Process of maximizing production of chemical raw materials by gaseous phase catalytic cracking crude oil with multi-stages in milliseconds in combination with hydrogenation

Patent metadata

Field	Value
Publication number	US-10508247-B2
Application number	US-201916386872-A
Country	US
Kind code	B2
Filing date	Apr 17, 2019
Priority date	Apr 17, 2018
Publication date	Dec 17, 2019
Grant date	Dec 17, 2019

Abstract

The invention provides a process of maximizing production of chemical raw materials by gaseous phase catalytic cracking crude oil with multi-stages in milliseconds in combination with hydrogenation, comprising: a high-efficiency atomizing nozzle sprays the preheated crude oil into an upper portion of the downflow modification reaction tube, the produced oil mist is mixed with a high temperature heat carrier flowing downward from a first return controller for pyrolysis in milliseconds and then the pyrolysis products are subject to a gas-solid separation; the coked heat carrier obtained by the separation enters into a modification regeneration reactor to conduct a regeneration reaction, the obtained high temperature heat carrier returns to a top of the downflow reaction tube to participate in circulation, the regeneration gas is subject to heat exchange and then output; the high temperature oil and gas produced by the pyrolysis reaction directly flow into the millisecond cracking reactor and conduct a cracking reaction with the regenerated cracking catalyst and subject to a gas-solid separation; then the cracking catalyst to be regenerated enters the crack regeneration reactor and performs a regeneration reaction and then are subject to a gas-solid separation, the obtained high temperature crack catalyst passes through a second return controller and flows into the millisecond cracking reactor to participate the circulation reaction, the obtained flue gas is subject to heat exchange and then output; the cracked oil and gas produced by the cracking reaction enter into a fractionation tower for separation, thereby obtain the cracked gas, gasoline fraction, diesel fraction, recycle oil and oil slurry; furthermore, the diesel fraction, recycle oil and oil slurry are subject to saturation or open-ring in a hydrogenation reactor, return and mix with crude oil such that the mixture is used as a raw material.

First claim

The invention claimed is:

1. A process of maximizing production of chemical raw materials by gaseous phase catalytic cracking crude oil with multi-stages in milliseconds in combination with hydrogenation, the process comprising:
1) spraying crude oil, or a crude oil mix, preheated to 150° C.-350° C. with an atomizing nozzle, producing an oil mist, from a feed inlet of a downflow modification reaction tube into an upper portion of the downflow modification reaction tube, mixing the oil mist with a solid heat carrier at a temperature ranging from 650° C.-1,200° C. flowing downward from a first return controller for milliseconds, so as to heat, vaporize and pyrolyze the oil mist and obtain an oil and gas, and a solid heat carrier to be regenerated, wherein the pyrolysis reaction temperature is within a range of 480° C.−850° C. and the downflow modification reaction tube comprises a top and a bottom;
2) carrying out a gas-solid separation by allowing the oil and gas as well as the solid heat carrier to be regenerated to flow rapidly and downward to a first gas-solid separator at the bottom of the downflow modification reaction tube to carry out the gas-solid separation to obtain a coked solid heat carrier to be regenerated and a separated oil and gas;
3-1) allowing the coked solid heat carrier to be regenerated to flow through a first flow controller and enter into a lower portion of a modification regeneration reactor to conduct a regeneration reaction with a regeneration agent and produce a regeneration gas and a regenerated solid heat carrier, the temperature of the regeneration reaction within a range of 680° C.-1,250° C.; then subjecting the regeneration gas and the separated solid heat carrier to a gas-solid separation in a second gas-solid separator on top of the modification regeneration reactor to produce a regenerated solid heat carrier with a carrier/oil ratio of 1-14, then recirculating the regenerated solid heat carrier with a carrier/oil ratio of 1-14 through the first return controller, into the top of the downflow modification reaction tube, and into the downflow modification reaction tube so as to participate in the heating, vaporizing, and pyrolyzing of the oil mist; and subjecting the regeneration gas, after the second gas-solid separator on top of the modification regeneration reactor, to heat exchange and then output;
3-2) allowing the separated oil and gas, which is not condensed, from the first gas-solid separator to directly flow in the gaseous phase into a millisecond cracking reactor, and mix with a regeneration cracking catalyst having a temperature of 600° C.-850° C. to carry out a gaseous phase catalytic cracking reaction producing a cracking oil and gas and a cracking catalyst to be regenerated, the temperature of the gaseous phase catalytic cracking reaction is within a range of 530° C.−750° C., then subjecting the cracking oil and gas and a cracking catalyst to be regenerated to gas-solid separation in milliseconds;
4-1) allowing the cracking catalyst to be regenerated to flow through a second flow controller and enter a lower portion of a crack regeneration reactor for performing a regeneration reaction with air to produce a regenerated crack catalyst, the temperature of the regeneration reaction is 630° C.-900° C., subjecting a flue gas and the regenerated crack catalyst to a gas-solid separation in a third gas-solid separator at the top of the crack regeneration reactor to produce a crack catalyst with a catalyst/oil ratio of 1-8; passing the crack catalyst with a catalyst/oil ratio of 1-8 through a second return controller and into the millisecond cracking reactor to participate in the gaseous phase catalytic cracking reaction, and subjecting the flue gas to heat exchange and then output;
4-2) passing the cracking oil and gas into a catalytic fractionation tower and separating the cracking oil and gas in the catalytic fractionation tower into different fraction products, which are cracked gas, gasoline fraction, diesel fraction, recycle oil and oil slurry;
5-1) separating the cracked gas to obtain low-carbon olefins,
5-2) extracting and separating the gasoline fraction to obtain low-carbon aromatic hydrocarbons and a gasoline fraction raffinate oil;
5-3) mixing the diesel fraction with the recycle oil and the oil slurry to carry out catalytic saturation or open-ring reaction with a hydrogenation catalyst to obtain a hydrogenated modified oil, mixing the hydrogenated modified oil with the gasoline fraction raffinate oil to obtain a mixture, and returning the mixture to mix with the crude oil to form the crude oil mix, which enters the upper portion of the downflow modification reaction tube for mixing with at least one of the solid heat carrier or the regenerated solid heat carrier with a carrier/oil ratio of 1-14.

