Disclosed is a method for starting up fluidized reaction apparatus that is used for producing lower olefins from methanol or/and dimethyl ether. Said method includes after heating the catalyst bed of circulating fluidized catalytic reaction apparatus to above 200 C. or 300 C. by using a starting-up auxiliary heat source, feeding methanol or dimethyl ether raw materials to a reactor, whereby heat released by the reaction makes the temperature of the reaction system apparatus increase quickly to a designed temperature, consequently making the system reach normal operation state rapidly. Said method is suitable for starting up an exothermic fluidized catalytic reaction apparatus and can simplify the apparatus and operation, accordingly lowering the cost.

Disclosed is a method for starting up fluidized reaction apparatus that is used for producing lower olefins from methanol or/and dimethyl ether. Said method includes after heating the catalyst bed of circulating fluidized catalytic reaction apparatus to above 200 C. or 300 C. by using a starting-up auxiliary heat source, feeding methanol or dimethyl ether raw materials to a reactor, whereby heat released by the reaction makes the temperature of the reaction system apparatus increase quickly to a designed temperature, consequently making the system reach normal operation state rapidly. Said method is suitable for starting up an exothermic fluidized catalytic reaction apparatus and can simplify the apparatus and operation, accordingly lowering the cost.

A catalyst comprising a Group IIIA metal, a Group VIII noble metal, and an optional promoter metal, on a support selected from silica, alumina, silica-alumina compositions, rare earth modified alumina, and combinations thereof, doped with iron, a Group VIB metal, a Group VB metal, or a combination thereof, offers decreased reactivation time under air soak in comparison with otherwise identical catalysts. Reducing reactivation time may, in turn, reduce costs, both in inventory and capital.

A catalyst comprising a Group IIIA metal, a Group VIII noble metal, and an optional promoter metal, on a support selected from silica, alumina, silica-alumina compositions, rare earth modified alumina, and combinations thereof, doped with iron, a Group VIB metal, a Group VB metal, or a combination thereof, offers decreased reactivation time under air soak in comparison with otherwise identical catalysts. Reducing reactivation time may, in turn, reduce costs, both in inventory and capital.

The present invention provides a method of cooling and cycling a regenerated catalyst. The regenerated catalyst that is from the regenerator is cooled by the catalyst cooler to 200-720 C., and without being mixed with the hot regenerated catalyst directly enters a riser reactor, or mixes with another part of hot regenerated catalyst that has not been cooled to obtain a mixed regenerated catalyst with a temperature below the regenerator temperature, and enters the riser reactor. The hydrocarbon raw material performs the contact reaction with the catalyst in the riser reactor, a reactant stream enters a settler to perform a separation of the catalyst and an oil gas, the separated spent catalyst is steam stripped by a steam stripping section and enters a regenerator to be charring regenerated, and the regenerated catalyst after being cooled returns to the riser reactor to be circularly used. The bottom of each of the catalyst coolers is provided with at least one fluidized medium distributor, the range of the superficial gas velocity is 0-0.7 m/s (preferably 0.005-0.3 m/s, and most preferably 0.01-0.15 m/s), and the temperature of the cold regenerated catalyst is controlled mainly by adjusting a flow rate of the fluidized medium. The method of cooling and cycling a regenerated catalyst of the present invention has extensive application, and can be used for various fluidized catalytic cracking processes, including heavy oil catalytic cracking, wax oil catalytic cracking, gasoline catalytic conversion reforming and the like, and can also be used for other gas-solid reaction processes, including residual oil pretreating, methanol to olefin, methanol to aromatics, methanol to propylene, fluid coking, flexicoking and the like.

Systems for dehydrogenating an alkane are provided. An exemplary system includes a furnace and further includes alkane heating chambers, regeneration mixture heating chambers, and two groups of reaction chambers, all located within the furnace. The alkane heating chambers and regeneration mixture heating chambers can preheat an alkane feed and a regeneration mixture feed, respectively. The two groups of reaction chambers can be switchably coupled to an alkane feed and a regeneration mixture feed such that an alkane can flow through one group of reaction chambers while a regeneration mixture flows through the other group of reaction chambers. Processes for dehydrogenating an alkane are also provided.

A catalyst regeneration gas loop is operated in a heat exchanger decoking mode. A regeneration gas is diverted away from a burn zone of the catalyst regeneration gas loop and to a heat exchanger, where coke deposits are disposed on a surface of the heat exchanger. The regeneration gas is prevented from flowing to an oxychlorination/calcination zone of the catalyst regeneration gas loop. Within the heat exchanger, the coke deposits are combusted with oxygen of the regeneration gas, thereby removing the coke deposits from the surface of the heat exchanger and producing carbon dioxide. Oxygen is replenished to the regeneration gas. The regeneration gas is recycled to the heat exchanger.

A catalyst regeneration gas loop is operated in a heat exchanger decoking mode. A regeneration gas is diverted away from a burn zone of the catalyst regeneration gas loop and to a heat exchanger, where coke deposits are disposed on a surface of the heat exchanger. The regeneration gas is prevented from flowing to an oxychlorination/calcination zone of the catalyst regeneration gas loop. Within the heat exchanger, the coke deposits are combusted with oxygen of the regeneration gas, thereby removing the coke deposits from the surface of the heat exchanger and producing carbon dioxide. Oxygen is replenished to the regeneration gas. The regeneration gas is recycled to the heat exchanger.

A catalyst regeneration gas loop is operated in a heat exchanger decoking mode. A regeneration gas is diverted away from a burn zone of the catalyst regeneration gas loop and to a heat exchanger, where coke deposits are disposed on a surface of the heat exchanger. The regeneration gas is prevented from flowing to an oxychlorination/calcination zone of the catalyst regeneration gas loop. Within the heat exchanger, the coke deposits are combusted with oxygen of the regeneration gas, thereby removing the coke deposits from the surface of the heat exchanger and producing carbon dioxide. Oxygen is replenished to the regeneration gas. The regeneration gas is recycled to the heat exchanger.

A catalyst regeneration gas loop is operated in a heat exchanger decoking mode. A regeneration gas is diverted away from a burn zone of the catalyst regeneration gas loop and to a heat exchanger, where coke deposits are disposed on a surface of the heat exchanger. The regeneration gas is prevented from flowing to an oxychlorination/calcination zone of the catalyst regeneration gas loop. Within the heat exchanger, the coke deposits are combusted with oxygen of the regeneration gas, thereby removing the coke deposits from the surface of the heat exchanger and producing carbon dioxide. Oxygen is replenished to the regeneration gas. The regeneration gas is recycled to the heat exchanger.