NO140274B - PROCEDURE FOR HYDROCRACKING OF HYDROCARBONS OVER A PLATINUM AND / OR PALLADIUM CATALYMER ON A CARRIER MINERAL CARRIER WITH SELECTED ACIDITY - Google Patents

PROCEDURE FOR HYDROCRACKING OF HYDROCARBONS OVER A PLATINUM AND / OR PALLADIUM CATALYMER ON A CARRIER MINERAL CARRIER WITH SELECTED ACIDITY Download PDF

Info

Publication number
NO140274B
NO140274B NO741185A NO741185A NO140274B NO 140274 B NO140274 B NO 140274B NO 741185 A NO741185 A NO 741185A NO 741185 A NO741185 A NO 741185A NO 140274 B NO140274 B NO 140274B
Authority
NO
Norway
Prior art keywords
acidity
carrier
hydrocracking
palladium
platinum
Prior art date
Application number
NO741185A
Other languages
Norwegian (no)
Other versions
NO741185L (en
NO140274C (en
Inventor
Marco Taramasso
Orfeo Forlani
Bruno Notari
Original Assignee
Snam Progetti
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
Publication of NO741185L publication Critical patent/NO741185L/en
Application filed by Snam Progetti filed Critical Snam Progetti
Publication of NO140274B publication Critical patent/NO140274B/en
Publication of NO140274C publication Critical patent/NO140274C/en

Links

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
    • C10G47/00—Cracking of hydrocarbon oils, in the presence of hydrogen or hydrogen- generating compounds, to obtain lower boiling fractions
    • C10G47/02—Cracking of hydrocarbon oils, in the presence of hydrogen or hydrogen- generating compounds, to obtain lower boiling fractions characterised by the catalyst used
    • C10G47/10—Cracking of hydrocarbon oils, in the presence of hydrogen or hydrogen- generating compounds, to obtain lower boiling fractions characterised by the catalyst used with catalysts deposited on a carrier
    • C10G47/12—Inorganic carriers
    • C10G47/14—Inorganic carriers the catalyst containing platinum group metals or compounds thereof
    • 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
    • B01J21/00—Catalysts comprising the elements, oxides, or hydroxides of magnesium, boron, aluminium, carbon, silicon, titanium, zirconium, or hafnium
    • B01J21/16—Clays or other mineral silicates
    • 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
    • B01J23/38—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of noble metals
    • B01J23/40—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of noble metals of the platinum group metals
    • 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
    • B01J23/38—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of noble metals
    • B01J23/40—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of noble metals of the platinum group metals
    • B01J23/42—Platinum
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C4/00—Preparation of hydrocarbons from hydrocarbons containing a larger number of carbon atoms
    • C07C4/02—Preparation of hydrocarbons from hydrocarbons containing a larger number of carbon atoms by cracking a single hydrocarbon or a mixture of individually defined hydrocarbons or a normally gaseous hydrocarbon fraction
    • C07C4/06—Catalytic processes
    • 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
    • C07C5/22—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by isomerisation
    • C07C5/2206—Catalytic processes not covered by C07C5/23 - C07C5/31
    • C07C5/226—Catalytic processes not covered by C07C5/23 - C07C5/31 with metals
    • 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
    • C07C5/22—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by isomerisation
    • C07C5/27—Rearrangement of carbon atoms in the hydrocarbon skeleton
    • C07C5/2702—Catalytic processes not covered by C07C5/2732 - C07C5/31; Catalytic processes covered by both C07C5/2732 and C07C5/277 simultaneously
    • C07C5/2724—Catalytic processes not covered by C07C5/2732 - C07C5/31; Catalytic processes covered by both C07C5/2732 and C07C5/277 simultaneously with metals
    • 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
    • B01J21/00—Catalysts comprising the elements, oxides, or hydroxides of magnesium, boron, aluminium, carbon, silicon, titanium, zirconium, or hafnium
    • B01J21/06—Silicon, titanium, zirconium or hafnium; Oxides or hydroxides thereof
    • B01J21/08—Silica
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C2521/00—Catalysts comprising the elements, oxides or hydroxides of magnesium, boron, aluminium, carbon, silicon, titanium, zirconium or hafnium
    • C07C2521/16—Clays or other mineral silicates
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C2523/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group C07C2521/00
    • C07C2523/38—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group C07C2521/00 of noble metals
    • C07C2523/40—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group C07C2521/00 of noble metals of the platinum group metals
    • C07C2523/42—Platinum
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C2523/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group C07C2521/00
    • C07C2523/38—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group C07C2521/00 of noble metals
    • C07C2523/40—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group C07C2521/00 of noble metals of the platinum group metals
    • C07C2523/44—Palladium

