JP2009011938A - Catalyst for reducing carbon monoxide, its manufacturing method and method for producing hydrocarbon - Google Patents

Abstract

<P>PROBLEM TO BE SOLVED: To provide a catalyst for reducing carbon monoxide which exhibits high selectivity when a hydrocarbon fraction of 10-20 carbon atoms is produced and to provide a method for manufacturing the catalyst for reducing carbon monoxide and a method for producing a hydrocarbon efficiently by reducing carbon monoxide. <P>SOLUTION: The method for manufacturing the catalyst for reducing carbon monoxide comprises: a step (1) of impregnating a metal oxide being a carrier with a chelating agent; a step (2) of drying the chelating agent-impregnated metal oxide; a step (3) of impregnating the dried chelating agent-impregnated metal oxide with a transition metal compound-containing solution; a step (4) of drying the metal oxide impregnated with the transition metal compound-containing solution; and a step (5) of firing the metal oxide which is obtained by impregnating and drying the transition metal compound-containing solution. <P>COPYRIGHT: (C)2009,JPO&INPIT

Description

  The present invention relates to a carbon monoxide reduction catalyst that can be used in a Fischer-Tropsch synthesis reaction, a method for producing the same, and a method for producing hydrocarbons by reduction of carbon monoxide using the catalyst.

The reduction of carbon monoxide is an effective reaction as a method for producing fuels and chemical raw materials composed of clean hydrocarbons that do not contain sulfur, and is referred to as “Fischer-Tropsch” synthesis (hereinafter referred to as “FT synthesis”). .)is called. Syngas (a mixture of carbon monoxide and hydrogen), which is a raw material for FT synthesis, can be produced from non-petroleum-based carbon resources other than petroleum (natural gas, biomass, coal, etc.), and FT synthesis will be used in future petroleum. This is important for the diversification of energy and chemical raw materials in response to depletion and from the viewpoint of reducing emissions of environmentally hazardous substances such as sulfur oxides. In particular, since the C10-C20 hydrocarbon fraction obtained by FT synthesis has a high cetane number and does not substantially contain sulfur, this reaction is attracting attention as a method for synthesizing high-grade diesel fuel.
Under such circumstances, effective utilization of unused carbon resources such as natural gas from large-scale natural gas fields has already been studied.

  It is known that many transition metals show catalytic activity for FT synthesis in a broad sense. Among them, cobalt catalysts supported on silica and alumina have high synthesis gas conversion activity and liquid hydrocarbons at low temperature and moderate pressure. It is known to exhibit selectivity. In these commercial processes, a silica-supported cobalt catalyst to which zirconium, rhenium, platinum or the like is added is used, and the productivity of the C10-C20 hydrocarbon fraction is said to be about 100 to 200 g / kg-cat · h. However, this level of activity is inadequate in terms of profitability to convert unused carbon resources such as natural gas from medium and small-scale natural gas fields into fuel, improving catalyst activity and selectivity. is necessary. On the other hand, when a catalyst having cobalt supported on mesoporous silica having a special pore structure is used for FT synthesis, it has been found that high productivity of C10-C20 hydrocarbon fraction can be obtained. Manufacturing requires a complicated process and has a problem of low mechanical strength.

In the production of cobalt catalysts, it has been reported that cobalt nitrate can be formed as a highly dispersed cobalt species on an alumina or titania support by using cobalt nitrate as a precursor and blending with ethylenediaminetetraacetic acid (EDTA) and citric acid. (For example, refer nonpatent literature 1 and nonpatent literature 2.).
However, in the catalyst thus obtained, there is a problem that the reduction of the cobalt species to the metallic cobalt is difficult to proceed, and therefore, there is almost no activity for the reduction reaction of carbon monoxide.

