WO2005094990A1 - Composition catalytique de craquage catalytique de dechets plastiques - Google Patents

Composition catalytique de craquage catalytique de dechets plastiques Download PDF

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Publication number
WO2005094990A1
WO2005094990A1 PCT/IN2004/000366 IN2004000366W WO2005094990A1 WO 2005094990 A1 WO2005094990 A1 WO 2005094990A1 IN 2004000366 W IN2004000366 W IN 2004000366W WO 2005094990 A1 WO2005094990 A1 WO 2005094990A1
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Prior art keywords
catalyst
plastic
waste
catalytic cracking
mixture
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PCT/IN2004/000366
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English (en)
Inventor
Umesh Zadgaonkar
Ajay Kumar Arora
Biswanath Sarkar
Shanti Parkash
Krishan Kumar Swami
Rakesh Sarin
Venkatachalam Krishnan
Satish Makhija
Ram Prakash Verma
Sobhan Ghosh
Niranjan Raghunath Raje
Alka Umesh Zadgaonkar
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Indian Oil Corporation Limited
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Publication of WO2005094990A1 publication Critical patent/WO2005094990A1/fr

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    • 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
    • B01J37/0009—Use of binding agents; Moulding; Pressing; Powdering; Granulating; Addition of materials ameliorating the mechanical properties of the product catalyst
    • B01J37/0027—Powdering
    • B01J37/0045—Drying a slurry, e.g. spray drying
    • 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
    • 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
    • B01J29/084—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
    • B01J29/08—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
    • C—CHEMISTRY; METALLURGY
    • C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
    • C08J—WORKING-UP; GENERAL PROCESSES OF COMPOUNDING; AFTER-TREATMENT NOT COVERED BY SUBCLASSES C08B, C08C, C08F, C08G or C08H
    • C08J11/00—Recovery or working-up of waste materials
    • C08J11/04—Recovery or working-up of waste materials of polymers
    • C08J11/10—Recovery or working-up of waste materials of polymers by chemically breaking down the molecular chains of polymers or breaking of crosslinks, e.g. devulcanisation
    • C08J11/16—Recovery or working-up of waste materials of polymers by chemically breaking down the molecular chains of polymers or breaking of crosslinks, e.g. devulcanisation by treatment with inorganic material
    • 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
    • C10G1/00—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
    • C10G1/08—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal with moving catalysts
    • 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
    • C10G1/00—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
    • C10G1/10—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal from rubber or rubber waste
    • 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
    • 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
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
    • Y02W30/00—Technologies for solid waste management
    • Y02W30/50—Reuse, recycling or recovery technologies
    • Y02W30/62—Plastics recycling; Rubber recycling

