US3593968A - Rapid cooling for high-temperature gas streams - Google Patents

Rapid cooling for high-temperature gas streams Download PDF

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Publication number
US3593968A
US3593968A US762871A US3593968DA US3593968A US 3593968 A US3593968 A US 3593968A US 762871 A US762871 A US 762871A US 3593968D A US3593968D A US 3593968DA US 3593968 A US3593968 A US 3593968A
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United States
Prior art keywords
quench
chamber
zone
oil
pyrolysis
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Expired - Lifetime
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US762871A
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English (en)
Inventor
Ray L Geddes
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Stone and Webster Engineering Corp
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Stone and Webster Engineering Corp
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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F28—HEAT EXCHANGE IN GENERAL
    • F28C—HEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA COME INTO DIRECT CONTACT WITHOUT CHEMICAL INTERACTION
    • F28C3/00—Other direct-contact heat-exchange apparatus
    • F28C3/06—Other direct-contact heat-exchange apparatus the heat-exchange media being a liquid and a gas or vapour
    • 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
    • C10G9/00—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
    • C10G9/002—Cooling of cracked gases
    • 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
    • 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
    • Y10—TECHNICAL SUBJECTS COVERED BY FORMER USPC
    • Y10S—TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10S585/00—Chemistry of hydrocarbon compounds
    • Y10S585/919—Apparatus considerations
    • Y10S585/921—Apparatus considerations using recited apparatus structure

