EP1242185A2 - Ex situ solid-state phosphorus activation of crystalline porous silicates - Google Patents

Ex situ solid-state phosphorus activation of crystalline porous silicates

Info

Publication number
EP1242185A2
EP1242185A2 EP00990607A EP00990607A EP1242185A2 EP 1242185 A2 EP1242185 A2 EP 1242185A2 EP 00990607 A EP00990607 A EP 00990607A EP 00990607 A EP00990607 A EP 00990607A EP 1242185 A2 EP1242185 A2 EP 1242185A2
Authority
EP
European Patent Office
Prior art keywords
activated
phosphorus
crystalline porous
porous silicate
solid
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.)
Withdrawn
Application number
EP00990607A
Other languages
German (de)
French (fr)
Inventor
Eelco Titus Carel Vogt
Arno Tissler
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.)
Alsi Penta Zeolithe GmbH
Akzo Nobel NV
Original Assignee
Alsi Penta Zeolithe GmbH
Akzo Nobel NV
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Alsi Penta Zeolithe GmbH, Akzo Nobel NV filed Critical Alsi Penta Zeolithe GmbH
Priority to EP00990607A priority Critical patent/EP1242185A2/en
Publication of EP1242185A2 publication Critical patent/EP1242185A2/en
Withdrawn legal-status Critical Current

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
    • C10G35/00—Reforming naphtha
    • C10G35/04—Catalytic reforming
    • C10G35/06—Catalytic reforming characterised by the catalyst used
    • C10G35/095—Catalytic reforming characterised by the catalyst used containing crystalline alumino-silicates, e.g. molecular sieves
    • 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
    • B01J27/00—Catalysts comprising the elements or compounds of halogens, sulfur, selenium, tellurium, phosphorus or nitrogen; Catalysts comprising carbon compounds
    • B01J27/14—Phosphorus; Compounds thereof
    • B01J27/182—Phosphorus; Compounds thereof with silicon
    • 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
    • B01J29/00—Catalysts comprising molecular sieves
    • B01J29/04—Catalysts comprising molecular sieves having base-exchange properties, e.g. crystalline zeolites
    • B01J29/06—Crystalline aluminosilicate zeolites; Isomorphous 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
    • B01J29/00—Catalysts comprising molecular sieves
    • B01J29/04—Catalysts comprising molecular sieves having base-exchange properties, e.g. crystalline zeolites
    • B01J29/06—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof
    • B01J29/40—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of the pentasil type, e.g. types ZSM-5, ZSM-8 or ZSM-11, as exemplified by patent documents US3702886, GB1334243 and US3709979, respectively
    • B01J29/42—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of the pentasil type, e.g. types ZSM-5, ZSM-8 or ZSM-11, as exemplified by patent documents US3702886, GB1334243 and US3709979, respectively containing iron group metals, noble metals or copper
    • 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
    • B01J29/00—Catalysts comprising molecular sieves
    • B01J29/04—Catalysts comprising molecular sieves having base-exchange properties, e.g. crystalline zeolites
    • B01J29/06—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof
    • B01J29/80—Mixtures of different zeolites
    • 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
    • B01J37/00—Processes, in general, for preparing catalysts; Processes, in general, for activation of catalysts
    • B01J37/04—Mixing
    • 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
    • B01J37/00—Processes, in general, for preparing catalysts; Processes, in general, for activation of catalysts
    • B01J37/28—Phosphorising
    • 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
    • C10G11/00—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
    • C10G11/02—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils characterised by the catalyst used
    • C10G11/04—Oxides
    • C10G11/05—Crystalline alumino-silicates, e.g. molecular sieves
    • 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
    • C10G29/00—Refining of hydrocarbon oils, in the absence of hydrogen, with other chemicals
    • C10G29/20—Organic compounds not containing metal atoms
    • C10G29/205—Organic compounds not containing metal atoms by reaction with hydrocarbons added to the hydrocarbon oil
    • 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
    • C10G45/00—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds
    • C10G45/58—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to change the structural skeleton of some of the hydrocarbon content without cracking the other hydrocarbons present, e.g. lowering pour point; Selective hydrocracking of normal paraffins
    • C10G45/60—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to change the structural skeleton of some of the hydrocarbon content without cracking the other hydrocarbons present, e.g. lowering pour point; Selective hydrocracking of normal paraffins characterised by the catalyst used
    • C10G45/64—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to change the structural skeleton of some of the hydrocarbon content without cracking the other hydrocarbons present, e.g. lowering pour point; Selective hydrocracking of normal paraffins characterised by the catalyst used containing crystalline alumino-silicates, e.g. molecular sieves
    • 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
    • B01J2229/00—Aspects of molecular sieve catalysts not covered by B01J29/00
    • B01J2229/30—After treatment, characterised by the means used
    • B01J2229/36—Steaming
    • 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
    • B01J2229/00—Aspects of molecular sieve catalysts not covered by B01J29/00
    • B01J2229/30—After treatment, characterised by the means used
    • B01J2229/40—Special temperature treatment, i.e. other than just for template removal
    • 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
    • B01J2229/00—Aspects of molecular sieve catalysts not covered by B01J29/00
    • B01J2229/30—After treatment, characterised by the means used
    • B01J2229/42—Addition of matrix or binder particles
    • 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
    • B01J29/00—Catalysts comprising molecular sieves
    • B01J29/04—Catalysts comprising molecular sieves having base-exchange properties, e.g. crystalline zeolites
    • B01J29/06—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof
    • B01J29/08—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of the faujasite type, e.g. type X or Y
    • B01J29/085—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of the faujasite type, e.g. type X or Y containing rare earth elements, titanium, zirconium, hafnium, zinc, cadmium, mercury, gallium, indium, thallium, tin or lead
    • B01J29/088—Y-type faujasite
    • 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
    • B01J29/00—Catalysts comprising molecular sieves
    • B01J29/04—Catalysts comprising molecular sieves having base-exchange properties, e.g. crystalline zeolites
    • B01J29/06—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof
    • B01J29/40—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of the pentasil type, e.g. types ZSM-5, ZSM-8 or ZSM-11, as exemplified by patent documents US3702886, GB1334243 and US3709979, respectively

