WO2013175014A1 - Methanol conversion process - Google Patents
Methanol conversion process Download PDFInfo
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- WO2013175014A1 WO2013175014A1 PCT/EP2013/060812 EP2013060812W WO2013175014A1 WO 2013175014 A1 WO2013175014 A1 WO 2013175014A1 EP 2013060812 W EP2013060812 W EP 2013060812W WO 2013175014 A1 WO2013175014 A1 WO 2013175014A1
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- methanol
- sio
- sda
- crystalline material
- microporous crystalline
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- YGDZKYYCJUNORF-UHFFFAOYSA-N CCCN(CC1)CCC1=O Chemical compound CCCN(CC1)CCC1=O YGDZKYYCJUNORF-UHFFFAOYSA-N 0.000 description 1
Classifications
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C1/00—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon
- C07C1/20—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon starting from organic compounds containing only oxygen atoms as heteroatoms
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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
- 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
- B01J29/70—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of types characterised by their specific structure not provided for in groups B01J29/08 - B01J29/65
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B39/00—Compounds having molecular sieve and base-exchange properties, e.g. crystalline zeolites; Their preparation; After-treatment, e.g. ion-exchange or dealumination
- C01B39/02—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof; Direct preparation thereof; Preparation thereof starting from a reaction mixture containing a crystalline zeolite of another type, or from preformed reactants; After-treatment thereof
- C01B39/46—Other types characterised by their X-ray diffraction pattern and their defined composition
- C01B39/48—Other types characterised by their X-ray diffraction pattern and their defined composition using at least one organic template directing agent
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C11/00—Aliphatic unsaturated hydrocarbons
- C07C11/02—Alkenes
-
- 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
- C10G3/00—Production of liquid hydrocarbon mixtures from oxygen-containing organic materials, e.g. fatty oils, fatty acids
- C10G3/42—Catalytic treatment
- C10G3/44—Catalytic treatment characterised by the catalyst used
- C10G3/45—Catalytic treatment characterised by the catalyst used containing iron group metals or compounds thereof
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- 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
- C10G3/00—Production of liquid hydrocarbon mixtures from oxygen-containing organic materials, e.g. fatty oils, fatty acids
- C10G3/42—Catalytic treatment
- C10G3/44—Catalytic treatment characterised by the catalyst used
- C10G3/48—Catalytic treatment characterised by the catalyst used further characterised by the catalyst support
- C10G3/49—Catalytic treatment characterised by the catalyst used further characterised by the catalyst support containing crystalline aluminosilicates, 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
- C10G50/00—Production of liquid hydrocarbon mixtures from lower carbon number hydrocarbons, e.g. by oligomerisation
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L1/00—Liquid carbonaceous fuels
- C10L1/04—Liquid carbonaceous fuels essentially based on blends of hydrocarbons
- C10L1/06—Liquid carbonaceous fuels essentially based on blends of hydrocarbons for spark ignition
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- 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
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/70—Catalyst aspects
-
- 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
- C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
- C10G2400/02—Gasoline
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- 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
- C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
- C10G2400/08—Jet fuel
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L2270/00—Specifically adapted fuels
- C10L2270/02—Specifically adapted fuels for internal combustion engines
- C10L2270/023—Specifically adapted fuels for internal combustion engines for gasoline engines
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- 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
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/50—Improvements relating to the production of bulk chemicals
- Y02P20/52—Improvements relating to the production of bulk chemicals using catalysts, e.g. selective catalysts
-
- 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
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P30/00—Technologies relating to oil refining and petrochemical industry
- Y02P30/20—Technologies relating to oil refining and petrochemical industry using bio-feedstock
Definitions
- This invention relates to a process for the conversion of methanol to hydrocarbons over a zeolite catalyst.
- hydrocarbons are known and have become of great interest in recent times because they offer an attractive way of producing liquid hydrocarbon fuels, especially gasoline, from sources which are not of liquid petroliferous origin. In particular, they provide a way by which methanol can be converted to gasoline boiling range products in good yields.
