US2908636A - Hydroforming process - Google Patents

Hydroforming process Download PDF

Info

Publication number
US2908636A
US2908636A US555353A US55535355A US2908636A US 2908636 A US2908636 A US 2908636A US 555353 A US555353 A US 555353A US 55535355 A US55535355 A US 55535355A US 2908636 A US2908636 A US 2908636A
Authority
US
United States
Prior art keywords
catalyst
chlorine
platinum
hydroforming
vessel
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
US555353A
Other languages
English (en)
Inventor
Steffgen Frederick Williams
Jr Charles Newton Kimberlin
Fred J Buchmann
Jr Alexis Voorhies
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.)
ExxonMobil Technology and Engineering Co
Original Assignee
Exxon Research and Engineering Co
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
Priority to NL212345D priority Critical patent/NL212345A/xx
Priority to FR1135954D priority patent/FR1135954A/fr
Application filed by Exxon Research and Engineering Co filed Critical Exxon Research and Engineering Co
Priority to US555353A priority patent/US2908636A/en
Priority to GB33836/56A priority patent/GB796310A/en
Priority to FR70853D priority patent/FR70853E/fr
Application granted granted Critical
Publication of US2908636A publication Critical patent/US2908636A/en
Anticipated expiration legal-status Critical
Expired - Lifetime legal-status Critical Current

Links

Images

Classifications

    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G35/00—Reforming naphtha
    • C10G35/04—Catalytic reforming
    • C10G35/10—Catalytic reforming with moving catalysts
    • C10G35/14—Catalytic reforming with moving catalysts according to the "fluidised-bed" technique
    • 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
    • B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
    • B01J23/90—Regeneration or reactivation
    • B01J23/96—Regeneration or reactivation of catalysts comprising metals, oxides or hydroxides of the noble metals
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G35/00—Reforming naphtha
    • C10G35/04—Catalytic reforming
    • C10G35/06—Catalytic reforming characterised by the catalyst used
    • C10G35/085—Catalytic reforming characterised by the catalyst used containing platinum group metals or compounds thereof