Definitions

  • the present invention is directed to phosphorus-activated crystalline porous silicates such as layered silicates and microporous silicates, processes for said phosphorus activation, catalyst compositions containing said phosphorus- activated crystalline porous silicates, and catalyst additives containing said phosphorus-activated crystalline porous silicates.
  • crystalline porous layered silicates are also referred to as clays, including anionic clays and cationic clays.
  • the most common crystalline microporous silicates (which are also referred to as zeolites) are metallosilicates.
  • a specific type of metallosiiicate is crystalline alumina silicate. Within the framework of this description all these terms will be used as categorised above.
  • crystalline porous silicates have catalytic activity and are used in numerous catalytic reactions. It is known to use phosphorus-containing compounds to improve the selectivity, activity or physical properties of said crystaiiine porous silicates.
  • Mobil's US 5,126,298 and US 5,231 ,064 describe the preparation of a catalyst composition by providing a zeolite slurry and two types of clay slurries, treating at least one of these slurries with a source of phosphorus, combining the slurries, and spray-drying at a pH of below 3. Catalyst compositions obtained with this process are said to have an improved attrition resistance.
  • US 5,110,776 a phosphorus treatment was used to improve the attrition resistance of catalyst compositions and to improve the octane yield.
  • a Y zeolite is treated with a phosphorus-containing aqueous solution, and said treated zeolite is combined directly with a matrix precursor to form a slurry. Said slurry is spray-dried.
  • US 5,601,699 describes the treatment with phosphorus of zeolite BETA, ZSM-12, and ZSM-20 to obtain catalytic cracking catalysts with improved attrition restistance.
  • EP-A-511 013 describes the treatment of ZSM-5 with phosphorus to increase the propyiene selectivity.
  • US 5,472,594 describes a process for converting a hydrocarbon feed to a product containing improved yields of olefins with a catalyst composition containing zeolite Y and an additive comprising a phosphorus-containing medium pore zeolite such as ZSM-5.
  • Mobil's WO 98/41595 describes a process for the catalytic cracking of a hydrocarbon feedstock to produce an enhanced yield of C 3 to C 5 olefins using a catalyst composition comprising a large pore molecular sieve such as zeolite Y and an additive comprising a phosphorus-containing ZSM-5 blended in with the base catalyst containing zeolite Y. The same is described in US 5,456,821.
  • WO 94/13754 describes the same process using a catalyst composition containing a large pore molecular sieve and an additive containing a specific ZSM-5 which, optionally, contains 1.5 to 5.5 wt% elemental phosphorus.
  • US 5,521 ,133 describes the preparation of a ZSM-5 additive by injecting a ZSM-5 and kaolin slurry with phosphoric acid prior to spray-drying.
  • US 3,972,832 describes the phosphorus treatment of ZSM-5 for use as a catalyst for the conversion of aliphatics.
  • phosphorus-treated ZSM-5 is described for use in the catalytic methylating of toluene.
  • Said activated crystalline porous silicates can be used as a component of a catalyst composition or in additives which can be physically mixed with a catalyst composition, the appropriate physical form depending on the desired use.
  • care must be taken not to dilute the total catalyst composition too much. This means that for use as additive, it must be possible to include a sufficient amount of crystalline porous silicate in the additive to obtain the desired activity. Further, it is necessaryry to activate the crystalline porous silicate to a sufficent level. In the case of use as a catalyst component, care must be taken that the incorporation of the activated crystalline porous silicate does not interfere with the other components of the catalyst composition.
  • a catalyst composition for the production of light olefins by mixing the matrix components, adding a mixture of a Y-type zeolite and a high silica zeolite with pentasil structure such as ZSM-5 containing 2-8 wt% (based on the weight of the zeolite) of phosphorus (calculated as P 2 O 5 ) and 0.3-3 wt% of aluminium or magnesium or calcium.
  • the zeolite mixture is treated with an aqueous solution of phosphorus/aluminium or phosphorus/- magnesium or calcium compounds, dried, and calcined prior to the addition to the matrix components.
  • NL-9301333 describes the ex situ activation of ZRP zeolite with an aluminium phosphate sol. Said activated ZRP zeolite is incorporated into a catalyst composition containing zeolite Y, clay, and organic oxides.
  • the present invention provides an ex situ activation, so rendering the activated crystalline porous silicate suitable for incorporation into catalyst compositions.
  • Said novel activation method further provides sufficient activation to render the activated crystalline porous silicate suitable for use in additives.
  • the activation method is universally applicable, which means that all types of crystalline porous silicates may be treated in this fashion. Therefore, starting materials may be used which were not previously applicable and novel activated materials can be obtained.
  • the invention provides an activation method which is more economical and more environmentally friendly than the known phosphorus activation methods. In the known activation methods, the phosphorus-containing compound is always combined with the crystalline porous silicate in the liquid state: the crystalline porous silicate is always impregnated with a phosphorus compound-containing solution.
  • the phosporus-containing compound is solid, it is first dissolved in a solvent prior to being combined with the zeolite. This means that after treatment the mixture must be dried and sometimes filtered before drying. This is uneconomical, because it requires an additional step and extra energy and is, of course, environmentally unfriendly.
  • the present invention is directed to ex situ solid-state phosphorus-activated crystalline porous silicate. Although the p-NMR spectrum of the phosphorus- activated crystalline porous silicate according to the invention differs from the phosphorus-activated porous silicates of the prior art, the present invention provides an activated crystalline porous silicate with an activity which is comparable with that of crystalline porous silicates activated using conventional methods.
  • the ex situ phosphorus-activated crystalline porous silicate according to the invention may be prepared by: a) combining crystalline porous silicate with a phosphorus-containing compound in the solid state, b) intimately mixing the crystalline porous silicate/phosphorus-containing compound mixture, c) calcining the crystalline porous silicate/phosphorus-containing compound mixture to obtain a phosphorus-activated crystalline porous silicate.
  • a) combining crystalline porous silicate with a phosphorus-containing compound in the solid state b) intimately mixing the crystalline porous silicate/phosphorus-containing compound mixture, c) calcining the crystalline porous silicate/phosphorus-containing compound mixture to obtain a phosphorus-activated crystalline porous silicate.
  • Crystalline porous silicates and p-containing compounds usually contain some water, and it is not necessary to dry the starting materials until they are completely dry.
  • solid-state is defined as not having to dry the resulting mixture before calcining.
  • Suitable phosphorus-containing compounds are all phosphorus compounds which are solid at the temperature at which they are combined with the crystalline alumina silicate.
  • Examples are phosphoric acid salts such as ammonium dihydrogen phosphate and diammonium hydrogen phosphate, ammonium hypophosphate, ammonium orthophosphate, ammonium dihydrogen orthophosphate, ammonium hydrogen orthophosphate, triammonium phosphate, phosphines, and phosphites and mixtures thereof. It is preferred to use phosphorus-containing compounds which do not leave undesirable metals on the crystalline porous silicate. Therefore, the addition of for instance sodium salts is not advised.
  • the amount of phosphorus-containing compound to be used may vary from 0.1 to 50 wt% (calculated as P 2 Os based on the crystalline alumina silicate). In FCC applications preferably 10-25 wt% is used.
  • crystaiiine porous silicates may be used. These include both layered silicates and microporous silicates.
  • suitable crystalline porous layered silicates which in the prior art are also referred to as clays, including anionic clays and cationic clays, are kaolin, hydrotalcites, smectites, hectorites, montmorillonites, saponites, sepiolites, sj ⁇ grenites, etcetera.
  • microporous silicates are metallosiiicates. All types of microporous silicates may be used and may be in the hydrogen form, the ammonium form, or the ion-exchanged form, e.g., one or more rare earth metals.
  • a specific type of metallosilicate which can suitably be used is the crystalline alumina silicate.
