CN110961096B

CN110961096B - Fischer-Tropsch synthesis catalyst and preparation method and application thereof

Info

Publication number: CN110961096B
Application number: CN201811160636.7A
Authority: CN
Inventors: 侯朝鹏; 徐润; 孙霞; 李学锋; 吕庐峰; 夏国富; 吴玉; 张哲民; 李明丰
Original assignee: Sinopec Research Institute of Petroleum Processing; China Petroleum and Chemical Corp
Current assignee: Sinopec Research Institute of Petroleum Processing; China Petroleum and Chemical Corp
Priority date: 2018-09-30
Filing date: 2018-09-30
Publication date: 2022-09-27
Anticipated expiration: 2038-09-30
Also published as: CN110961096A

Abstract

The invention relates to a Fischer-Tropsch synthesis catalyst and a preparation method and application thereof, wherein the method comprises the following steps: loading an active metal component on the surface of a catalytic carrier; wherein the roundness value range E of the catalytic carrier is set to 0.15 to 0.95. The Fischer-Tropsch synthesis catalyst provided by the invention has high CO conversion rate, C5+ hydrocarbon selectivity and low methane selectivity when being used for carrying out Fischer-Tropsch synthesis reaction.

Description

Fischer-Tropsch synthesis catalyst and preparation method and application thereof

Technical Field

The invention relates to a Fischer-Tropsch synthesis catalyst, and a preparation method and application thereof.

Background

In recent years, with the increasing shortage of petroleum resources, the rising price of crude oil, the gradual rigorous requirement on fuel and the increasing exploration of reserves of coal and natural gas, the research in the field of Fischer-Tropsch synthesis is very active, and many companies carry out research and development on Fischer-Tropsch synthesis.

Fischer-tropsch synthesis refers to a reaction in which synthesis gas is converted over a catalyst to produce hydrocarbons, including alkanes, alkenes, and mixed alcohols of various carbon numbers. The Fischer-Tropsch synthesis reaction process releases a large amount of heat, local overheating of the catalyst often occurs, so that the selectivity of methane and low-carbon hydrocarbon is increased, and the catalyst is caused to deposit carbon and even block a bed layer, therefore, the control of the temperature of the bed layer in the reaction process is very important for keeping the activity, stability and selectivity of heavy hydrocarbon of the catalyst, and how to effectively remove the reaction heat is the problem to be considered in the design of the reactor. Therefore, researchers develop different types of synthesis processes, and can be divided into two types of low-temperature and high-temperature synthesis processes according to the operation temperature; according to the reactor form, the method can be divided into a fixed bed process, a fluidized bed process, a slurry bed process and the like, and one of the purposes is to remove reaction heat and ensure that the reaction is smoothly carried out.

The Fischer-Tropsch synthesis reaction is a gas-solid-liquid heterogeneous reaction system, and in a conventional fixed bed reactor, the particle diameter of a catalyst is generally several mm, so that the influence of diffusion control on the catalytic activity is difficult to avoid. The heavy paraffin obtained by Fischer-Tropsch synthesis is usually loaded on the surface of the catalyst in the form of liquid, steam sol or slurry, and reacts on the reactant H ₂ And the diffusion of CO inside the catalyst particles. During the internal diffusion of the reactants, H ₂ Has a diffusion speed higher than that of CO, and the diffusion limiting effect of CO in the catalyst particles is obviously stronger than that of H ₂ . Because the particle sizes of the particles are different, the difference of CO concentration gradient in the particles is caused, the combination of CO and the active center position of the metal is influenced, the H/C ratio adsorbed on the active center is increased, the carbon chain growth probability is reduced, and the selectivity of C5+ hydrocarbon is reduced. An effective way for solving the problem is to optimally design the catalyst, and the regulation and control of the selectivity of the product is also the key point of the Fischer-Tropsch synthesis.

Disclosure of Invention

The invention aims to provide a Fischer-Tropsch synthesis catalyst, and a preparation method and application thereof, and the Fischer-Tropsch synthesis catalyst provided by the invention has high CO conversion rate, C5+ hydrocarbon selectivity and low methane selectivity when in Fischer-Tropsch synthesis reaction.

In order to achieve the above object, the present invention provides a method for preparing a fischer-tropsch synthesis catalyst, comprising:

loading an active metal component on the surface of a catalytic carrier; wherein the circularity value range E of the catalytic carrier is set to 0.15 to 0.95, preferably to 0.25 to 0.90, further preferably to 0.35 to 0.80, still further preferably to 0.45 to 0.75; the method for obtaining the roundness value range E of the catalytic carrier comprises the following steps:

acquiring an image containing the catalytic carrier particles by using a microscope; wherein the magnification of the microscope is 5-300 times;

measuring the numerical values of the minor axis b and the major axis a of all the catalytic carrier particles in the image, and calculating to obtain the roundness value e of each catalytic carrier particle as b/a;

and taking the maximum value and the minimum value of the calculated roundness value E as the endpoint values of the roundness value range E.

Optionally, the surface roughness Rz of the catalytic carrier is set to 0.25 to 25 micrometers, preferably to 0.5 to 20 micrometers, further preferably to 1 to 10 micrometers; the surface roughness Rz of the catalytic carrier is determined by an interferometry.

Optionally, the catalytic carrier is one or a mixture or a composite of more of alumina, silica-alumina, aluminum silicate, silica, titania and zirconia.

Characterized by mercury intrusion method, the pore volume of the catalytic carrier is 0.2-3 ml/g, and the specific surface area is 60-400 m ² Per gram, the proportion of the pore volume of pores with the diameter of 2-30 nanometers in the total pore volume is more than 30 percent by volume; it is preferable that the catalytic carrier has a pore volume of 0.3 to 1.5 ml/g and a specific surface area of 100-300 m ² Per gram, the proportion of the pore volume of pores with the diameter of 2-30 nanometers in the total pore volume is more than 50 percent；

The catalytic carrier is formed by at least one forming mode selected from spray forming, rolling ball forming, dropping ball forming, tabletting forming and strip extrusion forming;

the particle size d of the catalytic carrier meets the following condition: d is 0.10 μm or less and 1000 μm or less, preferably 1.0 μm or less and 750 μm or less, more preferably 10 μm or less and 500 μm or less, still more preferably 20 μm or less and 300 μm or less, and still more preferably 50 μm or less and 200 μm or less, the particle size being measured by a microscopic image method.

Optionally, the active metal component comprises at least one selected from cobalt, iron and ruthenium.

