阅读说明：本技术 一种用于合成气直接制取低碳α-烯烃的催化剂及其制备方法 (Catalyst for directly preparing low-carbon alpha-olefin from synthesis gas and preparation method thereof ) 是由 韩一帆 徐晶 查斌斌 张征湃 张俊 于 2018-06-08 设计创作，主要内容包括：本发明公开了一种用于合成气直接制取低碳α-烯烃的催化剂及其制备方法。所述方法包括步骤：(1)将含有铁元素及第二金属元素的有机溶液和表面活性剂混合,置于零下30℃至30℃形成前驱体溶液；优选零下30℃至零下5℃；更优选零下20℃至零下5℃；(2)使前驱体溶液与沉淀剂混合得到沉淀物；(3)沉淀物经含有其他元素的水溶液浸渍后,干燥、煅烧得到用于合成气直接制取低碳α-烯烃的催化剂。(The invention discloses a catalyst for directly preparing low-carbon alpha-olefin from synthesis gas and a preparation method thereof. The method comprises the following steps: (1) mixing an organic solution containing iron element and a second metal element with a surfactant, and placing at-30 ℃ to form a precursor solution; preferably from-30 ℃ to-5 ℃; more preferably from-20 ℃ to-5 ℃; (2) mixing the precursor solution with a precipitator to obtain a precipitate; (3) and soaking the precipitate in water solution containing other elements, drying and calcining to obtain the catalyst for directly preparing low-carbon alpha-olefin from the synthesis gas.)

1. A method for preparing a catalyst for directly preparing low-carbon alpha-olefin from synthesis gas is characterized by comprising the following steps:

(1) Mixing an organic solution containing iron element and a second metal element with a surfactant, and placing at-30 ℃ to form a precursor solution; preferably from-30 ℃ to-5 ℃; more preferably from-20 ℃ to-5 ℃;

(2) Mixing the precursor solution with a precipitator to obtain a precipitate;

(3) And soaking the precipitate in water solution containing other elements, drying and calcining to obtain the catalyst for directly preparing low-carbon alpha-olefin from the synthesis gas.

2. The method according to claim 1, wherein the second metal element is one or two or more selected from the group consisting of: nickel, copper, manganese, vanadium, zinc, cobalt, molybdenum and niobium; the other elements are selected from one or more than two of the following elements: chromium, cerium, lanthanum, zirconium, sodium, indium, tin and potassium.

3. The method according to claim 1, wherein the organic solution containing the iron element and the second metal element is obtained by uniformly mixing an iron source and a second metal source with an organic solvent;

the iron source is selected from one or more than two of the following: ferric sulfate, ferrous sulfate, ferric chloride, ferrous nitrate, ferric citrate, ferric ammonium citrate, hydroxyl iron, ferric acetate, carbonyl iron and ferric carbonate. (ii) a

The second metal source is selected from one or more than two of the following: sulfates, carbonates, nitrates and chlorides of nickel, copper, manganese, vanadium, zinc, cobalt, molybdenum, niobium; preferably copper;

The organic solvent is selected from one or more than two of the following: methanol, ethanol, ethylene glycol, glycerol, n-propanol, isopropanol, n-butanol, isobutanol, pentanol, toluene, xylene, chloroform, acetone, ethylenediamine, triethylamine, triethanolamine, polyether, and polyvinyl alcohol;

The aqueous solution containing other elements is an aqueous solution of a source of the other elements; the other element source is selected from one or more than two of the following: sulfates, carbonates, nitrates and chlorides of chromium, cerium, lanthanum, zirconium, sodium, indium, tin, potassium.

4. The preparation method according to claim 1, wherein the precursor solution is mixed with the precipitant to achieve a pH of 3 to 12, and the method comprises uniformly dropping the precipitant into the precursor solution, uniformly dropping the precursor solution into the precipitant, or simultaneously dropping the precursor solution and the precipitant; the dropping speed is 0.2-12 mL/min.