Definitions

  • the present invention relates generally to quenching the gaseous products discharged from pyrolysis furnaces. More I particularly, the present invention is directed to reducing the accumulation of inimical deposits of material such as tar or coke in the quench chambers associated with pyrolysis furnaces.
  • the operating problems connected with the formation of coke deposits are particularly troublesome during the quenching of the products from pyrolysis of high-boiling oils such as naphtha, kerosene, and gas oils where, in the course of the quenching, high-boiling oil products are condensed out onto metal surfaces at relatively high temperatures.
  • the condensed liquid is subject to pyrolysis-polymerization reactions leading to partial conversion to coke residue which remains on the surface of the quench chamber.
  • This harmful coke deposition phenomenon is particularly troublesome at the point in the cooling of the pyrolysis gas mixture where the dew point of the gas mixture is just reached and the first small amount of condensed liquid appears. At this point of incipient condensation the very small amount of liquid forming flows very slowly and thus is subjected longest to the pyrolytic-condensation reactions leading to coke deposits. Generally, the rate of coke formation is most rapid when the initial condensation of the pyrolysis product is in the temperature range of about 500900 F.
  • One of the advantages of the present invention is the avoidance of the harmful coke deposits during rapid quenching through the critical 500-900 F. range with a suitable means for minimizing or eliminating thin, long residence liquid films in the 500900 F. range.
  • a method and apparatus for quenching hot pyrolysis gases which minimizes harmful coke deposition.
  • pyrolysis gases may be cooled to below their dew points under conditions where the chamber walls surrounding the initial condensation are covered by rapidly flowing thick liquid films in which the short residence time at high temperature markedly reduces the extent of the pyrolytic-condensation reactions and coke deposition.
  • hot pyroly' sis gases leaving the pyrolysis furnace or cracking zone are conveyed, under pressure, generally downwardly into a quenching zone.
  • the upper portion of the quenching zone surrounds the lowermost portion of the conduit delivering hot gas from the cracking zone to the quenching zone.
  • the said conduit extends a short distance into the quench chamber and is separated therefrom by a suitable insulation means, said means comprising a layer of solid insulation or preferably a combination of solid insulation and one or more annular zones which may be purged by inert fluid such as steam or nitrogen.
  • means are provided for flowing a film of quench oil over the entire interior surface of the quench zone.
  • the film of quench oil will generally flow continuously downwardly along the vertically extending walls of the quench zone.
  • a means or plurality of means are also provided for spraying quench oil into the quench zone into contact with the hot pyrolysis gases whereby cooling is effected.
  • the length of the quench zone and the temperature and boiling range characteristics of the quench oil are selected in accordance with the initial temperature of the pyrolysis gases and the final temperature desired to be achieved by quenching.
  • means are located for flowing quench oil and quenched gases to suitable f ractionatin g means.
  • the quench fluid employed is preferably an oil that is capable of wetting the metal walls of the quench zone.
  • Suitable quench oils are those known to the prior art, including various gas oils and light petroleum distillates.
  • the boiling range of the quench liquid should be such that not more than about 75 percent will be vaporized when in use.
  • the entry temperature of the quench liquid will be selected in accordance with the final temperature desired for the material leaving the quench zone.
  • the quench liquid which flows down the wall and the quench liquid which is sprayed into the quenching zone may be from the same source or from separate sources, according to availability. When separate sources are used, the higher boiling of the two liquids should be directed to flow down the quench chamber wall while the lower boiling liquid is sprayed into the quench zone.
  • FIG. 1 represents a schematic drawing showing the location of the quench zone in relation to the preceding pyrolysis zone and the subsequent fractionating zone;
  • FIG. 2 is a sectional elevational view of the upper portion of the quench zone showing one embodiment of the apparatus for applying a film of quench liquid to the walls of the quench zone;