- the methanol may be readily obtained from coal by gasification to synthesis gas and conversion of the synthesis gas to methanol by well-established industrial processes. As an alternative, the methanol may be obtained from natural gas by other conventional processes.
- This process is the well known methanol to gasoline process as developed and operated my ExxonMobil as the ExxonMobil MTG process. This technology is extensively discussed and described in the review "Methanol-to- hydrocarbons: process technology", Author: Frerich J. Keil, in Microporous and Mesoporous Materials, Volume 29, Issues 1-2, June 1999, Pages 49-66.
- the conversion of methanol to hydrocarbon products may take place in a fluidized bed process as described, for example, in U.S. Pat. Nos. 4,071 ,573 and 4,138,440, or in a fixed bed as described in U.S. Pat. Nos. 3,998,899, 3,931 ,349 and 4,035,430.
- the methanol is usually first subjected to a dehydrating step, using a catalyst such as gamma-alumina, to form an equilibrium mixture of methanol, dimethyl ether (DME) and water. This mixture is then passed over a catalyst such as zeolite ZSM-5 which brings about the conversion to the hydrocarbon products which are mainly in the range of light gas to gasoline.
- the water may be removed from the methanol dehydration products prior to conversion to hydrocarbons as may the methanol which can be recycled to the dehydration step, as described in U.S. Pat. No. 4,035,430. Removal of the water is desirable because the catalyst may tend to become deactivated by the presence of the water vapor at the reaction temperatures employed, but this step is by no means essential. [0005] In the operation of the fixed bed process, a major problem which has to be dealt with is the thermal balance. The conversion of the oxygenated feed stream (methanol, DME) to the hydrocarbons is a strongly exothermic reaction liberating approximately 1480 kJ. (1400 Btu) of heat per kilogram of methanol.
- a degree of control over the temperature of the catalyst bed can be achieved by suitable choice of bed configuration but this expedient is generally insufficient by itself and other methods must be employed.
- One particularly useful method is to employ a light gas portion of the hydrocarbon product as recycle, as described in U.S. Pat. No. 3,931 ,349.
- An alternative proposal is set out in U.S. Pat. No. 4,035,430.
- the process described in this patent employs a number of sequential catalyst beds and recycle gas may be injected between the successive beds to control the exotherm.
- the currently preferred catalyst for the MTG process is ZSM-5, which is an aluminosilicate zeolite mineral of MFI structure type belonging to the pentasil family of zeolites.
- Ci 7 range in the presence of a zeolite microporous crystalline material ITQ-39.
- the present invention in one aspect provides a process for the conversion of methanol to hydrocarbons within the C 5 to Ci 7 range, which process comprises contact of a feed comprising methanol with a zeolite microporous crystalline material ITQ-39 and recovery of hydrocarbons within the C 5 to Ci 7 range from the conversion product.
- the process of the present invention may be operated under typical
- the catalyst used in the process of the present invention is a zeolite microporous crystalline material ITQ-39, comprising, in the heated state and in the absence of defects in its crystalline framework manifested by the presence of silanols, the empirical formula:
- M is selected from H + , an inorganic cation of charge +n, and mixtures thereof
- X is at least one chemical element having an oxidation state of +3
- Y is at least one second chemical element other than Si having an oxidation state +4
- x has a value between 0 and about 0.3
- y has a value between 0 and about 0.1
- the synthesized material has an X-ray diffraction pattern having at least values of angle 26(degrees) and relative intensities (l/l 0 ) shown in Table 1 .
