.
- the present invention improves the coefficient of performance of the cooling cycle of a liquefied ethane cargo comprising a significant methane amount, i.e. the present invention improves the coefficient of performance of cargo currently considered de minimus (e.g. 0.1 mol% or less methane), and allows operation with cargoes comprising much higher methane contents (e.g. about or above 0.4 or 0.5 mol% methane.
- the present invention also seeks to maintain the use of current onboard equipment and apparatus with its known OPEX and CAPEX, rather than seeking to introduce and work out how to use new equipment with new operating requirements.
- the cooling of the first cooled compressed BOG stream against the second coolant stream is carried out in an economiser.
- all the first cooled compressed BOG stream is cooled against the second coolant stream.
- all the second cooled compressed BOG stream is cooled against the third coolant stream.
- the method further comprises the steps of: providing a gaseous vent stream from the first cooled compressed BOG stream;
- the present invention can further provide increased re- liquefying of previously considered 'non-condensables' or' non- condensing' components in the compressed BOG.
- the heated fourth coolant stream is or can be used as, a BOG recycle stream.
- the method may further comprise:
- an intermediate compressed BOG stream such as a first or second, preferably first intermediate compressed BOG stream.
- the method of the present invention comprising the further step of:
- the method of the present invention comprising the further steps of:
- the method comprises the further steps of: expanding the cooled vent BOG return stream to provide an expanded cooled vent BOG return stream;
- the stages of compression are the compression stages of a multi-stage compressor.
- the first cooled compressed BOG stream is cooled against at least one second coolant stream to provide a second cooled compressed BOG stream.
- the first cooled compressed BOG stream is wholly or substantially cooled against a second coolant stream only comprising the first expanded heated BOG stream.
- all of the second coolant stream comprises the first expanded heated BOG stream. That is, first cooled compressed BOG stream may be cooled against one or more other second coolant streams, but these are secondary or minor compared to the cooling provided by the use of the first expanded heated BOG stream.
- the first expanded heated BOG stream used as the second coolant stream comprises both liquid and gas phases.
- the liquid and gas phases of the first expanded heated BOG stream used as the second coolant stream are separated in the cooling of the first cooled compressed BOG stream. This is preferably by the apparatus allowing the first cooled compressed BOG stream to be cooled, preferably an economiser.
- an apparatus to cool a boil off gas stream from a liquefied ethane cargo in a floating transportation vessel comprising a plurality of components, said apparatus comprising at least:
- a compression system to compress a boil off gas stream from a liquefied ethane cargo, said compression system comprising two or more stages of compression comprising at least a first stage and a final stage to provide a compressed BOG discharge stream, wherein intermediate, optionally cooled, compressed BOG streams are provided between consecutive stages of compression;
- one or more first heat exchangers to cool the compressed BOG discharge stream to provide a first cooled compressed BOG stream
- one or more second heat exchangers to further cool the first cooled compressed BOG stream against a mixed phase coolant stream to be separated in the one or more second heat exchangers, t o provide a second cooled compressed BOG stream;
- one or more third heat exchangers to further cool the second cooled compressed BOG stream to provide a third cooled compressed BOG stream.
- the apparatus as defined herein is operable using the method as defined herein.
- the second heat exchanger is an economiser.
- a floating transportation vessel for a liquefied ethane cargo having the apparatus as defined herein or operating the method as defined herein.
- the present invention is applicable to any floating transportation vessel for a liquefied ethane cargo.
- the present invention may be utilized in floating transportation vessels where the liquefied ethane cargo storage tanks are fully refrigerated to maintain the cargo in liquid phase at approximately atmospheric pressure by lowering the temperature, as well as in those vessels in which the cargo in the storage tanks is maintained in the liquid phase by a combination of reduced temperature and increased pressure versus ambient.
- the use of economizers is not required.
- heat exchangers such as economizers can be placed between consecutive stages of compression, such as between the first and second stages, to cool the intermediate compressed BOG streams. Where three or more stages of compression are present, heat
- an intercooler can be situated between the second and third stages of compression.
- an economizer can be situated between the second and third, as well as between the first and second stages of compression.
- an expanded, optionally further cooled, portion of the cooled compressed BOG stream can be heat exchanged with an intermediate compressed BOG stream.
