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WO2016140868A1 - Échangeur de chaleur à calandre - Google Patents

Échangeur de chaleur à calandre Download PDF

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Publication number
WO2016140868A1
WO2016140868A1 PCT/US2016/019683 US2016019683W WO2016140868A1 WO 2016140868 A1 WO2016140868 A1 WO 2016140868A1 US 2016019683 W US2016019683 W US 2016019683W WO 2016140868 A1 WO2016140868 A1 WO 2016140868A1
Authority
WO
WIPO (PCT)
Prior art keywords
shell
feed
effluent
heat exchanger
tube
Prior art date
Application number
PCT/US2016/019683
Other languages
English (en)
Inventor
Kiran Ladkat
Deepak BISHT
Suvrendra CHAKRABORTY
Soumendra Mohan BANERJEE
Original Assignee
Uop Llc
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Uop Llc filed Critical Uop Llc
Priority to EP16759296.3A priority Critical patent/EP3265735B1/fr
Priority to CN201680011829.9A priority patent/CN107250703A/zh
Publication of WO2016140868A1 publication Critical patent/WO2016140868A1/fr

Links

Classifications

    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F28—HEAT EXCHANGE IN GENERAL
    • F28F—DETAILS OF HEAT-EXCHANGE AND HEAT-TRANSFER APPARATUS, OF GENERAL APPLICATION
    • F28F9/00—Casings; Header boxes; Auxiliary supports for elements; Auxiliary members within casings
    • F28F9/22—Arrangements for directing heat-exchange media into successive compartments, e.g. arrangements of guide plates
    • 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
    • F28D7/00—Heat-exchange apparatus having stationary tubular conduit assemblies for both heat-exchange media, the media being in contact with different sides of a conduit wall
    • F28D7/16—Heat-exchange apparatus having stationary tubular conduit assemblies for both heat-exchange media, the media being in contact with different sides of a conduit wall the conduits being arranged in parallel spaced relation
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G45/00—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G47/00—Cracking of hydrocarbon oils, in the presence of hydrogen or hydrogen- generating compounds, to obtain lower boiling fractions
    • 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
    • F28D7/00—Heat-exchange apparatus having stationary tubular conduit assemblies for both heat-exchange media, the media being in contact with different sides of a conduit wall
    • F28D7/06—Heat-exchange apparatus having stationary tubular conduit assemblies for both heat-exchange media, the media being in contact with different sides of a conduit wall the conduits having a single U-bend
    • 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
    • F28D2021/0075—Other heat exchangers for particular applications; Heat exchange systems not otherwise provided for for syngas or cracked gas cooling systems

