CN117920182A - Catalyst for preparing BTX-rich aromatic hydrocarbon by directly converting catalytic synthesis gas and application thereof - Google Patents

Catalyst for preparing BTX-rich aromatic hydrocarbon by directly converting catalytic synthesis gas and application thereof Download PDF

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CN117920182A
CN117920182A CN202211244708.2A CN202211244708A CN117920182A CN 117920182 A CN117920182 A CN 117920182A CN 202211244708 A CN202211244708 A CN 202211244708A CN 117920182 A CN117920182 A CN 117920182A
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molecular sieve
aromatic hydrocarbon
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潘秀莲
张舒弛
苗登云
包信和
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Dalian Institute of Chemical Physics of CAS
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Dalian Institute of Chemical Physics of CAS
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Abstract

The invention discloses a catalyst and a method for preparing aromatic hydrocarbon rich in benzene (B), toluene (T) and xylene (X) by directly converting synthesis gas, which belong to the field of directly preparing aromatic hydrocarbon from synthesis gas. The reaction process has very high BTX product yield and selectivity, the aromatic hydrocarbon selectivity can reach 50-80%, the proportion of benzene, toluene and xylene in aromatic hydrocarbon can reach 30-80%, and the byproduct methane selectivity is lower than 10%, so that the method has very good application prospect.

Description

Catalyst for preparing BTX-rich aromatic hydrocarbon by directly converting catalytic synthesis gas and application thereof
Technical Field
The invention belongs to the field of aromatic hydrocarbon preparation by synthesis gas, and particularly relates to a catalyst and a method for preparing BTX-rich aromatic hydrocarbon by direct conversion of synthesis gas.
Background
Benzene, toluene and xylene (collectively referred to as BTX) are important basic chemicals, and are mainly used for producing synthetic materials such as terylene and polyurethane. In addition, aromatic hydrocarbons are also used as gasoline blending components and in the production of pesticides, herbicides, medicines, dyes and the like. Although the aromatic hydrocarbon production capacity of China rapidly develops in recent years, the requirements of national economy development cannot be met. In 2017, the external dependence of paraxylene reaches 60%. Currently, large-scale industrial production of BTX relies mainly on petroleum, with more than 70% of BTX derived from naphtha reforming. But because of the energy structure of rich coal and lean oil in China, petroleum in China depends on import in a large amount. With the rapid development of Chinese economy, the demand of crude oil is increased year by year, and the external dependence of crude oil is over 65 percent. Therefore, the preparation of aromatic hydrocarbons from non-petroleum resources such as coal, natural gas, biomass, etc. would have significant strategic significance. The preparation of aromatic hydrocarbons from non-petroleum resources can be achieved by converting the non-petroleum resources such as coal, natural gas, biomass, etc. into synthesis gas (mixed gas of CO and H 2) and then preparing aromatic hydrocarbons from the synthesis gas. The composite catalyst of the metal oxide and the ZSM-5 molecular sieve can realize the direct preparation of aromatic hydrocarbon from the synthesis gas, but the selectivity of BTX is very low and is about 30 percent. In 2017, the university of Xiamen Wang Ye teaches that team uses Zn-ZrO 2 to couple with ZSM-5 molecular sieves, achieving 80% aromatics selectivity with 20% CO conversion, but only 21.9% BTX selectivity. Although the BTX selectivity can be improved by shielding the acid sites on the external surface of the ZSM-5 molecular sieve, the silicon deposited on the external surface can partially block the pore opening, resulting in a decrease in CO conversion, a decrease in aromatics selectivity, and a decrease in catalyst efficiency. Therefore, the development of the catalyst which can directly produce high BTX selectivity and has stable efficiency from the synthesis gas has very important significance for the industries of energy, textile, chemical fiber, plastics and the like in China.
Disclosure of Invention
Aiming at the problems, the invention provides a catalyst and a method for preparing BTX-rich aromatic hydrocarbon by directly converting synthesis gas.
The technical scheme of the invention is as follows:
A catalyst which is a composite catalyst and comprises a component I, a component II and a component III; the component comprises a metal oxide I; the component II is one or two of ZSM-5 molecular sieve and ZSM-11 molecular sieve, and the component III is one or more than two of SAPO-34, SAPO-18 or SAPO-17; the component I, the component II and the component III in the catalyst are compounded into I+II+III in a powder mixing mode; the active component metal oxide I in the component I is one or more than two of ZrO2、Cr2O3、ZnCrxO(1+1.5x)、ZnAlxO(1+1.5x)、ZnCrxAlyO(1+1.5x+1.5y)、ZnZrxO(1+2x)、ZnGaxO(1+1.5x)、ZnInxO(2+1.5x)、MnCrxOy、ZnMnxOy、MnGaxOy; the value range of x is 1-3.5, and the value range of y is 0.1-10.
