Catalysts

专利摘要:

公开号:BR112013030533B1
申请号:R112013030533-9
申请日:2011-04-28
公开日:2018-07-03
发明作者:Albertus Jacobus Sandee；Robert Johan Andreas Maria Terorde
申请人:Sasol Technology (Proprietary) Limited；Basf Nederland B.V.；
IPC主号:

专利说明:

(54) Title: CATALYSTS (51) Int.CI .: B01J 23/72; B01J 23/75; B01J 23/755; B01J 23/89; B01J 37/02; B01J 37/06; B01J 37/08; B01J 37/18; C10G 2/00; B01J 35/00 (73) Holder (s): SASOL TECHNOLOGY (PROPRIETARY) LIMITED. BASF NEDERLAND B.V.
(72) Inventor (s): ALBERTUS JACOBUS SANDEE; ROBERT JOHAN ANDREAS MARIA TERORDE “CATALYSTS”
This invention relates to catalysts. In particular, it refers to a process for the preparation of a catalyst precursor, and a process for the preparation of a catalyst, such a catalyst can be used, for example, in hydrogenation reactions, which include hydrocarbon synthesis (for example , Fischer-Tropsch (FT) synthesis) and which include other hydrogenation reactions, such as the hydrogenation of organic compounds.
Description of the State of the Art
The preparation of catalyst precursors by means of metal impregnation on catalyst supports using various impregnation techniques is well known for the elements skilled in the art. The impregnated supports thus obtained are then usually subjected to drying and calcination to provide catalyst precursors, and the precursors are then subjected to reduction to produce, finally, a catalyst.
The document under on ^e . EP-A-0 736 326 describes Fischer-Tropsch synthesis catalysts based on cobalt-impregnated alumina synthesized through aqueous slurry phase impregnation of a cobalt salt, for example, cobalt nitrate hexahydrate, on a alumina support, coupled with drying the impregnated support, followed by calcination of the fluidized bed directly from the resulting impregnated support, to obtain a catalyst precursor and then reducing the precursor to obtain the Fischer-Tropsch synthesis catalysts. These catalysts contain cobalt dispersed on the support. Larger cobalt loads, which result in larger catalyst activities, can be achieved by repeating the cobalt salt impregnation step. However, this has a negative impact on the total costs of the catalyst manufacturing process and the time required to prepare the catalyst. In addition, the maximum amount of metal that can be deposited per impregnation step is limited by the pore volume of the support.
Alternatively, suitable Fischer-Tropsch catalysts with high cobalt loads can be prepared by grinding or kneading alumina (EP-A-0 455 307), silica (EP-A-0 510 771) or zirconia (EP- A-0 510 772) with a source of soluble or insoluble cobalt. In this way, a paste can be obtained which is extruded, dried and calcined in order to obtain a catalyst or catalyst precursor. Especially in the case of an insoluble cobalt source, such as Co (OH) ₂ , a high cobalt charge can be obtained in this way. In this approach, the final shape of the support is determined during the catalyst preparation process. As a result, the mechanical strength and physical shape of the substrate cannot be predefined. In addition, in order to obtain mechanically strong catalysts according to these known methods, the extrudates have to be calcined at relatively high temperatures. The disadvantages of such high calcination temperatures are that the catalyst performance is adversely affected. An additional disadvantage of crushing or kneading is that delamination agents are often required. Such compounds give rise to an exothermic combustion with an exhaust of polluting volatile organic compounds.
Another additional alternative method of obtaining high cobalt fillers consists of the precipitation of an insoluble cobalt compound with the use of an excess alkaline precipitation agent, subsequently deposited on a support through the addition of an aluminum compound. soluble, such as sodium aluminate (WO-A2006 / 021754). The precipitation of a cobalt compound at a pH of> 8 on a solid support, such as Kieselguhr (WO-A-01/28962) by adding a base, has also been reported. In such cases, Co (NC> 3) ₂ is often used as a starting compound which is suggested to have precipitated on the support as a kind of cobalt hydroxide (Appl. Catai. A: Gen. 311 (2006), 146). The disadvantage of precipitation processes that require chemical treatment, such as the addition of a base, is the production of residues, such as salts. This requires excessive washing or filtration steps in the preparation process. In addition, such processes do not ensure sufficient mechanical strength of the catalyst to avoid problems downstream with respect to friction issues.
Hence, there is a need for hydrogenation catalysts, which include Fischer-Tropsch catalysts, with heavy fillers of active catalyst component, such as cobalt, obtained by a simple preparation process that allows for mechanically strong preformed supports to be used. and that avoids or at least reduces the use of chemical treatments, such as adding a base, or other disadvantages as described above.
Objectives and brief description of the invention
Thus, according to a first aspect of the invention, a process is provided for the preparation of a catalyst precursor, such a process includes forming a particulate slurry of an insoluble metal compound, where the metal of the insoluble metal compound consists into an active catalyst component, with particles and / or one or more bodies of a preformed catalyst support in a carrier liquid, with the particles of the insoluble metal compound being thus placed in contact with the particles and / or the one or more bodies of the preformed catalyst support, to thereby produce a treated catalyst support; and removing the carrier liquid from the slurry to obtain a dry treated catalyst support, which either directly constitutes the catalyst precursor or is optionally calcined to obtain the catalyst precursor.
Thus, it will be appreciated that, in some embodiments of the invention, the treated catalyst support does not need to be calcined and thus forms or constitutes the catalyst precursor directly. However, in other embodiments of the invention, it will be necessary to first calcine the treated catalyst support in order to obtain the catalyst precursor.
By "active catalyst component" is meant that the metal of the insoluble metal compound is such that it actively catalyzes chemical reactions in which an eventual catalyst obtained from the catalyst precursor is used as a catalyst.
In this specification, the terms “insoluble metal compound” or insoluble metal salt refer to a metal compound or metal salt, respectively, in relation to the fact that there is no dissolution or only very low levels of dissolution in the liquid used carrier. It is preferred that its solubility constant (K _sp at 25 ° C) in the carrier liquid is below 1.10 ⁸ , preferably below 1.10 ^'12 . For example, the K _sp at 25 ° C of cobalt hydroxide in water is 1.09.10 ^'15 , of nickel hydroxide in water is 5.47.10' ¹⁶ , of manganese hydroxide is 2.06.10 ^-13 and of copper hydroxide in water is 2.2.10 ^-20 .
The insoluble metal compound preferably consists of an insoluble metal salt, more preferably an insoluble inorganic metal salt.
In this specification, the term “inorganic metal salt” refers to a salt in which at least one metal atom is only associated with one or more organic groups, such an association is by means of a bond, for example, by means of a covalent bond, a metal-to-ligand coordination or an ionic interaction.
In this specification, the term “slurry” is understood in terms of its general meaning as being a multiphase system of solid particles suspended in a carrier liquid. The weight ratio of carrier liquid to dry solids mass, i.e. particles of insoluble metal compound plus particles / catalyst support bodies, can be at least 1: 1, typically about 2: 1.
The contact of the particles of the insoluble metal compound with the particles and / or the one or more bodies of the preformed catalyst support may be carried out for a period of time, preferably for at least 1 minute, more preferably for at least 10 minutes and even more preferably, for at least 15 minutes, and most preferably, for at least 20 minutes, but preferably for no more than 48 hours, more preferably, for no more than 36 hours, even more preferably, for no more than 20 hours, and most preferably, for no more than 2 hours, before removal of the carrier liquid is started.
The process may include contacting the particles of the insoluble metal compound with the particles and / or the one or more bodies of the preformed catalyst support at an elevated temperature above 25 ° C, preferably above 50 ° C ; preferably, however, the elevated temperature is below 100 ° C.
The process may include bringing the preformed catalyst support and / or the treated catalyst support and / or the dry treated catalyst support and / or the calcined treated catalyst support, into contact at least once with a soluble metal compound. The metal of the soluble metal compound can also consist of an active catalyst component. The soluble metal compound can in particular consist of a soluble metal salt.
A "soluble metal compound" or "soluble metal salt" consists of a metal compound or salt, respectively, that does not consist of an insoluble metal salt or compound. It is preferred that the soluble metal compound / salt has a solubility, in the liquid that is in use to be dissolved, above 25g / 100 ml of liquid, preferably above 100g / 100 ml of liquid, at 25 ° C . For example, the solubility of cobalt nitrate in water is 133.8g / 100 ml, of nickel nitrate in water is 238.5g / 100 ml, of copper nitrate in water is 243.7g / 100 ml and of manganese nitrate is 426.4 g / 100 ml, all at 25 ° C.
The soluble metal salt, when used, can thus be brought into contact at least once with the particles of the insoluble inorganic metal salt and / or with the preformed catalyst support particles. In this way, it can form part of the slurry, that is, it can be dissolved in the carrier liquid. On the contrary, however, the treated catalyst support can be brought into contact at least once with the soluble metal salt, for example, with a solution separate from the soluble metal salt. In cases where the treated catalyst support is calcined to form the catalyst precursor, the calcined treated catalyst support, that is, the catalyst precursor, can even be brought into contact at least once with the soluble metal salt solution. .
Formation of the slurry may include adding the insoluble metal salt particles and / or the preformed catalyst support particles to the carrier liquid to form a mixture which is mixed in order to suspend the particles in the carrier liquid. This mixture may consist of a low shear mixture. It should be noted that the consistency of the slurry is (its viscosity is low enough) in such a way that neither crushing nor kneading nor extrusion can be carried out. In addition, the mixture, especially low shear mixture, does not constitute crushing or kneading.
The process can then include, as a pretreatment step, bringing the insoluble metal salt particles and / or catalyst support particles into contact with the soluble metal salt, for example, with a solution of the soluble metal salt .
More particularly, the slurry can be formed by first forming a suspension of the insoluble inorganic metal salt particles in the carrier liquid and then adding the preformed catalyst support particles and / or bodies to the suspension to form the slurry.
It is preferred that the particles of the insoluble inorganic metal salt are added to the carrier liquid to form a suspension. The preformed catalyst support can be added to the carrier liquid before and / or during and / or subsequent to the formation of the suspension, to form the slurry. It will be observed, therefore, that the insoluble inorganic metal salt particles do not form in situ; the suspension is formed by mixing pre-existing insoluble inorganic metal salt particles with the carrier liquid.
The metals in the metal salts, i.e., the insoluble inorganic metal salt and the soluble metal salt, can be independently selected, and can be the same or different metals. It is preferred, however, that they consist of the same metal. Metals suitable for the purpose of the present invention can be selected from the group consisting of Groups Ib, llb, Vb, Vlb, Vllb and VIII of the periodic table of elements. Most preferably, they are selected from cobalt, nickel, ruthenium, manganese, iron, copper, zinc, molybdenum, a precious metal, and combinations of two or more of the same. Cobalt, nickel and copper are particularly suitable for the preparation of a hydrogenation catalyst precursor according to the process of the present invention. For cobalt-based catalyst precursors, cobalt is preferably used in combination with it.
The insoluble inorganic metal salt can, at least in principle, consist of any insoluble inorganic metal salt; however, metal carbonate salts and, in particular, metal hydroxide salts, are preferred. The metal of the insoluble inorganic metal salt is preferably selected from the group consisting of cobalt, copper, nickel, manganese, or combinations of two or more thereof. When the metal in the insoluble inorganic metal salt consists of cobalt, cobalt hydroxide, cobalt carbonate and, in particular, Co (OH) ₂ , they are preferred.
The soluble metal salt is therefore preferably such that its metal is also an active catalyst component. The soluble metal salt can be an inorganic metal salt and / or an organic metal salt. Combinations of different soluble metal salts, for example,
I salts of different metals or salts with different organic or inorganic anions can be used.
In this specification, the term "organic metal salt" refers to a compound in which at least one metal atom is associated with at least one organic group through a bond, for example, through a covalent bond, a metal coordination for binder or an ionic interaction. It is preferred that the metal atom is associated with at least one atom other than carbon than at least one organic group, in particular, with an oxygen atom of the organic group. The organic metal compound can also include one or more organic groups attached to the metal. It is preferred that the one or more organic groups are cationic groups.
When a soluble inorganic metal salt is used, it can consist, at least in principle, of any soluble inorganic metal salt.
Suitable soluble metal salts include ammonium nitrates, sulfates, chlorides and citrates, preferably ammonium nitrates, acetates and citrates. The metal in the soluble metal salt is preferably selected from the group consisting of cobalt, copper, nickel, manganese, or combinations of two or more thereof. When a soluble inorganic metal salt is used, and its metal is cobalt, Co (NO3) 2.6H ₂ O is preferred.
When a soluble organic cobalt salt is used, it can consist of that obtained by reacting a cobalt compound, such as cobalt hydroxide or cobalt nitrate, with an organic acid, optionally, in the presence of at least one source of counterion . The cobalt compound therefore preferably consists of a basic cobalt compound.
The counterion source, when present, preferably consists of an inorganic source, and is preferably a source of one or more cations. In one embodiment of the invention, the counterion source may be ammonia.
The organic cobalt salt can be formed in situ. In this way, the cobalt compound, for example, cobalt hydroxide, can be dissolved in a solution of the organic acid in water.
* t
Organic acid can consist of a carboxylic acid, such as acetic acid, citric acid (CgHgOz), succinic acid (C ₄ H ₆ O ₄ ), oxalic acid (C2H2O4), acetic acid (C ₂ H ₄ O ₂ ), gluconic acid (0 ₆ Ηι ₂ 0 ₇ ) or EDTA, that is, ethylenediaminetetraacetic acid. It is preferred that the organic acid consists of citric acid.