Definitions

  • hydroprocessing units such as kerosene, diesel, gas oil, resid hydrotreating and hydrocracking units
  • hydrogen rich recycle gas and fresh hydrocarbon feed are preheated in a series of heat exchangers utilizing heat available from the reactor effluent.
  • the hot hydrocarbon feed and recycle gas are mixed together to form a combined feed stream at the inlet of the charge heater.
  • the charge heater provides the necessary heat to the combined stream to obtain the desired reactor inlet temperature.
  • This particular flow scheme is known as a separate heat exchanger scheme.
  • the separate heat exchanger flow scheme is used for units that require more than two passes for the charge heater. This flow scheme increases the equipment count and required plot space.
  • Fig. 1 is an illustration of one embodiment of an arrangement for pre-heating a fresh hydrocarbon feed and hydrogen rich recycle gas using the reactor effluent.
  • the hydrocarbon feed 105 is pre-heated in first reactor effluent-feed heat exchanger 110 and second reactor effluent-feed heat exchanger 115 to form pre-heated hydrocarbon feed stream 120.
  • the hydrogen rich recycle gas 125 is pre-heated in first reactor effluent- recycle gas heat exchanger 130, second reactor effluent-recycle gas heat exchanger 135, and third reactor effluent-recycle gas heat exchanger 140 to form pre-heated recycle gas stream 145.
  • pre-heated combined feed stream 150 is combined to form pre-heated combined feed stream 150.
  • Pre-heated combined feed stream 150 is heated in charge heater 155 to form heated feed stream 160.
  • Heated feed stream 160 is sent to reactor 165.
  • the reactor effluent stream 170 from reactor 165 is successively sent to third reactor effluent-recycle gas heat exchanger 140, second reactor effluent-feed heat exchanger 115, second reactor effluent-recycle gas heat exchanger 135, first reactor effluent-feed heat exchanger 110, and first reactor effluent- recycle gas heat exchanger 130.
  • the cooled reactor effluent stream 175 can then be sent for separation between the gas and the liquid (not shown).
  • the shell and tube heat exchanger includes a shell side having a separation plate dividing the shell into at least two compartments, each of the compartments having a feed inlet and a feed outlet; and a tube side comprising a plurality of tubes in the shell, at least one tube in each compartment, and the tube side having an effluent inlet and an effluent outlet.
  • Another aspect of the invention is method of heating a feed and gas stream for a reaction zone using reactor effluent.
  • the method includes providing a shell and tube heat exchanger as described.
  • the feed stream is divided into at least two portions.
  • the two portions of the feed stream re passed from the feed inlets to the feed outlets of each compartment, and the reactor effluent is passed from the effluent inlet to the effluent outlet to pre-heat the two portions of the feed stream.
  • the two pre-heated portions of the feed stream are heated in a charge heater.
  • the two heated portions of the feed stream from the charge heater are introduced into the reaction zone.
  • Fig. 1 is an illustration of a prior art separate heat exchanger configuration for pre-heating a feed and hydrogen rich recycle gas using reactor effluent.
  • Fig. 2 is an illustration of one embodiment of a shell and tube heat exchanger of the present invention.
  • Fig. 3 is an illustration of one embodiment of a configuration for pre-heating a combined feed stream using reactor effluent and employing the shell and tube heat exchanger of the present invention for a two charge heater pass configuration.
  • Fig. 4 is an illustration of another embodiment of a configuration for preheating a combined feed stream using reactor effluent and employing the shell and tube heat exchanger of the present invention for a four charge heater pass configuration.
  • the shell and tube heat exchanger has a split shell design.
  • the shell side has a separation plate dividing the shell into at least two separate compartments. Each of the compartments has a feed inlet and a feed outlet.
  • the tube side has a plurality of tubes, and there is at least one tube in each compartment.
  • the tube side has an effluent inlet and an effluent outlet.
  • the feed inlet, feed outlet, effluent inlet, and effluent outlet are typically nozzles.
  • the compartments are substantially equal in size (for example, within ⁇ 10%).
  • the shell includes at least one baffle.
  • each compartment contains at least one baffle.
  • the baffles are typically arranged to create turbulence for efficient indirect heat transfer between the tube side reactor effluent stream and the shell side combined feed stream. For example, one baffle could contact the bottom (or one side) of the compartment leaving an opening at the top (or opposite side) of the compartment, and the next baffle could contact the top (or the opposite side) leaving an opening at the bottom (or the first side).