5. the production method according to any one of claims 1 to 4, wherein the surfactant is one or two or more selected from the group consisting of: dodecylbenzene sulfonic acid, sodium dodecylbenzene sulfonate, hexadecyl trimethyl ammonium bromide, sodium succinic acid (-2-ethyl) hexyl ester sulfonate, sodium linoleate, oleic acid, polyethylene glycol, tween-80 and polyoxyethylene-polyoxypropylene-polyoxyethylene (P123).

6. A catalyst produced by the production method according to any one of claims 1 to 5, comprising the following metal oxides based on the total weight of the catalyst:

40-80 wt% iron oxide

15-40 wt% of a second metal oxide

0% -35% of other metal oxides;

The second metal is selected from one or more than two of the following metals: nickel, copper, manganese, vanadium, zinc, cobalt, molybdenum and niobium;

The other metal is selected from one or more than two of the following metals: chromium, cerium, lanthanum, zirconium, sodium, indium, tin or potassium.

7. The catalyst of claim 6, wherein the catalyst has a specific surface area of 30 to 500m²/g。

8. Use of a catalyst according to claim 6 or 7 for the direct preparation of low carbon alpha-olefins from synthesis gas.

9. The use of claim 8, wherein the synthesis gas is in the molar ratio CO to H₂1 (0.5-5) of CO and H₂The selectivity of the long-chain alkane with 5 to 20 carbon atoms in the molecule in the total product is 2.0 to 10.0 percent.

10. a method for directly preparing low-carbon alpha-olefin from synthesis gas is characterized by comprising the following steps:

(i) At the temperature of 200 ℃ and 500 ℃ and under the pressure of 0-5.0MPa, the molar ratio of CO to H is used₂CO/H of 1 (0.5-5)₂Mixed gas of H₂Or carrying out in-situ reduction treatment on the catalyst of claim 6 or 7 in a CO atmosphere for 5-50 hours;

(ii) The synthesis gas is reacted through a reactor filled with the catalyst reduced in the step (i), the reaction temperature T is more than or equal to 200 ℃ and less than or equal to 500 ℃, the reaction pressure P is more than or equal to 0.5MP and less than or equal to 5MPa, and the reaction space velocity GHSV is 800h^-1≤GHSV≤30000h^-1(ii) a The product of C2-C8 alpha-olefin is collected at the outlet of the reactor.

Technical Field

The invention belongs to the field of energy and chemical engineering, and relates to a method for directly preparing C by using synthesis gas as raw material gas₂-C₈Preparation and application of a catalyst for low-carbon alpha-olefin. In particular to a non-supported iron-based catalyst synthesized by a novel preparation method and application of the catalyst in the aspect of directly catalyzing synthesis gas to prepare low-carbon alpha-olefin with high selectivity.

Background

The α -olefin generally refers to a monoolefin having a double bond at the end of the molecular chain, and the linear α -olefin refers to a linear olefin having 4 or more carbon atoms and containing a carbon-carbon double bond. C₂-C₈The normal olefins are all within the category of alpha-olefins. Wherein ethylene and propylene are important basic organic chemical raw materials, and C₄-C₈Linear alpha-olefins, such as 1-butene, 1-hexene and 1-octene, are important organic feedstocks and chemical intermediates and are widely used in polyethylene comonomers, surfactants, lubricants, plasticizers, polyalphaolefins, adjuvants and fine chemicals.

direct preparation of C from synthesis gas from coal, natural gas and biomass₂-C₈The precipitation method in the alpha-olefin technology is the most commonly used method for preparing the Fischer-Tropsch synthesis Fe catalyst. The traditional precipitation method mostly adopts a high-temperature precipitation mode, however, the precipitation at high temperature is beneficial to crystal growth and is not beneficial to the dispersion of metal particles, and the metal nanoparticles are easy to agglomerate to form large particles.