In the organic cobalt salt solution, the molar ratio of cobalt to organic acid can vary widely, for example, from 0.1.1 to 10: 1. However, the molar ratio of cobalt to organic acid is normally expected to be in the range of 0.5: 1 to 2: 1, typically about 1: 1.
In the preferred embodiments of the invention, the organic cobalt salt may be ammonium cobalt citrate or ammonium cobalt EDTA.
In contrast, the organic cobalt salt may consist of that obtained by reacting a cobalt compound with acetylacetone (C ₅ H ₈ O ₂ ).
In a preferred embodiment, the sufficient insoluble inorganic metal salt and, optionally, soluble metal salt can be used so that the resulting amount of active metal component in proportion to the support in the catalyst precursor is between 5 and 90% by weight preferably between 10 and 70% by weight, with the greatest preference between 10 and 70%
0 50% by weight, based on the total mass of precursor.
The process may include subjecting the catalyst precursor, i.e., the treated catalyst support, to further treatment by forming a particle slurry from the treated catalyst support, particles of an insoluble metal salt and a carrier liquid, removing the carrier liquid from the slurry and, optionally, calcining the additional treated particles thus obtained, to obtain the catalyst precursor.
In specific embodiments of the invention as described in accordance with this document, particles of the preformed catalyst support are used. However, it should be noted that, in other embodiments of the invention, the same principles can be applied to the bodies of the preformed catalyst support.
In a first embodiment of the invention, the slurry formation may comprise suspending the particles of metal compound insoluble in the carrier liquid to form a suspension, and adding the particles of the preformed catalyst support to the carrier liquid before and / or during and / or subsequent to the formation of the suspension, to form the slurry, with the active catalyst component, i.e., the metal of the insoluble metal compound, being deposited on the support particles. It is preferred that no soluble metal compound is included in the slurry. It is preferred that the deposition can be by means of chemisorption, preferably at a neutral or slightly acidic pH value, typically in the range of 8 to 2. The effect of chemisorption in this process is expressed by a change in pH value. This modality is, therefore, characterized so that only the chemisorption is carried out.
Without sticking to the theory, it is believed that, during chemisorption, the deposition of a molecule of the active catalyst component on the support is achieved by the formation of a chemical bond between the support and the molecule. Also without sticking to the theory, it is believed that this chemical bond is most likely the result of a condensation reaction.
In a second embodiment of the invention, the slurry formation may comprise suspending the particles of metal compound insoluble in the carrier liquid to form a suspension, and adding the particles of the preformed catalyst support to the carrier liquid before and / or during and / or subsequent to the formation of the suspension, to form the slurry, with the metal of the insoluble metal compound being deposited on the support particles, preferably by means of chemisorption; and the second embodiment of the invention, which additionally includes, after removing carrier liquid from the slurry, bringing the treated dry catalyst support into contact with the soluble metal compound by treating the treated dry catalyst support at least once with a solution of the metal compound soluble in a carrier liquid, with the metal of the soluble metal compound being deposited within and / or on the support particles, preferably by impregnation. It is preferred that no soluble metal compound is included in the slurry. During the formation of the slurry, there is, therefore, a first step in the process, the deposition of a first part of an active catalyst component on the support particles. This deposition can be by means of chemisorption, as described in the present document in relation to the first embodiment of the invention. However, in this embodiment of the invention, the treated catalyst support particles thus obtained are then, with or without calcination, subjected to further treatment by placing them at least once, in an additional process step. , in contact with a solution of the metal salt soluble in a carrier liquid with the metal of the soluble metal salt which thus also consists of an active catalyst component and in which the metal of the soluble metal salt impregnates the particles of treated substrates, thus forming a second part of the active metal component. The impregnated and chem-vivid support is then calcined and the catalyst precursor thus obtained.
This second embodiment of the invention is thus characterized by the fact that the chemisorption and impregnation is strictly carried out using the metal chemisorption sequence first with the insoluble metal salt and, subsequently, the impregnation with the soluble metal salt. .
In a third embodiment of the invention, the slurry formation may comprise forming a solution of the metal compound soluble in the carrier liquid, suspending the particles of inorganic metal compound insoluble in the carrier liquid to form a suspension, and adding the particles of the backing support. catalyst preformed to the carrier liquid before and / or during and / or subsequent to the formation of the suspension, to form a
- A slurry, with the metal of the insoluble metal compound being deposited on the support particles, preferably by means of chemisorption, while the metal of the soluble metal compound is deposited inside and / or on the support particles, preferably by means of impregnation. The metal in the soluble metal salt, then, also consists of an active catalyst component. The active metal component is, therefore, at the same stage of the process, deposited by means of chemisorption and is also impregnated on and in the support to form the treated catalyst support, which is then calcined to obtain the precursor of catalyst.
This third embodiment of the invention is thus characterized by the fact that the chemisorption and impregnation are carried out simultaneously, that is, at the same stage of the process.
It is preferred that the impregnated support be subjected to removal of carrier liquid at least partial before calcination.
Thus, the preferred way of depositing the metal of the insoluble metal salt on the preformed catalyst support is by means of chemisorption; the preferred way of depositing the metal of the soluble metal compound on the preformed catalyst support is by impregnation.
Surprisingly, it has been found that with a process according to the invention, which preferably includes at least one chemisorption step and an impregnation step, a high dispersion of metal, for example, cobalt, is usually obtained and at the same time time, a high charge of metal, for example, cobalt, can be achieved, usually with increased catalyst activity compared to the standard way of preparing such catalysts by depositing only inorganic metal salts, for example, inorganic cobalt salts through of impregnation. In addition, the process of the invention provides catalytic materials at low calcination temperatures, excluding exotherms.
A promoter can also be introduced on and / or into the catalyst support particles by pretreating the catalyst support particles before the slurry is formed or, preferably, by adding the promoter, or a precursor to the catalyst. even to the slurry. When present, the promoter preferably consists of one that is able to optimize the reducibility of the active catalyst component. The promoter can be introduced as a promoter compound or precursor which is a compound of a metal selected from the group consisting of palladium (Pd), platinum (Pt), ruthenium (Ru), rhenium (Re), Rhodium (Rh ) and a mixture of one or more of them. It is preferred that the promoter compound consists of an inorganic or organic salt and is preferably soluble in water. It is preferred that the promoter consists of an acetate, acetyl acetonate, nitrate or nitrosyl nitrate. The ratio of mass of the metal of the promoter to mass of metal of active component can be in the ratio of 1: 5 to 1: 10000. The mass ratio of the promoter metal (especially palladium or platinum) to the metal mass of the active component (especially cobalt) can be in the ratio of 1: 300 to 1: 3000. The mass ratio of the promoter metal (rhenium) to the metal mass of the active component (especially cobalt) can be in the ratio of 1: 5 to 1: 300.
The carrier liquid can therefore consist of any liquid solvent suitable for the soluble metal salt, provided that the insoluble inorganic metal salt is certainly insoluble therein. However, it preferably consists of water.
In this specification, the term "pre-formed catalyst support" refers to the fact that the shape of the catalyst support is determined by the catalyst support used and remains essentially the same during the process of preparing the catalyst precursor, that is, it is not transformed or altered during the catalyst precursor preparation process. In particular, there is therefore no shaping of the catalyst support after it has been brought into contact with the insoluble metal salt.
The preformed catalyst support can be porous. It can be selected from the group consisting of a monolith, structured fillers, tablets, shaped artifacts, extrudates, spheres, or combinations of two or more of them. In other words, when the preformed catalyst support is in the form of one or more bodies, the bodies can be monoliths; however, when the pre-shaped catalyst support is in the form of particles, the particles can consist of structured fillers, tablets, shaped artifacts, extrudates, spheres, or combinations of two or more of them. However, spherical preformed catalyst support particles are preferred; they can have an average particle size of 50 to 150 micrometers.
Optionally, the support used in the slurry may have undergone, as a pre-treatment, a chemical modification. Such chemical modification means that the support could be pre-treated (i) being coated with another chemical inorganic material, such as, without limitation, silica, alumina, zeolitic or zirconia coating, or (ii) being impregnated with an organic material, which facilitates the dispersion of metal, or (iii) be impregnated with a metal salt. Organic materials suitable for use in (ii) are widely known in the field and include materials such as organic acids, sugars or sugar alcohols, polyols or detergents, preferably detergents are non-ionic. Metal salts suitable for use in (iii) include some alkali metals, alkaline earth metals, rare earth metals or transition metals, and can be impregnated to specifically alter the acid-base properties of the support and the final catalyst. In addition, impregnations with molybdates or tungstates, especially ammonium para-molybdate, can also be performed. Optionally, such additional impregnations with metal salts can, on the contrary, occur in the treated catalyst support particles, before or after calcination.
Preformed or preformed catalyst support particles may preferably have an average pore diameter between 8 and 50 nanometers, more preferably between 10 and 15 nanometers. The support pore volume can be between 0.1 and 1 ml / g of catalyst support, preferably between 0.3 and 0.9 ml / g of catalyst support. The pre-formed support may consist of a particulate support, preferably with an average particle size between 1 and 500 microns, preferably between 10 and 250 microns, more particularly between 45 and 200 microns. The forming of a preformed support with particle sizes between 1 and 500 micrometer can be done by means of spray drying. After spray drying, this shaped support can be calcined.
The preformed catalyst support can be selected from the group consisting of alumina in the form of one or more oxides of aluminum, silica, titania, zirconia, magnesia, zinc oxide, activated carbon, molecular sieves, in particular, zeolites , and mixtures or combinations thereof. It is preferred that the support is selected from the group consisting of alumina in the form of one or more aluminum oxides; titania and silica. Typically, the support consists of alumina in the form of one or more aluminum oxides. The one or more aluminum oxides can be selected from the group that includes (preferably, consisting of) gamma alumina, delta alumina, theta alumina and a mixture of two or more of them. It is preferred that the group includes or, preferably, consists of gamma alumina, delta alumina and a mixture of gamma alumina and delta alumina. The aluminum oxide catalyst support can consist of one obtainable under the trademark Puralox, preferably Puralox SCCa available from SASOL Germany GmbH. Puralox SCCa (trademark) consists of a spray-dried aluminum oxide support consisting of a mixture of gamma and delta aluminum oxide or Al 4505 available from BASF Germany GmbH. Al 4505 is available as a powder and conformed, for example, as AI4505 T1 / 8, as tablets.
Aluminum oxide preferably consists of a crystalline compound that can be described by the formula AI2O3.XH2O where 0 <x <1. The term aluminum oxide thus excludes AI (OH) ₃ , and AIO (OH) , but includes compounds such as gamma, delta and theta alumina.
It is preferred that the catalyst support includes one or more modifying components. This is particularly the case where the support base, that is, the support excluding the modifying component, is soluble in a neutral and / or acidic aqueous solution, or where the support base is susceptible to hydrothermal attack as described below.
The modification component can comprise a component that results in one or more of the following:
(i) decreases the dissolution of the catalyst support in an aqueous environment, (ii) suppresses the susceptibility of the catalyst support to hydrothermal attack (especially during Fischer-Tropsch synthesis);
(iii) increases the pore volume of the catalyst support;
(iv) increases the strength and / or friction and / or abrasion resistance of the catalyst support.
In a preferred embodiment of the invention, the modifying component decreases the dissolution of the catalyst support in an aqueous environment, that is, it increases the inertia of the catalyst support towards dissolution in an aqueous environment and / or suppresses the susceptibility of the catalyst support. catalyst to hydrothermal attack, especially during Fischer-Tropsch synthesis. Such an aqueous environment can include an aqueous acidic solution and / or a neutral aqueous solution, especially such an environment encountered during an aqueous phase impregnation catalyst preparation step. The hydrothermal attack can cause the catalyst support to sinter (for example, aluminum oxide), dissolve Al ions or decompose the catalyst particles during hydrocarbon synthesis, especially Fischer-Tropsch synthesis, due to exposure to high temperature and water.
The modifying component is typically present in an amount that results in a level of the same in the catalyst support of at least 0.06 atoms per square nanometer.
The modification component can be selected from the group consisting of Si, Zr, Co, Ti, Cu, Zn, Mn, Ba, Ni, Na, K, Ca, Sn, Cr, Fe,
Li, Ti, Sr, Ga, Sb, V, Hf, Th, Ce, Ge, U, Nb, Ta, W, La and mixtures thereof.
The modification component can, more particularly, be selected from the group consisting of Si; Zr; Ass; Zn; Mn; Ba; Over there; You; W; Ni and mixtures thereof. It is preferred that the modifying component is selected from the group consisting of Si and Zr. In a preferred embodiment of the invention, the modifying component is Si.
