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US3090684A - Conversion of oils with amounts of oxygen insufficient for complete combustion for the formation of carbon monoxide and hydrogen - Google Patents

Conversion of oils with amounts of oxygen insufficient for complete combustion for the formation of carbon monoxide and hydrogen Download PDF

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US3090684A
US3090684A US681945A US68194557A US3090684A US 3090684 A US3090684 A US 3090684A US 681945 A US681945 A US 681945A US 68194557 A US68194557 A US 68194557A US 3090684 A US3090684 A US 3090684A
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oxygen
vaporous
nonvaporous
hydrogen
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Nonnenmacher Helmut
Bartholome Ernst
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BASF SE
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    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
    • C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
    • C01B3/22—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by decomposition of gaseous or liquid organic compounds
    • C01B3/24—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by decomposition of gaseous or liquid organic compounds of hydrocarbons
    • C01B3/28—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by decomposition of gaseous or liquid organic compounds of hydrocarbons using moving solid particles
    • C01B3/30—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by decomposition of gaseous or liquid organic compounds of hydrocarbons using moving solid particles using the fluidised bed technique
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
    • C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
    • C01B3/32—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air
    • C01B3/34—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents
    • C01B3/38—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents using catalysts
    • C01B3/386—Catalytic partial combustion
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/02—Processes for making hydrogen or synthesis gas
    • C01B2203/025—Processes for making hydrogen or synthesis gas containing a partial oxidation step
    • C01B2203/0261—Processes for making hydrogen or synthesis gas containing a partial oxidation step containing a catalytic partial oxidation step [CPO]
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
    • C01B2203/0465—Composition of the impurity
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/10—Catalysts for performing the hydrogen forming reactions
    • C01B2203/1041—Composition of the catalyst
    • C01B2203/1047—Group VIII metal catalysts
    • C01B2203/1052—Nickel or cobalt catalysts
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/12—Feeding the process for making hydrogen or synthesis gas
    • C01B2203/1258—Pre-treatment of the feed
    • 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
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/50—Improvements relating to the production of bulk chemicals
    • Y02P20/52—Improvements relating to the production of bulk chemicals using catalysts, e.g. selective catalysts