Optionally, if the active metal component comprises cobalt, the content of cobalt in the catalyst is 5 to 80 wt%, preferably 10 to 70 wt%, and more preferably 20 to 60 wt%, calculated as element and based on the weight of the catalyst on a dry basis;

if the active metal component comprises iron, the amount of iron in the catalyst is from 5 to 80 wt.%, preferably from 10 to 70 wt.%, and more preferably from 20 to 60 wt.%, calculated as element and based on the weight of the catalyst on a dry basis;

if the active metal component comprises ruthenium, the ruthenium content of the catalyst is from 0.1 to 20% by weight, preferably from 0.5 to 10% by weight, calculated as oxide and based on the weight of the catalyst on a dry basis.

Optionally, the catalyst also contains an auxiliary agent;

if the active metal component is cobalt, the promoter is at least one selected from the group consisting of non-noble metals, rare earth oxides and noble metals, the non-noble metals are at least one selected from the group consisting of Cu, Mo, Ta, W, Ru, Zr, Ti, Re, Hf, La, Ce, Mn and V, preferably at least one selected from the group consisting of W, Zr, Re, Ru and Ce, and the noble metals are at least one selected from the group consisting of Pt, Pd, Rh, Ir, Re, Au and Ag; if the auxiliary agent is at least one selected from non-noble metals and rare earth oxides, the content of the auxiliary agent is less than 30 wt%, preferably less than 20 wt%, and more preferably less than 15 wt% in terms of oxides and based on the dry weight of the catalyst; if the auxiliary is at least one selected from noble metals, the content of the auxiliary is 10 wt% or less, more preferably 1 wt% or less, in terms of metal and based on the dry weight of the catalyst;

if the active metal component is iron, the promoter is at least one selected from the group consisting of Ti, V, Cr, Mn, Co, Ni, Cu, Zn, Zr, Nb, Mo, W, Ce, Ru, Re, La, Li, Mg, K and Ca, preferably at least one selected from the group consisting of Mn, Cu, W, Zr, Re and Ru; the content of the auxiliary agent is 30 wt% or less, preferably 20 wt% or less, and more preferably 15 wt% or less, in terms of oxide and based on the dry weight of the catalyst;

if the active metal component is ruthenium, the auxiliary agent is at least one selected from non-noble metals, rare earth oxides and noble metals, the non-noble metals are at least one selected from Li, K, Mg, Ca, Cu, Mo, Ta, Cr, W, Zr, Ti, Re, Hf, Ce, Mn, V, Si and Pr, and the noble metals are at least one selected from Pt, Pd, Rh, Ir, Re, Au and Ag; if the auxiliary agent is at least one selected from non-noble metals and rare earth oxides, the content of the auxiliary agent is preferably 30 wt% or less, more preferably 20 wt% or less, and even more preferably 15 wt% or less, calculated as the oxide and based on the dry weight of the catalyst; when the auxiliary is at least one selected from noble metals, the content of the auxiliary is 10% by weight or less, more preferably 1% by weight or less, in terms of metal and based on the dry weight of the catalyst.

The invention also provides a Fischer-Tropsch synthesis catalyst, which comprises a catalytic carrier and an active metal component loaded on the surface of the catalytic carrier; wherein the circularity value range E of the catalytic carrier is set to 0.15 to 0.95, preferably to 0.25 to 0.90, further preferably to 0.35 to 0.80, still further preferably to 0.45 to 0.75; the method for obtaining the roundness value range E of the catalytic carrier comprises the following steps:

acquiring an image containing catalytic carrier particles by using a microscope; wherein the magnification of the microscope is 5-300 times;

Optionally, the surface roughness Rz of the catalytic carrier is set to 0.25 to 25 micrometers, preferably to 0.5 to 20 micrometers, further preferably to 1 to 10 micrometers; the surface roughness Rz of the catalytic carrier is measured by interferometry.

Optionally, the catalytic carrier is one or a mixture or a compound of more of alumina, silica-alumina, aluminum silicate, silica, titania and zirconia;

characterized by mercury intrusion method, the pore volume of the catalytic carrier is 0.2-3 ml/g, and the specific surface area is 60-400 m ² Per gram, the proportion of the pore volume of pores with the diameter of 2-30 nanometers in the total pore volume is more than 30 percent by volume; it is preferable that the catalytic carrier has a pore volume of 0.3 to 1.5 ml/g and a specific surface area of 100-300 m ² Per gram, the proportion of the pore volume of pores with the diameter of 2-30 nanometers in the total pore volume is more than 50 percent by volume;

the catalytic carrier is formed by at least one forming mode selected from spray forming, rolling ball forming, dropping ball forming, tabletting forming and extrusion molding;

the particle size d of the catalytic carrier meets the following condition: d is 0.10 μm or less and 1000 μm or less, preferably 1.0 μm or less and 750 μm or less, more preferably 10 μm or less and 500 μm or less, more preferably 20 μm or less and 300 μm or less, and still more preferably 50 μm or less and 200 μm or less, the particle size being measured by a microscopic image method.

if the active metal component comprises iron, the amount of iron in the catalyst is from 5 to 80 wt%, preferably from 10 to 70 wt%, more preferably from 20 to 60 wt%, calculated as element and based on the weight of the catalyst on a dry basis;

Optionally, the catalyst also contains an auxiliary agent;

if the active metal component is cobalt, the promoter is at least one selected from the group consisting of non-noble metals, rare earth oxides and noble metals, the non-noble metals being at least one selected from the group consisting of Cu, Mo, Ta, W, Ru, Zr, Ti, Re, Hf, La, Ce, Mn and V, preferably at least one selected from the group consisting of W, Zr, Re, Ru and Ce, the noble metals being at least one selected from the group consisting of Pt, Pd, Rh, Ir, Re, Au and Ag; if the auxiliary agent is at least one selected from non-noble metals and rare earth oxides, the content of the auxiliary agent is less than 30 wt%, preferably less than 20 wt%, and more preferably less than 15 wt% in terms of oxides and based on the dry weight of the catalyst; if the auxiliary is at least one selected from noble metals, the content of the auxiliary is 10 wt% or less, more preferably 1 wt% or less, in terms of metal and based on the dry weight of the catalyst;

if the active metal component is ruthenium, the auxiliary agent is at least one selected from non-noble metals, rare earth oxides and noble metals, the non-noble metals are at least one selected from Li, K, Mg, Ca, Cu, Mo, Ta, Cr, W, Zr, Ti, Re, Hf, Ce, Mn, V, Si and Pr, and the noble metals are at least one selected from Pt, Pd, Rh, Ir, Re, Au and Ag; if the auxiliary agent is at least one selected from non-noble metals and rare earth oxides, the content of the auxiliary agent is preferably 30 wt% or less, more preferably 20 wt% or less, and even more preferably 15 wt% or less, calculated as the oxide and based on the dry weight of the catalyst; when the auxiliary is at least one selected from noble metals, the content of the auxiliary is 10 wt% or less, more preferably 1 wt% or less, in terms of metal and based on the dry weight of the catalyst.

