Abstract: A gas replacement process and a gas replacement apparatus are employed, in the nitro compound hydrogenation reaction process. The gas replacement process at least includes a first step of subjecting a stream to be replaced to the gas replacement in presence of a first replacement gas, and then a second step of subjecting to the gas replacement in presence of the second replacement gas. Assuming the superficial velocity of the first replacement gas is V1, and the superficial velocity of the second replacement gas is V2, then V2/V1?1.5.

Abstract: The present invention relates to a nitro compound hydrogenation reaction process and hydrogenation reaction apparatus, which can achieve the objects of the continuous reaction of the nitro compound and the long-period run of regeneration and activation. The nitro compound hydrogenation reaction process comprises a hydrogenation step, a regeneration step, an optional activation step and a recycling step. There exists at least one step of degassing the spent catalyst between the hydrogenation step and the regeneration step. According to circumstances, there exists at least one step of degassing the regenerated catalyst between the regeneration step and the activation step.

Abstract: A fluidized apparatus contains a double-trapezoid structural member. These fluidized apparatuses are used in the nitro compound hydrogenation reaction process. The fluidized apparatus includes a shell, a gas distributor, and an inner chamber defined by an inner wall of said shell and an upper surface of said gas distributor, in the middle region of said inner chamber is disposed a perforated plate, the perforated plate comprise an outer edge region and a center region, assuming the opening rate of the outer edge region is A1 (the unit is %), assuming the opening rate of the center region is A2 (the unit is %), then A1/A2=0-0.95.

Abstract: A fluidized bed reactor is provided, comprising an inlet zone at a lower position, an outlet zone at an upper position, and a reaction zone between the inlet zone and the outlet zone. A guide plate with through holes is disposed in the reaction zone, comprising a dense channel region in an intermediate region thereof and a sparse channel region disposed on a periphery thereof and encompassing the dense channel region. Catalysts in said fluidized bed reactor can be homogeneously distributed in the reaction zone thereof, whereby the reaction efficiency can be improved. A reaction regeneration apparatus comprising said fluidized bed reactor, and a process for preparing olefins from oxygenates and a process for preparing aromatic hydrocarbons from oxygenates using the reaction regeneration apparatus.

Abstract: Device for use in a fluidized bed reactor includes a gas-solid separator communicated with an outlet of the fluidized bed reactor; a vertically arranged damper, a solid outlet of the gas-solid separator communicated with a lower region of the damper, a gas outlet of the gas-solid separator communicated with an upper region of the damper; a fine gas-solid separator, an inlet of the fine gas-solid separator communicated with the upper region of the damper, and a solid outlet of the fine gas-solid separator communicated with the lower region of the damper. Product from the fluidized bed reactor is fed into the preliminary gas-solid separator, most solid catalysts separated and fed into the lower region; the product entraining the rest catalysts is fed into the upper region, and into the fine gas-solid separator, the rest catalysts fed into the lower region; and final product is obtained from the fine gas-solid separator.

Abstract: A fluidized bed reactor is provided, comprising an inlet zone at a lower position, an outlet zone at an upper position, and a reaction zone between the inlet zone and the outlet zone. A guide plate with through holes is disposed in the reaction zone, comprising a dense channel region in an intermediate region thereof and a sparse channel region disposed on a periphery thereof and encompassing the dense channel region. Catalysts in said fluidized bed reactor can be homogeneously distributed in the reaction zone thereof, whereby the reaction efficiency can be improved. A reaction regeneration apparatus comprising said fluidized bed reactor, and a process for preparing olefins from oxygenates and a process for preparing aromatic hydrocarbons from oxygenates using the reaction regeneration apparatus.

Abstract: Device for use in a fluidized bed reactor includes a gas-solid separator communicated with an outlet of the fluidized bed reactor; a vertically arranged damper, a solid outlet of the gas-solid separator communicated with a lower region of the damper, a gas outlet of the gas-solid separator communicated with an upper region of the damper; a fine gas-solid separator, an inlet of the fine gas-solid separator communicated with the upper region of the damper, and a solid outlet of the fine gas-solid separator communicated with the lower region of the damper. Product from the fluidized bed reactor is fed into the preliminary gas-solid separator, most solid catalysts separated and fed into the lower region; the product entraining the rest catalysts is fed into the upper region, and into the fine gas-solid separator, the rest catalysts fed into the lower region; and final product is obtained from the fine gas-solid separator.

