US3287434A - Process for the partial combustion of hydrocarbons to produce acetylene - Google Patents

Process for the partial combustion of hydrocarbons to produce acetylene Download PDF

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Publication number
US3287434A
US3287434A US311158A US31115863A US3287434A US 3287434 A US3287434 A US 3287434A US 311158 A US311158 A US 311158A US 31115863 A US31115863 A US 31115863A US 3287434 A US3287434 A US 3287434A
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United States
Prior art keywords
burner block
gas mixture
acetylene
gas
temperature
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Expired - Lifetime
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US311158A
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English (en)
Inventor
Walter H Stanton
Jr George O Hunt
Walter B Howard
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Monsanto Co
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Monsanto Co
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Publication date
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Priority to US311158A priority Critical patent/US3287434A/en
Priority to DE19641468356 priority patent/DE1468356A1/de
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Expired - Lifetime legal-status Critical Current

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    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C2/00—Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms
    • C07C2/76—Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms by condensation of hydrocarbons with partial elimination of hydrogen
    • C07C2/78—Processes with partial combustion
    • 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
    • Y10S585/909—Heat considerations
    • Y10S585/911—Heat considerations introducing, maintaining, or removing heat by atypical procedure
    • Y10S585/913—Electric
    • 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
    • Y10S585/922—Reactor fluid manipulating device
    • Y10S585/923—At reactor inlet