When the modifying component is Si, the level of silicon in the resulting catalyst support is in an amount of at least 0.06 Si atoms per square nanometer of the catalyst support, preferably at least 0.13 Si atoms per square nanometer of the catalyst support, and more preferably, at least 0.26 Si atoms per square nanometer of the catalyst support.
It is preferred that the upper level is 2.8 Si atoms / nm ² of the catalyst support.
The modified aluminum oxide catalyst support can consist of that obtainable under the trademark Siralox, obtainable from Sasol Germany GmbH, containing between 1.4 and 2.2% by weight of Si.
In another embodiment of the invention, the catalyst support is in the form of one or more aluminum oxides or a modified aluminum oxide
5 with silica and is preferred over supports, such as silica and titania, since these supports are believed to provide a much more resistant to friction catalyst. The catalyst support in the form of one or more aluminum oxides or a silica-modified aluminum oxide can also include La. La is believed to improve frictional resistance.
In an additional embodiment of the invention, the
1U catalyst is in the form of one or more aluminum oxides or a silica-modified aluminum oxide may include titanium, preferably in an amount, expressed as elementary titanium, of at least 500 ppm by weight, preferably from about 1000 ppm to about 2000 ppm by weight.
Addition of titanium to the catalyst support is believed to increase the activity of a formed catalyst, especially in the case of a cobalt FT catalyst, particularly when no prime metal promoters and, preferably, no Re or Ta promoters are present. in the catalyst. It is preferred that the titanium is included in the internal structure of the support and, preferably, no titanium is present as a deposit on the support. It is believed that the presence of this titanium in the support also improves the resistance to friction of a catalyst that includes such support.
In yet another embodiment of the invention, the catalyst support may be in the form of porous particles coated with carbon. In an alternative embodiment of the invention, the porous particles can, however, be free of such a carbon coating.
The catalyst support can be modified by introducing a modification component precursor that includes a modification component, as described earlier in that
The document, on and / or inside a catalyst support material.
Removing the carrier liquid from the slurry may include subjecting the slurry to drying and / or filtration. When drying is employed, drying by heat treatment, i.e., at an elevated temperature, is preferred.
The chemisorption, as previously described, is carried out, therefore, by mixing the slurry phase with the use of a slurry composed of the pre-formed support and the insoluble inorganic salt in the carrier liquid. It is preferred that the slurry is aqueous. After chemisorption, the remaining carrier liquid can be removed by drying above 25 ° C in subatmospheric pressure and / or can be removed by filtration.
When present, drying during impregnation can be carried out under conditions in which the soluble metal salt (inorganic or organic) will not decompose readily. It is preferred that the drying step is carried out at above 25 ° C and, preferably, at subatmospheric pressure. It is preferred that the slurry be dried at a temperature in the range of 40 ° C to 120 ° C, typically about 100 ° C, with the final pressure typically being in the range of 50 to 120 mbar, typically about 80 mbar.
During a potential repetition of the catalyst precursor chemisorption step, as described earlier in this document, the calcined treated catalyst support can be subjected to the slurry phase chemisorption, with the use of a slurry composed of the calcined treated catalyst support. and an insoluble inorganic metal salt (the metal of which consists of an active catalyst component, as described earlier in that document) in a carrier liquid. Again, after chemisorption, the residual liquid can be removed by drying at above 25 ° C in subatmospheric pressure or it can be removed by means of filtration.
Any subsequent impregnation can be carried out under conditions in which the soluble metal salt (inorganic or organic) will not readily decompose. It is preferred that the drying step is carried out at above 25 ° C and, preferably, at subatmospheric pressure.
The nitrogen content in the catalyst precursor can be less than 1 mass%, preferably less than 0.5 mass%.
Calcination, when carried out, is preferably carried out at a temperature above 25 ° C which causes the deposited and impregnated metal salts to decompose and / or react with oxygen. Calcination is therefore carried out preferably under oxidation conditions. For example, cobalt nitrate can be converted to a compound selected from CoO, CoO (OH), C03O4, C02O3 or a mixture of one or more of them.
Calcination is typically carried out in a fluidized bed, or in a rotary kiln. The at least partially dried impregnated treated catalyst support can be calcined in the air. The temperature during calcination can then be between 100 ° C to 600 ° C, preferably between 120 ° C and 350 ° C, more preferably between 150 ° C and 300 ° C, typically about 250 ° C , to obtain cobalt oxide catalyst precursors. The temperature is normally increased from room temperature, typically 25 ° C, to 200 to 350 ° C at a rate between 0.1 and 10 ° C / min., Preferably between 0.5 and 3 ° C / min . The GHSV during calcination, especially of importance in fluidized beds and in the presence of nitrate impregnations, will normally be in the range of 100 to 3000 h ' ¹ , typically around 2000 h' ¹ . More particularly, the calcination conditions in the second preparation step can be selected in such a way that, in the catalyst precursor, substantially all of the reducible metal is present in a calcined state. Apart from the methods mentioned above, calcination can also be carried out, for example, in fixed or mobile beds.
Calcination can be performed using a heating rate and a spatial speed that meets the following criteria:
(i) when the heating rate is 1 ° C / min., the spatial speed is at least 0.76 m _n ³ / (kg of Co (NO3) 2 6H2O) / h; and (ii) when the heating rate is greater than 1 ° C / min., the spatial speed satisfies the relationship:
log 20 - log 0.76 log (space speed)> log 0.76 + -log (heating ax)
According to a second aspect of the invention, a catalyst precursor is provided, which is obtained or obtainable by the process according to the first aspect of the invention, and comprises metal in an amount between 5 and 90% by weight, based on in the total mass of precursor.
The precursor preferably comprises between 10 and 70% by weight, and more preferably between 10 and 50% by weight of metal. The catalyst precursor is essentially free of exchangeable ions.
The catalyst precursor may consist of a hydrocarbon synthesis catalyst precursor. It is preferred that it can then consist of a Fischer-Tropsch synthesis catalyst precursor. More preferably, it can then consist of a slurry phase Fischer-Tropsch synthesis catalyst precursor. The salt metal / soluble metal compound can be cobalt. It is preferred that the metal of the insoluble metal salt / compound is therefore also cobalt, which thus consists of the active component of the eventual catalyst. The catalyst precursor then consists of a cobalt-based Fischer-Tropsch synthesis catalyst precursor.
However, on the contrary, the catalyst precursor may be a hydrogenation catalyst precursor suitable for the hydrogenation of organic compounds. More specifically, the catalyst precursor can then be an aromatic hydrogenation catalyst precursor, of nitro, nitrile, alkaline, alkene, diene or aldehyde compound, or a hydrodeclorination catalyst precursor. For example, the catalyst precursor may also consist of an alcohol or ammonia synthesis catalyst precursor.
When the hydrotreating catalyst precursor is cobalt-based, it can be formed in the same way as the cobalt-based Fischer-Tropsch synthesis catalyst precursor described earlier in this document. Typically, the catalyst support will be impregnated with ammonium molybdate, dried and, optionally, calcined and used as such in the invention. A similar preparation process can be applied to prepare NiMo catalysts. Cobalt and / or nickel in combination with molybdenum are particularly suitable for the preparation of a hydrotreating catalyst precursor according to the present invention, especially, this type of catalyst can be applied for HDM (hydro demetallization), HDS (hydro desulfurization) ), HDN (hydrodesnitrogenation) or for pyrolysis gas hydrogenations.
According to a third aspect of the invention, there is provided a process for preparing a catalyst, which includes preparing a catalyst precursor using the process of the first aspect of the invention, and reducing the catalyst precursor so prepared, to get a catalyst,
When the catalyst precursor consists of a hydrogenation catalyst precursor as described earlier in that document, the catalyst will then naturally be a hydrogenation catalyst. The hydrogenation catalyst can then be used for the hydrogenation of aromatics, composed of nitro, nitrile, alkaline, alkene, diene or an aldehyde or synthesis of alcohol or ammonia or hydrodeclorination or for HDM (hydro demetallization), HDS (hydro desulfurization) ), HDN (hydrodesnitrogenation) or for pyrolysis gas hydrogenations.
More particularly, the hydrogenation catalyst can then be applied very suitably to the production of fine chemicals, where it is important that high selectivity is maintained. Examples of reactions that can be catalyzed by nickel-based catalysts prepared in accordance with the present invention consist of hydrogenation, hydro-dechlorination, and the like.
In hydro-dechlorination reactions, the hydrogenation catalyst of the invention makes it possible to control the amount of hydrogen and the partial pressures of hydrogen / HCI in the system very carefully, thereby substantially improving the selectivity of the reaction.
When the catalyst precursor consists of a cobalt-based Fischer-Tropsch synthesis catalyst precursor as described earlier in that document, the catalyst will naturally be a Fischer-Tropsch synthesis catalyst.
Surprisingly, it was found that when a cobalt-based Fischer-Tropsch synthesis catalyst precursor, as shown above, is converted to a FischerTropsch synthesis catalyst by reduction, the catalyst has a high and stable Fischer activity -Tropsch. Even more surprisingly, it was found that through the use of the chemisorption-impregnation preparation process, as defined earlier in this document, not only is a desired high cobalt charge achieved, but a high degree of cobalt dispersion is also achieved ( metal and / or oxide), resulting in a catalyst with enhanced Fischer-Tropsch synthesis activity.
The catalyst precursor can be reduced or activated by any type of known reduction, preferably by placing the catalyst precursor in contact with pure hydrogen or a gas mixture containing hydrogen. The gas mixture may consist of hydrogen and one or more inert gases that are inert to the active catalyst. It is preferred that the hydrogen concentration is in the range of 0.1 to 100% and the reduction is carried out at any temperature above 100 ° C.
When the catalyst consists of a FischerTropsch catalyst, the gas mixture preferably contains at least 90% by volume of hydrogen. The reduction can be carried out at a temperature in the range from 250 ° C to 550 ° C, preferably from about 300 ° C to about 425 ° C, for a period in the range from 0.5 ha to about 24 h and at a pressure that is in the range from about 40 atmosphere to atmosphere. Suitable reduction conditions for the preparation of the catalyst of the present invention can be found in the patents under nos. ²² . WO-A-03/035257, WO-A-2008/135939, WO-A-2008/135940 and WO-A2008 / 135941.
According to a fourth aspect of the present invention, there is provided a hydrocarbon synthesis process which comprises preparing a catalyst using the process of the third aspect of the invention; and placing the hydrogen in contact with carbon monoxide at a temperature above 100 ° C and a pressure of at least 10 bar with the catalyst so prepared, to produce hydrocarbons and, optionally, hydrocarbon oxygen.
The temperature can be from 180 ° C to 250 ° C, more preferably, from 210 ° C to 240 ° C. The pressure can be more preferably from 10 bar to 70 bar.
It is preferred that the hydrocarbon synthesis process consists of a Fischer-Tropsch process, more preferably a three-phase Fischer-Tropsch process, even more preferably, a fluid bed bed Fischer-Tropsch process the production of a wax product.
The hydrocarbon synthesis process can also include a hydroprocessing step to convert hydrocarbons and, optionally, oxygenates to chemicals and / or liquid fuels.
The present invention also extends to products produced by the hydrocarbon synthesis process of the fourth aspect of the invention.
According to a fifth aspect of the present invention, a hydrogenation process is provided which comprises preparing a catalyst using the process of the third aspect of the invention; and placing hydrogen and an organic compound in contact with the catalyst so prepared, to hydrogenate the organic compound.
The present invention also extends to products produced by the hydrogenation process of the fifth aspect of the invention.
Brief description of the drawings
The invention will now be described in greater detail, with reference to the following non-limiting examples and the accompanying drawings.
In the drawings,
Figure 1 shows, for example 23, images of a Co (OH) ₂ slurry in water containing silica modified alumina support before and after mixing at 80 ° C;
Figure 2 shows, for example 23, images of a sample of a mixture containing Co (NO ₃ ) ₂ on top of the outgoing cobalt hydroxide, dark purple solid, on the support;
Figure 3 shows, for Example 23, the TPR data from a physical mixture of Co (OH) 2 and silica modified alumina versus Co (OH) ₂ chemisorbed on alumina modified with silica; and
Figure 4 shows, for example 23, images of a mixture of Co (OH) 2 and alumina tablets in water.
Detailed description of the invention
EXAMPLE 1 - Preparation of comparative catalyst 1
A catalyst of 30g Co / 0.075g Pt / 100g (1.5g Si / 1 OOg Puralox SCCa, see also the document under WO-A-99/42214, example 1) was prepared on a support preformed 1.5g Si / 1 OOg of modified Puralox particulate SCCa using aqueous slurry phase impregnation and drying, followed by direct fluidized bed calcination in air.
This preparation was carried out through two steps of impregnation and calcination, both of which used a soluble inorganic cobalt compound.
In particular, the catalyst, which is suitable for use in a Fischer Tropsch synthesis of slurry phase, was prepared as follows:
43.70g of Co (NO ₃ ) ₂ 6H ₂ O was dissolved in 40 ml of distilled water and 0.024g of Pt (NH ₃ ) 4. (NO ₃ ) ₂ (dissolved in 10 ml of distilled water) was added to this solution , after that, 50, Og of the modified preformed support of 1.5g of Si / 1 OOg of Puralox SCCa was added to the solution. The aqueous slurry phase impregnation and vacuum drying were then carried out by increasing the temperature from 60 to 95 ° C, while the vacuum was reduced from 170 to 75 mbar.
This vacuum-dried intermediate was directly subjected to a fluidized bed calcination step, according to the following procedure, using a continuous air flow of 1.7 dm ³ n / min., While increasing the temperature from 25 ° C to 250 ° C at 1 ° C / min. and it is kept at 250 ° C for 6 h.