  • suitable crystalline microporous silicates include the MFI-type zeolites, faujasite-type zeolites such as Y-type zeolite, zeolite X and ZSM-20, MEL-type zeolites such as ZSM-11 , ZSM-12, mordenite zeolites, ETS-4-type, ETS-10-type, MTW-type zeolites such as ZSM-12, MWW-type zeolites such as MCM -22, MCM-36, MCM-49, MCM-56, HEU-type zeolites, CHA-type zeolites, GME-type zeolites, EUO-type zeolites, ERI-type zeolites, FER-type zeolites, OFF-type zeolites, and BEA-type zeolites such as zeolite beta. MFI-type zeolites and faujasite-type zeolites are preferred.
  • MFI-type zeolites are as defined in the ATLAS OF ZEOLITE STRUCTURE TYPES, W.M. Meier and D.H. Olson, 3rd revised edition (1992), Butterworth-
  • Heinemann and include ZSM-5, ST-5, ZSM-8, ZSM-11, silicalite, LZ-105, LZ-
  • faujasite-type zeolites are the Y zeolites and zeolite X. All zeolites Y which are normally used in catalyst compositions are suitable and may be in the hydrogen form, the ammonium form, or the ion-exchanged form, e.g., one or more rare earth metals. Examples are de-aluminated zeolite Y, silica-enriched de-aluminated zeolite Y, and ultrastable zeolite Y (USY).
  • the phosphorus-containing compound and the crystalline porous silicate are intimately mixed. This may be done by means of dry milling, for instance in a ball mill, a kneader or any other means which allows intimate mixing of solid materials. As mentioned above, some liquid may be present in the mixture, as long as no drying step is necessary prior to calcination. For instance, processing aids may be added to improve the conditions for intimate mixing.
  • the mixing temperature may vary fom 0°C to the decomposition temperature of the phosphorus-containing compound used. The mixing time depends on the mixing means used.
  • the resulting mixture is calcined at temperatures between 300 and 1000X, preferably between 450 and 700°C, for about 15 minutes to 24 hours, depending on the amount of phosphorus-containing compound used and the type and amount of crystalline porous silicate used.
  • the calcination step may be conducted in an inert, a reducing or an oxidising atmosphere such as air.
  • the activated crystalline porous silicates according to the invention are suited to be incorporated into catalyst compositions. Owing to the ex situ activation, the phosphorus-containing compound present on the crystalline porous silicate is immobilised and will hardly interfere with any other catalyst components in the strike.
  • Conventional catalyst components are catalytically active components such as the activated crystalline porous silicate according to the invention, optionally, additional catalytic components besides the activated crystalline porous silicate of the invention, binder or matrix material, and, optionally, additives to improve the physical and catalytic properties of the catalyst composition such as crystalline alumina, anionic clays, cationic clays, metal compounds, etctera, and fillers such as clay, for instance kaolin.
  • Suitable binders ususally are alumina, silica, and silica-alumina.
  • catalyst compositions according to the invention may comprise activated porous silicates according to the invention such as activated crystalline layered silicates, activated crystalline microporous silicates including metallosilicates or mixtures thereof.
  • activated metallosilicate such as actived MFI-type zeolite, activated faujasite-type zeolite, activated MCM-22 zeolite, activated mordenite, activated FER-type zeolite and/or BEA-type zeolite.
  • catalyst compositions can suitably be used for the conversion of hydrocarbon feedstocks, the catalytic cracking of hydrocarbon feedstocks, and the conversion of aromatics or aliphatics.
  • the various catalyst components can be combined in any sequence, but it is preferred to add the phosphorus treated crystalline porous silicate to the strike last, so as to avoid any interference of the phosphorus with the other catalyst components.
  • An example of a catalyst composition which is very suitable for use in FCC comprises: a) 10 to 40 wt% Y type zeolite, b) 0.1 to 35 wt% activated MFI-type zeolite according to the invention, c) 10-20 wt% alumina binder, d) 1-15 wt% silica.
  • This catalyst composition appears to provide high propylene yields in combination with bottoms cracking, which is highly desirable for use in FCC.
  • catalyst compositions can be prepared which are extremely suitable for the alkylation of aromatics.
  • catalyst compositions can be prepared which are extremely suitable for the disproportionation of aromatics.
  • catalyst compositions can be prepared which are extremely suitable for the isomerisation of aromatics.
  • catalyst compositions can be prepared which are extremely suitable for the alkylation of aliphatic compounds.
  • activated FER-type zeolites or activated MFI-type zeolites may be incorporated into catalyst compositions.
  • activated MFI-type zeolites according to the invention may be incorporated into catalyst compositions.
  • the ex situ solid-state phosphorus-activated crystalline alumina silicates according to the invention can suitably be incorporated into catalyst additives. Said additives may then be physically mixed with a catalyst composition. Usually, said activated crystalline alumina silicate is combined with a matrix (precursor), and optionally other additives suchas metal compounds, and spray- dried or shaped by any other means conventionally used in the catalyst field. All matrix (precursors) normally used may be applied here. Examples are aluminas such as (pseudo)boehmite, silica, silica-alumina, titania, zirconia. Said additives are suitable for various purposes.
  • a catalyst additive comprising an activated MFI-type crystalline alumina silicate can suitably be used for octane enhancement in FCC processes or for increasing the propylene yield in FCC processes.
  • the phosphorus content on the MFI-type zeolite should be at least 10 wt% (calculated as P 2 O based on the MFI-type zeolite). Usually between 5 and 25 wt% of the additive is added to the FCC base catalyst.
  • Example 1 solid-state ex situ activation of MFI-type zeolite
  • Dried SM-27 ® (ex AISi Penta) was mixed with 25wt% (NH 4 )H 2 PO corresponding to an addition of 15.3 wt% P 2 O 5 (on a phosphorus basis) on SM- 27 and milled in a ball mill for 1 hour. The mixture was calcined at 600°C for 1 hour. The resulting activated MFI-type zeolite had a P 2 Os content of 10.5 wt%.
  • P-NMR showed a material having a single broad peak at about 38 ppm.
  • Comparative example 2 slurry ex situ activation of MFI-type zeolite
  • SM-27 ® (ex AISi Penta) was slurried to obtain a 30 % slurry.
  • H 3 PO 4 was added to a level of 10 wt% P 2 O 5 on SM-27.
  • the pH was adjusted to above 4.5 with ammonia.
  • the mixture was dried at 120°C overnight and calcined at 600°C for 1 hour.
  • P-NMR showed a material with a different pattern: a compound feature containing multiple peaks with the maximum at about 5 ppm.
  • micropore volume of both the solid state phosphorus activated MFI type zeolite and the slurry activated MFI type zeolite was measured by ESW (excess surface work) nitrogen adsorption measurement.
  • ESW extraction surface work
  • the zeolites are provided in a pressure vessel containing nitrogen gas immersed in liquid nitrogen. Nitrogen adsorption isotherms are measured with the P/P 0 varying from 0.000001 to 1. The first minimum obtained when plotting the product of the amount of nitrogen adsorbed and the natural logarithm ln(P/P 0 ) against the amount of nitogen adsorbed, gives a measure of the amount of nitrogen which is adsorbed in the micropore volume (n a m ⁇ n ).
  • the micropore volume can be calculated by multiplying it by the density of liquid nitrogen (i.e., 0.00155 ).
  • the first minimum of the solid state activated MFI-type zeolite was 22.37 at a pressure of 5.6 X 10 "5 Pa which corresponds to a micropore volume of 0.035 ml/g.
  • the first minimum of the slurry activated MFI- type zeolite was 27.37 at a pressure of 8.0 X 10 "5 Pa, which corresponds to a mocropore volume of 0.042 ml/g.
  • Example 3 incorporation of activated MFI-type zeolite into catalyst composition
  • Catalyst compositions were prepared of both the solid-state-activated and the slurry-activated MFI-type zeolite by adding 5 wt% of the activated MFI-type zeolite as the last component to a strike containing 13.5 wt% REY zeolite, 18 wt% peptised pseudoboehmite, and 5 wt% silica. The strike was spray-dried. The catalyst compositions were steamed for 20 hours at 788°C. The physical properties of the two catalyst compositions are listed in TABLE 1.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Crystallography & Structural Chemistry (AREA)
  • Materials Engineering (AREA)
  • General Chemical & Material Sciences (AREA)
  • Catalysts (AREA)
  • Silicates, Zeolites, And Molecular Sieves (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
  • Exhaust Gas Treatment By Means Of Catalyst (AREA)
  • Low-Molecular Organic Synthesis Reactions Using Catalysts (AREA)