Definitions

  • This invention relates to a process for the production of carbon monoxide and hydrogen by reacting oils with amounts of oxygen insufficient for complete combustion.
  • the hydrocarbon mixture is separated by thermal treatment into a vaporous and a non-vaporous fraction.
  • the kind of thermal treatment depends on the initial material. As a rule it is carried out so that in the first stage more than one third, preferably more than one half, advantageously more than two-thirds of the initial material forms a vaporous fraction.
  • a distillation is usually sufiicient, if necessary in the presence of steam, at temperatures up to about 380 C.
  • the first stage can consist of a so-called destructive pressure distillation, i.e.
  • the first stage consists of a thermal cracking to vaporous products and coke at temperatures of 400 to 600 C. and long residence times.
  • the non-vaporous fraction obtained in the first stage is reacted in a flame with oxygen and if desired steam and/or carbon dioxide.
  • the non-vaporous fraction from the first stage is liquid, it is preferable to atomize it with the oxygen-containing gases and if desired steam and/or carbon dioxide as propellant in a two-fluid nozzle, to ignite the mixture and to react it in a flame.
  • the products of the first stage are vaporous products and coke, it is preferable to grind the coke and to react it in dust form with the oxygen and the endothermic gasifying agents in a flame.
  • the amount of oxygen to be introduced in the second stage for each kilogram of non-vaporous components is dependent on the relative amount of this fraction in relation to the whole of the hydrocarbon mixture and is preferably greater the smaller this relative proportion is.
  • At least 0.9 ch. 111. (cubic meter) (normal temperature and pressure), preferably 1.2 cb. m. of oxygen per kilogram of non-vaporous fraction is used. If in the first stage more than one third of the initial material forms a vaporous fraction, at least 0.9 cb. m. of oxygen per kilogram of non-vaporous fraction is used. if the vaporous fraction is more than one half, at least 1.2 eh. m.
  • the vaporous fraction is more than two-thirds of the initial material, at least 1.5 cb. m. of oxygen per kilogram of non-vaporous fraction is used. If the nonvaporous fraction amounts to a maximum of 25% by weight of the hydrocarbon mixture, it is advantageous to use an amount of oxygen at least sufficient for the complete combustion of this fraction. Slight formation of carbon black which sometimes occurs can be substantially or completely prevented by introducing continuously or periodically into the second stage compounds of the elements of the first and/ or second group of the periodic system and/or of the metals of the iron group. If the non-vaporous fraction is liquid it is preferable to dissolve therein oil-soluble compounds of the said kind.
  • the hot reaction products of the second stage and the vaporous fraction from the first stage are introduced, separately or together, if desired with further amounts of oxygen, steam and/or carbon dioxide, into a fluidized layer of catalyst and reacted therein to carbon monoxide and hydrogen without external supply of heat at temperatures of about 700 to 1200 C., especially about 800 to l0O0 C.
  • the reaction mixture flows upwardly through the fluidized layer.
  • the process as a rule is carried out at atmospheric or reduced pressure in the third stage. In many cases, however, it is advantageous to use an increased pressure, for example of 2 to about 30 atmospheres.
  • catalysts there are suitable for example refractory porous materials, such as magnesite and siliceous materials, which are provided with one or more metals of the 8th group of the periodic system, especially nickel. Mineral oils, and also their fractions, residues or conversion products, for example cracking or hydrogenation products are most often used as starting materials.
  • Example Through pipe 1 190 kilograms of a paraffin-based petroleum and through pipe 2 kilograms of steam are introduced per hour into a preheater 3 and heated up therein to about 380 C. The mixture then passes into a distillation column 4 from which 143 kilograms per hour of vaporous hydrocarbons pass together with the steam through pipe 7 and 47 kilograms of liquid residue run oil? from the bottom through pipe 5.
  • the liquid residue is forced by the pump P into a two-fluid atomizer nozzle 6 and atomized with 124 N cb. m. (normal temperature and pressure) of oxygen and 72 kilograms of steam per hour, introduced through pipes 8 and 9.
  • the atomized mixture is reacted in a flame reaction in a combustion chamber 10 and the hot reaction gases and vapors are supplied to the lower conical part of a fluidized layer chamber 11, the cross-section of which in the cylindrical part amounts to 2 square meters.
  • the vaporous fraction flowing through the pipe 7 is also introduced into the lower conical partrof the fluidized layer chamber 11.
  • the fluidized layer consists of a finely-grained magnesite-nickel catalyst containing about 10% by Weight of nickel.
  • a reaction temperature of about 1000 C. is set up therein without the supply of heat from outside.
  • the reaction gases leaving the fluidized layer are freed in a cyclone 12 from the bulk of the entrained solid substances. These are supplied to the fluidized layer again through pipe 15.
  • reaction gas freed from Water also contains a few percent of C small amounts of nitrogen, sulphur-containing compounds and less than 0.3% by volume of hydrocarbons in the form of methane.
  • the catalyst has a life of several months. It can be withdrawn through pipe 13 and replenished from vessel 14.
  • a process for the production of a gas consisting essentially of carbon monoxide and hydrogen from mineral oils wherein said mineral oils are reacted with amounts of oxygen which are insufficient for complete combustion which process comprises:
  • reaction catalyst is selected from the group consisting of porous refractory materials and siliceous materials, which materials contain at least one metal of the 8th group of the periodic system.

