USRE21911E - Process for converting hydro - Google Patents

Process for converting hydro Download PDF

Info

Publication number
USRE21911E
USRE21911E US21911DE USRE21911E US RE21911 E USRE21911 E US RE21911E US 21911D E US21911D E US 21911DE US RE21911 E USRE21911 E US RE21911E
Authority
US
United States
Prior art keywords
oxides
catalyst
hydrocarbons
oxide
dehydrogenation
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
Application number
Publication date
Application granted granted Critical
Publication of USRE21911E publication Critical patent/USRE21911E/en
Expired legal-status Critical Current

Links

Classifications

    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C5/00—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms
    • C07C5/32—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by dehydrogenation with formation of free hydrogen
    • C07C5/321—Catalytic processes
    • C07C5/322—Catalytic processes with metal oxides or metal sulfides
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C5/00—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms
    • C07C5/32—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by dehydrogenation with formation of free hydrogen
    • C07C5/327—Formation of non-aromatic carbon-to-carbon double bonds only
    • C07C5/333—Catalytic processes
    • C07C5/3332—Catalytic processes with metal oxides or metal sulfides

Definitions

  • This invention relates to processes wherein saturated hydrocarbons are converted into oleflns by catalytic dehydrogenation at elevated temperatures, the nature of the catalyst and the conditions of the conversion being such as to effect simple dehydrogenation of the saturated into the corresponding unsaturated hydrocarbon with very slight decomposition of the usual kind wherein the carbon chain breaks and smaller molecules are formed.
  • Catalytic dehydrogenation is widely applied to organic compounds, more particularly to alcohols and hydrocarbons.
  • the dehydrogenation of alcohols is readily effected at low temperatures in the presence of various catalytic metas and metallic oxides.
  • That class of hydrocarbons containing the hexamethylene ring may be dehydrogenated in a characteristic manner into the corresponding aromatic hydrocarbons by a small group of catalysts comprising the most active of the hydrogenation catalysts.
  • Both alcohols and hexamethylene hydrocarbons can be successfully dehydrogenated to yield molecular hydrogen and the corresponding, dehydrogenation product at moderate temperatures, which need not exceed 300 C.
  • the parafiln hydrocarbons on the other hand, cannot be dehydrogenated at such low temperatures because of the unfavorable thermodynamic relationships.
  • the activity must be high toallow the dehydrogenation to be accomplished in a time so short that cracking is not marked; the active nature of the surface must not be destroyed by the hightemperatures; the composition and mechanical structure of the catalyst should discourage tar and carbon'iormation.
  • Nickel, platinum, and palladium comprise the .efiective catalysts for dehydrogenating hexamethylene hydrocarbons but these tail under the conditions required for parafiins. Many other substances have been suggested for the dehydrogenation of paraflins which fail in one or more respects.
  • the two more meta lic salts may be dissolved together in water and the hydrous oxides precipitated by an excess of alkali, preferably ammonium, sodium or potassium hydroxide. amount of acetic acid prior to precipitation assists .in maintaining the gel structure during the subsequent drying of the precipitate.
  • alkali preferably ammonium, sodium or potassium hydroxide.
  • acetic acid prior to precipitation assists .in maintaining the gel structure during the subsequent drying of the precipitate.
  • Titanium dioxide, boric oxide and silicon dioxide are of an acidic nature and are'best introduced in the form The addition of a small of their alkali salts in aqueous solution. Such a solution may be introduced into the alkali solu tion used for the precipitation before the solution of thecliromium -or other salts is introduced, or
  • the catalyst prepared in this way may be supported in a suitable container and the saturated hydrocarbon to be dehydrogenated passed over the catalyst while a suitable reaction temperature of preferably 450-550" C. is maintained.