The invention also provides a Fischer-Tropsch synthesis process, which comprises the following steps: the hydrogen and carbon monoxide are contacted with the catalyst provided by the invention in a reactor and the Fischer-Tropsch synthesis reaction is carried out.

Optionally, the reactor is a microchannel reactor and/or a fixed bed reactor, preferably a microchannel reactor.

The Fischer-Tropsch synthesis catalyst adopts a carrier with a small circle value, enlarges the diffusion area and diffusion flux of reactants and products on the catalyst, shortens the diffusion distance, improves the reaction diffusion surface area of the catalyst with equal weight, reduces the influence of a wax film generated by the reaction on the coverage of the catalyst, improves the activity, selectivity and reaction rate of the catalyst, has high CO conversion rate, C5+ hydrocarbon selectivity and low methane selectivity, and is particularly suitable for a fixed bed and a microchannel reactor.

Additional features and advantages of the invention will be set forth in the detailed description which follows.

Drawings

The accompanying drawings, which are included to provide a further understanding of the invention and are incorporated in and constitute a part of this specification, illustrate embodiments of the invention and together with the description serve to explain the principles of the invention and not to limit the invention. In the drawings:

FIGS. 1-2 are photomicrographs of selected supports DB1-DB2 of comparative examples 1-2 of the present invention.

FIGS. 3-6 are photomicrographs of selected vectors Z1-Z4 of examples 1-4 of the present invention.

Detailed Description

The following detailed description of embodiments of the invention refers to the accompanying drawings. It should be understood that the detailed description and specific examples, while indicating the present invention, are given by way of illustration and explanation only, not limitation.

Unless otherwise specified, the dry basis weight in the present invention refers to the result measured after the sample is calcined at 650 ℃ for 3 hours.

The invention provides a preparation method of a Fischer-Tropsch synthesis catalyst, which comprises the following steps: loading an active metal component on the surface of a catalytic carrier; wherein the roundness value range E of the catalytic carrier is set to 0.15 to 0.95, preferably to 0.25 to 0.90, further preferably to 0.35 to 0.80, still further preferably to 0.45 to 0.75; the method for obtaining the roundness value range E of the catalytic carrier comprises the following steps:

In the above-mentioned obtaining step, the image should include at least two particles, preferably 2-100, and more preferably 5-50, and the particles preferably do not occlude each other, and if there is an occluded particle, it is not necessary to calculate the circularity value of the particle.

In addition, the roundness value of the catalyst carrier is not as small as possible, and if it is too small, the fluidity of the catalyst is lowered, and the filling of the catalyst is affected, thereby causing a bridging phenomenon.

The invention also provides a Fischer-Tropsch synthesis catalyst, which comprises a catalytic carrier and an active metal component loaded on the surface of the catalytic carrier; wherein the roundness value range E of the catalytic carrier is set to 0.15 to 0.95, preferably to 0.25 to 0.90, further preferably to 0.35 to 0.80, still further preferably to 0.45 to 0.75; the roundness value range E of the catalytic carrier is obtained by the following steps:

According to the present invention, the circularity value is used to characterize the proximity of the support particles to a spherical shape, and for convenience of characterization, the circularity value is instead characterized by the circularity used in the image processing, and when e is 1, the single catalytic support particle in the above image is circular, and the smaller e, the more the above particle deviates from the spherical shape. Microscopes are well known to those skilled in the art, and the present invention employs a trinocular stereo microscope, model XTZ-CT, manufactured by Shanghai optical instruments, with circularity measurements made using the microscope particle size analysis software UV-G.

According to the present invention, the surface roughness Rz of the catalytic carrier may be set to 0.25 to 25 micrometers, preferably to 0.5 to 20 micrometers, further preferably to 1 to 10 micrometers; the surface roughness Rz of the catalytic carrier is determined by an interferometry. The interference method utilizes the principle of light wave interference to display the shape error of the measured surface as an interference fringe pattern, and utilizes a microscope with high magnification to amplify and measure the microscopic parts of the interference fringes so as to obtain the roughness of the measured surface. The surface roughness Rz can also be called as the maximum height of the profile, which means the height of the sum of the maximum profile peak height (Zp) and the maximum profile valley depth (Zv) in one sampling length of the carrier particles, and the average value can be calculated by sampling for multiple times.

According to the invention, the roundness value is used for representing the integral appearance of the carrier, the surface roughness is used for representing the microscopic appearance of the surface of the carrier, and the carrier of the catalyst meets the roundness value parameter, preferably meets the roundness value and the surface roughness parameter, so that the catalyst has better catalytic effect.

The catalyst carrier can be prepared by the existing method or the commercial method, as long as the roundness value range E, or the roundness value range E and the surface roughness Rz meet the ranges and are suitable for preparing the Fischer-Tropsch synthesis catalyst, for example, one or more carriers can be obtained firstly, then the roundness value range E, or the roundness value range E and the surface roughness Rz of each carrier are measured, and if the roundness value range E, or the roundness value range E and the surface roughness Rz of a certain carrier meet the ranges, the carrier is used as the catalyst carrier. The method can quickly screen out the catalytic carrier, and conveniently control the quality of the catalyst prepared by carriers of different batches.

According to the invention, the catalytic support can be a support of various materials, for example a mixture or composite of one or more of the above-mentioned materials selected from alumina, silica-alumina, aluminium silicate, silica, titania and zirconia, preferably alumina. The invention is also not particularly restricted with respect to other parameters of the catalytic support, for example characterized by mercury intrusion, which may have a pore volume of from 0.2 to 3 ml/g and a specific surface area of from 60 to 400 m ² Per gram, the proportion of the pore volume of pores with the diameter of 2-30 nanometers in the total pore volume can be more than 30 percent by volume; preferably, the catalytic carrier may have a pore volume of 0.3 to 1.5 ml/g and a specific surface area of 100-300 m ² The proportion of pore volume per gram of pores with diameters of 2 to 30 nanometers in relation to the total pore volume may be greater than 50% by volume.