CN101906009A discloses a method for preparing linear alpha-olefin, which comprises introducing a catalyst solution and ethylene into a first reactor to obtain a first linear alpha-olefin, introducing the first mixture of ethylene and the catalyst solution into a second reactor to obtain a second mixture, subjecting the second mixture to gas-liquid separation, introducing the separated ethylene into the first reactor for recycling, and rectifying a liquid-phase product to obtain alpha-olefin. The main catalyst of the method is prepared from pyridine diimineBody and acetylacetone metal salt, in which product C₄-C₈78.4% by mass of linear alpha-olefin, C₁₀-C₂₀20.4% by mass of linear alpha-olefin, C₂₂-C₄₀The alpha-olefin content was 1.2% by mass, the linear selectivity was 97.1% by mass, and the activity was 3.25X 10⁸g/mol Fe/h, but the majority of the oligomerized olefin is even alpha-olefin, so that large-scale odd alpha-olefin cannot be obtained.

CN1065026A discloses a method for preparing ethylene from syngas, wherein the catalyst is prepared by a chemical precipitation method or a mechanical mixing method, and the ethylene selectivity is 65% to 94% by using noble metals or rare metals, such as more than ten chemical elements of niobium, gallium, scandium, indium, cerium, lanthanum, ytterbium, etc., but the CO conversion rate is low, only 10%, 12%, 15%, the CO recycling increases the energy consumption, and the catalyst cost is high.

CN104056627A discloses a method for preparing a catalyst for generating low-carbon olefin with high selectivity from synthesis gas, the catalyst is prepared by adopting an impregnation method or a coprecipitation method, a relatively inert iron source is used as a precursor to be loaded on an inert carrier, and C2 of the catalyst is C2^＝-C4^＝The selectivity of olefin is 45-55%, but the selectivity of C5+ reaches 20-40%, the conversion rate of CO is not high and is only about 2-15%, the energy consumption is increased by recycling CO, and the chain growth capability is strong.

CN103664436A discloses a preparation method of a catalyst for directly converting synthesis gas into low-carbon olefins, wherein the catalyst is a mixture of a Fischer-Tropsch synthesis catalyst and a ZSM-5 molecular sieve catalyst, activated carbon is selected as a carrier, and the Fischer-Tropsch synthesis catalyst is prepared by a vacuum impregnation method, so that active components and auxiliaries can be highly and uniformly dispersed on the surface of the activated carbon carrier, the low-carbon olefin selectivity is 58-72%, and the conversion rate is over 95%. However, the activated carbon as a catalyst carrier has poor mechanical strength and difficult catalyst molding, which affects the service life and stability of the catalyst and is not beneficial to industrial application.

CN101191066B discloses an iron-based catalyst for preparing hydrocarbons from synthesis gas, and the catalystThe elements comprise Fe, Mn, Al, K and the like, are prepared by an alloy melting method, show high activity and C₅₊The high selectivity of the hydrocarbon and the low-carbon olefin. Its CO conversion rate can be up to 90%, C₂-C₄Olefin selectivity 18.45% and C₅₊The hydrocarbon selectivity reaches 60 percent. The preparation process has strict conditions, the molten metal not only needs extremely high temperature, but also strictly requires the cooling rate to be more than 10⁶Preferably 10 ℃ per second⁷The catalyst has high preparation cost and difficult realization, and is not beneficial to large-scale production.

Therefore, the method for preparing the Fischer-Tropsch synthesis Fe catalyst with a simple process is urgently needed in the field, and the prepared catalyst has the advantages of good alpha-olefin selectivity and the like.

Disclosure of Invention

The invention aims to provide a method for directly preparing low-carbon olefin and co-producing C by using Fe-based synthesis gas₄-C₈An alpha-olefin catalyst and a method for preparing the same.

In a first aspect of the present invention, there is provided a method for preparing a catalyst for direct synthesis gas production of low-carbon α -olefins, the method comprising the steps of:

(1) Mixing an organic solution containing iron element and a second metal element with a surfactant, and placing at-30 ℃ to form a precursor solution;

(2) mixing the precursor solution with a precipitator to obtain a precipitate; and

(3) and soaking the precipitate in water solution containing other elements, drying and calcining to obtain the catalyst for directly preparing low-carbon alpha-olefin from the synthesis gas.