- an expanded, optionally further cooled, portion of the cooled compressed BOG stream can be heat exchanged with an optionally further cooled portion of the cooled compressed discharge stream.
- the method and apparatus disclosed herein can be applied to an existing floating transportation vessel as a retro-fit, by maintaining the number of stages of compression present and adding the necessary piping, valves and controls to carry out the cooling of a second cooled compressed BOG stream against an expanded portion of the third cooled BOG stream.
- the term "multiple stages of compression” defines two or more stages of compression in series in a compression system. Each stage of compression may be achieved by one or more compressors. The one or more compressors of each compression stage may be independent from those of the other stages of compression, such that they are driven separately. Alternatively, two or more of the stages of compression may utilize compressors which are linked, typically powered by a single driver and drive shaft, with optional gearing.
- Such linked compression stages may be part of a multi-stage compressor.
- the method and apparatus disclosed herein requires at least two stages of compression. After the first stage of compression, each subsequent stage provides an increased pressure compared to the pressure at the discharge of a previous stage.
- the term "consecutive stages" refers to pairs of adjacent stages of compression i.e. a stage (n) and the next (n+1 ) stage where 'n' is a whole number greater than 0. Consequently, consecutive stages are, for instance, first and second stages or second and third stages or third and fourth stages.
- Intermediate compressed streams (and cooled intermediate compressed streams) refer to those streams connecting consecutive stages of compression.
- next stage of compression or “subsequent stage of compression” used in relation to the cooled intermediate compressed stream refer to the numerically higher number (and higher pressure stage) of the two consecutive stages defining the intermediate stream.
- the heat exchange steps may be indirect, where the two or more streams involved in the heat exchange are separated and not in direct contact. Alternatively, the heat exchange may be direct, in which case the two or more streams involved in the heat exchange can be mixed, thereby producing a combined stream.
- a method integratively designing apparatus to cool a boil off gas stream from a liquefied ethane cargo in a floating transportation vessel comprising a plurality of components, comprising the steps of:
- a compression system to compress a boil off gas stream from a liquefied ethane cargo, said compression system comprising two or more stages of compression comprising at least a first stage and a final stage to provide a compressed BOG discharge stream, wherein
- intermediate, optionally cooled, compressed BOG streams are provided between consecutive stages of compression
- the method further comprises the steps of:
- a method of designing process for the cooling a boil off gas stream from a liquefied ethane cargo in a floating transportation vessel comprising at least the steps of:
- a compression system to compress a boil off gas stream from a liquefied ethane cargo, said compression system comprising two or more stages of compression comprising at least a first stage and a final stage to provide a compressed BOG discharge stream, wherein
- the method further comprising the steps of:
- the designing methods as discussed herein may incorporate computer aided processes for incorporating the relevant operational equipment and controls into the overall vessel construction and may incorporate relevant cost, capacity of operation parameters into the methodology and design.
- the methods described herein may be encoded onto media that is suitable for being read and processed on a computer.
- code to carry out the methods described herein may be encoded onto a magnetic or optical media which can be read by and copied to a personal or mainframe computer. The methods may then be carried out by a design engineer using such a personal or mainframe computer.
- Figure 1 shows a schematic diagram of one possible known system of re- liquefying boil off gas from a cargo tank in a carrier
- Figure 2 shows a schematic diagram of a system of cooling, particularly re-liquefying, boil off gas from a liquefied ethane cargo in a floating transportation vessel according to one embodiment of the invention
- Figures 3a and b are economiser temperature profiles of temperature against heat flow for a pure component BOG cooling system (3a) and a wide boiling multicomponent mixture cooling system (3b); and Figure 4 shows a schematic diagram of a system for cooling, particularly re-liquefying, boil off gas from a liquefied ethane cargo in a floating transportation vessel according to another embodiment of the invention.
- Floating re-liquefaction systems draw the vapor, also known as boil off gas, from one or more storage tanks and pass the boil off gas to a compressor in which it is compressed such that the compressed vapor can be cooled and condensed against one or more coolants as the heat sink/ refrigerant.
- a compressor in which it is compressed such that the compressed vapor can be cooled and condensed against one or more coolants as the heat sink/ refrigerant.
- seawater may be used to pre-cool, typically de- superheat, the compressed vapour in an open cycle pre-cooling circuit.