According to the present invention, the catalytic carrier is a particle type carrier having a specific shape, such as a micro sphere, a pellet, etc., and can be molded by a conventional method, such as at least one molding means selected from spray molding, roll ball molding, drop ball molding, tablet molding and bar extrusion molding. In the molding, for example, extrusion molding, in order to ensure that the molding is performed smoothly, water, an extrusion aid and/or an adhesive, with or without a pore-expanding agent, may be added to the catalytic carrier or the precursor of the catalytic carrier, followed by extrusion molding, followed by drying and calcination. The kinds and amounts of the extrusion aid, peptizing agent and pore-expanding agent are known to those skilled in the art, for example, the common extrusion aid can be one or more selected from sesbania powder, methyl cellulose, starch, polyvinyl alcohol and polyvinyl alcohol, the peptizing agent can be inorganic acid and/or organic acid, the pore-enlarging agent can be one or more of starch, synthetic cellulose, polymeric alcohol and surfactant, the synthetic cellulose is preferably one or more of hydroxymethyl cellulose, methyl cellulose, ethyl cellulose and hydroxy fiber fatty alcohol polyvinyl ether, the polymer alcohol is preferably one or more of polyethylene glycol, polypropylene alcohol and polyvinyl alcohol, and the surfactant is preferably one or more of fatty alcohol polyvinyl ether, fatty alcohol amide and derivatives thereof, an allyl alcohol copolymer with molecular weight of 200-10000 and a maleic acid copolymer. After the molding kneading, the mixture is crushed and sieved by a crusher into corresponding particle sizes. Drying and calcining are well known to those skilled in the art, for example, the drying conditions may include: the temperature is 40-300 ℃ and the time is 1-24 hours, and the roasting condition can comprise: the temperature is more than 500 to less than or equal to 1200 ℃, and the time is 1 to 8 hours. Preferred drying conditions include: the temperature is 100-200 ℃ and the time is 2-12 hours, and the preferable roasting conditions comprise: the temperature is more than 600 ℃ and less than or equal to 1000 ℃, and the roasting time is 2-6 hours.

According to the invention, the sizes of the catalytic carriers molded by different molding modes can be different, for example, the particle diameter d of the catalytic carrier can satisfy the following conditions: 0.10 μm. ltoreq. d.ltoreq.1000. mu.m, preferably 1.0 μm. ltoreq. d.ltoreq.750. mu.m, more preferably 10 μm. ltoreq. d.ltoreq.500. mu.m, more preferably 20 μm. ltoreq. d.ltoreq.300. mu.m, still more preferably 50 μm. ltoreq. d.ltoreq.200. mu.m, the particle size of the catalytic carrier being controllable by sieving. The particle size is measured by a microscopic image method, and equipment adopted by the microscopic image method can be composed of a microscope, a CCD camera (or a digital camera), a graphic acquisition card, a computer and the like. The basic working principle of the method is that particle images amplified by a microscope are transmitted to a computer through a CCD camera and a graphic acquisition card, the computer carries out edge recognition and other processing on the images, the particle size of each particle is obtained according to the equivalent projection area principle, and then the particle size distribution range can be obtained. Because the number of particles measured by the method at a single time is less, the authenticity and the universality of the test result can be improved by carrying out multiple measurements on the same sample by a method of changing the view field. The invention adopts a three-eye stereomicroscope produced by Shanghai optical instrument six factories, and the model is XTZ-CT. Particle size measurements were made using the microscope particle size analysis software UV-G.

According to the present invention, the active metal component is well known to those skilled in the art and mainly functions to provide a catalytically active site, for example, the active metal component may comprise at least one selected from cobalt, iron and ruthenium, wherein if the active metal component comprises cobalt, the amount of cobalt in the catalyst may be 5 to 80 wt%, preferably 10 to 70 wt%, and more preferably 20 to 60 wt%, calculated as the element and based on the weight of the catalyst on a dry basis; if the active metal component comprises iron, the amount of iron in the catalyst may be from 5 to 80 wt%, preferably from 10 to 70 wt%, more preferably from 20 to 60 wt%, calculated as element and based on the weight of the catalyst on a dry basis; if the active metal component comprises ruthenium, the ruthenium content of the catalyst may be from 0.1 to 20% by weight, preferably from 0.5 to 10% by weight, calculated as oxide and based on the weight of the catalyst on a dry basis.

According to the invention, the catalyst may contain, in addition to the active metal component, an auxiliary; auxiliaries are well known to those skilled in the art and are not described in detail here. For example, if the active metal component is cobalt, the promoter may be at least one selected from the group consisting of non-noble metals, rare earth oxides, and noble metals, the non-noble metals may be at least one selected from the group consisting of Cu, Mo, Ta, W, Ru, Zr, Ti, Re, Hf, La, Ce, Mn, and V, preferably at least one selected from the group consisting of W, Zr, Re, Ru, and Ce, and the noble metals may be at least one selected from the group consisting of Pt, Pd, Rh, Ir, Re, Au, and Ag; if the promoter is at least one selected from non-noble metals and rare earth oxides, the content of the promoter may be 30 wt% or less, preferably 20 wt% or less, and more preferably 15 wt% or less, based on the oxides and based on the dry weight of the catalyst; when the auxiliary is at least one selected from noble metals, the content of the auxiliary may be 10 wt% or less, more preferably 1 wt% or less, in terms of metal and based on the dry weight of the catalyst. If the active metal component is iron, the promoter may be at least one selected from the group consisting of Ti, V, Cr, Mn, Co, Ni, Cu, Zn, Zr, Nb, Mo, W, Ce, Ru, Re, La, Li, Mg, K and Ca, preferably at least one selected from the group consisting of Mn, Cu, W, Zr, Re and Ru; the content of the auxiliary may be 30% by weight or less, preferably 20% by weight or less, and more preferably 15% by weight or less, in terms of oxide, based on the dry weight of the catalyst. If the active metal component is ruthenium, the promoter may be at least one selected from non-noble metals, rare earth oxides, and noble metals, the non-noble metals may be at least one selected from Li, K, Mg, Ca, Cu, Mo, Ta, Cr, W, Zr, Ti, Re, Hf, Ce, Mn, V, Si, and Pr, and the noble metals may be at least one selected from Pt, Pd, Rh, Ir, Re, Au, and Ag; if the auxiliary agent is at least one selected from non-noble metals and rare earth oxides, the content of the auxiliary agent is preferably 30 wt% or less, more preferably 20 wt% or less, and even more preferably 15 wt% or less, calculated as the oxide and based on the dry weight of the catalyst; if the promoter is at least one selected from the group consisting of noble metals, the content of the promoter may be 10% by weight or less, more preferably 1% by weight or less, in terms of metal and based on the dry weight of the catalyst. If the catalyst contains two or more of cobalt, iron and ruthenium, the component with high content is used as the active metal component, and the component with low content is used as the auxiliary agent.