  • FIG. 3 is a partial sectional elevational view of the upper portion of the quench zone showing another embodiment of the apparatus for applying a film of quench liquid to the walls of the quench zone.
  • feed enters the pyrolysis zone wherein it is cracked and converted to lighter products which leave generally at a temperature between downwardly into the quench chamber 2.
  • the terminal portion 3 of the conduit 1 may be surrounded by a layer of insulation 4 to protect the walls of quench chamber 2 from the extremely high gas temperatures.
  • the insulation maybe a solid type as shown in FIG. 2 or may be a combination of the solid type and one or more insulating gaps as shown in H6. 3.
  • the quench chamber 2 suitably can be a metal pipe or chamber having an opening for receiving the lowermost portion 3 of conduit 1.
  • Means are provided in quench chamber 2 for continuously delivering a film of quench liquid along the vertically extending walls of quench chamber 2.
  • entry ports 5 connected to a source, not shown, of quench liquid at the desired temperature.
  • a metal ring 6 is positioned within the upper part ofquench chamber 2 and, as shown, is connected to quench chamber 2 by suitable connecting means such as bolts 7 or by fusion welding.
  • the ring 6 is essentially frustoconical in configuration with a maximum diameter somewhat smaller than the inside diameter of the quench chamber.
  • a small annular opening 8 is provided between the lowermost edge of the ring 6 and the wall of quench chamber 2.
  • One or more spray means such as shown by nozzles 9 and 10, are provided and are connected to a quench liquid supply, not shown, and are positioned to spray quench liquid supply, under pressure, into quench chamber 2.
  • conduit 1 When the gases passing through conduit 1 are at a temperature low enough that harmful coking of the nozzle does not occur, a single downwardly directed nozzle centrally located near the exit of the conduit 1 may be used.
  • conduit 1 can have dimensions of between about 3 and 18 inches in diameter with quench chamber 2 having a diameter generally at least 4 inches greater than that of conduit 1.
  • the annular opening 8 should be small and will preferably be less than one-quarter of an inch in diameter.
  • cracked gas at an elevated temperature and 5 under pressure passes through conduit 1 and exits through the lowermost portion of conduit 1 into quench chamber 2.
  • Quench liquid at a temperature below its boiling point is delivered through entry ports 5 and annular opening 8 to deliver a film of quench liquid 11 on the surface of quench chamber 2.
  • Additional quench liquid is simultaneously injected into the stream of pyrolysis products through nozzles 9 and and any additional nozzles, not shown, found to be necessary to achieve the desired final temperature.
  • the presence of insulation 4 serves to decrease the flow of heat from conduit 1 to ring 6, thus helping to maintain the ring at a relatively low temperature, ensuring that a minimum of unwanted side reactions will occur in the vicinity of annular opening 8, thus minimizing harmful coke deposition in that area.
  • the insulation 4 can be of any common variety of insulating material such as, for example, diatomaceous earth and will have a thickness such that the temperature on the external portion of the insulation will not exceed about 150 F. higher than the quench oil entry temperature.
  • the insulating material is retained in position and protected from the gaseous and liquid environment by a metallic covering 15. As seen in FIG. 2, the metallic covering 15 is attached directly to the terminal opening 3 of conduit 1 and to the metal wall ofthe quench chamber 2 by suitable means such as welding.
  • a pyrolysis gas containing 100 parts by-weight of hydrocarbons and 80 parts by weight of steam is passed through conduit 1 into quench chamber 2 where it is cooled using a quench oil which is a gas oil having a specific gravity of 0.9 10 and a boiling range of 450 F. to 850 F. and which is introduced into the quench chamber at a temperature below 450 F.
  • the hydrocarbon composition of the pyrolysis gases is approximately by weight, 1 percent hydrogen, 13.5 percent methane, 27.4 percent C s, 13.2 percent C 's, 7.0 percent C 's, 31.4 percent C 400 F., and 6.5 percent heavy oil.
  • the temperature of the mixture leaving the quench chamber is 575 F.
  • a similar pyrolysis gas mixture entering at a temperature of 1,200 F. is quenched with a similar gas oil at a temperature of 270 F.
  • the hot pyrolysis gases are delivered to and through conduit 1 whose diameter is 16 inches at a rate of about 46,000