  • the chromium oxide gel thus stabilized by the addition of a diiilcultly reducible oxide will lose activity during use, but the activity can be restored repeatedly by passing over the catalyst for a short time an oxygen containing gas 'while maintaining a temperature of 400-550 C.
  • an oxygen containing gas 'while maintaining a temperature of 400-550 C During the decay in activity, tar and carbon form in the catalyst granules and it is probably to this that the loss in activity must be attributed.
  • We have found that the addition of small amounts of certain heavy metal oxides incorporated in the catalyst will bring about a decrease in the rate at which activityis lost and the rate at which carbon forms. 'I'hallium and bismuth oxides are most effective, lead and mercury oxides less so.
  • the heavy metal oxides are incorporated in the catalyst most conveniently by adding a soluble salt of the metal, preferably the nitrate to the chromium salt prior to dissolving and precipitating It is preferable to 'perform The gelatinous precipitate of the mixed hydrous I the hydrous oxides as described. Large proportions of the heavy metal oxides cannot be introduced without loss of the coherent gel structure. Usually less than 20 mol. per cent should be incorporated in the catalyst and an addition of 0.5 to 5 per cent will produce a great lessening in decay of activity during continued dehydrogenation.
  • the improved catalysts are effective for converting not only parailins but also alicyclic or aromatic hydrocarbons containing alkyl substituent groups of two or more carbon atoms into the corresponding unsaturated hydrocarbons of the same number of carbon atoms per molecule but of lower hydrogen content. Oleilns containing at least four carbon atoms per molecule can similarly be converted into diolefins. Temperatures in the range 300 to 600 C. give best results. The reaction rate with the catalysts described is high and equilibrium extent of dissociation is readily attained. We have found that the lower temperatures at which equilibrium dishibit good activity at low hydrogen resist poisoning by sulfur compounds.
  • sociation is small may be used at the lower pressures which favor dissociations, or when treating the higher molecular weight hydrocarbons, for which the thermodynamic equilibrium dissociaw tion. is large at the lower temperatures.
  • the dissociation is repressed by high pressures, and pressures exceeding a few atmospheres are accordingly undesirable. Pressures in the neighborhood of atmospheric give good results, and pressures below atmospheric permit still greater dissociation.
  • catalysts are used to eii'ect hydrogenation of olefins or diolefins, temperatures of 200 to 500C. may be used, preferably the lower temperaturesand a high partial pressure of hydrogen and pressures above atmospheric are desirable but not necessary.
  • These catalysts expressures and Example 1.An aqueous solution of chromic nitrate and aluminum nitrate containing the salts in the molar ratios of one to one was introduced into an excess of dilute aqua ammonia.
  • Example 2 A chromium oxide-aluminum oxide gel was prepared as in Example 1 except that 2 mol. per cent of thallium nitrate was incorporated in the solution of the other metallic salts. The conversion of butane, carried out in the same way,
  • a process for the non-destructive dehydrogenating of aliphatic hydrocarbons of at least two carbon atoms per molecule to corresponding hydrocarbons of lower hydrogen content which comprises contacting said aliphatic hydrocarbons bons are contacted with a catalyst comprising chromium oxide vitreous gel at elevated temperatures, the method of rendering said chromium oxide gel thermostable, which comprises incorporating in intimate association therewith a difficultly reducibleoxide of the group aluminum, zirconium, titanium, silicon, thorium, boron, and
  • hydrocarbons to produce corresponding hydrocarbons of lower hydrogen-carbon ratio
  • steps which comprise passing the hydrocarbon over a vitreous gel catalyst consisting of chromium oxide together with a diiilcultly reducible oxide of the group aluminum, zirconium, titanium, silicon, thorium, boron, and magnesium, the said oxides having been combined in a state of intimate admixture, effected while in a highly hydrous condition, continuing such passage until the activity of said catalyst becomes reduced, and restoring the activity of the said catalyst by bringing it at an elevated temperature into contact with a gas containing free oxygen.