Landscapes

  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Engineering & Computer Science (AREA)
  • Materials Engineering (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • General Chemical & Material Sciences (AREA)
  • Inorganic Chemistry (AREA)
  • Dispersion Chemistry (AREA)
  • Catalysts (AREA)
  • Low-Molecular Organic Synthesis Reactions Using Catalysts (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)

Description

Foreliggende oppfinnelse angår en fremgangsmåte for hydrocracking, The present invention relates to a method for hydrocracking,

og det særegne ved fremgangsmåten i henhold til oppfinnelsen er at mettede hydrokarboner i dampfase i blanding med hydrogen føres over en katalysator som er bygget opp av and the distinctive feature of the method according to the invention is that saturated hydrocarbons in the vapor phase in a mixture with hydrogen are passed over a catalyst which is made up of

1) et bærermaterial valgt fra naturlige eller syntetiske mineraler av leiretypen med krystallinsk grunnmassestruktur i form av plane og ikke-porøse parallelle lag med høy ladningstetthet (0,4 til 1,0 elektronladninger pr. halvcelle Si^O^) , idet bærermaterialets overflate har sentre med for formålet likt innstilt surhet alle like, idet surheten er oppnådd ved ladningsforskyv- 1) a carrier material selected from natural or synthetic minerals of the clay type with a crystalline groundmass structure in the form of planar and non-porous parallel layers with a high charge density (0.4 to 1.0 electron charges per half-cell Si^O^), the surface of the carrier material having centers with the same set acidity for the purpose, all the same, since the acidity is achieved by charge displacement

ning eller er av typen protonsyre eller Lewis-syre, og 2) fint dispergert platina og/eller palladium i en mengde på ning or is of the proton acid or Lewis acid type, and 2) finely dispersed platinum and/or palladium in an amount of

mellom 0,01 og 0,5 vekt% regnet på hele katalysatoren, ved en temperatur på 150-450°C, et trykk på 35 - 150 kg/cm<2> og med en relativ volumhastighet på 0,1 - 10 h~ . between 0.01 and 0.5% by weight calculated on the whole catalyst, at a temperature of 150-450°C, a pressure of 35 - 150 kg/cm<2> and with a relative volume velocity of 0.1 - 10 h~ .

Hydrocracking av hydrokarboner er en operasjon som anvendes meget Hydrocracking of hydrocarbons is a widely used operation

i industrien, og tillater fremstilling av enkelte lette fraksjoner som er rike på isoparaff iner og derfor brukbare som motorbensin ved å gå ut fra tunge destillater eller gassoljer. in industry, and allows the production of certain light fractions that are rich in isoparaffins and therefore usable as motor petrol by starting from heavy distillates or gas oils.

Fremgangsmåten i henhold til oppfinnelsen gjennomføres ved hjelp The method according to the invention is carried out using

av velkjent teknikk ved å la passende petroleumfraksjoner reagere i nærvær av hydrogen ved høyt trykk, med katalysatorer i en reaktor som holdes ved ønsket temperatur. of well-known technique by allowing suitable petroleum fractions to react in the presence of hydrogen at high pressure, with catalysts in a reactor maintained at the desired temperature.

Det er videre nødvendig å peke på at arbeidsbetingelsene ved de fremgangsmåter hvor da katalysatorer som er kjent innen denne gren av teknikken vanlig kan brukes er meget kritiske på grunn av det begrensede område for temperatur og trykk hvor det er optimal omsetning og selektivitet. I motsetning hertil mulig-gjør fremgangsmåten i henhold til oppfinnelsen oppnåelse av høye selektiviteter ved omsetningsgrader som er meget nær dem som kan beregnes termodynamisk. It is also necessary to point out that the working conditions in the processes where catalysts known within this branch of technology can be commonly used are very critical due to the limited range of temperature and pressure where there is optimal conversion and selectivity. In contrast, the method according to the invention makes it possible to achieve high selectivities at conversion rates that are very close to those that can be calculated thermodynamically.