According to the present invention, the active metal component and the promoter can be loaded on the catalytic carrier by various methods, for example, a precursor of the active metal component and a precursor of the promoter are introduced by impregnation, and then drying and calcining are performed, wherein the impregnation times can be multiple times, generally 1 to 5 times is suitable, so as to increase the content of the metal active component and the promoter in the catalyst. The precursor of the active metal component may be at least one of an inorganic salt, an organic salt, a complex, etc. containing the active metal, which is soluble in a solvent, and the precursor of the auxiliary may be at least one of an inorganic salt, an organic salt, a complex, etc. containing the auxiliary, which is soluble in a solvent, which may be water or various common organic solvents. For example, if the active metal component is cobalt, the precursor thereof may be at least one selected from cobalt nitrate, cobalt chloride and other inorganic cobalt salts, and cobalt acetate, cobalt citrate and other organic cobalt salts; if the active metal component is iron, the precursor thereof may be at least one selected from the group consisting of ferric nitrate, ferric chloride and other inorganic ferric salts, and ferric acetate, ferric citrate and other organic ferric salts; if the active metal component is ruthenium, the precursor thereof may be at least one selected from ruthenium nitrosyl nitrate, ruthenium chloride and a soluble complex of ruthenium. In the present invention, the promoter may be introduced into the catalyst before, simultaneously with and after the active metal component, and preferably the promoter is introduced into the catalyst before or simultaneously with the active metal component. Specifically, the catalytic carrier may be first impregnated with a solution of a precursor containing the auxiliary agent, then dried and/or calcined, and then impregnated with a solution of a precursor containing the active metal component, and then dried and/or calcined; or the catalytic carrier is soaked in the solution of the precursor containing the active metal component, then the drying and/or roasting is carried out, then the solution of the precursor containing the auxiliary agent is soaked, and then the drying and/or roasting is carried out; it is also possible to impregnate the catalytic carrier with a solution containing both a precursor of the active metal component and a precursor of the auxiliary agent, followed by drying and/or calcination. The drying and roasting are well known to those skilled in the art, for example, the temperature of the drying may be 50 ℃ to 200 ℃, preferably 100 ℃ to 180 ℃, more preferably 120 ℃ to 150 ℃; the temperature of the calcination may be 200 to 600 c, preferably 250 to 500 c, and the calcination time may be 1 to 12 hours, preferably 2 to 6 hours, and in general, in the drying and calcination treatments which are sequentially performed, the drying temperature is lower than the calcination temperature.

According to the present invention, the active metal component in the catalyst prepared by drying and calcining is generally present in an oxidized state, and therefore it is necessary to subject the active metal component to reductive activation so that the active metal component is present in a metallic state. The reduction is generallyReducing the catalyst in a reducing atmosphere, e.g. H ₂ CO, etc., or H diluted with nitrogen or inert gas ₂ CO, etc., preferably H ₂ Or diluted H ₂ The hydrogen may be present in the catalyst to be reduced and in the hydrogen in a volume of from 0.5 to 100% by volume. Suitable reduction temperatures may be 100-; the heating rate can be 0.01-20 ℃/min, preferably 0.1-10 ℃/min; the pressure of the reducing atmosphere may be in the range of 0 to 4.0 mpa, preferably 0 to 2.0 mpa, more preferably 0 to 1.0 mpa; the hourly space velocity of the reducing gas can be 200-10000 l of gas (at standard conditions)/g of catalyst/h, preferably 500-8000 l of gas (at standard conditions)/g of catalyst/h. The reduction may be carried out at the desired temperature and pressure of the reducing atmosphere, preferably by reducing the catalyst in situ within the reactor.

The Fischer-Tropsch synthesis reaction according to the present invention is well known to those skilled in the art and will not be described herein, and the reaction conditions are also well known to those skilled in the art, for example, for a cobalt-based catalyst, the reaction temperature may be 120-; for the iron-based catalyst, the reaction temperature may be 120-550 ℃, preferably 160-450 ℃, more preferably 190-350 ℃; for ruthenium-based catalysts, the reaction temperature may be 120-350 ℃, preferably 160-280 ℃, more preferably 190-250 ℃. The reaction pressure may be in the range of from 0.5 to 15.0 MPa, preferably from 1.0 to 8.0 MPa, more preferably from 1.0 to 5.0 MPa; the molar ratio of hydrogen to carbon monoxide may be in the range of from 0.4 to 3.0, preferably from 1.0 to 2.5, more preferably from 1.5 to 2.2, and the hourly space velocity of the reaction gas may be in the range of from 200-.

Because the roundness value of the catalytic carrier in the catalyst is smaller and the catalytic carrier optionally has larger surface roughness, the catalyst is suitable for reacting under the relatively static condition without mutual collision, therefore, the reactor can be a microchannel reactor and/or a fixed bed reactor, preferably the microchannel reactor, and the microchannel reactor has the advantages of small catalyst consumption, high catalyst efficiency, short diffusion distance, quick heat transfer and the like, and can accelerate the catalytic reaction.

The invention will be further illustrated by the following examples, but is not to be construed as being limited thereto.

In the examples of the invention and the comparative examples:

the conversion of CO (weight of CO in the feed gas-weight of CO in the gas after reaction)/weight of CO in the feed gas × 100%;

methane selectivity-weight of methane in the reaction product/weight of reaction product x 100% (reaction product excluding feed gas component);

c5+ hydrocarbon selectivity ═ weight of C5+ hydrocarbons in the reaction product/weight of reaction product × 100%;

CO ₂ selectivity to CO in the reaction product ₂ Weight of (c)/weight of reaction product x 100%.

Preparation of comparative example 1

An alumina carrier provided by Changling catalyst division is selected and is marked as a carrier DB1, a micrograph is shown in figure 1, and specific properties are shown in Table 1.

Preparation of comparative example 2

An alumina carrier provided by Changling catalyst division is selected and is marked as carrier DB2, and a micrograph is shown in figure 2, and specific properties are shown in Table 1.

Preparation of example 1

An alumina carrier provided by Changling catalyst division is selected and is marked as a carrier Z1, and a micrograph is shown in figure 3, and specific properties are shown in Table 1.

Preparation of example 2

An alumina carrier provided by Changling catalyst division is selected and is marked as a carrier Z2, and a micrograph is shown in figure 4, and specific properties are shown in Table 1.

Preparation of example 3

An alumina carrier provided by Changling catalyst division was selected and recorded as carrier Z3, and a micrograph thereof is shown in FIG. 5, and specific properties thereof are shown in Table 1.

Preparation of example 4

An alumina carrier provided by Changling catalyst division is selected and is marked as a carrier Z4, and a micrograph is shown in figure 6, and specific properties are shown in Table 1.

Examples 1A to 4A

The carriers Z1, Z2, Z3 and Z4 in preparation examples 1 to 4 were impregnated with a mixed solution containing iron nitrate, manganese nitrate, copper nitrate and potassium nitrate in saturation, followed by drying and calcination to obtain catalysts Fe-C1, Fe-C2, Fe-C3 and Fe-C4, respectively. Wherein the drying temperature is 120 ℃, the drying time is 3 hours, the roasting temperature is 350 ℃, and the roasting time is 3 hours. The use amounts of the ferric nitrate, the manganese nitrate, the cupric nitrate and the potassium nitrate are controlled so that the Fe content, the Mn content, the Cu content and the K content in the final catalyst (on a dry basis) are 39-40 wt%, 4.5-5.0 wt%, 2.0-2.2 wt% and 0.10-0.12 wt%, respectively.