In the preparation for Fischer-Tropsch (FTS) synthesis procedures of continuous agitated tank reactor ('CSTR') of laboratory scale slurry phase, this calcined material was reduced and coated with wax according to the following procedure: 10g of the catalyst was reduced by 1 bar in pure H ₂ (space velocity = 2000 ml _n of H ₂ / g of catalyst / h), while the temperature was increased from 25 ° C to 425 ° C at a rate of 1 ° C / min., After that, the temperature was kept constant at this temperature of 425 ° C for 16 h. The reduced catalyst was allowed to cool to room temperature, at such a stage the hydrogen was replaced by argon, and the catalyst was discharged in Fischer-Tropsch wax fused under the protection of an argon blanket. This wax-coated catalyst was then transferred to the slurry reactor.
EXAMPLE 2 - Co (OH) only
Preparation of inventive catalyst precursor 2
A catalyst precursor of 5.0 g of Co / 100 g of support was prepared on a modified alumina support with particulate silica with the use of chemisorption, followed by calcination of the direct fluidized bed in air.
In particular, the catalyst precursor was prepared as follows:
Chimisection
40 g of silica-modified alumina was added to a suspension of 3.2 g of particulate cobalt hydroxide in 90 ml of water. The resulting mixture, which was in the form of a slurry, had a pH of 7.5. The phase chemisorption of aqueous slurry was carried out for 18 h at 80 ° C. During this process, the pH slowly decreases to 5. The water layer was decanted from the mixture, and after three washes with water, the light purple product was dried at 40 mbar and 80 ° C. This vacuum-treated catalyst intermediate or precursor was subjected to fluidized bed calcination, according to the following procedure using a continuous air flow of 1.6 dm ³ n / min, while increasing the temperature from 25 ° C to 250 ° C at 1 ° C / min. and it is kept at 250 ° C for 6 h.
EXAMPLE 3 - Co (OH) ₂ and Co (NO ₃ ) in succession
Preparation of inventive catalyst 3
A catalyst of 20g of Co / 0.070g of Pt / 1 OOg of support was prepared on a modified alumina support with particulate silica with the use of an aqueous chemisorption fluid phase preparation, sequential impregnation and drying, followed by bed calcination. fluidized directly in air.
This preparation was carried out by means of two preparation steps: 15 The first preparation step included chemisorption using cobalt hydroxide, while the second preparation step included impregnation using cobalt nitrate.
In particular, the catalyst was prepared as follows:
Cobalt nitrate solution
A cobalt nitrate solution was prepared using 0ο (Ν0 ₃ ) ₂ .6Η ₂ Ο and Ρΐ (ΝΗ ₃ ) _4. (ΝΟ ₃ ) 2 resulting in a solution containing 140.2 g / l of Co and 0 , 5328g / l of Pt. The pH of the solution was adjusted to 2.7 with the use of nitric acid.
Chemisection / impregnation
40 g of silica-modified alumina was added to 3.2 g of particulate cobalt hydroxide in 90 ml of water. The resulting suspension had a pH of 7.5. The phase chemisorption of aqueous slurry was carried out for 18 h at 80 ° C. During this process, the pH slowly decreases to 5. The water layer was decanted from the mixture, and after three washes with water, the purple product was dried at 40 bar and 80 ° C,
The intermediate material or catalyst support treated from the chemisorption was subjected to the following stage of cobalt / platinum impregnation and calcination:
30, Og of outgoing chemo-vivid material and 47.7 ml of the cobalt nitrate solution were subjected to the aqueous slurry phase impregnation and vacuum drying according to the details provided in the impregnation and vacuum drying protocol in Example 1. This vacuum-dried intermediate was directly subjected to a fluidized bed calcination step, according to the following procedure using a continuous air flow of 1.6 dm ³ n / min, while increasing the temperature at from 25 ° C to 250 ° C at 1 ° C / min. and it is kept at 250 ° C for 6 h.
The catalyst precursor (that is, after chemisorption, impregnation and calcination) was activated / reduced to obtain the catalyst using the procedure described in Example 1, except that the final reduction temperature was 375 ° Ç.
EXAMPLE 4 - (Co (QH) And CofNOÚg simultaneously)
Preparation of inventive catalyst 4
A catalyst of 19.2g of Co / 0.070g of Pt / 1 OOg of support was prepared on a modified alumina support with particulate silica with the use of the aqueous slurry phase preparation with simultaneous impregnation and drying, followed by calcination of direct fluidized bed in air.
This preparation was done through a single process or preparation step: The step includes chemisorption using cobalt hydroxide and impregnation using cobalt nitrate. In this way, chemisorption and impregnation occur at the same stage of the process and is referred to as simultaneous chemisorption and impregnation.
In particular, the catalyst was prepared as follows:
I
Cobalt nitrate solution
The cobalt nitrate solution was prepared using Co (NO ₃ ) 2.6H ₂ O and Pt (NH ₃ ) _4. (NO3) 2 resulting in a solution containing 140.2g / l of Co and 0.5328g / l of Pt. The pH of the solution was adjusted to 2.7 with the use of nitric acid.
Chemisorption / impregnation «
40g of silica-modified alumina was added to a suspension of 3.2g of solid particulate cobalt hydroxide in 57g of the cobalt nitrate solution and 50g of water. The phase chemisorption of aqueous slurry was carried out for 1 h at 80 ° C. During this process, the pH of the slurry changed from 6 to 3.5. The resulting slurry of purple solid material in a dark red solution was subjected to vacuum impregnation and drying according to the details provided in the vacuum drying and impregnation protocol in Example 1. This vacuum dried treated catalyst intermediate or precursor was directly subjected to a fluidized bed calcination step, according to the following procedure using a continuous air flow of 1.6 dm ³ n / min, while increasing the temperature from 25 ° C to 250 ° C ° C to 1 ° C / min. and it is kept at 250 ° C for 6 h.
The catalyst precursor (that is, after chemisorption, impregnation and calcination) was activated / reduced to obtain the catalyst using the procedure described in Example 1, except that the final reduction temperature was 375 ° Ç.
EXAMPLE 5 - (Co (OH) And Co (NO ₃ ) )
Preparation of inventive catalyst 5
A catalyst of 20.9g of Co / 0.0795g of Pt / 1 OOg of support was prepared on a modified alumina support with particulate silica with the use of a water-based phase of the chemisorption slurry, simultaneous impregnation and drying, followed by calcination. of direct fluidized bed in air.
This preparation was carried out through a single preparation step: The step includes chemisorption using cobalt hydroxide and impregnation using cobalt nitrate.
In particular, the catalyst was prepared as follows:
Cobalt nitrate solution
A cobalt nitrate solution was prepared using Co (NO3) 2.6H ₂ O and Pt (NH3) _4. (NO3) ₂ resulting in a solution containing 141.2g / l of Co and 0.5396g / l of Pt. The pH of the solution was adjusted to 2.6 with the use of nitric acid.
Chemisorption / impregnation
40g of silica-modified alumina was added to a suspension of 4g of solid parficulated cobalt hydroxide in 57g of the cobalt nitrate solution and 50g of water. The phase chemisorption of aqueous slurry was carried out for 30 min. at 60 ° C. During this process, the pH of the slurry changed from 6 to 3.5. The resulting slurry of purple solid material in a dark red solution was subjected to impregnation and vacuum according to the details provided in the impregnation and vacuum drying protocol in Example 1. This intermediate or vacuum-treated catalyst support was directly subjected to a fluidized bed calcination step, according to the following procedure, using a continuous air flow of 1.6 dm ³ n / min, while increasing the temperature from 25 ° C to 250 ° C at 1 ° C / min. and it is kept at 250 ° C for 6 h.
The catalyst precursor (that is, after chemisorption, impregnation and calcination) was activated / reduced to obtain the catalyst using the procedure described in Example 1, except that the final reduction temperature was 375 ° Ç.
EXAMPLE 6 - (higher load on ^the first preparation step)
Preparation of inventive catalyst 6
A catalyst 29.7g of Co / 0.041g of Pt / 100g of support was prepared on a modified alumina support with particulate silica with the use of a water-based phase of the chemisorption slurry, simultaneous impregnation and drying, followed by fluidized bed calcination. straight into the air.
This preparation was carried out through a single preparation step: The step included chemisorption using cobalt hydroxide and impregnation using cobalt nitrate.
In particular, the catalyst was prepared as follows:
Cobalt nitrate solution
A cobalt nitrate solution was prepared using
Co (NO ₃ ) ₂ , 6H ₂ O and Pt (NH ₃ ) _4. (NO ₃ ) ₂ resulting in a solution containing 154.4g / l of Co and 0.213g / l of Pt. The pH of the solution was adjusted to 3.2 with the use of nitric acid.
Chemistry / improprnection
40g of alumina modified with silica was added to a suspension of 10g of solid particulate cobalt hydroxide in 57g of the cobalt nitrate solution and 50g of water. The phase chemisorption of aqueous slurry was carried out for 48 h at 60 ° C. During this process, the pH of the
The slurry changed from 6 to 3.5. The resulting slurry of purple solid material in a dark red solution was subjected to impregnation and vacuum according to the details provided in the vacuum drying and impregnation protocol in Example 1. This intermediate or chemical treatment treated under vacuum was directly subjected to a fluidized bed calcination step, according to the following procedure, using a continuous air flow of 1.6 dm ^ / min., while increasing the temperature from 25 ° C to 250 ° C at 1 ° C / min. and it is kept at 250 ° C for 6 h.
The catalyst precursor (that is, after chemisorption, impregnation and calcination) was activated / reduced to obtain the catalyst using the procedure described in Example 1, except that the final reduction temperature was 375 ° Ç.
EXAMPLE 7 - (in Puralox)
Preparation of inventive catalyst 7
A catalyst of 21.1g of Co / 0.029g of Pt / 100g of support (Puralox SCCa) was prepared in a Puralox SCCa particulate support with the use of simultaneous wetting of the chemisorption slurry and drying, followed by calcination of direct fluidized bed in air.
This preparation was carried out through a single preparation step: The step included chemisorption using cobalt hydroxide and impregnation using cobalt nitrate.
In particular, the catalyst was prepared as follows:
Cobalt nitrate solution
A cobalt nitrate solution was prepared using Co (NO ₃ ) ₂ .6H ₂ O and Pt (NH ₃ ) _4. (NO ₃ ) ₂ resulting in a solution containing 154.4g / l of Co and 0.213g / l Pt. The pH of the solution was adjusted to 3.2 using nitric acid.
Chemistry / improprnection
40g of Puralox SCCa was added to a suspension of 4g of solid particulate cobalt hydroxide in 57g of the cobalt nitrate solution and 50g of water. The phase chemisorption of aqueous slurry was carried out for 30 min. at 60 ° C. During this process, the pH of the slurry changed from 6 to 3.5. The resulting slurry of purple solid material in a dark red solution was subjected to vacuum impregnation and drying according to the details provided in the vacuum drying and impregnation protocol in Example 1. This vacuum-treated catalyst intermediate or support was directly subjected to a fluidized bed calcination step, according to the following procedure, using a continuous air flow of 1.6 dm ³ n / min, while increasing the temperature from 25 ° C to 250 ° C to 1 ° C / min. and it is kept at 250 ° C for 6 h.
catalyst precursor (that is, after chemisorption, impregnation and calcination) was activated / reduced to obtain the catalyst using the procedure described in Example 1, except that the final reduction temperature was 375 ° C .
EXAMPLE 8 - Preparation of inventive catalyst 8
A 14.5g Co / 0.020g Pt / 100g support catalyst (modified Puralox SCCa) was prepared on a 1.5g Si / 1OO support of modified Puralox SCCa particulate using the paste phase preparation aqueous fluid of simultaneous chemisorption-impregnation and drying, followed by calcination of the direct fluidized bed in air.
This preparation was carried out through a single preparation step: The step included chemisorption using cobalt hydroxide and impregnation using cobalt nitrate.
In particular, the catalyst was prepared as follows:
Cobalt nitrate solution
A cobalt nitrate solution was prepared using Co (NO ₃ ) ₂ .6H ₂ O and Pt (NH ₃ ) _4. (NO ₃ ) ₂ resulting in a solution containing 154.4g / l of Co and 0.213g / l Pt. The pH of the solution was adjusted to 3.2 using nitric acid.
Chemistry / improprnection
40g of preformed support of 1.5g of Si / 1 OOg of modified Puralox SCCa 2/150 was added to a suspension of 4g of solid particulate cobalt hydroxide in 57g of the cobalt nitrate solution and 50g of water. The phase chemisorption of aqueous slurry was carried out for 30 min. at 60 ° C. During this process, the pH of the slurry changed from 6 to 3.5. The resulting slurry of purple solid material in dark red solution was subjected to impregnation and vacuum drying according to the details provided in the impregnation and vacuum drying protocol in
Example 1. This vacuum-treated catalyst intermediate or support was directly subjected to a fluidized bed calcination step, according to the following procedure, using a continuous air flow of
1.6 dm ³ n / min, while increasing the temperature from 25 ° C to
250 ° C to 1 ° C / min. and it is kept at 250 ° C for 6 h.
The catalyst precursor (that is, after chemisorption, impregnation and calcination) was activated / reduced to obtain the catalyst using the procedure described in Example 1, except that the final reduction temperature was 375 ° Ç.
EXAMPLE 9 - (Co (OH) And CoiNcEb in another reason)
Preparation of inventive catalyst 9
A catalyst of 21.2g of Co / 0.029g of Pt / 100g of support was prepared on a modified alumina support with particulate silica using the chemisorption aqueous slurry phase preparation15 simultaneous impregnation and drying, followed by calcination of direct fluidized bed in air.
This preparation was carried out through a single preparation step: The step included chemisorption using cobalt hydroxide and impregnation using cobalt nitrate.
In particular, the catalyst was prepared as follows:
Cobalt nitrate solution
A cobalt nitrate solution was prepared using Co (NO3) 2.6H ₂ O and Pt (NH3) 4. (NO ₃ ) ₂ resulting in a solution containing
141.2g / l of Co and 0.5366g / l of Pt. The pH of the solution was adjusted to 2.6 with the use of nitric acid.
Chemisorption / impregnation
40g of silica-modified alumina was added to a suspension of 10g of solid particulate cobalt hydroxide in 26g of the cobalt nitrate solution and 80g of water. The phase chemisorption of aqueous slurry was carried out for 3.5 h at 60 ° C. During this process, the pH of the slurry changed from 6 to 3.5. The resulting slurry of purple solid material in a dark red solution was subjected to vacuum impregnation and drying according to the details provided in the vacuum drying and impregnation protocol in Example 1. This vacuum-treated catalyst intermediate or support was directly subjected to a fluidized bed calcination step, according to the following procedure, using a continuous air flow of 1.6 dm ³ n / min, while increasing the temperature from 25 ° C to 250 ° C to 1 ° C / min. and it is kept at 250 ° C for 6 h.
The catalyst precursor (ie, after chemisorption, impregnation and calcination) was activated / reduced to obtain the catalyst using the procedure described in Example 1, except that the final reduction temperature was 375 ° Ç.
EXAMPLE 10 - (Co (OH) 2 and CofNQÚ - two consecutive impregnations)
Preparation of inventive catalyst 10
A catalyst of 41.2g of Co / 0.051g of Pt / 100g of support (alumina modified with silica) was prepared on a support of alumina modified with particulate silica using two subsequent steps, each consisting of: preparation of phase of simultaneous chemical chemisorption-impregnation slurry and drying, followed by direct fluidized bed calcination in air.