In one embodiment of the present invention, the precursor solution is preferably formed at-30 ℃ to-5 ℃ in step (1); more preferably from-20 ℃ to-5 ℃.

In another preferred example, the second metal element is selected from one or two or more of the following: nickel, copper, manganese, vanadium, zinc, cobalt, molybdenum and niobium; the other elements are selected from one or more than two of the following elements: chromium, cerium, lanthanum, zirconium, sodium, indium, tin and potassium.

In another preferred embodiment, the molar ratio of the iron to the second metal element is 2-6: 1; more preferably 3-5: 1.

In another preferred embodiment, the organic solution containing the iron element and the second metal element is obtained by uniformly mixing an iron source, a second metal source and an organic solvent;

The iron source is selected from one or more than two of the following: ferric sulfate, ferrous sulfate, ferric chloride, ferrous nitrate, ferric citrate, ferric ammonium citrate, hydroxyl iron, ferric acetate, carbonyl iron and ferric carbonate. (ii) a

The second metal source is selected from one or more than two of the following: sulfates, carbonates, nitrates and chlorides of nickel, copper, manganese, vanadium, zinc, cobalt, molybdenum, niobium; preferably copper;

The organic solvent is selected from one or more than two of the following: methanol, ethanol, ethylene glycol, glycerol, n-propanol, isopropanol, n-butanol, isobutanol, pentanol, toluene, xylene, chloroform, acetone, ethylenediamine, triethylamine, triethanolamine, polyether, and polyvinyl alcohol;

The aqueous solution containing other elements is an aqueous solution of a source of the other elements; the other element source is selected from one or more than two of the following: sulfates, carbonates, nitrates and chlorides of chromium, cerium, lanthanum, zirconium, sodium, indium, tin, potassium.

In another preferred embodiment, the precursor solution is mixed with a precipitant to make the pH value between 3 and 12, and the method comprises the steps of dropwise adding the precipitant into the precursor solution at a constant speed, dropwise adding the precursor solution into the precipitant at a constant speed, or dropwise adding the precursor solution and the precipitant at a constant speed simultaneously; the dropping speed is 0.2-12 mL/min.

In another preferred embodiment, the surfactant is selected from one or two or more of the following: dodecylbenzene sulfonic acid, sodium dodecylbenzene sulfonate, hexadecyl trimethyl ammonium bromide, sodium succinic acid (-2-ethyl) hexyl ester sulfonate, sodium linoleate, oleic acid, polyethylene glycol, tween-80 and polyoxyethylene-polyoxypropylene-polyoxyethylene (P123).

In another preferred embodiment, the precipitating agent is selected from one or more than two of the following: sodium carbonate, potassium carbonate, sodium bicarbonate, potassium bicarbonate, sodium hydroxide, potassium hydroxide, ammonia, and ammonium hydroxide.

In a second aspect of the present invention, there is provided a catalyst prepared by the preparation method provided by the present invention as described above, the catalyst comprising the following metal oxides, based on the total weight of the catalyst:

40-80 wt% iron oxide

15-40 wt% of a second metal oxide

0% -35% of other metal oxides;

The second metal is selected from one or more than two of the following metals: nickel, copper, manganese, vanadium, zinc, cobalt, molybdenum and niobium;

The other metal is selected from one or more than two of the following metals: chromium, cerium, lanthanum, zirconium, sodium, indium, tin or potassium.

In another preferred embodiment, the specific surface area of the catalyst is 30-500m²/g。

In a third aspect of the present invention, there is provided a use of the catalyst provided by the present invention as described above in the direct preparation of low carbon α -olefins from synthesis gas.

In another preferred embodiment, the synthesis gas is CO to H in a molar ratio₂1 (0.5-5) of CO and H₂The selectivity of the long-chain alkane with 5 to 20 carbon atoms in the molecule in the total product is 2.0 to 10.0 percent.