Abstract: A process for producing light olefins is provided. A feedstock enters a pre-reaction zone and contacts a catalyst comprising at least one silicon-aluminophosphate molecular sieve and produces a gas-phase stream; the gas-phase stream and the catalyst enter at least one riser, and the gas-phase stream and the catalyst pass from an outlet of the at least one riser and enter a gas-solid rapid separation zone; the separated gas-phase stream enters a separation section; a first portion of the separated catalyst returns to the pre-reaction zone, and a second portion is regenerated in a regenerator; wherein an inlet of the at least one riser extends into the pre-reaction zone, about 60% to about 90% of the height of the at least one riser passes through a heat exchange zone, and the outlet extends into the gas-solid rapid separation zone.

Abstract: The invention provides a start-up method for a reaction-regeneration unit for preparing light olefins from methanol, which comprises: (a) heating a regenerator with an auxiliary combustion chamber and a reactor with a start-up furnace; (b) charging a catalyst into the regenerator and reactor; (c) closing a spent catalyst slide valve and a regenerated catalyst slide valve after the reactor reaches about 350° C. or more; (d) feeding methanol to the reactor after the dense phase stage of the regenerator reaches about 350° C. or more; (e) opening the spent catalyst slide valve and introducing a carbon deposited catalyst from the reactor to the regenerator after the dense phase stage reaches about 400° C. or more and the average amount of carbon deposits on the catalyst in the reactor reaches about 2.5% or more; (f) raising the regenerator to above about 580° C.; and (g) stopping the start-up furnace and auxiliary combustion chamber.

Abstract: A process for producing at least one light olefin, comprising converting three raw materials in the presence of at least one catalyst comprising at least one molecular sieve and regenerating said at least one catalyst into three separate product streams.

Abstract: A process for producing at least one light olefin comprising: (a) contacting a first raw material comprising methanol with a least one catalyst in a first reaction zone to produce at least one light olefin and at least one inactivated catalyst; (b) transporting the at least one inactivated catalyst to a first regeneration zone to produce at least one first regenerated catalyst, and transporting a portion of the at least one first regenerated catalyst to the first reaction zone; (c) transporting another portion of the at least one first regenerated catalyst to a second regeneration zone to obtain at least one second regenerated catalyst; and (d) transporting the at least one second regenerated catalyst to a second reaction zone, and contacting the at least one second regenerated catalyst with a second raw material comprising C4 olefins to produce a product stream II comprising at least one light olefin.

Abstract: A process for producing light olefins from methanol and/or dimethyl ether is disclosed. It comprises: (a) introducing a feed comprising methanol and/or dimethyl ether into a fluidized-bed reactor from its bottom, and contacting the feed in a dense phase zone and a transition zone of the fluidized-bed reactor with a catalyst, to form an effluent I comprising unreacted feed, reaction products and entrained solid particulate catalyst; (b) introducing a terminating agent consisting of water, alcohol, ether, hydrocarbons, and aromatic at upper portion of the transition zone and/or lower portion of a gas-solid separating zone of the fluidized-bed reactor into the effluent I, to give an effluent II; and (c) passing the effluent II into the gas-solid separating zone in upper portion of the fluidized-bed reactor, where gas-solid separation is accomplished to give a gaseous product stream and solid catalyst.

Abstract: A process for producing light olefins is provided. A feedstock enters a pre-reaction zone and contacts a catalyst comprising at least one silicon-aluminophosphate molecular sieve and produces a gas-phase stream; the gas-phase stream and the catalyst enter at least one riser, and the gas-phase stream and the catalyst pass from an outlet of the at least one riser and enter a gas-solid rapid separation zone; the separated gas-phase stream enters a separation section; a first portion of the separated catalyst returns to the pre-reaction zone, and a second portion is regenerated in a regenerator; wherein an inlet of the at least one riser extends into the pre-reaction zone, about 60% to about 90% of the height of the at least one riser passes through a heat exchange zone, and the outlet extends into the gas-solid rapid separation zone.

