US20130153172A1 - Method and apparatus for reducing the impact of motion in a core-in-shell heat exchanger - Google Patents
Method and apparatus for reducing the impact of motion in a core-in-shell heat exchanger Download PDFInfo
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- US20130153172A1 US20130153172A1 US13/718,275 US201213718275A US2013153172A1 US 20130153172 A1 US20130153172 A1 US 20130153172A1 US 201213718275 A US201213718275 A US 201213718275A US 2013153172 A1 US2013153172 A1 US 2013153172A1
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Images
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
- F25J5/00—Arrangements of cold exchangers or cold accumulators in separation or liquefaction plants
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F28—HEAT EXCHANGE IN GENERAL
- F28D—HEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA DO NOT COME INTO DIRECT CONTACT
- F28D21/00—Heat-exchange apparatus not covered by any of the groups F28D1/00 - F28D20/00
- F28D21/0017—Flooded core heat exchangers
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F28—HEAT EXCHANGE IN GENERAL
- F28F—DETAILS OF HEAT-EXCHANGE AND HEAT-TRANSFER APPARATUS, OF GENERAL APPLICATION
- F28F1/00—Tubular elements; Assemblies of tubular elements
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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
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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
- F25J1/02—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
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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
- F25J1/0269—Arrangement of liquefaction units or equipments fulfilling the same process step, e.g. multiple "trains" concept
- F25J1/0271—Inter-connecting multiple cold equipments within or downstream of the cold box
- F25J1/0272—Multiple identical heat exchangers in parallel
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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
- F25J1/0278—Unit being stationary, e.g. on floating barge or fixed platform
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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
- F25J1/0279—Compression of refrigerant or internal recycle fluid, e.g. kind of compressor, accumulator, suction drum etc.
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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
- F25J5/00—Arrangements of cold exchangers or cold accumulators in separation or liquefaction plants
- F25J5/002—Arrangements of cold exchangers or cold accumulators in separation or liquefaction plants for continuously recuperating cold, i.e. in a so-called recuperative heat exchanger
- F25J5/005—Arrangements of cold exchangers or cold accumulators in separation or liquefaction plants for continuously recuperating cold, i.e. in a so-called recuperative heat exchanger in a reboiler-condenser, e.g. within a column
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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
- F25J2250/00—Details related to the use of reboiler-condensers
- F25J2250/02—Bath type boiler-condenser using thermo-siphon effect, e.g. with natural or forced circulation or pool boiling, i.e. core-in-kettle heat exchanger
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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
- F25J2250/00—Details related to the use of reboiler-condensers
- F25J2250/20—Boiler-condenser with multiple exchanger cores in parallel or with multiple re-boiling or condensing streams
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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
- F25J2290/00—Other details not covered by groups F25J2200/00 - F25J2280/00
- F25J2290/72—Processing device is used off-shore, e.g. on a platform or floating on a ship or barge
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F28—HEAT EXCHANGE IN GENERAL
- F28D—HEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA DO NOT COME INTO DIRECT CONTACT
- F28D21/00—Heat-exchange apparatus not covered by any of the groups F28D1/00 - F28D20/00
- F28D2021/0019—Other heat exchangers for particular applications; Heat exchange systems not otherwise provided for
- F28D2021/0061—Other heat exchangers for particular applications; Heat exchange systems not otherwise provided for for phase-change applications
- F28D2021/0066—Other heat exchangers for particular applications; Heat exchange systems not otherwise provided for for phase-change applications with combined condensation and evaporation
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P80/00—Climate change mitigation technologies for sector-wide applications
- Y02P80/10—Efficient use of energy, e.g. using compressed air or pressurized fluid as energy carrier
Definitions
- This invention relates to a method and apparatus for reducing the effects of motion in a core-in-shell type heat exchanger.
- Natural gas in its native form must be concentrated before it can be transported economically.
- the use of natural gas has increased significantly in the recent past due to its environmentally-friendly, clean burning characteristics. Burning natural gas produces less carbon dioxide than any other fossil fuel, which is important since carbon dioxide emissions have been recognized as a significant factor in causing the greenhouse effect.
- Liquefied natural gas (LNG) is likely to be used more and more in densely-populated urban areas with the increased concern over environmental issues.
- Abundant natural gas reserves are located all over the world. Many of these gas reserves are located offshore in places that are inaccessible by land and are considered to be stranded gas reserves based on application of existing technology. Existing technical reserves of gas are being replenished faster than oil reserves, making the use of LNG more important to meeting the demands of future energy consumption. In liquid form, LNG occupies 600 times less space than natural gas in its gaseous phase. Since many areas of the world cannot be reached by pipelines due to technical, economic, or political limits, locating the LNG processing plant offshore and utilizing a nautical vessels to directly transport the LNG offshore from the processing plant to the transportation vessel can reduce initial capital expenditure and release otherwise uneconomical offshore gas reserves.
- Floating liquefaction plants provide an off-shore alternative to on-shore liquefaction plants and alternative to costly subsea pipeline for stranded offshore reserves.
- a floating liquefaction plant can be moored off the coast, or close to or at a gas field. It also represents a moveable asset, which can be relocated to a new site when the gas field is nearing the end of its production life, or when required by economic, environmental or political conditions.
- a method for reducing the impact of motion in a heat exchanger includes: (a) flooding the heat exchanger with a vaporizing fluid, wherein the heat exchanger includes an internal volume defined within a shell and a plurality of spaced apart cores disposed within the internal volume of the shell; (b) introducing a hot process feed stream to an upper vessel, wherein the upper vessel is located above the heat exchanger, wherein the upper vessel is connected to the heat exchanger via a plurality of conductor pipes, wherein the conductor pipes include external pipes for connecting the upper vessel and the plurality of spaced apart cores, wherein the conductor pipes further include an internal diameter vapor riser, wherein the internal vapor riser is fixed to the top of the plurality of cores and floats inside the conductor pipe to allow for thermal expansion and contraction of the plurality of cores; (c) delivering the hot feed stream to a core within the internal volume of the shell via the conductor pipes, wherein the hot process feed stream undergoes indirect heat exchange with the vaporizing fluid
- a method for reducing the impact of motion in a heat exchanger includes: (a) flooding the heat exchanger with a vaporizing fluid, wherein the heat exchanger includes an internal volume defined within a shell and a plurality of spaced apart cores disposed within the internal volume of the shell; (b) introducing a hot process feed stream to a separation vessel, wherein the separation vessel is located above the heat exchanger, wherein the separation vessel is connected to the heat exchanger via a plurality of external pipes; (c) delivering the hot process feed stream to a core within the internal volume of the shell via the external pipes, wherein the hot process feed stream undergoes indirect heat exchange with the vaporizing fluid thereby producing a warm liquid stream and a non-vaporized stream, wherein the non-vaporized stream is a mixture of vapor and liquid; and (d) delivering the non-vaporized stream to the separation vessel to undergo separation.