Definitions

  • the present invention relates to a process of preparing catalytic cracking catalyst for use in catalytic cracking waste plastic.
  • Background of the In ention Plastic is widely used in all kinds of products in the industry and out- daily life and in considerable quantities because of its numerous advantages such as being cheap, light easily shaped and water resisting.
  • Polyethylene, polypropylene, polyvinylchloride, polystyrene are few examples of these polymeric plastic materials. Therefore, plastic waste has become a major element in garbage. However, because most of the plastic waste does not decompose naturally in garbage dumps and creates toxic smoke after burning, it is not environment friendly and causes very serious environmental problems.
  • plastic waste could be containing polyethylene, polypropylene, polyvinyl chloride, polyvinylidene chloride, ABS resin, polyvinyl alcohol, polycarbonate, polyester resin or polyamide.
  • the pyrolysis of plastic waste could lead to the formation of a mixture of hydrocarbons like paraffin and olefin.
  • PCDD polychlorinated dibenzodioxins
  • PCDF dibenzofurans
  • PCB polychloro biphenyls
  • a process for a making of high VI lubricating oil composition from mixture of waste plastics through the steps of pyrolysis, hydro-treating and catalytic dewaxing has been claimed in US Patent No. 6150577.
  • plastic waste has been converted to high VI lubricating oil composition with additional step of dimerization, as claimed in US Patent No. 62S8296.
  • the above-cited patents cover a wide spectrum of manufacture of hydrocarbon mixtures, from ethylene, propylene to lubricating oils and aromatic pitches.
  • Waste plastics, that are polymer of high molecular weight have a problem that on simple thermal decomposition they produce mainly waxy distillates with little or no production of gasoline, kerosene, light oils etc.
  • the object of the present invention is to provide a process for preparing a catalytic cracking catalyst for conversion of waste plastic to higher olefins (C to C 2 ).
  • the present invention provides a process of preparing a catalytic cracking catalyst comprising: mixing the following ingredients in the proportion indicated there against faujasite zeolite - 5-35 wt % pseudoboehmite alumina - 10-40 wt % polyammonium silicate - 1-10 wt % kaolin clay - 15-60wt % milling said ingredients and making a slurry using water, spray drying said slurry to micro-spheres, and - calcining said micro-spheres at 500°C for 1 hour to obtain the catalyst Water used is a demineralized water.
  • the said ingredients are in the following proportion: Faujasite zeolite - 15-30 wt % Pseudoboehmite alumina - 20-40 wt % Polyammonium silicate - 1-10 wt % Kaolin clay - 40-60wt %
  • the present invention also provides a catalytic cracking catalyst whenever prepared by the above process .
  • a process of catalytic cracking waste plastics using the catalyst comprises: cleaning, shredding and cutting waste plastics into at least lxl mm pieces, mixing said plastic waste pieces with 2-10 % by wt of said catalyst, cracking said mixture of plastic water pieces and catalyst at 300 to 400°C under atmospheric pressure to obtain a mixture of C 4 -C 25 olefins.
  • the waste plastics contain either polyethylene, polypropylene, polyvinyl chloride, polystyrene, polyethylene, teiphthalate, polymide and mixture thereof
  • the percentage of catalyst used in the catalytic cracking of plastic waste varies with respect to the plastic waste cracked.
  • DETAILED DESCRIPTION OF THE INVENTION The present invention provides a process for conversion of readily available waste plastic to selectively produce olefins (C 4 to C 25 ) using indigenously developed zeolite based acid catalyst C 4 - C 25 polyolefins are used for the synthesis of synthetic hydrocarbon products like pblypalphaolefin, linear alkyl benzene.
  • syntlietic lubricants exhibit lower friction characteristics and are used in various types of equipment including auto-engine, transmission, worm gears and traction-devices.
  • the superiority in terms of appropriate viscosity over wide temperature range, low pour point, high oxidative and thermal stability is well established than natural mineral oils.
  • the cost of ⁇ -olef ⁇ ns monomers has been major constraints in the commercialization of synthetic lubricant. The search efforts are directed towards development of new sources of ⁇
  • US Patent No. 5847209 claims to a process for the separation of olefins and paraffins from the paraffin-olefm mixture by formation of urea adduct refinery petroleum streams.
  • US Patent No. 6184429 has utilized the separated olefin mixture for the synthesis of olefin oligomers. There are claims for production of lower olefins by the pyrolysis plastic waste as in US Patent 5639937.
  • the raw materials for this process is usual urban and industrial waste plastic which contains PP, PE, PVC, PET, PS etc. type of plastic.
  • This waste plastic is treated with an indigenously developed solid acidic catalyst at 300 r 400 °C.
  • the catalyst to feed wt ratio is 1-10 % and heating rate is optimized in order to get preferentially higher olefins.
  • Catalyst The Zeolite Component
  • the zeolite used may be any derivatives of faujasite, like NaNH 4 . Y, ReNH .4 Y.
  • USY zeolite is employed having high hydrothe ⁇ nal stability, with S ; O 2 /Al .2 O3 ra ti° of 6.5-8.0.
  • the sodium content present h USY zeolite is preferred to be less than 1% wt.
  • rare-earth exchanged USY zeolite Rare earth source may be single rare-earth chloride or a mixture of rare- earth chlorides (of La, Ce, Nd, Pr).
  • low soda USY zeolite is dispersed in rare-earth chloride solution at elevated temperature of 60- 80. degree. C .
