Catalyst – solid sorbent – or support therefor: product or process – Catalyst or precursor therefor – Silicon containing or process of making
Reexamination Certificate
2000-09-08
2002-06-25
Bell, Mark L. (Department: 1755)
Catalyst, solid sorbent, or support therefor: product or process
Catalyst or precursor therefor
Silicon containing or process of making
C502S241000, C502S242000, C502S243000, C502S246000, C502S254000, C502S255000, C502S256000, C502S257000, C502S258000, C518S713000, C518S714000, C518S715000, C518S726000
Reexamination Certificate
active
06410477
ABSTRACT:
BACKGROUND OF THE INVENTION
The present invention relates to a hydrogenation catalyst of carbon monoxide and a method of manufacturing a hydrogenation product primarily containing gasoline fuel oil and diesel fuel oil.
Fuel oil manufactured from a gas mixture (synthetic gas) of carbon monoxide and hydrogen does not contain sulfur which forms sulfur oxide and aromatic hydrocarbon (aromatic) which generates soot and is carcinogenic, unlike fuel oil refined from petroleum. Hence, this type of fuel oil is attracting attention as low-environmental-load, high-quality fuel replacing petroleum fuel.
A hydrogenation product containing the above fuel oil component is conventionally manufactured by reacting the synthetic gas described above at a predetermined temperature and a predetermined pressure in the presence of a catalyst which is formed by causing silica or alumina to carry cobalt or iron. However, this method is not necessarily satisfactory in the manufacture of target components (e.g., gasoline fuel oil components or diesel fuel oil components) at higher selectivity than other components (e.g., methane).
BRIEF SUMMARY OF THE INVENTION
It is an object of the present invention to provide a hydrogenation catalyst of carbon monoxide, which is suited to the manufacture of a hydrogenation product containing target components (e.g., gasoline fuel oil components or diesel fuel oil components) at high selectivity from a gas mixture of hydrogen and carbon monoxide.
It is another object of the present invention to provide a method of manufacturing a hydrogenation product, capable of manufacturing a hydrogenation product containing target components (e.g., gasoline fuel oil components or diesel fuel oil components) at high selectivity from a gas mixture of hydrogen and carbon monoxide.
According to the present invention, there is provided a hydrogenation catalyst of carbon monoxide, comprising a transition metal and a porous material carrying the transition metal, the porous material having pores, 90% or more of which are fine pores each having a diameter of 1 to 50 nm.
According to the present invention, there is provided a method of manufacturing a hydrogenation product, comprising reacting a gas mixture containing carbon monoxide and hydrogen at a temperature of 200 to 400° C. and a pressure of 0.1 to 10 MPa in the presence of a catalyst in which a transition metal is carried by a porous material in which 90% or more of all pores are fine pores each having a diameter of 1 to 50 nm.
Additional objects and advantages of the invention will be set forth in the description which follows, and in part will be obvious from the description, or may be learned by practice of the invention. The objects and advantages of the invention may be realized and obtained by means of the instrumentalities and combinations particularly pointed out hereinafter.
DETAILED DESCRIPTION OF THE INVENTION
The present invention will be described in detail below.
A hydrogenation catalyst of carbon monoxide according to the present invention has a structure in which a transition metal or a noble metal is carried by a porous material in which 90% or more of all pores are fine pores each having a diameter of 1 to 50 nm.
This porous material is made of pure silica or a material formed by introducing a metal such as aluminum or gallium to pure silica as a base.
The “pore diameter” is the peak top of the distribution of pore diameters measured.
By defining the dimensions of fine pores and the fine pore distribution of the porous material within the above ranges, the transition metal can be carried as it is kept fine and uniformly dispersed. It is preferable that 90% or more of all pores in the porous material are fine pores each having a diameter of 1 to 10 nm. Known examples of this silica porous material include MCM-41 developed by Mobil Oil, FSM-16 developed by Tokyo University and Toyota Central Laboratory, and SBA-15 developed by Stanford University. MCM-41 is manufactured, for example, by hydrothermally synthesizing sodium silicate and hexadecyltrimethylammoniumbromide as a silica source and a surfactant (template), respectively, at 120° C. in a pressure reaction vessel (autoclave).