  • the shell, tubes, separation plate, and baffles can be made of any suitable material.
  • the shell side inlet and outlet are at opposite ends of the shell. In some embodiments, the tube side inlet and outlet are at the same end of the exchanger.
  • the tube side inlet and outlet are at the same end of the exchanger as the feed outlet.
  • the tubes in this arrangement are U-shaped tubes.
  • the tube side inlet and outlet are at opposite ends of the exchanger.
  • the tubes are straight tubes.
  • Other arrangements of feed inlets and outlets, effluent inlet and outlet, and tube shape could be used, as would be understood by those of skill in the art.
  • the split shell and tube heat exchanger can be used to heat the feed stream entering a reaction zone, for example, a hydrotreating or hydrocracking zone.
  • the feed stream can be heated using the effluent from the same reaction zone.
  • the effluent from one reaction zone could be used to heat the feed for another reaction zone.
  • the feed stream can be a mixture of liquid hydrocarbons and hydrogen rich gaseous hydrocarbons.
  • the liquid hydrocarbon stream could be a fresh hydrocarbon feed stream
  • the gaseous hydrocarbon feed stream could be a hydrogen rich recycle hydrocarbon stream.
  • the combined feed stream is split into two (or more) streams which enter the two (or more) compartments of the shell side of the heat exchanger through the feed stream inlets.
  • the effluent from the reaction zone enters the tube side of the heat exchanger.
  • the effluent can be a two phase mixture of liquid and gaseous hydrocarbons.
  • the heat from the effluent is used to pre-heat the combined feed stream in the two compartments of the shell side.
  • the pre-heated combined feed streams exit the two compartments of the shell side through the shell side outlet nozzles for each compartment.
  • the two pre-heated streams are sent to a charge heater to be further heated to the inlet temperature of the reaction zone.
  • the heated streams are sent from the charge heater to the reaction zone where the reaction occurs.
  • the combined heat exchanger scheme is more energy efficient and requires fewer heat exchangers than the separate heat exchanger scheme.
  • the split shell and tube heat exchanger allows a combined feed heat exchanger scheme when the number of charge heater passes is two or more.
  • a hydrogen rich gaseous hydrocarbon stream can be mixed with the feed stream after the feed stream is divided. Alternatively, it could be mixed with the feed stream after the feed stream is divided.
  • the heated streams from the charge heater can be combined before they are introduced into the reaction zone. Alternatively, they can be introduced into the reaction zone separately. More than one split shell and tube heat exchanger could be used in the process. For example, two or more heat exchangers could be used.
  • the feed stream will be divided into two (or more) streams for each heat exchanger. The number of feed streams per heat exchanger depends on the number of compartments in each heat exchanger.
  • Fig. 2 illustrates one embodiment of a shell and tube heat exchanger 200.
  • the shell and tube heat exchanger 200 includes a shell 205 and tubes 210.
  • the shell 205 has a separation plate 215 which divides the shell 205 into two separate compartments 220, 225.
  • feed inlet 230 and a feed outlet 235 for compartment 220 There is a feed inlet 230 and a feed outlet 235 for compartment 220, and a feed inlet 240 and a feed outlet 245 for compartment 225.
  • One portion of the feed flows through compartment 220 from the feed inlet 230 to the feed outlet 235, and another portion flows through compartment 225 from the feed inlet 240 to the feed outlet 245.
  • reactor effluent inlet 250 There is a reactor effluent inlet 250 and a reactor effluent outlet 255.
  • the reactor effluent inlet 250 is in fluid communication with the tube inlets 260.
  • the reactor effluent outlet 255 is in fluid communication with the tube outlets 265.
  • the reactor effluent flows from the reactor effluent inlet 250 into the tube inlets 260 through the tubes 210 to the tube outlets 265 and out though the reactor effluent outlet 255.
  • a plate 270 separates the tube inlets 260 from the tube outlets 265.
  • the tubes 210 are U-shaped, and the reactor effluent inlet 250 and reactor effluent outlet 255 are at the same end of the shell. However, if straight tubes were used, the reactor effluent inlet 250 would be at one end of the shell 205, and the reactor effluent outlet 255 would be at the opposite end of the shell 205.
  • reactor effluent inlet 250 and reactor effluent outlet 255 are at the same end of the shell 205 as the feed outlets 235, 245 for compartments 220, 225.
