US2941021A - Process and device for carrying out chemical reactions at high temperatures - Google Patents

Process and device for carrying out chemical reactions at high temperatures Download PDF

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Publication number
US2941021A
US2941021A US583567A US58356756A US2941021A US 2941021 A US2941021 A US 2941021A US 583567 A US583567 A US 583567A US 58356756 A US58356756 A US 58356756A US 2941021 A US2941021 A US 2941021A
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United States
Prior art keywords
combustion
gas
hydrocarbons
hydrogen
fuel
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Expired - Lifetime
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US583567A
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English (en)
Inventor
Krause Walter
Fischer Werner
Wirtz Rudolf
Schilken Hartmut
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Hoechst AG
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Hoechst AG
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    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C4/00—Preparation of hydrocarbons from hydrocarbons containing a larger number of carbon atoms
    • C07C4/02—Preparation of hydrocarbons from hydrocarbons containing a larger number of carbon atoms by cracking a single hydrocarbon or a mixture of individually defined hydrocarbons or a normally gaseous hydrocarbon fraction
    • C07C4/04—Thermal processes
    • 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
    • C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
    • C10G2400/20—C2-C4 olefins
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23B—METHODS OR APPARATUS FOR COMBUSTION USING ONLY SOLID FUEL
    • F23B2700/00—Combustion apparatus for solid fuel
    • F23B2700/01—Combustion apparatus for solid fuel adapted for boilers built up from sections
    • 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
    • Y02P30/00—Technologies relating to oil refining and petrochemical industry
    • Y02P30/40—Ethylene production
    • 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
    • Y10S585/949—Miscellaneous considerations
    • Y10S585/953—Pulsed, sonic, or plasma process
    • 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
    • Y10S585/949—Miscellaneous considerations
    • Y10S585/955—Specified mixing procedure