Based on the above technical scheme, preferably, in the component II, the silicon-aluminum ratio of the ZSM-5 or ZSM-11 molecular sieve is 20 to 1000, preferably 50 to 800, more preferably 50 to 600;
based on the above technical scheme, preferably, the component II has the characteristic of medium strong acid, and the amount of the medium strong acid site is 0.05-0.5mol/kg, preferably 0.05-0.4mol/kg, and more preferably 0.05-0.3mol/kg.
Wherein the temperature range corresponding to the peak top of the desorption peak of the NH 3 -TPD corresponding to the medium strong acid is 200-500 ℃; using acetone as the probe molecule, 13 C-NMR chemical shifts lie in the range 210-220 ppm.
Based on the above technical scheme, preferably, the skeleton element composition of the component III can be one or more than two of Si-O, si-Al-O, si-B-O, si-Al-Ti-O, ga-Si-O, ga-Si-Al-O, mg-Al-P-O, fe-Si-O, as-Si-O.
Based on the technical scheme, preferably, the component III has the characteristic of medium strong acid, wherein the amount of the medium strong acid site is 0.05-2.5mol/kg, and is selected to be 0.05-2.0mol/kg. Wherein the temperature range corresponding to the peak top of the desorption peak of the NH 3 -TPD corresponding to the medium strong acid is 200-500 ℃; using acetone as the probe molecule, 13 C-NMR chemical shifts lie in the range 210-220 ppm.
The acid strength is defined by an NH 3 -TPD peak and comprises three acidity of weak acid, medium strong acid and strong acid;
The NH 3 -TPD is based on the desorption peak position of NH 3, wherein the desorption peak position refers to the thermal conductivity signal of desorption NH 3 recorded by TCD under the test condition that the ratio of sample mass w to carrier gas flow rate f (w/f) =100 g.h/L and the heating rate of 10 ℃/min is increased under the standard test condition, a desorption curve is drawn, and the inorganic solid is divided into three acid intensities according to the peak position top point of the curve; weak acid refers to an acidic site with NH 3 desorption temperature less than 275 ℃; the medium strong acid is an acid site with NH 3 desorption temperature of 275-500 ℃; the strong acid is an acid site with a desorption temperature of NH 3 of more than 500 ℃.
Based on the above technical scheme, preferably, the weight ratio of the active ingredient in the component I to the component II is 0.1-20:1, preferably 0.3-5:1; the weight ratio of the active ingredient in component I to component III is 0.1-20:1, preferably 0.3-5:1.
Based on the technical scheme, preferably, the component I further comprises a dispersing agent, and the metal oxide I is dispersed in the dispersing agent; the active component is metal oxide I; the dispersing agent is one or more than two of Al 2O3、SiO2、TiO2, active carbon, graphene and carbon nano tubes.
Based on the technical scheme, the content of the dispersing agent in the component I is preferably 0.05-90wt% and the balance is the metal oxide I.
Based on the above technical scheme, preferably, the O element of the molecular sieve framework of the component II and the component III may be connected or not connected with H; and H can be completely or partially substituted by one or more than two of Na, mg, sn, mn, ag, mo, cr, fe, co, V, pt, pd, ti, zn, ga, as, ge in an ion exchange mode, and the molar ratio of total metal after substitution to B acid of the molecular sieve (the molecular sieve refers to the total molecular sieve of the component II and the component III) is 1-30%.
The invention also provides a method for preparing benzene, toluene and xylene by directly converting synthesis gas, which takes the synthesis gas as a reaction raw material, and carries out conversion reaction on a fixed bed by adopting the catalyst as the catalyst;
The pressure of the synthesis gas is 0.5-10MPa, preferably 1-8MPa; the reaction temperature is 300-600 ℃, preferably 350-500 ℃; the space velocity is 300-12000ml/g cat/h, preferably 300-9000ml/g cat/h, more preferably 300-7000ml/g cat/h; the synthesis gas is H 2/CO mixed gas, and the ratio of H 2/CO is 0.2-3.5, preferably 0.3-2.5.
