There is described a process for producing hydrocarbon products in the diesel boiling range, comprising mainly C 15 -C 18 paraffins and being highly effective as diesel fuel ignition improvers. The process comprises hydroprocessing vegetable oils such as canola, sunflower, soybean and rapeseed oils or some fatty acids in hydroprocessing temperatures (350°-450° C.), pressures (4.8-15.2 MPa) and liquid hourly space velocity (LHSV) of 0.5-5.0 hr -1 depending on the type and purity of the feedstock. Commercially available hydroprocessing catalysts may be used.

Production of hydrocarbons with a relatively high cetane rating

Succinic acid has recently received a great deal of attention in various publications and presentations when discussing the potential of renewable resources for the production of chemical building blocks. As a starting material for a number of conversions, it leads to important derivatives for various industrial branches. In this review, many suggested/published processes are analyzed and the feasibility of the processes toward industrial use in comparison with actual production routes has been evaluated.

Feasibility of production methods for succinic acid derivatives: a marriage of renewable resources and chemical technology

In recent years, the production of hydrocarbon cuts from various sources via the Fischer-Tropsch process has lived a renewed interest. Paraffinic cuts produced via the Fischer-Tropsch reaction can be upgraded either to liquid fuels (middle distillates) or to lubricant base oil of high quality. The first kind of upgrading involves the use of a hydrocracking catalyst whereas for the second kind of upgrading selective hydroisomerization catalysts can be selected. Both catalysts are bifunctional and contain an hydrogenation/dehydrogenation function and an acidic function; however, it is shown that depending of the kind of upgrading needed, the acidic function has to fulfill various requirements. The first part of this article is a short review dealing with long chain n-paraffin hydrocracking mechanisms and catalysts. Specificities of Fischer-Tropsch feedstocks compared to conventional ones as well as the potential impact of oxygenate compounds on the hydrocracking catalysts are underlined. The second part of this article is devoted to the selective hydroisomerization mechanisms and catalysts. It is shown that the topology of the solid acid porosity is a key factor for governing the selectivity of the catalyst towards hydroisomerization.

/pdf/fischer-tropsch-waxes-upgrading-via-hydrocracking-and-2jzcoevsku.pdf

Fischer-Tropsch Waxes Upgrading via Hydrocracking and Selective Hydroisomerization

Ethanol is produced by carbonylation of methanol by reaction with carbon monoxide in the presence of a carbonylation catalyst to form acetic acid which is then converted to an acetate ester followed by hydrogenolysis of the acetate ester formed to give ethanol or a mixture of ethanol and another alcohol which can be separated by distillation Preferably the other alcohol or part of the ethanol recovered from the hydrogenolysis step is recycled for further esterification Carbonylation can be effected using a CO/H2 mixture and hydrogenolysis can similarly be conducted in the presence of carbon monoxide, leading to the possibility of circulating gas between the carbonylation and hydrogenolysis zones with synthesis gas, preferably a 2:1 H2:CO molar mixture being used as make up gas

Process for the production of ethanol

Catalyst in powdered form comprising a major amount of the oxides of a first metal selected from copper or zinc, a second metal selected from chromium, molybdenum, tungsten and vanadium, and optionally, a minor amount of the oxide of a promoter metal. The average particle diameter is from 6 to 20 microns and the particle surface area is from 20 to 70 m2/g. Process for preparing said catalyst which comprises the steps of: (A) adding to a first vessel, (1) a first aqueous solution comprising a copper or zinc salt, and (2) a second aqueous solution comprising a soluble base, or (3) a third aqueous solution comprising a soluble salt of at least one second metal, (B) advancing at least a portion of the aqueous slurry from the first vessel to a second vessel; (C) recovering the solids from the second vessel; and (D) calcining the recovered solids. Catalysts of the invention are useful in both fixed bed and slurry phase reactions for hydrogenating aldehydes, ketones, carboxylic acids and carboxylic acid esters.

Hydrogenation catalyst, process for preparing and process of using said catalyst

A process for the manufacture of 1,4-butanediol and/or tetrahydrofuran, wherein maleic acid or succinic acid is used as the starting material, butyrolactone is produced in defined stages and is hydrogenated to butanediol or tetrahydrofuran, and the by-products formed are in each case recycled to the process.

Manufacture of butanediol and/or tetrahydrofuran from maleic and/or succinic anhydride via γ- butyrolactone

The application relates to crystalline metal silicate zeolites of the ZBM-30 type and to methods of preparing these crystalline metal silicate zeolites. They are prepared by hydrothermal crystallisation at temperatures of 100 to 200 DEG C for mixtures of YO2, in which Y represents the elements silicon and germanium, and W2O3, in which W represents the elements boron, aluminium, iron and gallium, by means of organic amines, the molar ratio of YO2:W2O3 in the reaction mixture being adjusted to a value as a function of the chain length of the organic amine suitable for forming the zeolite.

Crystalline metal-silicate zeolite ZBM-30 and method of preparing it

The double salt Ni6Al2(OH)16 - CO3 - 4H2O is obtained from an aqueous solution containing nickel and aluminum salts by precipitation with alkali metal carbonate or bicarbonate. This double salt (catalyst precursor) is dried, calcined and reduced. There is thus obtained a catalyst which is suitable for the selective hydrogenation of fats and oils.

Nickel-containing hydrogenation catalysts for the selective hydrogenation of fats and oils

Kristalline eisensilikate mit zeolithstruktur

Gases of various origins which contain carbon monoxide and dioxide and hydrogen, for example the gases obtained by steam reforming or the rich gas process, refinery gases or coal gasification gases are methanized on a nickel catalyst. The object of this reaction is to obtain methane or gases which can be substituted for natural gas. To produce the catalyst, the compound Ni6Al2(OH)16.CO3.4H2O is obtained from aqueous solution. The catalyst is obtained from this compound after drying, calcination and subsequent reduction in a stream of hydrogen, whilst maintaining very specific temperature gradients between the drying stage and the calcination stage.

Catalyst and its use for the manufacture of methane from gases containing carbon monoxide and dioxide and hydrogen

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