Abstract

The present invention is directed to ex situ phosphorus-activated crystalline porous silicates such as layered silicates and microporous silicates, processes for said ex situ phosphorus activation, catalyst compositions containing said ex situ phosphorus-activated crystalline porous silicates, and catalyst additives containing said phosphorus-activated crystalline porous silicates. The quintessence of the invention is that the crystalline porous silicate is ex situ activated with a phosphorus-containing compound in the solid state. The activation method is universally applicable and is more economical and more environmentally friendly than the known phosphorus activation methods, because the drying step necessary in the prior art methods can be avoided.

Description

EX SITU SOLID-STATE PHOSPHORUS ACTIVATION OF CRYSTALLINE POROUS SILICATES
The present invention is directed to phosphorus-activated crystalline porous silicates such as layered silicates and microporous silicates, processes for said phosphorus activation, catalyst compositions containing said phosphorus- activated crystalline porous silicates, and catalyst additives containing said phosphorus-activated crystalline porous silicates. In the prior art, crystalline porous layered silicates are also referred to as clays, including anionic clays and cationic clays. The most common crystalline microporous silicates (which are also referred to as zeolites) are metallosilicates. A specific type of metallosiiicate is crystalline alumina silicate. Within the framework of this description all these terms will be used as categorised above.
Most crystalline porous silicates have catalytic activity and are used in numerous catalytic reactions. It is known to use phosphorus-containing compounds to improve the selectivity, activity or physical properties of said crystaiiine porous silicates. For instance, Mobil's US 5,126,298 and US 5,231 ,064 describe the preparation of a catalyst composition by providing a zeolite slurry and two types of clay slurries, treating at least one of these slurries with a source of phosphorus, combining the slurries, and spray-drying at a pH of below 3. Catalyst compositions obtained with this process are said to have an improved attrition resistance. In US 5,110,776 a phosphorus treatment was used to improve the attrition resistance of catalyst compositions and to improve the octane yield. Here a Y zeolite is treated with a phosphorus-containing aqueous solution, and said treated zeolite is combined directly with a matrix precursor to form a slurry. Said slurry is spray-dried. US 5,601,699 describes the treatment with phosphorus of zeolite BETA, ZSM-12, and ZSM-20 to obtain catalytic cracking catalysts with improved attrition restistance. EP-A-511 013 describes the treatment of ZSM-5 with phosphorus to increase the propyiene selectivity. Further, US 5,472,594 describes a process for converting a hydrocarbon feed to a product containing improved yields of olefins with a catalyst composition containing zeolite Y and an additive comprising a phosphorus-containing medium pore zeolite such as ZSM-5. Also Mobil's WO 98/41595 describes a process for the catalytic cracking of a hydrocarbon feedstock to produce an enhanced yield of C3 to C5 olefins using a catalyst composition comprising a large pore molecular sieve such as zeolite Y and an additive comprising a phosphorus-containing ZSM-5 blended in with the base catalyst containing zeolite Y. The same is described in US 5,456,821. WO 94/13754 describes the same process using a catalyst composition containing a large pore molecular sieve and an additive containing a specific ZSM-5 which, optionally, contains 1.5 to 5.5 wt% elemental phosphorus. Also US 5,521 ,133 describes the preparation of a ZSM-5 additive by injecting a ZSM-5 and kaolin slurry with phosphoric acid prior to spray-drying. US 3,972,832 describes the phosphorus treatment of ZSM-5 for use as a catalyst for the conversion of aliphatics. In US 4,002,698 phosphorus-treated ZSM-5 is described for use in the catalytic methylating of toluene.
Said activated crystalline porous silicates can be used as a component of a catalyst composition or in additives which can be physically mixed with a catalyst composition, the appropriate physical form depending on the desired use. In the case of use as an additive, care must be taken not to dilute the total catalyst composition too much. This means that for use as additive, it must be possible to include a sufficient amount of crystalline porous silicate in the additive to obtain the desired activity. Further, it is necesarry to activate the crystalline porous silicate to a sufficent level. In the case of use as a catalyst component, care must be taken that the incorporation of the activated crystalline porous silicate does not interfere with the other components of the catalyst composition. This is a serious problem with phosphorus activation, because phosphorus-containing compounds tend to interfere with alumina, which is quite a conventional component of catalyst compositions. Said problem can be solved by using so-called ex situ activation. This means that the crystalline porous silicate is treated with a phosphorus-containing compound, dried and calcined, prior to addition of said crystalline porous compound to other catalyst or additive components shaping and calcination. Thus, ex situ activation should take place essentially in the absence of alumina. Sinopec's EP-A1 -0909-582 describes ex situ phosphorus activation of crystalline alumina silcates. It describes the preparation of a catalyst composition for the production of light olefins by mixing the matrix components, adding a mixture of a Y-type zeolite and a high silica zeolite with pentasil structure such as ZSM-5 containing 2-8 wt% (based on the weight of the zeolite) of phosphorus (calculated as P2O5) and 0.3-3 wt% of aluminium or magnesium or calcium. The zeolite mixture is treated with an aqueous solution of phosphorus/aluminium or phosphorus/- magnesium or calcium compounds, dried, and calcined prior to the addition to the matrix components. NL-9301333 describes the ex situ activation of ZRP zeolite with an aluminium phosphate sol. Said activated ZRP zeolite is incorporated into a catalyst composition containing zeolite Y, clay, and organic oxides.