- Processes for synthesising the microporous crystalline material comprising the steps of: forming a reaction mixture comprising: a source of Si02, a source of one or more tetravalent elements Y selected from the group consisting of Ge, Ti, Sn, V and mixtures thereof, a source of one or more trivalent elements X selected from the group consisting of Al, B, Ga, Fe, Cr and mixtures thereof, a source of inorganic cations M having a charge +n, a source of an organic dication SDA-1 having the structure of Formula 1
- a source of fluoride ions and water heating the reaction mixture to a temperature of between about 80 Q C and about 200 Q C until crystallisation is achieved; and forming the microporous crystalline material, wherein the material has a composition in the ranges:
- the microporous crystalline materials produced can be palletized in accordance with known techniques and used as a catalyst or catalyser component in processes of transformation of organic compounds or as an absorbent in a processes of absorption and separation of organic compounds.
- the material used in the above applications can be in its acid form and/or exchanged with suitable cations.
- FIG. 1 illustrates the organic dication, in the presence of which the zeolite ITQ-39 is synthesised.
- FIG. 2 illustrates characteristic peaks of the X-ray diffraction pattern of the ITQ-39 material, as synthesised according to example 5.
- FIG. 3 illustrates characteristic peaks of the X-ray diffraction pattern of the material of example 5 after heating.
- zeolite ITQ-39 microporous crystalline zeolite
- This material both in heated and synthesised forms without heating, have an X-ray diffraction patterns that are different from other known zeolite materials, and therefore, characteristic of this material.
- zeolite ITQ-39 microporous crystalline zeolite
- One example embodiment described herein is a zeolite microporous crystalline material that has, in the heated state and in the absence of defects in its crystalline framework manifested by the presence of silanols, the empirical formula:
- x(M 1/n X0 2 ):yYQ 2 :Si0 2 [0028] wherein M is selected from H + , an inorganic cation of charge +n, and mixtures thereof, X is at least one chemical element having an oxidation state of +3, Y is at least one second chemical element other than Si having an oxidation state +4, x has a value between 0 and about 0.3, y has a value between 0 and about 0.1 , and wherein the synthesized material has an X-ray diffraction pattern with at least the values of angle 2 ⁇ (degrees) and relative intensities (l/l 0 ) shown in Table I, l 0 being the intensity of the most intense peak to which a value of 100 is assigned:
- d has a weak intensity between 0 and 20%
- m has a medium intensity between 20 and 40%
- f has a strong intensity between 40 and 60%
- mf has a very strong intensity between 60 and 100%
- h has a peak of diffraction appearing as a shoulder.
- the constituents of the microporous crystalline material can be as follows.
- Element X is selected from the group consisting of Al, Ga, B, Fe, Cr and mixtures thereof.
- Element Y is selected from the group consisting of Ge, Ti, Sn, V and mixtures thereof. In the empirical formula above, x has a value of less than about 0.3 and y has a value of less than about 0.05.
- the zeolite microporous crystalline material has, in the heated state and in the absence of defects in its crystalline framework manifested by the presence of silanols, the empirical formula: x(M 1/n X0 2 ): y Y0 2 :Si0 2
- M is selected from H + , an inorganic cation of charge +n, and mixtures thereof
- X is at least one chemical element having an oxidation state of +3, selected from the group consisting of Al, Ga, B, Fe, Cr and mixtures thereof
- Y is at least one second chemical element other than Si having an oxidation state of +4, selected from the group consisting of Ge, Ti, Sn, V and mixtures thereof
- x has a value between 0 and about 0.3
- y has a value between 0 and about 0.05
- the synthesized material has an X-ray diffraction pattern with at least the values of angle 2 ⁇ (degrees) and relative intensities previously mentioned (Table I) and this material has in the heated state an X-ray diffraction pattern with at least the values of angle 2 ⁇ (degrees) and relative intensities (l/l 0 ) previously mentioned (Table II).