In a fourth aspect of the present invention, there is provided a method for directly producing low-carbon α -olefins from synthesis gas, the method comprising the steps of:

(i) At the temperature of 200 ℃ and 500 ℃ and under the pressure of 0-5.0MPa, the molar ratio of CO to H is used₂CO/H of 1 (0.5-5)₂Mixed gas of H₂Or carrying out in-situ reduction treatment on the catalyst of claim 6 or 7 in a CO atmosphere for 5-50 hours; and

(ii) the synthesis gas is reacted through a reactor filled with the catalyst reduced in the step (i), the reaction temperature T is more than or equal to 200 ℃ and less than or equal to 500 ℃, the reaction pressure P is more than or equal to 0.5MP and less than or equal to 5MPa, and the reaction space velocity GHSV is 800h^-1≤GHSV≤30000h^-1(ii) a Reactor with a reactor shellAnd C2-C8 alpha-olefin products are obtained by collection at an outlet.

Therefore, the invention provides the method for preparing the Fischer-Tropsch synthesis Fe catalyst with simple process, and the prepared catalyst has the advantages of good alpha-olefin selectivity and the like.

Drawings

FIG. 1 shows the stability test results (activation temperature 350 ℃, activation time 5H, reaction pressure 2.0MPa, molar composition of raw material gas: CO/H) of catalyst sample C-1(Fe-Co-La) obtained in example₂/N₂45/45/10, volume space velocity 12000h^-1)。

FIG. 2 is a perspective electron microscope image of catalyst samples C-2(Fe-Co-K) and C-3(Fe-Cu-Zr) obtained in the example; wherein (a) is Fe-Co-K and (b) is Fe-Cu-Zr.

Detailed Description

The inventor of the invention has extensively studied, prepared the low carbon olefin catalyst by using a new preparation method of low-temperature precipitation method, through mixing precipitant and metal salt organic solution drop by drop, make metal nucleate slowly in organic solvent, grow rapidly and split, get the stable crystalline form with specific structure after aging, while improving the catalyst physical and chemical properties, also produced the influence on the interaction and reduction performance of active ingredient and metal auxiliary agent.

Preparation method

The invention provides a preparation method of a catalyst for directly preparing alpha-olefin from synthesis gas, which comprises the following steps:

step one, preparing a precursor solution of a catalyst: mixing an organic mixed solution containing iron ions and metal ions such as nickel, copper, manganese, vanadium, zinc, cobalt, molybdenum, niobium, chromium, cerium, lanthanum, zirconium, sodium, indium, tin, potassium and the like with a proper amount of surfactant, and placing at a low temperature to form a precursor solution of the catalyst;

secondly, mixing a precursor solution of the catalyst with a precipitator solution at a low temperature to obtain a precipitate;

And thirdly, carrying out solid-liquid separation, washing, drying and roasting on the precipitate to obtain the catalyst for preparing the alpha-olefin from the synthesis gas.

In the first step, the organic mixed solution contains Fe²⁺，Fe³⁺And Ni²⁺，V⁵⁺，Zn²⁺，Mo⁶⁺，Nb^{5 +}，Cr³⁺，Ce⁴⁺，La³⁺，Zr⁴⁺，Na⁺，In³⁺，K⁺，SO₄ ^2-，Cl^-，NO₃ ^-，Co²⁺，Sn⁴⁺，Mn²⁺，Cu²⁺and one or more ions.

In one embodiment of the invention, Fe is used²⁺And Co²⁺an organic mixed solution; the concentration of iron and cobalt salts is 0.001-0.1mol/L, preferably 0.01-0.05mol/L, and more preferably the concentration of cobalt salts is one third to one fifth of the concentration of iron salts.

The organic solvent for forming the organic mixed solution in the first step is selected from C_1-10One or more of alcohols, toluene, xylene, chloroform, acetone, ethylenediamine, triethylamine, triethanolamine, polyether, polyvinyl alcohol, cyclohexane, carbon disulfide and carbon tetrachloride; preferably one or more of methanol, ethanol, ethylene glycol, glycerol, n-propanol, isopropanol, n-butanol, isobutanol and pentanol; more preferably C_2-3Alcohols such as, but not limited to, one or more of ethanol, ethylene glycol, glycerol, n-propanol, and isopropanol.