The present invention provides an ex situ activation, so rendering the activated crystalline porous silicate suitable for incorporation into catalyst compositions. Said novel activation method further provides sufficient activation to render the activated crystalline porous silicate suitable for use in additives. The activation method is universally applicable, which means that all types of crystalline porous silicates may be treated in this fashion. Therefore, starting materials may be used which were not previously applicable and novel activated materials can be obtained. Furthermore, the invention provides an activation method which is more economical and more environmentally friendly than the known phosphorus activation methods. In the known activation methods, the phosphorus-containing compound is always combined with the crystalline porous silicate in the liquid state: the crystalline porous silicate is always impregnated with a phosphorus compound-containing solution. If the phosporus-containing compound is solid, it is first dissolved in a solvent prior to being combined with the zeolite. This means that after treatment the mixture must be dried and sometimes filtered before drying. This is uneconomical, because it requires an additional step and extra energy and is, of course, environmentally unfriendly. The present invention is directed to ex situ solid-state phosphorus-activated crystalline porous silicate. Although the p-NMR spectrum of the phosphorus- activated crystalline porous silicate according to the invention differs from the phosphorus-activated porous silicates of the prior art, the present invention provides an activated crystalline porous silicate with an activity which is comparable with that of crystalline porous silicates activated using conventional methods.
The ex situ phosphorus-activated crystalline porous silicate according to the invention may be prepared by: a) combining crystalline porous silicate with a phosphorus-containing compound in the solid state, b) intimately mixing the crystalline porous silicate/phosphorus-containing compound mixture, c) calcining the crystalline porous silicate/phosphorus-containing compound mixture to obtain a phosphorus-activated crystalline porous silicate. For this process no intermediate drying is necessary. Crystalline porous silicates and p-containing compounds usually contain some water, and it is not necessary to dry the starting materials until they are completely dry. For the purpose of this description the term "solid-state" is defined as not having to dry the resulting mixture before calcining. Suitable phosphorus-containing compounds are all phosphorus compounds which are solid at the temperature at which they are combined with the crystalline alumina silicate. Examples are phosphoric acid salts such as ammonium dihydrogen phosphate and diammonium hydrogen phosphate, ammonium hypophosphate, ammonium orthophosphate, ammonium dihydrogen orthophosphate, ammonium hydrogen orthophosphate, triammonium phosphate, phosphines, and phosphites and mixtures thereof. It is preferred to use phosphorus-containing compounds which do not leave undesirable metals on the crystalline porous silicate. Therefore, the addition of for instance sodium salts is not advised.
The amount of phosphorus-containing compound to be used may vary from 0.1 to 50 wt% (calculated as P2Os based on the crystalline alumina silicate). In FCC applications preferably 10-25 wt% is used.
All types of crystaiiine porous silicates may be used. These include both layered silicates and microporous silicates. Examples of suitable crystalline porous layered silicates, which in the prior art are also referred to as clays, including anionic clays and cationic clays, are kaolin, hydrotalcites, smectites, hectorites, montmorillonites, saponites, sepiolites, sjόgrenites, etcetera.
The most common crystalline microporous silicates are metallosiiicates. All types of microporous silicates may be used and may be in the hydrogen form, the ammonium form, or the ion-exchanged form, e.g., one or more rare earth metals. A specific type of metallosilicate which can suitably be used is the crystalline alumina silicate.
Examples of suitable crystalline microporous silicates include the MFI-type zeolites, faujasite-type zeolites such as Y-type zeolite, zeolite X and ZSM-20, MEL-type zeolites such as ZSM-11 , ZSM-12, mordenite zeolites, ETS-4-type, ETS-10-type, MTW-type zeolites such as ZSM-12, MWW-type zeolites such as MCM -22, MCM-36, MCM-49, MCM-56, HEU-type zeolites, CHA-type zeolites, GME-type zeolites, EUO-type zeolites, ERI-type zeolites, FER-type zeolites, OFF-type zeolites, and BEA-type zeolites such as zeolite beta. MFI-type zeolites and faujasite-type zeolites are preferred.
MFI-type zeolites are as defined in the ATLAS OF ZEOLITE STRUCTURE TYPES, W.M. Meier and D.H. Olson, 3rd revised edition (1992), Butterworth-
Heinemann, and include ZSM-5, ST-5, ZSM-8, ZSM-11, silicalite, LZ-105, LZ-
222, LZ-223, LZ-241 , LZ-269, L2-242, AMS-1 B, AZ-1 , BOR-C, Boralite, Encilite, FZ-1 , NU-4, NU-5, T5-1 , TSZ, TSZ-III, TZ01 , TZ, USC-4, USI-108, ZBH, ZB-11 , ZBM-30, ZKQ-1B, ZMQ-TB.
Examples of faujasite-type zeolites are the Y zeolites and zeolite X. All zeolites Y which are normally used in catalyst compositions are suitable and may be in the hydrogen form, the ammonium form, or the ion-exchanged form, e.g., one or more rare earth metals. Examples are de-aluminated zeolite Y, silica-enriched de-aluminated zeolite Y, and ultrastable zeolite Y (USY).
Next, the phosphorus-containing compound and the crystalline porous silicate are intimately mixed. This may be done by means of dry milling, for instance in a ball mill, a kneader or any other means which allows intimate mixing of solid materials. As mentioned above, some liquid may be present in the mixture, as long as no drying step is necessary prior to calcination. For instance, processing aids may be added to improve the conditions for intimate mixing.The mixing temperature may vary fom 0°C to the decomposition temperature of the phosphorus-containing compound used. The mixing time depends on the mixing means used.
After the mixing step, the resulting mixture is calcined at temperatures between 300 and 1000X, preferably between 450 and 700°C, for about 15 minutes to 24 hours, depending on the amount of phosphorus-containing compound used and the type and amount of crystalline porous silicate used. The calcination step may be conducted in an inert, a reducing or an oxidising atmosphere such as air.
As mentioned above, the activated crystalline porous silicates according to the invention are suited to be incorporated into catalyst compositions. Owing to the ex situ activation, the phosphorus-containing compound present on the crystalline porous silicate is immobilised and will hardly interfere with any other catalyst components in the strike. Conventional catalyst components are catalytically active components such as the activated crystalline porous silicate according to the invention, optionally, additional catalytic components besides the activated crystalline porous silicate of the invention, binder or matrix material, and, optionally, additives to improve the physical and catalytic properties of the catalyst composition such as crystalline alumina, anionic clays, cationic clays, metal compounds, etctera, and fillers such as clay, for instance kaolin. Suitable binders ususally are alumina, silica, and silica-alumina. Thus, catalyst compositions according to the invention may comprise activated porous silicates according to the invention such as activated crystalline layered silicates, activated crystalline microporous silicates including metallosilicates or mixtures thereof. Preferred is the incorporation of activated metallosilicate such as actived MFI-type zeolite, activated faujasite-type zeolite, activated MCM-22 zeolite, activated mordenite, activated FER-type zeolite and/or BEA-type zeolite.