Definitions

  • Hydroforming is usually applied to a rather wide boiling range, naphtha, i.e. having a boiling range of from about 125 F. to about 400-430 F. It has been know that the lower boiling naphthas are not substantially improved by hydroforming processes as ordinarily conducted.
  • the extensive article on Hydrofonning in Petroleum Processing for August 1955 states at page 1174, Optimum reformer utilization is obtained by not using feed stock constituents boiling much below 200 F which do not contribute greatly to increased octane during reforming as these merely take up reformer capacity better used for high boiling materials more susceptible to octane upgrading. In view of the continuing demand for more and higher octane number gasolines however, it is becoming increasingly important to upgrade these lower boiling fractions.
  • the fraction boiling above 200 F. up to about 225 F. or 250 F. responds fairly well to the conventional hydrofroming processes employing either molybdena or platinum catalysts at about 200 p.s.i.g. or higher and may be included in the feed to such processes if desired.
  • this fraction also responds well to the present low pressure platinum process so that the method of handling this particular fraction of the virgin naphtha feed will depend upon circumstances such as the availablity of equipment and the volumes of the difierent boiling range fractions which it is desired to process.
  • a halogen or halogen compound such as chlorine or hydrogen chloride.
  • a freehalogen such as chlorine is the preferred treating agent for reactivation.
  • the deactivation of platinum hydroforming catalysts proceeds by two mechanisms, viz., (1) the loss of chlorine or other halogen that is normally present as a part of the catalyst composition and that contributes substantially to the catalytic activity, and (2) the agglomeration of the platinum metal into relatively large or massive crystals having crystal diameters in excess of about 50 :angstrom units.
  • Treatment of the catalyst with a halogen compound such as hydrogen chloride or the like is effective in restoring the halogen content of the catalyst to the desired value and to this extent is effective in restoring the activity of deactivated or partly deactivated catalysts.
  • treatmen with a halogen compound such as hydrogen chloride or the like is not effective for the reduction of the size of platinum crystals; therefore such treatment is only partially and not entirely effective in restoring the catalytic activity of deactivated catalysts.
  • treatment of the catalyst with an elementary halogen such as chlorine or the like not only restores the catalyst halogen content to the desired level but also ac- -complishes the redispersion of the platinum metal by breaking up the large platinum crystallites. This treatment, therefore, is entirely effective in restoring the activity to deactivated catalysts whose activity loss was not due to the accumulation of poisons such as arsenic or the like.
  • 10 represents a reactor vessel containing a fluidized bed 12 of catalyst comprising 0.01 to 1.0 wt. percent platinum and/or 0.1 to 2.0 Wt. percent palladium.
  • a suitable catalyst comprises about 0.1 to 0.6 wt. percent platinum widely dispersed on a high surface area alumina support, having a surface area of about 150 to 220 square meters per gram.
  • a preferred catalyst is one comprising a mixture of one part of a platinum catalyst concentrate consisting of 0.3 to 2.0 wt. percent platinum on alumina microspheres formed by spray drying an alcoholate alumina hydrosol mixed with sufficient unplatinized alumina to form a catalyst composition containing about 0.01 to 0.2 wt. percent platinum.
  • the pressure in vessel 10 may be in the range of to 125 p.s.i.g., and is preferably about 50 p.s.i.g.
  • the temperature of catalyst bed 12 may be in the range of about 800 to 975 F.; however, under the conditions of low pressure and low recycle hydrogen rates of the present invention, the dehydrogenation activity of platinum metal catalysts is extremely high, so that the reaction temperature may be somewhat lower than that of the prior art hydroforming processes.
  • a preferred temperature is in the range of 875 to 950 F.
  • Light virgin naphtha feed having a boiling range of from 110250 F., preferably 150 to 225 F. is preheated in heater 14 and passed by line 16 into the lower section of reactor 10.
  • the naphtha feed is preheated in heater 14- to a temperature in the range of 900 to 1050 F., preferably about 975 F. to 1000 F.
  • Recycled hydrogen which has been preheated to 900 to 1300 F., preferably about 1200 F., in heater 18 and which bears freshly regenerated and reactivated catalyst from lines 52 and 57, is also introduced into the lower section of reactor by line 20.
  • the naphtha feed from line 17 may be mixed with the recycle gas in line 32, and the combined stream preheated in heater 18; in this case the preferred preheat temperature is in the range of 900 to 1000 F.
  • the recycle gas, or recycle hydrogen normally contains about 65 to 90 mol percent hydrogen with the remainder being light hydrocarbon gases; the exact composition of the recycle gas depends upon the hydroforming conditions maintained in reactor 10 and upon the pressure and temperature at which the gas is separated from the liquid products.
  • the amount of recycle gas employed may be in the range of about 500 to 5000, preferably about 1000 to 3000 standard cubic feet per barrel of naphtha feed (s.c.f./b.).