  • a vitreous gel catalyst comprising chromium oxide together with a difiicultly reducible oxide of the group aluminum, zirconium, titanium, silicon, thorium, boron and magnesium, the said oxides having been combined in a state of intimate association effected while in a highly hydrous condition and having added also at least one-half per cent of a readily reducible oxide of the group thallium, bismuth, lead and mercury.
  • a process for the non-destructive dehydrogenation of aliphatic hydrocarbons of at least two carbon atoms per molecule to corresponding hydrocarbons of lower hydrogen content which comprises contacting said aliphatic hydrocarbons under dehydrogenation conditions with a vitre ous gel catalyst comprising not less than live per cent of chromium oxide and at least five per cent of a difflcultly reducible oxide or the group aluminum, zirconium, titanium, silicon, thorium, boron, and magnesium, the said oxides having been combined in a state of intimate association effected while the oxides are in a highly hydrous condition.
  • a process for the non-destructive dehydrogenation of aliphatic hydrocarbons of at least two carbon atoms per molecule to corresponding hydrocarbons of lower hydrogen content which comprises contacting said aliphatic hydrocarbons under dehydrogenation conditions with a vitreous gel catalyst comprising not less than live per cent of chromium oxide and at least flve per cent of aluminum oxide, the said oxides having been combined in a state of intimate association effected while the oxides are in a highly hydrous condition.
  • a process tor the non-destructive dehydrogenation of aliphatic hydrocarbons of at least two carbon atoms per molecule to corresponding hydrocarbons of lower hydrogen content which comprises contacting said aliphatic hydrocarbons under dehydrogenation conditions with a vitreous gel catalyst comprising not less than five percent of chromium oxide and at least five per cent 1 two carbon atoms per molecule to corresponding o! zirconium oxide, the said oxides having been combined in a state of intimate association ei-' iected while the oxides are in a highly hydrous condition.
  • a process for the non-destructive dehydrogenation of aliphatic hydrocarbons of at least hydrocarbons of lower hydrogen content which comprises contacting said aliphatic hydrocarbons under dehydrogenation conditions with a vitreous gel catalyst comprising not less than five percent oi. chromium oxide and at least five per cent or magnesium oxide, the said oxides having been combined in a state of intimate association ei-' Iected while the oxides are in a highly hydrous condition.
  • a process for the non-destructive dehydrogenation of aliphatic hydrocarbons of at least two carbon atoms per molecule to corresponding hydrocarbons of lower hydrogen content which comprises contacting said aliphatic hydrocarbons under dehydrogenation conditions with a vitreous gel catalyst comprising chromium oxide and aliuninum oxide in a molar ratio of about one to one, the said oxides having been combined in a state of intimate association eilfected while the oxides are in a highlyhydrous condition.
  • a process for the non-destructive dehydrogenation of aliphatic hydrocarbons of at least two carbon atoms per molecule to corresponding hydrocarbons of lower hydrogen content which comprises contacting. said aliphatic hydrocarbons under dehydrogenation conditions with a vitreous gel catalyst comprising chromium oxide and aluminum oxide in a molar ratio oi. about one to one together with about two mol per cent of thallium oxide, the said oxides having been combined in a state of intimate association effected while i the oxides are in a highly hydrous condition.
  • a process for the non-destructive dehydrogenation of aliphatic hydrocarbons or at least two carbon atoms per molecule to corresponding hydrocarbons or lower hydrogen content which comprises contacting a butane under dehydrogenation conditions with a vitreous gel catalyst comprising chromium oxide and aluminum ox-f,- ide in a molar ratio of about one to one, the'said oxides havin been combined in a state of intimate association efiected while the oxides are in g FREDERICK E. FREY. WALTER F. HUPPKE.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
  • Low-Molecular Organic Synthesis Reactions Using Catalysts (AREA)