This preparation was carried out by means of two subsequent equal preparation steps: each step included chemisorption using cobalt hydroxide and impregnation using cobalt nitrate.
In particular, the catalyst was prepared as follows:
Cobalt nitrate solution 1
A cobalt nitrate solution was prepared using
Co (NO ₃ ) 2-6H2O and Pt (NH ₃ ) 4. (NO ₃ ) ₂ resulting in a solution containing 154.4g / l of Co and 0.213g / l of Pt. The pH of the solution was adjusted to 3, 2 with the use of nitric acid.
Cobalt nitrate solution 2
A cobalt nitrate solution was prepared using Co (NO ₃ ) ₂ .6H2O and Pt (NH ₃ ) 4. (NO ₃ ) ₂ resulting in a solution containing 141.2g / l of Co and 0.537g / l Pt. The pH of the solution was adjusted to 2.5 with the use of nitric acid.
Chemisorption / impregnation
In step 1: 40 g of silica-modified alumina was added to a suspension of 10 g of solid particulate cobalt hydroxide in 57 g of cobalt nitrate solution 1 and 50 g of water. The phase chemisorption of aqueous slurry was carried out for 1 h at 80 ° C. During this process, the pH of the slurry changed from 6 to 3.5. The resulting slurry of purple solid material in a dark red solution was subjected to vacuum impregnation and drying according to the details provided in the vacuum drying and impregnation protocol in Example 1. This vacuum-treated catalyst intermediate or support was directly subjected to a fluidized bed calcination step, according to the following procedure, using a continuous air flow of 1.6 dm3n / min., while increasing the temperature from 25 ° C to 250 ° C at 1 ° C / min. and it is kept at 250 ° C for 6 h.
In step 2: 20g of the material from step 1 of exit was added to a suspension of 1.6g of solid particulate cobalt hydroxide in 32g of the solution of cobalt nitrate 2 and 30g of water. The phase chemisorption of aqueous slurry was carried out for 1 h at 80 ° C. During this process, the pH of the slurry changed from 6 to 3.5. The resulting slurry of black solid material in a transparent dark red solution was subjected to vacuum impregnation and drying according to the details provided in the vacuum drying and impregnation protocol in Example 1. This intermediate or vacuum-treated material was directly subjected to a fluidized bed calcination step, according to the following procedure, using a continuous air flow of 1.6 dm3n / min., while increasing the temperature from 25 ° C to 250 ° C at 1 ° C / min. and it is kept at 250 ° C for 6 h.
The catalyst precursor (that is, after chemisorption, impregnation and calcination) was activated / reduced to obtain the catalyst using the procedure described in Example 1, except that the final reduction temperature was 375 ° Ç.
EXAMPLE 11 - (Co (OH) And CofNOÚ )
Preparation of inventive catalyst 11
A catalyst of 26.7g of Co / 0.070g of Pt / 100g of support was prepared on a modified alumina support with particulate silica with the use of the water-based phase preparation of chemisorption, simultaneous impregnation and drying, followed by bed calcination. fluidized directly in air.
This preparation was done through a single preparation step. The step included chemisorption using cobalt hydroxide and impregnation using cobalt nitrate.
In particular, the catalyst was prepared as follows:
Cobalt nitrate solution
A cobalt nitrate solution was prepared using Co (NO3) 2.6H ₂ O and Pt (NH ₃ ) _4. (NO ₃ ) 2 resulting in a solution containing 140.2g / l of Co and 0.5328g / l of Pt. The pH of the solution was adjusted to 2.7 with the use of nitric acid.
Chemisection / impregnation
40g of silica-modified alumina was added to a suspension of 4g of solid particulate cobalt hydroxide in 57g of the cobalt nitrate solution and 50g of water. The phase chemisorption of aqueous slurry was carried out for 1 h at 80 ° C. During this process, the pH of the slurry changed from 6 to 3.5. The resulting slurry of purple solid material in a dark red solution was subjected to vacuum impregnation and drying according to the details provided in the vacuum drying and impregnation protocol in Example 1. This vacuum-treated catalyst intermediate or support was directly subjected to a fluidized bed calcination step, according to the following procedure, using a continuous air flow of 1.6 dm3n / min., while increasing the temperature from 25 ° C to 250 ° C to rc / min. and it is kept at 250 ° C for 6 h.
The catalyst precursor (that is, after chemisorption, impregnation and calcination) was activated / reduced to obtain the catalyst using the procedure described in Example 1, except that the final reduction temperature was 375 ° Ç.
EXAMPLE 12 - (Co (OH) And Co (NQg) g in two consecutive impregnations)
Preparation of inventive catalyst 12
A catalyst of 57.7g of Co / 0.06g of Pt / 100g of support (alumina modified with silica) was prepared in a support of alumina modified with particulate silica using two subsequent steps, each consisting of the preparation of simultaneous impregnation-drying aqueous slurry phase and drying, followed by direct fluidized bed calcination in air.
This preparation was carried out by means of two subsequent equal preparation steps: each step included chemisorption using cobalt hydroxide and impregnation using cobalt nitrate.
In particular, the catalyst was prepared as follows:
Cobalt nitrate solution 1
A cobalt nitrate solution was prepared using
Co (NO ₃ ) ₂ .6H ₂ O and Pt (NH ₃ ) 4. (NO ₃ ) ₂ resulting in a solution containing 154.4g / l of Co and 0.213g / l of Pt. The pH of the solution was adjusted to 3.2 with the use of nitric acid.
Cobalt nitrate solution 2
A cobalt nitrate solution was prepared using Co (NO ₃ ) ₂ .6H ₂ O and Pt (NH ₃ ) _4. (NO ₃ ) ₂ resulting in a solution containing 141.2g / l of Co and 0.537g / l Pt. The pH of the solution was adjusted to 2.5 with the use of nitric acid.
Chemisorption / impregnation
In step 1: 40 g of silica-modified alumina was added to a suspension of 8 g of solid particulate cobalt hydroxide in 57 g of cobalt nitrate solution 1 and 50 g of water. The phase chemisorption of aqueous slurry was carried out for 1 h at 80 ° C. During this process, the pH of the slurry changed from 6 to 3.5. The resulting slurry of purple solid material in a dark red solution was subjected to impregnation and vacuum drying according to the details provided in the impregnation and vacuum drying protocol in Example 1. This vacuum dried treated catalyst support intermediate was directly subjected to a fluidized bed calcination step, according to the following procedure, using a continuous air flow of 1.6 dm3n / min., while increasing the temperature from 25 ° C to 250 ° C at 1 ° C / min. and it is kept at 250 ° C for 6 h.
In step 2: 20g of the material from step 1 of exit was added to a suspension of 4g of solid particulate cobalt hydroxide in 32g of the solution of cobalt nitrate 2 and 30g of water. The phase chemisorption of aqueous slurry was carried out for 1 h at 80 ° C. During this process, the pH of the slurry changes from 6 to 3.5. The resulting slurry of black solid material in a transparent dark red solution was subjected to vacuum impregnation and drying according to the details provided in the vacuum impregnation and drying protocol in Example 1. This intermediate or vacuum-treated material was directly subjected to to a fluidized bed calcination step, according to the following procedure, using a continuous air flow of 1.6 dm3n / min., while increasing the temperature from 25 ° C to 250 ° C at 1 ° C / min. and it is kept at 250 ° C for 6 h.
The catalyst precursor (that is, after chemisorption, impregnation and calcination) was activated / reduced to obtain the catalyst using the procedure described in Example 1, except that the final reduction temperature was 375 ° Ç.
EXAMPLE 13 - (Νί (ΟΗ) ₂ and NiflMOgk simultaneously)
Preparation of inventive catalyst precursor 13
A catalyst precursor of 30.4g of Ni / 1 OOg of alumina support was prepared in a particulate Puralox SCCa support using the simultaneous chemisorption-impregnation aqueous slurry phase preparation and drying, followed by reactor calcination. of direct tubular flow in air.
This preparation was carried out through a single preparation step: The step includes chemisorption using nickel hydroxide and impregnation using nickel nitrate.
In particular, the catalyst precursor was prepared as follows:
Nickel nitrate solution
A nickel nitrate solution was prepared using Ni (NO ₃ ) 2.6H2O resulting in a solution containing 140g / l of Ni,
Chemisorption / impregnation
40g of Puralox SCC a-2/150 was added to a suspension of 8g of solid particulate nickel hydroxide in 63g of the nickel nitrate solution and 55g of water. The phase chemisorption of aqueous slurry was carried out for 20 h at 80 ° C. The resulting slurry of blue-green solid material in a green solution was subjected to vacuum impregnation and drying according to the details provided in the vacuum drying and impregnation protocol in Example 1. This intermediate or vacuum dried treatment catalyst support was directly subjected to calcination of a tubular flow reactor, according to the following procedure, using a continuous air flow of 69 dm ³ n / h, while increasing the temperature from 25 ° C to 375 ° C at 1 ° C / min. and it is kept at 375 ° C for 6 h.
EXAMPLE 14 - (Co (QH) - Co (NO ₃ ) ₂ and Ni (NO ₃ ) ₂ simultaneously)
Preparation of inventive catalyst 14
A catalyst of 19.2g of Co / 2.5g of Ni / 0.070g of Pt / 100g of support was prepared on a modified alumina support with particulate silica using the simultaneous chemisorption-impregnated aqueous slurry phase preparation. and drying, followed by calcination of the direct fluidized bed in air.
This preparation was carried out through a single preparation step: The step includes chemisorption using cobalt hydroxide and impregnation using cobalt nitrate and nickel nitrate.
In particular, the catalyst was prepared as follows:
Cobalt nitrate solution
A cobalt nitrate solution was prepared using Οο (Ν0 ₃ ) ₂ .6Η ₂ 0 and Pt (NH ₃ ) _4. (NO ₃ ) ₂ resulting in a solution containing 140.2g / l of Co and 0, 5328g / l of Pt. The pH of the solution was adjusted to 2.7 with the use of nitric acid.
Nickel nitrate solution
A nickel nitrate solution was prepared using Ni (NO ₃ ) ₂ .6H ₂ O resulting in a solution containing 140g / l of Ni
Chemisorption / impregnation
40g of silica-modified alumina was added to a suspension of 3.2g of solid particulate cobalt hydroxide in 57g of the cobalt nitrate solution and 7g of the nickel nitrate solution and 50g of water. The phase chemisorption of aqueous slurry was carried out for 18 h at 80 ° C. The resulting slurry of purple solid material in a dark red solution was subjected to vacuum impregnation and drying according to the details provided in the vacuum drying and impregnation protocol in Example 1. This vacuum dried treated catalyst intermediate or support was directly subjected to a fluidized bed calcination step, according to the following procedure, using a continuous air flow of
1.6 dmSn / min., While increasing the temperature from 25 ° C to 250 ° C to 1 ° C / min. and it is kept at 250 ° C for 6 h.
The catalyst precursor (that is, after chemisorption, impregnation and calcination) was activated / reduced to obtain the catalyst using the procedure described in Example 1, except that the final reduction temperature was 375 ° Ç.
EXAMPLE 15 - (Co (OHb and Ni (OHb and Co (NQ ₃ ) Simultaneously)
Preparation of inventive catalyst 15
A catalyst of 19.2g Co / 2.5g Ni / 0.070g Pt / 100g support was prepared in a modified alumina support with particulate silica using the simultaneous chemisorption-impregnated aqueous slurry phase preparation. and drying, followed by direct fluidized bed calcination in air.
This preparation was done through a single preparation step: The step includes chemisorption using cobalt hydroxide and nickel hydroxide and impregnation using cobalt nitrate.
In particular, the catalyst was prepared as follows:
Cobalt nitrate solution
A cobalt nitrate solution was prepared using Co (NO ₃ ) ₂ .6H ₂ O and Pt (NH ₃ ) _4. (NO ₃ ) ₂ resulting in a solution containing 140.2g / l of Co and 0, 5328g / l of Pt. The pH of the solution was adjusted to 2.7 with the use of nitric acid.
Chemisection / impregnation
40g of silica-modified alumina was added to a suspension of 3.2g of solid particulate cobalt hydroxide and 1.6g of solid particulate nickel hydroxide in 57g of the cobalt nitrate solution and 50g of water. The phase chemisorption of aqueous slurry was carried out for 18 h at 80 ° C. The resulting slurry of purple solid material in a dark red solution was subjected to vacuum impregnation and drying according to the details provided in the vacuum drying and impregnation protocol in Example 1. This vacuum-treated catalyst intermediate or support was directly subjected to a fluidized bed calcination step, according to the following procedure, using a continuous air flow of 1.6 dm3n / min., while increasing the temperature from 25 ° C to 250 ° C at 1 ° C / min. and it is kept at 250 ° C for 6 h.
The catalyst precursor (that is, after chemisorption, impregnation and calcination) was activated / reduced to obtain the catalyst using the procedure described in Example 1, except that the final reduction temperature was 375 ° Ç.
EXAMPLE 16 - (Co (OH) g and Mn (OHb and Co (NO )
0 simultaneously)
Preparation of inventive catalyst 16
A catalyst of 19.2g of Co / 4g of Mn / 0.070g of Pt / 100g of support was prepared on a modified alumina support with particulate silica with the use of the aqueous slurry phase preparation.
5 simultaneous chemisorption-impregnation and drying, followed by calcination of a fluidized direct effect in air.
This preparation was done through a single preparation step: The step includes chemisorption using cobalt hydroxide and nickel hydroxide and impregnation using cobalt nitrate.
In particular, the catalyst was prepared as follows:
Cobalt nitrate solution
A cobalt nitrate solution was prepared using Co (NO ₃ ) ₂ .6H ₂ O and Pt (NH ₃ ) 4. (NO ₃ ) ₂ resulting in a solution containing
140.2g / l of Co and 0.5328g / l of Pt. The pH of the solution was adjusted to 2.7 with the use of nitric acid.
Chemisorption / impregnation
40g of silica-modified alumina was added to a suspension of 3.2g of solid particulate cobalt hydroxide and 2.7g of solid manganese hydroxide in 57g of the cobalt nitrate solution and 50g of water. The phase chemisorption of aqueous slurry was carried out for 18 h at 80 ° C. The resulting slurry of purple solid material in dark red solution was subjected to impregnation and vacuum drying according to the details provided in the impregnation and vacuum drying protocol in
Example 1. This vacuum-treated catalyst intermediate or support was directly subjected to a fluidized bed calcination step, according to the following procedure, using a continuous air flow of
1.6 dm3n / min., While increasing the temperature from 25 ° C to 250 ° C to 1 ° C / min. and it is kept at 250 ° C for 6 h.
0 The catalyst precursor (that is, after chemisorption, impregnation and calcination) was activated / reduced to obtain the catalyst using the procedure described in Example 1, except that the final reduction temperature was 375 'Ç.
EXAMPLE 17 - (Co (OH) And Co (NO ₃ ) ₂ in ZrO ₂ )
Preparation of inventive catalyst 17
A catalyst of 26.6g Co / 0.070 Pt / 1 OOg of zinc (IV) support was prepared in a support of particulate ZrO ₂ (available from Acros Organics of quality pa (98% ZrO ₂ )) with the use of the simultaneous chemisorption-impregnation aqueous slurry phase preparation and drying, followed by direct fluidized bed calcination in air.
This preparation was carried out through a single preparation step: The step included chemisorption using cobalt hydroxide and impregnation using cobalt nitrate.