- the pre-cooled compressed vapour can then be further cooled against a refrigerant in a closed cycle refrigerant circuit.
- FIG. 1 shows a schematic diagram of a known system for re-liquefying boil off gas from an ethane cargo.
- ethane cargo tends to be transported in a repurposed ethylene carrier vessel.
- Liquefied ethane cargo is stored in a tank 50a which may be insulated and/or pressurized in order to maintain the ethane in a liquefied state.
- boil off gas In order to prevent the build-up of this gas, it is removed from the tank 50a as a boil off gas stream 01 a. All the components are compressed, and as many of the components as possible of the removed boil off gas are normally cooled to condense them before it is returned to the tank 50a.
- the boil off gas stream 01 a can be passed to a compression system 60, such as the two stage compressor shown in Figure 1 which comprises a first compression stage 65 and a second compression stage 75.
- the two - stage compression system 60 produces a compressed BOG discharge stream 06a which can be passed to a pre-cooling heat exchanger 100, in which the compressed BOG discharge stream 06a is cooled against a seawater stream 102.
- the pre-cooling heat exchanger 100 produces a pre-cooled compressed BOG stream 07a and a warmed seawater stream 104.
- the pre-cooling heat exchanger 100 can de-superheat the
- the pre-cooled compressed BOG stream 07a can be passed to a refrigerant heat exchanger 250, in which the pre-cooled compressed BOG stream 07a is cooled against a refrigerant stream 252.
- the refrigerant should be capable of condensing ethane at the discharge pressure of the compression system 60.
- the refrigerant may be propane or propylene.
- the refrigerant stream 252 can be part of a refrigerant circuit (not shown) comprising the refrigerant heat exchanger 250, a refrigerant compressor and a refrigerant cooler.
- the refrigerant circuit may be a closed refrigerant system. Such refrigerant circuits, also called refrigerant packs, are well known.
- the refrigerant heat exchanger 250 produces a cooled compressed BOG stream 08a and a heated refrigerant stream 254.
- the cooled compressed BOG stream 08a is an at least partially condensed stream comprising those components of the boil off gas capable, at the discharge pressure of the second stage of compression 75, of 're-liquefaction', i.e. condensation, against the refrigerant.
- the 'non-condensed' components which are incapable of re-liquefaction against the refrigerant in this system may be removed from the refrigerant heat exchanger 250, or an associated accumulator (not shown) located downstream of the refrigerant heat exchanger 250 as a vent stream 49, which is a vapor stream.
- the vent stream 49 is typically vented to the atmosphere, after expansion to atmospheric pressure.
- the cooled compressed BOG stream 08a can be passed to a further heat exchanger 80, to provide a cooled return fluid stream 18, which is typically a fully condensed stream.
- the cooled return fluid stream 18 may then be passed to a return pressure reduction device 22, such as an expander or Joule-Thomson valve, to provide an expanded cooled return fluid stream 24.
- a return pressure reduction device 22 will reduce the pressure of the cooled return fluid stream 18 from at or near the pressure of the compressed BOG discharge stream 06a to a pressure close to that of the liquid ethane and BOG in the tank 50a, such as a pressure just above that of the BOG in the tank which is sufficient to ensure an adequate flow of the expanded cooled return fluid stream 24 to the tank 50a.
- the pressure of the expanded cooled return fluid stream 24 is below that of the discharge pressure of the first stage 65 of compression.
- the first stage 65 of compression provides a first intermediate compressed BOG stream 02a, which is passed to further heat exchanger 80.
- the first intermediate compressed BOG stream 02a can be heat exchanged against an expanded portion 8b of the cooled compressed BOG stream 08a in the further heat exchanger 80 to provide a cooled first intermediate compressed BOG stream 03a, which can then be passed to the suction of the second stage 75 of compression.
- the second stage 75 compresses the cooled first intermediate compressed BOG stream 03a to provide the compressed BOG discharge stream 06a.
- the graph shows a typical temperature profile for the cooling of a 'pure' substance in a conventional shell & coil economiser, with the 'xxxx' line representing the shell side, and the ⁇ ' line representing the tube or coil temperature. It can be seen that the shell side temperature is 'flat', so that there is no change in the shell side temperature with increased heat flow. This represents cooling a 'pure' substance such as pure ethane.
- the method and apparatus disclosed herein seeks to provide an improved method and apparatus of re-liquefying BOG.