Moreover, the manufacturing method of the catalyst which impregnated the silica containing the solution containing this chelating agent and a cobalt compound using polyfunctional carboxylic acid as a chelating agent is disclosed (for example, refer patent document 1 and patent document 2). . However, when a carbon monoxide reduction reaction is carried out using the catalyst thus produced, carbon monoxide conversion and high value-added C10-C20 hydrocarbon fraction (kerosene oil fraction) are produced. In particular, the productivity per unit cobalt amount in the catalyst was low, and performance improvement was necessary.
J. vande L oosdrecht, M. vande Haar, A. M. vander Kraan, A. J. van D illen, J. W. Geus, "A ppl. Catal. A. G en.", 1 5 0, 3 6 5 (1 9 9 7) M. Kraum, M. Baems, "A ppl. Catal. A. Gen.", 1 8 6, 1 8 9 (1 9 9 9) Japanese Patent No. 3882044 Special Table 2002-512556 gazette

  The present invention provides a highly selective carbon monoxide reduction catalyst for a C10-C20 hydrocarbon fraction, which is a kerosene oil fraction, a production method thereof, and an efficient hydrocarbon production method by reduction of carbon monoxide. For the purpose.

  As a result of diligent research in view of the above-described problems of the prior art, the present inventors have previously supported a chelating agent on a general-purpose carrier such as amorphous silica, and then supported cobalt so that a particularly expensive noble metal can be obtained. The present invention was completed by finding that a carbon monoxide reduction catalyst with dramatically improved productivity of C10-C20 hydrocarbon fraction (up to about 4 times) can be obtained.

  That is, the first of the present invention is (1) a step of impregnating a metal oxide as a carrier with a chelating agent, (2) a step of drying the metal oxide impregnated with the chelating agent, and (3) impregnating the chelating agent. A step of impregnating a dried metal oxide with a solution containing a transition metal compound, (4) a step of drying a metal oxide impregnated with a solution containing the transition metal compound, and (5) the transition metal compound A carbon monoxide reduction catalyst characterized by being produced through a process including steps of impregnating a contained solution and firing a dried metal oxide.

  In the carbon monoxide reduction catalyst of the present invention, it is particularly preferable from the viewpoint of the activity and selectivity of the catalyst that the chelating agent in the production process is nitrilotriacetic acid and / or trans-cyclohexanediaminetetraacetic acid.

  Moreover, in the carbon monoxide reduction catalyst of the present invention, the metal oxide is particularly preferably silica or alumina from the viewpoints of catalyst activity, selectivity, mechanical strength, and the like.

  In the catalyst for reducing carbon monoxide of the present invention, the amount of the transition metal compound supported on the basis of the mass of the metal oxide is 1 to 40% by mass as a transition metal atom. And from the viewpoint of selectivity.

  In the catalyst for reducing carbon monoxide of the present invention, the activity and selectivity of the catalyst is such that the chelating agent is used at a ratio of 0.1 to 20 moles per mole of transition metal atoms in the transition metal compound. From the viewpoint of

  In the catalyst for reducing carbon monoxide of the present invention, the transition metal compound is particularly preferably nitrate and / or acetate from the viewpoint of catalyst activity and selectivity.

  In the catalyst for reducing carbon monoxide of the present invention, the transition metal is particularly preferably cobalt.

  Moreover, the carbon monoxide reduction catalyst of the present invention is manufactured by a manufacturing process including a step of firing the metal oxide before the step (1) of impregnating the metal oxide with the chelating agent. Is particularly preferable from the viewpoint of catalyst activity and selectivity.

  The second of the present invention is (1) a step of impregnating a metal oxide as a carrier with a chelating agent, (2) a step of drying the metal oxide impregnated with the chelating agent, (3) impregnating the chelating agent, A step of impregnating a dried metal oxide with a solution containing a transition metal compound, (4) a step of drying a metal oxide impregnated with a solution containing the transition metal compound, and (5) containing the transition metal compound. A method for producing a catalyst for reducing carbon monoxide, which is produced through steps including steps of impregnating a solution to be fired and firing a dried metal oxide.

  A third aspect of the present invention is a method for producing hydrocarbons by reduction of carbon monoxide, characterized by using the carbon monoxide reduction catalyst according to the present invention.

  Further, in the hydrocarbon production method of the present invention, the reduction conditions of carbon monoxide are reaction temperature of 200 to 500 ° C., W / F = 0.5 to 10 g · h / mol, pressure of 0.1 to 20 MPa, hydrogen / Carbon monoxide ratio = 1.0 to 4.0 (molar ratio) is particularly preferable from the viewpoint of the productivity of the intended hydrocarbon fraction.

