WO2015184600A1 - 一种高选择性制备对二甲苯联产丙烯的方法 - Google Patents
一种高选择性制备对二甲苯联产丙烯的方法 Download PDFInfo
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- WO2015184600A1 WO2015184600A1 PCT/CN2014/079144 CN2014079144W WO2015184600A1 WO 2015184600 A1 WO2015184600 A1 WO 2015184600A1 CN 2014079144 W CN2014079144 W CN 2014079144W WO 2015184600 A1 WO2015184600 A1 WO 2015184600A1
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- reaction zone
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- methanol
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Classifications
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- C—CHEMISTRY; METALLURGY
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- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C2/00—Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms
- C07C2/86—Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms by condensation between a hydrocarbon and a non-hydrocarbon
- C07C2/862—Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms by condensation between a hydrocarbon and a non-hydrocarbon the non-hydrocarbon contains only oxygen as hetero-atoms
- C07C2/864—Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms by condensation between a hydrocarbon and a non-hydrocarbon the non-hydrocarbon contains only oxygen as hetero-atoms the non-hydrocarbon is an alcohol
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- 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
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- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
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- B—PERFORMING OPERATIONS; TRANSPORTING
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- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C11/00—Aliphatic unsaturated hydrocarbons
- C07C11/02—Alkenes
- C07C11/06—Propene
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C15/00—Cyclic hydrocarbons containing only six-membered aromatic rings as cyclic parts
- C07C15/02—Monocyclic hydrocarbons
- C07C15/067—C8H10 hydrocarbons
- C07C15/08—Xylenes
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C2/00—Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms
- C07C2/86—Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms by condensation between a hydrocarbon and a non-hydrocarbon
- C07C2/862—Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms by condensation between a hydrocarbon and a non-hydrocarbon the non-hydrocarbon contains only oxygen as hetero-atoms
- C07C2/865—Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms by condensation between a hydrocarbon and a non-hydrocarbon the non-hydrocarbon contains only oxygen as hetero-atoms the non-hydrocarbon is an ether
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C2/00—Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms
- C07C2/86—Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms by condensation between a hydrocarbon and a non-hydrocarbon
- C07C2/88—Growth and elimination reactions
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07F—ACYCLIC, CARBOCYCLIC OR HETEROCYCLIC COMPOUNDS CONTAINING ELEMENTS OTHER THAN CARBON, HYDROGEN, HALOGEN, OXYGEN, NITROGEN, SULFUR, SELENIUM OR TELLURIUM
- C07F7/00—Compounds containing elements of Groups 4 or 14 of the Periodic Table
- C07F7/02—Silicon compounds
- C07F7/025—Silicon compounds without C-silicon linkages
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- B01J2229/30—After treatment, characterised by the means used
- B01J2229/32—Reaction with silicon compounds, e.g. TEOS, siliconfluoride
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- B01J29/00—Catalysts comprising molecular sieves
- B01J29/90—Regeneration or reactivation
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- B01J38/00—Regeneration or reactivation of catalysts, in general
- B01J38/04—Gas or vapour treating; Treating by using liquids vaporisable upon contacting spent catalyst
- B01J38/12—Treating with free oxygen-containing gas
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C2529/00—Catalysts comprising molecular sieves
- C07C2529/04—Catalysts comprising molecular sieves having base-exchange properties, e.g. crystalline zeolites, pillared clays
- C07C2529/06—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof
- C07C2529/40—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of the pentasil type, e.g. types ZSM-5, ZSM-8 or ZSM-11
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C2529/00—Catalysts comprising molecular sieves
- C07C2529/04—Catalysts comprising molecular sieves having base-exchange properties, e.g. crystalline zeolites, pillared clays
- C07C2529/06—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof
- C07C2529/80—Mixtures of different zeolites
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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
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/50—Improvements relating to the production of bulk chemicals
- Y02P20/582—Recycling of unreacted starting or intermediate materials
-
- 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
- Y02P20/584—Recycling of catalysts
Definitions
- the invention relates to a method for co-producing propylene by using p-toluene with high selectivity of toluene and methanol and/or dimethyl ether, and belongs to the field of chemistry and chemical engineering. Background technique
- Para-xylene (referred to as PX) and propylene are important basic chemical raw materials.
- p-xylene is mainly obtained by an aromatics unit.