Sentrene med likt innstilt surhet frembringes kunstig ved hjelp av forskjellige metoder og graden av surhet, som nevnt innstilles, avhenger av det anvendte fremstillingssystem for å. oppnå katalysatoren. The centers with the same set acidity are produced artificially by means of different methods and the degree of acidity, which is set as mentioned, depends on the manufacturing system used to obtain the catalyst.

Surheten som frembringes kunstig på overflaten av katalysatoren kan være av forskjellig natur og omfatter som nevnt: The acidity that is produced artificially on the surface of the catalyst can be of different nature and includes, as mentioned:

a) en surhet som skyldes ladningsforskyvning a) an acidity due to charge displacement

b) en surhet av typen protonsyre, og b) an acidity of the proton acid type, and

c) en surhet av typen Lewis-syre. c) an acidity of the Lewis acid type.

Surheten nevnt under punkt a) frembringes ved ladningsforskyvning The acidity mentioned under point a) is produced by charge displacement

ved å anvende et material med krystallinsk grunnmassestruktur i form av plane og ikke-porøse parallelle lag som inne i krystall-gitteret har manglende ladninger som for å oppnå elektrisk nøy-tralisering krever en kompensering fra kationer på den ytre overflate. Disse krav tilfredsstilles av de naturlige eller syntetiske mineraler av leiretypen og blant disse foretrekkes spesielt fyllosilikater med høyere ladningstetthet (0,4 - 1 elektronladninger pr. halvcelle Si4P1Q) med fortrinnsvis tetra-edrisk substitusjon. by using a material with a crystalline groundmass structure in the form of planar and non-porous parallel layers which inside the crystal lattice have missing charges which, in order to achieve electrical neutralisation, require compensation from cations on the outer surface. These requirements are satisfied by the natural or synthetic minerals of the clay type and among these phyllosilicates with a higher charge density (0.4 - 1 electron charges per half cell Si4P1Q) with preferably tetrahedral substitution are particularly preferred.

Spesifikt hører disse mineraler til gruppene: Specifically, these minerals belong to the groups:

smektitter av typen "beidellitt" (beidellitter, non-tronitter), og mineraler med begrenset ekspansjon av typen "vermikulitt" (vermi-kulitter, hydrobiotitter, illitter). smectites of the "beidellite" type (beidellites, non-tronites), and limited expansion minerals of the "vermiculite" type (vermiculites, hydrobiotites, illites).

Slike mineraler i findelt tilstand (partikkelstørrelse mindre Such minerals in a finely divided state (particle size smaller

enn 40^um underkastes kationisk utveksling med bi- eller poly- than 40 µm are subjected to cationic exchange with bi- or poly-

valente kationer av elementene fra gruppene Illb, IVb, VIb, Vllb, og VIII i det periodiske system og med rekken av lantanider (Handbook of Chemistry and Physics - 49. utgave 1968 - 1969 - Chemical Rubber Publishing Company), og da foretrukket kationer valence cations of the elements from groups Illb, IVb, VIb, Vllb, and VIII in the periodic system and with the series of lanthanides (Handbook of Chemistry and Physics - 49th edition 1968 - 1969 - Chemical Rubber Publishing Company), and then preferred cations

av lantan, cerium, titan og mangan. of lanthanum, cerium, titanium and manganese.

Den surhet som er nevnt under punkt b) (protonsyre) fremstilles ved å anvende de ovenfor beskrevne mineraler etter utveksling med ammoniumion og påfølgende oppvarming med temperatur til-strekkelig for spalting, med utvikling av ammoniakk, vanlig mellom 300 og 600°C og foretrukket ved ca. 450°C i 10 timer. The acidity mentioned under point b) (protic acid) is produced by using the minerals described above after exchange with ammonium ion and subsequent heating at a temperature sufficient for cleavage, with the evolution of ammonia, usually between 300 and 600°C and preferably at about. 450°C for 10 hours.

Den surhet som er nevnt under punkt c) (Lewis-syre) frembringes ved hjelp av oppvarming og delvis ved dehydratisering av hydroksyl-grupper knyttet til aluminium til stede i det oktaedriske lag av de før beskrevne materialer. Spesielt men ikke nødvendigvis frembys en slik surhet av det metakaolinitt som oppnås ved oppvarming mellom 3 50 og 450°C av kaolinitt-mineralet. The acidity mentioned under point c) (Lewis acid) is produced by heating and partly by dehydration of hydroxyl groups linked to aluminum present in the octahedral layer of the previously described materials. In particular, but not necessarily, such an acidity is produced by the metakaolinite which is obtained by heating between 350 and 450°C of the kaolinite mineral.

