A lift engager for providing a stream of fluidized catalyst particles with an adjustable conduit and process using the lift engager. The lift engager includes a vessel with an inlet configured to receive catalyst from a reaction zone. A first conduit, within the vessel, is configured to supply lift gas into the lift engager. The first conduit includes a fixed member and a movable member secured to the fixed member and is configured to adjust a length of the first conduit within the vessel. A second conduit inside the first conduit and configured to provide fluidized catalyst to a regeneration zone.

A family of highly charged crystalline microporous metallophosphate molecular sieves designated PST-17 has been synthesized. These metallophosphates are represented by the empirical formula of:
R.sup.p+.sub.rA.sub.m.sup.+M.sub.xE.sub.yPO.sub.z
where A is an alkali metal such as potassium, R is a quaternary ammonium cation such as ethyltrimethylammonium, M is a divalent metal such as zinc and E is a trivalent framework element such as aluminum or gallium. The PST-17 family of molecular sieves are stabilized by combinations of alkali and organoammonium cations, enabling unique metalloalumino(gallo)phosphate compositions and exhibit the BPH topology. The PST-17 family of molecular sieves has catalytic properties for carrying out various hydrocarbon conversion processes and separation properties for separating at least one component.

A process for producing transport fuel blendstocks comprises providing a first feedstock comprising butane and propane and a second feedstock comprising benzene and dehydrogenating the first feedstock in a first reactor to produce a C4 product comprising butane and butene and a C3 product comprising propane and propylene. The process also comprises oligomerizing the C4 product in a second reactor to produce a first transport fuel blendstock and alkylating the C3 product with the second feedstock in a third reactor to produce a second transport fuel blendstock.

Disclosed are a system device for preparing an alkylate oil using a sulfuric acid catalyst and a manufacturing method thereof. The system device comprises a reactor unit (100), a catalyst and hydrocarbon circulation unit (200), a separator unit (300), an isobutane circulation unit (500) and a fractionator unit (400). The reactor unit (100) is connected and in communication with the catalyst and hydrocarbon circulation unit (200) and the separator unit (300) via channels respectively. The catalyst and hydrocarbon circulation unit (200) is connected and in communication with the separator unit (300) via channels. The separator unit (300) is connected and in communication with the isobutane circulation unit (500) and the fractionator unit (400) via channels respectively. The catalyst and hydrocarbon circulation unit (200), the separator unit (300), the isobutane circulation unit (500) and the fractionator unit (400) are connected and in communication with the reactor unit (100) via channels respectively. The reactor unit (100) comprises at least a high gravity reactor. Due to the adopted high gravity reactor capable of highly reinforcing the mixing of materials under high viscosity, the system device can operate at a low temperature of 5 C. and prepare the alkylate oil having an octane number of 97-100 at an alkane/alkene ratio of 2-100.

Disclosed herein are processes for producing and separating ethane and ethylene. In some embodiments, an oxidative coupling of methane (OCM) product gas comprising ethane and ethylene is introduced to a separation unit comprising two separators. Within the separation unit, the OCM product gas is separated to provide a C.sub.2-rich effluent, a methane-rich effluent, and a nitrogen-rich effluent. Advantageously, in some embodiments the separation is achieved with little or no external refrigeration requirement.

Improved alkylation catalysts, alkylation methods, and methods of making alkylation catalysts are described. The alkylation method comprises reaction over a solid acid, zeolite-based catalyst and can be conducted for relatively long periods at steady state conditions. The alkylation catalyst comprises a crystalline zeolite structure, a Si/Al molar ratio of 20 or less, less than 0.5 weight percent alkali metals, and further having a characteristic catalyst life property. Some catalysts may contain rare earth elements in the range of 10 to 35 wt %. One method of making a catalyst includes a calcination step following exchange of the rare earth element(s) conducted at a temperature of at least 575 C. to stabilize the resulting structure followed by an deammoniation treatment. An improved method of deammoniation uses low temperature oxidation.

An improved alkylation process with improved octane number and lower final boiling point. Further, the present disclosure comprises an alkylation system that allows flexibility in the operating parameters without loss of productivity. This enhances the advantage of the solid acid alkylation process of the invention over the liquid acid processes, as the C9+ alkylate will mainly contain the desired highly branched paraffin's in the case of solid acid alkylation. By fractionation of C9+, the RON number of the gasoline alkylate after fractionation remains very high, while the final boiling point of the gasoline fraction will decrease, improving value and blending flexibility.

A process for the preparation of a chemical composition comprising an aromatic compound in a concentration B by weight, based on the total weight of the chemical composition, comprising: a. providing the following reaction components: i. a chemical composition comprising the following: a) The aromatic compound in a concentration A by weight based on the total weight of the chemical composition, and b) An olefin in an amount in an amount of about 50 to about 99.99 wt. %, based on the total weight of the chemical composition, and ii. An acid; and b. reacting the components to obtain the chemical composition comprising the aromatic compound in a concentration B by weight based on the total weight of the chemical composition; wherein the concentration B is less than the concentration A.

A liquid-solid axial moving bed reaction and regeneration apparatus and a solid acid alkylation process by using the liquid-solid axial moving bed reaction and regeneration apparatus. the liquid-solid axial moving bed reaction and regeneration apparatus comprise: An axial moving bed reactor (1), a spent catalyst receiver (5), a catalyst regenerator (4) and a regenerated catalyst receiver (6) that are successively connected, wherein, a catalyst outlet of the regenerated catalyst receiver (6) is communicated with a catalyst inlet of the axial moving bed reactor (1); Wherein, the axial moving bed reactor (1) is provided with at least two catalyst beds (3) arranged up and down, the axial moving bed reactor (1) is provided with a feed inlet (2) above each catalyst bed (3); A catalyst delivery pipe (16) is arranged between two adjacent catalyst beds (3) so that the catalyst can move from top to bottom in the axial moving bed reactor (1); A separation component (10) is provided between two adjacent catalyst beds (3), the inside space of the separation component (10) is communicated with the catalyst delivery pipe (16), the separation component (10) is for separating the stream after the reaction in the upstream catalyst bed from the catalyst, the catalyst obtained by the separation with the separation component (10) moves down through the catalyst delivery pipe (16).

Improved alkylation catalysts, alkylation methods, and methods of making alkylation catalysts are described. The alkylation method comprises reaction over a solid acid, zeolite-based catalyst and can be conducted for relatively long periods at steady state conditions. The alkylation catalyst comprises a crystalline zeolite structure, a Si/Al molar ratio of 20 or less, less than 0.5 weight percent alkali metals, and further having a characteristic catalyst life property. Some catalysts may contain rare earth elements in the range of 10 to 35 wt %. One method of making a catalyst includes a calcination step following exchange of the rare earth element(s) conducted at a temperature of at least 575 C. to stabilize the resulting structure followed by an deammoniation treatment. An improved method of deammoniation uses low temperature oxidation.