  • the Pseudoboehmite Component Preferably, binder grade/pseudoboehmite is used having high crystallinity and crystallite size in the range of 45-60 A 0 and having low sodium content, preferably less than 0.1% wt.
  • the alumina is preferred to have good surface area of 200-300 m 2 /g.
  • the pseudoboehmite alumina with the above properties is required to be gelled by a suitable acid, mineral or organic.
  • Organic acids are preferred in place of mineral acids as chloride, sulfate, and nitrate radicals present in the latter are hazardous to hardware as well as to environment.
  • Gelling character of alumina depends on nature of acid, quantity, and temperature. We have found that in order to obtain an alumina suitable to bind zeolite and clay and make the slurry pumpable, balanced quantity of acid must be used and gelled under controlled conditions. Alumina used in the present investigation has surface area of 260 m " /g, crystallite size of 55 A° pore radius of 28 A .
  • the Polysilicate Component Polysilicate either Na stabilized or NH 4 stabilized with low soda content is referred for use in the catalyst of our invention.
  • NH 4 stabilized polysilicate is more preferred than the Na stabilized polysilicate, for the reason of lower sodium level.
  • This ingredient due to its free flow nature and availability in low soda form, is ideal for creating low acidic matrix in the catalyst in the presence of alumina.
  • Polysilicate. with small particle size of 180-250 A 0 is preferred for incorporation into the catalyst of our invention.
  • Ammonium polysilicate w ith 16% Si0 2 content and average particle size of 220 A is used in the present investigation.
  • the Clay Component Clays are used in cracking catalysts as filler, for improving the density and dissipation of heat. The most commonly used clays are kaolinite and halloysite.
  • Clays for the application of catalyst formations are required to be purified and have average particle size of about 2 microns or less.
  • the clay, which is used in the present investigation, is of kaolinite type with more than 80 % fractions below 2 microns and sodium content of less than 0.3 wt %.
  • the zeolite component present hi the catalyst composite is in the range of 5-35 wt %, a preferred range being from 15-30 wt %, modified alumina is in the range of 10-40 wt %, a preferred range being 20-30 wt %.
  • Kaolin clay is present in the range of 40-60-wt %, the preferred range being 45-55 wt %.
  • the residual soda level in the finished catalyst is in the range of 0.2-0.7 wt %, preferred level being less than 0.5 wt %.
  • the rare earth oxide content in the catalyst is in the range of 0.5-2 wt %., the preferred range being 0.8-1.2 wt %.
  • the rare earth metal salts employed can either be the salt of a single rare earth metal or mixture of rare earth metals, such as chlorides consisting essentially of Lanthanum, Cerium, Neodymium with minor amounts of Samarium, Gadolinium, and Yttrium.
  • the features described in the foregoing description and in the following may, both separately and in any combination thereof, be material for realizing this invention in diverse forms thereof.
  • the present invention is further described in the following examples, which, however, is not to b e construed as limiting. The results are shown in Table I EXAMPLE-1
  • This example describes the process for the preparation of modified alumina with silica.
  • 38 gm .of formic acid 85 wt % concentration, LR grade, M/s SD Fine Chemicals, India
  • DM water 750 g
  • 214 g of alumina was added (Pural SB grade with 24 wt % moisture from M/s. Condea, Germany) under stirring.
  • the mixture was held for 24 hrs at 40 °C.
  • the viscous alumina product with a pH of 2.5-2.75 was then reacted with 156 g of Ammonium Polysilicate (16 wt% Si02, from M/s Bee Chems, Kanpur, India) and was ready for use.
  • This example illustrates the process for preparation of rare earth exchanged USY zeolite.
  • 300 g commercial USY zeolite (with 1 1 wt % moisture, 1 .35 wt % N a, 86% crystallinity, from M/s P Q Corporation, U SA) was dispersed in 1 wt % rare earth chloride solution, maintaining solid-liquid ratio o f 1: 10 at a t emperature of 60 ° C. C.
  • zeolite was washed chloride free and dried at 1 10 C , for 16 hours to obtain rare earth exchanged ammonium Y zeolite.
  • the product contains 4 wt %, ReO, 0.9
  • This example describes the process for preparation of catalyst using rare earth exchanged USY zeolite prepared as per example 2, non-modified alumina, ammonium polysilicate, and kaolin clay.
  • Slimy with pH of 3.5 and solid content of 28 wt% was prepared, having the following composition (wt %): zeolite 25, alumina 30, kaolin clay 40 and silica 5.
  • 214 g of alumina was reacted with 17.25 g of formic acid at room temperature (20 °C).
  • To the alumina 156 g of ammonium polysilicate and 253 g of kaolin clay (with 15 wt % moisture from M/s Huawei Ceramics, refinera, India) were added.
  • This example illustrates a process of preparing catalyst as per Example 3 with the exception that modified aluminum silica composite prepared as per example 1 of this invention was used. The product was calcined and steam deactivated.
  • Faujasite zeolite, pseudoboehmite, alumina, polyammonium silicate and kaolin clay are combined in particular ratios to get the finished catalyst.
  • the content of Faujasite zeolite is about 5 to 35 %
  • the content of pseudoboehmite, alumina is about 10 to 40 wt %
  • the content of polyammonium silicate is about 1 to 10 % wt
  • the content of the kaolin clay is about 1-60 wt%.
  • This example illustrates a process of preparing catalyst Faujasite zeolite, pseudoboehmite, alumina, polyammonium silicate and kaolin clay are combined in particular ratios to get the finished catalyst.
  • the content of Faujasite zeolite is about 25 %