The Fischer-Tropsch synthesis reaction performances of the catalysts Fe-C1, Fe-C2, Fe-C3 and Fe-C4 are respectively evaluated in a fixed bed reactor. Before the Fischer-Tropsch synthesis catalyst is used, the Fischer-Tropsch synthesis catalyst needs to be reduced to a metal state. Catalyst reduction reaction conditions: the pressure is normal pressure, the heating rate is 5 ℃/min, the space velocity of hydrogen is 600 liters of gas (under the standard condition)/gram of catalyst/hour, the reduction temperature is 400 ℃, and the reduction time is 5 hours. After the reduction of the catalyst, a reaction performance test was performed, and the reaction conditions were as follows: feed gas composition H ₂ /CO/N ₂ 45%/45%/10% (volume/percentage), pressure 2.5MPa, temperature 295 ℃, feed gas space velocity 8000 litres of gas (under standard conditions)/gram catalyst/hour. After the reaction had proceeded for 24 hours, gas samples were taken for chromatographic analysis, in which the CO conversion, methane selectivity, C5+ hydrocarbon selectivity and CO were ₂ The selectivities are listed in Table 2A.

Comparative examples 1A-2A

Catalysts were prepared and performance evaluations were performed by the methods of examples 1A-4A, except that the supports were replaced with DZ1 and DZ2 supports as in the preparation comparative examples, to obtain catalysts Fe-DB1 and Fe-DB2, respectively, and the specific reaction results are shown in Table 2A.

As can be seen from tables 1 and 2A, the alumina with small roundness value provided by the invention is used as a catalytic carrier to prepare the iron-based Fischer-Tropsch synthesis catalyst, and the catalyst has better Fischer-Tropsch reaction performance, higher CO conversion rate and C5+ hydrocarbon selectivity, and lower methane selectivity and CO selectivity under the same other conditions ₂ And (4) selectivity.

Examples 1B to 4B

The carriers Z1, Z2, Z3 and Z4 in the preparation examples were saturated with a mixed solution containing cobalt nitrate, zirconium nitrate and platinum chloride, and then dried and calcined to obtain catalysts Co-C1, Co-C2, Co-C3 and Co-C4, respectively. Wherein the drying temperature is 120 ℃, the drying time is 3 hours, the roasting temperature is 350 ℃, and the roasting time is 3 hours. The cobalt nitrate, zirconium nitrate and platinum chloride are used in such amounts that the Co content, Zr content and Pt content in the final catalyst (on a dry basis) are respectively controlled to be 38-39 wt%, 4.5-5.0 wt% and 0.09-0.11 wt%, respectively.

The Fischer-Tropsch synthesis reaction performances of the catalysts Co-C1, Co-C2, Co-C3 and Co-C4 were evaluated in a fixed bed reactor respectively. Before the Fischer-Tropsch synthesis catalyst is used, the Fischer-Tropsch synthesis catalyst needs to be reduced to a metal state. Catalyst reduction reaction conditions: the pressure is normal pressure, the heating rate is 5 ℃/min, the space velocity of hydrogen is 600 liters of gas (under the standard condition)/gram of catalyst/hour, the reduction temperature is 400 ℃, and the reduction time is 5 hours. After the catalyst reduction, a reaction performance test was performed, and the reaction conditions were as follows: feed gas composition H ₂ /CO/N ₂ 64%/32%/4% (v/v), pressure 2.5MPa, temperature 220 ℃, feed gas space velocity 18000 litres of gas (under standard conditions)/gram of catalyst/hour. After 24 hours the reaction was run, gas samples were taken for chromatography, where CO conversion, methane selectivity and C5+ hydrocarbon selectivity are listed in table 2B.

Comparative examples 1B to 2B

Catalysts were prepared and performance evaluations were performed by the methods of examples 1B-4B, except that the carriers were replaced with DZ1 and DZ2 carriers in the preparation comparative examples to obtain catalysts Co-DB1 and Co-DB2, and the specific reaction results are shown in Table 2B.

As can be seen from tables 1 and 2B, the alumina with small roundness value provided by the invention is used as a catalytic carrier to prepare a cobalt-based Fischer-Tropsch synthesis catalyst, and the catalyst has better Fischer-Tropsch reaction performance, higher CO conversion rate and C5+ hydrocarbon selectivity and lower methane selectivity under the same other conditions.

Examples 1C to 4C

The carriers Z1, Z2, Z3 and Z4 in the preparation examples were saturated with a mixed solution containing ruthenium nitrosyl nitrate and zirconium nitrate, followed by drying and calcination to obtain catalysts Ru-C1, Ru-C2, Ru-C3 and Ru-C4, respectively. Wherein the drying temperature is 120 ℃, the drying time is 3 hours, the roasting temperature is 350 ℃, and the roasting time is 3 hours. The dosage of the nitrosyl ruthenium nitrate and the zirconium nitrate ensures that the content of Ru in the final catalyst (on a dry basis) is controlled to be 7.5-7.8 wt%, and the content of Zr is controlled to be 4.5-5.0 wt%.

The Fischer-Tropsch synthesis reaction performances of the catalysts Ru-C1, Ru-C2, Ru-C3 and Ru-C4 are respectively evaluated in a fixed bed reactor. Before the Fischer-Tropsch synthesis catalyst is used, the Fischer-Tropsch synthesis catalyst needs to be reduced to a metal state. Catalyst reduction reaction conditions: the pressure is normal pressure, the heating rate is 5 ℃/min, the space velocity of hydrogen is 600 liters of gas (under the standard condition)/gram of catalyst/hour, the reduction temperature is 300 ℃, and the reduction time is 5 hours. After the catalyst reduction, a reaction performance test was performed, and the reaction conditions were as follows: feed gas composition H ₂ /CO/N ₂ 64%/32%/4% (v/v), pressure 2.5MPa, temperature 200 ℃, feed gas space velocity 15000 litres of gas (under standard conditions)/gram of catalyst per hour. After the reaction was carried out for 24 hours, a gas sample was taken for chromatography, wherein the conversion of CO, the selectivity to methane and the selectivity to C5+ hydrocarbons are shown in Table 2C.

Comparative examples 1C to 2C

Catalysts were prepared and performance evaluations were performed by the methods of examples 1C-4C, except that the supports were replaced with DZ1 and DZ2 supports in the preparation of comparative examples to obtain catalysts Ru-DB1 and Ru-DB2, and the specific reaction results are shown in Table 2C.