In one embodiment of the present invention, the organic mixed solution is obtained by mixing an iron source and a second metal source having metal ions such as nickel, copper, manganese, vanadium, zinc, cobalt, molybdenum, niobium, chromium, cerium, lanthanum, zirconium, sodium, indium, tin, potassium, etc. with an organic solvent, and then stirring and mixing them uniformly at a rotation speed of 400-; preferably at 400 and 600 rpm.

In an embodiment of the invention, in the first step, after the surfactant is added to the organic mixed solution, the organic mixed solution is placed in an environment with a temperature of-30 ℃ to 30 ℃ and is kept stand to form a precursor solution; preferably from-30 ℃ to-5 ℃; more preferably from-20 ℃ to-5 ℃. The surfactant is one or more of dodecylbenzene sulfonic acid, sodium dodecylbenzene sulfonate, hexadecyl trimethyl ammonium bromide, sodium sulfosuccinate (-2-ethyl) hexyl ester sulfonate, sodium linoleate, oleic acid, polyethylene glycol, tween-80 and polyoxyethylene-polyoxypropylene-polyoxyethylene (P123). Preferably dodecylbenzene sulfonic acid, cetyltrimethylammonium bromide, sodium (-2-ethyl) hexyl succinate sulfonate and sodium linoleate, preferably in an amount of 1.2g to 1.4 g. The organic solvent assisted by the surfactant is utilized to control the growth and the splitting of crystal nuclei, and the metal dispersity is improved, so that the structure of the catalyst is controlled, the specific surface area is optimized, and the activity selectivity of the catalyst is improved.

In one embodiment of the present invention, the second step is to mix the precursor solution obtained in the first step with a precipitating agent drop by drop to precipitate metal salt ions uniformly, and the precipitate is aged for 1-10 hours continuously and placed in an inert gas atmosphere in the whole process; the inert gas may be N₂One or a combination of several of Ar and He, and gas capable of isolating air can also be used. The mixing mode can be (1) positive addition: adding a precipitant to the salt solution; (2) and (3) reverse addition: adding a salt solution to a precipitating agent; (3) parallel flow feeding: the salt solution and the precipitant are added simultaneously. The environment of dropwise mixing is that the pH value is 3-12, preferably 3-5, and the temperature is minus 30 ℃ to 30 ℃; preferably from-30 ℃ to-5 ℃; more preferably from-20 ℃ to-5 ℃. The key to drop-wise mixing is the uniform rate, e.g., maintaining a rate of 0.2-12mL/min, and drop-wise mixing can be performed using a constant rate syringe pump, such as, but not limited to, a single channel constant rate syringe pump, a dual channel constant rate syringe pump, a combination syringe pump, an intravenous syringe pump, and the like.

In one embodiment of the present invention, the second step is to mix the precursor solution obtained in the first step with a precipitant drop by drop.

the precipitant in the second step can be one or more of sodium carbonate, potassium carbonate, sodium bicarbonate, potassium bicarbonate, sodium hydroxide, potassium hydroxide, ammonia water and ammonium hydroxide; carbonates are preferred.

In the second step, the concentration of the precipitant is 0.1 to 1mol/L, preferably 0.2 to 0.5 mol/L.

in one embodiment of the present invention, the catalyst precursor solution and the precipitant solution are mixed in the second step using a stirrer (such as, but not limited to, a magnetic stirrer, a flap stirrer, a mobile stirrer, a turbine stirrer, etc.), wherein the length of the rotor is 2-6cm, preferably 3-4cm, and the rotation speed is in the range of 400-.

The low temperature environment (e.g., 30 ℃ C. to 30 ℃ C.) in the first and second steps described above can be obtained by conventional means in the art, such as, but not limited to, a cryogenic tank, which can be a vertical cryogenic water bath, a vertical cryogenic oil bath, a horizontal cryogenic water bath, a horizontal cryogenic oil bath, and the like.

The solid-liquid separation in the third step may be one of suction filtration, filter pressing and centrifugation.