- the naphtha is firstly reformed to produce an aromatic-containing reforming oil, which is then subjected to aromatics extraction, aromatic fractionation, disproportionation and sulfhydryl transfer, and xylene isomerization. Units such as chemistry and adsorption separation maximize the availability of PX products. Since the content of p-xylene in the three isomers is thermodynamically controlled, p-xylene only accounts for about 23% of the ⁇ 8 mixed aromatics, so the material recycling process is large during the entire PX production process, the equipment is large, and the operation cost is high.
- the three isomers of xylene have a small difference in boiling point, and high-purity p-xylene cannot be obtained by the usual distillation technique, and an expensive adsorption separation process must be employed.
- Propylene is mainly produced from petroleum refineries and naphtha steam cracking to produce ethylene as a by-product, or from the production of propane as a raw material.
- Para-xylene is mainly used in the production of polyester.
- Propylene is mainly used in the preparation of polypropylene, acrylonitrile and 1,3-propanediol required for the production of polyester.
- USP 3,965,207 discloses the use of ZSM-5 molecular sieves as catalyst toluene methylation reaction with a maximum selectivity to para-xylene of about 90% at a reaction temperature of 600 ° C; USP 3,965,208 uses a VA element modified ZSM-5 molecular sieve as a catalyst, The formation of meta-xylene is inhibited, mainly producing para-xylene and ortho-xylene.
- the highest selectivity for p-xylene at a reaction temperature of 600 ° C is about 90%; USP 4,250,345 is a ZSM-modified with phosphorus and magnesium. 5 molecular sieves as catalysts, the optimal selectivity of p-xylene at a reaction temperature of 450 ° C reached 98%; USP 4,670,616 using borosilicate molecular sieves and silica or alumina to prepare a catalyst, p-xylene selectivity of 50 -60%; USP 4,276,438, 4,278,827 uses a special structure of molecular sieves 0 2 / ⁇ 1 2 0 3 ⁇ 12) and is modified with copper, silver, gold or antimony, tin, lead, etc.
- USP 4,444,989 uses crystalline pure silica molecular sieves to modify arsenic, phosphorus, magnesium, boron and cerium compounds to improve para-xylene selectivity; USP 4,491,678
- the use of crystalline borosilicates with lanthanum and cerium elements and silicon and phosphorus as common components can greatly increase the selectivity of para-xylene and increase the life of the catalyst.
- USP 5,034,362 ZSM-5 and ZSM-11 using Si0 2 /Al 2 0 3 ⁇ 12 as catalysts and calcination above 650 ° C can improve the selectivity to dimercaptobenzene.
- USP 5,563,310 The use of acidic molecular sieves containing IVB elements and modification of the catalyst with VIB metal can increase the selectivity of p-diphenylbenzene for the alkylation of toluene methanol; USP 6,504,072 uses a mesoporous molecular sieve, preferably ZSM-5, and is high. Treatment with water vapor at 950 ° C, and then modified with phosphorus oxide, proposed the effect of the diffusion effect of the catalyst micropores on the selectivity of p-xylene; USP 6,613,708 modification of the catalyst using organometallic compounds can greatly Improve the selectivity to dimercaptobenzene.
- CN102464549 A discloses a process for the production of propylene and para-xylene which is a process for the reversalization of ethylene and a carbon tetrahydrocarbon to produce propylene, which does not involve the process of ethylene and methanol/dimethyl ether thiolation to propylene.
- CN102464550 A discloses a method for co-production of lower olefins and para-xylene, which comprises introducing carbon tetracarbons and carbon five hydrocarbons into a first reaction zone to produce olefins, which is a C 4 or liquefied gas cracking olefins process, wherein Nor does it involve the process of propylene formation from ethylene and methanol/dimethyl ether.
- the present invention provides a method for the high selectivity of co-production of para-xylene to produce propylene, including The following steps:
- the catalyst-modified zeolite molecular sieve catalyst is obtained by hydrothermal treatment of ZSM-5 and/or ZSM-11 zeolite molecular sieves and surface modification of a siloxane-based compound. More preferably, in the modified zeolite molecular sieve catalyst, the amount of Si supported by the siloxane-based compound is 1 - 10% by weight based on the total weight of the modified zeolite molecular sieve catalyst.