  • the additional heat load required by the endothermic hydroforming reaction may be supplied to eatalyst bed 12 by heating coil 15 immersed therein. Hot flue gases, mercury, Dowtherm or the like may be passed through coil 15. Other means of supplying heat to eatalyst bed 12, for example, by circulating a stream of catalyst through coils in a furnace, are within the scope of the invention.
  • the naphtha vapor and recycled gas pass upwardly through catalyst bed 12 whereupon the naphtha is hydroformed. After leaving catalyst bed 12 the hydroformed vapor and gas is passed through conventional catalyst recovery equipment, such as a cyclone separator or filter, or the like, and through line 22 and condenser or cooler 24 into gas-liquid separator 26.
  • the hydroformed naphtha product is removed from the system by line 28.
  • the excess gaseous product is removed from the system by line 30 and the remainder of the gas is recycled by line 32.
  • Catalyst from bed 12 passes into standpipe 34 where it is stripped of adsorbed hydrocarbons by hydrogen from line 36.
  • Stripped catalyst from standpipe 34 passes into line 38 where it is picked up by a stream of air and transported to regenerator 40.
  • Regenerator 40 which is a relatively small vessel because of the low rate of coke formation on platinum and palladium catalysts, is maintained at a temperature of 900 to ]200 F., preferably, 1000 to 1100 F.
  • the pressure in regenerator 40 is approximately the same as that in reactor 10.
  • coke deposits are burned from the catalyst by air introduced by line 38.
  • a certain amount of water is formed by combustion of the hydrogen in the coke; this is stripped from the catalyst and passes overhead with the flue gases through conventional catalyst recovery means, such as a cyclone separator or filter, or
  • regenerator 40 Since for the subsequent chlorine reactivation, presently to be described, a completely regenerated or coke-free catalyst is desired, it is preferred to employ an excess of air in regenerator 40; the oxygen content of the flue gas in line 42 should be above 2%, and is preferably above 5%.
  • Regenerated catalyst passes by line 44 into the upper section of chlorine reactivator vessel 46. Since it is desired to maintain substantially anhydrous conditions in reactivator vessel 46, water vapor is further stripped from the catalyst passing through line 44 by means of air introduced by line 48.
  • Reactivator vessel 46 which may be comparatively small in cross-sectional area compared to its height, is preferably maintained at the same pressure and temperature as regenerator 40.
  • Chlorine gas or a mixture of chlorine gas in air is introduced into vessel 46 near the midsection thereof by line 50 and air is introduced into vessel 46 near the bottom thereof by line 54.
  • the air and chlorine pass upwardly through vessel 46 and are removed from the system. by line 45, .while catalyst from line 44 passes downwardly through vessel 46.
  • the upper section of reactivator vessel comprises a chlorine treating zone wherein regenerated (i.e., coke-free) catalyst is contacted with a mixture of chlorine gas and air
  • the lower section of reactivator vessel 46 comprises a stripping zone wherein adhering chlorine is stripped from the treated catalyst by means of air.
  • chlorine treating zone of vessel 46 the chlorine partial pressure may be in the range of about 0.001 to 2 atmospheres, preferably, about 0.01 to 1 atmosphere.
  • the quantity of chlorine admitted to vessel 46 by line 50 may be in the range of 0.1 to 2.0
  • the temperature and total (air plus chlorine) pressure in the chlorine treating zone is preferably about the same as the temperature and pressure in regenerator vessel 40.
  • the residence time of the catalyst in the chlorine treating zone may be in the range of seconds to 1 hour, preferably, about 1 to 15 minutes.
  • the action of the chlorine treatment on the catalyst is to destroy large platinum crystals and re-disperse the metal over the catalyst surface of the base or support, thus completely restoring the activity of the catalyst to that of fresh catalyst.
  • the chlorine treated catalyst descends from the upper chlorine treating zone of vessel 46 into the lower stripping zone of vessel 46, adhering clhorine is stripped from the catalyst by air fro-m line 54.
  • the quantity of chlorine remaining on the stripped catalyst may be controlled by the amount of air introduced into the stripping zone by line 54 and the partial pressure of the chlorine employed in the chlorine treating zone.
  • the amount of chlorine which it is desirable to have remaining on the stripped catalyst is related to the platinum content of the catalyst. With high platinum content catalysts, a relatively high chlorine content is desirable; a correspondingly lower chlorine content is desirable for lower platinum contents.
  • the total amount of chlorine (i.e., both chemically combined and adsorbed chlorine) remaining on the stripped catalyst when employing a catalyst of 0.6% platinum content may be in the range of about 0.2 to 1.25 wt. percent, and is preferably about 0.5 to 1.0 wt. percent.
  • the amount of chlorine remaining on the stripped catalyst may be proportionally lower when employing a lower platinum content catalyst.
  • the reactivated and stripped catalyst passes from vessel 46 by line 52 into line where it is picked up by recycle gas or by a mixture of recycle gas and naphtha feed and transported to reactor vessel 10 as hereinbefore set forth.