In one embodiment of the invention, the total time for solid-liquid separation and washing is not less than 1 hour, ensuring that the filtrate is washed to a pH of 5 to 7.

And in the third step, a vacuum oven is selected to dry the sample, the drying time is 24-48 hours, the temperature range is 40-120 ℃, after the drying is finished, the sample needs to be ground and then is put into a muffle furnace to be roasted, the roasting temperature is 800 ℃ for 300-. In one embodiment of the present invention, the dried sample is immersed in an aqueous solution containing other elements and then calcined; the aqueous solution containing other elements is an aqueous solution of a source of the other elements; the other element source is selected from one or more than two of the following: sulfates, carbonates, nitrates and chlorides of chromium, cerium, lanthanum, zirconium, sodium, indium, tin, potassium.

In one embodiment of the present invention, the grinding process in the third step is 40 to 300 mesh, and the grinding apparatus includes: one of a ball mill, an edge runner mill and a vibration mill; the ball milling medium is one or a mixture of several of ceramics, corundum, agate, stainless steel, tungsten nitride, tungsten carbide, tungsten oxide and silicon carbide.

In a preferred embodiment of the present invention, a powder mill, such as but not limited to, a dry mill, a hand mill or a mechanical mill, is used.

Catalyst and process for preparing same

Adopt toThe catalyst for preparing low-carbon alpha-olefin from synthesis gas, which is prepared by the preparation method, takes Fe as an active component and takes elements such as nickel, copper, manganese, vanadium, zinc, cobalt, molybdenum, niobium, chromium, cerium, lanthanum, zirconium, sodium, indium, tin, potassium and the like as auxiliaries, wherein the percentage content of Fe in the catalyst is 40-80%, and the percentage content of the auxiliaries is 20-60%. The specific surface area of the catalyst is 30-500m²In g, e.g. 40 to 500m²/g、60-500m²/g、70-500m²/g、100-500m²/g、130-500m²/g、30-300m²/g、40-300m²/g、60-300m²/g、70-300m²/g、100-300m²/g、130-300m²/g、30-250m²/g、40-250m²/g、60-250m²/g、70-250m²/g、100-250m²/g、130-250m²/g、30-200m²/g、40-200m²/g、60-200m²/g、70-200m²/g、100-200m²/g、130-200m²/g、30-150m²/g、40-1500m²/g、60-150m²/g、70-150m²/g、100-150m²/g、130-150m²and/g, etc.

In one embodiment of the invention, the catalyst for directly preparing low-carbon alpha-olefin from synthesis gas comprises iron oxide and other metal oxides (nickel, copper, manganese, vanadium, zinc, cobalt, molybdenum, niobium, chromium, cerium, lanthanum, zirconium, sodium, indium, tin, potassium and the like); based on the total weight of the catalyst, wherein,

40 to 80 percent of iron oxide

15-40% of second metal oxide (nickel, copper, manganese, vanadium, zinc, cobalt, molybdenum, niobium, etc.)

0-35% of other metal oxides (chromium, cerium, lanthanum, zirconium, sodium, indium, tin, potassium and the like).

In one embodiment of the invention, the other metal oxide content is < 1%, such as 0.2%, 0.5%, 0.8%, etc.

in one embodiment of the present invention, the amount of the organic solvent used to form the organic mixed solution in the first step of the preparation method is 15 times the total mass of the raw materials.

Use of

The catalyst for preparing the low-carbon alpha-olefin from the synthesis gas, which is prepared by the preparation method provided by the invention, can be used for directly preparing the low-carbon alpha-olefin from the synthesis gas, and the application method comprises the following steps:

(1) At the temperature of 200 ℃ and 500 ℃ and under the pressure of 0-5.0MPa, the molar ratio of CO to H is used₂CO/H of 1 (0.5-5)₂mixed gas of H₂Or carrying out in-situ reduction treatment on the catalyst in CO atmosphere for 5-50 h;

(2) Reacting the synthesis gas through a reactor filled with the catalyst reduced in the step (1), wherein the reaction temperature T is more than or equal to 200 ℃ and less than or equal to 500 ℃, the reaction pressure P is more than or equal to 0.5MP and less than or equal to 5MPa, and the reaction space velocity GHSV is 800h^-1≤GHSV≤30000h^-1(ii) a The product of C2-C8 alpha-olefin is collected at the outlet of the reactor.