- the reaction system includes a first reaction zone and a second reaction zone, and the method comprises the following steps:
- the raw material containing toluene and methanol and/or dimethyl ether is first contacted with the catalyst I through the first reaction zone, and then enters the second reaction zone to contact with the catalyst II; the second reaction zone is rich in ethylene.
- the c 2 -component is returned to the second reaction zone, and methanol and/or dimethyl ether in the second reaction zone is continuously reacted on the catalyst II to produce propylene;
- the reaction system comprises a first reaction zone and a second reaction zone
- the process comprises the steps of: a) passing the feedstock containing toluene with methanol and/or dimethyl ether first through the first
- the reaction zone is contacted with the catalyst I to obtain the product A, and then reacted with the catalyst II through the second reaction zone to obtain the product B; the ethylene-rich C component in the product A and the product B enters the second reaction.
- a zone reacting with methanol and/or dimethyl ether in the second reaction zone on the catalyst II to produce propylene;
- the C 3 component in the product A and the product B is further separated to obtain a product propylene.
- the catalyst I and the catalyst II are the same or different modified zeolite molecular sieve catalysts.
- the modified zeolite molecular sieve catalyst is obtained by hydrothermal treatment of a ZSM-5 and/or ZSM-11 zeolite molecular sieve and modification of a siloxane-based compound.
- the amount of Si supported by the siloxane-based compound is l-10wt of the total weight of the modified zeolite molecular sieve catalyst.
- the hydrothermal treatment conditions are carried out at 500 to 700 ° C for 3 to 6 hours under a saturated steam atmosphere.
- the structural formula of the siloxane-based compound used for the modification of the siloxane-based compound is as follows:
- R 2 , R 3 and R 4 are each independently a CWQ fluorenyl group.
- the siloxane based compound is ethyl orthosilicate.
- the reaction zone comprises one reactor or a plurality of reactors connected by series and/or parallel; and preferably, the reactor is selected from the group consisting of a fixed bed, a fluidized bed and a moving bed One or more of the reactors.
- the first reaction zone and the second reaction zone are in the same reactor; and preferably, the reactor is selected from the group consisting of a fixed bed, a fluidized bed, and a moving bed reactor. One or more.
- the first reaction zone comprises one reactor or a plurality of reactors connected by series and/or parallel;
- the second reaction zone comprises one reactor or a plurality of reactors and/or a reactor connected in parallel;
- the first reaction zone and the second reaction zone are connected by series or parallel; and
- the reactor is selected from a fixed bed, a fluidized bed, and a moving bed reaction One or more of the devices.
- the present invention provides a novel process for producing propylene in parallel with p-xylene in a highly selective reaction with toluene and methanol and/or dimethyl ether.
- the ethylene-rich c 2 -component in the resulting product is returned to the reaction system for thiolation with methanol and/or dimethyl ether by using a specific modified molecular sieve catalyst.
- FIG. 1 is a flow chart of a method in accordance with an embodiment of the present invention.
- FIG. 2 is a flow chart of a method in accordance with another embodiment of the present invention.
- FIG. 3 is a flow chart of a method in accordance with another embodiment of the present invention.
- reaction reaction of toluene with methanol and/or dimethyl ether the reaction of ethylene with methanol and/or dimethyl ether, and the reaction process are coupled with high selectivity.
- Toluene and propylene the reaction scheme of the method of the present invention is as shown in FIG. 1.
- the raw material toluene is contacted with methanol and/or dimethyl ether in a reaction system with a catalyst (the catalyst is present in the reactor), and the resulting product enters a separation system (for example, Separation column, etc.) separation; after separation by separation system, C 6 + component, C 4 - C 5 component (hydrocarbons having carbon numbers 4 and 5), C 3 component and ethylene-rich C 2 _ are obtained.
- a separation system for example, Separation column, etc.
- the components are separated by further separation (for example, a rectification column or the like) to obtain propylene, and a small amount of c 4 -c 5 components and
- the reaction system may be a single reaction zone, or a combination of two or more reaction zones, the plurality of reaction zones may be in the same reactor, or may be multiple reactors connected in series or in parallel.
- the reactor is any one or any of a fixed bed, a fluidized bed or a moving bed.
- the raw material contains toluene with methanol and/or dimethyl ether
- the raw material may be a mixture of toluene, methanol and dimethyl ether, or a mixture of toluene and methanol or a mixture of toluene and dimethyl ether.
- a reaction scheme for the method according to the invention is shown in FIG. In Fig.