Definitions

  • the present invention relates to a process and to a device for carrying out chemical reactions at high temperatures.
  • the energy may be supplied indirectly by passing the gases to be cracked through outsideheated pipes or heat exchangers.
  • This method involves the disadvantage that the Walls of the pipes are superheated and thus give rise to pronounced formation of coke and soot.
  • the process referred to above is restricted to the use of small diameter pipes, since a pipe of greater size in diameter enables only too slow and incomplete a heat transfer from the walls to the gas.
  • the gases in the border zones become too hot contrary to the gases in the middle zones which become insufiiciently hot and, therefore, do not participate in the reaction.
  • regenerative furnaces heated with a gas mixture obtained by combustion of fuel with air; heating is then interrupted, the furnace is cleansed with an inert gas and then charged with the hydrocarbons to be cracked at the hot filling material of the furnaces. The furnace is again heated with heating gas after a minimum temperature has been reached. This operation is continually repeated by automatic commutation in intervals of some minutes. Detrimental to this process is, in addition to the complicated reversing automatic, the inevitable deposition of tarry substances in the regenerative furnace and the constantly changing temperature of the furnace which jeopardize economy and the yields obtained.
  • the energy required for cracking is supplied direct by subjecting part of the hydrocarbon to be cracked to a combustion process in a special combustion device with oxygen, whereby the hydrocarbon itself furnishes the energy for pyrolizing the hydrocarbon in excess.
  • This process is however not applicable when it is desired to prevent the hydrocarbon to be cracked from partial combustion.
  • a carrier gas for example hydrogen or combustion gases such as steam heated to a high temperature
  • combustion gases such as steam heated to a high temperature
  • combustion gas there may also be used all products obtained by combustion of any combustible substance.
  • the fuel and the oxidizing agent are often premixed in a separate mixing chamber before they are introduced into the combustion chamber proper for combustion.
  • the combustion devices which aresupplied with pre-mixed gases involve however the risk that the flame flashes back into the mixing chamber and destroys the. combustion device unless the gas supply lines are provided with very sensitive and in most cases technically complicated control devices which maintain constant pressure and velocity of flow of the mixture of oxygen and vaporized or gaseous fuel, such as hydrogen, as is the case with combustion devices used for the incomplete combustion of methane or earth gas with oxygen.
  • our present invention comprises a combustion chamber for performing any pyrolytic reaction; more particularly, our present invention relates to the production of acetylene and/ or ethylene and/ or higher olefinic hydrocarbons, wherein fuel and oxidizing agent are completely mixed only after the components have reached the flame so that just as short a flame is produced as in the case where the flame is produced by the supply of pre-mixed gases.
  • finely divided liquid, vaporized or gaseous fuel and at least one oxidizing gas are introduced separately into the combustion chamber at a velocity corresponding to a Mach-number of at least 0.8, preferably at sonic speed, via at least one tangential bore hole arranged in at least one plane in or opposite to the direction of rotation and then subjected to a combustion process.
  • one of the reactants may be introduced wholly or partially via radial bore holes.
  • combustion chamber as used in the process of this invention involves the particular advantage that the whole combustion process is performed Within the smallest space-as is the case of flames produced with premixed gasesso that the heat losses caused by dissipation are small in relation to the energy produced; contrary to the known devices, a combustion chamber as used herein prevents the flame from flashing back into the mixing chamber and requires no complicated control mechanism.
  • Mach-number used herein is to define the gas velocity applied in relation to the sonic speed at the corresponding temperature.
  • the operating procedure according to'this invention involves the further advantgae that the combustion gases leaving the combustion chamber at flame temperature possess such a high turbulence-due to their having been whirled in said chamberthat they are practically instantaneously mixed with the reactant to be pyrolized.
  • the heat is especially Well transferred from the combustion gas to the reactants, whereby it is possible to perform a practically complete reaction.
  • the reactant to be pyrolized can be introduced into the combustion chamber radially or tangentially either of the oxidizing agent and reversely.
  • the fuel and the oxidizing agent may, howevenalso be' introduced through proper-:bore rings.”
  • the secondary gas can be introduced into the combustion gas radially or tangentially and both" in and opposite to the direction of rotation.
  • finely dividedjform shall comprise fine atoririzationofliq'uid hydrocarbons and shall 'alsocomprise th e use of gaseous and vaporous hydrocarbons.
  • fuels there may also be'used hydrogen, carbon monoxide or water gas which contains an excess of hydrogen and/0r carbon monoxide. 'Insome cases it is advisable V to use commerciallhydrogeu.
  • Figure 1 is a schematic view in elevation
  • Figures Zand 3 are sections taken through section line AA and BB, respectively, of Figure 1.
  • a coolinguagent for example water
  • the hydrocarbons to be cracked are also introduced radiand below shall include the vapo-urized' state-either radi ally or tangentially or in any other knownmanner into thecurrent of combustion gases in order to be mixed action chamber, "for example the reaction tube, with ceramic material to suppress undesirable soot formation which is favored by metal surfaces.
  • the heat taken up by the cooling agent can be recovered and used for other purposes.
  • the knownihydrocarbons for example saturated or unsaturated hydrocarbons containing up to 30 or more carbon atoms. It is. particularly advantageous to employ saturated hydrocarbons, such as methane, ethane, propane, butane, pentane,- heptane, octane, decane dodecane, especially in the form of liquid commercial mixtures, such as petroleum distiilates or hydrocarbon oils, for example topped I iu shimmer oil, aswell as in :the form of technical gases such as earth gas.
  • saturated hydrocarbons such as methane, ethane, propane, butane, pentane,- heptane, octane, decane dodecane
  • liquid commercial mixtures such as petroleum distiilates or hydrocarbon oils, for example topped I iu shimmer oil, aswell as in :the form of technical gases such as earth gas.
  • aliphatic'saturated hydrocarbons'containing from 1 to about 30 or more carbon instead of
  • a process for the manufacture of C -C unsaturated hydrocarbons which comprises continuously forming a rotating stream of hot combustiongas in a a combustion zone by introducing an excess of atomized fuel and an oxidizing gas therefor separatelyand tangentially with a velocity corresponding to a Machnumberof at least 0.8 into the combustion zone, contacting said combustion gas with an atomized aliphatic hydrocarbon for pyrolysis-thereof, and chilling the effluent mixture of pyrolyzed hydrocarbon and combustion gas.
  • a process'for the manufacture of C -C unsaturated hydrocarbons which comprises coritinuouslyforming a rotating stream of hot combustion: gas in acombustion zone by introducing an excess 'of atomizedufuel' and an oxidizing gas therefor separately into the .C01I1-' bustion zone, at leastione of said reactants being'intro prised tangentially: with a velocity correspondingitoia Mach number of at least, 0.8, adding a secondary gas selected fromthe group consisting of steam, hydrogen and mixtures thereof to the rotating stream of hot combustion gas, contacting an atomized aliphatic hydrocarbon with the gas mixture thus obtained for pyrolysis of said hydrocarbon, and chilling the effiuent reacted mixture.
  • a process for the manufacture of a product selected from the group consisting of acetylene, ethylene and a mixture thereof which comprises continuously forming a rotating stream of hot combustion gas by introducing, separately and at about sonic speed, commercial oxygen and an excess of commercial hydrogen tangentially into a combustion zone; adding a secondary gas selected from the group consisting of steam, hydrogen and mixtures thereof to said rotating stream; thereafter introducing into the rota-ting stream an aliphatic hydrocarbon in gaseous form for pyrolysis therein; and chilling the reacted mixture.