  • the quench chamber 2 has a diameter of 24 inches and quench oil is delivered through annular opening 8 at a rate of approximately 700 g.p.m. with the annular opening 8 being 0.135 inches.
  • a single solid cone spray head 9 is provided, operating to deliver about 300 g.p.m. of quench oil from a pressure of 40 p.s.i. g.
  • the total flow of quench oil is regulated to obtain an exit temperature from the bottom of the quench chamber 2 of 350 F. Approximately 10 percent of the quench oil is vaporized and 90 percent exits as liquid.
  • the hot pyrolysis gases are delivered to and through conduit 1 whose diameter is 16 inches at a rate of about 46,000
  • total length ofthe quench chamber 2 is about 14 feet.
  • a similar pyrolysis gas mixture entering at a temperature of 1,650 F. is quenched by spraying in a similar gas oil at a temperature of 400 F.
  • the hot .pyrolysis gases are delivered to and through conduit 1 whose diameter is 8 inches at a rate approximately 20,000 lb./hr.
  • the quench chamber has a diameter of approximately 18 inches.
  • a heavier quench oil of specific gravity 1.02 and boiling range 600 F. to 1,200 F. is delivered through annular opening 8 at the rate of approximately 100 gallons per minute at an inlet temperature of 580 with annular opening 8 being one-sixteenth of an inch.
  • Three solid cone spray heads one in addition to 9 and 10 are provided, each operating to deliver 55 gallons per minute of quench oil from a pressure of 40 p.s.i.g.
  • the sprayed oil rate is regulated to obtain an exit temperature of the gas leaving the bottom of quench chamber 2 of 588 F.
  • About 50 percent of the quench oil is vaporized.
  • the total length of quench chamber 2 in this instance is about 16 feet.
  • the embodiment of the present invention depicted in FIG. 3 includes the provision of an annular chamber 14 between the metallic wall 15 and the frustoconical ring 6 which defines the annular nozzle opening 8 for the quench liquid.
  • an annular array of openings or ports 5 are provided through which quench liquid or oil may be introduced and directed downwardly through an annular opening 8 to coat the walls of the quench chamber 2 with a film 11.
  • the insulation 4 and metallic retaining wall 15 therefore are also present in this embodiment.
  • an annular insulation chamber 14 is located between the insulation liner 15 and the annular frustoconical ring 45.
  • the annular insulation chamber 14 provides an additional thermal insulation structure to protect the quench liquid chamber and nozzle opening 8 from the hot gas discharging from the lowermost portion 3 of the conduit 1.
  • a plurality of openings 12 are provided through which an inert gas such as steam or nitrogen may be introduced into the system and directed downwardly through the annular chamber 14 between the metallic ring 6 and the metallic insulation liner 15.
  • the inert gas which is supplied to the system from a source not shown, is passed through the annular chamber 14 for the purpose of keeping it free of any residue accumulation.
  • FIG. 3 shows a single annular chamber 14 between the metallic ring 6 and the insulation retaining wall 15, two or more substantially concentric the spirit and scope thereof and therefore the invention is not limited by that which is shown in the drawings and described in the specification but only as indicated in the appended claims.
  • Apparatus for quenching a cracked gas stream from a hydrocarbon-cracking furnace comprising a conduit extcnd ing into a quenching zone for delivering hot cracked gases generally downwardly into the quenching zone, a quenching chamber surrounding the lowermost portion of said conduit means, said quenching chamber having a larger cross-sec tional area than the delivery conduit and extending downwardly to receive the downward flow of the cracked gas stream exiting from the conduit means, an internal sleeve located intermediately of the delivery conduit and the wall of the quench chamber, a frustoconical extremity on the bottom of the internal sleeve defining an annular opening to direct a flow of quench oil downwardly along the downwardly extending walls of the quench chamber to contact and cool cracked gas flowing therethrough; a layer of solid insulation arranged between the internal sleeve and the: portion of the hot gas delivery conduit, which solid insulation layer is configured and arranged to afford at least one annular gap between the internal sleeve and the layer of solid
  • Apparatus as in claim I further comprising means for passing inert gas through the annular gap forming part of the insulation means.