  • Aromatics volume percent 2.2. Sulfur 0.03 wt. percent.
  • Conditions in chlorine treater Temperature 1050 F. Pressure -L. 50 p.s.i.g. Residence time 5 minutes. Composition of treating gas 11% chlorine in air. Chlorine partial pressure About 0.5 atmosphere. Duration of air treat following chlorine treat 10 minutes. Wt. percent chlorine on stripped catalyst About 0.85.
  • the temperature in the hydroforming zone may vary from 800 to 975 F.
  • the pressure may vary from atmospheric to about 125 p.s.i.g., the length of each productive phase of the complete process cycle, including regeneration and chlorine treatment may vary from 1 to hours.
  • the catalyst composition may vary from one containing .01% of platinum to one containing 1% by weight of platinum, the remainder being a suitable support.
  • palladium may be used in place of platinum as the active hydrogenationdehydrogenation component of the catalyst, but pallidium must be used in about three times. the amount of platinum for similar results.
  • the amount of chlorine in the treating gas may vary from a chlorine partial pressure of about 0.001 atmosphere to a chlorine partial pressure of about 2 atmospheres, and that it will not be necessary to treat the catalyst during every cycle.
  • An examination of the regenerated catalyst periodically to determine average platinum crystallite size will determine whether or not it is necessary to increase the proportion of the catalyst being treated with the chlorine-containing gas. If the average crystallite size is above about or 75 A. units as determined by X-ray examination, then the proportion of the catalyst flowing through the chlorine treatment zone described above should be increased and the proportion of catalyst bypassing this zone should be decreased. It is important to note in connection with the chlorine treatment that the catalyst should be substantially free of water. In otherwords, the catalyst should be substantially free of water when subjected to chlorine treatment for best results.
  • the present invention relates to improvements in hydroforming light naphthas in the presence of a platinum group metal.
  • the present invention provides a process for the octane number improvement of light naphthas boiling in the range of about 110 to 250 F. and it is particularly adapted to the octane number improvement of naphtha fractions boiling in the range of about 150 to 200 F. Heavier naphthas boiling above about 250 F. up to about 430 F. may also be processed according to the present invention, although there is no particular advantage in doing so.
  • the heavier naphthas are generally more advantageously hydroformed by the conventional high pressure hydroforming processes using either platinum or molybdena catalysts and operating at pressures of about 20 pounds per square inch or higher.
  • the heavier naphthas respond well to the conventional hydroforming processes and at the higher pressures employed less coke is deposited on the catalyst and the rate of catalyst deactivation is less with these heavy feeds.
  • the present improvements comprise employing the fluidized catalyst technique, and it is further characterized in that the process is operated at relatively low pressures, low hydrogen recycle rates and short time on-stream pefiods. It has been discovered that the catalyst which is fouled during the on-stream phase cannot successfully be regenerated with air alone, nor can it be satisfactorily reactivated by subjecting the catalyst to a prolonged soaking in air at elevated temperatures and pressures, following the removal of deactivated deposits by oxidative re- It has been discovered, however, that the spent catalyst may be restored to a high level of activity by subjecting it first to oxidative regeneration and then subjecting it to the influence of a chlorine-containing gas for a short period of time. The chlorine treatment of the regenerated catalyst need not be performed during each cycle.
  • the platinum group metal particles are formed into large crystals as a result of use in the process.
  • the volatility of the hydroformate may be adjusted to the desired level by control of the amount of chlorine remaining on the catalyst after treatment with chlorine and stripping with air.
  • chlorine may be driven off possibly by the action of water either in the feed or formed during the process or during the regeneration of the catalyst.
  • the results of tests clearly dictate that the air regenerable platinum catalyst must be at least intermittently treated with the chlorine-containing gas following regeneration in order to maintain the activity and selectivity of the said catalyst at a high level.
  • a method for hydroforming virgin petroleum naphtha fractions boiling in the range of from about 150 to 225 P. which comprises contacting said fractions in admixture with a hydrogen-rich gas with a fluidized bed of finely divided platinum on alumina catalyst particles in a reaction zone at a temperature of 800 to 975 F.
  • the catalyst comprises 0.3 to 2.0 wt. percent platinum on alumina diluted to 0.01 to 0.2 wt. percent platinum with unplatinized alumina.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Organic Chemistry (AREA)
  • General Chemical & Material Sciences (AREA)
  • Materials Engineering (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
  • Catalysts (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
US555353A 1955-12-27 1955-12-27 Hydroforming process Expired - Lifetime US2908636A (en)