Det edelmetall (platina og/eller palladium) som er tilstede på overflaten av katalysatoren utgjør prosentvis mellom 0,01 og 5 vekt% og innføres på overflaten av katalysatoren ved hjelp av impregnering med en forbindelse av det nevnte metall. The noble metal (platinum and/or palladium) which is present on the surface of the catalyst amounts to a percentage of between 0.01 and 5% by weight and is introduced onto the surface of the catalyst by means of impregnation with a compound of the said metal.

I tilfellet med platina foretas impregneringen med H^PtCl^ eller Pt(NH3)4(OH)2- In the case of platinum, the impregnation is carried out with H^PtCl^ or Pt(NH3)4(OH)2-

Innføringen av edelmetallet gjennomføres i alle fall, uansett The introduction of the precious metal is carried out in any case, regardless

den type surhet som er tilstede på overflaten av katalysatoren og derfor uansett den fremgangsmåte som gjennomføres for å oppnå denne surhet. the type of acidity present on the surface of the catalyst and therefore regardless of the process carried out to achieve this acidity.

Fremgangsmåten i henhold til foreliggende oppfinnelsé muliggjør omdannelse og selektivitet som industrielt er meget interessante. Videre medfører den bemerkelsesverdige økonomiske fordeler i sammenligning med de konvensjonelle metoder på grunn av de billige mineraler som anvendes for fremstillingen eller den meget enkle og billige bearbeidelse som disse underkastes, eller på grunn av at denne katalysator gir resultater av industriell interesse med meget små mengder edelmetaller, som i tilfellet med isomerisering er fortrinnsvis 0,15 vekt%, dvs. mye mindre enn de mengder som kreves i konvensjonelle katalysatorer. Videre er det nødvendig å påpeke at det er mulig å oppnå katalysatorer med forskjellig surhetsgrad bare ved å endre utgangsmaterialet, arten av det kation som utvekslingen foretas med og fremstillingsmetoden. The method according to the present invention enables conversion and selectivity which are industrially very interesting. Furthermore, it entails remarkable economic advantages in comparison with the conventional methods due to the cheap minerals used for the production or the very simple and cheap processing to which these are subjected, or due to the fact that this catalyst gives results of industrial interest with very small amounts of precious metals , which in the case of isomerization is preferably 0.15% by weight, i.e. much less than the amounts required in conventional catalysts. Furthermore, it is necessary to point out that it is possible to obtain catalysts with different degrees of acidity simply by changing the starting material, the nature of the cation with which the exchange is carried out and the method of preparation.

I realiteten vil for det samme utgangsmaterial med en bestemt manglende ladning som tidligere omtalt, bruken av det ene eller det annet kation tillate oppnåelse av forskjellige katalysatorer, som har forskjellig overflatesurhet (med surhet menes enten surhet av typen proton-syre eller av typen Lewis-syre eller surhet som skyldes ladningsforskyvning) og som fra det samme tilførsels-material og under de samme reaksjonsbetingelser vil gi forskjellige reaksjonsprodukter. In reality, for the same starting material with a certain lack of charge as previously mentioned, the use of one or the other cation will allow the achievement of different catalysts, which have different surface acidity (by acidity is meant either acidity of the proton acid type or of the Lewis type acid or acidity due to charge displacement) and which from the same feed material and under the same reaction conditions will give different reaction products.

En annen fordeling av reaksjonsproduktene oppnås også med å endre utgangsmaterialet og med å bibeholde samme kation. Det kan også anvendes forskjellige surheter i tilfellet med en forskjellig fremstillingstype som tidligere omtalt. A different distribution of the reaction products is also achieved by changing the starting material and by retaining the same cation. Different acidities can also be used in the case of a different type of preparation as previously discussed.

Oppfinnelsen skal nærmere beskrives under anvendelse av de ovenfor beskrevne katalysatorer. The invention will be described in more detail using the catalysts described above.

Ved fremgangsmåten i henhold til oppfinnelsen sendes den til-førsel som skal behandles og som består av flytende tunge hydrokarboner til en reaktor som er fylt med katalysatoren av den nevnte spesielle type som her anvendes. In the method according to the invention, the supply to be treated and which consists of liquid heavy hydrocarbons is sent to a reactor which is filled with the catalyst of the aforementioned special type used here.