- An embodiment of the method and apparatus according to the present invention is disclosed in Figure 2. Where appropriate, identical stream and component names, and the same reference numerals as those in Figure 1 have been used for corresponding streams and components in the remaining Figures.
- Figure 2 shows a liquefied ethane cargo storage tank 50 in a floating transportation vessel, such as an ethane carrier.
- the liquefied ethane cargo may comprise ethane and methane.
- a boil off gas stream 01 comprising evaporated cargo, is passed to a compression system 60 having two or more stages of compression.
- the boil off gas stream 01 may have a pressure (the "BOG pressure") in the range of from above 0 to 500 kPa gauge.
- the compression system 60 may be a multi-stage compressor comprising two or more stages. By “multi-stage compressor” it is meant that each compression stage in the compressor is driven by the same drive shaft. Alternatively, the compression system 60 may comprise independently driven compressors for each of the stages of compression. When the compression system 60 is a multi-stage compressor, it is typically a reciprocating compressor.
- the embodiment of Figure 2 shows a compression system 60 having a first stage 65 and a second stage 70 and a third and final stage 75, although the method and apparatus described herein is also applicable to compressors having two stages or more than three stages.
- the first stage 65 and final stage 75 of compression provide low and high pressure streams respectively at their discharge.
- the compression system 60 compresses the boil off gas stream 01 to provide a compressed BOG discharge stream 06.
- the compressed BOG discharge stream 06 may have a pressure (the "final stage pressure") in the range of from 1.5 to 3.2 MPa or above, eg. up to 6 MPa.
- the compressed BOG discharge stream 06 is cooled in one or more first heat exchangers 200, 300 against one or more first coolant streams 202, 302 to provide first cooled compressed BOG stream 08.
- first heat exchangers 200, 300 against one or more first coolant streams 202, 302 to provide first cooled compressed BOG stream 08.
- the compressed BOG discharge stream 06 can be passed to a pre-cooling heat exchanger 200 as one of the one or more first heat exchangers.
- the compressed BOG discharge stream 06 is pre- cooled against a pre-cooling coolant stream as one of the one of more first coolant streams.
- the pre-cooling coolant stream 202 may be an air or a water stream, such as an ambient air or seawater stream.
- the pre-cooling heat exchanger 200 may be a shell and tube heat exchanger or a plate heat exchanger.
- the pre-cooling heat exchanger may de-superheat the compressed BOG discharge stream 06.
- the pre-cooling heat exchanger 200 provides a pre-cooled compressed BOG stream 07 and heated pre- cooling coolant stream 204.
- the seawater used as the pre- cooling coolant would have a temperature of +36 °C or below, more typically +32 °C or below.
- the pre-cooling heat exchange/exchanger 200 is optional in the method and apparatus disclosed herein. It is advantageous because it reduces the cooling duty of the subsequent cooling steps. However, is it not an essential aspect, such that in an alternative embodiment, the compressed BOG discharge stream 06 can be passed directly to the discharge heat exchanger 300 via line 06', such that the equipment shown by numeral 210 may be omitted. In such circumstances, the cooling capacity of the discharge heat exchanger 300 would have to be increased to compensate for the absence of pre-cooling.
- the pre-cooled compressed BOG stream 07 can then be passed to a discharge heat exchanger 300 as another of the one or more first heat exchangers.
- the discharge heat exchanger 300 cools the pre-cooled compressed BOG stream 07 against a first refrigerant stream 302 as another of the one or more first coolant streams.
- the discharge heat exchanger 300 provides a first cooled compressed BOG stream 08 and a heated first refrigerant stream 304.
- the first refrigerant stream 302, discharge heat exchanger 300 and heated first refrigerant stream 304 may be part of a first refrigerant system (not shown).
- a first refrigerant system may further comprise a first refrigerant compressor to compress the heated first refrigerant stream 304 to provide a compressed first refrigerant stream, a first refrigerant cooler to cool the first refrigerant to provide a cooled compressed first refrigerant stream and a first refrigerant expansion device to expand the cooled compressed first refrigerant stream to provide the first refrigerant stream 302.
- the first refrigerant system may be a closed system.