- the X-ray diffraction patterns of the microporous crystalline material, ITQ-39 were obtained by the powder method using a fixed divergence slit of 1/4° and using the Ka radiation of Cu. It should be taken into account that the diffraction data listed for this sample of zeolite ITQ-39 as simple or unique lines can be formed by multiple overlaps or superpositions of reflections that, under certain conditions such as differences in crystallographic changes, can appear as resolved or partially resolved lines. Generally, crystallographic changes can include small variations in the unit cell parameters and/or changes in the crystal symmetry without these producing a change in structure. Thus, the positions, widths and relative intensities of the peaks depend to a certain extent on the chemical composition of the material and on the degree of hydration and crystal size.
- Zeolite ITQ-39 presents an X-ray diffraction pattern as illustrated in FIG.
- This diffraction pattern is characterised by the values of angle 2 ⁇ (degrees) and relative intensities (l/l 0 ) shown in Table III.
- FIG. 3 This diffraction pattern is characterised by the values of angle 2 ⁇ (degrees)and relative intensities (l/l 0 ) that are shown in Table IV. Comparing the X-ray diffraction patterns of zeolite ITQ-39 as synthesised and after heating to various temperatures shows the great thermal stability of the material.
- the process for synthesising the microporous crystalline material comprises the steps of: forming a reaction mixture comprising one or more sources of Si0 2 , one or more sources of the organic cation SDA-1 , one or more sources of fluoride ions, and water; heating the reaction mixture to a temperature of between about 80 °C. and about 200 ' ⁇ . until crystallisation is achieved; and forming the microporous crystalline material.
- the reaction mixture has a composition, in terms of molar ratios, in the ranges:
- the reaction mixture additionally comprises a source of one or more trivalent elements X and has a composition, in terms of molar ratios, in the ranges:
- the reaction mixture additionally comprises a source of one or more other tetravalent elements Y other than Si and has a composition, in terms of molar ratios, in the ranges:
- the reaction mixture additionally comprises a source of one or more other tetravalent elements Y other than Si and source of one or more trivalent elements X, and has a composition, in terms of molar ratios, in the ranges:
- the reaction mixture comprises a source of Si0 2 , a source of one or more other tetravalent elements Y other than Si selected from the group consisting of Ge, Ti, V, Sn and mixtures thereof, a source of one or more trivalent elements X selected from the group consisting of Al, B, Ga, Fe, Cr and mixtures thereof, a source of inorganic cations M having a charge +n, selected from the alkaline metals, alkaline earths and mixtures thereof, a source of organic cation SDA-1 , a source of fluoride ions and water.
- the reaction mixture has a composition, in terms of molar ratios, in the ranges:
- the mixture can be heated with or without stirring to a temperature of between 80 °C. and 200 ' ⁇ . until crystallisation is achieved.
- composition of the reaction mixture producing the microporous crystalline material can be generally represented by the following formula, with the values of parameters indicating the molar ratios:
- M is one or more inorganic cations of charge +n, preferably alkaline metals or alkaline earths
- X is one or more trivalent elements, preferably Al, B, Ga, Fe, Cr or mixtures thereof
- Y is one or more tetravalent elements other than Si, preferably Ge, Ti, Sn, V or mixtures thereof
- SDA-1 is the dication
- F is one or more sources of fluoride ions, preferably HF, NH 4 F or mixtures thereof and the values of r, s, t, u, v and w are in the ranges:
- the components of the synthesis mixture can originate from different sources and the times and conditions of crystallisation may be affected by the same.
- the thermal treatment of the mixture is carried out at a temperature of between about 130 °C. and about 200 °C.
- the thermal treatment of the reaction mixture can be performed either statically or with stirring of the mixture.
- the solid product is separated by filtration or
- the source of Si0 2 can be, for example, tetraethyl orthosilicate, colloidal silica, amorphous silica or a mixture of these.
- the fluoride anion is used as a mobilising agent for the precursor species.
- the source of fluoride ions is preferably HF, NH4F or mixtures thereof.