  • the content of pseudoboehmite, alumina is about 30 wt %
  • the content of polyammonium silicate is about 5% wt
  • the content of the kaolin clay is about 40wt%.
  • EXAMPLE-7 The thermal cracking of polystyrene predominant plastic, which was cleaned, shredded and cut into 1 X 1 mm pieces was carried out in a catalytic reactor.
  • the cracking is carried out under atmospheric pressure and at a temperature range of 300-400°C.
  • the catalyst used is an indigenously developed zeolite based acidic catalyst, which is used in the ratio of 3 wt% of the plastic taken.
  • the resulting gaseous hydrocarbons are passed through column of calcium oxide to make it chlorine free gaseous hydrocarbons.
  • the wt% distillate obtained is in the range of 70-90 wt% by weight of the starting material taken.
  • Gas chromatography shows the distillate to be predominantly C 6 -C 9 olefins.
  • the residual left over in the catalytic reactor is mixed with equal amount of non - edible vegetable oil and heated to temperature range o f 1 00-120° C and then discharged from the residual discharging portion of the reactor.
  • EXAMPLE -9 The polyethylene predominant plastic was cleaned, shredded and cut into pieces of the size mm X 1mm, the plastic product was premixed wit 2 wt% catalyst and heated up in the pyrolysis reactor. The temperature range being 320-380°C. The distillate obtained was in the region of 55-65 wt% of the plastic taken. The gas chromatography analysis showed presence of predominantly C 6 - C- olefins in the distillate.
  • EXAMPLE -10 The cracking of high density polyethylene, which was cleaned, shredded and cut into 1 X 1 mm pieces was carried out in a catalytic reactor. The cracking is carried out under atmospheric pressure and at a temperature range of 300-350°C.
  • the catalyst used is an indigenously developed zeolite based acidic catalyst, which is used in the ratio of 4 wt% of the plastic taken.
  • the resulting gaseous hydrocarbons are passed through column of calcium oxide to make it chlorine free gaseous hydrocarbons.
  • the wt% distillate obtained is in the range of 80-90 wt% by weight of the starting material taken.
  • Gas chromatography shows the distillate to be predominantly C 6 -C 9 olefins.
  • EXAMPLE-11 The PNC containing plastic was cleaned and cut into 1 mm X 1mm pieces. These pieces were injected in a pyrolysis reactor and 8 wt% of catalyst was used. The temperature range being in the region of 320-360 °C.
  • the resulting gaseous hydrocarbons are passed through column containing calcium oxide in order to make it chlorine free.
  • the percentage of distillate obtained is in range of 50-70 wt% of the initial weight of plastic taken.
  • the gas chromatography analysis shows the distillate containing predominantly C( professionC 9 ,C] 3 ,C
  • EXAMPLE- 12 The p oly ethylene t erphthalate predominant plastic was c leaned and cut into 1 mm X 1mm pieces. These pieces were injected in a pyrolysis reactor and 4wl% of catalyst was used. The temperature range being in the region of 300- 340 °C.
  • the resulting gaseous hydrocarbons are passed through column containing calcium oxide or it's aqueous solution in order to make it chlorine free.
  • the percentage of distillate obtained is in range of 70-80 wt% of the initial weight o f plastic taken.
  • the gas chromatography analysis shows the distillate containing predominantly C 6 .C 10 and overall range being C 4 -C 25 .
  • EXAMPLE-13 The thermal cracking o f polyamide (nylon) predominant plastic, which was cleaned, shredded and cut into 1 X 1 mm pieces was carried out in a catalytic reactor. The cracking is carried out under atmospheric pressure and at a temperature range of 350-400°C.
  • the catalyst used is an indigenously developed zeolite based acidic catalyst, which is used in the ratio of 8 wt% of the plastic taken.
  • the resulting gaseous hydrocarbons are passed through column o f c alcium oxide to make it chlorine free gaseous hydrocarbons.
  • the wt% distillate obtained is in the range of 70-90 wt% by weight of the starting material taken.
  • Gas chromatography shows the distillate to be predominantly Ci 3 ⁇ C 18 olefins.
  • the residual left over in the catalytic reactor is mixed with equal amount of non -edible vegetable oil and heated to temperature range of 100-120° C and then discharged from the residual discharging portion of the reactor.
  • EXAMPLE- 14 The cracking of assorted municipal plastic, which was cleaned, shredded and cut into 1 X 1 mm pieces, was carried out in a catalytic reactor. The cracking is carried out under atmospheric pressure and at a temperature range of 300-350°C.
  • the catalyst used is an indigenously developed zeolite based acidic catalyst, which is used in the ratio of 2 wt% of the plastic taken.
  • the resulting gaseous hydrocarbons are passed through column of calcium oxide or it's aqueous solution to make it chlorine free gaseous hydrocarbons.
  • the wt% distillate obtained is in the range of 65-70 wt% by weight of the starting material taken.
  • the resulting gaseous hydrocarbons are passed through column of calcium oxide or it's aqueous solution to make it chlorine free gaseous hydrocarbons.
  • the wt% distillate obtained is in the range of 70-80 wt% by weight of the stalling material taken. Gas chromatography shows the distillate to be range- of C -C ⁇ 8 , predominantly C 6 -C 8 olefins.
  • EXAMPLE- 16 An experiment was repeated for the assorted municipal plastic under reaction conditions as for EXAMPLE-15 but without the catalyst. It was found that 30-40 wt% of distillate containing mixture of olefins were obtained and a substantial amount of solid residue was left over.
  • **Plastic mixture generally contains 3-5wt% PVC, 5-15 wt% PET, 20-35 wt% PP, 30-50 wt% PE, 5-10 wt% nylon etc.