In particular, the catalyst was prepared as follows:
Cobalt nitrate solution
A cobalt nitrate solution was prepared using Co (NO ₃ ) ₂ .6H ₂ O and Pt (NH ₃ ) _4. (NO ₃ ) ₂ resulting in a solution containing 140.2g / l of Co and 0, 5328g / l of Pt. The pH of the solution was adjusted to 2.7 with the use of nitric acid.
Chemistry / improprnection
40g of ZrO ₂ was added to a suspension of 8g of solid particulate cobalt hydroxide in 57g of the cobalt nitrate solution and 50g of water. The phase chemisorption of aqueous slurry was carried out for 18 h at 80 ° C. The resulting slurry of light pink solid material in red solution was subjected to vacuum impregnation and drying according to the details provided in the vacuum drying and impregnation protocol in Example 1. This vacuum-treated catalyst intermediate or support was directly subjected to a fluidized bed calcination step, according to the following procedure, using a continuous air flow of
1.6 dm3n / min., While increasing the temperature from 25 ° C to 250 ° C to 1 ° C / min. and it is kept at 250 ° C for 6 h.
The catalyst precursor (ie, after chemisorption, impregnation and calcination) was activated / reduced to obtain the catalyst using the procedure described in Example 1, except that the final reduction temperature was 375 ° Ç.
EXAMPLE 18 - (Cu (OH) _z and Cu (NO ₃ ) ₂ in ZrO )
Preparation of inventive catalyst precursor 18
A 19g Cu / 100g catalyst precursor of zinc (IV) support was prepared on a particulate ZrO ₂ support (available from Acros Organics of quality pa (98% ZrO2)) using the preparation of simultaneous impregnation-drying aqueous slurry phase and drying, followed by direct fluidized bed calcination in air.
This preparation was done through a single preparation step: The step includes chemisorption with the use of copper hydroxide and impregnation with the use of copper nitrate.
In particular, the catalyst precursor was prepared as follows:
Copper nitrate solution
A copper nitrate solution was prepared using Cu (NO3) 2-6H ₂ O resulting in a solution containing 140g / l of Cu.
Chemisorption / impregnation
40g of ZrO ₂ was added to a suspension of 4g of solid particulate copper hydroxide in 63g of the copper nitrate solution and 50g of water. The phase chemisorption of aqueous slurry was carried out for 18 h at 80 ° C. The resulting slurry of light blue-green solid material in blue solution was subjected to impregnation and vacuum drying.
EXAMPLE 19 - (Co (OH) And CoíNOft - eggshell catalyst)
Preparation of inventive catalyst precursor 19
A catalyst precursor of 7g of Co / 0.030 of Pt / 100g of support was prepared on a preformed support of Al 4505 T1 / 8 with the use of the aqueous chemisorption slurry phase preparation, simultaneous impregnation and drying, followed by calcination. of direct fluidized bed in air.
This preparation was carried out through a single preparation step: The step included chemisorption using cobalt hydroxide and impregnation using cobalt nitrate.
In particular, the catalyst precursor was prepared as follows:
Cobalt nitrate solution
A cobalt nitrate solution was prepared using Co (NO ₃ ) ₂ .6H ₂ O and Pt (NH ₃ ) _4. (NO ₃ ) 2 resulting in a solution containing 140.2g / l of Co and 0, 5328g / l of Pt. The pH of the solution was adjusted to 2.7 with the use of nitric acid.
Chemisection / impregnation
40g of Al 4505 T1 / 8 was added to a suspension of 0.5g of solid particulate cobalt hydroxide in 25g of the cobalt nitrate solution and 50g of water. The phase chemisorption of aqueous slurry was carried out for 18 h at 80 ° C. The slurry resulting from pinkish-purple tablets in a dark red transparent solution was subjected to impregnation and vacuum drying according to the details provided in the impregnation and vacuum drying protocol in Example 1. This intermediate or catalyst support treated dry to vacuum was directly subjected to a fixed bed calcination step, according to the following procedure, using a continuous air flow of 1.6 dm3n / min., while increasing the temperature from 25 ° C at 250 ° C to 1 ° C / min. and it is kept at 250 ° C for 6 h.
EXAMPLE 20 - Co (QH) ₂ and CofNQa) in succession, as per example 3, but with the use of less platinum
Preparation of comparative catalyst 20
A 20g Co / 0.035g Pt / 1 OO support slurry phase catalyst was prepared on a particulate silica modified alumina support using sequential impregnation-drying aqueous slurry phase preparation and drying. , followed by calcination of the direct fluidized bed in air.
This preparation was carried out through two preparation steps: The first preparation step included chemisorption using cobalt hydroxide, while the second preparation step included impregnation using cobalt nitrate.
In particular, the catalyst was prepared as follows:
Cobalt nitrate solution
A cobalt nitrate solution was prepared using Co (NO3) 2-6H ₂ O and Pt (NH3) 4. (NO ₃ ) ₂ resulting in a solution containing 140.2g / l of Co and 0.2664g / l of Pt. The pH of the solution was adjusted to 2.7 using nitric acid,
Chemisorption / impregnation
40g of alumina modified with silica was added to a suspension of 3.2g of particulate cobalt hydroxide in 90ml of water. The resulting slurry had a pH of 7.5. The phase chemisorption of aqueous slurry was carried out for 18 h at 80 ° C. During this process, the pH slowly decreases to 5. The water layer was decanted from the mixture, and after three washes with water, the purple product was dried at 40 mbar and 80 ° C.
The treated intermediate material or catalyst support resulting from the chemisorption was subjected to the following stage of cobalt / platinum impregnation and calcination:
30, Og of outgoing chemo-vivid material and 47.7 ml of the cobalt nitrate solution were subjected to the aqueous slurry phase impregnation and vacuum drying according to the details provided in the impregnation and vacuum drying protocol in Example 1. This vacuum-dried intermediate was directly subjected to a fluidized bed calcination step, according to the following procedure, using a continuous air flow of 1.6 dm3n / min., While increasing the temperature from from 25 ° C to 250 ° C to 1 ° C / min. and it is kept at 250 ° C for 6 h.
The catalyst precursor (that is, after chemisorption, impregnation and calcination) was activated / reduced to obtain the catalyst using the procedure described in Example 1, except that the final reduction temperature was 375 ° Ç.
EXAMPLE 21 - Co (QH) g and CoNQQ in succession, no platinum
Preparation of comparative catalyst 21
A 20g Co / 100g support catalyst was prepared on a modified alumina support with particulate silica using the sequential chemisorption-impregnated aqueous slurry phase preparation and drying, followed by direct fluidized bed calcination in air.
This preparation was carried out through two preparation steps: The first preparation step included chemisorption using cobalt hydroxide, while the second preparation step included impregnation using cobalt nitrate.
In particular, the catalyst was prepared as follows:
Cobalt nitrate solution
A cobalt nitrate solution was prepared using Co (NO3) 2.6H ₂ O resulting in a solution containing 140.2 g / l of Co. The solution's pH was adjusted to 2.7 with the use of nitric acid.
Chemistry / improprnection
40 g of silica-modified alumina was added to a suspension of 3.2 g of particulate cobalt hydroxide in 90 ml of water. The resulting slurry had a pH of 7.5. The phase chemisorption of aqueous slurry was carried out for 18 h at 80 ° C. During this process, the pH slowly decreases to 5. The water layer was decanted from the mixture, and after three washes with water, the purple product was dried at 40 mbar and 80 ° C.
The intermediate material or catalyst support treated from the chemisorption was subjected to the following stage of cobalt / platinum impregnation and calcination:
30, Og of outgoing chemo-vivid material and 47.7 ml of the cobalt nitrate solution were subjected to the aqueous slurry phase impregnation and vacuum drying according to the details provided in the impregnation and vacuum drying protocol in Example 1. This vacuum-dried intermediate was directly subjected to a fluidized bed calcination step, according to the following procedure, using a continuous air flow of 1.6 dm3n / min, while increasing the temperature at from 25 ° C to 250 ° C to 1 ° C / min. and it is kept at 250 ° C for 6 h.
The catalyst precursor (ie, after chemisorption, impregnation and calcination) was activated / reduced to obtain the catalyst using the procedure described in Example 1, except that the final reduction temperature was 375 ° Ç.
EXAMPLE 22 - Characterization of catalyst precursors versus comparative catalyst 1
Catalysts 1, 4, 5, 10, 12, 14 and 15 were tested for the performance of Fischer-Tropsch synthesis using a slurry phase CSTR. The following Fischer Tropsch synthesis reaction conditions were maintained:
Reactor temperature: 230 ° C Reactor pressure: 17 bar Catalyst inventory: ca. 10 g (H ₂ + CO) conversion: 50 to 65%
Input ratio of H ₂ : CO: 1.6: 1 Internal argon standard: 15% by volume
As all FT conditions were equal, the relative FT activity was determined by calculating the FT activity of each catalyst as mol of converted CO / g of catalysts and done relative to comparative catalyst 1 (see Table 1).
Catalyst 4, as prepared according to the invention with the use of cobalt hydroxide for chemisorption and cobalt nitrate for impregnation, had a relatively 19% lower cobalt charge and showed an activity comparable to catalyst 1, which was prepared by using cobalt nitrate in two successive impregnation steps, under the reaction conditions, as described above.
Catalyst 5, as prepared according to the invention using cobalt hydroxide for chemisorption and cobalt nitrate for impregnation, had a relatively 15% higher cobalt charge and showed 34% greater activity than the catalyst 1, which was prepared using cobalt nitrate in two successive impregnation steps, under the reaction conditions, as described above.
Catalyst 10, as prepared according to the invention with the use of cobalt hydroxide for the chemisorption and cobalt nitrate for the impregnation, but in a different ratio compared to the previous examples which comprise a charge of Co (OH) ₂ bigger. At a general cobalt content of 29.2% (w / w) (ie, a 46% higher cobalt load), this catalyst showed 52% greater activity than comparative catalyst 1, under reaction conditions , as described above.
The catalyst 12, as prepared according to the invention using a sequence of two repetitive preparation steps using cobalt hydroxide for chemisorption and cobalt nitrate for impregnation resulting in a high cobalt charge (36, 6% (w / w); that is, an 83% higher cobalt load) and showed an activity of 17% higher than catalyst 1, which was prepared using cobalt nitrate in two stages of impregnation successive, under reaction conditions, as described above.
Catalysts 2 to 11 and 13 to 16, as prepared according to the invention, showed a greater dispersion of smaller cobalt crystallites compared to catalyst 1 impregnated only with conventionally prepared cobalt nitrate. This improved dispersion is demonstrated by the XRD crystallite size, as shown in table 1. In addition, these catalysts had improved cobalt surface areas as demonstrated by comparing the hydrogen adsorption capacity (HAC) data (see also table 1). The HAC values are derived from the amount of hydrogen (in ml / g of supported catalyst) to be adsorbed after the cobalt reduction. The experiment is carried out in three stages; 1) reduction of cobalt, 2) saturation of the reduced catalyst with hydrogen and 3) desorption of hydrogen under an inert atmosphere from -75 ° C to 35 ° C.
TABLE 1: Cobalt / metal content. Cobalt / metal oxide crystallite size and relative Fischer-Tropsch (FT) activity for catalysts 1 to 21
Catalisaache Content ofmetal beforereduction[m%] Size ofXRD crystalliteprecursorof oxide beforereduction[nm] Capacity ofadsorption ofhydrogen [ml / g] Activityfrom FTrelative 1 (comp) 20 15 3.6 100 2 (comp) 5 14.2 3 (comp) 16.7 13.5 4.2 4 16.2 10.6 4.1 100 5 22.9 10.9 4.8 134 6 17.4 10.6 4 7 17.7 10.9 4.3 8 17.5 9.0 3.7 9 17.3 10.8 4.3 10 29.2 14.9 6.5 152 11 21.1 11.6 5.1 12 36.6 17.6 6.6 117 13 23.3 (Ni) 10-12 7.8
14 16.7 (+2.4 Ni) 10.7 4.5 75 15 16.7 (+1.9 Ni) 10.6 4.8 61 16 16.7 (+ 1.5Mn) 10.2 4 17 26.6 3.3 18 16.7 (Cu) 19 7 1.9 20(comp) 16.5 21(comp) 16.5
The average size of cobalt oxide crystallite determined by XRD, for comparative catalyst 1, was 15 nm, while the average size of cobalt oxide crystallite determined for catalysts 4 to 9 (that is, according to with the invention) was significantly lower, around 10 to 11 nm.
EXAMPLE 23 - Evidence of reaction between support and Co (OH) slurry
The reaction of a metal hydroxide slurry with a support is a surprising feature. For this reason, the invention is based on the images and data gathered in this example. In Figure 1, images of a Co (OH) ₂ slurry in water containing silica modified alumina support can be seen before (left) and after mixing at 80 ° C.
The images at the top represent a mixture without Co (NO ₃ ) 2. It was observed that the reaction between Co (OH) ₂ and the silica modified alumina was completed in 18 h at this temperature, resulting in a light purple solid with a transparent water layer on top.
The bottom images represent a mixture of Co (OH) ₂ , silica modified alumina and soluble Co (NO ₃ ) ₂ . In this case, the reaction between
Co (OH) ₂ and the support is complete within 4 min., Resulting in a purple solid.
A sample of the mixture containing Co (NO ₃ ) ₂ on top of the dark purple solid, cobalt hydroxide output on the support, is again described in Figure 2 (image on the left). When it is washed with three parts of water, the dark purple material, cobalt hydroxide outlet, remains attached to the support and the washes are transparent and colorless (image on the right).
Additional evidence is given based on the reduction profiles recorded using the programmed temperature reduction technique. Figure 3 shows the TPR data from a physical mixture of Co (OH) ₂ and silica modified alumina (dashed line) versus Co (OH) ₂ chemisorbed on alumina modified with silica (solid line). In a physical mixture of 10% Co (OH) ₂ and 90% alumina support, cobalt is typically reduced to
Co (0) at 260 ° C (Figure 3, dashed line). The product of the Co (OH) ₂ reaction from a slurry with alumina is clearly showing a different reduction profile (continuous line). A broad protuberance in the range from 400 to 750 ° C (continuous line) is an indication that this reduction to Co (0) originates from the cobalt species that has a strong
0 interaction with the alumina support.
Additionally, Co (OH) ₂ was chemo-vivid in alumina tablets according to the same technique. A mixture of Co (OH) ₂ and alumina tablets in water resulted in an eggshell distribution of the cobalt precursor on the tablets. In Figure 4, the image on the left
5 shows the resulting coated tablets. The middle image in Figure 4 shows the resulting product in water and that the cobalt remains completely on the tablets. The image on the right in figure 4 shows the separate stages of the cobalt charge of tablets that have been cut in pieces; the bottom row shows tablets both after chemisorption and after impregnation (distribution across the tablet), the middle row shows tablets after chemisorption only (eggshell distribution) and the top row shows the unloaded tablets as a reference.
It will be observed by those skilled in the art that the invention presents a commercially viable method that enables an objective and inexpensive preparation sequence for depositing metal on a support that allows good dispersion at high load on a mechanically robust support. Compared to the state of the art, disadvantages can be avoided, such as excessive washing procedures (no salt needs to be removed).