- the organic cation or dication SDA-1 is added to the reaction mixture preferably in the form of a salt, for example, a halide, or in the form of a hydroxide and, additionally, a source of alkaline metal, alkaline earth ions or a mixture of both (M) can be added in the form of a hydroxide or a salt.
- a salt for example, a halide, or in the form of a hydroxide and, additionally, a source of alkaline metal, alkaline earth ions or a mixture of both (M) can be added in the form of a hydroxide or a salt.
- M alkaline metal, alkaline earth ions or a mixture of both
- some crystalline ITQ-39 material is added to the reaction mixture as crystallisation promoter in a quantity in the range of about 0.01 % to about 20% by weight, preferably between about 0.05% and about 10% by weight with respect to the total added inorganic oxides.
- the materials produced herein can be pelletised in accordance with known techniques and used as catalysts or catalyser components in the transformation of organic compounds.
- the materials can also be used as absorbents in the absorption and separation of organic compounds.
- the ITQ-39 material can be in its acid form and/or exchanged with suitable cations.
- methanol may be converted into a hydrocarbon product preferably containing a kerosene fraction in a procedure similar to that used in the Mobil methanol to gasoline process.
- kerosene is the desried product it is preferred that the process is as follows.
- the crude methanol is initially preheated, vapourised and then superheated to between 300-320 ° C in a series of heat exchangers.
- the vapour is then sent to the dimethyl ether (DME) reactor containing a dehydration catalyst such as r-alumina where approximately 75% of the methanol is partially dehydrated to an equilibrium mixture of DME, water and methanol.
- DME dimethyl ether
- the reaction is rapid, reversible and exothermic.
- the resulting mixture at a temperature greater than 320 ⁇ and preferably between 320 and 420 °C is passed into the methanol converter.
- This reaction is very exothermic and the process gas can be mixed with some recycle gas and then passed to the conversion reactors to absorb some of the heat of reaction.
- DME and/or methanol is further dehydrated to give the final product containing a kerosene fraction, by a mechanism which may involve the initial formation of light alkenes which can then oligomerize and cyclise with the evolution of further heat.
- the heat thus recovered can be used elsewhere in the process, for example, pre heating process gas streams or for distillation of the final product.
- the reactor effluent is cooled and the heat can be recovered, by generating medium pressure steam for use elsewhere in the process. Conversion of methanol is very high and can reach almost 100%.
- the condensate comprises liquid
- hydrocarbons generally in the range C 5 to Ci 7 and water
- the non condensable fraction used for recycle generally contains low molecular weight hydrocarbons, principally methane, carbon dioxide and hydrogen.
- Kerosene is recovered from the liquid product by separation from the aqueous component, and distillation.
- the quarternisation of the diamine is performed as follows: 100 g of propyl idodide are added on a solution of 43.5 g of diamine in 70 ml_ of MeOH. The mixture is maintained with continuous stirring at ambient temperature for 7 days, after which a white precipitate is formed. The solid is vacuum filtered. The characterisation of this solid by elemental analysis and nuclear magnetic resonance of H and of 3 C confirms that it is the diiodide of the cation [SDA-1 ] 2+ illustrated in FIG. 1 .
- the iodide of the cation is exchanged for a hydroxide using an ion exchange resin in accordance with the following process: 44 mmol of the iodide of the cation ([SDA-1 ]I 2 ) are dissolved in water. 89 g of Dowex SBR resin are added to the solution obtained and this is maintained with stirring until the next day. Then, the mixture is filtered, washed with distilled water and a solution of the dihydroxide ([SDA- 1 ](OH) 2 ) is obtained. This is evaluated with aqueous HCI using phenolphaline as an indicator, obtaining an exchange efficiency higher than 90%. The final solution contains 0.62 equivalents of hydroxide per 1000 g of solution. [0066] Example 2 - Synthesis of ITQ-39
- the gel is heated statically for 7 days in a steel autoclave with an internal Teflon cover at 150 °C.
- the solid obtained after filtration, washing with distilled water and drying at 100 ⁇ €. is ITQ-39.