- the first refrigerant may comprise one or more organic compounds, particularly hydrocarbons and fluorinated hydrocarbons such as propane, propylene, difluoromethane and pentafluoromethane, including the fluorinated hydrocarbon mixture R-410A, as well as one or more inorganic compounds
- the first cooled compressed BOG stream 08 may be a partially
- condensed, compressed BOG stream comprising those components of the boil off gas which can be condensed against the first refrigerant at the discharge pressure of the final stage of compression.
- Any non-condensed components can be removed either from the discharge heat exchanger 300 as a vent stream (not shown) or from a discharge receiver (not shown) which functions as a gas/liquid separator located downstream of the discharge heat exchanger 300.
- Discharge heat exchangers suitable for the separation of gaseous and liquid components are shell and tube heat exchangers in which the cooled compressed BOG is located in the shell- side.
- Any discharge receiver may be an accumulator and can operate to maintain a liquid seal in the discharge heat exchanger 300 and/ or maintain the discharge pressure at the final stage 75 of compression.
- the discharge heat exchanger 300 may be of a type which could not adequately separate vapor and condensed phases into separate streams, such as a plate and fin type heat exchanger. In such a situation, the discharge receiver will be located downstream of the discharge heat exchanger 300 to separate the non-condensed components as a vent stream.
- the first cooled compressed BOG stream 08 is then second cooled. This can be achieved by passing the first cooled compressed BOG stream 08 to a second heat exchanger 180.
- the second heat exchanger 180 may be of any type, and an intermediate stage, particularly first stage, economizer for cooling the intermediate BOG streams 02 or 04 as well as the first cooled compressed stream 08 is shown in Figure 2.
- the cooling of the first cooled compressed BOG stream 08 is against a second coolant stream to provide a second cooled compressed BOG stream 34.
- a portion of the first cooled compressed BOG stream 08 can be used elsewhere prior to passage into the second heat exchanger (180), but in the present invention, it is preferred that wholly or substantially all of the first cooled compressed BOG stream 08 passes into the first heat exchanger 180.
- the action of the second coolant is to provide a second cooled compressed BOG stream 34. Again, a portion of this stream 34 could be used elsewhere, but preferably wholly or substantially all of the second cool compressed BOG stream 34 passes into a third heat exchanger 195 to further cool the second cooled compressed BOG stream 34 and to provide a third cooled compressed BOG stream 35.
- the third heat exchanger 195 may be of any type, such as an economiser, but is preferably a countercurrent heat exchanger such as a plate and fin heat exchanger known in the art.
- a portion of the third cooled compressed BOG stream 35 is expanded to a pressure between that of the first stage discharge pressure and the final stage suction pressure to provide a first expanded cooled BOG stream 33a.
- This action can be carried out through a pressure reduction device 80 such as a Joule-Thomson valve or expander in a manner known in the art.
- the first expanded cooled BOG stream 33a is used as the third coolant in the third heat exchanger 195, which heat exchange provides the third cooled compressed BOG stream 35, and a first expanded heated BOG stream 33b as heated third coolant stream 33b, which can either indirectly, or more preferably directly, be used as the second coolant stream 33b.
- the first expanded heated BOG stream/second coolant stream 33b is not separated (to separate gas/liquid phases) prior to use as the second coolant stream 33b, to fully utilise all of the remaining cooling effect of the first expanded heated BOG stream after use in the third heat exchanger 195.
- the first expanded heated BOG stream/second coolant stream 33b is passed into the second heat exchanger 180, such that the heat exchange with the first cooled compressed BOG stream 08 provides the second cooled compressed BOG stream 34 and a heated second coolant in the second heat exchanger 180.
- the heated second coolant may comprise vapour and liquid components, which are conveniently separated in the second heat exchanger 180, and which is discussed hereinafter.
- the heated second coolant stream which is a first expanded further heated BOG stream, may be passed to an intermediate compressed BOG stream of the appropriate pressure. In the embodiment of Figure 2, the heated second coolant stream is combined with the first intermediate compressed BOG stream 02.
- the portion of the third cooled compressed BOG stream 35 which is not used to provide the first expanded cooled BOG stream 33a can be returned as a return stream to the cargo tank 50 via a pressure reduction device 82 as expanded cooled BOG return stream 36 in a manner known in the art. It is a particular feature of the present invention that no CAPEX change is required in the nature of the first heat exchangers 200, 300 and second heat exchanger 180, such that the operator can continue to use a
- Figure 4 shows a liquefied ethane cargo storage tank 50 from which a boil off gas stream 01 , comprising evaporated cargo, is passed to a compression system 60, having three stages of compression being a first stage 65, a second and intermediate stage 70 and a third and final stage 75.