Definitions

  • the present invention is related to the production of acetylene by the partial combustion of methane. More particularly, it is concerned with a method and apparatus for preheating a paraflinic hydrocarbon and an oxygencontaining gaseous mixture from about 600 C. to a temperature up to about 1150" C. without preignition of the hydrocarbon.
  • acetylene by the reaction between methane and insufficient quantities of oxygen or air is well known.
  • acetylene may be produced by conducting the combustion process at a temperature of from about 1200 to about 1800 C. The process is usually carried out at essentially atmospheric conditions. After combustion of part of the methane and the oxygen to produce a high temperature, the excess methane is cracked to acetylene and immediately thereafter the reaction products are quenched with a cooling liquid, generally a water spray. This quenching is necessary to limit the reaction time and minimize decomposition of the hydrocarbon products to facilitate the recovery of acetylene and to eliminate the production of carbon and hydrogen.
  • the apparatus comprises an inlet or mixing chamber separated by a perforated or porous plate from the reaction chamber where a portion of the hydrocarbon reactant is burned to provide the heat for effecting the conversion of the remainder of the hydrocarbon reactant into acetylene.
  • the perforated or porous plate is commonly called a burner block and creates a gas velocity which is greater than the rate of flame propagation and thereby prevents the flame in the reaction chamber from flashing back into the inlet chamber and igniting the hydrocarbon being supplied to the reaction chamber.
  • oxygen and a methane gas for instance, natural gas
  • a methane gas for instance, natural gas
  • the mixed gas velocity through the burner block is in excess of the rate of flame propagation thus preventing flashbacks into the diffuser. Partial combustion of the methane and oxygen and cracking of the excess methane follows and the reaction products are quenched by direct contact with a water spray to limit the total reaction time to less than 0.1 second.
  • Preheating the reactants has a beneficial effect on the acetylene yield, the quantity of acetylene in the cracked efi'luent gas increasing as the preheat temperature is increased. In addition to the increased concentration of acetylene in the effluent gas, the oxygen requirements are also reduced.
  • preheating of the react-ants to temperatures higher than approximately 600 to 700 C. has been difficult in commercial operations because of the likelihood of preignition of the reactants before introduction into the reaction chamber.
  • Another object of this invention is to provide an improved burner block means to permit a preheated mixture of hydrocarbon and an oxygen-containing gas to be introduced into a combustion or reaction zone without the occurrence of either preignition or flashback.
  • preheating of a gas mixture containing paraffinic hydrocarbon and an oxygen-containing gas is accomplished in the burner block through which the preheated mixture is introduced into the reaction chamber for conversion into acetylene.
  • the burner block is provided with at least one passage having a heating element arranged therein for heating the gas mixture to a temperature in the range of 800 to 1150" C.
  • the passage in the burner block is of a size to provide a gas velocity which is greater than the rate of flame propagation of the gas mixture, thereby flashback of the flame is prevented.
  • the rate of heat transfer is suflicient that the desired temperature of the high velocity gases is reached and the preheated gas mixture injected into the reaction chamber before the end of the flame induction period; that is, before ignition commences.
  • FIGURE 1 is a cut-away view of an ordinary acetylene converter showing the burner block of this invention containing an electric heating element.
  • FIGURE 2 is a plan view of the inlet end of a burner block which is show-n in section in FIGURE 1, showing the physical arrangement of the passage and electric heating element disposed therein.
  • a gaseous mixture at about 600 C. consisting of oxygen and natural gas enters the acetylene converter through line 10 and burner block 11.
  • the acetylene converter comprises a cylindrical metal shell 12 containing inner liner 13 which encloses combustion chamber 14. Liner 13 is separated from metallic shell 12 by annular space 15 through which a cooling fluid is circulated via lines 16 and 17 to maintain liner 13 at a moderate temperature.
  • a cooling fluid is circulated via lines 16 and 17 to maintain liner 13 at a moderate temperature.
  • Burner block 11 is constructed of solid material and is provided with a passage 20 for the flow of gas mixture into reaction chamber 14. Electrical heating element 21 is arranged within passage 20 and heated by the application of an electric current from electric source 22 via electrical conductors 23 and 24 to a maximum temperature in the range of 1100 to 1250 C. Multiple passages may be used if desired.
  • burner block 11 is made from a solid'non-metallic refractory material, for instance aluminum oxide, with U-shape passage 20 therethrough.
  • Electric heating element 21 is arranged within passage 20 and electrically connected through electrical conductors 2 3 and 24 to a source of electrical energy.
  • Electric heating element 21 may be designed in any of several ways to provide the maximum amount of heat transfer area and still permit uniform gas velocities across the cross-section of gas flow. As shown, heating element 21 is a crimped surface with a crimped distance d in the order of 0.1 to 0.25 inch.
  • Example I An electric heating element constructed of Hastelloy X was designed to provide 8.95 square feet of heat transfer area in an acetylene burner block 4 inches in diameter and 12 inches long.
  • the heating element was crimped, as shown in FIGURE 2, with a crimping distance of 0.12 inch.
  • the thickness of the metal was 0.02 inch.
  • the passage or opening in the burner block was U-shaped and had a cross-sectional area which comprised 17.4 percent of the total cross-sectional area of the burner block.
  • Methane and oxygen at a flow rate of 8.33 moles per hour and 4.33 moles per hour, respectively, and a temperature of 600 C. were introduced into the burner block. Electricity at a rate of 892 amps and 22.9 volts heated the heating element to a temperature of 1150 C.
  • Example 11 An electric heating element constructed of Hastelloy X was designed to provide 11.0 square feet of heat trans fer area in an acetylene burner block 4 inches in diameter and 12 inches long.
  • the heating element was crimped, as shown in FIGURE 2, with crimping distance of 0.10 inch.
  • the thickness of the metal was 0.012 inch.
  • the passage or opening in the burner block was U shaped and had a cross-sectional area which comprised 23.8 percent of the total cross-sectional area of the burner block.
  • Methane and oxygen at a flow rate of 8.60 moles per hour and 4.33 moles per hour, respectively, and a temperature of 600 C. were introduced into the burner block. Electricity at a rate of 1440 amps and 36 volts heated the heating element to a temperature at the exit of 1210 C.
  • the percent acetylene in the cracked gas leaving the acetylene converter was 11.1 mole percent on a Water-free basis.
  • Example 111 Methane and oxygen at a flow rate of 7.15 moles per hour and 4.33 moles per hour, respectively, were introduced at a temperature of 600 C. into the acetylene converter of Examples I and II without benefit of preheating in the burner block. After partial combustion and cracking of the methane followed by quenching of the reaction, the eflluent gas leaving the acetylene converter had an acetylene content of 8.75 mole percent on a water-free basis.
