There is provided a catalyst that enables the production of isobutylene with a high selectivity in the production of isobutylene by dehydration of isobutanol. The catalyst according to the present invention contains at least one metal selected from Group 6 to Group 14 metal elements in Period 4 to Period 6 of the periodic table, in alumina which includes alumina consisting of one or more crystal phases of a monoclinic crystal phase, a tetragonal crystal phase, and a cubic crystal phase.

There is provided a catalyst that enables the production of isobutylene with a high selectivity in the production of isobutylene by dehydration of isobutanol. The catalyst according to the present invention contains at least one metal selected from Group 6 to Group 14 metal elements in Period 4 to Period 6 of the periodic table, in alumina which includes alumina consisting of one or more crystal phases of a monoclinic crystal phase, a tetragonal crystal phase, and a cubic crystal phase.

A method of producing a fuel additive includes passing a feed stream comprising C4 hydrocarbons through a hydrogenation unit producing a hydrogenated stream; passing the hydrogenated stream through a distillation unit producing a first stream and a second stream; producing an isobutylene stream by passing the first stream through a molecular sieve unit; passing the isobutylene stream to a hydration unit as a feedstock for the fuel additive; and forming the fuel additive in the hydration unit.

A method of producing a fuel additive includes passing a feed stream comprising C4 hydrocarbons through a hydrogenation unit producing a hydrogenated stream; passing the hydrogenated stream through a distillation unit producing a first stream and a second stream; producing an isobutylene stream by passing the first stream through a molecular sieve unit; passing the isobutylene stream to a hydration unit as a feedstock for the fuel additive; and forming the fuel additive in the hydration unit.

Process for preparing a catalyst composition containing a modified crystalline aluminosilicate and a binder, wherein the catalyst composition comprises from 5 to 95% by weight of crystalline aluminosilicate as based on the total weight of the catalyst composition, the process being remarkable in that it comprises a step of steaming said crystalline aluminosilicate: at a temperature ranging from 100° C. to 380° C.; under a gas phase atmosphere containing from 5 wt % to 100 wt % of steam; at a pressure ranging from 2 to 200 bars; at a partial pressure of H.sub.2O ranging from 2 to 200 bars; and said steaming being performed during at least 30 min and up to 144 h;
and in that the process also comprises a step of shaping, or of extruding, the crystalline aluminosilicate with a binder, wherein the binder is selected to comprise at least 85 wt % of silica as based on the total weight of the binder, and less than 1000 ppm by weight as based on the total weight of the binder of aluminium, gallium, boron, iron and/or chromium.

Process for preparing a catalyst composition containing a modified crystalline aluminosilicate and a binder, wherein the catalyst composition comprises from 5 to 95% by weight of crystalline aluminosilicate as based on the total weight of the catalyst composition, the process being remarkable in that it comprises a step of steaming said crystalline aluminosilicate: at a temperature ranging from 100° C. to 380° C.; under a gas phase atmosphere containing from 5 wt % to 100 wt % of steam; at a pressure ranging from 2 to 200 bars; at a partial pressure of H.sub.2O ranging from 2 to 200 bars; and said steaming being performed during at least 30 min and up to 144 h;
and in that the process also comprises a step of shaping, or of extruding, the crystalline aluminosilicate with a binder, wherein the binder is selected to comprise at least 85 wt % of silica as based on the total weight of the binder, and less than 1000 ppm by weight as based on the total weight of the binder of aluminium, gallium, boron, iron and/or chromium.

The present disclosure relates to a process for converting one or more methyl halides to acyclic C3-C6 olefins, said process comprising the steps of (a) providing a feedstream comprising one or more methyl halides; (b) providing a catalyst composition; and (c) contacting said feedstream with said catalyst composition under reaction conditions. The process is remarkable in that said reaction conditions include a reaction temperature below 400° C., and in that said catalyst composition comprises one or more molecular sieves with a Si/Al atomic ratio ranging from 2 to 18 and wherein said one or more molecular sieves comprise a plurality of pores, wherein said pores have a shape of an 8-membered ring or less.

The present disclosure relates to a process for converting one or more methyl halides to acyclic C3-C6 olefins, said process comprising the steps of (a) providing a feedstream comprising one or more methyl halides; (b) providing a catalyst composition; and (c) contacting said feedstream with said catalyst composition under reaction conditions. The process is remarkable in that said reaction conditions include a reaction temperature below 400° C., and in that said catalyst composition comprises one or more molecular sieves with a Si/Al atomic ratio ranging from 2 to 18 and wherein said one or more molecular sieves comprise a plurality of pores, wherein said pores have a shape of an 8-membered ring or less.

The invention relates to a process, unit and reaction system of low-carbon alkane dehydrogenation, which comprises the following steps: C3-C5 low-carbon alkane feed gas, together with CO and/or CO.sub.2 process gas, get into reactor after being preheated to 200-500° C., contact with a Cr—Ce—Cl/Al.sub.2O.sub.3 dehydrogenation catalyst, a Cu—Ce—Ca—Cl/Al.sub.2O.sub.3 thermal generating agent and thermal storage/support inert alumina balls, and convert to dehydrogenation products for 5-30 minutes under the conditions: temperature, 500-700° C., pressure, 10-100 kPa and weight hourly space velocity (WHSV), 0.1-5 hours.sup.−1. The products formed enter the downstream separation unit for separating out the low-carbon alkenes. The periodic regeneration process of the catalyst bed includes steam purging, hot air regenerating, bed heating, evacuating and reducing at 560 to 730° C. and 0.01 to 1 MPa. Each cycle needs about 10-70 minutes. With such dehydrogenation process, the reaction heat balance is moderated, and temperature gradient and reaction severity in the catalyst bed are reduced. As a consequence, the catalytic conversion, product selectivity, operation cycle and service life are improved. The system energy consumption is reduced.

The invention relates to a process, unit and reaction system of low-carbon alkane dehydrogenation, which comprises the following steps: C3-C5 low-carbon alkane feed gas, together with CO and/or CO.sub.2 process gas, get into reactor after being preheated to 200-500° C., contact with a Cr—Ce—Cl/Al.sub.2O.sub.3 dehydrogenation catalyst, a Cu—Ce—Ca—Cl/Al.sub.2O.sub.3 thermal generating agent and thermal storage/support inert alumina balls, and convert to dehydrogenation products for 5-30 minutes under the conditions: temperature, 500-700° C., pressure, 10-100 kPa and weight hourly space velocity (WHSV), 0.1-5 hours.sup.−1. The products formed enter the downstream separation unit for separating out the low-carbon alkenes. The periodic regeneration process of the catalyst bed includes steam purging, hot air regenerating, bed heating, evacuating and reducing at 560 to 730° C. and 0.01 to 1 MPa. Each cycle needs about 10-70 minutes. With such dehydrogenation process, the reaction heat balance is moderated, and temperature gradient and reaction severity in the catalyst bed are reduced. As a consequence, the catalytic conversion, product selectivity, operation cycle and service life are improved. The system energy consumption is reduced.