As the transition metal, it is possible to use cobalt, nickel, iron, copper, chromium, manganese, zirconium, molybdenum, tungsten, rhenium, osmium, iridium, palladium. silver, ruthenium, rhodium, gold, and platinum. Cobalt, iron, ruthenium, rhodium, and platinum arc particularly preferable.
When the transition metal is cobalt or iron, this transition metal is preferably loaded within the range of 5 to 40 wt % by the porous material. When the transition metal is a noble metal selected from ruthenium, rhodium, and platinum, this transition metal is preferably loaded within the range of 1 to 15 wt % by the porous material. If the loaded amount of the transition metal is less than the lower-limit value of the above range, during the reaction of a gas mixture of hydrogen and carbon monoxide the conversion (to be described later) of carbon monoxide may decrease. On the other hand, if the loaded amount of the transition metal exceeds the upper-limit value of the above range, the conversion of carbon monoxide corresponding to this loaded amount cannot be expected.
The aforesaid hydrogenation catalyst of carbon monoxide is manufactured by, e.g., the IMP method or the TIE method described below.
(IMP method)
First, a porous material such as MCM-41 is air-calcined to remove any residual surfactant (template) by burning at a temperature of 500 to 600° C. Subsequently, the calcined porous material is dipped into an aqueous solution of a transition metal compound and impregnated with this aqueous solution. After that, the porous material is again dried and calcined at a temperature of 500 to 600° C. to manufacture a target catalyst.
(TIE method)
First, a porous material such as uncalcined MCM-41 is added to an aqueous solution of a transition metal compound, and the porous material and the aqueous solution are mixed. Since some surfactant (template) remains in the porous material, transition metal ions and template ions are exchanged. Subsequently, the mixture is dried and calcined at a temperature of 500 to 600° C. to remove the template by burning, thereby manufacturing a target catalyst.
Of the above hydrogenation catalyst manufacturing methods, in a catalyst formed by the TIE method, pores of the porous material do not collapse in the step of carrying the transition metal, and pores within a predetermined range are regularly arranged. That is, a catalyst formed by this TIE method is preferable in that it can carry a large amount of transition metal while the pore structure of the porous material before the transition metal is loaded is maintained.
A method of manufacturing a hydrogenation product according to the present invention will be described below.
In the presence of the above-mentioned catalyst in which a transition metal is carried by a porous material in which 90% or more of all pores are fine pores each having a diameter of 1 to 50 nm, a gas mixture of hydrogen and carbon monoxide is reacted at a temperature of 200 to 400° C. and a pressure of 0.1 to 10 MPa to manufacture a hydrogenation product containing gasoline fuel oil components or diesel fuel oil components.
More specifically, the catalyst in the form of, e.g., a powder is packed into a cylindrical stainless-steel high-pressure reaction tube, and this reaction tube is heated by a heater placed outside the reaction tube such that the internal temperature of the tube is 200 to 400° C. In this state, a high-pressure gas mixture (0.1 to 10 MPa) of hydrogen and carbon monoxide is supplied to manufacture a hydrogenation product.
Alternatively, a slurry formed by dispersing the powdery catalyst in a high-boiling organic solvent is placed in a high-pressure tank having an entrance and exit. While this high-pressure tank is heated by a heater placed outside the tank such that the internal temperature of the tank is 200 to 400° C., a high-pressure gas mixture (0.1 to 10 MPa) containing hydro
Ohtsuka Yasuo
Wang Ye
Yamada Muneyoshi
Bell Mark L.
Hailey Patricia L.
Oblon & Spivak, McClelland, Maier & Neustadt P.C.
President of Tohoku University
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