US3542894A - Production of acetylene - Google Patents

Production of acetylene Download PDF

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US3542894A
US3542894A US715369A US3542894DA US3542894A US 3542894 A US3542894 A US 3542894A US 715369 A US715369 A US 715369A US 3542894D A US3542894D A US 3542894DA US 3542894 A US3542894 A US 3542894A
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oxygen
auxiliary
acetylene
mixture
burner block
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US715369A
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Ernst Bartholome
Hans Friz
Franz Neumayr
Martin Reichert
Ulrich Wagner
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BASF SE
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BASF SE
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Priority claimed from DE19671618125 external-priority patent/DE1618125A1/en
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    • CCHEMISTRY; METALLURGY
    • C07ORGANIC CHEMISTRY
    • C07CACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C11/00Aliphatic unsaturated hydrocarbons
    • C07C11/22Aliphatic unsaturated hydrocarbons containing carbon-to-carbon triple bonds
    • C07C11/24Acetylene
    • CCHEMISTRY; METALLURGY
    • C10PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10GCRACKING 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
    • C10G9/00Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
    • C10G9/34Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils by direct contact with inert preheated fluids, e.g. with molten metals or salts
    • C10G9/36Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils by direct contact with inert preheated fluids, e.g. with molten metals or salts with heated gases or vapours
    • C10G9/38Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils by direct contact with inert preheated fluids, e.g. with molten metals or salts with heated gases or vapours produced by partial combustion of the material to be cracked or by combustion of another hydrocarbon
    • YGENERAL 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
    • Y10TECHNICAL SUBJECTS COVERED BY FORMER USPC
    • Y10STECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10S585/00Chemistry of hydrocarbon compounds
    • Y10S585/919Apparatus considerations
    • Y10S585/921Apparatus considerations using recited apparatus structure
    • Y10S585/922Reactor fluid manipulating device
    • YGENERAL 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
    • Y10TECHNICAL SUBJECTS COVERED BY FORMER USPC
    • Y10STECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10S585/00Chemistry of hydrocarbon compounds
    • Y10S585/919Apparatus considerations
    • Y10S585/921Apparatus considerations using recited apparatus structure
    • Y10S585/922Reactor fluid manipulating device
    • Y10S585/923At reactor inlet
    • YGENERAL 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
    • Y10TECHNICAL SUBJECTS COVERED BY FORMER USPC
    • Y10STECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10S585/00Chemistry of hydrocarbon compounds
    • Y10S585/919Apparatus considerations
    • Y10S585/921Apparatus considerations using recited apparatus structure
    • Y10S585/924Reactor shape or disposition
    • YGENERAL 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
    • Y10TECHNICAL SUBJECTS COVERED BY FORMER USPC
    • Y10STECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10S585/00Chemistry of hydrocarbon compounds
    • Y10S585/949Miscellaneous considerations
    • Y10S585/95Prevention or removal of corrosion or solid deposits