These types of catalyst compositions can suitably be used for the conversion of hydrocarbon feedstocks, the catalytic cracking of hydrocarbon feedstocks, and the conversion of aromatics or aliphatics.
The various catalyst components can be combined in any sequence, but it is preferred to add the phosphorus treated crystalline porous silicate to the strike last, so as to avoid any interference of the phosphorus with the other catalyst components.
An example of a catalyst composition which is very suitable for use in FCC comprises: a) 10 to 40 wt% Y type zeolite, b) 0.1 to 35 wt% activated MFI-type zeolite according to the invention, c) 10-20 wt% alumina binder, d) 1-15 wt% silica.
This catalyst composition appears to provide high propylene yields in combination with bottoms cracking, which is highly desirable for use in FCC. With an activated MFI-type zeolite or activated MCM-22 according to the invention, catalyst compositions can be prepared which are extremely suitable for the alkylation of aromatics.
With an activated MFI-type zeolite, activated MCM-22 or activated mordenite according to the invention, catalyst compositions can be prepared which are extremely suitable for the disproportionation of aromatics.
With an activated MFI-type zeolite, activated MCM-22 or activated zeolite beta according to the invention, catalyst compositions can be prepared which are extremely suitable for the isomerisation of aromatics.
With an activated FER-type zeolite, activated faujasite or activated zeolite beta according to the invention, catalyst compositions can be prepared which are extremely suitable for the alkylation of aliphatic compounds.
For the isomerisation of aliphatic compounds, activated FER-type zeolites or activated MFI-type zeolites may be incorporated into catalyst compositions. Also for the preparation of caprolactam activated MFI-type zeolites according to the invention may be incorporated into catalyst compositions.
The ex situ solid-state phosphorus-activated crystalline alumina silicates according to the invention can suitably be incorporated into catalyst additives. Said additives may then be physically mixed with a catalyst composition. Usually, said activated crystalline alumina silicate is combined with a matrix (precursor), and optionally other additives suchas metal compounds, and spray- dried or shaped by any other means conventionally used in the catalyst field. All matrix (precursors) normally used may be applied here. Examples are aluminas such as (pseudo)boehmite, silica, silica-alumina, titania, zirconia. Said additives are suitable for various purposes. For instance, a catalyst additive comprising an activated MFI-type crystalline alumina silicate can suitably be used for octane enhancement in FCC processes or for increasing the propylene yield in FCC processes. For these applications the phosphorus content on the MFI-type zeolite should be at least 10 wt% (calculated as P2O based on the MFI-type zeolite). Usually between 5 and 25 wt% of the additive is added to the FCC base catalyst.
The present invention is further illustrated by the Examples, which should in no way be construed as being limitative.
EXAMPLES
Example 1 : solid-state ex situ activation of MFI-type zeolite
Dried SM-27 ® (ex AISi Penta) was mixed with 25wt% (NH4)H2PO corresponding to an addition of 15.3 wt% P2O5 (on a phosphorus basis) on SM- 27 and milled in a ball mill for 1 hour. The mixture was calcined at 600°C for 1 hour. The resulting activated MFI-type zeolite had a P2Os content of 10.5 wt%. P-NMR showed a material having a single broad peak at about 38 ppm.
Comparative example 2: slurry ex situ activation of MFI-type zeolite
SM-27 ® (ex AISi Penta) was slurried to obtain a 30 % slurry. H3PO4 was added to a level of 10 wt% P2O5 on SM-27. The pH was adjusted to above 4.5 with ammonia. The mixture was dried at 120°C overnight and calcined at 600°C for 1 hour. P-NMR showed a material with a different pattern: a compound feature containing multiple peaks with the maximum at about 5 ppm.
The micropore volume of both the solid state phosphorus activated MFI type zeolite and the slurry activated MFI type zeolite was measured by ESW (excess surface work) nitrogen adsorption measurement. In this method the zeolites are provided in a pressure vessel containing nitrogen gas immersed in liquid nitrogen. Nitrogen adsorption isotherms are measured with the P/P0 varying from 0.000001 to 1. The first minimum obtained when plotting the product of the amount of nitrogen adsorbed and the natural logarithm ln(P/P0) against the amount of nitogen adsorbed, gives a measure of the amount of nitrogen which is adsorbed in the micropore volume (na mιn). From na mιπ ( in cm3/g) the micropore volume can be calculated by multiplying it by the density of liquid nitrogen (i.e., 0.00155 ). The first minimum of the solid state activated MFI-type zeolite was 22.37 at a pressure of 5.6 X 10"5 Pa which corresponds to a micropore volume of 0.035 ml/g. The first minimum of the slurry activated MFI- type zeolite was 27.37 at a pressure of 8.0 X 10"5 Pa, which corresponds to a mocropore volume of 0.042 ml/g. This shows that with solid state phosphorus activation a different material is obtained then with conventional slurry phosphorus activation. Not only are the micropore volumes different, but also the pore volumes are built up in a different way, which is shown by the fact that the minima occur at different pressures.
Example 3: incorporation of activated MFI-type zeolite into catalyst composition
Catalyst compositions were prepared of both the solid-state-activated and the slurry-activated MFI-type zeolite by adding 5 wt% of the activated MFI-type zeolite as the last component to a strike containing 13.5 wt% REY zeolite, 18 wt% peptised pseudoboehmite, and 5 wt% silica. The strike was spray-dried. The catalyst compositions were steamed for 20 hours at 788°C. The physical properties of the two catalyst compositions are listed in TABLE 1.
TABLE 1 : Physical properties of the catalyst compositions
Both catalyst compositions were tested for catalytic cracking using Kuwait vacuum gas oil as a feedstock. The performance at catalyst to oil ratio 4 is reported in TABLE 2. It was acceptable to report at constant catalyst to oil ratio instead of at constant conversion because the activity difference was minimal, so the overall ranking was not changed by this.
TABLE 2: comparison performance of the catalyst compositions
The results show that with the activation method according to the invention, activated crystalline alumina silicates can be obtained which are comparable with the activated zeolites obtained by other, less economical and less universally applicable ex situ activation methods.