Description

Reizsued Sept. 30, 1941 p PROCESS FOR CONVERTING HYDRO- CARBONS Frederick E. Frey, Bartlesville, kla., and Walter F. Huppke, Lomita, CaliL, assignors to Phillips Petroleum Company, Bartlesville, 0kla., a corporation of Delaware No Drawing. Original No. 2,098,959, dated November 16, 1937, Serial No. 723,608, May 2, 1934. Application for reissue December 18, 1940, Se-
rial No. 370,736
12 Claims.
This invention relates to processes wherein saturated hydrocarbons are converted into oleflns by catalytic dehydrogenation at elevated temperatures, the nature of the catalyst and the conditions of the conversion being such as to effect simple dehydrogenation of the saturated into the corresponding unsaturated hydrocarbon with very slight decomposition of the usual kind wherein the carbon chain breaks and smaller molecules are formed.
Catalytic dehydrogenation is widely applied to organic compounds, more particularly to alcohols and hydrocarbons. The dehydrogenation of alcohols is readily effected at low temperatures in the presence of various catalytic metas and metallic oxides. That class of hydrocarbons containing the hexamethylene ring may be dehydrogenated in a characteristic manner into the corresponding aromatic hydrocarbons by a small group of catalysts comprising the most active of the hydrogenation catalysts. Both alcohols and hexamethylene hydrocarbons can be successfully dehydrogenated to yield molecular hydrogen and the corresponding, dehydrogenation product at moderate temperatures, which need not exceed 300 C. The parafiln hydrocarbons, on the other hand, cannot be dehydrogenated at such low temperatures because of the unfavorable thermodynamic relationships. Temperatures in the range 450 to 600 C. are required to obtain high extents of conversion and while temperatures somewhat below 400 C. will give a measurable dissociation, a prohibitively low pressure or other artifice must be resorted to if extensive conversion, exceeding ten per cent or so is to be effected. In this higher temperature range ordinary decomposition or cracking will take place in the absence of a catalyst to yield smaller molecules by fracture of the carbon chain, and furthermore a protracted exposure to such temperatures will lead to the formation of tar and carbon which will deposit on any catalytic surfaces present and destroy their effectiveness. For these reasons an effective dehydrogenation catalyst for paratfins specifically must meet certain requirements not called for in the other cases. The activity must be high toallow the dehydrogenation to be accomplished in a time so short that cracking is not marked; the active nature of the surface must not be destroyed by the hightemperatures; the composition and mechanical structure of the catalyst should discourage tar and carbon'iormation. Nickel, platinum, and palladium comprise the .efiective catalysts for dehydrogenating hexamethylene hydrocarbons but these tail under the conditions required for parafiins. Many other substances have been suggested for the dehydrogenation of paraflins which fail in one or more respects. Many difficultly reducible oxides, such as zinc oxide, magnesia, chromic oxide and others prepared in ordinary ways, show high dehydrogenating activity when applied to alcohols, but exhibit little or no dehydrogenating activity when applied to parafiins. The ultimate mechanism of the reaction is probably quite different from that of the alcohol dehydrogenation. The objectives to be achieved by the use of mix tures as catalysts are far from parallel for thetwo fields of catalysts and the most effective compositions for the two purposes are widely different.
In U. S, Patent 1,905,383, there has been described the use of chromium oxide in the form of a hard dark colored vitreous gel for the purpose of dehydrogenating parafiins. This catalyst is highly active in the useful temperature range. The activity falls off during use and can be restored by heating to 400-550 C. in an oxygen containing gas which effects oxidation of deposited tar and carbon. At 550 to 600" C. however it passes over into the common inert form of chromic oxide; the activity is lost and cannot be restored by the oxygen treatment. At somewhat lower temperatures the transformation requires one or more days but ultimately takes place within the elevated temperature range-useful in practice for obtaining high conversions. We have discovered that the addition of certain diffi-" cultly reducible oxides having little dehydrogenation activity in themselves will delay or prevent the transformation of chromium oxide into the inactive form at temperatures within the Working range. Most effective we have found to be the infusible oxides, alumina, zirconia, thorium oxide, silicon dioxide, boric oxide, magnesium oxide and titanium dioxide incorporated in the chromium oxide in such a way that the gel characteristics are conserved. This may be accomplished by precipitating together from aqueous solution the gelatinous hydrous oxides of chromium and one or more of the elements named. The two more meta lic salts may be dissolved together in water and the hydrous oxides precipitated by an excess of alkali, preferably ammonium, sodium or potassium hydroxide. amount of acetic acid prior to precipitation assists .in maintaining the gel structure during the subsequent drying of the precipitate. Titanium dioxide, boric oxide and silicon dioxide are of an acidic nature and are'best introduced in the form The addition of a small of their alkali salts in aqueous solution. Such a solution may be introduced into the alkali solu tion used for the precipitation before the solution of thecliromium -or other salts is introduced, or