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  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Health & Medical Sciences (AREA)
  • General Health & Medical Sciences (AREA)
  • Inorganic Chemistry (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)

Description

M y 1963 HT NONNENMACHER ETAL 3,
CONVERSION OF OILS WITH AMOUNTS 0F OXYGEN INSUFFICIENT FOR COMPLETE COMBUSTION FOR THE FORMATION OF CARBON MONOXIDE AND HYDROGEN Filed Sept. 4, 1957 lNVENTORS HELMUT NONNENIVIACHER ERNST BARTHOLOME ATT'YS United States Patent Office 3,090,634 Patented May 21, 1963 CGNVERSIGN F OILS WITH AMOUNTS OF OXY- GEN INSUFFICIENT FOR COMPLETE COMBUS- TION FGR THE FORMATION OF CARBON MONOXIDE AND HYDROGEN Heimut Nonnenmacher, Ludwigshafen (Rhine), and Ernst Bartholom, Heidelberg, Germany, assignors to Badische Anilin- & Soda-Fahrik Aktiengesellschaft, Ludwigshafen (Rhine), Germany Filed Sept. 4, 1957, Ser. No. 681,945 iaims priority, application Germany Sept. 8, 1956 3 Claims. (Cl. 48-212) This invention relates to a process for the production of carbon monoxide and hydrogen by reacting oils with amounts of oxygen insufficient for complete combustion.
It is known to convert liquid hydrocarbons together with oxygen and, if desired, steam into carbon monoxide and hydrogen in a bed of fluidized solid substances at high temperatures. In this method the liquid hydrocarbons are sprayed into the fluidized layer and the oxygen-containing gas is led upwardly through the fluidized layer. The disadvantage of this method of operation consists in the fact that even when using highly active catalysts and temperatures of more than 1000" C. it is not possible in continuous operation to obtain a synthesis gas with a low content of hydrocarbons. Moreover, troublesome and expensive distributor devices are necessary in an industrial plant in order to distribute the liquid hydrocarbon uniformly over the fluidized mass and to avoid a breakthrough of oxygen or the formation of soot. Furthermore, the catalyst is impaired in its activity by coking and, especially when oils with non-vaporizable components are being worked up, deactivated relatively rapidly by the impurities introduced with the liquid hydrocarbons so that a high consumption of catalyst must be accepted.
We have now found that the said disadvantages are avoided by carrying out in three stages the conversion of oirs containing unvaporizable components, especially mineral oils or their fractions or residues, with amounts of oxygen insufiicient for complete combustion, by contact with fluidized catalysts.
In the first stage, the hydrocarbon mixture is separated by thermal treatment into a vaporous and a non-vaporous fraction. The kind of thermal treatment depends on the initial material. As a rule it is carried out so that in the first stage more than one third, preferably more than one half, advantageously more than two-thirds of the initial material forms a vaporous fraction. In the case of mineral oils and mineral oil residues, which contain a considerable proportion of vaporizable hydrocarbons, a distillation is usually sufiicient, if necessary in the presence of steam, at temperatures up to about 380 C. In the case of mineral oil residues of higher boiling point, the first stage can consist of a so-called destructive pressure distillation, i.e. a mild thermal decomposition under pressure, at temperatures of about 400 to 530 C., the residence times being kept so short that substantially only vaporous and liquid products are formed. In the case of mineral oil residues of very high boiling point and poor in hydrogen, and in the case of tars, pitches and similar substances, the first stage consists of a thermal cracking to vaporous products and coke at temperatures of 400 to 600 C. and long residence times.
In the second stage, the non-vaporous fraction obtained in the first stage is reacted in a flame with oxygen and if desired steam and/or carbon dioxide. If the non-vaporous fraction from the first stage is liquid, it is preferable to atomize it with the oxygen-containing gases and if desired steam and/or carbon dioxide as propellant in a two-fluid nozzle, to ignite the mixture and to react it in a flame. If on the other hand the products of the first stage are vaporous products and coke, it is preferable to grind the coke and to react it in dust form with the oxygen and the endothermic gasifying agents in a flame.
The amount of oxygen to be introduced in the second stage for each kilogram of non-vaporous components is dependent on the relative amount of this fraction in relation to the whole of the hydrocarbon mixture and is preferably greater the smaller this relative proportion is. At least 0.9 ch. 111. (cubic meter) (normal temperature and pressure), preferably 1.2 cb. m. of oxygen per kilogram of non-vaporous fraction is used. If in the first stage more than one third of the initial material forms a vaporous fraction, at least 0.9 cb. m. of oxygen per kilogram of non-vaporous fraction is used. if the vaporous fraction is more than one half, at least 1.2 eh. m. is used, and if the vaporous fraction is more than two-thirds of the initial material, at least 1.5 cb. m. of oxygen per kilogram of non-vaporous fraction is used. If the nonvaporous fraction amounts to a maximum of 25% by weight of the hydrocarbon mixture, it is advantageous to use an amount of oxygen at least sufficient for the complete combustion of this fraction. Slight formation of carbon black which sometimes occurs can be substantially or completely prevented by introducing continuously or periodically into the second stage compounds of the elements of the first and/ or second group of the periodic system and/or of the metals of the iron group. If the non-vaporous fraction is liquid it is preferable to dissolve therein oil-soluble compounds of the said kind.