  • Compartments 220, 225 have at least one baffle 275. Typically, there are at least two baffles 275 in each compartment 220, 225.
  • the baffles 275 fill the space around the tubes 210 with an opening 280 for the feed to flow around the baffles 275.
  • the baffles 275 are typically arranged so that the feed flows over one baffle 275 and under the next in an S- shaped path to provide maximum heat exchange of the feed with the effluent from the reaction zone flowing through the tubes 210.
  • Fig. 3 is an illustration of a process 300 for heating a feed 305.
  • the feed stream 305 is split into two portions 305A and 305B.
  • a gas stream 310 is also split into two portions 310A and 310B.
  • the feed portions 305A and 305 B are mixed with the gas portions 310A and 31 OB to form combined feeds 315A and 315B.
  • Combined feeds 315A and 315B are sent to a shell and tube heat exchanger 320 with a split shell such as the one illustrated in Fig. 2.
  • the effluent 325 from reaction zone 330 is used to pre-heat the combined feeds 315A and 315B.
  • Pre-heated combined feeds 335 A and 335B are sent to the same charge heater 340 for further heating. Heated combined feeds 345A and 345B are then combined into stream 350 and sent to the reaction zone 330, such as a hydro processing reaction zone.
  • the effluent 325 from the reaction zone 330 is sent to the split shell heat exchanger 320 to heat the combined feeds 315A and 315B.
  • the effluent 355 from the shell and tube heat exchanger 320 with the split shell can be sent to a downstream separator (not shown) for further separation between the gas and the liquid.
  • Fig. 4 is another illustration of a process 400 in which two shell and tube heat exchangers 420A and 420B with split shells are used to heat a feed 405.
  • the feed 405 is split into four portions 405 A, 405B, 405C, and 405D.
  • a gas 410 is also split into four portions 41 OA, 410B, 4 IOC, and 410D.
  • the feed portions 405 A, 405B, 405C, and 405D are mixed with the gas portions 41 OA, 410B, 4 IOC, and 410D to form combined feed 415 A, 415B, 415C, and 415D.
  • Combined feeds 415 A, 415B, 415C, and 415D are sent to the shell and tube heat exchangers 420A and 420B with the split shells.
  • the effluent 425 from reaction zone 430 is used to pre-heat the combined feeds 415A, 415B, 415C, and 415D in the shell and tube heat exchangers 420 A and 420B with the split shells.
  • Pre-heated combined feeds 435 A, 435B, 435C, and 435D are sent to the same charge heater 440 for further heating. Heated combined feeds 445A, 445B, 445C, and 445D are then combined into stream 450 and sent to reaction zone 430, such as a hydroprocessing reaction zone.
  • the effluent 425 from reaction zone 430 is sent to the split shell heat exchangers 420A and 420B to heat the combined feeds 415 A, 415B, 415C, and 415D.
  • the effluent 455 from the shell and tube heat exchangers 420 A and 420B with the split shells can be sent to a downstream separator (not shown) for further separation between the gas and the liquid.
  • a first embodiment of the invention is a shell and tube heat exchanger comprising a shell side having a separation plate dividing the shell into at least two compartments, each of the compartments having a feed inlet and a feed outlet; and a tube side comprising a plurality of tubes in the shell, at least one tube in each compartment, the tube side having an effluent inlet and an effluent outlet.
  • An embodiment of the invention is one, any or all of prior embodiments in this paragraph up through the first embodiment in this paragraph further comprising at least one baffle in the shell.
  • An embodiment of the invention is one, any or all of prior embodiments in this paragraph up through the first embodiment in this paragraph wherein there are at least two baffles in each compartment.
  • An embodiment of the invention is one, any or all of prior embodiments in this paragraph up through the first embodiment in this paragraph wherein the at least two baffles in at least one compartment are arranged with an opening at a first end of one baffle followed by an opening at an opposite end of the next baffle.
  • An embodiment of the invention is one, any or all of prior embodiments in this paragraph up through the first embodiment in this paragraph wherein at least one of the feed inlet of at least one compartment comprises a nozzle; the feed outlet of at least one compartment comprises a nozzle; the effluent inlet of the tube side comprises a nozzle; and the effluent outlet of the tube side comprises a nozzle.
  • An embodiment of the invention is one, any or all of prior embodiments in this paragraph up through the first embodiment in this paragraph wherein the feed inlets of each compartment are at a first end of the shell and the feed outlets of each compartment are at a second end of the shell.