Abstract: A process for producing light olefins is provided. A feedstock enters a pre-reaction zone and contacts a catalyst comprising at least one silicon-aluminophosphate molecular sieve and produces a gas-phase stream; the gas-phase stream and the catalyst enter at least one riser, and the gas-phase stream and the catalyst pass from an outlet of the at least one riser and enter a gas-solid rapid separation zone; the separated gas-phase stream enters a separation section; a first portion of the separated catalyst returns to the pre-reaction zone, and a second portion is regenerated in a regenerator; wherein an inlet of the at least one riser extends into the pre-reaction zone, about 60% to about 90% of the height of the at least one riser passes through a heat exchange zone, and the outlet extends into the gas-solid rapid separation zone.

Abstract: The present invention provides a process for increasing ethylene and/or propylene yield during conversion of oxygenates using a system comprising a reactor and a regenerator, wherein the reactor comprises a fluidized bed reactor and a riser reactor, which process increases ethylene and/or propylene yield by using a mixture of the deactivated catalyst from the fluidized bed reactor and the regenerated catalyst from the regenerator in the riser reactor for further cracking the C4+ hydrocarbon stream separated from the product stream.

Abstract: A process for producing light olefins. A feedstock enters a pre-reaction zone and contacts a catalyst comprising at least one silicon-aluminophosphate molecular sieve and produces a gas-phase stream and a catalyst to be regenerated; the gas-phase stream and catalyst to be regenerated enter at least one riser, and the gas-phase stream and catalyst to be regenerated pass from an outlet of the at least one riser and enter a gas-solid rapid separation zone; the separated gas-phase stream enters a separation section; a first portion of the separated catalyst returns to the pre-reaction zone, and a second portion is regenerated in a regenerator; wherein an inlet of the at least one riser extends into the pre-reaction zone, about 60% to about 90% of the height of the at least one riser passes through a heat exchange zone, and the outlet extends into the gas-solid rapid separation zone.

Abstract: Provided are processes for producing ethylene glycol from oxalate(s), wherein two or more reaction zones in series are used, and oxalate feedstock is fed stagewise, or hydrogen feedstock and optionally a solvent are fed stagewise. The present processes achieve higher selectivity for the product and improved stability of catalysts.

Abstract: A process for producing at least one light olefin, comprising converting three raw materials in the presence of at least one catalyst comprising at least one molecular sieve and regenerating said at least one catalyst into three separate product streams.

Abstract: A process for producing at least one light olefin comprising: (a) contacting a first raw material comprising methanol with a least one catalyst comprising at least one silicon-aluminophosphate molecular sieve in a first reaction zone to produce a product stream I comprising at least one light olefin and at least one inactivated catalyst; (b) transporting the at least one inactivated catalyst to a first regeneration zone to produce at least one first regenerated catalyst, and transporting a portion of the at least one first regenerated catalyst to the first reaction zone, wherein the at least one first regenerated catalyst comprises a carbon deposit present in an amount ranging from about 0.8% to about 2.

Abstract: A process for producing lower olefins is disclosed. The technical problem is to overcome the defects presented in the prior art including high reaction pressure, high reaction temperature, low yield and selectivity of lower olefins as the target products, poor stability and short life of catalyst, and limited suitable feedstocks. The disclosed process, which is carried out under the conditions of catalytic cracking olefins and adopts as a feedstock an olefins-enriched mixture containing one or more C4 or higher olefins and optionally an organic oxygenate compound, comprises the steps of: a) letting the feedstock contact with a crystalline aluminosilicate catalyst having a SiO2/Al2O3 molar ratio of at least 10, to thereby produce a reaction effluent containing lower olefins; and b) separating lower olefins from the reaction effluent; wherein, the reaction pressure is from ?0.1 MPa to <0 MPa.