37results about How to "Reduce hydrothermal deactivation" patented technology

The invention provides a method of heavy raw material catalytic conversion and the device, comprising: the heavy hydrocarbon raw material passing through the first and second reaction area of the raiser reactor and contacting with catalyst for first reaction and second reaction, the reactants entering into the settler for the separation of catalyst and oil gas, steam stripping the separated catalyst through stripping section and introducing it to the reactivator for carbon burning reactivation, the reactivated catalyst returning to the raiser reactor after cooled or directly to the raiser reactor for reuse. After the heavy oil passing through the device said above, the volume content of olefin decreases by 10~40%, octane value increases 0.5~1 units, sulfur content in petrol decreases 10~30% by weight. After the poor petrol passing through the device said above, the volume content of olefin decreases by 10~60%, octane value increases 0.5~40 units, sulfur content in petrol decreases 10~50% by weight.

The invention provides a method for circulating a cold regenerated catalyst and application thereof. A regenerated catalyst from a regenerator is cooled by a catalyst cooler to between 200 and 720DEGC, and is not mixed with a hot regenerated catalyst to directly enter a riser reactor, or is mixed with another part of uncooled hot regenerated catalyst into a mixed regenerated catalyst of which thetemperature is not lower than that of the regenerator to enter the riser reactor; and a hydrocarbon raw material undergoes contact reaction with the catalyst in the riser reactor, the reaction material flow enters a settler for the separation of the catalyst and oil gas, the separated catalyst to be regenerated is subjected to steam stripping in a steam stripping section, and then enters the regenerator for coke burning regeneration, and the regenerated catalyst is cooled and returns to the riser reactor for recycling. The method for circulating the cold regenerated catalyst has wide application, can be used for various fluid catalytic cracking processes comprising resid fluid catalytic cracking, wax oil catalytic cracking, gasoline catalytic conversion upgrading and the like, and also can be sued for other gas-solid reaction processes comprising residual oil pretreatment, fluid coking and the like.

The invention provides a method for catalytic conversion of heavy oil, which comprises a fluidized catalytic conversion process that: heavy hydrocarbon raw materials contacts a catalyst in a riser reactor or fluidized bed reactor to react; the reaction temperature is 400 to 650 DEG C (preferably 480 to 560 DEG C); the reaction pressure is 0.11 to 0.4MPa; the contact time is 0.05 to 5 seconds (preferably 0.1 to 3 seconds); and the weight ratio of the catalyst to the raw materials ( catalyst to oil ratio) generally is 3 to 15, preferably 5 to 12. The reaction products flow in a settler for catalyst and oil gas separation; the separated catalyst to be regenerated is stripped by a stripping section and enters a regenerator for coke burning regeneration; and the regenerated catalyst is cooled or directly returns to the riser reactor to be recycled. The method can solve the problems encountered in the resid-blend ratio improvement and gasoline upgrade and update processes of the prior catalytic conversion.

The invention relates to a method for preparing aromatic hydrocarbons through catalytic conversion of methanol. A purpose of the present invention is mainly to solve the problems of low aromatic hydrocarbon yield and serious hydrothermal deactivation of the catalyst in the prior art. According to the technical scheme, a methanol raw material enters a fluidized bed reactor, and is subjected to a contact reaction with a modified ZSM-5 catalyst to obtain an aromatic hydrocarbon-containing product and a spent catalyst; the steam stripped spent catalyst enters a riser regenerator, and contacts a regeneration medium I, and charring is performed at a temperature of 500-600 DEG C; the outlet of the riser regenerator is connected to at least a set of closed cyclone separators; the semi-regeneratedcatalyst separated by the closed cyclone separators enter a fluidized bed regenerator, and contacts a regeneration medium II, and charring is continuously performed at a temperature of 630-700 DEG C;the regenerated catalyst enters a degassing tank; and the degassed product returns to the fluidized bed regenerator. With the technical scheme, the problems in the prior art are well solved. The method of the present invention can be used in the industrial production of aromatic hydrocarbons.

The invention discloses a regeneration method of a catalyst for producing aromatic hydrocarbon from organic oxide through catalytic conversion. The method includes the steps of: 1) feeding a to-be-regenerated catalyst from a system of producing the aromatic hydrocarbon from the organic oxide through the catalytic conversion to a first regenerator to contact the catalyst with a first oxygen-containing gas to perform first regeneration at 500-650 DEG C to obtain a semi-regenerated catalyst and a first regeneration flue gas; and 2) feeding the semi-regenerated catalyst to a second regenerator to contact the catalyst with a second oxygen-containing gas to perform second regeneration at 600-750 DEG C to obtain the regenerated catalyst and a second regeneration flue gas, and then feeding the regenerated catalyst back into a system of producing the aromatic hydrocarbon from the organic oxide through catalytic conversion, wherein the two regenerators are arranged in an up-and-down manner and the first regenerator is arranged above the second regenerator. Compared with the prior art, the method is safer and is low in hydrothermal deactivation and loss rate of the catalyst.