Wherein, the selectivity of long-chain alkane with 5-20 carbon atoms in the molecule in the total product is 2.0-10.0 percent, and the synthesis gas is CO to H in molar ratio₂1 (0.5-5) of CO and H₂the mixed gas of (1).

The features mentioned above with reference to the invention, or the features mentioned with reference to the embodiments, can be combined arbitrarily. All the features disclosed in this specification may be combined in any combination, and each feature disclosed in this specification may be replaced by alternative features serving the same, equivalent or similar purpose. Thus, unless expressly stated otherwise, the features disclosed are merely generic examples of equivalent or similar features.

The main advantages of the invention are:

the invention provides a method for directly preparing low-carbon olefin and co-producing C by Fe-based synthesis gas₄-C₈The alpha-olefin catalyst has the advantages of high stability of long-period operation activity, good alpha-olefin selectivity, simple preparation process, easily obtained raw materials and the like, and is favorable for process application and popularization.

The invention will be further illustrated with reference to the following specific examples. It should be understood that these examples are for illustrative purposes only and are not intended to limit the scope of the present invention. The experimental procedures, in which specific conditions are not noted in the following examples, are generally carried out according to conventional conditions or according to conditions recommended by the manufacturers. All percentages, ratios, proportions, or parts are by weight unless otherwise specified. The weight volume percentage units in the present invention are well known to those skilled in the art and refer to, for example, the weight of solute in a 100ml solution. Unless defined otherwise, all technical and scientific terms used herein have the same meaning as commonly understood by one of ordinary skill in the art. In addition, any methods and materials similar or equivalent to those described herein can be used in the methods of the present invention. The preferred embodiments and materials described herein are intended to be exemplary only.

The following methods were used in the following examples for correlation detection:

1. Evaluation of catalyst Performance:

And (3) carrying out quantitative analysis on the reaction product of directly preparing the low-carbon olefin from the synthesis gas by adopting an online gas chromatography.

and (3) chromatography: fuli GC9790II

FID column chromatography: HP-PLOT-Q19091P-Q04, 30mx0.32mm (inside diameter), 20um film thickness

Carrier gas: argon, 2ml/min

temperature of the column box: keeping at 60 deg.C for 5min

60℃-220℃，10℃/min

Keeping the temperature of 220-220 ℃ for 5min

A detector: FID; temperature: 300 deg.C

TCD column: carbon molecular sieve column, TDX-012 m x 2mm (internal diameter)

carrier gas: argon, 23ml/min

temperature of the column box: 50-150 ℃ and 30 ℃/min

keeping at 150 deg.C for 5min

150℃-270℃，20℃/min

maintaining at 270 deg.C for 20min

A sample inlet: the isolation pad sweeps a sample inlet: the temperature is 250 DEG C

A detector: TCD; temperature: 100 deg.C

2. Catalyst Process parameters (processing Capacity)

Hair brushThe space velocity of the reaction volume is defined as the volume of feed gas (dry basis) entering the reaction system treated per hour per unit volume of catalyst, expressed as GHSV in units of h^-1。

3. The application of the catalyst comprises the following steps:

The catalyst samples in the examples were each 100mg placed in a constant temperature zone of a fixed bed reactor. Before reaction, the catalyst is reduced on line at 350 deg.C and normal pressure in the presence of 5% H reducing gas₂and/Ar, the reduction time is 5 h. After the reduction is finished, the temperature controller and the back pressure valve are adjusted to ensure that the reaction temperature and the reaction pressure are respectively 300 ℃ and 2.0MPa, and the airspeed of the reaction gas is set to be 12000h^-1The reaction was started when the temperature and pressure were stable. The product was analyzed on-line and sampled every hour.