- a method for reducing the impact of motion in a heat exchanger includes: (a) flooding the heat exchanger with a vaporizing liquid, wherein the heat exchanger includes an internal volume defined within a shell and a plurality of spaced apart cores disposed within the internal volume of the shell; (b) introducing a hot process feed stream to a separation vessel, wherein the separation vessel is located at an elevation higher than the heat exchanger, wherein the separation vessel includes a liquid outlet and a vapor inlet; (c) delivering the hot feed stream to a core within the internal volume of the shell at or near the top of the core via the liquid outlet, wherein the hot feed stream undergoes indirect heat exchange with the vaporizing fluid thereby producing a warm liquid stream and a non-vaporized stream, wherein the non-vaporized stream is a mixture of vapor and liquid; and (d) delivering the non-vaporized stream to the separation vessel to undergo separation.
- an apparatus in a further embodiment, includes: (a) a heat exchanger, wherein the heat exchanger includes an internal volume defined within a shell and a plurality of spaced apart cores disposed within the internal volume of the shell, wherein the internal volume is flooded with a vaporizing fluid; and (b) a separation vessel connected to the heat exchanger, wherein the separation vessel is located at higher elevation than the heat exchanger, wherein the separation vessel is connected to the heat exchanger in such a manner so as to deliver a hot feed stream to heat exchanger and the receive a non-vaporizing stream from the heat exchanger.
- FIG. 1 is a schematic of a core-in-shell heat exchanger, according to one embodiment of the invention involving an external horizontal separator.
- FIG. 2 is a schematic of a core-in-shell heat exchanger, according to one embodiment of the invention involving a vertical separator.
- FIG. 3 is a schematic of a core-in-shell heat exchanger, according to one embodiment of the invention involving an external vertical separator.
- a heat exchanger 10 generally includes a shell 12 and a plurality of spaced apart cores, i.e., a first core 16 , a second core 18 , and a third core 20 within the shell 12 .
- the plurality of spaced apart cores within the heat exchanger 10 includes at least one core.
- the heat exchanger is horizontally disposed; however, the heat exchanger may be positioned in any commercially operable manner, such as vertically, for example.
- the plurality of spaced apart cores within the shell 12 are completely submerged, i.e., flooded, in vaporizing fluid, i.e., a liquid refrigerant.
- a principle design of the core-in-shell heat exchanger provides cross exchange of a hot process feed stream against the colder vaporizing fluid.
- the vaporizing fluid resides in a pressure vessel where brazed aluminum compact exchanger cores are mounted and completely submerged in the vaporizing fluid which is at or near its boiling point.
- the liquid is drawn into the bottom face of the exchanger where it contacts the hotter surfaces within the core.
- the vaporizing fluid then transfers heat through the exchanger core channels. The majority of the heat transfer is from the latent heat of vaporization of the vaporizing fluid.
- the hot process feed stream is cooled or condensed as it passes through the opposite side of the channels in the exchanger cores.
- thermosiphon effect is a passive fluid transfer phenomenon resulting from natural convective thermal forces.
- the vaporizing fluid is heated and the vaporizing fluid density decreases.
- fresh liquid is drawn in. This results in a natural circulation of the vaporizing fluid into the core channels induced by the thermal gradient inside the core. Not all vaporizing fluid in the channel is vaporized and a mixture of liquid and vapors typically are transported up through the exchanger core channels and expelled through the top of the core.
- thermosiphon circulation effect in the core is enhanced or impaired by the external hydraulic pressure (level differences) between the effective liquid levels inside the core versus the liquid level outside the core.
- the driving force for the transfer of the liquid into the exchanger core is decreased, and the effective heat transfer is reduced.
- the vaporizing fluid circulation stops due to the loss of the thermosiphon effect which results in the loss of heat transfer. If the heat exchanger is operated with a liquid level higher than the core, i.e., flooded, the heat transferred is impaired further as the vapor produced in the core has to overcome the additional head to escape from the core.
- an upper vessel 30 is utilized, such as depicted in FIG. 1 .
- the upper vessel 30 is located above the heat exchanger 10 and includes a plurality of vapor disengaging conductor pipes 32 connecting the upper vessel 30 to the shell 12 of the heat exchanger 10 .
- the conductor pipes 32 consist of an external pipe connecting the two vessels. Inside the conductor pipes resides an internal smaller diameter vapor riser.
- the vapor riser not shown in FIG. 1 , is fixed to the top of the core, 16 , 18 , 20 and floats inside the conductor pipe 32 so as to allow for thermal expansion and contraction of the exchanger cores 16 , 18 , 20 .
- the vapor riser terminates inside the upper vessel 30 above the normal liquid level of the upper vessel 30 .
- the vapor riser is fastened to the top of the cores 16 , 18 , 20 via a top manifold on the cores 16 , 18 , 20 so as to collect the non-vaporized stream exiting the internal cores 16 , 18 , or 20 .
- the non-vaporized stream is introduced to the upper vessel 30 .
- the non-vaporized stream is then separated in the upper vessel 30 so that liquid flows down the annulus (between the outside of the vapor riser and the inside of the conductor pipe) of the conductor pipe 32 into the shell 12 of the heat exchanger 10 via the plurality of conductor pipes 32 .
- the hot process feed streams are delivered to the plurality of spaced apart cores via externally connecting pipes in order to separately undergo indirect heat exchanger with the vaporizing fluid.
- the plurality of spaced apart cores each receives a separate hot process feed stream, allowing for simultaneous indirect heat transfer between the vaporizing fluid and the separate hot process feed streams.
- the vaporizing fluid and the hot process feed stream flow in a cross-current manner in alternating plate and fin channels inside each core.
- the vaporizing fluid is vaporized in the core resulting in a mixture of vapor and liquid, i.e., the non-vaporized stream, existing the top of the core, which must be disengaged in the upper vessel 30 .