Omsetningen drives ved en temperatur mellom 150 og 450°C ved et trykk mellom 35 og 150 atmosfærer. The reaction is carried out at a temperature between 150 and 450°C at a pressure between 35 and 150 atmospheres.

Relativ volumhastighet utgjør mellom 0,1 og 10 h ^. Produktene fra reaktoren underkastes konvensjonelle behandlinger med de-butanisering og fraksjonering. Relative volume velocity is between 0.1 and 10 h ^. The products from the reactor are subjected to conventional treatments with de-butanisation and fractionation.

I det følgende skal en foretrukket utførelsesform for oppfinnelsen beskrives ved hjelp av et utførelseseksempel. In the following, a preferred embodiment of the invention will be described by means of an embodiment example.

I dette eksempel menes det med uttrykket "omdannelse" forholdet mellom antall molekyler som omsettes In this example, the term "conversion" means the ratio between the number of molecules that are converted

antall molekyler tilført. number of molecules added.

EKSEMPEL EXAMPLE

Normal heksadekan-hydrocracking. Normal hexadecane hydrocracking.

20 g katalysator i form av vermikulitt utbyttet med titan med 0,15 vekt SS Pt ble prøvet for hydrocrackings-reaksjon av n-heksadekan. 20 g of catalyst in the form of vermiculite substituted with titanium with 0.15 weight SS Pt was tested for hydrocracking reaction of n-hexadecane.

De oppnådde data var følgende: The data obtained were the following:

Reaksjonsbetingelser: Reaction conditions:

T = 350°C T = 350°C

2 2

P = 50 kg/cm P = 50 kg/cm

HLSV =0,5 ( = relativ væskevolumhastighet) HLSV =0.5 ( = relative liquid volume velocity)

f^/hydrokarbon-forhold = 10 f^/hydrocarbon ratio = 10

Produktegenskaper: Product features:

Omdannelse = 80 % Conversion = 80%

Molfordeling av reaksjonsproduktene: Molar distribution of the reaction products:

I det ovenstående representerer C^, C^, Cj. osv. isoparaffiniske og paraffiniske hydrokarboner med det angitte antall karbonatomer. In the above, C^, C^, Cj represent. etc. isoparaffinic and paraffinic hydrocarbons having the indicated number of carbon atoms.

Claims (1)

Fremgangsmåte for hydrocracking,karakterisert ved at mettede hydrokarboner i dampfase i blanding med hydrogen; føres over en katalysator som er bygget opp av 1) et bærermaterial valgt fra naturlige eller syntetiske mineraler av leiretypen med krystallinsk grunnmassestruktur i form av plane og ikke-porøse parallelle lag med høy ladningstetthet (0,4 til 1,0 elektronladninger pr. halvcelle Si^O^) , idet bærermaterialets overflate har sentre med for formålet likt innstilt surhet, alle like, idet surheten er oppnådd ved ladningsforskyvning eller er av typen protonsyre eller Lewis-syre, og 2) fint dispergert platina og/eller palladium i en mengde på mellom 0,01 og 0,5 vekt% regnet på hele katalysatoren, ved en temperatur på 150 - 450°C, et trykk på 35 - 150 kg/cm<2> og med en relativ volumhastighet på 0,1 - 10 h~ .Process for hydrocracking, characterized in that saturated hydrocarbons in the vapor phase are mixed with hydrogen; is passed over a catalyst which is made up of 1) a support material selected from natural or synthetic minerals of the clay type with a crystalline groundmass structure in the form of planar and non-porous parallel layers with a high charge density (0.4 to 1.0 electron charges per half-cell Si ^O^), in that the surface of the carrier material has centers with the same set acidity for the purpose, all equal, in that the acidity is obtained by charge displacement or is of the type proton acid or Lewis acid, and 2) finely dispersed platinum and/or palladium in an amount of between 0.01 and 0.5% by weight calculated on the entire catalyst, at a temperature of 150 - 450°C, a pressure of 35 - 150 kg/cm<2> and with a relative volume velocity of 0.1 - 10 h~ .
NO741185A 1971-04-09 1974-04-02 PROCEDURE FOR HYDROCRACKING OF HYDROCARBONS OVER A PLATINUM AND / OR PALLADIUM CATALYMER ON A CARRIER MINERAL CARRIER WITH SELECTED ACIDITY NO140274C (en)

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
IT2296671 1971-04-09

Publications (3)