The composite catalyst is used for preparing aromatic hydrocarbon rich in BTX by directly converting synthetic gas in one step, wherein the selectivity of the aromatic hydrocarbon can reach 50-80%, preferably 65-80%, the proportion of BTX in the aromatic hydrocarbon is 30-80%, preferably 60-80%, and the selectivity of byproduct methane is lower than 10%.
Advantageous effects
1. The technology is different from the traditional liquid fuel prepared by Fischer-Tropsch synthesis, and realizes the efficient conversion of the synthesis gas into BTX by one step. The proportion of BTX in the aromatic hydrocarbon product is high and can reach 30-80%.
2. The use of component I, component II or component III, or a combination of both, as described herein, alone, does not fully achieve the functions of the present invention, e.g., the methane selectivity is very high and the conversion is very low in the component I product alone, while the use of component II or component III alone or component II+III does not activate the converted synthesis gas; the I+II can be used for directly preparing aromatic hydrocarbon from the synthesis gas, but the BTX selectivity is very low; the use of I+III cannot realize the preparation of aromatic hydrocarbon from synthesis gas, and most of products are low-carbon olefins. Only the synergistic catalysis of the component I, the component II and the component III can realize the direct conversion of the synthesis gas to prepare the aromatic hydrocarbon rich in BTX.
3. The preparation process of the composite catalyst is simple, and the conditions are mild; the reaction process has high product yield and selectivity, the selectivity of aromatic hydrocarbon can reach 50-80%, the proportion of BTX can reach 30-80%, and the selectivity of byproduct methane is low (lower than 10%).
Detailed Description
The invention is further illustrated by the following examples, but the scope of the claims is not limited by these examples. Meanwhile, the embodiments only give some conditions for achieving this object, but do not mean that these conditions must be satisfied to achieve this object.
The specific surface area of the sample may be tested by physical adsorption of nitrogen or argon.
The metal oxide I can be obtained by purchasing commercially available metal oxide with high specific surface area, and can also be obtained by the following methods:
1. preparation of catalyst component I
(I), synthesizing the ZrO 2 material by a precipitation method:
weighing 0.5g of zirconyl nitrate into a container, weighing 0.795g (7.5 mmol) of zirconyl nitrate into the container, weighing 30ml of deionized water into the container, stirring at 70 ℃ for more than 0.5h to uniformly mix the solution, and naturally cooling to room temperature. Centrifugally separating the reaction liquid, collecting the centrifugally separated precipitate, and washing with deionized water for 2 times to obtain a ZrO 2 metal oxide precursor; and (3) drying the obtained product in the air, and roasting the dried product in the air at 500 ℃ for 3 hours to obtain the ZrO 2 material. Designated Ox-1.
(II) precipitation method synthesis ZnCrxO(1+1.5x)、ZnAlxO(1+1.5x)、ZnCrxAlyO(1+1.5x+1.5y)、ZnZrxO(1+2x)、ZnGaxO(1+1.5x)、ZnInxO(2+1.5x)、MnCrxOy：
Mixing one or more than two of zinc nitrate, chromium nitrate, manganese nitrate, zirconium nitrate, gallium nitrate and indium nitrate serving as precursors, dispersing agents such as aluminum nitrate, titanium nitrate, activated carbon, graphene and carbon nano tubes, dispersing agent precursors and ammonium carbonate with each other in water at room temperature (wherein the ammonium carbonate is taken as a precipitator, and the feeding ratio is that the ammonium carbonate is excessive or the ratio of ammonium ions to metal ions is preferably 1:1); the above mixed solution was aged, then taken out for washing, filtration and drying, and the obtained solid was calcined under an air atmosphere to obtain component I, specific samples and preparation conditions thereof are shown in table 1 below.
TABLE 1 preparation of component I
2. Preparation of component II
The medium and strong acid described in the invention can be tested by means of H spectrum, NH 3 -TPD, infrared and chemical titration of solid nuclear magnetism. However, the method for testing acidity is not limited to the above test method.
The component II can be a ZSM-5 molecular sieve or a ZSM-11 molecular sieve with commercial acid density meeting the requirement of the invention, and also can be a self-synthesized molecular sieve, and here, the ZSM-5 molecular sieve and the ZSM-11 molecular sieve prepared by a hydrothermal synthesis method are taken as an example.
