A process for converting a hydrocarbon feedstock to provide an effluent containing light olefins, the process comprising passing a hydrocarbon feedstock, the feedstock containing at least one C 1 to C 6 aliphatic hetero compound selected from alcohols, ethers, carbonyl compounds and mixtures thereof and steam in an amount whereby the feedstock contains up to 80 weight % steam, through a reactor containing a crystalline silicate catalyst to produce an effluent including propylene, the crystalline silicate having been subjected to de-alumination by a steaming step and being selected from at least one of an MFI-type crystalline silicate having a silicon/aluminium atomic ratio of from 250 to 500 and an MEL-type crystalline silicate having a silicon/aluminium atomic ratio or from 150 to 800.

Production of olefins

An FCC process for obtaining light olefins comprises contacting a hydrocarbon feed stream with blended catalyst comprising regenerated catalyst and coked catalyst. The catalyst has a composition including a first component and a second component compring a zeolite with no greater than medium pore size wherein the zeolite comprises at least 1 wt-% of the catalyst composition. The hydrocarbon feed stream is in contact with the blended catalyst in a riser for less than or equal to 2 seconds on average. A first portion of the coked catalyst is passed to a regeneration zone, while a second portion of the coked catalyst is blended with the regenerated catalyst and introduced to the riser.

FCC process with improved yield of light olefins

Methods for separating olefins from non-olefins, such as paraffins, including cycloparaffins, oxygenates and aromatics, are provided. The methods use metal salts to complex olefins, allowing the non-olefins to be separated by a variety of methods, including decantation and distillation. The metal salts are dissolved in ionic liquids, which tend to have virtually no vapor pressure, and which poorly solubilize the non-olefins. Accordingly, the non-olefins phase separate well, and can be distilled without carrying over any of the ionic liquid into the distillate. Preferred salts are Group IB salts, more preferably silver salts. A preferred silver salt is silver tetrafluoroborate. Preferred ionic liquids are those which form stable solutions or dispersions of the metal salts, and which do not dissolve the non-olefins. Further, if the olefins are subject to isomerization, the ionic liquid is preferably relatively non-acidic. The methods involve forming a solution of a suitable olefin-complexing salt in an appropriate ionic liquid. An olefin-containing mixture is contacted with the ionic liquid/salt solution, and the olefins are adsorbed. After the paraffins are removed, the olefins can be isolated by desorption. The olefin-containing mixture can be in the gas phase, or in the liquid phase. The flow of olefin-containing mixtures over/through the ionic liquid can be, for example, co-current, counter-current, or staged in stirred tanks. Countercurrent is preferred as it is the most efficient. The methods can be optimized using combinatorial chemistry.

Separation of olefins from paraffins using ionic liquid solutions

Disclosed is a process for making middle distillate and lower olefins. The process includes catalytically cracking a gas oil feedstock within a riser reactor zone by contacting under suitable catalytic cracking conditions within the riser reactor zone the gas oil feedstock with a middle distillate selective cracking catalyst that comprises amorphous silica alumina and a zeolite to yield a cracked gas oil product and a spent cracking catalyst. The spent cracking catalyst is regenerated to yield a regenerated cracking catalyst. Within a dense bed reactor zone and under suitable high severity cracking conditions a gasoline feedstock is contacted with the regenerated cracking catalyst to yield a cracked gasoline product and a used regenerated cracking catalyst. The used regenerated cracking catalyst is utilized as the middle distillate selective catalyst.

Method and apparatus for making a middle distillate product and lower olefins from a hydrocarbon feedstock

Described is a hydrocarbon cracking process for converting a heavy hydrocarbon feedstock selectively to middle distillate and lower olefins by catalytically cracking a heavy hydrocarbon feedstock within a riser reactor zone by contacting the heavy hydrocarbon feedstock with both a middle distillate selective cracking catalyst in combination with a shape selective zeolite additive under suitable catalytic cracking reaction conditions.

Hydrocarbon cracking process for converting gas oil preferentially to middle distillate and lower olefins

Various fractions of petroleum, including residual oils and crude oils, are catalytically converted to produce gaseous olefins, especially propylene and butylene, in fluidized or moving bed or transfer line reactors with solid, acidic catalysts in the presence of steam at a temperature of 500° to 650° C. and a pressure of 1.5×10 5 Pa to 3×10 5 Pa, with a weight space velocity of 0.2 to 20 hr -1 and catalyst-to-oil ratio of 2 to 12. Spent catalyst is continuously removed from the reactor to a regenerator where the coke is burned off and the hot catalyst is returned to the reactor. In a comparison with conventional catalytic cracking and tubular furnance pyrolysis processes, it is found that the process of the present invention produces more propylene and butylene. The total yield of the process of the present invention is about 40 percent by weight of the feedstock.

Production of gaseous olefins by catalytic conversion of hydrocarbons

A cracking catalyst for the production of light olefins comprises 0-70% (based on the weight of the catalyst) of clay, 5-99% of inorganic oxides, and 1-50% of zeolite. The zeolite in the catalyst is a mixture of 0-25 wt % of REY or high silica Y zeolite and 75-100 wt % of phosphorus and rare earth containing high silica zeolite having a structure of pentasil. The catalyst exhibits higher hydrothermal activity-stability, conversion level, and C2 -C4 olefin yields in cracking reaction, comparing with the catalyst using HZSM-5 zeolite as active component.

Cracking catalyst for the production of light olefins

Hydrocarbon catalytic converting process for manufacturing of lower olefine

Various fractions of petroleum, including residual oils and crude oils, are catalytically converted to produce gaseous olefins, especially propylene and butylene, in fluidized or moving bed reactors with solid acidic catalysts in the presence of steam at a temperature of 500 DEG C to 650 DEG C and a pressure of 15 x 10 Pa to 3 x 10 Pa, with a weight space velocity of 02 to 20 hr and a catalyst-to-oil ratio of 2 to 12 Spent catalyst is continuously removed from the reactor to a regenerator where the coke is burned off and then the hot catalyst returned to the reactor Comparing with the conventional catalytic cracking and tubular furnace pyrolysis process, the present invention produces more propylene and butylene, their total yield is about 40 per cent by weight of the feedstock

Ge Xingpin

Papers

Production of gaseous olefins by catalytic conversion of hydrocarbons

Cracking catalyst for the production of light olefins

Hydrocarbon catalytic converting process for manufacturing of lower olefine

Catalytic conversion method for prodn. of low carbon olefine