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EP3265735B1 - Échangeur de chaleur à calandre - Google Patents

Échangeur de chaleur à calandre Download PDF

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Publication number
EP3265735B1
EP3265735B1 EP16759296.3A EP16759296A EP3265735B1 EP 3265735 B1 EP3265735 B1 EP 3265735B1 EP 16759296 A EP16759296 A EP 16759296A EP 3265735 B1 EP3265735 B1 EP 3265735B1
Authority
EP
European Patent Office
Prior art keywords
shell
effluent
tube
feed
inlet
Prior art date
Legal status (The legal status 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 status listed.)
Not-in-force
Application number
EP16759296.3A
Other languages
German (de)
English (en)
Other versions
EP3265735A4 (fr
EP3265735A1 (fr
Inventor
Kiran Ladkat
Deepak BISHT
Suvrendra CHAKRABORTY
Soumendra Mohan BANERJEE
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Honeywell UOP LLC
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
Publication of EP3265735A1 publication Critical patent/EP3265735A1/fr
Publication of EP3265735A4 publication Critical patent/EP3265735A4/fr
Application granted granted Critical
Publication of EP3265735B1 publication Critical patent/EP3265735B1/fr
Not-in-force legal-status Critical Current
Anticipated expiration legal-status Critical

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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 hydrocarbon feed stream 120 and pre-heated recycle gas stream 145 are 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 multiple heat exchangers (five in this example) increase the equipment cost and the space required. Therefore, there is a need for a heat exchanger design which allows the use of a single exchanger train for the scheme which requires more than two heater passes.
  • 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. at the same end of the shell and separated by a plate, and whereby the tubes are U-shaped.
  • 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 are 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.
  • 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 are U-shaped tubes.
  • 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.
  • 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.
  • 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 310B 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 335A 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 405A, 405B, 405C, and 405D.
  • a gas 410 is also split into four portions 410A, 410B, 410C, and 410D.
  • the feed portions 405A, 405B, 405C, and 405D are mixed with the gas portions 410A, 410B, 410C, and 410D to form combined feed 415A, 415B, 415C, and 415D.
  • Combined feeds 415A, 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 420A and 420B with the split shells.
  • Pre-heated combined feeds 435A, 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.
  • 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 415A, 415B, 415C, and 415D.
  • the effluent 455 from the shell and tube heat exchangers 420A and 420B with the split shells can be sent to a downstream separator (not shown) for further separation between the gas and the liquid.

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  • 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)

Claims (10)