- the reaction system consists of a reactor having two reaction zones, wherein the main reaction in the first reaction zone is the reaction of toluene with methanol and/or dimethyl ether, and the main reaction of the second reaction zone is Ethylene (a by-product of the first reaction zone) is thiolated with methanol and/or dimethyl ether.
- the raw material toluene and methanol and/or dimethyl ether are first passed through the first reaction zone and contacted with the catalyst I therein, and then passed through the second reaction zone and contacted with the catalyst II therein, and the resulting product is separated into the separation system; After system separation, a C 6 + component, a C 4 -C 5 component, a C 3 component and a c 2 -component, and a 3 ⁇ 40 are obtained, wherein the ethylene-rich c 2 -component is returned to the second reaction zone and enters the The methanol and/or dimethyl ether in the second reaction zone is contacted with the catalyst II therein; the C 6 + component is separated by further separation to obtain p-xylene, and the C 3 component is further separated to obtain propylene.
- a reaction scheme for the method according to the invention is shown in FIG.
- the reaction system consists of two parallel reaction zones.
- the main reaction in the first reaction zone is toluene with methanol and/or dimethyl ether
- the main reaction in the second reaction zone is ethylene (first
- the by-product of the reaction zone is reacted with methanol and/or dimethyl ether.
- toluene is contacted with methanol and/or dimethyl ether in the first reaction zone with the catalyst I therein to form product A, and product A is separated into the separation system; the c 2 -component rich in ethylene from the separation system is returned to the first
- the second reaction zone is reacted with the raw material methanol and/or dimethyl ether directly entering the second reaction zone to form the product B, and the product B and the product A are separated into the separation system for separation; after separation by the separation system , wherein the C component rich in ethylene is returned to the second reaction zone, and the C 6 + component obtained by separating the product A and the product B by the separation system is further separated to obtain p-xylene, and the C 3 component is further The propylene is separated at a time.
- a reaction scheme for the method according to the invention is illustrated in Figure 4.
- the reaction system consists of two reaction zones in the same reactor, the reaction process is the same as that described above with respect to Fig. 3, and will not be described again here.
- Such a reaction system can be multi-staged. Material realization.
- the catalyst used contains ZSM-5 and/or ZSM-11 zeolite molecular sieves, more preferably ZSM-5 and/or ZSM-11 zeolite molecular sieves are hydrothermally treated, siloxane-based compounds are modified for surface acidity and pores. Structured modified ZSM-5 and/or ZSM-11 zeolite molecular sieves. Most preferably, after the modification with the siloxane-based compound, the supported amount of Si is from 1 to 10% by weight based on the total weight of the catalyst.
- the catalyst I and the catalyst II respectively present therein may be Think of the same or different catalysts.
- the catalyst I and the catalyst II are the same catalyst or the same catalyst.
- the catalyst used in the process of the invention is prepared as follows:
- the above acidic zeolite molecular sieve is subjected to hydrothermal treatment to obtain a modified zeolite molecular sieve.
- the hydrothermal treatment condition is treated at 500-700 ° C for 3-6 hours under a saturated steam atmosphere;
- siloxane based compound used in the present invention is as follows:
- R 2 , R 3 and R 4 are each independently C wo fluorenyl, such as methyl, ethyl, propyl, butyl, pentyl, hexyl, heptyl and octyl, and isomer forms thereof.
- the silicone-based compound used is tetraethyl orthosilicate.
- both the first reaction zone and the second reaction zone in the present invention may use a fixed bed reaction process, and may be combined with a regenerator to employ a fluidized bed or moving bed reaction process.
- the first reaction zone and the second reaction zone may be realized by multiple stages of feeding in one reactor or in a plurality of identical or different reactors connected in series or in parallel, respectively.
- the reaction temperature of the toluene with methanol and/or dimethyl ether, the reaction of ethylene with methanol and/or dimethyl ether thiolation is in the range of 300-600 ° C, and toluene with methanol and / or
- the preferred reaction temperature for dimethyl ether oximation is from 400 to 500 ° C, and the reaction temperature of ethylene with methanol and/or dimethyl ether is preferably from 350 to 450 ° C.
- the mass space velocity of the alkylation reaction of toluene with methanol and/or dimethyl ether is Ol-1Oh- 1 , preferably 1-5 h.