Publication Number Publication Date
NO741185L NO741185L (en) 1972-10-10
NO140274B true NO140274B (en) 1979-04-23
NO140274C NO140274C (en) 1979-08-01

Family

ID=11202381

Family Applications (5)

Application Number Title Priority Date Filing Date
NO1185/72A NO137985C (en) 1971-04-09 1972-04-07 BYFUNCTIONAL CATALYST FOR ISOMERIZATION AND HYDROCRACKING OF HYDROCARBONS
NO741184A NO140266C (en) 1971-04-09 1974-04-02 PROCEDURE FOR ISOMERIZATION OF SATURATED HYDROCARBONS OVER A PLATINUM AND / OR PALLADIUM CATALYM ON A CARRYED ACIDITY CARRIER MATERIAL
NO741181A NO137986C (en) 1971-04-09 1974-04-02 PROCEDURE FOR THE PREPARATION OF A BIFUNCTIONAL CATALYST SUITABLE FOR ISOMERIZATION AND HYDROCRACKING OF HYDROCARBONS
NO741182A NO137987C (en) 1971-04-09 1974-04-02 PROCEDURE FOR THE PREPARATION OF A BIFUNCTIONAL CATALYST SUITABLE FOR ISOMERIZATION AND HYDROCRACKING OF HYDROCARBONS
NO741185A NO140274C (en) 1971-04-09 1974-04-02 PROCEDURE FOR HYDROCRACKING OF HYDROCARBONS OVER A PLATINUM AND / OR PALLADIUM CATALYMER ON A CARRIER MINERAL CARRIER WITH SELECTED ACIDITY

Family Applications Before (4)

Application Number Title Priority Date Filing Date
NO1185/72A NO137985C (en) 1971-04-09 1972-04-07 BYFUNCTIONAL CATALYST FOR ISOMERIZATION AND HYDROCRACKING OF HYDROCARBONS
NO741184A NO140266C (en) 1971-04-09 1974-04-02 PROCEDURE FOR ISOMERIZATION OF SATURATED HYDROCARBONS OVER A PLATINUM AND / OR PALLADIUM CATALYM ON A CARRYED ACIDITY CARRIER MATERIAL
NO741181A NO137986C (en) 1971-04-09 1974-04-02 PROCEDURE FOR THE PREPARATION OF A BIFUNCTIONAL CATALYST SUITABLE FOR ISOMERIZATION AND HYDROCRACKING OF HYDROCARBONS
NO741182A NO137987C (en) 1971-04-09 1974-04-02 PROCEDURE FOR THE PREPARATION OF A BIFUNCTIONAL CATALYST SUITABLE FOR ISOMERIZATION AND HYDROCRACKING OF HYDROCARBONS

Country Status (18)

Country Link
JP (1) JPS5730533B1 (en)
AT (1) AT346816B (en)
BE (1) BE781719A (en)
CA (1) CA978552A (en)
CH (1) CH562635A5 (en)
CS (1) CS185608B2 (en)
DD (3) DD106341A5 (en)
DK (1) DK143973C (en)
ES (1) ES402459A1 (en)
FR (1) FR2132684B1 (en)
GB (1) GB1392197A (en)
LU (1) LU65125A1 (en)
NL (1) NL161685C (en)
NO (5) NO137985C (en)
PL (4) PL86964B1 (en)
SE (1) SE392401B (en)
SU (2) SU686600A3 (en)
YU (1) YU36622B (en)

Families Citing this family (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP1837320A1 (en) 2006-03-23 2007-09-26 ETH Zürich Production of saturated C2 to C5 hydrocarbons
EA025338B1 (en) * 2013-04-30 2016-12-30 Институт Нефтехимических Процессов Им. Академика Ю. Мамедалиева, Нан Азербайджана Method for production of light petroleum products from heavy petroleum residues
KR20210087019A (en) * 2018-10-26 2021-07-09 가부시키가이샤 아데카 composite material

Family Cites Families (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3632502A (en) * 1969-08-06 1972-01-04 Chevron Res Hydrocracking catalyst comprising a layered clay-type crystalline aluminosilicate component a group viii component and a rare earth component and process using said catalyst