As can be seen from tables 1 and 2C, the alumina with small roundness value provided by the invention is used as a catalytic carrier to prepare the ruthenium-based Fischer-Tropsch synthesis catalyst, and the catalyst has better Fischer-Tropsch synthesis performance, higher CO conversion rate and C5+ hydrocarbon selectivity and lower methane selectivity under the same other conditions.

TABLE 1 physical Properties of the support

Item	Type of the Carrier	Particle size of carrier/μm	Roundness value Range E
				Preparation of comparative example 1	DB1	70～140	0.85～0.92
Preparation of comparative example 2	DB2	50～150	0.92～0.95
				Preparation of example 1	Z1	100～250	0.50～0.55
Preparation of example 2	Z2	50～150	0.45～0.48
				Preparation of example 3	Z3	100～200	0.47～0.52
Preparation of example 4	Z4	80～220	0.51～0.68

TABLE 2 reaction results of the catalysts

TABLE 2B reaction results of the catalysts

TABLE 2C reaction results of the catalysts

Claims

1. A method of preparing a fischer-tropsch synthesis catalyst, the method comprising:

loading an active metal component on the surface of a catalytic carrier; wherein the catalytic carrier is one or a mixture or a composite of a plurality of the alumina, silica-alumina, aluminum silicate, silica, titania and zirconia, and the roundness value range E of the catalytic carrier is set to be 0.35-0.80; the method for obtaining the roundness value range E of the catalytic carrier comprises the following steps:

2. The production method according to claim 1, wherein the roundness value range E of the catalytic carrier is set to 0.45 to 0.75.

3. The production method according to claim 1, wherein a surface roughness Rz of the catalytic carrier is set to 0.25 to 25 μm; the surface roughness Rz of the catalytic carrier is determined by an interferometry.

4. The production method according to claim 3, wherein a surface roughness Rz of the catalytic carrier is set to 0.5 to 20 μm.

5. The production method according to claim 4, wherein a surface roughness Rz of the catalytic carrier is set to 1 to 10 μm.

6. The process according to claim 1, wherein the catalytic support has a pore volume of 0.2 to 3 ml/g and a specific surface area of 60 to 400 m, characterized by mercury intrusion ² Per gram, the proportion of the pore volume of pores with the diameters of 2-30 nanometers in the total pore volume is more than 30 percent by volume;

the particle size d of the catalytic carrier meets the following conditions: d is more than or equal to 0.10 mu m and less than or equal to 1000 mu m, and the particle size is measured by adopting a microscope image method.

7. The preparation method as claimed in claim 6, wherein the catalytic carrier has a pore volume of 0.3-1.5 ml/g, a specific surface area of 100-300 m ² Per gram, the proportion of the pore volume of pores with diameters of 2-30 nanometers to the total pore volume is more than 50 volume percent.

8. The production method according to claim 6, wherein the particle diameter d of the catalytic carrier satisfies the following condition: d is more than or equal to 1.0 mu m and less than or equal to 750 mu m.

9. The production method according to claim 8, wherein the particle diameter d of the catalytic carrier satisfies the following condition: d is more than or equal to 10 mu m and less than or equal to 500 mu m.

10. The production method according to claim 9, wherein the particle diameter d of the catalytic carrier satisfies the following condition: d is more than or equal to 20 mu m and less than or equal to 300 mu m.

11. The production method according to claim 10, wherein the particle diameter d of the catalytic carrier satisfies the following condition: d is more than or equal to 50 mu m and less than or equal to 200 mu m.

12. The production method according to claim 1, wherein the active metal component includes at least one selected from cobalt, iron, and ruthenium.

13. The method of claim 12 wherein if the active metal component comprises cobalt, the amount of cobalt in the catalyst is from 5 to 80 wt.% on an elemental basis and on a weight of the catalyst on a dry basis;

if the active metal component comprises iron, the iron content of the catalyst is 5-80 wt% calculated on element and based on the dry weight of the catalyst;

if the active metal component comprises ruthenium, the ruthenium content of the catalyst is from 0.1 to 20% by weight, calculated as oxide and based on the weight of the catalyst on a dry basis.

14. The method of claim 13 wherein if the active metal component comprises cobalt, the amount of cobalt in the catalyst is from 10 to 70 wt% on an elemental basis and based on the weight of the catalyst on a dry basis;

if the active metal component comprises iron, the iron content of the catalyst is 10-70 wt% calculated on element and based on the dry weight of the catalyst;

if the active metal component comprises ruthenium, the ruthenium content of the catalyst is from 0.5 to 10% by weight, calculated as oxide and based on the weight of the catalyst on a dry basis.

15. The method of claim 14 wherein if the active metal component comprises cobalt, the amount of cobalt in the catalyst is from 20 to 60 wt.% on an elemental basis and based on the weight of the catalyst on a dry basis;

if the active metal component comprises iron, the iron content of the catalyst is from 20 to 60% by weight, calculated as element and based on the weight of the catalyst on a dry basis.

16. The preparation method according to claim 12, wherein the catalyst further comprises an auxiliary agent;

if the active metal component is cobalt, the auxiliary agent is at least one selected from non-noble metals, rare earth oxides and noble metals, the non-noble metals are at least one selected from Cu, Mo, Ta, W, Ru, Zr, Ti, Re, Hf, La, Ce, Mn and V, and the noble metals are at least one selected from Pt, Pd, Rh, Ir, Re, Au and Ag; if the auxiliary agent is at least one selected from non-noble metals and rare earth oxides, the content of the auxiliary agent is less than 30 weight percent based on the oxide and the dry weight of the catalyst; if the auxiliary agent is at least one selected from noble metals, the content of the auxiliary agent is less than 10 weight percent based on the metal and the dry weight of the catalyst;

if the active metal component is iron, the auxiliary agent is at least one selected from Ti, V, Cr, Mn, Co, Ni, Cu, Zn, Zr, Nb, Mo, W, Ce, Ru, Re, La, Li, Mg, K and Ca; the content of the auxiliary agent is less than 30 wt% in terms of oxide and on the basis of the dry weight of the catalyst;

if the active metal component is ruthenium, the auxiliary agent is at least one selected from non-noble metals, rare earth oxides and noble metals, the non-noble metals are at least one selected from Li, K, Mg, Ca, Cu, Mo, Ta, Cr, W, Zr, Ti, Re, Hf, Ce, Mn, V, Si and Pr, and the noble metals are at least one selected from Pt, Pd, Rh, Ir, Re, Au and Ag; if the auxiliary agent is at least one selected from non-noble metals and rare earth oxides, the content of the auxiliary agent is less than 30 weight percent based on the oxide and the dry weight of the catalyst; if the auxiliary is at least one selected from noble metals, the content of the auxiliary is 10 wt% or less in terms of metal and based on the dry weight of the catalyst.