Definitions

  • ABSTRACT OF THE DISCLOSURE A process for the production of acetylene by partial oxidation of hydrocarbons with oxygen, the flame formed in the oxidation being stabilized by auxiliary oxygen which is injected into the gas mixture at an angle of from more than 0 to 90 to the direction of flow of the gas mixture.
  • the acetylene yield is thus improved and the amount of soot formed is decreased.
  • the present invention relates to a process for the production of acetylene by partial oxidation of hydrocarbons with oxygen with the formation of a flame, this flame being stabilized by auxiliary oxygen which is injected into the gas mixture at an angle to the direction of flow thereof of from more than 0 to 90.
  • acetylene In the production of acetylene by partial oxidation of hydrocarbons (for example C to C hydrocarbon) with oxygen by prior art methods, the two components are heated separately to about 250 to 700 C. and then mixed with each other in a mixing unit. The mixture then flows through a burner block and is thereafter caused to react in the combustion chamber. This reaction is a flame re action which takes place within ,4 to A of a second at a temperature of about 1200 to 1600" C. of a flame. After the formation of acetylene has ended the temperature is lowered to about 50-300 C.
  • hydrocarbons for example C to C hydrocarbon
  • a liquid water or hydrocarbons, in particular fairly highboiling heat-resistant hydrocarbons such as naphthalene or substituted nahpthalenes
  • a liquid water or hydrocarbons, in particular fairly highboiling heat-resistant hydrocarbons such as naphthalene or substituted nahpthalenes
  • FIGS. 1 and 2 of the drawing which are respectively a section of a prior art acetylene burner and a plan view of the burner block as seen from the combustion chamber, show the characteristic features of a prior art acetylene burner such as is used in industrial plant.
  • the reaction mixture of hydrocarbon and oxygen which has been preheated flows through a diffuser A to the burner block B, which contains a number of parallel, preferably cylindrical channels C through which the gas mixture flows at a velocity which is greater than the velocity of the flame.
  • the gas mixture which contains 20 to 80% by volume of hydrocarbons and 80 to 20% by volume of oxygen, flows into a combustion chamber H which is bounded by the burner block B and a water-cooled jacket K.
  • Oxygen is injected at the front face of the burner block (at E, hereinafter called auxiliary outlet) through line D. It enters the combustion chamber H parallel to the direction of flow of the mixture.
  • oxygen is supplied through lines F in the jacket K perpendicular to the direc tion of flow on the mixture (at G, hereinafter called jacket outlets).
  • auxiliary oxygen The oxygen passed through D and F (hereinafter called auxiliary oxygen) is ignited in this combustible gas and burns at auxiliary outlets E and jacket outlets G, forming small flames.
  • the amount of oxygen required for the reaction is mixed with the hydrocarbon, the auxiliary oxygen flames igniting the mixture in the reaction chamber and stabilizing the reaction flame during continuous operation.
  • the ratio of the oxygen issuing from the auxiliary outlets to the oxygen contained in the gas mixture issuing from the channels is in general from 1:1000 to 1:10.
  • Another object if the invention is to decrease the soot content in the gas obtained.
  • auxiliary oxygen issuing from the burner block so that it forms an angle of considerably more than 0, for example 20, and not more than 90, preferably from 60 to with the direction of the gases issuing from the burner block.
  • the auxiliary oxygen is supplied through the auxiliary outlets not parallel to the stream of the reaction mixture, but at an angle at E, as shown in FIG. 3.
  • the angle a at which the auxiliary oxygen impinges on the reaction mixture may be varied within wide limits of from more than 0 to not more than preferably from 20 to 90 and particularly from 60 to 80", without the stabilization of the reaction flame being impaired.
  • auxiliary oxygen flames it is advantageous for one or more auxiliary oxygen flames to be pointed toward each channel in the burner block. It has been found to be expedient to arrange the auxiliary outlets between the channels in such a Way that three flames issue from each auxiliary outlet into the combustion chamber and either one, two or three auxiliary flames are pointed toward each channel.
  • FIG. 4 of the accompanying drawing shows one of these arrangements in which the auxiliary outlets and the channels form a hexagonal pattern in the cross-section of the burner block and in which three auxiliary flames are pointed toward one flame issuing from the channels except some of those channels situated next to the jacket and toward which only two auxiliary flames are pointed.
  • the result of the process according to the invention is that a gas is obtained having both a higher acetylene content and a lower soot content than has been possible in the prior art methods using the same hydrocarbon mixture.
  • naphtha specific gravity 0.69, boiling point range 34 to 124 C., vapor density 4.0 kg./m. at STP.
  • the water-cooled burner block contains nineteen channels C each having a diameter of 19 mm. They are arranged in a. hexagonal pattern whose parallel outer boundary lines K are spaced apart by a distance of 165 mm.
  • the mixture is ignited in the reaction chamber H (FIG. 3) which is bounded by the burner and the water-cooled combustion chamber K having a length of 250 mm.
  • Another 4 in. per hour (STP.) of oxygen is introduced through line F and auxiliary outlets G.
  • the mixture is quenched to 80 C. by injecting water.
  • the yield is 134 kg./h. of C H with a specific naphtha consumption of 3.95 kg. per kg. of C H a specific oxygen consumption of 4.07 kg. per kg. of C H and a specific oxygen consumption of 4.07 kg. per kg. of C H and a specific soot formation of 0.11 kg. per kg. of CgHg.
  • the same reaction is carried out in a prior art burner block having identical dimensions to those of the above block.
  • the auxiliary oxygen is introduced into the reaction chamber H at E parallel to the stream of reaction mixture (::0) as shown in FIG. 1.
  • 400 kg. of naphtha of the abovementioned type and 268 m. (STP.) of oxygen are reacted per hour; at a higher load, the reaction flame becomes unstable and some unreacted oxygen is found in the quenched acetylene-containing gas.
  • 6 m. (STP.) per hour of auxiliary oxygen is supplied at each of the outlets E and G.
  • the other operating data are the same as described above.
  • a process for the production of acetylene by partial oxidation of hydrocarbons with oxygen wherein the gaseous or vaporous components are separately preheated and then mixed, the mixture is passed through channels in a burner block to a combustion chamber and the flame in said combustion chamber as stabilized by auxiliary flames which are fed with auxiliary oxygen which issues from said burner block at an angle of 20 to 90 to the direction of said mixture issuing from said burner block.
  • a process as claimed in claim 2 wherein the angle between the emerging auxiliary oxygen and the emerging mixture is from to 5.
  • a process as claimed in claim 1 wherein the angle between the emerging auxiliary oxygen and the emerging mixture is from 60 to 80.