- the vapor risers are designed such that the non-vaporized stream exiting the core remains a mixed phase stream and are routed inside the inner pipe connected via manifold from the top of the plurality of cores 16 , 18 , 20 of the heat exchanger 10 and terminates inside the upper vessel 30 above the normal liquid level in the upper vessel 30 .
- the vapor from non-vaporized stream disengages in the upper vessel 30 and is mixed with the vapor from the non-vaporized stream entering the upper chamber 30 .
- Liquid separates from the hot process feed stream and mixes with the re-circulating liquid from the vapor risers and flows in the outer annulus of the conductor pipes 32 to the bottom of the heat exchanger.
- the upper vessel includes slosh suppressing baffles to minimize liquid surface movement.
- a separation vessel 40 can be utilized to overcome the effects of a flooded heat exchanger to ensure disengagement of the non-vaporized stream, as depicted in FIG. 2 .
- the separation vessel 40 is vertically disposed above the heat exchanger 10 and includes a plurality of conductor pipes 42 connected to the heat exchanger 10 .
- the non-vaporized stream is introduced to the separation vessel 40 .
- the vapor and liquid in non-vaporized stream is separated in the separation vessel 40 and the liquid flows through the external separation vessel to the heat exchanger 10 via the plurality of conductor pipes 42 through the bottom of the separation vessel 40 .
- the vapor risers within the conductor pipes are designed such that the non-vaporized liquid vapor mixture exiting the core remains a mixed two phase stream and are routed inside the inner pipe connected via a manifold from the top of the plurality of cores 16 , 18 , 20 and terminates inside the separation vessel 40 above the normal liquid level in the horizontal return header 43 connected to the vapor space of the separation vessel 40 .
- the vapor from the plurality of cores 16 , 18 , 20 disengages in the separation vessel 40 and is mixed with the vapor from the non-vaporized stream entering the separation vessel 40 and exits the top of the separation vessel 40 .
- Re-circulating liquid is returned to the bottom of the shell 10 via the annulus of the conductor pipes or via the bottom of the separation vessel 40 .
- the hot process feed streams are delivered to the plurality of spaced apart cores via externally connecting pipes in order to separately undergo indirect heat exchanger with the vaporizing fluid.
- the plurality of spaced apart cores each receives a separate hot process feed stream, allowing for simultaneous indirect heat transfer between the vaporizing fluid and the hot process feed streams.
- the vaporizing fluid and the hot process feed stream flow in a cross-current manner in alternating plate and fin channels inside each core.
- the resulting non-vaporized stream is disengaged in the plurality of external pipes 42 .
- the liquid stream is re-circulated back into the heat exchanger 10 via the external side of the annulus pipe inside the conductor pipe 42 .
- the vapor stream flows through the external pipes 42 into the separation vessel 40 .
- a liquid level is maintained in the separation vessel via an external liquid level control valve. Since the separation vessel 40 is vertical, motion suppression may not be required. However, in an embodiment, slosh suppressing baffles are utilized in the separation vessel.
- a separation vessel 50 located at an elevation higher to or at the same elevation as than the heat exchanger 10 can be utilized to overcome the effects of motion and is an alternative method to flood completely flooding the heat exchanger 10 .
- the separation vessel 50 is located to the side of the heat exchanger 10 and includes a feed liquid outlet pipe 52 and a plurality of vapor disengaging conductor inlet pipes 54 .
- a hot process feed stream, i.e., a mixed phase feed stream, is introduced to the separation vessel 50 .
- the vaporizing fluid is delivered to the heat exchangers 10 from the separation vessel 50 through one or more free drains via the feed outlet pipe 52 .
- the hot process feed streams are delivered to the plurality of spaced apart cores via externally connecting pipes in order to separately undergo indirect heat exchanger with the vaporizing fluid.
- the plurality of spaced apart cores each receives a separate feed stream, allowing for simultaneous indirect heat transfer between the vaporizing fluid and the separate feed streams.
- the vaporizing fluid and the feed stream flow in a cross-current manner in alternating plate and fin channels inside each core.
- the resulting non-vaporized stream is disengaged in the plurality of vapor inlet pipes 54 .
- the liquid stream is re-circulated back into the heat exchanger 10 .
- the vapor stream flows through the vapor disengaging conductor inlet pipes into the separation vessel 50 .
- a liquid level is maintained in the separation vessel 50 via an external liquid level control valve. Since the separation vessel 50 is vertical, motion suppression may not be required. However, in an embodiment, slosh suppressing baffles are utilized in the separation vessel 50 .
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- Chemical & Material Sciences (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Ocean & Marine Engineering (AREA)
- Heat-Exchange Devices With Radiators And Conduit Assemblies (AREA)
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Abstract
Methods and apparatuses for reducing the effects of motion in a core-in-shell type heat exchanger are provided. One apparatus includes: (a) a heat exchanger, wherein the heat exchanger includes an internal volume defined within a shell and a plurality of spaced apart cores disposed within the internal volume of the shell, wherein the internal volume is flooded with a vaporizing fluid; and (b) a separation vessel connected to the heat exchanger, wherein the separation vessel is located at higher elevation than the heat exchanger, wherein the separation vessel is connected to the heat exchanger in such a manner so as to deliver a hot feed stream to heat exchanger and the receive a non-vaporizing stream from the heat exchanger.
Description
- This application claims priority benefit under 35 U.S.C. Section 119(e) to U.S. Provisional Patent Ser. No. 61/578,144 filed on Dec. 20, 2011, the entire disclosure of which is incorporated herein by reference and is related to “Internal Baffle For Suppressing Slosh in a Core-in-Shell Heat Exchanger” filed on Dec. 18, 2012.
- This invention relates to a method and apparatus for reducing the effects of motion in a core-in-shell type heat exchanger.
- Natural gas in its native form must be concentrated before it can be transported economically. The use of natural gas has increased significantly in the recent past due to its environmentally-friendly, clean burning characteristics. Burning natural gas produces less carbon dioxide than any other fossil fuel, which is important since carbon dioxide emissions have been recognized as a significant factor in causing the greenhouse effect. Liquefied natural gas (LNG) is likely to be used more and more in densely-populated urban areas with the increased concern over environmental issues.