- Teflon cover at 135[deg.] C. The solid obtained after filtration, washing with distilled water and drying at 100[deg.] C. is ITQ-39.
- the gel is statically heated for 14 days in steel autoclave with an internal
- the solid obtained after filtration, washing with distilled water and drying at 100 ⁇ €. is ITQ-39.
- D. 1 .21 g of Al isopropoxide are added over 15.94 g of tetraethyl orthosilicate (TEOS).
- TEOS tetraethyl orthosilicate
- 58.55 g of a solution of [SDA-1 ](OH) 2 from Example 1 is added.
- the mixture is allowed to evaporate while stirring until complete elimination of the ethanol from the hydrolysis of the TEOS plus the quantity of water required in reaching the final composition indicated.
- 1 .58 g of a solution of hydrofluoric acid (48% HF by weight) is added.
- the composition of the gel is:
- the gel is statically heated for 1 1 days in steel autoclave with an internal
- the solid obtained after filtering, washing with distilled water and drying at ⁇ ⁇ ' ⁇ . is ITQ-39 and its X-ray diffraction pattern is shown in FIG. 2.
- the solid after heating in air at 580 ' ⁇ . for six hours maintains the zeolite structure, as can be deduced from the X-ray diffraction pattern shown in FIG. 3.
Abstract
Description
Claims
Priority Applications (5)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
GB1422904.1A GB2519005A (en) | 2012-05-24 | 2013-05-24 | Methanol conversion process |
EP13730814.4A EP2855403A1 (en) | 2012-05-24 | 2013-05-24 | Methanol conversion process |
CA2913061A CA2913061A1 (en) | 2012-05-24 | 2013-05-24 | Methanol conversion process |
US14/403,302 US20150275099A1 (en) | 2012-05-24 | 2013-05-24 | Methanol conversion process |
IN10935DEN2014 IN2014DN10935A (en) | 2012-05-24 | 2014-12-20 |
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
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GBGB1209162.5A GB201209162D0 (en) | 2012-05-24 | 2012-05-24 | Methanol conversion process |
GB1209162.5 | 2012-05-24 |
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WO2013175014A1 true WO2013175014A1 (en) | 2013-11-28 |
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PCT/EP2013/060812 WO2013175014A1 (en) | 2012-05-24 | 2013-05-24 | Methanol conversion process |
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US (1) | US20150275099A1 (en) |
EP (1) | EP2855403A1 (en) |
CA (1) | CA2913061A1 (en) |
GB (2) | GB201209162D0 (en) |
IN (1) | IN2014DN10935A (en) |
WO (1) | WO2013175014A1 (en) |
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US9725328B1 (en) * | 2016-05-20 | 2017-08-08 | Chevron U.S.A. Inc. | Molecular sieve SSZ-104, its synthesis and use |
AU2017383560B2 (en) | 2016-12-23 | 2023-05-25 | Carbon Engineering Ltd. | Method and system for synthesizing fuel from dilute carbon dioxide source |
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US3931349A (en) | 1974-09-23 | 1976-01-06 | Mobil Oil Corporation | Conversion of methanol to gasoline components |
US3998899A (en) | 1975-08-06 | 1976-12-21 | Mobil Oil Corporation | Method for producing gasoline from methanol |
US4035430A (en) | 1976-07-26 | 1977-07-12 | Mobil Oil Corporation | Conversion of methanol to gasoline product |
US4071573A (en) | 1974-09-23 | 1978-01-31 | Mobil Oil Corporation | Prolonging zeolite catalyst life in methanol conversion to gasoline by disposing of exothermic reaction heat |