In the third stage the hot reaction products of the second stage and the vaporous fraction from the first stage are introduced, separately or together, if desired with further amounts of oxygen, steam and/or carbon dioxide, into a fluidized layer of catalyst and reacted therein to carbon monoxide and hydrogen without external supply of heat at temperatures of about 700 to 1200 C., especially about 800 to l0O0 C. The reaction mixture flows upwardly through the fluidized layer. It has been found that the inorganic constituents entrained by the reaction gases from the second stage and originating from the compounds added in the second stage or being contained in the initial materials, and also any carbon black formed in the second stage and carried through to the third stage, do not impair the catalytic reaction of the third stage or shorten the life of the catalyst.
The process as a rule is carried out at atmospheric or reduced pressure in the third stage. In many cases, however, it is advantageous to use an increased pressure, for example of 2 to about 30 atmospheres. As catalysts there are suitable for example refractory porous materials, such as magnesite and siliceous materials, which are provided with one or more metals of the 8th group of the periodic system, especially nickel. Mineral oils, and also their fractions, residues or conversion products, for example cracking or hydrogenation products are most often used as starting materials.
The invention will now be further described in the following example with reference to the accompanying drawing which shows diagrammatically an apparatus suitable for carrying out the invention. The invention is not limited to the said apparatus or to the process now to be described.
Example Through pipe 1 190 kilograms of a paraffin-based petroleum and through pipe 2 kilograms of steam are introduced per hour into a preheater 3 and heated up therein to about 380 C. The mixture then passes into a distillation column 4 from which 143 kilograms per hour of vaporous hydrocarbons pass together with the steam through pipe 7 and 47 kilograms of liquid residue run oil? from the bottom through pipe 5. The liquid residue is forced by the pump P into a two-fluid atomizer nozzle 6 and atomized with 124 N cb. m. (normal temperature and pressure) of oxygen and 72 kilograms of steam per hour, introduced through pipes 8 and 9. The atomized mixture is reacted in a flame reaction in a combustion chamber 10 and the hot reaction gases and vapors are supplied to the lower conical part of a fluidized layer chamber 11, the cross-section of which in the cylindrical part amounts to 2 square meters.
The vaporous fraction flowing through the pipe 7 is also introduced into the lower conical partrof the fluidized layer chamber 11. The fluidized layer consists of a finely-grained magnesite-nickel catalyst containing about 10% by Weight of nickel. A reaction temperature of about 1000 C. is set up therein without the supply of heat from outside. The reaction gases leaving the fluidized layer are freed in a cyclone 12 from the bulk of the entrained solid substances. These are supplied to the fluidized layer again through pipe 15.
About 600 eh. m. ((normal temperature and pressure) of carbon monoxide and hydrogen per hour are obtained. The reaction gas freed from Water also contains a few percent of C small amounts of nitrogen, sulphur-containing compounds and less than 0.3% by volume of hydrocarbons in the form of methane.
The catalysthas a life of several months. It can be withdrawn through pipe 13 and replenished from vessel 14.
We claim:
1. A process for the production of a gas consisting essentially of carbon monoxide and hydrogen from mineral oils wherein said mineral oils are reacted with amounts of oxygen which are insufficient for complete combustion which process comprises:
(1) thermally treating said mineral oil to separate the oil into a vaporous and a nonvaporuos fraction, the vaporous fraction constituting more than one-third by weight of the total,
(2) reacting the nonvaporous fraction in a flame (a) with at least 0.9 cubicrneter of oxygen per kilogram of the nonvaporous fraction where said vaporous fraction is up to one-half by weight of the total initial material,
(12) with at least 1.2 cubic meters of oxygen per kilogram of the nonvaporous fraction where said vaporous fraction is more than one-half and up to two-thirds by weight of said total initial material, and
(c) with at least 1.5 cubic meters of oxygen per kilogram of the nonvaporous fraction where said vaporous fraction is more than two-thirds by weight of the total initial material, said quantities of oxygen being measured at normal temperature and pressure, and
(3) thereafter leading the substances thus formed in said nonvaporous fraction-oxygen reaction and said vaporous fraction simultaneously into a fluidized layer of reaction catalyst at a temperature of from about 700 to 1200 C. wherein a further reaction takes place between said mineral oil and oxygen and whereby a synthesis gas is produced consisting essentially of carbon monoxide and hydrogen.
2. A process as in claim 1 wherein the reaction catalyst is selected from the group consisting of porous refractory materials and siliceous materials, which materials contain at least one metal of the 8th group of the periodic system.
3. A process as in claim 2 wherein the said vaporous fraction is at least by weight of the said oil, and wherein said nonvaporous fraction is burned with an amount of oxygen at least sufiicient for complete combustion.
References Cited in the file of this patent UNITED STATES PATENTS Haney Nov. 10, 1959