  • An embodiment of the invention is one, any or all of prior embodiments in this paragraph up through the first embodiment in this paragraph wherein the effluent inlet and the effluent outlet are at the same end of the shell.
  • An embodiment of the invention is one, any or all of prior embodiments in this paragraph up through the first embodiment in this paragraph wherein the feed outlets of each compartment are at the same end of the shell as the effluent inlet and the effluent outlet.
  • An embodiment of the invention is one, any or all of prior embodiments in this paragraph up through the first embodiment in this paragraph wherein the plurality of tubes are U-shaped tubes.
  • An embodiment of the invention is one, any or all of prior embodiments in this paragraph up through the first embodiment in this paragraph wherein the plurality of tubes are straight tubes.
  • An embodiment of the invention is one, any or all of prior embodiments in this paragraph up through the first embodiment in this paragraph wherein each compartment has the same number of tubes.
  • a second embodiment of the invention is a method of heating a feed stream for a reaction zone using reactor effluent comprising providing a shell and tube heat exchanger comprising a shell side having a separation plate dividing the shell into at least two compartments, each of the compartments having a feed inlet and a feed outlet; and a tube side comprising a plurality of tubes in the shell, at least one tube in each compartment, the tube side having an effluent inlet and an effluent outlet; dividing the feed stream into at least two portions; passing the two portions of the feed stream from the feed inlets to the feed outlets of each compartment and passing the reactor effluent from the effluent inlet to the effluent outlet to pre-heat the two portions of the feed stream; heating the two pre-heated portions of the feed stream in a charge heater; and introducing the two heated portions of the feed stream from the charge heater into the reaction zone.
  • An embodiment of the invention is one, any or all of prior embodiments in this paragraph up through the second embodiment in this paragraph further comprising mixing a hydrogen rich gaseous hydrocarbon stream with the feed stream.
  • An embodiment of the invention is one, any or all of prior embodiments in this paragraph up through the second embodiment in this paragraph wherein the hydrogen rich gaseous hydrocarbon stream is introduced into the feed stream after the feed stream is divided into the two portions.
  • An embodiment of the invention is one, any or all of prior embodiments in this paragraph up through the second embodiment in this paragraph wherein the reactor effluent comprises a liquid hydrocarbon phase and a gaseous hydrocarbon phase.
  • An embodiment of the invention is one, any or all of prior embodiments in this paragraph up through the second embodiment in this paragraph wherein the two heated portions of the feed stream from the charge heater are combined before introducing the two heated portions of the feed stream from the charge heater into the reaction zone.
  • An embodiment of the invention is one, any or all of prior embodiments in this paragraph up through the second embodiment in this paragraph wherein there are at least two shell and tube heat exchangers; the feed stream is divided into at least four portions; two portions of the feed stream are sent to the first shell and tube heat exchanger and two portions of the feed stream are sent to the second shell and tube heat exchanger; the four preheated portions of the feed stream are heated in the charge heater; the four heated portions of the feed stream from the charge heater are introduced into the reaction zone.
  • An embodiment of the invention is one, any or all of prior embodiments in this paragraph up through the second embodiment in this paragraph wherein there are at least two baffles in each compartment and wherein the at least two baffles in the first compartment or the at least two baffles in the second compartment or both are arranged with an opening at a first end of the first baffle followed by an opening at an opposite end of the second baffle.
  • An embodiment of the invention is one, any or all of prior embodiments in this paragraph up through the second embodiment in this paragraph wherein the feed inlets of each compartment are at a first end of the shell and the feed outlets of each compartment are at a second end of the shell.
  • An embodiment of the invention is one, any or all of prior embodiments in this paragraph up through the second embodiment in this paragraph wherein the effluent inlet and the effluent outlet are at the same end of the shell and wherein the feed outlets of each compartment are at the same end of the shell as the effluent inlet and the effluent outlet, and wherein the plurality of tubes are U-shaped tubes.