权利要求:
Claims (16)
[1]
1. Process for the preparation of a catalyst precursor, characterized by the fact that it comprises:
form a slurry of particles of an insoluble inorganic metal salt, particles and / or one or more bodies of a preformed catalyst support in a carrier liquid, and a soluble metal salt dissolved in the carrier liquid, in which the salt metals of insoluble inorganic metal and the soluble metal salt are the same, and where said metal consists of an active catalyst component, with the particles of the insoluble inorganic metal salt being thus placed in contact with the particles and / or the one or more bodies of the preformed catalyst support and the preformed catalyst support, thus being brought into contact at least once with the soluble metal salt, to thereby produce a treated catalyst support; and removing the carrier liquid from the slurry to obtain a dry treated catalyst support, which directly constitutes the catalyst precursor or is optionally calcined to obtain the catalyst precursor.
[2]
2. Process according to claim 1, characterized by the fact that the contact of the particles of the insoluble inorganic metal salt with the particles and / or the one or more bodies of the preformed catalyst support is carried out by at least one minute.
[3]
3. Process according to claim 1 or 2, characterized by the fact that the pre-shaped catalyst support is porous and is selected from the group consisting of a monolith, tablets, shaped artifacts, extrudates, spheres and combinations two or more of them.
[4]
4. Process according to any one of claims 1 to 3, characterized by the fact that the pre-shaped catalyst support is selected from the group consisting of aluminum oxide, silica, titania, zirconia, magnesia, oxide of zinc, activated carbon, molecular sieves, zeolites and combinations of two or more of them.
Petition 870170087882, of 11/14/2017, p. 12/10
[5]
Process according to any one of claims 1 to 4, characterized in that the metal of the insoluble inorganic metal salt and the soluble metal salt is selected from the group consisting of cobalt, nickel, manganese, iron, copper, ruthenium, molybdenum, zinc and combinations of two or more of them.
[6]
6. Process according to claim 5, characterized in that the insoluble inorganic metal salt is Co (OH) ₂ and / or in which the soluble metal salt is Co (NO3) 2.6H2O.
[7]
Process according to any one of claims 1 to 5, characterized in that the particles of the pre-shaped catalyst support are used and in which the formation of the slurry comprises forming a solution of the metal salt soluble in the carrier liquid, suspending particles of inorganic metal salt insoluble in the carrier liquid to form a suspension and add the particles of the preformed catalyst support to the carrier liquid before and / or during and / or subsequent to the suspension formation, to form the slurry, with the metal of the insoluble inorganic metal salt being deposited on the support particles and the metal of the soluble metal salt being deposited within and / or on the support particles.
[8]
8. Process according to claim 1, characterized by the fact that the catalyst precursor comprises metal in an amount between 5% by mass and 90% by mass, based on the total mass of precursor.
[9]
9. Process according to claim 1, characterized by the fact that the catalyst precursor is essentially free of exchangeable ions.
[10]
10. Process according to claim 1, characterized by the fact that the catalyst precursor consists of a Fischer-Tropsch synthesis catalyst precursor.
[11]
11. Process according to claim 1, characterized by the fact that the catalyst precursor consists of a hydrogenation catalyst precursor.
Petition 870170087882, of 11/14/2017, p. 12/11
[12]
12. Process for the preparation of a catalyst, characterized by the fact that it includes preparing a catalyst precursor using the process according to any one of claims 1 to 11 inclusive, and reducing the catalyst precursor so prepared, to obtain a catalyst .
[13]
13. Hydrocarbon synthesis process, characterized by the fact that it comprises preparing a catalyst using the process according to claim 12, and placing the hydrogen in contact with carbon monoxide at a temperature above 100 ° C and a pressure of steel minus 10 bar with the catalyst so prepared, to produce hydrocarbons and, optionally, hydrocarbon oxygenates.
[14]
14. Process according to claim 13, characterized by the fact that it consists of a Fischer-Tropsch fluid bed process for the production of a wax product.
[15]
15. Process according to claim 13 or 14, characterized by the fact that it includes a hydroprocessing step for the conversion of hydrocarbons and, optionally, oxygenates to chemicals and / or liquid fuels.
[16]
16. Hydrogenation process, characterized by the fact that it comprises preparing a catalyst using the process according to claim 12, and placing the hydrogen and an organic compound in contact with the catalyst so prepared, to hydrogenate the organic compound.
Petition 870170087882, of 11/14/2017, p. 12/12
1/2