US4138440A (en) | 1974-08-14 | 1979-02-06 | Mobil Oil Corporation | Conversion of liquid alcohols and ethers with a fluid mass of ZSM-5 type catalyst |
EP2119669A1 (en) * | 2007-02-01 | 2009-11-18 | Consejo Superior De Investigaciones Científicases | Microporous crystalline material of zeolitic nature, zeolite itq-39, method of preparation and uses |
Family Cites Families (1)
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US4992611A (en) * | 1989-12-13 | 1991-02-12 | Mobil Oil Corp. | Direct conversion of C1 -C4 oxygenates to low aromatic distillate range hydrocarbons |
-
2012
- 2012-05-24 GB GBGB1209162.5A patent/GB201209162D0/en not_active Ceased
-
2013
- 2013-05-24 GB GB1422904.1A patent/GB2519005A/en not_active Withdrawn
- 2013-05-24 CA CA2913061A patent/CA2913061A1/en not_active Abandoned
- 2013-05-24 US US14/403,302 patent/US20150275099A1/en not_active Abandoned
- 2013-05-24 WO PCT/EP2013/060812 patent/WO2013175014A1/en active Application Filing
- 2013-05-24 EP EP13730814.4A patent/EP2855403A1/en not_active Withdrawn
-
2014
- 2014-12-20 IN IN10935DEN2014 patent/IN2014DN10935A/en unknown
Patent Citations (6)
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US4138440A (en) | 1974-08-14 | 1979-02-06 | Mobil Oil Corporation | Conversion of liquid alcohols and ethers with a fluid mass of ZSM-5 type catalyst |
US3931349A (en) | 1974-09-23 | 1976-01-06 | Mobil Oil Corporation | Conversion of methanol to gasoline components |
US4071573A (en) | 1974-09-23 | 1978-01-31 | Mobil Oil Corporation | Prolonging zeolite catalyst life in methanol conversion to gasoline by disposing of exothermic reaction heat |
US3998899A (en) | 1975-08-06 | 1976-12-21 | Mobil Oil Corporation | Method for producing gasoline from methanol |
US4035430A (en) | 1976-07-26 | 1977-07-12 | Mobil Oil Corporation | Conversion of methanol to gasoline product |
EP2119669A1 (en) * | 2007-02-01 | 2009-11-18 | Consejo Superior De Investigaciones Científicases | Microporous crystalline material of zeolitic nature, zeolite itq-39, method of preparation and uses |
Non-Patent Citations (4)
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D.H. OLSON, ET AL.: "CHEMICAL AND PHYSICAL PROPERTIES OF THE ZSM-5 SUBSTITUTIONAL SERIES", JOURNAL OF CATALYSIS, vol. 61, no. 2, February 1980 (1980-02-01), Academic Press, Duluth, MN, US, pages 390 - 396, XP000856253, ISSN: 0021-9517, DOI: 10.1016/0021-9517(80)90386-3 * |
FRERICH J. KEIL: "Methanol-to hydrocarbons : process technology", MICROPOROUS AND MESOPOROUS MATERIALS, vol. 29, no. 1-2, June 1999 (1999-06-01), pages 49 - 66 |
FRERICH J. KEIL: "Methanol-to- hydrocarbons: process technology", MICROPOROUS AND MESOPOROUS MATERIALS, vol. 29, no. 1-2, June 1999 (1999-06-01), pages 49 - 66 |
M. STOCKER: "Methanol-to-hydrocarbons: catalytic materials and their behaviour", MICROPOROUS AND MESOPOROUS MATERIALS, vol. 29, no. 1-2, June 1999 (1999-06-01), Elsevier Science, Amsterdam, NL, pages 3 - 48, XP004167548, ISSN: 1387-1811, DOI: 10.1016/S1387-1811(98)00319-9 * |
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GB2519005A (en) | 2015-04-08 |
CA2913061A1 (en) | 2013-11-28 |
GB201209162D0 (en) | 2012-07-04 |
US20150275099A1 (en) | 2015-10-01 |
EP2855403A1 (en) | 2015-04-08 |
IN2014DN10935A (en) | 2015-09-18 |
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