US2801159A - Method for the catalytic decomposition of hydrocarbons by steam - Google Patents

Method for the catalytic decomposition of hydrocarbons by steam Download PDF

Info

Publication number
US2801159A
US2801159A US285764A US28576452A US2801159A US 2801159 A US2801159 A US 2801159A US 285764 A US285764 A US 285764A US 28576452 A US28576452 A US 28576452A US 2801159 A US2801159 A US 2801159A
Authority
US
United States
Prior art keywords
stream
temperature
steam
primary
hydrocarbons
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Expired - Lifetime
Application number
US285764A
Other languages
English (en)
Inventor
Carton Pierre
Albert H Gosselin
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Societe Chimique de la Grande Paroisse Azote et Produits Chimiques
Original Assignee
Societe Chimique de la Grande Paroisse Azote et Produits Chimiques
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Societe Chimique de la Grande Paroisse Azote et Produits Chimiques filed Critical Societe Chimique de la Grande Paroisse Azote et Produits Chimiques
Application granted granted Critical
Publication of US2801159A publication Critical patent/US2801159A/en
Anticipated expiration legal-status Critical
Expired - Lifetime legal-status Critical Current

Links

Images

Classifications

    • 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
    • C01B3/384—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 the catalyst being continuously externally heated
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
    • 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
    • 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
    • C01B3/40—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 characterised by the catalyst
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
    • B01J2208/00008—Controlling the process
    • B01J2208/00017—Controlling the temperature
    • B01J2208/00026—Controlling or regulating the heat exchange system
    • B01J2208/00035—Controlling or regulating the heat exchange system involving measured parameters
    • B01J2208/00097—Mathematical modelling
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
    • B01J2208/00008—Controlling the process
    • B01J2208/00017—Controlling the temperature
    • B01J2208/00106—Controlling the temperature by indirect heat exchange
    • B01J2208/00168—Controlling the temperature by indirect heat exchange with heat exchange elements outside the bed of solid particles
    • B01J2208/00212—Plates; Jackets; Cylinders
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
    • B01J2208/00008—Controlling the process
    • B01J2208/00017—Controlling the temperature
    • B01J2208/0053—Controlling multiple zones along the direction of flow, e.g. pre-heating and after-cooling
    • 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