- the molar ratio of toluene to methanol and/or dimethyl ether feed may be in the range of from 0.1 to 10, preferably from 0.2 to 5, in the reaction of toluene with methanol and/or dimethyl ether.
- the molar ratio of ethylene to methanol and/or dimethyl ether can be It is in the range of 0.1 to 10, preferably 0.5 to 5.
- the C 2 -component means a component having a carbon number of 2 or less in the formula, including ethylene and acetamidine, formazan, CO, C0 2 and 3 ⁇ 4, etc., and the gas is mainly acetamidine, A ⁇ , co, co 2 and 3 ⁇ 4.
- the ⁇ 3 component means a compound having a carbon number of 3 in the formula, and includes propylene, propane or the like.
- the 0 ⁇ 5 component refers to a component having a carbon number of 4 and 5 in the formula, including isobutane, isobutylene, butyl hydrazine, 1-butene, 2-butene, isovaleryl, new Pentamidine, pentamidine, 1-pentene, 2-pentene, and the like.
- the C 6 + component means a component having a carbon number of 6 or more in the formula, including p-xylene and other aromatic hydrocarbons and derivatives thereof.
- the invention is described in detail below by way of examples, but the invention is not limited to the examples.
- the product composition was analyzed online by gas chromatography, and the analysis conditions were:
- Carrier gas helium, 5ml/min
- Oven temperature 60-220 °C, temperature programmed, 15 °C/min
- Catalyst preparation Si-HZSM-5 zeolite molecular sieve catalyst and Si-HZSM-11 zeolite molecular sieve catalyst
- HZSM-5 and HZSM-11 zeolite molecular sieves were modified by hydrothermal treatment respectively: HOOSM-5 and HZSM-11 molecular sieves were placed in a quartz reactor, and the temperature was raised to 650 °C, and the water flow rate was 5 ml/ Min, constant temperature treatment for 4 hours, obtained hydrothermally modified HZSM-5 zeolite molecular sieve, HZSM-11 zeolite molecular sieve.
- hydrothermally modified HZSM-5 zeolite molecular sieve and the HZSM-11 zeolite molecular sieve were surface-modified by using tetraethyl silicate as a siloxane reagent, respectively, and the steps were as follows: hydrothermally modified HZSM-5 zeolite Molecular sieves, HZSM-11 zeolite molecular sieves were immersed in 150 g of tetraethyl silicate overnight, and the liquid was decanted, dried at 120 ° C, and calcined in air at 550 ° C for 4 hours to obtain modified Si-HZSM- 5 zeolite molecular sieve catalyst and Si-HZSM-11 zeolite molecular sieve catalyst, named as catalysts TMPC-06 and TMPC-07, respectively.
- the HZSM-5/HZSM-11 zeolite molecular sieve was modified by hydrothermal treatment: 100 g of HZSM-5/HZSM-11 molecular sieve was placed in a quartz reactor, heated to 650 ° C, and then water was introduced, and the water flow rate was 5 ml/min. After thermostatic treatment for 4 hours, a hydrothermally modified HZSM-5/HZSM-11 zeolite molecular sieve was obtained.
- the surface modification of the hydrothermally modified HZSM-5/HZSM-11 zeolite molecular sieve was carried out using the silicone reagent tetraethyl silicate. The steps were as follows: The hydrothermally modified HZSM-5/HZSM-11 zeolite molecular sieve was placed in 150 g. After immersing in tetraethyl silicate overnight, the liquid was decanted, dried at 120 ° C, and calcined in air at 550 ° C for 4 hours to obtain a modified Si-HZSM-5/HZSM-1l zeolite molecular sieve catalyst, which was named For the catalyst TMPC-08.
- the catalysts TMPC-06, TMPC-07 and TMPC-08 catalyst samples prepared in Examples 1 and 2 were separately tableted and crushed into 40-60 mesh catalysts.
- the catalysts were separately charged into two reaction zones of a fixed bed reactor (10 g each for each reaction zone).
- the first reaction zone is subjected to a toluene methanol conversion reaction, wherein the molar ratio of toluene/methanol is shown in Table 1 below, and the second reaction zone is subjected to ethylene and methanol thiolation reaction.
- the nitrogen gas is blown online.
- the sweep was then switched to air to regenerate the catalyst at 550 ° C for 5 hours to recycle the catalyst.
- the ethylene-rich c 2 - component of the toluene methanol thiolation reaction product distribution in the first reaction zone is co-introduced into the second reaction zone with methanol, wherein the ethylene/methanol molar ratio is 1/1.