Claims (1)

1. A PROCESS FOR THE PRODUCTION OF A GAS CONSISTING ESSENTIALLY OF CARBON MONOXIDE AND HYDROGEN FROM MINERAL OILS WHEREIN SAID MINERAL OILS ARE REACTED WITH AMOUNTS OF OXYGEN WHICH ARE INSUFFICIENT FOR COMPLETE COMBUSTION WHICH PROCESS COMPRISES: (1) THERMALLY TREATING SAID MINERAL OIL TO SEPARATE THE OIL INTO VAPOROUS AND A NONVAPOROUS FRACTION, THE VAPOROUS FRACTION CONSTITUTING MORE THAN ONE-THIRD BY WEIGHT OF THE TOTAL, (2) REACTING THE NONVAPOROUS FRACTION IN A FLAME (A) WITH AT LEAST 0.9 CUBIC METER OF OXYGEN PER KILOGRAM OF THE NONVAPOROUS FRACTION WHERE SAID VAPOROUS FRACTION IS UP TO ONE-HALF BY WEIGHT OF THE TOTAL INITIAL MATERIAL, (B) WITH AT LEAST 1.2 CUBIC METERS OF OXYGEN PER KILOGRAM OF THE NONVAPOROUS FRACTION WHERE SAID VAPOROUS FRACTION IS MORE THAN ONE-HALF AND UP TO TWO-THIRDS BY WEIGHT OF SAID TOTAL INITIAL MATERIAL, AND (C) WITH AT LEAST 1.5 CUBIC METERS OF OXYGEN PER KILOGRAM OF THE NONVAPOROUS FRACTION WHERE SAID VAPOROUS FRACTION IS MORE THAN TWO-THIRDS BY WEIGHT OF THE TOTAL INITIAL MATERIAL, SAID QUANTITIES OF OXYGEN BEING MEASURED AT NORMAL TEMPERATURES AND PRESSURE, AND (3) THERAFTER LEADING THE SUBSTANCES THUS FORMED IN SAID NONVAPOROUS FRACTION-OXYGEN REACTION AND SAID VAPOROUS FRACTION SIMULTANEOUSLY INTO FLUIDIZED LAYER OF REACTION CATALYST AT A TEMPERATURE OF FROM ABOUT 700* TO 1200*C. WHEREIN A FURTHER REACTION TAKES PLACE BETWEEN SAID MINERAL OIL AND OXYGEN AND WHEREBY A SYNTHESIS GAS IS PRODUCED CONSISTING ESSENTIALLY OF CARBON MONOXIDE AND HYDROGEN.
US681945A 1956-09-08 1957-09-04 Conversion of oils with amounts of oxygen insufficient for complete combustion for the formation of carbon monoxide and hydrogen Expired - Lifetime US3090684A (en)

