KR900013059A - Process and apparatus for catalytic cracking of hydrocarbons - Google Patents

Abstract

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Description

Process and apparatus for catalytic cracking of hydrocarbons

Since this is an open matter, no full text was included.

The accompanying drawings are schematic diagrams of the process and apparatus of the present invention as shown in a combination fluidization catalytic cracking-regeneration operation, each of which is provided with two riser reactors, a heavy hydrocarbon feed and a light naphtha feed. Are catalytically cracked independently, and catalyst regeneration is carried out continuously in two separate relative hot and cold zones.

Claims (6)

Fluidized Catalytic Decomposition comprising a Separated First and Second Catalytic Regeneration Zone and Decomposing a Hydrocarbon Feed Material or Vapor as a Decomposition Catalyst In a regeneration process, the catalyst is a relatively carbon monoxide-rich first regeneration zone. The first and second continuously by burning hydrocarbonaceous deposits on the catalyst in the presence of an oxygen-containing gas under conditions effective to produce a flue gas and a second, regeneration zone flue gas enriched with relatively carbon dioxide. Continued regeneration in the regeneration zone, the temperature of the first regeneration zone is in the range of about 1100 ° F to about 1300 ° F, and the temperature of the second regeneration zone is in the range of about 1300 ° F to about 1800 ° F, (a) At a temperature of at least 1300 ° F., a catalyst to oil ratio of 5 to 10 and a settling time of 1 to 4 seconds, the first catalyst is present in the presence of the regenerated cracking catalyst supplied from the second catalyst regeneration zone. Decomposing a first hydrocarbon feed comprising gas oil and / or residual oil ratio range materials in the enter riser reactor, in which step coke is deposited on the catalyst in an amount of less than 1.2% by weight. A first hydrocarbon comprising naphtha fraction, a substance that boils more than the heavy naphtha fraction, a light cycle oil, a heavy cycle oil, and a substance that is higher than the heavy cycle oil; Obtaining the evaporative conversion product of the feed and (b) from the second catalyst regeneration zone at a temperature of at least 1300 ° F., a catalyst to oil ratio of 3 to 12 and a settling time of 1 to 5 seconds, concurrently with the above steps A second carbonization comprising virgin naphtha and / or intermediate and cracked naphtha boiling range materials in a second extension riser reactor in the presence of a regenerated cracking catalyst supplied Wherein the coke is deposited on the catalyst in an amount of less than 0.5 weight percent, comprising light hydrocarbon material from light cycle oil material and gasoline boiling range material with high aromatic content and octane number. Obtaining an evaporative conversion product of the second hydrocarbon feed, (c) passing and combining the evaporative conversion product from the first and second extension riser reactors in a conventional disengaging zone, incorporating in this step The entrained catalyst particles are separated from the evaporative product and the combined conversion products are passed through a fractional distillation zone, so that at least gasoline boiling range fraction and light gaseous hydrocarbon fraction fraction, heavy naphtha boiling range fraction, slurry oil and Heavy-cycle boiling range mass fraction and light cycle oil boiling, including high-boiling substance mass fraction A method for improving a process comprising recovering a range of substances and the like. The method of claim 1, wherein at least a portion of the gasoline and / or heavy naphtha fraction is recycled and recomposed in a second riser reactor and / or a first riser reactor. The method of claim 2, wherein the gasoline and / or heavy naphtha fraction is re-decomposed in the presence of direct current naphna to improve the octane ratio and aromatic content. The method of claim 1, wherein the first hydrocarbon feed comprises a heavy hydrocarbon feed, the heavy hydrocarbon feed having at least 400 ° with at least 20 weight percent of its components boiling at 1000 ° F. or more. The first hydrocarbon feed has at least 2 weight percent Conradsor carbon boiling at F, and the second hydrocarbon feed is medium containing a direct boiling naphtha boiling in the range of 10 ° F to 392 ° F and boiling up to about 450 ° F. And / or heavy naphtha. The hydrocarbon feed or its vapors are cracked in a fluidized state with micronized cracking catalyst to produce spent catalyst particles and cracking products with hydrocarbonaceous deposits, stripping evaporative hydrocarbon products from the catalyst particles and fouling The fouled catalyst is transported to the first regeneration zone and associated with hydrocarbonaceous deposits on the catalyst at temperatures below about 1300 ° F in the presence of an effective amount of oxygen and gas containing pressure ranging from about 15 to about 40 psig. By burning almost all hydrocarbons the catalyst is partially regenerated to produce a first regeneration zone flue gas having a carbon monoxide content ranging from about 2 to about 80 volume percent, and then the partially regenerated