Definitions

  • the carbon may form at a higher rate than that of its oxidation and the deposit of carbon thus produced leads to a number of drawbacks such as the clogging of the flow of gases, an embedding and a poisoning of the catalyst, a disaggregation of the catalyst carrier, etc.
  • our invention has for its object to remove the drawbacks of the above method while retaining its advantages and reducing the amount of the secondary stream of steam, whether admixed with other gases or otherwise, to be incorporated to the primary streams of hydrocarbons generally admixed with steam.
  • our invention consists chiefly in subdividing the primary stream containing heavy hydrocarbons into a number of elementary stream fractions that are introduced separately at corresponding points of the reaction stream constituted bythe secondary stream to which the successive fractions of the primary stream are being introduced'in succession for cracking in the presence of a catalyst submitted to the action of external heating means. At each point of intrduction of an elementary fraction of the primary stream, said fraction mixes speedily and completely with the totality of the circulating mixture undergoing reaction.
  • the outward heating of the catalyst should be sulficient for the heat transferred to the gasiform mixture undergoing reaction in the path separating two successive points of introduction of the primary mixture to produce the following results: raising suddenly the temperature of the fraction of the primary mixture that has just been introduced from a value below t1 to a value above t2-making up for the endothermic character of the reactionkeeping the mixture undergoing reaction between the successive points of introduction of the elementary fractions at a temperature above t2 in a manner such that in spite of the addition of the following elementary fractions of the primary stream that remain at a temperature below t1 the temperature of the compound mixture may lie in all cases above 22.
  • the secondary stream introduced at the beginning of the reaction should remain at a temperature higher than 12 and its amount should be sufficient for the first fraction of the primary fluid introduced at a temperature below t1 to be suddenly brought through this incorporation to the secondary stream to which it is admixed and with which it is stirred, to a temperature above t2.
  • the amount of secondary fluid used may in its turn be comparatively small and this is all the more true when its temperature is higher.
  • catalysts that do not lead, at temperatures approximating t2, to a dehydrogenization producing a deposit of free carbon, but lead only to a splitting of the heavy molecules into groups CH or CH2, which are readily attacked by steam, and into CH4 in accordance with the reactions performed on hydrocarbons, such as It has been found, according to our invention, that such catalysts may advantageously be constituted by zircon associated with magnesia and carried by refractory carriers hving e. g. a basis of zircon or alumina.
  • These catalysts do not contain substantial amounts of metals and in particular no metals of the nickel type and they have consequently no dehydrogenizing capacity. They allow a large fraction of CH4 to remain in the gaseous mixture at a temperature 12, whereby the system of Reactions 4 is much less endothermic than the Reaction 1 and this allows reducing the amount of heat to be transmitted to the fluid during its movement over the height h and consequently, this height may, in fact, be reduced.
  • Said single figure is a vertical cross-section of a catalyzing column according to our invention.
  • the column 1 is made of refractory steel having a diameter of the magnitude of to cm. It
  • ' is heated by external means and brought to a temperature of about 800 to 1000 C. or above.
  • This arrangement provides over the height ho means for superheating speedily the steam to a temperature of about 800850 C., but any other manner of superheating steam may be used, provided it allows reaching said temperature.
  • the arrangement includes a first pipe 5 and a second pipe 5 feeding vapors of the hydrocarbons to be transformed.
  • the pipe 5 allows introducing steadily a portion of the primary preheated stream of a mixture, say, of hydrocarbons and steam brought to about 400-450 C. and including 10 kg. per hour of hydrocarbons and 5 to 10 kg. per hour of steam.
  • This fluid is projected at a considerable speed by means of an injector system that provides simultaneously a perfect admixture of this primary mixture with the steam that has been superheated during its travel over the height ha along the wall of the column 1, while this injector also urges the mixture speedily into the catalyzing area.
  • thermic dissociation of the superheated mixture accompanied by the formation of carbon black may be avoided, provided the contacting with the catalyst is performed after a very short lapse of time that is less than one third or even than one tenth of a second; this dissociation is performed in practice in accordance with a procedure the speed of which depends on the temperature and on the nature of the reacting hydrocarbons.
  • the catalyst furthers the oxidizing action of the steam and consequently prevents efficiently the formation of free carbon.
  • the mixture When in contact with the mass of the catalyst that is outwardly heated over a height hi of a magnitude of 0.50 to 1 m., the mixture is transformed into C0, C02, Hz with the accompaniment of a certain amount of light hydrocarbons such as CzHs, C2H4, CH4.
  • baflle plates 9 that shift the downwardly moving gasiform flow towards the axis of the pipe in the vicinity of the distributing ports or perforations 6.
  • the mass of nickel-free catalyst 10 extends downwardly by 50 to cm. over a height h beyond the lowermost row of distributing ports or perforations; the tube is filled in its remaining lower portion i. e. over the height h" with a nickel-containing catalyst 11.
  • a gaseous mixture at a temperature of 750 to 780 C., formed by a stream feeding approximately 178 cbm. of gas per hour, admixed with about 25 ohm. of steam per hour.
  • the composition of gas obtained is approximately the following:
  • centesimal composition of the gas considered dry which is as follows:
  • the secondary mixture should be constituted by steam admixed with CO2 and possibly with air, if required.
  • the arrangement shows thus the advantage of a high stability, while it removes automatically the carbon deposits which might have a tendency to form in the catalystcontaining area.
  • a method for the catalytic decomposition of heavy hydrocarbons by steam consisting in preheating a primary stream of heavy hydrocarbons admixed With steam to a temperature of about 400 to 450 C. and lower than the threshold of pyrolysis leading to the formation of free carbon, subdividing said heated stream into a piurality of successive elementary fractions, the first of which contains less than about one third of the total throughput of the primary stream, heating a secondary gasiform stream containing steam to a temperature substantially above the threshold of thermal hydrolysis at about 800 to 850 C., maintaining said stream permanently above said threshold temperature, introducing the different fractions of the first stream into corresponding successive points of the secondary stream to obtain at each of said points a homogeneous reaction mixture, the temperature of which is still higher than said threshold of thermal hydrolysis and causing said successive portions of the secondary stream admixed with the primary stream fractions to react with a zircon-containing nickel-free catalyst to produce the cracking of the heavy hydrocarbons.
  • a method for the catalytic decomposition of heavy hydrocarbons by steam consisting in preheating a primary stream of heavy hydrocarbons admixed with steam to a temperature of about 400 to 450 C. and lower than the threshold of pyrolysis leading to the formation of free carbon, subdividing said heated stream into a plurality of successive elementary fractions, the first of which contains less than about one third of the total throughput of the primary stream, heating a secondary gasiform stream containing steam to a temperature substantially above the threshold of thermal hydrolysis, at about 800 to 850 C., maintaining said stream permanently above said threshold temperature, introducing the difierent fractions of the first stream into corresponding successive points of the secondary stream to obtain at each of said points a homogeneous reaction mixture, the temperature of which is still higher than said threshold of thermal hydrolysis, causing said successive portions of the secondary stream admixed with the primary stream fractions to react on a zircon-containing nickel-free catalyst to produce the cracking of the heavy hydrocarbons and to split the heavy hydrocarbon molecules into hydro