- Abundant natural gas reserves are located all over the world. Many of these gas reserves are located offshore in places that are inaccessible by land and are considered to be stranded gas reserves based on application of existing technology. Existing technical reserves of gas are being replenished faster than oil reserves, making the use of LNG more important to meeting the demands of future energy consumption. In liquid form, LNG occupies 600 times less space than natural gas in its gaseous phase. Since many areas of the world cannot be reached by pipelines due to technical, economic, or political limits, locating the LNG processing plant offshore and utilizing a nautical vessels to directly transport the LNG offshore from the processing plant to the transportation vessel can reduce initial capital expenditure and release otherwise uneconomical offshore gas reserves.
- Floating liquefaction plants provide an off-shore alternative to on-shore liquefaction plants and alternative to costly subsea pipeline for stranded offshore reserves. A floating liquefaction plant can be moored off the coast, or close to or at a gas field. It also represents a moveable asset, which can be relocated to a new site when the gas field is nearing the end of its production life, or when required by economic, environmental or political conditions.
- One problem encountered in floating liquefaction vessels is the sloshing of vaporizing fluid inside heat exchangers. Sloshing in a heat exchanger may result in the production of forces that can affect stability and control of the heat exchanger. If the vaporizing fluid is allowed to slosh freely inside the shell of the heat exchanger, the moving fluid can have an adverse effect on the thermal function of the heat exchanger core. Furthermore, the cyclical nature of motion may result in cyclical behavior in heat transfer efficiency, and hence, process conditions in the LNG liquefaction plant may be impacted. These instabilities may result in poorer overall plant performance and may lead to narrower operating envelopes and limits to the available production capacity.
- Therefore, a need exists for a method and apparatus for reducing the effects of motion within a core-in-shell type heat exchanger.
- In an embodiment, a method for reducing the impact of motion in a heat exchanger includes: (a) flooding the heat exchanger with a vaporizing fluid, wherein the heat exchanger includes an internal volume defined within a shell and a plurality of spaced apart cores disposed within the internal volume of the shell; (b) introducing a hot process feed stream to an upper vessel, wherein the upper vessel is located above the heat exchanger, wherein the upper vessel is connected to the heat exchanger via a plurality of conductor pipes, wherein the conductor pipes include external pipes for connecting the upper vessel and the plurality of spaced apart cores, wherein the conductor pipes further include an internal diameter vapor riser, wherein the internal vapor riser is fixed to the top of the plurality of cores and floats inside the conductor pipe to allow for thermal expansion and contraction of the plurality of cores; (c) delivering the hot feed stream to a core within the internal volume of the shell via the conductor pipes, wherein the hot process feed stream undergoes indirect heat exchange with the vaporizing fluid thereby producing a warm liquid stream and a non-vaporized stream, wherein the non-vaporized stream includes a mixture of vapor and liquid; and (d) delivering the non-vaporized stream to the upper vessel via the conductor pipes to undergo disengagement.
- In another embodiment, a method for reducing the impact of motion in a heat exchanger includes: (a) flooding the heat exchanger with a vaporizing fluid, wherein the heat exchanger includes an internal volume defined within a shell and a plurality of spaced apart cores disposed within the internal volume of the shell; (b) introducing a hot process feed stream to a separation vessel, wherein the separation vessel is located above the heat exchanger, wherein the separation vessel is connected to the heat exchanger via a plurality of external pipes; (c) delivering the hot process feed stream to a core within the internal volume of the shell via the external pipes, wherein the hot process feed stream undergoes indirect heat exchange with the vaporizing fluid thereby producing a warm liquid stream and a non-vaporized stream, wherein the non-vaporized stream is a mixture of vapor and liquid; and (d) delivering the non-vaporized stream to the separation vessel to undergo separation.
- In yet another embodiment, a method for reducing the impact of motion in a heat exchanger includes: (a) flooding the heat exchanger with a vaporizing liquid, wherein the heat exchanger includes an internal volume defined within a shell and a plurality of spaced apart cores disposed within the internal volume of the shell; (b) introducing a hot process feed stream to a separation vessel, wherein the separation vessel is located at an elevation higher than the heat exchanger, wherein the separation vessel includes a liquid outlet and a vapor inlet; (c) delivering the hot feed stream to a core within the internal volume of the shell at or near the top of the core via the liquid outlet, wherein the hot feed stream undergoes indirect heat exchange with the vaporizing fluid thereby producing a warm liquid stream and a non-vaporized stream, wherein the non-vaporized stream is a mixture of vapor and liquid; and (d) delivering the non-vaporized stream to the separation vessel to undergo separation.
- In a further embodiment, an apparatus includes: (a) a heat exchanger, wherein the heat exchanger includes an internal volume defined within a shell and a plurality of spaced apart cores disposed within the internal volume of the shell, wherein the internal volume is flooded with a vaporizing fluid; and (b) a separation vessel connected to the heat exchanger, wherein the separation vessel is located at higher elevation than the heat exchanger, wherein the separation vessel is connected to the heat exchanger in such a manner so as to deliver a hot feed stream to heat exchanger and the receive a non-vaporizing stream from the heat exchanger.
- The invention, together with further advantages thereof, may best be understood by reference to the following description taken in conjunction with the accompanying drawings in which:
-
FIG. 1 is a schematic of a core-in-shell heat exchanger, according to one embodiment of the invention involving an external horizontal separator. -
FIG. 2 is a schematic of a core-in-shell heat exchanger, according to one embodiment of the invention involving a vertical separator. -
FIG. 3 is a schematic of a core-in-shell heat exchanger, according to one embodiment of the invention involving an external vertical separator. - Reference will now be made in detail to embodiments of the present invention, one or more examples of which are illustrated in the accompanying drawings. Each example is provided by way of explanation, not as a limitation. It will be apparent to those skilled in the art that various modifications and variations can be made in the present invention without departing from the scope or spirit of the invention. For instance, features illustrated or described as part of one embodiment can be used in another embodiment to yield a still further embodiment. Thus, it is intended that the present invention cover such modifications and variations that come within the scope of the appended claims and their equivalents.
- Referring to
FIGS. 1-3 , aheat exchanger 10 generally includes a shell 12 and a plurality of spaced apart cores, i.e., afirst core 16, asecond core 18, and athird core 20 within the shell 12. The plurality of spaced apart cores within theheat exchanger 10 includes at least one core. For illustrative purposes, the heat exchanger is horizontally disposed; however, the heat exchanger may be positioned in any commercially operable manner, such as vertically, for example. The plurality of spaced apart cores within the shell 12 are completely submerged, i.e., flooded, in vaporizing fluid, i.e., a liquid refrigerant. - A principle design of the core-in-shell heat exchanger provides cross exchange of a hot process feed stream against the colder vaporizing fluid. The vaporizing fluid resides in a pressure vessel where brazed aluminum compact exchanger cores are mounted and completely submerged in the vaporizing fluid which is at or near its boiling point. The liquid is drawn into the bottom face of the exchanger where it contacts the hotter surfaces within the core. The vaporizing fluid then transfers heat through the exchanger core channels. The majority of the heat transfer is from the latent heat of vaporization of the vaporizing fluid. The hot process feed stream is cooled or condensed as it passes through the opposite side of the channels in the exchanger cores.