Priority Applications (5)

Application Number Priority Date Filing Date Title
NL212345D NL212345A (xx) 1955-12-27
FR1135954D FR1135954A (fr) 1955-12-27 1955-08-31 Procédé d'hydroreformation
US555353A US2908636A (en) 1955-12-27 1955-12-27 Hydroforming process
GB33836/56A GB796310A (en) 1955-12-27 1956-11-06 Improved hydroforming process
FR70853D FR70853E (fr) 1955-12-27 1956-11-29 Procédé d'hydroreformation

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
US555353A US2908636A (en) 1955-12-27 1955-12-27 Hydroforming process

Publications (1)

Publication Number Publication Date
US2908636A true US2908636A (en) 1959-10-13

Family

ID=24216938

Family Applications (1)

Application Number Title Priority Date Filing Date
US555353A Expired - Lifetime US2908636A (en) 1955-12-27 1955-12-27 Hydroforming process

Country Status (4)

Country Link
US (1) US2908636A (xx)
FR (2) FR1135954A (xx)
GB (1) GB796310A (xx)
NL (1) NL212345A (xx)

Cited By (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3496096A (en) * 1969-03-12 1970-02-17 Chevron Res Regenerating a platinium-rhenium reforming catalyst
EP0021854A1 (en) * 1979-07-02 1981-01-07 Exxon Research And Engineering Company Process for reforming hydrocarbons in a magnetically stabilized bed of fluidized, magnetizable reforming catalyst, and reformed hydrocarbon product
US5053371A (en) * 1990-11-02 1991-10-01 Uop Catalyst regeneration method with three-zone combustion gas addition
US5151392A (en) * 1989-12-11 1992-09-29 Uop Moving bed regeneration process with separate dispersion and chloriding steps
US5397458A (en) * 1993-12-27 1995-03-14 Uop Moving bed regeneration process with internally mixed chloride gas
US5457077A (en) * 1993-12-30 1995-10-10 Uop Moving bed regeneration process with combined drying and dispersion steps
US5824619A (en) * 1994-05-12 1998-10-20 Uop Particulate cooling process with reduced thermal channeling
JP2011032333A (ja) * 2009-07-30 2011-02-17 Chiyoda Kako Kensetsu Kk 連続式流動接触芳香族製造プラントの運転方法

Citations (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2373254A (en) * 1942-05-09 1945-04-10 Universal Oil Prod Co Catalytic reforming
US2479110A (en) * 1947-11-28 1949-08-16 Universal Oil Prod Co Process of reforming a gasoline with an alumina-platinum-halogen catalyst
US2587425A (en) * 1949-04-30 1952-02-26 Standard Oil Dev Co Reforming naphtha with activated carbon catalyst
US2636865A (en) * 1948-11-19 1953-04-28 Standard Oil Dev Co Preparation of alumina from higher alcoholates of aluminum
US2642384A (en) * 1949-07-22 1953-06-16 Universal Oil Prod Co Process for reforming of hydrocarbons boiling within the gasoline range utilizing a platinum-alumina-halide catalyst
US2689208A (en) * 1951-01-31 1954-09-14 Universal Oil Prod Co Hydrocarbon conversion process
US2746909A (en) * 1955-01-31 1956-05-22 Exxon Research Engineering Co Hydroforming
US2758063A (en) * 1951-10-01 1956-08-07 Exxon Research Engineering Co Method of regenerating hydroforming catalysts
US2816857A (en) * 1951-05-01 1957-12-17 Exxon Research Engineering Co Fluid hydroforming process with regeneration of the platinum containing catalyst