Landscapes

  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Organic Chemistry (AREA)
  • Health & Medical Sciences (AREA)
  • General Health & Medical Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Inorganic Chemistry (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
US285764A 1951-05-04 1952-05-02 Method for the catalytic decomposition of hydrocarbons by steam Expired - Lifetime US2801159A (en)

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
FR1073309T 1951-05-04

Publications (1)

Publication Number Publication Date
US2801159A true US2801159A (en) 1957-07-30

Family

ID=9606068

Family Applications (1)

Application Number Title Priority Date Filing Date
US285764A Expired - Lifetime US2801159A (en) 1951-05-04 1952-05-02 Method for the catalytic decomposition of hydrocarbons by steam

Country Status (2)

Country Link
US (1) US2801159A (fr)
FR (1) FR1073309A (fr)

Cited By (10)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3118927A (en) * 1959-10-29 1964-01-21 Du Pont Process for preparing acrylic acid and acrylonitrile from propylene
US3334971A (en) * 1964-08-18 1967-08-08 Chemical Construction Corp Catalytically reforming hydrocarbon and steam mixtures
US3351563A (en) * 1963-06-05 1967-11-07 Chemical Construction Corp Production of hydrogen-rich synthesis gas
US3532472A (en) * 1967-03-20 1970-10-06 Shell Oil Co Apparatus for carrying out partial oxidation of organic compounds
US3732078A (en) * 1971-04-16 1973-05-08 Marathon Oil Co Flow redistributor for a fixed bed down flow reactor
US4036180A (en) * 1975-03-05 1977-07-19 Nippon Soken, Inc. Fuel reforming system for an internal combustion engine
US4491573A (en) * 1983-03-25 1985-01-01 Metallgesellschaft Aktiengesellschaft Process for heating hydrogen
US5554351A (en) * 1993-05-17 1996-09-10 Haldor Topsoe A/S High temperature steam reforming
EP3501625A1 (fr) * 2017-12-20 2019-06-26 Hamilton Sundstrand Corporation Système d'inertage de réservoir de carburant catalytique
US10994860B2 (en) 2017-12-20 2021-05-04 Hamilton Sunstrand Corporation Catalytic fuel tank inerting system

Citations (14)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB382620A (en) * 1931-07-24 1932-10-24 Julius Franz Ludwig Moeller Improvement in the manufacture of gases from oil
US1989927A (en) * 1933-05-13 1935-02-05 Houdry Process Corp Use of contact masses
US2056911A (en) * 1931-01-17 1936-10-06 Ig Farbenindustrie Ag Production of hydrogen from hydrocarbons
US2103182A (en) * 1937-12-21 Process for making gas
US2192815A (en) * 1937-12-10 1940-03-05 Combustion Utilities Corp Manufacture of combustible gas
US2518583A (en) * 1945-06-27 1950-08-15 Universal Oil Prod Co Catalytic reactor
US2526521A (en) * 1948-05-29 1950-10-17 Standard Oil Dev Co Production of gas mixtures containing co and h2
US2585737A (en) * 1948-10-21 1952-02-12 Standard Oil Dev Co Catalytic reforming process
US2593584A (en) * 1948-12-01 1952-04-22 Standard Oil Dev Co Reforming hydrocarbon gases in the presence of a magnesia catalyst
US2605178A (en) * 1946-09-27 1952-07-29 Standard Oil Dev Co Preparation of gaseous fuel
US2626204A (en) * 1949-01-29 1953-01-20 Universal Oil Prod Co Apparatus for conducting catalytic endothermic and exothermic reactions
US2639224A (en) * 1950-08-31 1953-05-19 Gulf Oil Corp Catalytic reactor
US2668101A (en) * 1949-01-21 1954-02-02 Nat Cylinder Gas Co Method of preparing mixtures of hydrogen and carbon oxides
US2692193A (en) * 1948-07-29 1954-10-19 Inst Gas Technology Method of preparing a gas interchangeable with coke oven gas, carbureted gas, or mixtures thereof