- the first stage 65 provides a first intermediate compressed BOG stream 02 which passes into the second heat exchanger 180 to provide a cooled first intermediate BOG stream 03 which passes into the intermediate compression stage 70, to provide a second intermediate compressed BOG stream 04 which passes into the suction of the final stage 75 of compression.
- the compression system 60 provides a compressed BOG discharge stream 06 which can be passed into a pre-cooling heat exchanger 200 as one of the one or more first heat exchangers to be cooled against one first coolant being seawater in a seawater stream 202 in a manner previously described, to provide a pre-cooled compressed BOG stream 07.
- the pre-cooled compressed BOG stream 07 can then be passed to a discharge heat exchanger 300 as another of the one or more first heat exchangers in a manner previously described.
- the discharge heat exchanger 300 provides a first cooled compressed BOG stream 08 and a heated first refrigerant stream 304.
- the first cooled compressed BOG stream 08 can be provided either directly, or optionally after passage through a discharge receiver 305 as shown in Figure 4.
- a gaseous vent stream 51 also provided, either from the discharge heat exchanger 300 as stream 51 a, and/or from the discharge receiver 305 as stream 51 b.
- Figure 4 shows the two streams 51 a, 51 b as separate, such streams may be provided separately or combined or without any distinction, depending upon the nature and construction of the discharge heat exchanger 300 and the discharge receiver 305. The provision of these stream or streams is known in the art.
- the gaseous vent stream 51 may comprise both 'non-condensable' components and ⁇ -condensable' components.
- the in-condensable components are generally considered to be components which cannot practically ever by compressed and condensed within the confines and operating parameters of a particular floating transportation vessel BOG cooling system, and primarily relate to nitrogen. Conventionally, it is considered that the major non-condensable component is methane, whose boiling point at 1 atmosphere is
- the method and apparatus may further comprise, as shown by way of example in Figure 4, the steps of expanding a portion of the third cooled compressed BOG stream 35 to form a fourth coolant stream 33c, generally by passage of a portion of the third cooled compressed BOG stream 35 through a pressure reduction valve 87 in an amount which allows that portion of the third cooled compressed BOG stream 35 to act as a fourth coolant 33c in a fourth heat exchanger 197, such as a vent heat exchanger.
- the fourth heat exchanger 197 may be of any type, but is preferably a countercurrent heat exchanger such as a plate and fin arrangement. As shown in Figure 4, the gaseous vent stream 51 can be cooled against the fourth coolant stream 33c to provide a cooled vent stream 53 and a heated fourth coolant stream 38. Optionally, the heated fourth coolant stream 38 is a BOG recycle stream which can pass into the second heat exchanger 180 such that vapour therefrom can be used as part of the cooled first intermediate BOG stream 03.
- the cooling of the gaseous vent stream 51 in the vent heat exchanger 197 can condense a portion of the components of the boil off gas which could not be condensed in the discharge heat exchanger 300 against the first refrigerant such as propane or propylene.
- the cooled vent stream 53 is typically an at least partly condensed stream.
- the cooled vent stream 53 can be passed to a vent stream pressure reduction device 61 (dashed line), such as a Joule- Thomson valve or expander, where its pressure is reduced to provide an expanded further cooled vent stream 63 (dashed line).
- the expanded further cooled vent stream 63 may have a pressure at or slightly above the pressure of the liquefied ethane cargo storage tank 50, so that it can be returned to the tank, for instance by addition to expanded cooled BOG return stream 36 to provide combined expanded cooled BOG return stream 1 1 .
- the cooled vent stream 53 can be passed to a vent stream separator 150, such as a gas/ liquid separator.
- the vent stream separator 150 provides a vent discharge stream 55 being wholly or substantially the in-condensable components, which is typically a vapour stream, and a cooled vent BOG return stream 57, which is typically a condensed stream, comprising those components of the boil off gas which were condensed in the fourth heat exchanger 197.
- the pressure of the vent discharge stream 55 may be reduced, for instance to a pressure appropriate for return to the storage tank 50, for storage elsewhere or for venting.