Landscapes

  • Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Physics & Mathematics (AREA)
  • Thermal Sciences (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Heat-Exchange Devices With Radiators And Conduit Assemblies (AREA)

Abstract

La présente invention concerne un échangeur de chaleur à calandre. L'échangeur de chaleur à calandre comprend un côté enveloppe ayant une plaque de séparation divisant l'enveloppe en au moins deux compartiments, chacun des compartiments comportant une entrée d'alimentation et une sortie d'alimentation ; et un côté tube comprenant une pluralité de tubes dans l'enveloppe, au moins un tube dans chaque compartiment, et le côté tube ayant une entrée d'effluent et une sortie d'effluent. La présente invention concerne en outre un procédé de chauffage d'un flux d'alimentation pour une zone de réaction au moyen d'un effluent de réacteur en utilisant l'échangeur de chaleur à calandre.
PCT/US2016/019683 2015-03-02 2016-02-26 Échangeur de chaleur à calandre WO2016140868A1 (fr)

Priority Applications (2)

Application Number Priority Date Filing Date Title
EP16759296.3A EP3265735B1 (fr) 2015-03-02 2016-02-26 Échangeur de chaleur à calandre
CN201680011829.9A CN107250703A (zh) 2015-03-02 2016-02-26 壳管式热交换器

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
US14/635,446 US20160258690A1 (en) 2015-03-02 2015-03-02 Shell and tube heat exchanger with split shell and method of using
US14/635,446 2015-03-02

Publications (1)

Publication Number Publication Date
WO2016140868A1 true WO2016140868A1 (fr) 2016-09-09

Family

ID=56848413

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/US2016/019683 WO2016140868A1 (fr) 2015-03-02 2016-02-26 Échangeur de chaleur à calandre

Country Status (4)

Country Link
US (1) US20160258690A1 (fr)
EP (1) EP3265735B1 (fr)
CN (1) CN107250703A (fr)
WO (1) WO2016140868A1 (fr)

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2020121171A1 (fr) * 2018-12-12 2020-06-18 Sabic Global Technologies B.V. Dimérisation de cyclopentadiène à l'aide d'un échangeur de chaleur à tubes et calandre

Families Citing this family (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US10436525B2 (en) * 2016-05-12 2019-10-08 Golden Renewable Energy, LLC Cyclonic cooling system

Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2340138A (en) * 1941-12-31 1944-01-25 Lummus Co Heat exchanger
US2819882A (en) * 1953-10-01 1958-01-14 Westinghouse Electric Corp Heat exchange apparatus
SU920346A1 (ru) * 1978-12-13 1982-04-15 Производственное объединение "Красный котельщик" Конденсатор
US4561496A (en) * 1983-01-25 1985-12-31 Borsig Gmbh Heat exchanger for the cooling of gases, particularly from the synthesis of ammonia
US7384539B2 (en) * 2004-07-28 2008-06-10 Conocophillips Company Optimized preheating of hydrogen/hydrocarbon feed streams

Family Cites Families (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
AU529228B2 (en) * 1977-07-13 1983-06-02 Nippon Shokubai Kagaku Kogyo Co. Ltd. Catalytic vapour phase oxidation
DE4431957A1 (de) * 1994-09-08 1995-03-16 Basf Ag Verfahren zur katalytischen Gasphasenoxidation von Propen zu Acrolein
US6276442B1 (en) * 1998-06-02 2001-08-21 Electric Boat Corporation Combined condenser/heat exchanger

Patent Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2340138A (en) * 1941-12-31 1944-01-25 Lummus Co Heat exchanger
US2819882A (en) * 1953-10-01 1958-01-14 Westinghouse Electric Corp Heat exchange apparatus
SU920346A1 (ru) * 1978-12-13 1982-04-15 Производственное объединение "Красный котельщик" Конденсатор
US4561496A (en) * 1983-01-25 1985-12-31 Borsig Gmbh Heat exchanger for the cooling of gases, particularly from the synthesis of ammonia
US7384539B2 (en) * 2004-07-28 2008-06-10 Conocophillips Company Optimized preheating of hydrogen/hydrocarbon feed streams

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2020121171A1 (fr) * 2018-12-12 2020-06-18 Sabic Global Technologies B.V. Dimérisation de cyclopentadiène à l'aide d'un échangeur de chaleur à tubes et calandre
US11465951B2 (en) 2018-12-12 2022-10-11 Sabic Global Technologies B.V. Dimerization of cyclopentadiene using shell and tube heat exchanger

Also Published As

Publication number Publication date
CN107250703A (zh) 2017-10-13
US20160258690A1 (en) 2016-09-08
EP3265735B1 (fr) 2020-04-15
EP3265735A4 (fr) 2018-08-01
EP3265735A1 (fr) 2018-01-10

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