  The catalyst of the present invention can be produced at low cost by using a general-purpose carrier, without adding noble metals or the like, and without particularly requiring special processes and equipment. Then, by performing the FT synthesis reaction using the catalyst of the present invention, the productivity of the most useful C10-C20 hydrocarbon fraction is greatly improved.

  Hereinafter, the best embodiment of the present invention will be described in detail.

  Silica, alumina, zirconia, titania and the like can be used as the metal oxide which is a carrier of the catalyst for reducing carbon monoxide of the present invention, and silica or alumina is preferable. Before impregnating these metal oxides with a chelating agent, it is preferable to use them after firing at 100 to 800 ° C., preferably 500 to 600 ° C. for 3 to 24 hours, preferably in air.

The specific surface area, pore volume, and average pore diameter of the metal oxide support are not particularly limited, but the specific surface area is 100 m ² / g or more, the pore volume is 0.5 mL / g or more, and the average pore diameter is The thickness is preferably 10 nm or more from the viewpoint of the activity of the catalyst for the reduction reaction of carbon monoxide and the kerosene fraction selectivity.

  In the step of impregnating the metal oxide carrier with a chelating agent, first, a solution (impregnating solution) in which the chelating agent is dissolved in a solvent is prepared. As the solvent, water, alcohols, ethers, ketones, and aromatic compounds can be used, and water is particularly preferable from the viewpoints of solubility, exhaust during drying, and the like.

  Chelating agents include gluconic acid, citric acid, oxalic acid, formic acid, tartaric acid, phytic acid, succinic acid, lactic acid, ethylenediaminetetraacetic acid (EDTA), trans-cyclohexanediaminetetraacetic acid (CyDTA), nitrilotriacetic acid (NTA), hydroxy Ethylethylenediaminetriacetic acid (HEDTA), diethylenetriaminepentaacetic acid (DTPA), triethylenetetraaminehexaacetic acid (TTHA), hydroxyethyliminodiacetic acid (HIDA), dihydroxyethylglycine (DHEG), hydroxyethylidene diphosphonic acid (HEDP), Ethylenediaminetetramethylenephosphonic acid (EDTMP), glycol etherdiaminetetraacetic acid (GEDTA), L-aspartic acid diacetic acid (ASDA), L-glutamic acid diacetic acid ( LDA), pyrophosphate, tripolyphosphate, trimetaphosphate, tetrametaphosphoric acid, and hexametaphosphoric acid can be used, in terms of activity and kerosene and gas oil distillates selectivity of the catalysts prepared, are preferably NTA and CyDTA.

  Examples of the method of impregnating the metal oxide carrier with the chelating agent include a wet impregnation method, a dry impregnation method, a spray impregnation method or a vacuum impregnation method. From the viewpoint of simplifying the operation, the wet impregnation method is preferable.

  The metal oxide carrier impregnated with the chelating agent can be dried by an atmospheric drying method, a reduced pressure drying method, or the like. For example, in the case of a normal pressure drying method, it can be performed under conditions of 10 to 200 ° C. and 0.2 to 48 hours in an atmospheric pressure atmosphere, preferably room temperature to 150 ° C. and 0.5 to 24 hours. .

  After impregnating a metal oxide carrier with a chelating agent and drying, a transition metal compound capable of reducing and hydrogenating carbon monoxide is supported thereon. As the transition metal, for example, cobalt, nickel, iron, copper, chromium, manganese, zirconium, molybdenum, tungsten, rhenium, osmium, iridium, palladium, silver, ruthenium, rhodium, and platinum can be used. In particular, for synthesizing high molecular weight hydrocarbons, cobalt, iron, and ruthenium are preferable, and cobalt is particularly preferable.

  These transition metals include the group consisting of salts such as nitrates, carbonates, organic acid salts, oxides, hydroxides, halides, cyanides, oxide salts, hydroxide salts, halide salts, and cyanide salts. It can be used as at least one metal compound selected from: Of these, nitrates and / or acetates are more preferred, and cobalt nitrate and / or cobalt acetate are particularly preferred. A metal compound may be used independently and may be used in mixture of 2 or more types.