- the cooled vent BOG return stream 57 may be passed through a vent return stream pressure reduction device 58, such as a Joule-Thomson valve or expander, to provide an expanded cooled vent BOG return stream 59.
- the expanded cooled vent BOG return stream 59 can be passed to the storage tank 50, for instance by addition to the expanded cooled BOG return stream 36.
Abstract
Description
Claims
Priority Applications (4)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
EP15756225.7A EP3183489B1 (en) | 2014-08-21 | 2015-08-21 | Method of cooling boil off gas and an apparatus therefor |
JP2017510369A JP6553714B2 (en) | 2014-08-21 | 2015-08-21 | Boil-off gas cooling method and apparatus |
CN201580050405.9A CN107208841B (en) | 2014-08-21 | 2015-08-21 | Method for cooling boil-off gas and device therefor |
KR1020177007660A KR102379711B1 (en) | 2014-08-21 | 2015-08-21 | Method of cooling boil off gas and an apparatus therefor |
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
GBGB1414893.6A GB201414893D0 (en) | 2014-08-21 | 2014-08-21 | Method of cooling boil off gas and apparatus therefor |
GB1414893.6 | 2014-08-21 |
Publications (1)
Publication Number | Publication Date |
---|---|
WO2016027098A1 true WO2016027098A1 (en) | 2016-02-25 |
Family
ID=51726906
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
PCT/GB2015/052429 WO2016027098A1 (en) | 2014-08-21 | 2015-08-21 | Method of cooling boil off gas and an apparatus therefor |
Country Status (6)
Country | Link |
---|---|
EP (1) | EP3183489B1 (en) |
JP (1) | JP6553714B2 (en) |
KR (1) | KR102379711B1 (en) |
CN (1) | CN107208841B (en) |
GB (1) | GB201414893D0 (en) |
WO (1) | WO2016027098A1 (en) |
Cited By (8)
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KR20180031217A (en) * | 2016-09-19 | 2018-03-28 | 대우조선해양 주식회사 | BOG Reliquefaction System and Method for Vessel |
EP3437981A4 (en) * | 2016-03-31 | 2019-11-27 | Daewoo Shipbuilding & Marine Engineering Co., Ltd. | Ship |
WO2019234025A1 (en) * | 2018-06-04 | 2019-12-12 | Wärtsilä Gas Solutions Norway AS | Method and system for storage and transport of liquefied petroleum gases |
WO2020193971A1 (en) * | 2019-03-27 | 2020-10-01 | Babcock Ip Management (Number One) Limited | Method of cooling boil off gas and an apparatus therefor |
WO2021038220A2 (en) | 2019-08-26 | 2021-03-04 | Babcock Ip Management (Number One) Limited | Method of cooling boil off gas and an apparatus therefor |
CN113490827A (en) * | 2019-02-12 | 2021-10-08 | Lge知识产权管理有限公司 | Method and apparatus for cooling boil-off gas |
DE102021105999A1 (en) | 2021-03-11 | 2022-09-15 | Tge Marine Gas Engineering Gmbh | Method and device for reliquefaction of BOG |
WO2023177306A1 (en) * | 2022-03-15 | 2023-09-21 | Equinor Energy As | A method of storing ethane |
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KR102377796B1 (en) * | 2020-02-17 | 2022-03-23 | 한국조선해양 주식회사 | Gas treatment system and ship having the same |
KR102542651B1 (en) * | 2021-05-11 | 2023-06-14 | 에이치디현대중공업 주식회사 | Boil-off gas re-liquefaction system and ship having the same |
KR102460400B1 (en) * | 2021-06-24 | 2022-10-31 | 대우조선해양 주식회사 | Boil-Off Gas Treatment System and Method for Ship |
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Also Published As
Publication number | Publication date |
---|---|
EP3183489B1 (en) | 2019-12-04 |
JP6553714B2 (en) | 2019-07-31 |
EP3183489A1 (en) | 2017-06-28 |
KR20170043637A (en) | 2017-04-21 |
CN107208841B (en) | 2020-06-16 |
JP2017525910A (en) | 2017-09-07 |
GB201414893D0 (en) | 2014-10-08 |
CN107208841A (en) | 2017-09-26 |
KR102379711B1 (en) | 2022-03-25 |
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