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Physics & Mathematics (AREA)
  • Thermal Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Engineering & Computer Science (AREA)
  • General Chemical & Material Sciences (AREA)
  • Mechanical Engineering (AREA)
  • Organic Chemistry (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
  • Physical Or Chemical Processes And Apparatus (AREA)
  • Chemical Vapour Deposition (AREA)
US762871A 1968-09-26 1968-09-26 Rapid cooling for high-temperature gas streams Expired - Lifetime US3593968A (en)

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US76287168A 1968-09-26 1968-09-26

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BE (1) BE739454A (zh)
DE (1) DE1942001C3 (zh)
ES (1) ES371918A1 (zh)
FR (1) FR2022196A1 (zh)
GB (1) GB1232940A (zh)
NL (1) NL163252C (zh)

Cited By (46)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3907661A (en) * 1973-01-29 1975-09-23 Shell Oil Co Process and apparatus for quenching unstable gas
US3959420A (en) * 1972-05-23 1976-05-25 Stone & Webster Engineering Corporation Direct quench apparatus
US4085034A (en) * 1975-10-14 1978-04-18 Kureha Kagaku Kogyo Kabushiki Kaisha Method for the thermal cracking of heavy hydrocarbon
US4087497A (en) * 1976-05-15 1978-05-02 Hoechst Aktiengesellschaft Cooling device
US4115072A (en) * 1977-04-07 1978-09-19 Chevron Research Company Retractable fluids spraying assembly
US4121908A (en) * 1976-04-23 1978-10-24 Linde Aktiengesellschaft Apparatus for the cooling of a cracking-gas stream
US4147753A (en) * 1975-10-14 1979-04-03 Kureha Kagaku Kogyo Kabushiki Kaisha Apparatus for the thermal cracking of heavy hydrocarbon
US4322222A (en) * 1975-11-10 1982-03-30 Occidental Petroleum Corporation Process for the gasification of carbonaceous materials
EP0066384A1 (en) * 1981-05-18 1982-12-08 Exxon Research And Engineering Company Method and apparatus for cooling a cracked gas stream
US4446003A (en) * 1981-06-02 1984-05-01 British Gas Corporation Heat recovery process and apparatus
EP0122415A2 (de) * 1983-03-17 1984-10-24 Hoechst Aktiengesellschaft Abkühlungseinrichtung
US4558451A (en) * 1982-07-19 1985-12-10 The United States Of America As Represented By The Secretary Of The Air Force Tubular singlet delta oxygen generator
US4597780A (en) * 1981-06-04 1986-07-01 Santek, Inc. Electro-inertial precipitator unit
US4614229A (en) * 1983-06-20 1986-09-30 Exxon Research & Engineering Co. Method and apparatus for efficient recovery of heat from hot gases that tend to foul heat exchanger tubes
US4702818A (en) * 1983-11-28 1987-10-27 Mitsubishi Jukogyo Kabushiki Kaisha Process for recovering heat of a tar-containing high-temperature gas
US4780196A (en) * 1985-07-12 1988-10-25 Institut Francais Du Petrole Hydrocarbon steam cracking method
US4801307A (en) * 1984-04-27 1989-01-31 Texaco Inc. Quench ring and dip-tube assembly
US4849057A (en) * 1987-06-30 1989-07-18 Bbc Brown Boveri Aktiengesellschaft Apparatus for the pyrolysis of waste material
US5043058A (en) * 1990-03-26 1991-08-27 Amoco Corporation Quenching downstream of an external vapor catalyst separator
US5087427A (en) * 1990-03-26 1992-02-11 Amoco Corporation Catalytic cracking unit with internal gross cut separator and quench injector
US5089235A (en) * 1990-03-26 1992-02-18 Amoco Corporation Catalytic cracking unit with external cyclone and oil quench system
US6626424B2 (en) * 1999-03-24 2003-09-30 Shell Oil Company Quench nozzle
US20070007172A1 (en) * 2005-07-08 2007-01-11 Strack Robert D Method for processing hydrocarbon pyrolysis effluent
US20070007174A1 (en) * 2005-07-08 2007-01-11 Strack Robert D Method for processing hydrocarbon pyrolysis effluent
WO2007008406A1 (en) 2005-07-08 2007-01-18 Exxonmobil Chemical Patents Inc. Method for processing hydrocarbon pyrolysis effluent
WO2007083076A1 (en) * 2006-01-20 2007-07-26 Ineos Europe Limited Quench tube, apparatus and process for catalytic gas phase reactions
US20090030254A1 (en) * 2007-06-26 2009-01-29 Spicer David B Process and Apparatus for Cooling Liquid Bottoms from Vapor/Liquid Separator During Steam Cracking of Hydrocarbon Feedstocks
US20090056223A1 (en) * 2007-09-04 2009-03-05 Patel Sunilkant A Quench ring rim and methods for fabricating
WO2009033543A1 (de) * 2007-09-07 2009-03-19 Choren Industries Gmbh Verfahren und vorrichtung zur behandlung von beladenem heissgas
US20090074636A1 (en) * 2005-07-08 2009-03-19 Robert David Strack Method for Processing Hydrocarbon Pyrolysis Effluent
US20090085234A1 (en) * 2007-10-02 2009-04-02 Spicer David B Method And Apparatus For Cooling Pyrolysis Effluent
US20090301935A1 (en) * 2008-06-10 2009-12-10 Spicer David B Process and Apparatus for Cooling Liquid Bottoms from Vapor-Liquid Separator by Heat Exchange with Feedstock During Steam Cracking of Hydrocarbon Feedstocks
US7763162B2 (en) 2005-07-08 2010-07-27 Exxonmobil Chemical Patents Inc. Method for processing hydrocarbon pyrolysis effluent
US8118996B2 (en) 2007-03-09 2012-02-21 Exxonmobil Chemical Patents Inc. Apparatus and process for cracking hydrocarbonaceous feed utilizing a pre-quenching oil containing crackable components
US20140090296A1 (en) * 2012-09-28 2014-04-03 General Electric Company Apparatus for a syngas cooler and method of maintaining the same
WO2014210297A1 (en) 2013-06-28 2014-12-31 Uop Llc High temperature quench system and process
EP2870991A1 (en) * 2013-11-08 2015-05-13 Mat Plus Co., Ltd. Inlet for scrubber
KR20150054608A (ko) * 2013-11-08 2015-05-20 엠에이티플러스 주식회사 스크러버용 인렛
WO2016032730A1 (en) 2014-08-28 2016-03-03 Exxonmobil Chemical Patents Inc. Process and apparatus for decoking a hydrocarbon steam cracking furnace
EP2231817B1 (en) 2007-11-20 2016-08-17 Ensyn Renewables, Inc. Rapid thermal conversion with rapid quenching
US9828554B2 (en) 2014-08-28 2017-11-28 Exxonmobil Chemical Patent Inc. Process and apparatus for decoking a hydocarbon steam cracking furnace
US9896396B2 (en) 2015-11-04 2018-02-20 Exxonmobil Chemical Patents Inc. Process and system for making cyclopentadiene and/or dicyclopentadiene
US10160919B2 (en) 2015-09-21 2018-12-25 Exxonmobil Chemical Patents Inc. Process and apparatus for reducing thermal shock in a hydrocarbon steam cracking furnace
US10400176B2 (en) 2016-12-29 2019-09-03 Ensyn Renewables, Inc. Demetallization of liquid biomass
US10981101B2 (en) * 2016-06-09 2021-04-20 Giorgio Micheletti System for scrubbing or filtering a gas stream
US12098337B2 (en) 2021-09-30 2024-09-24 Exxonmobil Chemical Patents Inc. Conduits for cooling a hydrocarbon gas-containing stream and processes for using same