Patent Citations (14)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2103182A (en) * 1937-12-21 Process for making gas
US2056911A (en) * 1931-01-17 1936-10-06 Ig Farbenindustrie Ag Production of hydrogen from hydrocarbons
GB382620A (en) * 1931-07-24 1932-10-24 Julius Franz Ludwig Moeller Improvement in the manufacture of gases from oil
US1989927A (en) * 1933-05-13 1935-02-05 Houdry Process Corp Use of contact masses
US2192815A (en) * 1937-12-10 1940-03-05 Combustion Utilities Corp Manufacture of combustible gas
US2518583A (en) * 1945-06-27 1950-08-15 Universal Oil Prod Co Catalytic reactor
US2605178A (en) * 1946-09-27 1952-07-29 Standard Oil Dev Co Preparation of gaseous fuel
US2526521A (en) * 1948-05-29 1950-10-17 Standard Oil Dev Co Production of gas mixtures containing co and h2
US2692193A (en) * 1948-07-29 1954-10-19 Inst Gas Technology Method of preparing a gas interchangeable with coke oven gas, carbureted gas, or mixtures thereof
US2585737A (en) * 1948-10-21 1952-02-12 Standard Oil Dev Co Catalytic reforming process
US2593584A (en) * 1948-12-01 1952-04-22 Standard Oil Dev Co Reforming hydrocarbon gases in the presence of a magnesia catalyst
US2668101A (en) * 1949-01-21 1954-02-02 Nat Cylinder Gas Co Method of preparing mixtures of hydrogen and carbon oxides
US2626204A (en) * 1949-01-29 1953-01-20 Universal Oil Prod Co Apparatus for conducting catalytic endothermic and exothermic reactions
US2639224A (en) * 1950-08-31 1953-05-19 Gulf Oil Corp Catalytic reactor

Cited By (11)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3118927A (en) * 1959-10-29 1964-01-21 Du Pont Process for preparing acrylic acid and acrylonitrile from propylene
US3351563A (en) * 1963-06-05 1967-11-07 Chemical Construction Corp Production of hydrogen-rich synthesis gas
US3334971A (en) * 1964-08-18 1967-08-08 Chemical Construction Corp Catalytically reforming hydrocarbon and steam mixtures
US3532472A (en) * 1967-03-20 1970-10-06 Shell Oil Co Apparatus for carrying out partial oxidation of organic compounds
US3732078A (en) * 1971-04-16 1973-05-08 Marathon Oil Co Flow redistributor for a fixed bed down flow reactor
US4036180A (en) * 1975-03-05 1977-07-19 Nippon Soken, Inc. Fuel reforming system for an internal combustion engine
US4491573A (en) * 1983-03-25 1985-01-01 Metallgesellschaft Aktiengesellschaft Process for heating hydrogen
US5554351A (en) * 1993-05-17 1996-09-10 Haldor Topsoe A/S High temperature steam reforming
EP3501625A1 (fr) * 2017-12-20 2019-06-26 Hamilton Sundstrand Corporation Système d'inertage de réservoir de carburant catalytique
US10569896B2 (en) 2017-12-20 2020-02-25 Hamilton Sundstrand Corporation Catalytic fuel tank inerting system
US10994860B2 (en) 2017-12-20 2021-05-04 Hamilton Sunstrand Corporation Catalytic fuel tank inerting system

Also Published As

Publication number Publication date
FR1073309A (fr) 1954-09-23

Similar Documents

Publication Publication Date Title
US2902432A (en) Catalytic conversion of hydrocarbons
US4388218A (en) Regeneration of cracking catalyst in two successive zones
US2231231A (en) Process and apparatus for catalytic operations
US2468508A (en) Conversion processes in the presence of a dense turbulent body of finely divided solid material
US3808121A (en) Method of regenerating a hydrocarbon conversion catalyst to minimize carbon monoxide in regenerator effluent
US2376564A (en) Catalytic conversion
US2320318A (en) Method for catalytic conversion
US2801159A (en) Method for the catalytic decomposition of hydrocarbons by steam
US2398954A (en) Process and apparatus for promoting thermal reactions
US2597346A (en) Method for effecting the conversion of organic reactant streams
US2438728A (en) Temperature control in fluidized catalyst systems
US3128163A (en) Method of carrying out exothermic catalytic carbon monoxide-steam gas reactions
KR101489768B1 (ko) 알칸 스트림을 탈수소화하는 촉매 탈수소화 방법 및 장치
US3843330A (en) Regeneration apparatus
US2730556A (en) Method for effecting endothermic dehydrogenation reactions
US3048476A (en) Conversion of hydrocarbons and carbonaceous materials
US2376191A (en) Chemical process
US2727810A (en) Apparatus for the conversion of fluid reactant streams in the presence of subdivided particles maintained in dispersed suspension
JPS5852229A (ja) 脱水素方法
US3754051A (en) Production of olefin from saturated hydrocarbon
GB543838A (en) An improved process for catalytic treatment of hydrocarbons
US2402875A (en) Catalytic conversion process
KR20230041813A (ko) 온도 분포에 있어서 유동 촉매와 공급물을 반응시키기 위한 방법 및 장치
US2330710A (en) Regeneration of catalysts
US2340814A (en) Process for converting hydrocarbon oils