Patent Citations (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2373254A (en) * 1942-05-09 1945-04-10 Universal Oil Prod Co Catalytic reforming
US2479110A (en) * 1947-11-28 1949-08-16 Universal Oil Prod Co Process of reforming a gasoline with an alumina-platinum-halogen catalyst
US2636865A (en) * 1948-11-19 1953-04-28 Standard Oil Dev Co Preparation of alumina from higher alcoholates of aluminum
US2587425A (en) * 1949-04-30 1952-02-26 Standard Oil Dev Co Reforming naphtha with activated carbon catalyst
US2642384A (en) * 1949-07-22 1953-06-16 Universal Oil Prod Co Process for reforming of hydrocarbons boiling within the gasoline range utilizing a platinum-alumina-halide catalyst
US2689208A (en) * 1951-01-31 1954-09-14 Universal Oil Prod Co Hydrocarbon conversion process
US2816857A (en) * 1951-05-01 1957-12-17 Exxon Research Engineering Co Fluid hydroforming process with regeneration of the platinum containing catalyst
US2758063A (en) * 1951-10-01 1956-08-07 Exxon Research Engineering Co Method of regenerating hydroforming catalysts
US2746909A (en) * 1955-01-31 1956-05-22 Exxon Research Engineering Co Hydroforming

Cited By (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3496096A (en) * 1969-03-12 1970-02-17 Chevron Res Regenerating a platinium-rhenium reforming catalyst
EP0021854A1 (en) * 1979-07-02 1981-01-07 Exxon Research And Engineering Company Process for reforming hydrocarbons in a magnetically stabilized bed of fluidized, magnetizable reforming catalyst, and reformed hydrocarbon product
US5151392A (en) * 1989-12-11 1992-09-29 Uop Moving bed regeneration process with separate dispersion and chloriding steps
US5053371A (en) * 1990-11-02 1991-10-01 Uop Catalyst regeneration method with three-zone combustion gas addition
US5397458A (en) * 1993-12-27 1995-03-14 Uop Moving bed regeneration process with internally mixed chloride gas
US5498756A (en) * 1993-12-27 1996-03-12 Uop Moving bed regeneration process with internally mixed chloride gas
US5457077A (en) * 1993-12-30 1995-10-10 Uop Moving bed regeneration process with combined drying and dispersion steps
US5824619A (en) * 1994-05-12 1998-10-20 Uop Particulate cooling process with reduced thermal channeling
JP2011032333A (ja) * 2009-07-30 2011-02-17 Chiyoda Kako Kensetsu Kk 連続式流動接触芳香族製造プラントの運転方法

Also Published As

Publication number Publication date
GB796310A (en) 1958-06-11
FR1135954A (fr) 1957-05-07
FR70853E (fr) 1959-09-02
NL212345A (xx)

Similar Documents

Publication Publication Date Title
US3554902A (en) Platinum iridium
US3939062A (en) Catalyst regeneration procedure
US3134732A (en) Reactivation of regenerated noble metal catalysts with gaseous halogens
US3943052A (en) Regeneration procedure
US4046673A (en) Simplified regeneration procedure
US5776849A (en) Regeneration of severely deactivated reforming catalysts
EP0057551A1 (en) Catalyst regeneration procedure
US2749287A (en) Reactivation of hydroforming catalysts using dry air
US4354925A (en) Catalytic reforming process
US5270272A (en) Sulfur removal from molecular-sieve catalyst
US3011967A (en) Platinum catalyst hydroforming and reactivation technique
US2587425A (en) Reforming naphtha with activated carbon catalyst
US2908636A (en) Hydroforming process
EP0421584B1 (en) Cleanup of contaminated hydrocarbon conversion system to enable use with contaminant-sensitive catalyst
US4255289A (en) Process for the preparation of magnetic catalysts
US5368720A (en) Fixed bed/moving bed reforming with high activity, high yield tin modified platinum-iridium catalysts
US2758063A (en) Method of regenerating hydroforming catalysts
US2746909A (en) Hydroforming
US3558479A (en) Low pressure regenerative reforming process for high paraffin feeds
US2965563A (en) Hydroforming and regeneration and reactivation of platinum catalyst with chlorine gas under anhydrous conditions
US3705095A (en) Plural stage platinum catalyst reforming with rhenium in the last stage
US2816857A (en) Fluid hydroforming process with regeneration of the platinum containing catalyst
US3950270A (en) Promoted platinum-iridium-containing reforming catalysts
US2914462A (en) Slurry liquid phase hydrogenation
US2958644A (en) Production of high octane motor fuels