Claims

Claims
1. Ex situ solid-state phosphorus-activated crystalline porous silicate.
2. Process for the ex situ phosphorus activation of a crystalline porous silicate comprising the following steps: a) combining crystalline porous silicate with a phosphorus-containing compound in a solid-state, b) intimately mixing the crystalline porous silicate/phosphorus-containing compound mixture, c) calcining the crystalline porous siiicate/phosphorus-containing compound mixture to obtain a phosphorus activated crystalline porous silicate.
3. Ex situ solid-state phosphorus-activated crystalline porous silicate according to claim 1 wherein the crystalline porous silicate is a crystalline layered porous silicate, preferably an anionic clay or a cationic clay .
4. Ex situ solid-state phosphorus-activated crystalline porous silicate according to claim 1 wherein the crystaiiine porous silicate is a crystalline microporous silicate, preferably a metallosilicate, in particular an aluminosilicate.
5. Ex situ solid-state phosphorus-activated crystalline aluminosilicate according to claim 4 wherein the crystalline aluminosilicate is an MFI-type zeolite or a Y-type zeolite.
6. Catalyst composition comprising an ex situ solid-stae phosphorus- activated crystalline porous silicate according to any one of claims 1 , 3, 4, and 5.
7. Use of the catalyst composition of claim 6 in the conversion of hydrocarbon feeds, e.g., in the alkylation of aromatics, the solid-state phosphorus-activated crystalline porous silicate being activated MFI type zeolite or activated MCM-22 zeolite, or in the isomerisation of aromatics, the solid-state phosphorus-activated crystalline porous silicate being activated MFI type zeolite, activated MCM-22 zeolite, or activated beta zeolite, or in the disproportionation of aromatics, the solid-state phosphorus-activated crystalline porous silicate being activated MFI type zeolite, activated MCM-22 zeolite, or activated mordenite, or in the alkylation of aliphatic compounds, the solid-state phosphorus-activated crystalline porous silicate being activated FER type zeolite, activated faujasite or activated zeolite beta, or in the isomerisation of aliphatic compounds, the solid-state phosphorus-activated crystalline porous silicate being activated FER type zeolite or activated MFI type zeolite, or in the preparation of caprolactam, the solid-state phosphorus-activated crystalline porous silicate being activated MFI type zeolite.
8. Catalyst composition comprising: a) 10 to 40 wt% Y-type zeolite, b) 0.1 to 35 wt% ex situ solid-state phosphorus-activated MFI-type zeolite according to claim 5, c) 10-20 wt% alumina binder, d) 1-15 wt% silica.
9. Catalyst additive comprising a solid state phosphorus-activated crystaiiine porous silicate according to any one of claims 1 , 3, 4 or 5.
10. Use of the catalyst of claim 6 or 8 or the additive of claim 9 comprising an activated MFI-type zeolite in the catalytic cracking of a hydrocarbon feed, with the additive being used in combination with a conventional catalytic cracking catalyst, to effect octane enhancement in FCC processes, and/or for increasing the propylene yield in FCC processes.
EP00990607A 1999-11-22 2000-11-17 Ex situ solid-state phosphorus activation of crystalline porous silicates Withdrawn EP1242185A2 (en)