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Abstract

L'invention concerne un procédé de préparation d'un catalyseur de craquage catalytique. Ce procédé consiste : à mélanger les ingrédients suivants dans les proportions suivantes : zéolite faujasite 5-35 % en poids ; alumine pseudoboehmite 10-40 % en poids ; silicate de polyammonium 1-10 % en poids ; kaolinton 15-60 % en poids ; à broyer lesdits ingrédients pour obtenir une suspension épaisse au moyen d'eau ; à sécher par atomisation ladite suspension sur des microsphères ; et à calciner lesdites microsphères à 500 °C pendant une heure pour obtenir le catalyseur selon l'invention.
PCT/IN2004/000366 2004-03-30 2004-11-25 Composition catalytique de craquage catalytique de dechets plastiques WO2005094990A1 (fr)

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Cited By (14)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2008007384A1 (fr) * 2006-07-10 2008-01-17 Sarjerao Nivrutti Sutar DÉpolymÉrisation de dÉchets de caoutchoucS et de thermoplastiques, y compris de PVC ou de PET, en carburants hydrocarbonÉs
WO2010139997A3 (fr) * 2009-06-03 2011-03-31 University Of Manchester Zéolites modifiées et leur utilisation dans le recyclage de déchets plastiques
US8895790B2 (en) 2013-02-12 2014-11-25 Saudi Basic Industries Corporation Conversion of plastics to olefin and aromatic products
WO2015012676A1 (fr) 2013-07-25 2015-01-29 Newpek S.A. De C.V. Procédé et équipement pour la production d'hydrocarbures par décomposition catalytique de déchets plastiques en un seul passage
US20160040074A1 (en) * 2013-04-04 2016-02-11 Achim Methling Joesef Ranftl GbR Method for the Degrading of Synthetic Polymers and Device for Carrying Out Said Method
US9428695B2 (en) 2013-02-12 2016-08-30 Saudi Basic Industries Corporation Conversion of plastics to olefin and aromatic products with product recycle
US9447332B2 (en) 2013-02-12 2016-09-20 Saudi Basic Industries Corporation Conversion of plastics to olefin and aromatic products using temperature control
JP2020007424A (ja) * 2018-07-05 2020-01-16 三菱電機株式会社 再生スチレン系樹脂組成物
US10537876B2 (en) 2015-12-18 2020-01-21 Solvay Sa Use of a catalyst composition for the catalytic depolymerization of plastics waste
US10647922B2 (en) 2015-12-18 2020-05-12 Solvay Sa Use of a catalyst composition for the catalytic depolymerization of plastics waste
EP3971264A1 (fr) * 2020-09-21 2022-03-23 Indian Oil Corporation Limited Pyrolyse catalytique du polystyrène en produit liquide riche en aromatiques à l'aide d'un catalyseur sphérique
KR20220062320A (ko) * 2019-09-09 2022-05-16 바셀 폴리올레핀 이탈리아 에스.알.엘 할로이사이트를 이용한 플라스틱 해중합
CN115672391A (zh) * 2021-07-28 2023-02-03 中国石油天然气股份有限公司 一种废塑料裂解催化剂及其制备方法与应用
CN116328820A (zh) * 2021-12-22 2023-06-27 中国石油天然气股份有限公司 一种废塑料裂解多产轻质油催化剂及其制备方法与应用