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引用文献:

---

公开号 | 申请日 | 公开日 | 申请人 | 专利标题

---

---

GB9010075D0|1990-05-04|1990-06-27|Shell Int Research|Process for the preparation of alumina based extrudates|

---

GB9108656D0|1991-04-23|1991-06-12|Shell Int Research|Process for the preparation of a catalyst or catalyst precursor|

---

GB9108663D0|1991-04-23|1991-06-12|Shell Int Research|Process for the preparation of a catalyst or catalyst precursor|

---

US5744419A|1994-12-19|1998-04-28|Council Of Scientific And Industrial Research|Process for the preparation of an improved supported catalyst, containing nickel and cobalt, with or without noble metals, useful for the oxidative conversion of methane, natural gas and biogas to syngas|

---

DZ2013A1|1995-04-07|2002-10-23|Sastech Ltd|Catalysts.|

---

DE69823550T2|1997-12-30|2005-04-14|Shell Internationale Research Maatschappij B.V.|COBALT BASED FISCHER TROPSCH CATALYST|

---

DZ2724A1|1998-02-20|2003-09-01|Sasol Tech Pty Ltd|Process for the production of hydrocarbons from a synthesis gas and their catalysts.|

---

US20020019309A1|1999-10-15|2002-02-14|Lapidus Albert L?Apos;Vovich|Process for the preparation of high activity carbon monoxide hydrogenation catalysts; the catalyst compositions, use of the catalysts for conducting such reactions, and the products of such reactions|

---

GC0000360A|2000-05-04|2007-03-31|Shell Int Research|A catalyst support and a supported metal catalyst, a process for their preparation, and the use of the catalyst|

---

JP2005506190A|2001-10-25|2005-03-03|サソールテクノロジー（プロプライエタリー）リミテッド|Method for activating a cobalt catalyst|

---

GB0222240D0|2002-09-25|2002-10-30|Ici Plc|Cobalt catalysts|

---

PL228196B1|2003-06-13|2018-02-28|Yara Int Asa|Method for producing supported oxide catalysts|

---

GB0418934D0|2004-08-25|2004-09-29|Johnson Matthey Plc|Catalysts|

---

WO2008135940A2|2007-05-04|2008-11-13|Sasol Technology Limited|Catalysts|

---

AP3156A|2009-02-26|2015-03-31|Sasol Tech Pty Ltd|Process for the preparation of fischer-tropsch catalysts and their use|

---

WO2012156834A2|2011-05-19|2012-11-22|Skarboevig Nils Mittet|Textile strength testing equipment|US20130225876A1|2012-02-29|2013-08-29|Celanese International Corporation|Hydrogenation Catalyst Using Multiple Impregnations of an Active Metal Solution|

---

RU2640583C2|2013-03-25|2018-01-10|Космо Ойл Ко., Лтд.|Hydrodesulfurization catalyst for diesel fuel and method of hydrocleaning diesel fuel|

---

CN104722327B|2013-12-18|2018-05-22|武汉凯迪工程技术研究总院有限公司|It is a kind of for metal base monolithic film catalyst of Fiscber-Tropscb synthesis and preparation method thereof|

---

EA036728B1|2014-12-19|2020-12-14|Бп П.Л.К.|Process for preparation of a supported cobalt-containing fischer-tropsch synthesis catalyst|

---

US10569258B2|2014-12-19|2020-02-25|Shell Oil Company|Method for preparing a catalyst|

---

CN106590720B|2015-10-20|2018-07-31|中国石油化工股份有限公司|A method of using coal and oil refinery dry gas as raw material alpha-olefin|

---

US11084021B2|2015-10-27|2021-08-10|W.R. Grace & Co.—Conn|Acid-resistant catalyst supports and catalysts|

---

CN105396569A|2015-12-16|2016-03-16|钟俊超|Preparation method for antiwear large-pore-volume microspherical silicon dioxide carrier|

---

CN105435858A|2015-12-16|2016-03-30|钟俊超|Preparation method of wear-resistant large-pore-volume microspherical silica carrier|

---

CN105536796A|2015-12-16|2016-05-04|钟俊超|Wear-resistant microspheric Fe2O3/SiO2 catalyst preparation method|

---

CN105536881A|2015-12-16|2016-05-04|钟俊超|Preparation method of wear-resistant microspheroidal silica carrier|

---

CN105498853A|2015-12-16|2016-04-20|钟俊超|Method for preparing wear-resisting large-pore-volume micro-spherical silicon dioxide carrier|

---

CN105521829A|2015-12-16|2016-04-27|钟俊超|Preparation method of wear-resistant large-pore-volume microspherical silica carrier|

---

WO2017131231A1|2016-01-29|2017-08-03|Ｊｘエネルギー株式会社|Method for producing catalyst for fischer-tropsch synthesis and method for producing hydrocarbon|

---

CN108250023A|2016-12-29|2018-07-06|中国石油天然气股份有限公司|A kind of method of acetylene hydrogenation in front-end deethanization front-end hydrogenation technique|

---

CN108250021A|2016-12-29|2018-07-06|中国石油天然气股份有限公司|A kind of acetylene hydrogenation method of MTO technology ethylene feed|

---

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---

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---

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---

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---

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---

CN108262044B|2016-12-30|2021-06-11|中国石油化工股份有限公司|Preparation method of Fischer-Tropsch synthesis catalyst and prepared Fischer-Tropsch synthesis catalyst|

---

EP3351300A1|2017-01-20|2018-07-25|SASOL Germany GmbH|Manganese oxide containing alumina composition, a method for manufacturing the same and use thereof|

---

GB201702251D0|2017-02-10|2017-03-29|Bp Plc|Process for producting a fischer-tropsch synthesis catalyst|

---

EA202092182A1|2018-03-22|2021-02-08|Бп П.Л.К.|COBALT-CONTAINING CATALYST ON A SUBSTRATE FOR FISHER-TROPSCH SYNTHESIS, METHOD OF ITS PREPARATION AND ITS APPLICATION|

---

CN109621966B|2018-12-14|2021-07-09|国网山东省电力公司电力科学研究院|Preparation method of catalyst for sodium hypochlorite oxidation of desulfurization wastewater of coastal power plant|

---

GB201903502D0|2019-03-14|2019-05-01|Johnson Matthey Plc|Cobalt catalysts and precursors therefor|

---

CN111068716A|2019-12-28|2020-04-28|西安建筑科技大学|VOCs separating and degrading film and preparation method thereof|

法律状态:
2018-06-05| B09A| Decision: intention to grant|

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2018-07-03| B16A| Patent or certificate of addition of invention granted|

优先权:

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申请号 | 申请日 | 专利标题

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PCT/IB2011/051876|WO2012146950A1|2011-04-28|2011-04-28|Catalysts|

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