- Reaction conditions toluene space velocity of the first reaction zone mass 211-1, the reaction temperature was 480 ° C; a second reaction zone temperature of 420 ° C.
- the gas chromatograph was used to analyze the composition of the mixed product in the reaction zone on-line.
- the product distribution after removing the formed water is shown in Table 1, and the product distribution after removing the C 2 -component is shown in Table 2.
- the TMPC-06 catalyst prepared in Example 1 was tableted and crushed into 40-60 mesh catalyst samples, and each of the catalysts was separately charged into a fixed bed reactor. Two reaction zones (10 g each). The first reaction zone was subjected to a toluene methanol conversion reaction in which the molar ratio of toluene/methanol was 4/1, 2/1, 1/1 and 1/2, respectively (see Table 3 below), and the second reaction zone was subjected to ethylene and methanol.
- the first reaction zone and the second reaction zone are both purged with nitrogen gas, then switched to air to regenerate the catalyst at 550 Torr for 5 hours, nitrogen purged and cooled to the reaction temperature.
- Other reaction conditions Toluene mass space velocity of the first reaction zone 211-1, a reaction temperature of 480 ° C; a second reaction zone temperature of 400 ° C.
- the composition of the mixed product in the first reaction zone and the second reaction zone was analyzed online by gas chromatography, and the product distribution after removing the generated water is shown in Table 3.
- the product distribution after removal of the C 2 -component is shown in Table 4.
- the TMPC-06 catalyst prepared in Example 1 was tableted and crushed into 40-60 target catalyst samples, and 10 g of the catalyst was charged into the reactor for toluene methanol conversion reaction, and the toluene/methanol molar ratio was 4/ respectively. 1, 2/1, 1/1 and 1/2, when one of the ratios of the reaction is completed, a nitrogen purge is applied to the line, and then switched to air to regenerate the catalyst at 550 ° C for 5 hours, nitrogen purge And cooling to the reaction temperature for another ratio of toluene methanol conversion reaction.
- Other reaction conditions were: toluene mass space velocity of 2 h - reaction temperature of 480 °C.
- the product composition was analyzed online using a gas chromatograph, and the product distribution after removal of water was as shown in Table 5.
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SG11201610150PA SG11201610150PA (en) | 2014-06-04 | 2014-06-04 | Method for preparing p-xylene and co-producing propylene with high selectivity |
US15/315,603 US10099973B2 (en) | 2014-06-04 | 2014-06-04 | Method for preparing p-xylene and co-producing propylene with high selectivity |
MYPI2016704499A MY188942A (en) | 2014-06-04 | 2014-06-04 | Method for preparing p-xylene and co-producing propylene with high selectivity |
EP14894165.1A EP3153490B1 (en) | 2014-06-04 | 2014-06-04 | Method for preparing paraxylene with co-production of propylene with high selectivity |
PCT/CN2014/079144 WO2015184600A1 (zh) | 2014-06-04 | 2014-06-04 | 一种高选择性制备对二甲苯联产丙烯的方法 |
JP2016571213A JP6408612B2 (ja) | 2014-06-04 | 2014-06-04 | 高選択率でp−キシレンを製造してプロピレンを併産する方法 |
KR1020177000245A KR101912398B1 (ko) | 2014-06-04 | 2014-06-04 | 선택도가 높은 파라자일렌을 제조하고 프로필렌을 공동 생성하는 방법 |
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JP2020517427A (ja) * | 2017-04-27 | 2020-06-18 | 中国科学院大▲連▼化学物理研究所Dalian Institute Of Chemical Physics,Chinese Academy Of Sciences | トルエン、p−キシレン及び軽質オレフィンのうちの少なくとも1種を製造するための触媒のインサイチュ製造方法及び反応プロセス |
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EP3153490B1 (en) | 2019-11-27 |
JP2017518995A (ja) | 2017-07-13 |
JP6408612B2 (ja) | 2018-10-17 |
KR101912398B1 (ko) | 2018-10-26 |
KR20170013988A (ko) | 2017-02-07 |
US10099973B2 (en) | 2018-10-16 |
EP3153490A1 (en) | 2017-04-12 |
SG11201610150PA (en) | 2017-01-27 |
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US20170152197A1 (en) | 2017-06-01 |
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