- The thermal and hydraulic performance of the core-in-shell heat exchanger is dependent upon the liquid level in the exchanger. A driving force for circulation of the vaporizing fluid into the exchanger cores is the thermosiphon effect. The thermosiphon effect is a passive fluid transfer phenomenon resulting from natural convective thermal forces. As the vaporization of the fluid occurs, the vaporizing fluid is heated and the vaporizing fluid density decreases. As it naturally flows upward in the channels, fresh liquid is drawn in. This results in a natural circulation of the vaporizing fluid into the core channels induced by the thermal gradient inside the core. Not all vaporizing fluid in the channel is vaporized and a mixture of liquid and vapors typically are transported up through the exchanger core channels and expelled through the top of the core. Above the core, adequate space must be provided for the vapor and liquid to disengage so that only vapor leaves the overhead section of the shell side of the core. Liquid that separates in the upper section of the exchanger is then re-circulated to the bottom of the vessel where it is then vaporized in the core. The driving force for separation of the liquid and the gas in the upper section of the core-in-shell heat exchanger is gravity.
- The thermosiphon circulation effect in the core is enhanced or impaired by the external hydraulic pressure (level differences) between the effective liquid levels inside the core versus the liquid level outside the core. As the liquid level in the shell falls, the driving force for the transfer of the liquid into the exchanger core is decreased, and the effective heat transfer is reduced. When the liquid level falls below the core, the vaporizing fluid circulation stops due to the loss of the thermosiphon effect which results in the loss of heat transfer. If the heat exchanger is operated with a liquid level higher than the core, i.e., flooded, the heat transferred is impaired further as the vapor produced in the core has to overcome the additional head to escape from the core.
- To overcome the impact of a flooded heat exchanger and to ensure disengagement of the non-vaporized stream, a mixture of vapor and liquid, an
upper vessel 30 is utilized, such as depicted inFIG. 1 . Theupper vessel 30 is located above theheat exchanger 10 and includes a plurality of vapor disengagingconductor pipes 32 connecting theupper vessel 30 to the shell 12 of theheat exchanger 10. Theconductor pipes 32 consist of an external pipe connecting the two vessels. Inside the conductor pipes resides an internal smaller diameter vapor riser. The vapor riser, not shown inFIG. 1 , is fixed to the top of the core, 16, 18, 20 and floats inside theconductor pipe 32 so as to allow for thermal expansion and contraction of theexchanger cores upper vessel 30 above the normal liquid level of theupper vessel 30. The vapor riser is fastened to the top of thecores cores internal cores upper vessel 30. The non-vaporized stream is then separated in theupper vessel 30 so that liquid flows down the annulus (between the outside of the vapor riser and the inside of the conductor pipe) of theconductor pipe 32 into the shell 12 of theheat exchanger 10 via the plurality ofconductor pipes 32. - Upon entry into the
heat exchanger shell 10 via a plurality of connecting pipes, the hot process feed streams are delivered to the plurality of spaced apart cores via externally connecting pipes in order to separately undergo indirect heat exchanger with the vaporizing fluid. The plurality of spaced apart cores each receives a separate hot process feed stream, allowing for simultaneous indirect heat transfer between the vaporizing fluid and the separate hot process feed streams. The vaporizing fluid and the hot process feed stream flow in a cross-current manner in alternating plate and fin channels inside each core. - As previously discussed, only a portion of the vaporizing fluid is vaporized in the core resulting in a mixture of vapor and liquid, i.e., the non-vaporized stream, existing the top of the core, which must be disengaged in the
upper vessel 30. The vapor risers are designed such that the non-vaporized stream exiting the core remains a mixed phase stream and are routed inside the inner pipe connected via manifold from the top of the plurality ofcores heat exchanger 10 and terminates inside theupper vessel 30 above the normal liquid level in theupper vessel 30. The vapor from non-vaporized stream disengages in theupper vessel 30 and is mixed with the vapor from the non-vaporized stream entering theupper chamber 30. Liquid separates from the hot process feed stream and mixes with the re-circulating liquid from the vapor risers and flows in the outer annulus of theconductor pipes 32 to the bottom of the heat exchanger. In this embodiment, the upper vessel includes slosh suppressing baffles to minimize liquid surface movement. - Alternatively, a
separation vessel 40 can be utilized to overcome the effects of a flooded heat exchanger to ensure disengagement of the non-vaporized stream, as depicted inFIG. 2 . Theseparation vessel 40 is vertically disposed above theheat exchanger 10 and includes a plurality ofconductor pipes 42 connected to theheat exchanger 10. The non-vaporized stream is introduced to theseparation vessel 40. The vapor and liquid in non-vaporized stream is separated in theseparation vessel 40 and the liquid flows through the external separation vessel to theheat exchanger 10 via the plurality ofconductor pipes 42 through the bottom of theseparation vessel 40. The vapor risers within the conductor pipes are designed such that the non-vaporized liquid vapor mixture exiting the core remains a mixed two phase stream and are routed inside the inner pipe connected via a manifold from the top of the plurality ofcores separation vessel 40 above the normal liquid level in the horizontal return header 43 connected to the vapor space of theseparation vessel 40. The vapor from the plurality ofcores separation vessel 40 and is mixed with the vapor from the non-vaporized stream entering theseparation vessel 40 and exits the top of theseparation vessel 40. Re-circulating liquid is returned to the bottom of theshell 10 via the annulus of the conductor pipes or via the bottom of theseparation vessel 40. - Upon entry into the shell 12 of the
heat exchanger 10 via a plurality of connecting pipes, the hot process feed streams are delivered to the plurality of spaced apart cores via externally connecting pipes in order to separately undergo indirect heat exchanger with the vaporizing fluid. The plurality of spaced apart cores each receives a separate hot process feed stream, allowing for simultaneous indirect heat transfer between the vaporizing fluid and the hot process feed streams. The vaporizing fluid and the hot process feed stream flow in a cross-current manner in alternating plate and fin channels inside each core. - The resulting non-vaporized stream is disengaged in the plurality of