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Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3481987A (en) * 1967-08-14 1969-12-02 Union Oil Co Removal of oxygen impurity from carbon monoxide
US3506417A (en) * 1966-05-13 1970-04-14 Phillips Petroleum Co Hydrocarbon reforming
EP0178853A2 (en) * 1984-10-18 1986-04-23 The British Petroleum Company p.l.c. Conversion process

Families Citing this family (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE1292634B (en) * 1957-09-24 1969-04-17 Celleco Ab Process for the production of highly concentrated gaseous oxides
DE1144239B (en) * 1959-09-01 1963-02-28 Basf Ag Process for the conversion of gaseous and liquid, sulfur-containing hydrocarbons, especially minerals, to hydrogen and carbon oxide
DE1129134B (en) * 1960-07-26 1962-05-10 Basf Ag Process for the catalytic conversion of liquid, sulphurous hydrocarbons with insufficient amounts of oxygen for complete combustion to form carbon oxide and hydrogen using fluidized beds consisting of catalyst bodies

Citations (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2378116A (en) * 1941-07-10 1945-06-12 Phillips Petroleum Co Method and apparatus for control of vapor pressure
US2630378A (en) * 1949-07-23 1953-03-03 Texaco Development Corp Generation of synthesis gas
US2697655A (en) * 1947-12-31 1954-12-21 Kellogg M W Co Manufacture of a hydrogen-rich gas
US2707147A (en) * 1948-02-07 1955-04-26 Hercules Powder Co Ltd Production of domestic gas
US2716597A (en) * 1951-06-12 1955-08-30 Koppers Co Inc Method and apparatus for the production of combustible gases from liquid fuels
US2828196A (en) * 1954-04-30 1958-03-25 United Gas Improvement Co Method of producing combustible gas rich in oil gas
US2912315A (en) * 1956-10-10 1959-11-10 Exxon Research Engineering Co Fluidized solids town gas manufacturing process

Family Cites Families (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR1028172A (en) * 1950-11-04 1953-05-20 Lummus Co Improvements in the distillation of hydrocarbons
DE923843C (en) * 1952-01-06 1955-02-21 Basf Ag Process for the generation of fuel, in particular synthesis gases, from gaseous or liquid fuels and lump fuels

Patent Citations (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2378116A (en) * 1941-07-10 1945-06-12 Phillips Petroleum Co Method and apparatus for control of vapor pressure
US2697655A (en) * 1947-12-31 1954-12-21 Kellogg M W Co Manufacture of a hydrogen-rich gas
US2707147A (en) * 1948-02-07 1955-04-26 Hercules Powder Co Ltd Production of domestic gas
US2630378A (en) * 1949-07-23 1953-03-03 Texaco Development Corp Generation of synthesis gas
US2716597A (en) * 1951-06-12 1955-08-30 Koppers Co Inc Method and apparatus for the production of combustible gases from liquid fuels
US2828196A (en) * 1954-04-30 1958-03-25 United Gas Improvement Co Method of producing combustible gas rich in oil gas
US2912315A (en) * 1956-10-10 1959-11-10 Exxon Research Engineering Co Fluidized solids town gas manufacturing process

Cited By (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3506417A (en) * 1966-05-13 1970-04-14 Phillips Petroleum Co Hydrocarbon reforming
US3481987A (en) * 1967-08-14 1969-12-02 Union Oil Co Removal of oxygen impurity from carbon monoxide
EP0178853A2 (en) * 1984-10-18 1986-04-23 The British Petroleum Company p.l.c. Conversion process
EP0178853A3 (en) * 1984-10-18 1988-07-20 The British Petroleum Company P.L.C. Conversion process

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