catalyst is subjected to a second regeneration zone. To about 1300 ° F to 1800 ° F in the presence of an effective amount of oxygenated gas. Fluidization catalytic cracking—regeneration, whereby the catalyst is completely regenerated by burning almost all hydrocarbonaceous deposits remaining on the catalyst surface at a high temperature to produce a second regeneration zone flue gas having a carbon monoxide content of less than about 1200 parts per million of volume. In the process, (a) the first catalyst in the presence of a regenerated cracking catalyst supplied from a second catalyst regeneration zone at a residence time of 1 to 4 seconds, a catalyst to oil ratio of 5 to 10 and a temperature of at least 1300 ° F. Decomposing a first hydrocarbon feed comprising gas oil and / or residual oil boiling range material in an extended riser reactor, in which step coke is deposited on the catalyst in an amount of less than 1.2 weight percent, thereby providing a heavy naphtha fraction and the Substances boiling higher than heavy naphtha oil, light cycle oils, heavy cycle oils, and substances boiling higher than the heavy cycle oils, etc. Obtaining an evaporative conversion product of the first hydrocarbon feed comprising, and (b) concurrently with the above steps, a second residence time of 1 to 5 seconds, a catalyst to oil ratio of 3 to 12, and a temperature of at least 1300 ° F. Agents comprising direct current naphtha, intermediate cracked naphtha or intermediate cracked naphtha, or mixtures thereof, boiling range materials, etc. in a second extended riser reactor in the presence of a regenerated cracking catalyst supplied from the catalyst regeneration zone of In this step, the hydrocarbon feed is decomposed, and coke is deposited on the catalyst in an amount of less than 0.4% by weight to light hydrocarbon materials from light cycle oil materials and gasoline boiling range materials having high aromatic content and octane number. Obtaining an evaporative conversion product of the second hydrocarbon feed comprising, and (c) evaporative conversion production from the first and second extended riser reactors. Water is passed through and combined in a normal disengaging zone, where the mixed catalyst particles are separated from the evaporative product and the combined conversion product is passed through a fractional distillation zone, at least gasoline boiling range material fraction and hard Recovering the heavy cycle boiling range material and light cycle oil boiling material fraction comprising gaseous hydrocarbon material fraction, heavy naphtha boiling range fraction, slurry oil and high boiling fraction fraction, and the like. . (A) consumption of cracked products and hydrocarbonaceous deposits by contacting them with gas oil and / or residual oil boiling range materials, including fluidized beds of finely divided regenerated catalyst particles, which break down hydrocarbon feedstocks into cracking catalysts. A first riser reactor producing an effluent comprising catalyst particles, and (b) contacting the catalyst particles with direct current naphtha, moderately decomposed naphtha or moderately decomposed naphtha boiling range materials or mixtures thereof containing a fluidized bed of finely divided regenerated catalyst particles. Thereby receiving a second riser reactor that produces an exhaust comprising spent catalyst particles with hydrocarbonaceous deposits and a cracked product, and (c) receiving the emissions from the first and second riser reactors to consume the cracked product. Separation zone to separate from. (d) stripping zones for receiving spent catalyst particles from the separation zone to separate the evaporative hydrocarbon material from the spent catalyst in the presence of stripping gas, (e) consumed catalyst particles from the strip zone. To burn almost all of the hydrogen associated with the hydrocarbonaceous deposits on the catalyst particles at temperatures ranging from about 1100 ° F. to about 1300 ° F. in the presence of an effective amount of carbonaceous gas and a pressure ranging from 15 to 40 psig. A first fluidized catalyst regeneration zone having a first catalyst regeneration zone having from 2 to about 8 volume percent carbon monoxide and an inlet containing an oxygen-containing gas for combustion, (f) a portion from the first catalyst regeneration zone In the presence of an effective amount of oxygen containing gas and a temperature in the range of 1300 ° F. to 1800 ° F. Burn almost all hydrocarbonaceous deposits on the catalyst, produce a fully regenerated catalyst having a carbon content of less than about 0.003 weight percent and a second catalytic regeneration zone exhaust gas having less than 1200 parts carbon monoxide per million, First and second riser reactors for contacting the hydrocarbon feed, an outlet for passing the fully regenerated catalyst to (a) and (b), respectively, and an inlet for accommodating the oxygen-containing gas needed for fluidization and combustion The apparatus comprises a second fluidized catalyst regeneration zone and (g) a fractionation distillation zone for receiving the cracked product from the separation zone (c) and the vaporizable hydrocarbon material from step (d) to recover product fractions. . ※ Note: The disclosure is based on the initial application.