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  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Physics & Mathematics (AREA)
  • Thermal Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
US583567A 1955-05-13 1956-05-08 Process and device for carrying out chemical reactions at high temperatures Expired - Lifetime US2941021A (en)

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
DEF17525A DE1040533B (de) 1955-05-13 1955-05-13 Verfahren und Vorrichtung zur Durchfuehrung chemischer Reaktionen bei hohen Temperaturen

Publications (1)

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US2941021A true US2941021A (en) 1960-06-14

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US583567A Expired - Lifetime US2941021A (en) 1955-05-13 1956-05-08 Process and device for carrying out chemical reactions at high temperatures

Country Status (5)

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US (1) US2941021A (ru)
BE (1) BE547808A (ru)
DE (1) DE1040533B (ru)
GB (1) GB834419A (ru)
NL (1) NL104369C (ru)

Cited By (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3055957A (en) * 1957-06-08 1962-09-25 Belge Produits Chimiques Sa Process and apparatus for production of unsaturated hydrocarbons
US3140323A (en) * 1958-05-21 1964-07-07 Montedison Spa Process for production of acetylene and other products by partial combustion of hydrocarbons
US3240836A (en) * 1960-06-21 1966-03-15 Hoechst Ag Process for cracking hydrocarbons
US3959401A (en) * 1973-05-14 1976-05-25 Union Carbide Corporation Process for cracking
US4832822A (en) * 1983-05-20 1989-05-23 Rhone-Poulenc Chimie De Base Steam cracking of hydrocarbons
US9815919B2 (en) 2011-01-19 2017-11-14 Exxonmobil Chemical Patents Inc. Hydrocarbon conversion process
US10570345B2 (en) * 2011-11-08 2020-02-25 Exxonmobil Chemical Patents Inc. Regenerative reactor system

Families Citing this family (15)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE1934304C3 (de) * 1969-07-07 1979-04-05 Basf Ag, 6700 Ludwigshafen Verfahren zur Gewinnung von Acetylen
US4256565A (en) * 1979-11-13 1981-03-17 Rockwell International Corporation Method of producing olefins from hydrocarbons
CN101486626B (zh) * 2009-02-19 2013-03-20 山东科技大学 一种气态烃制乙炔的工艺和设备
WO2012099677A2 (en) 2011-01-19 2012-07-26 Exxonmobil Chemical Patents Inc. Method and apparatus for converting hydrocarbons into olefins
US9708231B2 (en) 2011-01-19 2017-07-18 Exxonmobil Chemical Patents Inc. Method and apparatus for converting hydrocarbons into olefins using hydroprocessing and thermal pyrolysis
US9676681B2 (en) 2011-01-19 2017-06-13 Exxonmobil Chemical Patents Inc. Method and apparatus for managing hydrogen content through the conversion of hydrocarbons into olefins
US9505680B2 (en) 2011-01-19 2016-11-29 Exxonmobil Chemical Patents Inc. Method and apparatus for managing the conversion of hydrocarbons into olefins
EP2665690A2 (en) 2011-01-19 2013-11-27 ExxonMobil Chemical Patents Inc. Hydrocarbon conversion process
US9868680B2 (en) 2011-01-19 2018-01-16 Exxonmobil Chemical Patents Inc. Method and apparatus for converting hydrocarbons into olefins
WO2012099679A1 (en) 2011-01-19 2012-07-26 Exxonmobil Chemical Patents Inc. Method and apparatus for converting hydrocarbons into olefins
US9677014B2 (en) 2011-01-19 2017-06-13 Exxonmobil Chemical Patents Inc. Process and apparatus for converting hydrocarbons
US9815751B2 (en) 2011-01-19 2017-11-14 Exxonmobil Chemical Patents Inc. Hydrocarbon and oxygenate conversion by high severity pyrolysis to make acetylene and ethylene
WO2012099676A2 (en) 2011-01-19 2012-07-26 Exxonmobil Chemical Patents Inc. Process and apparatus for converting hydrocarbons
US9708232B2 (en) 2011-01-19 2017-07-18 Exxonmobil Chemical Patents Inc. Method and apparatus for converting hydrocarbons into olefins
WO2020086681A2 (en) 2018-10-23 2020-04-30 Sabic Global Technologies B.V. Method and reactor for conversion of hydrocarbons