Description

NOV. 24, 1970 BARTHOLOME ETAL 3,542,894
. PRODUCTION OF ACETYLENE Filed March 22, 1968 z Sheets-Sheet 1 FIG. 2
PRIOR ART u. INVENTORS:
Q ERNST BARTHOLOME HANS FRIZ FRANZ NEU R MARTIN REI RT FIG. I
PRIOR ART ULRICH WAGNER ATT'YS Nov. 24, 1970' E. BARTHOLOME ETAL 3,542,894
PRODUCTION OF ACETYLENE Filed March 22, 1968 i z Sheets-Sheet 2 v o 4 c: mvemohs:
ERNST BARTHOLOME RIZ FIG. 3'
. HANS F FRANZ NEUMAYR TIN REIC T. RICH WAG ATT'YS United States Patent 3,542,894 PRODUCTION OF ACETYLENE Ernst Bartholome, Heidelberg, Hans Friz and Franz Neumayr, Ludwigshafen (Rhine), Martin Reichert, Frankenthal, Pfalz, and Ulrich Wagner, Limburgerhof, Pfalz, Germany, assignors to Badische Anilin- & Soda-Fabrik Aktiengesellschaft, Ludwigshafen (Rhine), Germany Filed Mar. 22, 1968, Ser. No. 715,369 Claims priority, application Germany, Mar. 25, 1967, 1,618,125 Int. Cl. C07c 11/24 US. Cl. 260-679 Claims ABSTRACT OF THE DISCLOSURE A process for the production of acetylene by partial oxidation of hydrocarbons with oxygen, the flame formed in the oxidation being stabilized by auxiliary oxygen which is injected into the gas mixture at an angle of from more than 0 to 90 to the direction of flow of the gas mixture. The acetylene yield is thus improved and the amount of soot formed is decreased.
The present invention relates to a process for the production of acetylene by partial oxidation of hydrocarbons with oxygen with the formation of a flame, this flame being stabilized by auxiliary oxygen which is injected into the gas mixture at an angle to the direction of flow thereof of from more than 0 to 90.
In the production of acetylene by partial oxidation of hydrocarbons (for example C to C hydrocarbon) with oxygen by prior art methods, the two components are heated separately to about 250 to 700 C. and then mixed with each other in a mixing unit. The mixture then flows through a burner block and is thereafter caused to react in the combustion chamber. This reaction is a flame re action which takes place within ,4 to A of a second at a temperature of about 1200 to 1600" C. of a flame. After the formation of acetylene has ended the temperature is lowered to about 50-300 C. as rapidly as possible (within about to 7 of a second) by injecting a liquid (water or hydrocarbons, in particular fairly highboiling heat-resistant hydrocarbons such as naphthalene or substituted nahpthalenes) into the current of gas in order to prevent decomposition of the acetylene formed.
FIGS. 1 and 2 of the drawing, which are respectively a section of a prior art acetylene burner and a plan view of the burner block as seen from the combustion chamber, show the characteristic features of a prior art acetylene burner such as is used in industrial plant. The reaction mixture of hydrocarbon and oxygen, which has been preheated flows through a diffuser A to the burner block B, which contains a number of parallel, preferably cylindrical channels C through which the gas mixture flows at a velocity which is greater than the velocity of the flame.
The gas mixture, which contains 20 to 80% by volume of hydrocarbons and 80 to 20% by volume of oxygen, flows into a combustion chamber H which is bounded by the burner block B and a water-cooled jacket K. Oxygen is injected at the front face of the burner block (at E, hereinafter called auxiliary outlet) through line D. It enters the combustion chamber H parallel to the direction of flow of the mixture. In addition, oxygen is supplied through lines F in the jacket K perpendicular to the direc tion of flow on the mixture (at G, hereinafter called jacket outlets). When the burner is started up, hydrocarbon is at first supplied by itself through the diffuser to the burner block B, through the channels C into the combustion chamber H.
ice
The oxygen passed through D and F (hereinafter called auxiliary oxygen) is ignited in this combustible gas and burns at auxiliary outlets E and jacket outlets G, forming small flames. After the auxiliary oxygen has been ignited, the amount of oxygen required for the reaction is mixed with the hydrocarbon, the auxiliary oxygen flames igniting the mixture in the reaction chamber and stabilizing the reaction flame during continuous operation. During continuous operation the ratio of the oxygen issuing from the auxiliary outlets to the oxygen contained in the gas mixture issuing from the channels is in general from 1:1000 to 1:10.
It has become evident that this type of stabilization of the reaction flame has disadvantages, particularly in the case of flames formed by partial oxidation of vaporized liquid hydrocarbons, for example those having 5 to 10 carbon atoms. The flame is stabilized at very diflerent distances from the burner block. Flames of this type are unfavorable because they result in differences in residence times of the hot acetylene in the combustion chamber and consequently in diminished production of acetylene and increased formation of soot.
It is an object of this invention to provide a process for the production of acetylene in such a way that the content of acetylene in the reacted gas is increased.
Another object if the invention is to decrease the soot content in the gas obtained.
These and other objects of the invention are achieved by directing the auxiliary oxygen issuing from the burner block so that it forms an angle of considerably more than 0, for example 20, and not more than 90, preferably from 60 to with the direction of the gases issuing from the burner block. Thus the auxiliary oxygen is supplied through the auxiliary outlets not parallel to the stream of the reaction mixture, but at an angle at E, as shown in FIG. 3. The angle a at which the auxiliary oxygen impinges on the reaction mixture may be varied within wide limits of from more than 0 to not more than preferably from 20 to 90 and particularly from 60 to 80", without the stabilization of the reaction flame being impaired.