A transition metal compound is dissolved in a solvent to prepare a solution (impregnating solution), which is used to impregnate a metal oxide carrier on which a chelating agent is supported.
As the solvent, water, alcohols, ethers, ketones, and aromatic compounds can be used, and water is particularly preferable from the viewpoints of solubility, dispersibility of metal species, exhaust during drying, and the like. Examples of the impregnation method include a wet impregnation method, a dry impregnation method, a spray impregnation method, and a vacuum impregnation method. From the viewpoint of simplification of the activity and selectivity of the produced catalyst, equipment and operation during catalyst production. The wet impregnation method is preferable. If the desired metal loading described later is not achieved by only one impregnation, the impregnation and drying steps may be repeated a plurality of times.

  In the carbon monoxide reduction catalyst of the present invention, the preferred amount of transition metal to be supported on the metal oxide support is determined according to the type of the metal. For example, in the case of cobalt or iron, it is preferably supported in the range of 1 to 40% by mass as a metal atom based on the mass of the metal oxide support. More preferably, it is 5-30 mass%. Further, in the case of ruthenium which is a noble metal, it is preferably supported in the range of 1 to 10% by mass. When the amount of transition metal supported is less than the lower limit of the above range, the conversion rate of carbon monoxide during the reaction of a mixed gas of hydrogen and carbon monoxide described later tends to decrease. On the other hand, even if a large amount is supported exceeding the upper limit value, the conversion rate of carbon monoxide corresponding to the amount cannot be improved.

  The ratio of the chelating agent to be supported and the transition metal compound is an important factor that affects the carbon monoxide reduction reaction performance. The mixing ratio of the chelating agent is preferably 0.1 to 20 mol, more preferably 0.3 to 10 mol, per 1 mol of the transition metal atom. When the mixing ratio of the chelating agent is less than 0.1 mol, the supporting effect of the chelating agent is small, and the activity of the catalyst finally obtained tends not to be improved. On the other hand, when it exceeds 20 moles, the viscosity of the impregnating solution is significantly increased, and thus impregnation into the metal oxide support tends to be difficult.

In the production of the catalyst for reducing carbon monoxide of the present invention, as described above, the metal oxide carrier is impregnated with the solution containing the chelating agent and then dried, and further impregnated with the impregnating solution containing the transition metal compound. Then, drying and baking are performed.
Drying can be performed by an atmospheric drying method, a reduced pressure drying method, or the like. For example, in the case of a normal pressure drying method, it can be performed under conditions of room temperature to 150 ° C. and 0.1 to 24 hours in an atmospheric pressure atmosphere.

  The subsequent firing is preferably performed, for example, in air at 300 to 500 ° C. for about 2 to 5 hours.

  There is no restriction | limiting in particular in the shape of the catalyst for carbon monoxide reduction of this invention, It can use as powder form (for example, average particle diameter 50-150 micrometers) or granular form (for example, average particle diameter 1-20 mm). In addition to this, the powder may be formed into a pellet by molding silica, alumina, boria or the like as a binder, or may be used in the form of a granulated powder. Moreover, a molded article can be made into shapes, such as a column shape, a trilobal shape, a tetralobal shape, and a spherical shape, as needed.

  By the method described above, a catalyst in which an oxide of a transition metal capable of hydrogenating and reducing carbon monoxide is highly dispersed on a support is produced. The obtained catalyst can be used for a carbon monoxide reduction reaction after being subjected to an activation treatment (reduction treatment) by a conventional method.

  As the activation treatment, for example, a catalyst before the activation treatment is filled in a reaction tower, and hydrogen or carbon monoxide or a synthesis gas of hydrogen and carbon monoxide is circulated as an activating agent, while 300 to 500 ° C. And a process of maintaining the temperature at a predetermined actual operation temperature for about 4 to 12 hours.

The catalyst of this invention is manufactured through the process including each process of said (1)-(5) as mentioned above.
In the presence of the catalyst of the present invention prepared by such a method, a mixed gas containing hydrogen and carbon monoxide is heated at a temperature of 200 to 500 ° C., a pressure of 0.1 to 20 MPa, and 0.5 to 10 g · h / mol. By reacting at a W / F of 1.0 to 4.0 mol / mol of hydrogen / carbon monoxide ratio, a hydrocarbon which is a hydrogenated product containing gasoline fuel oil components, diesel fuel components and the like is obtained. .
Here, “W” represents the mass (g) of the catalyst charged in the reactor, “F” represents the total flow rate (mol / h) of carbon monoxide and hydrogen supplied to the reactor, “W / F” is a numerical value that is a measure of the contact time of the raw material with the catalyst.