A heat exchanging method in hydrocarbon oil transforming process comprises the step of exchanging heat of hydrocarbon oil with that of a regeneration catalyst in a regenerator by a heat exchanger, wherein the heat exchanger is positioned in the regenerator. The invention also provides a hydrocarbon oil transforming method including the heat exchanging method. According to the heat exchanging method in the hydrocarbon oil transforming process in the invention, the heat exchanger is positioned in the regenerator to exchange the heat of the high-temperature regeneration catalyst with that of the raw material oil in the regenerator, so that the high-temperature regenerator catalyst has less heat loss and that the amount of the raw material oil that can be heated by reducing a certain temperature of the regeneration catalyst per unit is improved, thus improving the heat exchanging efficiency. Additionally, the heat exchanging method of the method can simultaneously perform the function of lowering temperature in the regenerator and preventing the catalyst from hydrothermal deactivation due to overhigh temperature, thus reducing the amount of fresh catalyst to be supplemented and reducing the catalyst consumption. The hydrocarbon oil transforming method of the invention can reduce the yields of dry gas and coke and improve the yield of liquid products.

The invention discloses a technique for producing styrene by alkylating toluene and methanol side chains. The method comprises the steps of mixing and heating methanol vapor and air to obtain a mixture, enabling the mixture to enter a reactor producing formaldehyde by using methanol, and generating formaldehyde under the action of a catalyst; condensing a product, enabling the condensed product to enter a rectifying tower so as to remove water generated in the reaction, pressurizing a product at the tower top, enabling the pressurized product to enter a high-pressure separator, discharging noncondensable gas containing hydrogen from the top of the high-pressure separator, mixing and heating and a product at the bottom and toluene, enabling the mixture to enter a side chain alkylation reactor, enabling a gaseous product to return to therectifying tower after a product obtained in the reaction is subjected to separation by a gas-liquid separator, enabling a liquid product to enter a toluene tower, an ethylbenzene tower and a styrene tower sequentially, enabling toluene to return to the side chain alkylation reactor, and discharging ethylbenzene, styrene and C9<+>heavy aromatics. The technique is of a two-step method for toluene and methanol side chain alkylation, not only can the generation degree of a side reaction between styrene and hydrogen be effectively inhibited, but also the hydrothermal deactivation of the catalyst for side chain alkylation can be alleviated.

The invention relates to a method for preparing aromatic hydrocarbons through efficient conversion of methanol. A purpose of the present invention is mainly to solve the problems of low aromatic hydrocarbon yield and serious hydrothermal deactivation of the catalyst in the prior art. According to the technical scheme, a methanol raw material enters a fluidized bed reactor, and is subjected to a contact reaction with a modified ZSM-5 catalyst under the effective reaction conditions; a spent catalyst enters a riser regenerator, and is regenerated; the obtained semi-regenerated catalyst and fluegas I enter a riser regeneration cyclone separator connected to the riser regenerator; the separated semi-regenerated catalyst enters the zone A of a two-dense bed, and is degassed; the degassed semi-regenerated catalyst partially returns to the riser regenerator, and partially enters a fast bed regenerator and is regenerated; and the obtained regenerated catalyst enters the zone B of the two-dense bed and is degassed and the degassed regenerated catalyst enters the fluidized bed reactor. With the technical scheme, the problem in the prior art is well solved. The method of the present invention can be used in the industrial production of aromatic hydrocarbons.

The invention discloses an anti-reprocessing process for improving oil refining efficiency in the process of oil refining. Mixed wax oil and atmospheric residual oil are respectively fed into a static mixer in a device from a raw material tank in a tank farm and mixed evenly, and then enter a raw material buffer tank. Then use the raw material pump to pump out, pass through the flow control valve, return to heat exchange, and then exchange heat with the oil slurry to 170-220 ° C, and enter the static mixer together with the refined oil to mix evenly. The steam enters the riser through six feed nozzles, contacts with the high-temperature regenerated catalyst from the secondary stage and immediately vaporizes, cracks into light products and generates oil slurry, dry gas and coke. The process strictly controls the reaction and regeneration process, so that the obtained product meets the quality, improves the refining precision, and improves the utilization rate of oil.

A process for catalytic conversion of heavy petroleum hydrocarbon to increase output of ethylene and propylene includes such steps as reaction of crude hydrocarbon oil on catalyst containing pentacycle high-Si zeolite, segmentally filling steam, separating oil gas from carbon-deposited catalyst, separating oil from gas, and gas stripping and regenerating catalyst.

The invention provides a downer reactor light hydrocarbon catalytic converting method and device. The method specifically includes the following steps of firstly, making a preheated or non-preheated light hydrocarbon raw material and a low-temperature regenerant from a regenerant cooler enter the inlet end of a downer reactor and flow downwards along the reactor for catalytic cracking and other reactions, and making a mixture of reaction oil gas and a catalyst go downwards to the tail end of the reactor to be rapidly separated so that the catalyst and the oil gas can be rapidly separated, wherein the main operation conditions include the reaction temperature of 520-680 DEG C, the reaction pressure of 0.11-0.4 MPa, the contact time of 0.05-2 seconds and the agent-to-oil ratio of 6-50; secondly, making a separated to-be-generated agent enter a regenerator to be burned and regenerated after the to-be-generated agent is subjected to steam stripping through a to-be-generated agent stripper,wherein the regeneration temperature is controlled to be 630-730 DEG C; thirdly, making a regenerant from the regenerator enter the regenerant cooler to be cooled into 200-720 DEG C, and making the regenerant recycled in the downer reactor.