  1. Échangeur de chaleur à calandre (200) comprenant :
    un côté enveloppe ayant une plaque de séparation (215) divisant l'enveloppe (205) en au moins deux compartiments (220, 225), chacun des compartiments ayant une entrée d'alimentation (230, 240) et une sortie d'alimentation (235, 245) ; et
    un côté tube comprenant une pluralité de tubes (210) dans l'enveloppe (205), au moins un tube (210) dans chaque compartiment, le côté tube ayant une entrée d'effluent (250) et une sortie d'effluent (255) ;
    dans lequel l'entrée d'effluent (250) est en communication fluidique avec les entrées de tube (260) et la sortie d'effluent (255) est en communication fluidique avec les sorties de tube (265) ; et
    dans lequel une plaque (270) sépare les entrées de tube (260) des sorties de tube (265) ; et
    dans lequel les tubes (210) sont en forme de U et l'entrée d'effluent (250) et la sortie d'effluent (255) sont à la même extrémité de l'enveloppe.
  2. Échangeur de chaleur à calandre selon la revendication 1, comprenant en outre au moins un déflecteur (275) dans l'enveloppe (205).
  3. Échangeur de chaleur à calandre selon l'une quelconque des revendications 1 à 2, dans lequel au moins l'un de : l'entrée d'alimentation (230, 240) d'au moins un compartiment comprend une buse ; la sortie d'alimentation (235, 245) d'au moins un compartiment comprend une buse ; l'entrée d'effluent (250) du côté tube comprend une buse ; et la sortie d'effluent (255) du côté tube comprend une buse.
  4. Échangeur de chaleur à calandre selon l'une quelconque des revendications 1 à 2, dans lequel les entrées d'alimentation (230, 240) de chaque compartiment sont à une première extrémité de l'enveloppe (205) et les sorties d'alimentation (235, 245) de chaque compartiment sont à une seconde extrémité de l'enveloppe (205).
  5. Échangeur de chaleur à calandre selon l'une quelconque des revendications 1 à 2, dans lequel l'entrée d'effluent (250) et la sortie d'effluent (255) sont à la même extrémité de l'enveloppe (205).
  6. Échangeur de chaleur à calandre selon la revendication 5, dans lequel les sorties d'alimentation (235, 245) de chaque compartiment sont à la même extrémité de l'enveloppe (205) que l'entrée d'effluent (250) et la sortie d'effluent (255).
  7. Procédé de chauffage d'un flux d'alimentation pour une zone de réaction utilisant un effluent de réacteur comprenant :
    la fourniture d'un échangeur de chaleur à calandre (320) comprenant :
    un côté enveloppe ayant une plaque de séparation (215) divisant l'enveloppe (205) en au moins deux compartiments (220, 225), chacun des compartiments ayant une entrée d'alimentation (230, 240) et une sortie d'alimentation (235, 245) ; et
    un côté tube comprenant une pluralité de tubes (210) dans l'enveloppe (205), au moins un tube (210) dans chaque compartiment, le côté tube ayant une entrée d'effluent (250) et une sortie d'effluent (255) ;
    dans lequel l'entrée d'effluent (250) est en communication fluidique avec les entrées de tube (260) et la sortie d'effluent (255) est en communication fluidique avec les sorties de tube (265) ;
    dans lequel l'effluent de réacteur s'écoule de l'entrée d'effluent (250) dans les entrées de tube (260) à travers les tubes (210) vers les sorties de tube (265) et sort par la sortie d'effluent (255) ; et
    dans lequel une plaque (270) sépare les entrées de tube (260) des sorties de tube (265) ; et
    dans lequel les tubes (210) sont en forme de U et l'entrée d'effluent (250) et la sortie d'effluent (255) sont à la même extrémité de l'enveloppe ;
    la division du flux d'alimentation (305) en au moins deux parties (305A, 305B) ;
    le passage des deux parties (305A, 305B) du flux d'alimentation (305) des entrées d'alimentation (230, 240) aux sorties d'alimentation (235, 245) de chaque compartiment et le passage de l'effluent de réacteur (325) de l'entrée d'effluent (250) à la sortie d'effluent (255) pour préchauffer les deux parties (305A, 305B) du flux d'alimentation (305) ;
    le chauffage des deux parties préchauffées (335A, 335B) du flux d'alimentation (305) dans un dispositif de chauffage de charge (340) ; et
    l'introduction des deux parties chauffées (345A, 345B) du flux d'alimentation (305) depuis le dispositif de chauffage de charge (340) dans la zone de réaction (330).
  8. Procédé selon la revendication 7, comprenant en outre le mélange d'un flux d'hydrocarbure gazeux riche en hydrogène (310) avec le flux d'alimentation (305).
  9. Procédé selon l'une quelconque des revendications 7 à 8, dans lequel l'effluent de réacteur (325) comprend une phase hydrocarbonée liquide et une phase hydrocarbonée gazeuse.
  10. Procédé selon l'une quelconque des revendications 7 à 8, dans lequel les deux parties chauffées (345A, 345B) du flux d'alimentation (305) issu du dispositif de chauffage de charge (340) sont combinées avant d'introduire les deux parties chauffées (345A, 345B) du flux d'alimentation (305) issu du dispositif de chauffage de charge (340) dans la zone de réaction (330).
EP16759296.3A 2015-03-02 2016-02-26 Échangeur de chaleur à calandre Not-in-force EP3265735B1 (fr)

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
PCT/US2016/019683 WO2016140868A1 (fr) 2015-03-02 2016-02-26 Échangeur de chaleur à calandre

Publications (3)

Publication Number Publication Date
EP3265735A1 EP3265735A1 (fr) 2018-01-10
EP3265735A4 EP3265735A4 (fr) 2018-08-01
EP3265735B1 true EP3265735B1 (fr) 2020-04-15

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ID=56848413

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Application Number Title Priority Date Filing Date
EP16759296.3A Not-in-force EP3265735B1 (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)

Families Citing this family (2)

* 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
CN113260601A (zh) * 2018-12-12 2021-08-13 沙特基础全球技术有限公司 使用壳管式热交换器进行的环戊二烯二聚

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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
AU529228B2 (en) * 1977-07-13 1983-06-02 Nippon Shokubai Kagaku Kogyo Co. Ltd. Catalytic vapour phase oxidation
SU920346A1 (ru) * 1978-12-13 1982-04-15 Производственное объединение "Красный котельщик" Конденсатор
DE3302304A1 (de) * 1983-01-25 1984-07-26 Borsig Gmbh, 1000 Berlin Waermetauscher zum kuehlen von heissen gasen, insbesondere aus der ammoniak-synthese
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
US7384539B2 (en) * 2004-07-28 2008-06-10 Conocophillips Company Optimized preheating of hydrogen/hydrocarbon feed streams

Non-Patent Citations (1)

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Title
None *

Also Published As

Publication number Publication date
CN107250703A (zh) 2017-10-13
US20160258690A1 (en) 2016-09-08
EP3265735A4 (fr) 2018-08-01
WO2016140868A1 (fr) 2016-09-09
EP3265735A1 (fr) 2018-01-10

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