Priority Applications (1)

Application Number Priority Date Filing Date Title
EP00990607A EP1242185A2 (en) 1999-11-22 2000-11-17 Ex situ solid-state phosphorus activation of crystalline porous silicates

Applications Claiming Priority (6)

Application Number Priority Date Filing Date Title
US16689499P 1999-11-22 1999-11-22
US166894P 1999-11-22
EP00200091A EP1116519A1 (en) 2000-01-12 2000-01-12 Solid-state phosphorous activation of crystalline porous silicates
EP00200091 2000-01-12
PCT/EP2000/011534 WO2001037994A2 (en) 1999-11-22 2000-11-17 Ex situ solid-state phosphorus activation of crystalline porous silicates
EP00990607A EP1242185A2 (en) 1999-11-22 2000-11-17 Ex situ solid-state phosphorus activation of crystalline porous silicates

Publications (1)

Publication Number Publication Date
EP1242185A2 true EP1242185A2 (en) 2002-09-25

Family

ID=8170901

Family Applications (2)

Application Number Title Priority Date Filing Date
EP00200091A Withdrawn EP1116519A1 (en) 1999-11-22 2000-01-12 Solid-state phosphorous activation of crystalline porous silicates
EP00990607A Withdrawn EP1242185A2 (en) 1999-11-22 2000-11-17 Ex situ solid-state phosphorus activation of crystalline porous silicates

Family Applications Before (1)

Application Number Title Priority Date Filing Date
EP00200091A Withdrawn EP1116519A1 (en) 1999-11-22 2000-01-12 Solid-state phosphorous activation of crystalline porous silicates

Country Status (7)

Country Link
EP (2) EP1116519A1 (en)
JP (1) JP2003514752A (en)
KR (1) KR20020059669A (en)
CN (1) CN1391500A (en)
BR (1) BR0015725A (en)
CA (1) CA2389510A1 (en)
WO (1) WO2001037994A2 (en)

Families Citing this family (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US7038100B2 (en) * 2001-04-30 2006-05-02 Exxonmobil Chemical Patents, Inc. Aromatics alkylation
JP5229986B2 (en) * 2004-03-22 2013-07-03 エクソンモービル・ケミカル・パテンツ・インク Steam cracking method for heavy hydrocarbon feedstock
WO2006107462A1 (en) 2005-03-31 2006-10-12 Exxonmobil Chemical Patents Inc. Process and catalyst for the transalkylation of aromatics
US7368410B2 (en) * 2005-08-03 2008-05-06 Saudi Basic Industries Corporation Zeolite catalyst and method of preparing and use of zeolite catalyst
JP5400215B2 (en) * 2010-03-18 2014-01-29 株式会社小松製作所 Hydraulic pump / motor and method for preventing pulsation of hydraulic pump / motor
JP2012139640A (en) 2010-12-28 2012-07-26 Jx Nippon Oil & Energy Corp Catalyst for producing monocyclic aromatic hydrocarbon and method of producing the monocyclic aromatic hydrocarbon
WO2013059169A1 (en) 2011-10-17 2013-04-25 Exxonmobil Research And Engineering Company Phosphorus modified zeolite catalysts
WO2018064599A1 (en) 2016-09-30 2018-04-05 Abdelrahman Omar A Forming dienes from cyclic ethers and diols, including tetrahydrofuran and 2-methyl-1,4-butanediol

Family Cites Families (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4250059A (en) * 1979-08-27 1981-02-10 Uop Inc. Catalytic composite, method of manufacture
JPS6115848A (en) * 1984-06-30 1986-01-23 Agency Of Ind Science & Technol Production of lower olefin using zeolite catalyst modified with calcium phosphate
US4975180A (en) * 1989-06-05 1990-12-04 Exxon Research And Engineering Company Cracking process
WO1999002260A1 (en) * 1997-07-11 1999-01-21 Shell Internationale Research Maatschappij B.V. Catalyst composition comprising a molecular sieve and an aluminium phosphate containing matrix

Non-Patent Citations (1)

* Cited by examiner, † Cited by third party
Title
See references of WO0137994A2 *

Also Published As

Publication number Publication date
CA2389510A1 (en) 2001-05-31
JP2003514752A (en) 2003-04-22
KR20020059669A (en) 2002-07-13
WO2001037994A2 (en) 2001-05-31
EP1116519A1 (en) 2001-07-18
BR0015725A (en) 2002-08-06
WO2001037994A3 (en) 2001-11-01
CN1391500A (en) 2003-01-15

Similar Documents

Publication Publication Date Title
CA2392232C (en) Catalyst composition with high efficiency for the production of light olefins
JP6133989B2 (en) A novel catalyst to increase propylene yield from fluid catalytic cracking unit
KR100903898B1 (en) Catalyst for the production of light olefins
CA2618039C (en) Hydrothermally stable microporous molecular sieve catalyst and preparation method thereof
EP0185500B1 (en) Hydrocarbon conversion catalysts and processes utilizing the same
EP2248582B1 (en) Catalyst for catalytic cracking of hydrocarbon, which is used in production of light olefin and production method thereof
JP5135457B2 (en) Catalytic cracking process using a catalyst composition comprising phosphorus-containing zeolite IM-5
US20100144514A1 (en) Process for Making Catalyst for Olefin Upgrading
MX2014005436A (en) Phosphorus modified cracking catalysts with enhanced activity and hydrothermal stability.
US20160216242A1 (en) Fcc catalyst additive and a method for its preparation
RU2612973C2 (en) Novel catalyst to increase propylene yields from fluid catalytic cracking unit
WO2001037994A2 (en) Ex situ solid-state phosphorus activation of crystalline porous silicates
JP2023544829A (en) Zeolite stabilized with phosphorus

Legal Events

Date Code Title Description
PUAI Public reference made under article 153(3) epc to a published international application that has entered the european phase

Free format text: ORIGINAL CODE: 0009012

17P Request for examination filed

Effective date: 20020410

AK Designated contracting states

Kind code of ref document: A2

Designated state(s): AT BE CH CY DE DK ES FI FR GB GR IE IT LI LU MC NL PT SE TR

STAA Information on the status of an ep patent application or granted ep patent

Free format text: STATUS: THE APPLICATION HAS BEEN WITHDRAWN

18W Application withdrawn

Effective date: 20030512