  In the method for producing hydrocarbons by reduction of carbon monoxide according to the present invention, the form of the reaction phase to be used is not limited, and a fixed bed, a fluidized bed, a suspension bed and the like are used. As the reactor, a tower reactor, a tank reactor (equipped with a stirrer) and the like are used.

  Specifically, for example, a powdery catalyst is filled in a cylindrical stainless steel high-pressure reaction tube, and the reaction tube is heated, for example, with a heater disposed outside so that the internal temperature becomes 200 to 500 ° C. . In this state, a hydrogenated product is produced by circulating a high-pressure mixed gas (0.1 to 20 MPa) containing hydrogen and carbon monoxide.

  In addition, a slurry in which a powdery catalyst of the present invention is dispersed in a high-boiling organic solvent is contained in a high-pressure tank having an inlet / outlet, and the internal temperature of the high-pressure tank is, for example, 200 to 500 by a heater disposed outside. It is also possible to produce a hydrogenated product by circulating a high-pressure mixed gas (0.1 to 20 MPa) containing hydrogen and carbon monoxide from the inlet into the slurry in a state heated to ° C. is there.

  In the reaction system in which the mixed gas is reacted in the presence of the catalyst for reducing carbon monoxide of the present invention, by setting the temperature and the pressure within the above ranges, C1 methane to C4 butane as target components, and C5 It becomes possible to selectively produce a gasoline fuel oil component of ˜C9 and a diesel fuel oil component of C10 to C20 and a high-boiling paraffin such as wax.

  The present invention will be described more specifically with reference to the following examples. However, the present invention is not limited to the following examples.

Example 1
Silica (Q-15 manufactured by Fuji Silysia Chemical Ltd.) was prepared as a carrier. This silica has a specific surface area of about 200 m ² / g, a pore volume of about 1.0 mL / g, and an average pore diameter of about 15 nm. This silica was used after calcination in air at 55 ° C. for 2 hours.
The impregnation of the chelating agent into silica was performed as follows.
0.8 g of NTA as a chelating agent was taken in a volumetric flask having an internal volume of 5 mL, and distilled water was added to make 5 mL to prepare an impregnation solution. A silica carrier was impregnated with a chelating agent by the Incipient Wetness method using 1.0 mL of the impregnation solution. Silica impregnated with the chelating agent was dried in air at 120 ° C. for 12 hours.
Impregnation of cobalt as a transition metal was performed as follows.
After dissolving 1.23 g of cobalt nitrate in a volumetric flask having an internal volume of 5 mL, an aqueous solution (impregnation solution) having a total volume of 5 mL by adding distilled water was prepared. Using 1.0 mL of this solution, silica impregnated with a chelating agent was impregnated so that the supported amount of cobalt was 20 wt%.
The silica impregnated with the solution was dried in air at 120 ° C. for 12 hours.
Then, it baked at 350 degreeC in the air for 4 hours, and obtained the catalyst.
The obtained catalyst was accommodated in a high-pressure fixed bed flow reactor, and was heated at 500 ° C. in a hydrogen stream.
Pretreatment was carried out by reduction at Then, the hydrogenation product was manufactured by introduce | transducing the mixed gas containing hydrogen and carbon monoxide, and performing FT synthesis reaction on the following conditions.
Reaction temperature: 230 ° C
Total pressure: 1.1 MPa
H ₂ / CO = 62/33 (mol / mol)
W / F = 1.25 g-cat · h / mol
Productivity (STY, unit: g / kg-cat / h) of C10-C20 fraction and C5 + fraction 20 hours after the start of FT reaction was examined by analysis by gas chromatography. The results obtained are summarized in Table 1 below.

(Example 2)
A catalyst was prepared in the same manner as in Example 1 except that NTA was changed to 1.5 g of CyDTA, and an FT synthesis reaction was performed under the same conditions. The results are shown in Table 1.