effect stabilization to heat. Higher proportions impart greater stability but a proportion-so great as to reduce the chromium oxide content'to below five per cent is usually undesirable since the activity is unduly decreased. Th gelatinous precipitate obtained by this procedure is washed with water, dried slowly in air, granulated, and finally heated to reaction temperature. Prepared in this way, the catalyst is obtained in hard glass granules. the heating prior to use in a stream of hydrogen whereupon some reduction of the chromium oxides is effected with formation of water.
The catalyst prepared in this way may be supported in a suitable container and the saturated hydrocarbon to be dehydrogenated passed over the catalyst while a suitable reaction temperature of preferably 450-550" C. is maintained.
The chromium oxide gel thus stabilized by the addition of a diiilcultly reducible oxide will lose activity during use, but the activity can be restored repeatedly by passing over the catalyst for a short time an oxygen containing gas 'while maintaining a temperature of 400-550 C. During the decay in activity, tar and carbon form in the catalyst granules and it is probably to this that the loss in activity must be attributed. We have found that the addition of small amounts of certain heavy metal oxides incorporated in the catalyst will bring about a decrease in the rate at which activityis lost and the rate at which carbon forms. 'I'hallium and bismuth oxides are most effective, lead and mercury oxides less so. Since these oxides are readily reduced, they are no doubt finely distributed, for the most part, in the metallic form in the catalyst during use. The heavy metal oxides are incorporated in the catalyst most conveniently by adding a soluble salt of the metal, preferably the nitrate to the chromium salt prior to dissolving and precipitating It is preferable to 'perform The gelatinous precipitate of the mixed hydrous I the hydrous oxides as described. Large proportions of the heavy metal oxides cannot be introduced without loss of the coherent gel structure. Usually less than 20 mol. per cent should be incorporated in the catalyst and an addition of 0.5 to 5 per cent will produce a great lessening in decay of activity during continued dehydrogenation.
The improved catalysts are effective for converting not only parailins but also alicyclic or aromatic hydrocarbons containing alkyl substituent groups of two or more carbon atoms into the corresponding unsaturated hydrocarbons of the same number of carbon atoms per molecule but of lower hydrogen content. Oleilns containing at least four carbon atoms per molecule can similarly be converted into diolefins. Temperatures in the range 300 to 600 C. give best results. The reaction rate with the catalysts described is high and equilibrium extent of dissociation is readily attained. We have found that the lower temperatures at which equilibrium dishibit good activity at low hydrogen resist poisoning by sulfur compounds.
sociation is small may be used at the lower pressures which favor dissociations, or when treating the higher molecular weight hydrocarbons, for which the thermodynamic equilibrium dissociaw tion. is large at the lower temperatures. The dissociation is repressed by high pressures, and pressures exceeding a few atmospheres are accordingly undesirable. Pressures in the neighborhood of atmospheric give good results, and pressures below atmospheric permit still greater dissociation.
Where the catalysts are used to eii'ect hydrogenation of olefins or diolefins, temperatures of 200 to 500C. may be used, preferably the lower temperaturesand a high partial pressure of hydrogen and pressures above atmospheric are desirable but not necessary. These catalysts expressures and Example 1.An aqueous solution of chromic nitrate and aluminum nitrate containing the salts in the molar ratios of one to one was introduced into an excess of dilute aqua ammonia.
oxides was then washed with water thoroughly, filtered off, dried slowly in air to a glassy gel and granulated. A 5 cc. portion of the granular gel was supported in a catalyst tube and a stream of n-butane passed over it at rate of ten liters per hour while the temperature was maintained at 450 C. A 12 per cent conversion into butenes plus hydrogen was obtained. The activity decayed during use; the conversion fell to 6 per cent during 14 hours. The flow of butane was interrupted, the catalyst treated with oxygen at 450 C. and the catalyst was found to have been restored to original activity. The catalyst was used and restored to original activity in this way many times. A chromium oxide gel containing no added metals or other oxides which was used and reactivated in the same way suffered a serious loss in activity after two reactivations by oxygen.
Example 2.--A chromium oxide-aluminum oxide gel was prepared as in Example 1 except that 2 mol. per cent of thallium nitrate was incorporated in the solution of the other metallic salts. The conversion of butane, carried out in the same way,
proceeded for 72 hours before extent of conversion.
fell to 6 percent and the catalyst was successfully reactivated many times by oxygen.