The preparation process comprises the following steps:
Raw materials are weighed according to the oxide SiO 2:Al2O3:TPAOH:H2 o=1:0.02-0.0017:0.4:45 (molar ratio): a silicon source; an aluminum source; tetrapropylammonium hydroxide; deionized water, mixing and stirring at room temperature, transferring to a hydrothermal kettle after 2h, and crystallizing for 4-7 days at 160-180 ℃. Quenching in water bath to room temperature, repeatedly centrifuging and washing to obtain supernatant with pH of 7 at the end of washing, drying precipitate at 110deg.C for 12 hr, and calcining in air at 600deg.C for 3 hr to obtain ZSM-5 molecular sieve.
Raw materials are weighed according to the oxide SiO 2:Al2O3:TBAOH:H2 o=1:0.02-0.0017:0.4:45 (molar ratio): a silicon source; an aluminum source; tetrabutylammonium hydroxide; deionized water, mixing and stirring at room temperature, transferring to a hydrothermal kettle after 2h, and crystallizing at 160-180 ℃ for 1-7 days. Quenching in water bath to room temperature, repeatedly centrifuging and washing to obtain supernatant with pH of 7 at the end of washing, drying precipitate at 110deg.C for 12 hr, and calcining in air at 600deg.C for 3 hr to obtain ZSM-11 molecular sieve.
The silicon source is selected as follows: one or more than two of TEOS, silica sol and white carbon black; the aluminum source is selected as follows: one or more of sodium metaaluminate, al (OH) 3, alOOH and aluminum isopropoxide;
The framework element composition with the ZSM-5 molecular sieve or the ZSM-11 molecular sieve can be one or more than two of Si-O, si-Al-O, si-B-O, si-Al-Ti-O, ga-Si-O, ga-Si-Al-O, mg-Al-P-O, fe-Si-O, as-Si-O;
H is connected to O element of partial skeleton, and corresponding products are defined as sub 2-1, sub 2-2, sub 2-3 and sub 2-4 in sequence;
TABLE 2 preparation of ZSM-5 molecular sieves and ZSM-11 molecular sieves and performance parameters thereof
Preparation of comparative component II (MOR molecular sieve) of 2-5: raw materials are weighed according to the proportion of oxide SiO2 to Al2O3 to NaOH to H2O=1:0.05:0.375:32 (molar ratio): a silicon source; an aluminum source; sodium hydroxide; deionized water, mixing and stirring at room temperature, and then transferring to a reaction kettle for dynamic crystallization at 160 ℃ for 48 hours. Quenching in water bath to room temperature, repeatedly centrifuging and washing to obtain supernatant with pH of 7 at the end of washing, drying precipitate at 110deg.C for 12 hr, and calcining in air at 600deg.C for 3 hr to obtain Na-type MOR molecular sieve. The synthesized Na-MOR molecular sieves were subjected to ammonium exchange with 1.0mol/L ammonium chloride solution at 80℃to exchange Na + for NH4 + (ammonium chloride solution volume to molecular sieve mass ratio: 50 ml/g) three times in succession, each exchange time being 2 hours. And then centrifugally washing and drying, transferring the mixture into a muffle furnace, and burning the mixture in an air atmosphere at 500 ℃ for 2 hours to obtain the H-type MOR molecular sieve.
3. Preparation of component III (SAPO-34 or SAPO-18 or SAPO-17):
the component III can be a commercial SAPO-34 or SAPO-18 or SAPO-17 molecular sieve with acid density meeting the requirements of the invention, or a self-synthesized molecular sieve, wherein the commercial molecular sieve is taken as an example, and the specific table is shown below.
TABLE 3 amount of Medium Strong acids of SAPO-34 or SAPO-18 or SAPO-17 molecular sieves
Sample numbering Molecular sieve Amount of medium and strong acid mol/kg
Divide 3-1 SAPO-34 0.4
Divide 3-2 SAPO-18 0.3
Divide 3-3 SAPO-17 0.5
3. Preparation of the catalyst
Preparation of I+II+III composite catalyst:
The catalyst I, the catalyst II and the catalyst III in required proportions are added into a container, the purposes of separation, crushing, uniform mixing and the like are realized by utilizing one or more than two actions of extrusion force, impact force, shearing force, friction force and the like generated by high-speed movement of the materials and/or the container, the conversion of mechanical energy, thermal energy and chemical energy is realized by regulating the temperature and carrier gas atmosphere, and the interaction among different components is further regulated.
The powder mixing can be carried out by adopting one or more than two of mechanical stirring, grinding and ball milling.