Also Published As

Publication number Publication date
NO741182L (en) 1972-10-10
ES402459A1 (en) 1976-04-01
DE2264621A1 (en) 1974-05-22
FR2132684B1 (en) 1974-06-28
DE2264621B2 (en) 1976-12-23
NO140266C (en) 1979-08-01
PL83829B1 (en) 1976-02-28
NO741184L (en) 1972-10-10
DK143973C (en) 1982-04-26
SU686600A3 (en) 1979-09-15
PL86965B1 (en) 1976-06-30
DD101660A5 (en) 1973-11-12
FR2132684A1 (en) 1972-11-24
NO137985C (en) 1978-06-07
NO140266B (en) 1979-04-23
NL161685B (en) 1979-10-15
PL86964B1 (en) 1976-06-30
SU833145A3 (en) 1981-05-23
CH562635A5 (en) 1975-06-13
NL7204644A (en) 1972-10-11
YU36622B (en) 1984-08-31
DE2216812B2 (en) 1975-10-02
DD109234A5 (en) 1974-10-20
NO741181L (en) 1972-10-10
DE2216812A1 (en) 1972-10-26
CS185608B2 (en) 1978-10-31
DD106341A5 (en) 1974-06-12
LU65125A1 (en) 1972-07-12
NO741185L (en) 1972-10-10
NO140274C (en) 1979-08-01
ATA310372A (en) 1978-04-15
NO137987B (en) 1978-02-27
NO137987C (en) 1978-06-07
JPS5730533B1 (en) 1982-06-29
NO137985B (en) 1978-02-27
BE781719A (en) 1972-07-31
PL83830B1 (en) 1976-02-28
GB1392197A (en) 1975-04-30
AT346816B (en) 1978-11-27
NO137986C (en) 1978-06-07
DK143973B (en) 1981-11-09
NL161685C (en) 1980-03-17
NO137986B (en) 1978-02-27
YU84372A (en) 1982-02-25
SE392401B (en) 1977-03-28
CA978552A (en) 1975-11-25

Similar Documents

Publication Publication Date Title
EP0288622B1 (en) Process for the isomerization of paraffinic hydrocarbons
EA024491B1 (en) Process for the conversion of ethane to aromatic hydrocarbons
Sadek et al. Fischer-Tropsch reaction on Co-containing microporous and mesoporous Beta zeolite catalysts: The effect of porous size and acidity
JP5689950B2 (en) Catalyst for hydrodewaxing process and process for producing the same
DE3880455T2 (en) METHOD FOR ISOMERIZING WAXES TO LUBRICANT BASED OILS.
EP0361767A1 (en) Process for the conversion of a C2-C6 aliphatic hydrocarbon into naphthenic hydrocarbons
RU2076845C1 (en) Crystalline zeolite-like gallosilicate, method of its synthesis and catalyst base for hydrocarbon conversion
US4579832A (en) Class of hydroprocessing catalysts and preparation methods
JPS6270223A (en) Zeolite having omega structure
KR20200126984A (en) Catalyst systems useful for dehydrogenation reactions
US20080249346A1 (en) Catalyst for selective opening of cyclic naphtha and process for using the catalyst
Patrylak et al. Ukrainian mordenite–clinoptilolite rocks as a base for linear hexane isomerization catalyst
CA1189056A (en) Process for the preparation of a catalytically active cross-linked metal silicate
Campelo et al. Catalytic properties of the silicoaluminophosphates SAPO-5 and SAPO-11 in n-octane and isooctane hydroconversion
US3511773A (en) Process for producing lpg and a high octane reformate
NO140274B (en) PROCEDURE FOR HYDROCRACKING OF HYDROCARBONS OVER A PLATINUM AND / OR PALLADIUM CATALYMER ON A CARRIER MINERAL CARRIER WITH SELECTED ACIDITY
US3966642A (en) Hydrocarbon conversion catalyst
Dzhikiya et al. A study of fluorine-containing catalysts based on MOR and BEA zeolites in isomerization of n-hexane
Gerzeliev et al. Features of the isobutane alkylation with butylenes on zeolite catalysts
US3847796A (en) Hydrocracking process for the production of lpg
Comboni et al. The elastic behavior of zeolitic frameworks: The case of MFI type zeolite under high-pressure methanol intrusion
US3963600A (en) Combination process for the conversion of heavy distillates to LPG
JPH02184517A (en) Gallosilicate zeolite beta, making thereof and use thereof as catalyst
US4022684A (en) Hydrocarbon conversion process using a Ni and/or CO substituted synthetic aluminosilicate catalyst
Ejtemaei et al. n-pentane isomerization over Pt-Al promoted sulfated zirconia nanocatalyst