Having described our invention, what we claim 1. A process for the non-destructive dehydrogenating of aliphatic hydrocarbons of at least two carbon atoms per molecule to corresponding hydrocarbons of lower hydrogen content, which comprises contacting said aliphatic hydrocarbons bons are contacted with a catalyst comprising chromium oxide vitreous gel at elevated temperatures, the method of rendering said chromium oxide gel thermostable, which comprises incorporating in intimate association therewith a difficultly reducibleoxide of the group aluminum, zirconium, titanium, silicon, thorium, boron, and
hydrocarbons to produce corresponding hydrocarbons of lower hydrogen-carbon ratio, the steps which comprise passing the hydrocarbon over a vitreous gel catalyst consisting of chromium oxide together with a diiilcultly reducible oxide of the group aluminum, zirconium, titanium, silicon, thorium, boron, and magnesium, the said oxides having been combined in a state of intimate admixture, effected while in a highly hydrous condition, continuing such passage until the activity of said catalyst becomes reduced, and restoring the activity of the said catalyst by bringing it at an elevated temperature into contact with a gas containing free oxygen.
4. In a process for. dehydrogenating aliphatic hydrocarbons to produce corresponding hydrocarbons of lower hydrogen-carbon ratio, the step which comprises passing the hydrocarbon at a reaction temperature in contact with a vitreous gel catalyst comprising chromium oxide together with a difiicultly reducible oxide of the group aluminum, zirconium, titanium, silicon, thorium, boron and magnesium, the said oxides having been combined in a state of intimate association effected while in a highly hydrous condition and having added also at least one-half per cent of a readily reducible oxide of the group thallium, bismuth, lead and mercury.
5. A process for the non-destructive dehydrogenation of aliphatic hydrocarbons of at least two carbon atoms per molecule to corresponding hydrocarbons of lower hydrogen content, which comprises contacting said aliphatic hydrocarbons under dehydrogenation conditions with a vitre ous gel catalyst comprising not less than live per cent of chromium oxide and at least five per cent of a difflcultly reducible oxide or the group aluminum, zirconium, titanium, silicon, thorium, boron, and magnesium, the said oxides having been combined in a state of intimate association effected while the oxides are in a highly hydrous condition. y
6. A process for the non-destructive dehydrogenation of aliphatic hydrocarbons of at least two carbon atoms per molecule to corresponding hydrocarbons of lower hydrogen content, which comprises contacting said aliphatic hydrocarbons under dehydrogenation conditions with a vitreous gel catalyst comprising not less than live per cent of chromium oxide and at least flve per cent of aluminum oxide, the said oxides having been combined in a state of intimate association effected while the oxides are in a highly hydrous condition.
'1. A process tor the non-destructive dehydrogenation of aliphatic hydrocarbons of at least two carbon atoms per molecule to corresponding hydrocarbons of lower hydrogen content, which comprises contacting said aliphatic hydrocarbons under dehydrogenation conditions with a vitreous gel catalyst comprising not less than five percent of chromium oxide and at least five per cent 1 two carbon atoms per molecule to corresponding o! zirconium oxide, the said oxides having been combined in a state of intimate association ei-' iected while the oxides are in a highly hydrous condition.
8. A process for the non-destructive dehydrogenation of aliphatic hydrocarbons of at least hydrocarbons of lower hydrogen content, which comprises contacting said aliphatic hydrocarbons under dehydrogenation conditions with a vitreous gel catalyst comprising not less than five percent oi. chromium oxide and at least five per cent or magnesium oxide, the said oxides having been combined in a state of intimate association ei-' Iected while the oxides are in a highly hydrous condition.
, I 9. A process for the non-destructive dehydrogenation of aliphatic hydrocarbons of at least two carbon atoms per molecule to corresponding hydrocarbons of lower hydrogen content, which comprises contacting said aliphatic hydrocarbons under dehydrogenation conditions with a vitreous gel catalyst comprising chromium oxide and aliuninum oxide in a molar ratio of about one to one, the said oxides having been combined in a state of intimate association eilfected while the oxides are in a highlyhydrous condition.
10. A process for the non-destructive dehydrogenation of aliphatic hydrocarbons of at least two carbon atoms per molecule to corresponding hydrocarbons of lower hydrogen content, which comprises contacting. said aliphatic hydrocarbons under dehydrogenation conditions with a vitreous gel catalyst comprising chromium oxide and aluminum oxide in a molar ratio oi. about one to one together with about two mol per cent of thallium oxide, the said oxides having been combined in a state of intimate association effected while i the oxides are in a highly hydrous condition.
11. A process for the non-destructive dehydrogenation of aliphatic hydrocarbons or at least two carbon atoms per molecule to corresponding hydrocarbons or lower hydrogen content, which comprises contacting a butane under dehydrogenation conditions with a vitreous gel catalyst comprising chromium oxide and aluminum ox-f,- ide in a molar ratio of about one to one, the'said oxides havin been combined in a state of intimate association efiected while the oxides are in g FREDERICK E. FREY. WALTER F. HUPPKE.
US21911D Process for converting hydro Expired USRE21911E (en)