external pipes 42. The liquid stream is re-circulated back into theheat exchanger 10 via the external side of the annulus pipe inside theconductor pipe 42. The vapor stream flows through theexternal pipes 42 into theseparation vessel 40. A liquid level is maintained in the separation vessel via an external liquid level control valve. Since theseparation vessel 40 is vertical, motion suppression may not be required. However, in an embodiment, slosh suppressing baffles are utilized in the separation vessel. - Referring to
FIG. 3 , aseparation vessel 50 located at an elevation higher to or at the same elevation as than theheat exchanger 10 can be utilized to overcome the effects of motion and is an alternative method to flood completely flooding theheat exchanger 10. InFIG. 3 , theseparation vessel 50 is located to the side of theheat exchanger 10 and includes a feedliquid outlet pipe 52 and a plurality of vapor disengagingconductor inlet pipes 54. A hot process feed stream, i.e., a mixed phase feed stream, is introduced to theseparation vessel 50. The vaporizing fluid is delivered to theheat exchangers 10 from theseparation vessel 50 through one or more free drains via thefeed outlet pipe 52. Upon entry into theheat exchanger shell 10 via a plurality of connecting pipes, the hot process feed streams are delivered to the plurality of spaced apart cores via externally connecting pipes in order to separately undergo indirect heat exchanger with the vaporizing fluid. The plurality of spaced apart cores each receives a separate feed stream, allowing for simultaneous indirect heat transfer between the vaporizing fluid and the separate feed streams. The vaporizing fluid and the feed stream flow in a cross-current manner in alternating plate and fin channels inside each core. - The resulting non-vaporized stream is disengaged in the plurality of
vapor inlet pipes 54. The liquid stream is re-circulated back into theheat exchanger 10. The vapor stream flows through the vapor disengaging conductor inlet pipes into theseparation vessel 50. A liquid level is maintained in theseparation vessel 50 via an external liquid level control valve. Since theseparation vessel 50 is vertical, motion suppression may not be required. However, in an embodiment, slosh suppressing baffles are utilized in theseparation vessel 50. - In order to minimize the size of the vapor disengaging space required in the external or integral separator device, internal devices like vane packs, demister pads, or cyclonic devices could be utilized to reduce the diameter required in the separator and thus reduce the overall size required to remove the liquid droplets from the vapor stream.
- In closing, it should be noted that the discussion of any reference is not an admission that it is prior art to the present invention, especially any reference that may have a publication date after the priority date of this application. At the same time, each and every claim below is hereby incorporated into this detailed description or specification as additional embodiments of the present invention.
- Although the systems and processes described herein have been described in detail, it should be understood that various changes, substitutions, and alterations can be made without departing from the spirit and scope of the invention as defined by the following claims. Those skilled in the art may be able to study the preferred embodiments and identify other ways to practice the invention that are not exactly as described herein. It is the intent of the inventors that variations and equivalents of the invention are within the scope of the claims while the description, abstract and drawings are not to be used to limit the scope of the invention. The invention is specifically intended to be as broad as the claims below and their equivalents.
Claims (10)
1. A method for reducing the impact of motion in a heat exchanger comprising:
a. flooding the heat exchanger with a vaporizing fluid, wherein the heat exchanger includes an internal volume defined within a shell and a plurality of spaced apart cores disposed within the internal volume of the shell;
b. introducing a hot process feed stream to an upper vessel, wherein the upper vessel is located above the heat exchanger, wherein the upper vessel is connected to the heat exchanger via a plurality of conductor pipes, wherein the conductor pipes include external pipes for connecting the upper vessel and the plurality of spaced apart cores, wherein the conductor pipes further include an internal diameter vapor riser, wherein the internal vapor riser is fixed to the top of the plurality of cores and floats inside the conductor pipe to allow for thermal expansion and contraction of the plurality of cores;
c. delivering the hot feed stream to a core within the internal volume of the shell via the conductor pipes, wherein the hot process feed stream undergoes indirect heat exchange with the vaporizing fluid thereby producing a warm liquid stream and a non-vaporized stream, wherein the non-vaporized stream includes a mixture of vapor and liquid; and
d. delivering the non-vaporized stream to the upper vessel via the conductor pipes to undergo disengagement.
2. The method according to claim 1 , wherein the vaporizing fluid is a refrigerant.
3. The method according to claim 1 , wherein the upper vessel includes slosh suppressing baffles.
4. A method for reducing the impact of motion in a heat exchanger comprising:
a. flooding the heat exchanger with a vaporizing fluid, wherein the heat exchanger includes an internal volume defined within a shell and a plurality of spaced apart cores disposed within the internal volume of the shell;
b. introducing a hot process feed stream to a separation vessel, wherein the separation vessel is located above the heat exchanger, wherein the separation vessel is connected to the heat exchanger via a plurality of external pipes;
c. delivering the hot process feed stream to a core within the internal volume of the shell via the external pipes, wherein the hot process feed stream undergoes indirect heat exchange with the vaporizing fluid thereby producing a warm liquid stream and a non-vaporized stream, wherein the non-vaporized stream is a mixture of vapor and liquid; and
d. delivering the non-vaporized stream to the separation vessel to undergo separation.
5. The method according to claim 4 , wherein the vaporizing fluid is a refrigerant.
6. The method according to claim 4 , wherein the separation vessel includes slosh suppressing baffles.
7. A method for reducing the impact of motion in a heat exchanger comprising:
a. flooding the heat exchanger with a vaporizing liquid, wherein the heat exchanger includes an internal volume defined within a shell and a plurality of spaced apart cores disposed within the internal volume of the shell;
b. introducing a hot process feed stream to a separation vessel, wherein the separation vessel is located at an elevation higher than the heat exchanger, wherein the separation vessel includes a liquid outlet and a vapor inlet;
c. delivering the hot feed stream to a core within the internal volume of the shell at or near the top of the core via the liquid outlet, wherein the hot feed stream undergoes indirect heat exchange with the vaporizing fluid thereby producing a warm liquid stream and a non-vaporized stream, wherein the non-vaporized stream is a mixture of vapor and liquid; and
d. delivering the non-vaporized stream to the separation vessel to undergo separation.