The weight ratio of the component I to the component II to the component III is 1:0-10:0-10, preferably 1:0.5-5:0.5 to 5, more preferably 1:0.5-3:0.5-3.
The specific catalyst preparation is shown in table 4.
The comparative catalyst was prepared as shown in table 5.
Preparation of Table 4I+II+III composite catalyst and its parameter characteristics
Catalyst numbering Catalyst component I Catalyst component II Catalyst component III I: II: III weight ratio Mixing mode
I+II+Ⅲ-1 Ox-1 Divide into 2-1 Divide 3-1 1：1：2 Grinding
I+II+Ⅲ-2 Ox-1 Divide into 2-1 Divide 3-1 1：3：1.5 Grinding
I+II+Ⅲ-3 Ox-2 Divide into 2-2 Divide 3-2 1：1.5：1.5 Ball milling
I+II+Ⅲ-4 Ox-2 Divide into 2-2 Divide 3-2 1：2：1 Ball milling
I+II+Ⅲ-5 Ox-3 Divide into 2-3 Divide 3-3 1：1.5：1.5 Mechanical stirring
I+II+Ⅲ-6 Ox-4 Divide into 2-4 Divide 3-1 1：1.5：1.5 Mechanical stirring
I+II+Ⅲ-7 Ox-5 Divide into 2-1 Divide 3-1 1：1.5：1.5 Grinding
I+II+Ⅲ-8 Ox-6 Divide into 2-1 Divide 3-1 1：1.5：1.5 Grinding
I+II+Ⅲ-9 Ox-7 Divide into 2-1 Divide 3-1 1：1.5：1.5 Grinding
Table 5 preparation of comparative example composite catalyst and its parameter characteristics
Catalyst numbering Catalyst component I Catalyst component II Catalyst component III I: II: III weight ratio Mixing mode
Comparative catalyst 1 Ox-1 - - 1:0:0 -
Comparative catalyst 2 - Divide into 2-1 Divide 3-1 0:1:1 Grinding
Comparative catalyst 3 Ox-2 - Divide 3-2 1:0:1 Grinding
Comparative catalyst 4 Ox-1 Divide into 2-5 - 1:1:0 Grinding
Comparative catalyst 5 Ox-3 Divide into 2-3 - 1:1:0 Grinding
Comparative catalyst 6 Ox-1 Divide into 2-1 Divide 3-1 1:2:1 Particle mixing
Comparative catalyst 7 Ox-1 Divide into 2-5 Divide 3-1 1:1:1 Grinding
Catalytic reaction examples
The fixed bed reaction device is provided with a gas mass flowmeter and an online product analysis chromatograph (the tail gas of the reactor is directly connected with a quantitative valve of the chromatograph to carry out periodic real-time sampling analysis).
2G of the catalyst of the present invention was placed in a fixed bed reactor, the air in the reactor was replaced with Ar, then the temperature was raised to 300℃and the synthesis gas (H 2/CO molar ratio=1) was switched to a pressure of 4MPa, the temperature was raised to a reaction temperature of 430℃and the space velocity of the reaction feed gas was adjusted to 2500ml/g/H. The product was analyzed by on-line chromatographic detection.
The specific applications of the catalysts and their effect data are shown in Table 6.
Table 6 specific application of catalyst and effect data thereof
The catalyst used in comparative example 1 was only component I, contained no components ii and III, had very low conversion, and no aromatic hydrocarbon in the product.
The catalyst used in comparative example 2 did not contain component I, contained components II and III, and had a CO conversion of 0.
Comparative example 3 uses a catalyst that does not contain component II, contains components I and III, and does not contain aromatic hydrocarbons in the product.
The catalyst used in comparative example 4 did not contain component III, contained components I and II, and component II replaced ZSM-5 or ZSM-11 with MOR molecular sieves, with only 2% aromatics selectivity in the product.
The catalyst used in comparative example 5 did not contain component III, and contained components I and II, with a BTX selectivity of only 25% in the aromatic hydrocarbon.
The catalyst used in comparative example 6 was one in which the mixing mode of components i+ii+iii was changed from powder mixing to particle mixing, the selectivity for aromatic hydrocarbon was only 32%, and the selectivity for BTX was only 35%.
The catalyst used in comparative example 7 was prepared by replacing component II with components 2 to 5 and then mixing the powders of components I+II+III, the aromatic selectivity in the product being only 2%.