2. The process of maximizing production of chemical raw materials by gaseous phase catalytic cracking crude oil with multi-stages in milliseconds in combination with hydrogenation according to claim 1 , wherein the crude oil is one of heavy oil, coal tar, shale oil and oil sand bitumen.

3. The process of maximizing production of chemical raw materials by gaseous phase catalytic cracking crude oil with multi-stages in milliseconds in combination with hydrogenation according to claim 1 , wherein the regeneration agent is an oxidizing agent or a mixture of an oxidizing agent and water vapor, wherein the oxidizing agent is one of oxygen, air and oxygen-enriched air; and the regeneration gas is syngas or flue gas.

4. The process of maximizing production of chemical raw materials by gaseous phase catalytic cracking crude oil with multi-stages in milliseconds in combination with hydrogenation according to claim 1 , wherein the solid heat carrier is at least one of semi-coke microspheres, calcium aluminate porous microspheres, magnesium aluminate spinel porous microspheres, aluminum silicate porous microspheres, calcium silicate porous microspheres, magnesium silicate porous microspheres, porous microsphere carriers loaded with alkali metals and alkaline-earths metal.

5. The process of maximizing production of chemical raw materials by gaseous phase catalytic cracking crude oil with multi-stages in milliseconds in combination with hydrogenation according to claim 1 , wherein the second gas-solid separator and the third gas-solid separator are independently selected from the group consisting of an inertial separator, a horizontal cyclone separator and a vertical cyclone.

6. The process of maximizing production of chemical raw materials by gaseous phase catalytic cracking crude oil with multi-stages in milliseconds in combination with hydrogenation according to claim 1 , wherein the cracking catalyst is at least one selected from a group consisting of a FCC molecular sieve catalyst, a shape selective molecular sieve catalyst and an alkaline solid porous catalyst.

7. The process of maximizing production of chemical raw materials by gaseous phase catalytic cracking crude oil with multi-stages in milliseconds in combination with hydrogenation according to claim 1 , wherein the modification regeneration reactor is one selected from a group consisting of a riser regenerator, a turbulent fluidized bed regenerator and a bubbling fluidized bed regenerator.

8. The process of maximizing production of chemical raw materials by gaseous phase catalytic cracking crude oil with multi-stages in milliseconds in combination with hydrogenation according to claim 1 , wherein the millisecond cracking reactor is one selected from a group consisting of a downflow tube reactor, a horizontal inertia rotary separation reactor and a cross-staggered short contact reactor.

9. The process of maximizing production of chemical raw materials by gaseous

Assignees

• Univ China Petroleum East China

Inventors

• Tian Yuanyu
• Qiao Yingyun
• Zhang Juntao
• Zhang Jinhong
• Jiang Yuan
• Li Jie

Classifications

• C10G2400/06

  Gasoil · CPC title

• C10G2300/302

  Viscosity · CPC title

• C10G2400/20

  C2-C4 olefins · CPC title

• C10G67/02 Primary

  plural serial stages only · CPC title

• C10G2400/04

  Diesel oil · CPC title