It is advantageous for one or more auxiliary oxygen flames to be pointed toward each channel in the burner block. It has been found to be expedient to arrange the auxiliary outlets between the channels in such a Way that three flames issue from each auxiliary outlet into the combustion chamber and either one, two or three auxiliary flames are pointed toward each channel. FIG. 4 of the accompanying drawing shows one of these arrangements in which the auxiliary outlets and the channels form a hexagonal pattern in the cross-section of the burner block and in which three auxiliary flames are pointed toward one flame issuing from the channels except some of those channels situated next to the jacket and toward which only two auxiliary flames are pointed.
The result of the process according to the invention is that a gas is obtained having both a higher acetylene content and a lower soot content than has been possible in the prior art methods using the same hydrocarbon mixture.
It has also been found that a prior art burner block can be subjected to much greater loads in the process according to this invention than in the prior art methods.
The process according to this invention is illustrated by the following example.
EXAMPLE 530 kg. of naphtha (specific gravity 0.69, boiling point range 34 to 124 C., vapor density 4.0 kg./m. at STP.) per hour is vaporized in a preheater and heated to 320 C. The naphtha vapor is mixed in a mixing unit with 380 m.
(STP.) of oxygen which has also been heated to 320 C. in a separate preheater, and then passed through the diffuser of an apparatus according to the invention to the burner block. Prior to entering the burner block, the mixture has a temperature of 280 C. The water-cooled burner block (FIG. 4) contains nineteen channels C each having a diameter of 19 mm. They are arranged in a. hexagonal pattern whose parallel outer boundary lines K are spaced apart by a distance of 165 mm.
The mixture is ignited in the reaction chamber H (FIG. 3) which is bounded by the burner and the water-cooled combustion chamber K having a length of 250 mm. The auxiliary oxygen (4 m. per hour at STP.) is supplied through line D and auxiliary outlets E to the reaction mixture at an angle oc=60. Another 4 in. per hour (STP.) of oxygen is introduced through line F and auxiliary outlets G. After reaction has taken place, the mixture is quenched to 80 C. by injecting water.
1156 m. per hour at STP. of dry cracked gas is obtained having the following composition:
Percent by volume and 13 g./m. (STP.) of soot.
From this it can be calculated that the yield is 134 kg./h. of C H with a specific naphtha consumption of 3.95 kg. per kg. of C H a specific oxygen consumption of 4.07 kg. per kg. of C H and a specific oxygen consumption of 4.07 kg. per kg. of C H and a specific soot formation of 0.11 kg. per kg. of CgHg.
For comparison, the same reaction is carried out in a prior art burner block having identical dimensions to those of the above block. In this case, however, the auxiliary oxygen is introduced into the reaction chamber H at E parallel to the stream of reaction mixture (::0) as shown in FIG. 1. In this arrangement, 400 kg. of naphtha of the abovementioned type and 268 m. (STP.) of oxygen are reacted per hour; at a higher load, the reaction flame becomes unstable and some unreacted oxygen is found in the quenched acetylene-containing gas. 6 m. (STP.) per hour of auxiliary oxygen is supplied at each of the outlets E and G. The other operating data are the same as described above.
When using this method, 870 m. (STP.) per hour of dry cracked gas is obtained having the following composition:
Percent by volume and 19.4 g./m. (STP.) of soot. From this it can be cal- 4 culated that the yield of C H is 82.5 kg. per hour of acetylene with a specific naphtha consumption of 4.04 kg. per kg. of C H a specific oxygen consumption of 4.10 kg. per kg. of C H and a specific soot formation of 0.17 kg. per kg. of C H We claim:
1. A process for the production of acetylene by partial oxidation of hydrocarbons with oxygen wherein the gaseous or vaporous components are separately preheated and then mixed, the mixture is passed through channels in a burner block to a combustion chamber and the flame in said combustion chamber as stabilized by auxiliary flames which are fed with auxiliary oxygen which issues from said burner block at an angle of 20 to 90 to the direction of said mixture issuing from said burner block.
2. In a process for the production of acetylene by partial oxidation of gaseous or vaporous hydrocarbons with oxygen wherein the gaseous or vaporous components are separately preheated to a temperature ranging from 250 to 700 C. and then mixed, the mixture containing 20 to 80% by volume of hydrocarbons and 80 to 20% by volume of oxygen is passed through a plurality of parallel channels in a burner block to a combustion chamber where the partial oxidation takes place at a temperature ranging from 1200 to 1600 C., the gas mixture then being quenched rapidly by injection of water or hydrocarbon to temperatures of from 50 to 300 C., and wherein the flame in said combustion chamber is stabilized with auxiliary flames by feeding auxiliary oxygen through auxiliary outlet-s, the molar ratio of said auxiliary oxygen to the oxygen contained in said gas mixture being 1:1000 to 1:10, the improvement which comprises providing means at said auxiliary outlets which cause the auxiliary oxygen to issue at an angle of 20 to 90 to the direction of said mixture issuing from said channels of said burner block.
3. A process as claimed in claim 1 wherein one or more than one auxiliary oxygen flame is provided for each channel in the burner block.
4. A process as claimed in claim 2 wherein the angle between the emerging auxiliary oxygen and the emerging mixture is from to 5. A process as claimed in claim 1 wherein the angle between the emerging auxiliary oxygen and the emerging mixture is from 60 to 80.
References Cited UNITED STATES PATENTS 3,438,741 4/1969 Boyd et al 23277 3,121,616 2/1964 Braconier et a1. 23277 2,998,464 8/1961 Burleson et al. 260679 DELBERT E. GANTZ, Primary Examiner I. M. NELSON, Assistant Examiner US. Cl. X.R. 23-277; 260683
US715369A 1967-03-25 1968-03-22 Production of acetylene Expired - Lifetime US3542894A (en)