8. The method according to claim 12, wherein the vaporizing fluid is a refrigerant.
9. The method according to claim 12, wherein the separation vessel includes slosh suppressing baffles.
10. An apparatus comprising:
a. a heat exchanger, wherein the heat exchanger includes an internal volume defined within a shell and a plurality of spaced apart cores disposed within the internal volume of the shell, wherein the internal volume is flooded with a vaporizing fluid; and
b. a separation vessel connected to the heat exchanger, wherein the separation vessel is located at higher elevation than the heat exchanger, wherein the separation vessel is connected to the heat exchanger in such a manner so as to deliver a hot feed stream to heat exchanger and the receive a non-vaporizing stream from the heat exchanger.
Priority Applications (7)
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RU2014129909A RU2611537C2 (en) | 2011-12-20 | 2012-12-18 | Method and device for reducing movement effect in “core-shell” type heat exchanger |
JP2014549209A JP6170943B2 (en) | 2011-12-20 | 2012-12-18 | Method and apparatus for reducing the effects of motion in an in-shell core heat exchanger |
PCT/US2012/070383 WO2013096328A1 (en) | 2011-12-20 | 2012-12-18 | Method and apparatus for reducing the impact of motion in a core-in-shell heat exchanger |
CN201280063617.7A CN104024776B (en) | 2011-12-20 | 2012-12-18 | For the method and apparatus reducing the impact of the motion in core shell-type exchangers |
US13/718,275 US20130153172A1 (en) | 2011-12-20 | 2012-12-18 | Method and apparatus for reducing the impact of motion in a core-in-shell heat exchanger |
AU2012355362A AU2012355362B2 (en) | 2011-12-20 | 2012-12-18 | Method and apparatus for reducing the impact of motion in a core-in-shell heat exchanger |
AP2014007702A AP2014007702A0 (en) | 2011-12-20 | 2012-12-18 | Method and apparatus for reducing the impact of motion in a core-in-shell heat exchanger |
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US13/718,275 US20130153172A1 (en) | 2011-12-20 | 2012-12-18 | Method and apparatus for reducing the impact of motion in a core-in-shell heat exchanger |
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Cited By (1)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
WO2015134188A1 (en) * | 2014-03-07 | 2015-09-11 | Conocophillips Company | Heat exchanger system with mono-cyclone inline separator |
Citations (21)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US2720082A (en) * | 1952-02-04 | 1955-10-11 | N A Hardin | Multiple unit barge having an expansion chamber communicating with plural storage tanks |
US2928254A (en) * | 1954-09-20 | 1960-03-15 | Garrett Corp | Storage tank for low temperature liquids |
GB918920A (en) * | 1959-03-04 | 1963-02-20 | Honeywell Regulator Co | Improvements in or relating to methods and apparatus for butt welding fine metal filaments |
US3103206A (en) * | 1961-12-26 | 1963-09-10 | Combustion Eng | Shell and tube type vapor generating unit |
US3521605A (en) * | 1968-07-05 | 1970-07-28 | Blaw Knox Co | Forced recirculation evaporator |
US3563308A (en) * | 1969-04-21 | 1971-02-16 | Stewart Warner Corp | Submerged core heat exchanger |
US3583370A (en) * | 1969-08-22 | 1971-06-08 | J F Pritchard And Co | Shroud for fire-tube boiler |
GB1299643A (en) * | 1969-04-26 | 1972-12-13 | Messer Griesheim Gmbh | Evaporator-condenser apparatus |
GB1515631A (en) * | 1976-01-30 | 1978-06-28 | Raffinage Cie Francaise | Tank for storing liquefied gas and utilisation of said tank for storing butane |
US5667005A (en) * | 1994-04-04 | 1997-09-16 | Jgc Corporation | Heat exchanging unit and heat exchanging apparatus |
US6158238A (en) * | 1996-09-04 | 2000-12-12 | Abb Power Oy | Arrangement for transferring heating and cooling power |
FR2797943A1 (en) * | 1999-08-24 | 2001-03-02 | Air Liquide | Evaporator-condenser for air distillation installation comprises dihedral body with fluid passage opening on first face hermetically covered by cylindrical connecting box |
US20010030042A1 (en) * | 2000-04-13 | 2001-10-18 | L' Air Liquide, Societe Anonyme Pour L' Etude Et L' Exploitation Des Procedes Georges Claude | Reboiler/condenser heat exchanger of the bath type |
JP2003336933A (en) * | 2002-05-17 | 2003-11-28 | Takuma Co Ltd | Flooded-double tube evaporator and ammonia absorption refrigerating machine |
US20050039486A1 (en) * | 2002-01-17 | 2005-02-24 | York Refrigeration Aps | Submerged evaporator with integrated heat exchanger |
US6918433B2 (en) * | 2000-08-23 | 2005-07-19 | Vahterus Oy | Heat exchanger with plate structure |
US7073572B2 (en) * | 2003-06-18 | 2006-07-11 | Zahid Hussain Ayub | Flooded evaporator with various kinds of tubes |
US20080041096A1 (en) * | 2005-04-06 | 2008-02-21 | Mayekawa Mfg. Co., Ltd. | Flooded evaporator |
WO2008112549A2 (en) * | 2007-03-09 | 2008-09-18 | Johnson Controls Technology Company | Heat exchanger |
US20100319877A1 (en) * | 2009-06-23 | 2010-12-23 | Conocophillips Company | Removable Flow Diversion Baffles for Liquefied Natural Gas Heat Exchangers |
US20120175091A1 (en) * | 2010-12-30 | 2012-07-12 | Linde Aktiengesellschaft | Distribution system and heat exchanger apparatus |
Family Cites Families (11)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
SU476436A1 (en) * | 1973-04-02 | 1975-07-05 | Предприятие П/Я А-3605 | Heat exchanger for air separation unit |
US4882283A (en) * | 1987-11-17 | 1989-11-21 | Phillips Petroleum Company | Heat exchange apparatus |
US5651270A (en) * | 1996-07-17 | 1997-07-29 | Phillips Petroleum Company | Core-in-shell heat exchangers for multistage compressors |