Citations (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2343866A (en) * 1938-10-07 1944-03-14 Wulff Process Company Process for the pyrolysis of hydrocarbons
US2599981A (en) * 1949-12-22 1952-06-10 Columbian Carbon Carbon black
US2706210A (en) * 1950-12-05 1955-04-12 Wulff Process Company Process suitable for converting primary hydrocarbons to secondary hydrocarbons
US2750434A (en) * 1953-06-11 1956-06-12 Phillips Petroleum Co Conversion of hydrocarbons
US2767233A (en) * 1952-01-07 1956-10-16 Chemical Construction Corp Thermal transformation of hydrocarbons
US2813138A (en) * 1953-07-27 1957-11-12 Phillips Petroleum Co Production of unsaturated hydrocarbons and reactor therefor
US2816941A (en) * 1953-11-27 1957-12-17 Phillips Petroleum Co Production of unsaturated hydrocarbons and apparatus therefor
US2868856A (en) * 1955-06-21 1959-01-13 Union Carbide Corp Process and apparatus for partial oxidation of hydrocarbons

Family Cites Families (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2377245A (en) * 1943-12-03 1945-05-29 Phillips Petroleum Co Process for producing acetylene
GB709035A (en) * 1952-02-06 1954-05-12 Chemical Construction Corp Improvements relating to the production of pyrogenic chemical reactions

Patent Citations (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2343866A (en) * 1938-10-07 1944-03-14 Wulff Process Company Process for the pyrolysis of hydrocarbons
US2599981A (en) * 1949-12-22 1952-06-10 Columbian Carbon Carbon black
US2706210A (en) * 1950-12-05 1955-04-12 Wulff Process Company Process suitable for converting primary hydrocarbons to secondary hydrocarbons
US2767233A (en) * 1952-01-07 1956-10-16 Chemical Construction Corp Thermal transformation of hydrocarbons
US2750434A (en) * 1953-06-11 1956-06-12 Phillips Petroleum Co Conversion of hydrocarbons
US2813138A (en) * 1953-07-27 1957-11-12 Phillips Petroleum Co Production of unsaturated hydrocarbons and reactor therefor
US2816941A (en) * 1953-11-27 1957-12-17 Phillips Petroleum Co Production of unsaturated hydrocarbons and apparatus therefor
US2868856A (en) * 1955-06-21 1959-01-13 Union Carbide Corp Process and apparatus for partial oxidation of hydrocarbons

Cited By (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3055957A (en) * 1957-06-08 1962-09-25 Belge Produits Chimiques Sa Process and apparatus for production of unsaturated hydrocarbons
US3140323A (en) * 1958-05-21 1964-07-07 Montedison Spa Process for production of acetylene and other products by partial combustion of hydrocarbons
US3240836A (en) * 1960-06-21 1966-03-15 Hoechst Ag Process for cracking hydrocarbons
US3959401A (en) * 1973-05-14 1976-05-25 Union Carbide Corporation Process for cracking
US4832822A (en) * 1983-05-20 1989-05-23 Rhone-Poulenc Chimie De Base Steam cracking of hydrocarbons
US9815919B2 (en) 2011-01-19 2017-11-14 Exxonmobil Chemical Patents Inc. Hydrocarbon conversion process
US10570345B2 (en) * 2011-11-08 2020-02-25 Exxonmobil Chemical Patents Inc. Regenerative reactor system

Also Published As

Publication number Publication date
NL104369C (ru) 1900-01-01
GB834419A (en) 1960-05-11
DE1040533B (de) 1958-10-09
BE547808A (ru) 1900-01-01

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