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Cited By (12)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4570028A (en) * 1984-04-06 1986-02-11 Atlantic Richfield Company Process for producing acetylene using a homogeneous mixture
US4952743A (en) * 1987-12-03 1990-08-28 Gaz De France Process and apparatus for the conversion of hydrocarbons
US5886056A (en) * 1997-04-25 1999-03-23 Exxon Research And Engineering Company Rapid injection process and apparatus for producing synthesis gas (law 560)
US5935489A (en) * 1997-04-25 1999-08-10 Exxon Research And Engineering Co. Distributed injection process and apparatus for producing synthesis gas
US5980596A (en) * 1997-04-25 1999-11-09 Exxon Research And Engineering Co. Multi-injector autothermal reforming process and apparatus for producing synthesis gas (law 565).
US5980782A (en) * 1997-04-25 1999-11-09 Exxon Research And Engineering Co. Face-mixing fluid bed process and apparatus for producing synthesis gas
US6267912B1 (en) 1997-04-25 2001-07-31 Exxon Research And Engineering Co. Distributed injection catalytic partial oxidation process and apparatus for producing synthesis gas
EP1182181A1 (en) * 2000-08-25 2002-02-27 Basf Aktiengesellschaft Premix burner block for partial oxidation processes
EP1462162A2 (en) * 2003-03-26 2004-09-29 Basf Aktiengesellschaft Process to scale-up a reactor to obtain a high-temperature reaction, reactor and use
EP1462160A2 (en) * 2003-03-26 2004-09-29 Basf Aktiengesellschaft Process to obtain a high-temperature rection, reactor for the implementation of this process, process to scale-up a reactor and use thereof
US20060201065A1 (en) * 2005-03-09 2006-09-14 Conocophillips Company Compact mixer for the mixing of gaseous hydrocarbon and gaseous oxidants
CN105473217A (en) * 2013-08-29 2016-04-06 巴斯夫欧洲公司 Device and method for producing acetylenes and synthesis gas

Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2998464A (en) * 1957-08-05 1961-08-29 Monsanto Chemicals Quench system
US3121616A (en) * 1958-04-08 1964-02-18 Belge Produits Chimiques Sa Solid metal block reaction furnace for treatment of hydrocarbons
US3438741A (en) * 1966-08-25 1969-04-15 Monsanto Co Apparatus for flame reaction of hydrocarbons

Patent Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2998464A (en) * 1957-08-05 1961-08-29 Monsanto Chemicals Quench system
US3121616A (en) * 1958-04-08 1964-02-18 Belge Produits Chimiques Sa Solid metal block reaction furnace for treatment of hydrocarbons
US3438741A (en) * 1966-08-25 1969-04-15 Monsanto Co Apparatus for flame reaction of hydrocarbons

Cited By (16)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4570028A (en) * 1984-04-06 1986-02-11 Atlantic Richfield Company Process for producing acetylene using a homogeneous mixture
US4952743A (en) * 1987-12-03 1990-08-28 Gaz De France Process and apparatus for the conversion of hydrocarbons
US5886056A (en) * 1997-04-25 1999-03-23 Exxon Research And Engineering Company Rapid injection process and apparatus for producing synthesis gas (law 560)
US5935489A (en) * 1997-04-25 1999-08-10 Exxon Research And Engineering Co. Distributed injection process and apparatus for producing synthesis gas
US5980596A (en) * 1997-04-25 1999-11-09 Exxon Research And Engineering Co. Multi-injector autothermal reforming process and apparatus for producing synthesis gas (law 565).
US5980782A (en) * 1997-04-25 1999-11-09 Exxon Research And Engineering Co. Face-mixing fluid bed process and apparatus for producing synthesis gas
US6267912B1 (en) 1997-04-25 2001-07-31 Exxon Research And Engineering Co. Distributed injection catalytic partial oxidation process and apparatus for producing synthesis gas
EP1182181A1 (en) * 2000-08-25 2002-02-27 Basf Aktiengesellschaft Premix burner block for partial oxidation processes
EP1462162A2 (en) * 2003-03-26 2004-09-29 Basf Aktiengesellschaft Process to scale-up a reactor to obtain a high-temperature reaction, reactor and use
EP1462160A2 (en) * 2003-03-26 2004-09-29 Basf Aktiengesellschaft Process to obtain a high-temperature rection, reactor for the implementation of this process, process to scale-up a reactor and use thereof
EP1462160A3 (en) * 2003-03-26 2004-11-03 Basf Aktiengesellschaft Process to obtain a high-temperature rection, reactor for the implementation of this process, process to scale-up a reactor and use thereof
EP1462162A3 (en) * 2003-03-26 2004-11-03 Basf Aktiengesellschaft Process to scale-up a reactor to obtain a high-temperature reaction, reactor and use
US20060201065A1 (en) * 2005-03-09 2006-09-14 Conocophillips Company Compact mixer for the mixing of gaseous hydrocarbon and gaseous oxidants
US7416571B2 (en) 2005-03-09 2008-08-26 Conocophillips Company Compact mixer for the mixing of gaseous hydrocarbon and gaseous oxidants
CN105473217A (en) * 2013-08-29 2016-04-06 巴斯夫欧洲公司 Device and method for producing acetylenes and synthesis gas
CN105473217B (en) * 2013-08-29 2018-01-30 巴斯夫欧洲公司 Apparatus and method for preparing acetylene and synthesis gas

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