From the above table, it can be seen that the topology of the molecular sieve, the matching between the catalyst components I, II and III, and the manner of mixing the three components are critical, directly affecting the carbon monoxide conversion, the aromatic selectivity, and the proportion of BTX therein.
The preparation process of the composite catalyst is simple, and the conditions are mild; the reaction process has high product yield and selectivity, the selectivity of aromatic hydrocarbon can reach 50-80%, the proportion of BTX can reach 30-80%, and the selectivity of byproduct methane is low (less than 10%).

Claims (7)

1. A catalyst, characterized in that: the catalyst is a composite catalyst and comprises a component I, a component II and a component III; component I comprises a metal oxide I; the component II is one or two of ZSM-5 molecular sieve and ZSM-11 molecular sieve, and the component III is one or more than two of SAPO-34, SAPO-18 or SAPO-17; the component I, the component II and the component III in the catalyst are compounded into I+II+III in a powder mixing mode; the active component metal oxide I in the component I is one or more than two of ZrO2、Cr2O3、ZnCrxO(1+1.5x)、ZnAlxO(1+1.5x)、ZnCrxAlyO(1+1.5x+1.5y)、ZnZrxO(1+2x)、ZnGaxO (1+1.5x)、ZnInxO(2+1.5x)、MnCrxOy、ZnMnxOy、MnGaxOy; the value range of x is 1-3.5, and the value range of y is 0.1-10.
2. The catalyst of claim 1, wherein: in the component II, the component A is prepared from the following components,
The ZSM-5 molecular sieve or ZSM-11 molecular sieve has a silica-alumina ratio of from 20 to 1000, preferably from 50 to 800, more preferably from 50 to 600; the ZSM-5 molecular sieve or ZSM-11 molecular sieve has the characteristic of medium strong acid, and the amount of the medium strong acid sites is 0.05-0.5mol/kg, preferably 0.05-0.4mol/kg, and more preferably 0.05-0.3mol/kg.
3. The catalyst of claim 1, wherein: in the component III, the component A is a compound,
The molecular sieve skeleton element composition in the SAPO-34 or the SAPO-18 or the SAPO-17 is one or more than two of Si-O, si-Al-O, si-B-O, si-Al-Ti-O, ga-Si-O, ga-Si-Al-O, mg-Al-P-O, fe-Si-O, as-Si-O; has the characteristic of medium strong acid, and the amount of the medium strong acid site is 0.05-2.5mol/kg, preferably 0.05-2.0mol/kg.
4. The catalyst of claim 1, wherein: the powder mixing mode of the component I, the component II and the component III is to mix the component I, the component II and the component III by adopting grinding, ball milling and other modes, and the aim of uniform mixing is realized by utilizing the actions of extrusion force, impact force, shearing force, friction force and the like generated by the movement of materials and/or containers.
5. The catalyst of claim 1, wherein: the weight ratio of the active ingredient in the component I to the component II is 0.1-20:1, preferably 0.3-5:1; the weight ratio of the active ingredient in component I to component III is 0.1-20:1, preferably 0.3-5:1.
6. The catalyst of claim 1, wherein: the component I also comprises a dispersing agent, wherein the metal oxide I is dispersed in the dispersing agent, and the dispersing agent is one or more than two of Al 2O3、SiO2、TiO2, active carbon, graphene and carbon nano tubes; in the component I, the content of the dispersing agent is 0.05-90wt% and the balance is metal oxide I.
7. A method for preparing BTX-rich aromatic hydrocarbon by directly converting synthesis gas is characterized by comprising the following steps: carrying out conversion reaction on a fixed bed by taking synthesis gas as a reaction raw material, wherein the adopted catalyst is the catalyst of any one of claims 1-6;
The pressure of the synthesis gas is 0.5-10MPa, preferably 1-8MPa; the reaction temperature is 300-600 ℃, preferably 350-500 ℃; the space velocity is 300-12000ml/g cat/h, preferably 300-9000ml/g cat/h, more preferably 300-7000ml/g cat/h; the synthesis gas is H 2/CO mixed gas, and the ratio of H 2/CO is 0.2-3.5, preferably 0.3-2.5; the aromatic hydrocarbon selectivity of the method can reach 50-80%, and the byproduct methane selectivity is lower than 10%; benzene, toluene and xylene can reach 30-80% in aromatic hydrocarbon.
CN202211244708.2A 2022-10-12 2022-10-12 Catalyst for preparing BTX-rich aromatic hydrocarbon by directly converting catalytic synthesis gas and application thereof Pending CN117920182A (en)

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