  • the electric heating element used in this invention must be one which has reasonable strength at temperatures up to about 1250 C., can withstand the atmosphere to which it is exposed at high temperatures and has favorable electrical resistance.
  • Such metals as Hastelloy X (about 45% nickel, 2.5% cobalt, 23% chrome, 10% molybdenum, 20% iron, 1% tungsten, 15% carbon), Kanthal Al (about 5% aluminum, 22% chrome, ,6 cobalt, and the remainder iron), Chromel A nickel, 20% chrome), and Nichrome V (about 80% nickel, 20% chrome) are materials which can be used.
  • the heating element In obtaining a maximum temperature of up to 1150" C. in the gas discharged from the burner block, it is desirable to maintain the heating element at a minimum temperature and to provide the heating element with a maximum heat transfer area. Also, gas temperatures in this range necessitate that the temperature of the heating element be within the range of 1100 C. to about 1250 C. The heat transfer area is dependent upon the rate of gas flow, desired exit gas temperature, inlet feed gas temperature, length of the heating element, and thickness of the heating element material.
  • the thickness of the heating element shown in FIG- URES l and 2 is at least 5 mils and not more than about 50 mils.
  • the crimp distance d is preferably in the range of from 50 to 250 mils for economy of operation and maximum heat transfer. It will .be noted in the examples that sufficient heat transfer area is provided to obtain a heat flux, Btu/hour per square foot of area, in the range of from about 10,000 to about 25,000.
  • the pressure drop through the burner block must not be excessive, the velocity of the mixed gas must be greater than the rate of flame propagation to prevent flashbacks, the flow of gas through the burner block must be at uniform velocity throughout the transverse, cross-sectional area and the residence time of the gas in the burner block must be less than the time required for a suflicient concentration of flame initiators to form for combustion to take place.
  • the pressure drop through the burner block is preferably limited to less than about 20 p.s.i. in order to avoid excessive cost for compression of the feed gases. Ordinarily, the pressure drop is less than about 5 p.s.i.
  • the residence time of the gases in the burner block should be less than about 10 milliseconds when preheating a gas mixture from about 600 C. to about 1150 C., although it is preferred to limit the residence time to about 5 milliseconds.
  • the residence time may be as high as 200 milliseconds without flames developing, but preferably the residence time is limited to about 10 milliseconds. Unless the heated gas is discharged into,
  • the velocity of the mixed gas through the burner block must be greater than the rate of flame propagaton of the gas mixture and, ordinarily, must be at least 300 feet per second at an exit temperature of from 1000 C. to 1150 C. and preferably about 400 to 500 feet per second. At a temperature of 800 C., the velocity may be as low as 200 feet per second.
  • the flow of gas through the burner block must be of a substantially uniform velocity. If the gas flows at a lower velocity in one area than in another area, the lower velocity may not be sufficiently greater than the rate of flame propagation and flashback of the flame would occur. Also, the lower-velocity gas would be heated to a higher temperature, thereby reducing the flame induction period and causing preignition of the gas mixture.
  • Another important factor in the burner block of this invention is the relation between the cross-sectional area of the passage or opening through the burner block and the total cross-sectional area of the burner block.
  • Sufficient closed area is necessary to permit eddy currents to form downstream from the block and develop a stable flame front at the exit from the burner block.
  • the open area necessary to achieve this condition is ordinarily from about 15 to 30% of the total cross-sectional area of the burner block.
  • the burner block may be constructed from any convenient nonmetallic refractory material capable of withstanding temperatures of 1250 C. Such materials as aluminum oxide, alumina-silica ceramics, alumina foam and silicon carbide foam are satisfactory for this purpose. Preferably, the material is substantially non-porous in nature.
  • the surface in direct contact with the heating element should be pure aluminum oxide.
  • the electrical resistance of the heating element ordinarily must be at least about 50 microh-m-inches at temperatures of 1000 C. to 1150 C. in order to develop suflicient wattage input in amperages of 1000 to 2000 amps.
  • the heating element may be constructed in various configurations and one configuration has been exemplified in the examples and shown in FIGURE 2. This corrugated design is advantageous because current flows through the entire heater element so that an exceedingly long length can be employed in order to obtain the total resistance desired. Generally, the heating element must be so designed for maximum total resistance so that the amperage required is not excessive. Amperage requirements above 5000 amperes would result in unreasonably large electric leads. A preferred range of electric current is from 1000 to 2000 amperes.
  • the heating element has a temperature variation of from about 600 C. at the inlet end to as high as 1250 C. at the outlet end, it is beneficial in order to avoid distortion to divide the heating element into at least three sections, for instance, a 12-inch deep heating element should be made up of at least three 4-inch sections.
  • the combustion of the gas mixture must develop temperatures in the range of about 1200 C. to about 1800 C. in order to furnish sufiicient heat to convert the remaining hydrocarbon, ordinarily methane, in the feed gas to acetylene.
  • temperatures higher than 1800 C. it is not possible to achieve the optimum acetylene content in the stack gas, also, large quantities of carbon or coke are produced at the higher temperatures.
  • the reaction is carried out below 1800 C. For example, from about 1400 C. to about 1600 C. has proved to be very desirable.
  • the preferred hydrocarbon used in the process of this invention is methane; however, any paraffinic hydrocarbon which can be converted into acetylene by a partial combustion process may be used. Ordinarily, the paraflinic hydrocarbon will have less than seven carbon atoms. Examples of suitable hydrocarbons, besides methane, include ethane, propane, butane and pentane. Natural gas, comprising essentially methane, is a preferred hydrocarbon stream for use in this invention.
  • the oxygen-containing stream mixed with the parafiinic hydrocarbon for use in this invention is preferably oxygen; however, any oxygen-containing stream can be used.
  • any oxygen-containing stream can be used.
  • either a relatively pure oxygen stream or oxygen-enriched air can be used.
  • Pressure is not critical in the partial combustion of hydrocarbons to produce acetylene.
  • the converter operates at essentially atmospheric pressure under normal conditions but also operates satisfactorily at as high as 40 p.s.i.a. and as low as 5 p.s.i.a.
  • preheating of the feed gases to at least 1000 C. is preferred for the best results
  • the scope of this invention includes preheating feed gases from about 600 C. to at least 800 C. and up to a temperature of about 1150" C.
  • a temperature of about 1150 C. is a practical limit for heating the feed gas because of the materials of construction problem. Also, the flame induction period becomes too short above that temperature.