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Cited By (23)

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WO2008007384A1 (fr) * 2006-07-10 2008-01-17 Sarjerao Nivrutti Sutar DÉpolymÉrisation de dÉchets de caoutchoucS et de thermoplastiques, y compris de PVC ou de PET, en carburants hydrocarbonÉs
WO2010139997A3 (fr) * 2009-06-03 2011-03-31 University Of Manchester Zéolites modifiées et leur utilisation dans le recyclage de déchets plastiques
EP3608019A1 (fr) * 2009-06-03 2020-02-12 University of Manchester Zéolites modifiées et leur utilisation dans le recyclage de déchets plastiques
US9447332B2 (en) 2013-02-12 2016-09-20 Saudi Basic Industries Corporation Conversion of plastics to olefin and aromatic products using temperature control
US8895790B2 (en) 2013-02-12 2014-11-25 Saudi Basic Industries Corporation Conversion of plastics to olefin and aromatic products
US9212318B2 (en) 2013-02-12 2015-12-15 Saudi Basic Industries Corporation Catalyst for the conversion of plastics to olefin and aromatic products
US9428695B2 (en) 2013-02-12 2016-08-30 Saudi Basic Industries Corporation Conversion of plastics to olefin and aromatic products with product recycle
US10494572B2 (en) * 2013-04-04 2019-12-03 Achim Methling Joesef Ranftl GbR Method for the degrading of synthetic polymers and device for carrying out said method
US20160040074A1 (en) * 2013-04-04 2016-02-11 Achim Methling Joesef Ranftl GbR Method for the Degrading of Synthetic Polymers and Device for Carrying Out Said Method
US10240093B2 (en) 2013-07-25 2019-03-26 Newpek S.A. De C.V. Method and equipment for producing hydrocarbons by catalytic decomposition of plastic waste products in a single step
WO2015012676A1 (fr) 2013-07-25 2015-01-29 Newpek S.A. De C.V. Procédé et équipement pour la production d'hydrocarbures par décomposition catalytique de déchets plastiques en un seul passage
US10647922B2 (en) 2015-12-18 2020-05-12 Solvay Sa Use of a catalyst composition for the catalytic depolymerization of plastics waste
US10537876B2 (en) 2015-12-18 2020-01-21 Solvay Sa Use of a catalyst composition for the catalytic depolymerization of plastics waste
JP2020007424A (ja) * 2018-07-05 2020-01-16 三菱電機株式会社 再生スチレン系樹脂組成物
JP7085923B2 (ja) 2018-07-05 2022-06-17 三菱電機株式会社 再生スチレン系樹脂組成物
KR20220062320A (ko) * 2019-09-09 2022-05-16 바셀 폴리올레핀 이탈리아 에스.알.엘 할로이사이트를 이용한 플라스틱 해중합
JP2022542193A (ja) * 2019-09-09 2022-09-29 バーゼル・ポリオレフィン・イタリア・ソチエタ・ア・レスポンサビリタ・リミタータ ハロイサイトを用いるプラスチック解重合
KR102650762B1 (ko) * 2019-09-09 2024-03-22 바셀 폴리올레핀 이탈리아 에스.알.엘 할로이사이트를 이용한 플라스틱 해중합
EP3971264A1 (fr) * 2020-09-21 2022-03-23 Indian Oil Corporation Limited Pyrolyse catalytique du polystyrène en produit liquide riche en aromatiques à l'aide d'un catalyseur sphérique
US11613623B2 (en) 2020-09-21 2023-03-28 Indian Oil Corporation Limited Catalytic pyrolysis of polystyrene into aromatic rich liquid product using spherical catalyst
CN115672391A (zh) * 2021-07-28 2023-02-03 中国石油天然气股份有限公司 一种废塑料裂解催化剂及其制备方法与应用
CN115672391B (zh) * 2021-07-28 2024-02-02 中国石油天然气股份有限公司 一种废塑料裂解催化剂及其制备方法与应用
CN116328820A (zh) * 2021-12-22 2023-06-27 中国石油天然气股份有限公司 一种废塑料裂解多产轻质油催化剂及其制备方法与应用

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