(Comparative Example 1)
A catalyst was prepared by the same method as in Example 1 except that NTA was not blended, and an FT synthesis reaction was performed under the same conditions. The results are shown in Table 1.

(Comparative Example 2)
A catalyst was prepared in the same manner as in Example 2 except that the chelating agent was not impregnated in advance with the chelating agent and cobalt was impregnated at the same time, and an FT synthesis reaction was performed under the same conditions. The results are shown in Table 1.

As shown in Table 1 above, C10-20 STY of a catalyst (Comparative Example 1) produced using a solution containing no chelating agent (unit catalyst amount, weight of hydrocarbon produced per unit reaction time) Is 207 g / kg-cat / h. On the other hand, when it prepared using the solution containing a chelating agent, productivity improved. In particular, in the catalyst to which CyDTA is added, STY is increased to 815, nearly four times. This value is higher than any existing reported value. By using a chelating agent, especially CyDTA, and supporting the transition metal compound in the previous process to produce the catalyst, it is possible to develop a highly active catalyst. Successful.
Further, in Comparative Example 2 in which the chelating agent and the transition metal compound were co-impregnated and supported, the addition effect of the chelating agent as disclosed in the prior art was not confirmed. Compared to this, the activity was extremely high. From these results, the usefulness of the present invention was confirmed.

  By using the carbon monoxide reduction catalyst of the present invention, a hydrocarbon, which is a main product of the carbon monoxide reduction reaction, particularly a useful C10 to C20 fraction is produced with extremely high productivity. It can be suitably used in industries used as fuels or chemical raw materials, that is, energy-related industries and chemical industries.

Claims (11)

  (1) a step of impregnating a metal oxide as a carrier with a chelating agent, (2) a step of drying the metal oxide impregnated with the chelating agent, (3) a transition to a metal oxide impregnated with the chelating agent and dried Impregnating the solution containing the metal compound, (4) drying the metal oxide impregnated with the solution containing the transition metal compound, and (5) impregnating and drying the solution containing the transition metal compound. A carbon monoxide reduction catalyst, which is produced through a process including steps of firing a metal oxide.   The catalyst for carbon monoxide reduction according to claim 1, wherein the chelating agent is nitrilotriacetic acid and / or trans-cyclohexanediaminetetraacetic acid.   The catalyst for reducing carbon monoxide according to claim 1 or 2, wherein the metal oxide is silica or alumina.   4. The monoxide according to claim 1, wherein the amount of the transition metal compound supported on the basis of the mass of the metal oxide is 1 to 40 mass% as a transition metal atom. Carbon reduction catalyst.   The said chelating agent is used in the ratio of 0.1-20 mol per mol of transition metal atoms in the said transition metal compound, The carbon monoxide reduction object of any one of Claims 1-4 characterized by the above-mentioned. catalyst.   The catalyst for reducing carbon monoxide according to any one of claims 1 to 5, wherein the transition metal compound is a nitrate and / or an acetate.   The catalyst for reducing carbon monoxide according to any one of claims 1 to 6, wherein the transition metal is cobalt.   It manufactures by the manufacturing process provided with the process of baking the said metal oxide before the process (1) of impregnating the said chelating agent with the said chelating agent. The catalyst for carbon monoxide reduction described in 1.   (1) a step of impregnating a metal oxide as a carrier with a chelating agent, (2) a step of drying the metal oxide impregnated with the chelating agent, (3) a transition to a metal oxide impregnated with the chelating agent and dried Impregnating the solution containing the metal compound, (4) drying the metal oxide impregnated with the solution containing the transition metal compound, and (5) impregnating and drying the solution containing the transition metal compound. A process for producing a catalyst for carbon monoxide reduction, which is produced through a process including steps of firing a metal oxide.   A method for producing hydrocarbons by reduction of carbon monoxide, wherein the catalyst for reducing carbon monoxide according to any one of claims 1 to 8 is used.   The reduction conditions for carbon monoxide are as follows: reaction temperature 200 to 500 ° C., W / F = 0.5 to 10 g · h / mol, pressure 0.1 to 20 MPa, hydrogen / carbon monoxide ratio = 1.0 to 4.0. It is (molar ratio), The manufacturing method of the hydrocarbon of Claim 10 characterized by the above-mentioned.