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  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
US311158A 1963-09-24 1963-09-24 Process for the partial combustion of hydrocarbons to produce acetylene Expired - Lifetime US3287434A (en)

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US311158A US3287434A (en) 1963-09-24 1963-09-24 Process for the partial combustion of hydrocarbons to produce acetylene
DE19641468356 DE1468356A1 (de) 1963-09-24 1964-09-24 Verfahren und Vorrichtung zur partiellen Verbrennung eines paraffinischen Kohlenwasserstoffes zur Bildung von Acetylen

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Cited By (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4613485A (en) * 1984-02-17 1986-09-23 Stauffer Chemical Company Pnictide trap for vacuum systems
US5124134A (en) * 1987-12-03 1992-06-23 Gaz De France Apparatus for the conversion of hydrocarbons
EP1462161A2 (de) 2003-03-26 2004-09-29 Basf Aktiengesellschaft Reaktor für Hochtemperaturreaktionen und Verwendung
EP1462160A3 (de) * 2003-03-26 2004-11-03 Basf Aktiengesellschaft Verfahren zur Durchführung einer Hochtemperaturreaktion, Reaktor zur Durchführung des Verfahrens, Verfahren zum Scale-Up eines Reaktors sowie Verwendung
EP1462162A3 (de) * 2003-03-26 2004-11-03 Basf Aktiengesellschaft Verfahren zum Scale-up eines Reaktors zur Durchführung einer Hochtemperaturreaktion, Reaktor und Verwendung

Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2167471A (en) * 1934-09-25 1939-07-25 Gen Electric Gas reaction method
US2543743A (en) * 1947-08-22 1951-02-27 Socony Vacuum Oil Co Inc Method and apparatus for hightemperature hydrocarbon conversions
US2768061A (en) * 1953-02-26 1956-10-23 Gen Electric Hydrogen reduction method and apparatus
GB902415A (en) * 1961-03-15 1962-08-01 Union Carbide Corp Improvements in and relating to the production of acetylene

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2167471A (en) * 1934-09-25 1939-07-25 Gen Electric Gas reaction method
US2543743A (en) * 1947-08-22 1951-02-27 Socony Vacuum Oil Co Inc Method and apparatus for hightemperature hydrocarbon conversions
US2768061A (en) * 1953-02-26 1956-10-23 Gen Electric Hydrogen reduction method and apparatus
GB902415A (en) * 1961-03-15 1962-08-01 Union Carbide Corp Improvements in and relating to the production of acetylene

Cited By (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4613485A (en) * 1984-02-17 1986-09-23 Stauffer Chemical Company Pnictide trap for vacuum systems
US5124134A (en) * 1987-12-03 1992-06-23 Gaz De France Apparatus for the conversion of hydrocarbons
EP1462161A2 (de) 2003-03-26 2004-09-29 Basf Aktiengesellschaft Reaktor für Hochtemperaturreaktionen und Verwendung
EP1462160A3 (de) * 2003-03-26 2004-11-03 Basf Aktiengesellschaft Verfahren zur Durchführung einer Hochtemperaturreaktion, Reaktor zur Durchführung des Verfahrens, Verfahren zum Scale-Up eines Reaktors sowie Verwendung
EP1462162A3 (de) * 2003-03-26 2004-11-03 Basf Aktiengesellschaft Verfahren zum Scale-up eines Reaktors zur Durchführung einer Hochtemperaturreaktion, Reaktor und Verwendung
EP1462161A3 (de) * 2003-03-26 2004-11-03 Basf Aktiengesellschaft Reaktor für Hochtemperaturreaktionen und Verwendung

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DE1468356A1 (de) 1969-03-20

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