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SE380125B (zh) * 1974-12-02 1975-10-27 Ericsson Telefon Ab L M
DE2646691A1 (de) * 1976-10-15 1978-04-20 Linde Ag Verfahren und vorrichtung zur kuehlung von spaltgas
US6613127B1 (en) 2000-05-05 2003-09-02 Dow Global Technologies Inc. Quench apparatus and method for the reformation of organic materials

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US2353803A (en) * 1942-10-30 1944-07-18 L C Smith & Corona Typewriters Typewriting machine
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US2868856A (en) * 1955-06-21 1959-01-13 Union Carbide Corp Process and apparatus for partial oxidation of hydrocarbons
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Cited By (73)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3959420A (en) * 1972-05-23 1976-05-25 Stone & Webster Engineering Corporation Direct quench apparatus
US3907661A (en) * 1973-01-29 1975-09-23 Shell Oil Co Process and apparatus for quenching unstable gas
US4085034A (en) * 1975-10-14 1978-04-18 Kureha Kagaku Kogyo Kabushiki Kaisha Method for the thermal cracking of heavy hydrocarbon
US4147753A (en) * 1975-10-14 1979-04-03 Kureha Kagaku Kogyo Kabushiki Kaisha Apparatus for the thermal cracking of heavy hydrocarbon
US4322222A (en) * 1975-11-10 1982-03-30 Occidental Petroleum Corporation Process for the gasification of carbonaceous materials
US4121908A (en) * 1976-04-23 1978-10-24 Linde Aktiengesellschaft Apparatus for the cooling of a cracking-gas stream
US4087497A (en) * 1976-05-15 1978-05-02 Hoechst Aktiengesellschaft Cooling device
US4115072A (en) * 1977-04-07 1978-09-19 Chevron Research Company Retractable fluids spraying assembly
EP0066384A1 (en) * 1981-05-18 1982-12-08 Exxon Research And Engineering Company Method and apparatus for cooling a cracked gas stream
US4444697A (en) * 1981-05-18 1984-04-24 Exxon Research & Engineering Co. Method and apparatus for cooling a cracked gas stream
US4446003A (en) * 1981-06-02 1984-05-01 British Gas Corporation Heat recovery process and apparatus
US4597780A (en) * 1981-06-04 1986-07-01 Santek, Inc. Electro-inertial precipitator unit
US4558451A (en) * 1982-07-19 1985-12-10 The United States Of America As Represented By The Secretary Of The Air Force Tubular singlet delta oxygen generator
EP0122415A2 (de) * 1983-03-17 1984-10-24 Hoechst Aktiengesellschaft Abkühlungseinrichtung
US4552727A (en) * 1983-03-17 1985-11-12 Hoechst Aktiengesellschaft Cooling device
EP0122415A3 (en) * 1983-03-17 1987-08-12 Hoechst Aktiengesellschaft Cooling device cooling device
US4614229A (en) * 1983-06-20 1986-09-30 Exxon Research & Engineering Co. Method and apparatus for efficient recovery of heat from hot gases that tend to foul heat exchanger tubes
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NL163252C (nl) 1980-08-15
NL163252B (nl) 1980-03-17
GB1232940A (zh) 1971-05-26
DE1942001C3 (de) 1978-09-21
DE1942001B2 (de) 1978-02-16
ES371918A1 (es) 1972-03-16
DE1942001A1 (de) 1970-04-02
FR2022196A1 (zh) 1970-07-31
BE739454A (zh) 1970-03-02

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