17. The production method according to claim 16, wherein if the active metal component is cobalt, the non-noble metal is at least one selected from the group consisting of W, Zr, Re, Ru and Ce; if the auxiliary agent is at least one selected from non-noble metals and rare earth oxides, the content of the auxiliary agent is less than 20 weight percent based on the oxide and the dry weight of the catalyst; if the auxiliary agent is at least one selected from noble metals, the content of the auxiliary agent is less than 1 weight percent calculated by metals and based on the dry weight of the catalyst;

if the active metal component is iron, the auxiliary agent is at least one selected from Mn, Cu, W, Zr, Re and Ru; the content of the auxiliary agent is less than 20 wt% calculated by oxide and based on the dry weight of the catalyst;

if the active metal component is ruthenium and if the auxiliary agent is at least one selected from non-noble metals and rare earth oxides, the content of the auxiliary agent is less than 20 wt% calculated by the oxides and based on the dry weight of the catalyst; if the auxiliary is at least one selected from the group consisting of noble metals, the content of the auxiliary is 1% by weight or less, based on the metal and the weight of the catalyst on a dry basis.

18. The production method according to claim 17, wherein if the active metal component is cobalt, if the promoter is at least one selected from a non-noble metal and a rare earth oxide, the content of the promoter is 15% by weight or less in terms of oxide and based on the dry weight of the catalyst;

if the active metal component is iron, the content of the auxiliary agent is less than 15 weight percent calculated by oxide and based on the dry weight of the catalyst;

if the active metal component is ruthenium and if the promoter is at least one selected from non-noble metals and rare earth oxides, the promoter is present in an amount of 15 wt.% or less, based on the oxides and on the dry weight of the catalyst.

19. A Fischer-Tropsch synthesis catalyst comprises a catalytic carrier and an active metal component loaded on the surface of the catalytic carrier; wherein the catalytic carrier is one or a mixture or a compound of more of alumina, silica-alumina, aluminum silicate, silica, titania and zirconia; the roundness value range E of the catalytic carrier is set to 0.35 to 0.80; the method for obtaining the roundness value range E of the catalytic carrier comprises the following steps:

20. The catalyst according to claim 19, wherein the roundness value range E of the catalytic carrier is set to 0.45-0.75.

21. The catalyst according to claim 19, wherein the surface roughness Rz of the catalytic carrier is set to 0.25-25 micron; the surface roughness Rz of the catalytic carrier is measured by interferometry.

22. The catalyst according to claim 21, wherein the surface roughness Rz of the catalytic carrier is set to 0.5-20 microns.

23. The catalyst according to claim 22, wherein the surface roughness Rz of the catalytic carrier is set to 1-10 microns.

24. The catalyst of claim 19, wherein the catalytic support has a pore volume of 0.2 to 3 ml/g and a specific surface area of 60 to 400 m, characterized by mercury intrusion ² Per gram, the proportion of the pore volume of pores with the diameter of 2-30 nanometers in the total pore volume is more than 30 percent by volume; the catalytic carrier is formed by at least one forming mode selected from spray forming, rolling ball forming, dropping ball forming, tabletting forming and extrusion molding;

the particle size d of the catalytic carrier meets the following condition: d is more than or equal to 0.10 mu m and less than or equal to 1000 mu m, and the particle size is measured by adopting a microscope image method.

25. The catalyst as claimed in claim 24, wherein the catalytic carrier has a pore volume of 0.3 to 1.5 ml/g, a specific surface area of 100-300 m ² Per gram, the proportion of the pore volume of pores with diameters of 2-30 nanometers in the total pore volume is more than 50 volume percent.

26. The catalyst according to claim 24, wherein the particle size d of the catalytic carrier satisfies the following condition: d is more than or equal to 1.0 mu m and less than or equal to 750 mu m.

27. The catalyst according to claim 26, wherein the particle size d of the catalytic carrier satisfies the following condition: d is more than or equal to 10 mu m and less than or equal to 500 mu m.

28. The catalyst according to claim 27, wherein the particle size d of the catalytic carrier satisfies the following condition: d is more than or equal to 20 mu m and less than or equal to 300 mu m.

29. The catalyst according to claim 28, wherein the particle size d of the catalytic carrier satisfies the following condition: d is more than or equal to 50 mu m and less than or equal to 200 mu m.

30. The catalyst of claim 19, wherein the active metal component comprises at least one selected from cobalt, iron, and ruthenium.

31. The catalyst of claim 30 wherein if the active metal component comprises cobalt, the amount of cobalt in the catalyst is from 5 to 80 wt% calculated on an elemental basis and based on the weight of the catalyst on a dry basis;

32. The catalyst of claim 31 wherein if the active metal component comprises cobalt, the amount of cobalt in the catalyst is from 10 to 70 wt% on an elemental basis and based on the weight of the catalyst on a dry basis;

33. The catalyst of claim 32 wherein if the active metal component comprises cobalt, the amount of cobalt in the catalyst is from 20 to 60 wt% calculated on an elemental basis and based on the weight of the catalyst on a dry basis;

34. The catalyst of claim 31, wherein the catalyst further comprises an adjunct;

35. The catalyst of claim 34, wherein if the active metal component is cobalt, the non-noble metal is at least one selected from the group consisting of W, Zr, Re, Ru, and Ce; if the auxiliary agent is at least one selected from non-noble metals and rare earth oxides, the content of the auxiliary agent is less than 20 weight percent based on the oxide and the dry weight of the catalyst; if the auxiliary agent is at least one selected from noble metals, the content of the auxiliary agent is less than 1 weight percent calculated by metals and based on the dry weight of the catalyst;

if the active metal component is iron, the auxiliary agent is at least one selected from Mn, Cu, W, Zr, Re and Ru; the content of the auxiliary agent is less than 20 wt% in terms of oxide and on the basis of the dry weight of the catalyst;

36. The catalyst as claimed in claim 35, wherein if the active metal component is cobalt, and if the promoter is at least one selected from non-noble metals and rare earth oxides, the promoter is present in an amount of 15 wt% or less, calculated as oxide and based on the dry weight of the catalyst;

if the active metal component is iron, the content of the auxiliary agent is less than 15 wt% calculated by oxide and based on the dry weight of the catalyst;

37. A fischer-tropsch synthesis process, the process comprising: contacting hydrogen and carbon monoxide with a catalyst according to any one of claims 19 to 36 in a reactor and carrying out a fischer-tropsch synthesis reaction.

38. The process of claim 37, wherein the reactor is a microchannel reactor and/or a fixed bed reactor.

39. The process of claim 38, wherein the reactor is a microchannel reactor.