US5875837A (en) * | 1998-01-15 | 1999-03-02 | Modine Manufacturing Company | Liquid cooled two phase heat exchanger |
US6158240A (en) * | 1998-10-23 | 2000-12-12 | Phillips Petroleum Company | Conversion of normally gaseous material to liquefied product |
US7310971B2 (en) * | 2004-10-25 | 2007-12-25 | Conocophillips Company | LNG system employing optimized heat exchangers to provide liquid reflux stream |
FR2834783B1 (en) * | 2002-01-17 | 2004-06-11 | Air Liquide | THERMAL EXCHANGE FIN, METHOD FOR MANUFACTURING SAME, AND CORRESPONDING HEAT EXCHANGER |
US6568209B1 (en) * | 2002-09-06 | 2003-05-27 | Praxair Technology, Inc. | Cryogenic air separation system with dual section main heat exchanger |
US6848725B2 (en) * | 2003-04-11 | 2005-02-01 | Dwws, Llc | Thermal expansion connection for rigid pipes |
US6827138B1 (en) * | 2003-08-20 | 2004-12-07 | Abb Lummus Global Inc. | Heat exchanger |
US7266976B2 (en) * | 2004-10-25 | 2007-09-11 | Conocophillips Company | Vertical heat exchanger configuration for LNG facility |
-
2012
- 2012-12-18 RU RU2014129909A patent/RU2611537C2/en active
- 2012-12-18 US US13/718,275 patent/US20130153172A1/en not_active Abandoned
- 2012-12-18 ES ES12859864T patent/ES2762736T3/en active Active
- 2012-12-18 EP EP12859864.6A patent/EP2795216B1/en active Active
- 2012-12-18 WO PCT/US2012/070383 patent/WO2013096328A1/en active Application Filing
- 2012-12-18 CN CN201280063617.7A patent/CN104024776B/en active Active
- 2012-12-18 AP AP2014007702A patent/AP2014007702A0/en unknown
- 2012-12-18 AU AU2012355362A patent/AU2012355362B2/en active Active
- 2012-12-18 JP JP2014549209A patent/JP6170943B2/en active Active
Patent Citations (21)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US2720082A (en) * | 1952-02-04 | 1955-10-11 | N A Hardin | Multiple unit barge having an expansion chamber communicating with plural storage tanks |
US2928254A (en) * | 1954-09-20 | 1960-03-15 | Garrett Corp | Storage tank for low temperature liquids |
GB918920A (en) * | 1959-03-04 | 1963-02-20 | Honeywell Regulator Co | Improvements in or relating to methods and apparatus for butt welding fine metal filaments |
US3103206A (en) * | 1961-12-26 | 1963-09-10 | Combustion Eng | Shell and tube type vapor generating unit |
US3521605A (en) * | 1968-07-05 | 1970-07-28 | Blaw Knox Co | Forced recirculation evaporator |
US3563308A (en) * | 1969-04-21 | 1971-02-16 | Stewart Warner Corp | Submerged core heat exchanger |
GB1299643A (en) * | 1969-04-26 | 1972-12-13 | Messer Griesheim Gmbh | Evaporator-condenser apparatus |
US3583370A (en) * | 1969-08-22 | 1971-06-08 | J F Pritchard And Co | Shroud for fire-tube boiler |
GB1515631A (en) * | 1976-01-30 | 1978-06-28 | Raffinage Cie Francaise | Tank for storing liquefied gas and utilisation of said tank for storing butane |
US5667005A (en) * | 1994-04-04 | 1997-09-16 | Jgc Corporation | Heat exchanging unit and heat exchanging apparatus |
US6158238A (en) * | 1996-09-04 | 2000-12-12 | Abb Power Oy | Arrangement for transferring heating and cooling power |
FR2797943A1 (en) * | 1999-08-24 | 2001-03-02 | Air Liquide | Evaporator-condenser for air distillation installation comprises dihedral body with fluid passage opening on first face hermetically covered by cylindrical connecting box |
US20010030042A1 (en) * | 2000-04-13 | 2001-10-18 | L' Air Liquide, Societe Anonyme Pour L' Etude Et L' Exploitation Des Procedes Georges Claude | Reboiler/condenser heat exchanger of the bath type |
US6918433B2 (en) * | 2000-08-23 | 2005-07-19 | Vahterus Oy | Heat exchanger with plate structure |
US20050039486A1 (en) * | 2002-01-17 | 2005-02-24 | York Refrigeration Aps | Submerged evaporator with integrated heat exchanger |
JP2003336933A (en) * | 2002-05-17 | 2003-11-28 | Takuma Co Ltd | Flooded-double tube evaporator and ammonia absorption refrigerating machine |
US7073572B2 (en) * | 2003-06-18 | 2006-07-11 | Zahid Hussain Ayub | Flooded evaporator with various kinds of tubes |
US20080041096A1 (en) * | 2005-04-06 | 2008-02-21 | Mayekawa Mfg. Co., Ltd. | Flooded evaporator |
WO2008112549A2 (en) * | 2007-03-09 | 2008-09-18 | Johnson Controls Technology Company | Heat exchanger |
US20100319877A1 (en) * | 2009-06-23 | 2010-12-23 | Conocophillips Company | Removable Flow Diversion Baffles for Liquefied Natural Gas Heat Exchangers |
US20120175091A1 (en) * | 2010-12-30 | 2012-07-12 | Linde Aktiengesellschaft | Distribution system and heat exchanger apparatus |
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Publication number | Priority date | Publication date | Assignee | Title |
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WO2015134188A1 (en) * | 2014-03-07 | 2015-09-11 | Conocophillips Company | Heat exchanger system with mono-cyclone inline separator |
AU2015225689B2 (en) * | 2014-03-07 | 2019-01-03 | Conocophillips Company | Heat exchanger system with mono-cyclone inline separator |
US10488104B2 (en) | 2014-03-07 | 2019-11-26 | Conocophillips Company | Heat exchanger system with mono-cyclone inline separator |
Also Published As
Publication number | Publication date |
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AU2012355362A1 (en) | 2014-06-12 |
RU2611537C2 (en) | 2017-02-28 |
JP2015510572A (en) | 2015-04-09 |
CN104024776A (en) | 2014-09-03 |
EP2795216A1 (en) | 2014-10-29 |
EP2795216A4 (en) | 2016-05-18 |
AU2012355362B2 (en) | 2017-02-02 |
JP6170943B2 (en) | 2017-07-26 |
RU2014129909A (en) | 2016-02-20 |
EP2795216B1 (en) | 2019-11-20 |
CN104024776B (en) | 2016-08-17 |
ES2762736T3 (en) | 2020-05-25 |
WO2013096328A1 (en) | 2013-06-27 |
AP2014007702A0 (en) | 2014-06-30 |
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