Publications (1)

Publication Number Publication Date
USRE21911E true USRE21911E (en) 1941-09-30

Family

ID=2088036

Family Applications (1)

Application Number Title Priority Date Filing Date
US21911D Expired USRE21911E (en) Process for converting hydro

Country Status (1)

Country Link
US (1) USRE21911E (en)

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2638455A (en) * 1948-06-14 1953-05-12 Phillips Petroleum Co Alumina-metal oxide dehydrogenation catalyst and its preparation

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2638455A (en) * 1948-06-14 1953-05-12 Phillips Petroleum Co Alumina-metal oxide dehydrogenation catalyst and its preparation

Similar Documents

Publication Publication Date Title
US2184235A (en) Catalytic dehydrogenation of organic compounds
US3651167A (en) Selective hydrogenation of c4-acetylenic hydrocarbons
US3168587A (en) Method of dehydrogenation
CA1240709A (en) Selective oxidation of hydrogen
US3485887A (en) Process for the treatment by hydrogenation of c4-hydrocarbons containing butadiene and n-but-1-ene
US2408140A (en) Dehydrogenation catalyst
US3128317A (en) Selective hydrogenation of acetylene in ethylene with a zeolitic catalyst
US2927141A (en) Catalyst for the selective hydrogenation of acetylene
US2718535A (en) Hydroisomerization of hydrocarbons
US2231446A (en) Treatment of hydrocarbons
Farkas Part. II.—Catalytic reactions of hydrocarbons. The activation of hydrogen in catalytic reactions of hydrocarbons
US2098959A (en) Processes for converting hydrocarbons
US2426118A (en) Process for the catalytic dehydrogenation of hydrocarbons
US3200167A (en) Process for the removal of acetylenic hydrocarbons by selective catalyst hydrogenation
US2337190A (en) Cyclization of hydrocarbons
US2337191A (en) Dehydrogenation process
US3409702A (en) Catalytic olefin isomerization process
US3274286A (en) Process for the removal of acetylenic hydrocarbons from hydrocarbon mixtures containing diolefines
US4812597A (en) Dehydrogenation of dehydrogenatable hydrocarbons
USRE21911E (en) Process for converting hydro
US3555106A (en) Process for selective hydrogenation of acetylenic hydrocarbons in a diolefinic hydrocarbon fraction,and catalyst therefor
US2909578A (en) Hydrogenation of acetylene
US2814650A (en) Process of treating dehydrogenationhydrogenation catalysts
US2098960A (en) Processes for converting hydrocarbons
US2483929A (en) Catalytic hydrocarbon conversion