Control of fluid catalytic cracking process for minimizing additive usage in the desulfurization of petroleum feedstocks

Patent metadata

Field	Value
Publication number	US-9764314-B2
Application number	US-78564710-A
Country	US
Kind code	B2
Filing date	May 24, 2010
Priority date	Nov 7, 2006
Publication date	Sep 19, 2017
Grant date	Sep 19, 2017

Abstract

A method and apparatus for the cracking of a petroleum oil feedstock to produce a desulfurized full-range gasoline product. The petroleum oil feedstock is contacted with a base cracking catalyst and an FCC additive in an FCC unit, wherein the catalyst includes a stable Y-type zeolite and a rare-earth metal oxide and the additive includes a shape selective zeolite. The catalyst, additive and petroleum oil feedstock can be contacted in a down-flow or riser fluid catalytic cracking unit, that can also include a regeneration zone, a separation zone, and a stripping zone. The FCC unit includes an integrated control and monitoring system that monitors at least one parameter selected from FCC operating parameters, feed rate, feedstock properties, and product stream properties, and adjusts at least one parameter in response to the measured parameter to increase production of desulfurized products.

First claim

That which is claimed is:

1. A method for the fluid catalytic cracking of petroleum oil feedstock to produce a full-range low-sulfur gasoline product stream, the method comprising the steps of:
feeding petroleum oil feedstock to a reaction zone of a fluid catalytic cracking unit;
feeding a base cracking catalyst to the reaction zone of the fluid catalytic cracking unit, the base cracking catalyst comprising a stable Y-type zeolite and less than 0.6% by weight of rare-earth metal oxide;
feeding a fluid catalytic cracking additive to the reaction zone of the fluid catalytic cracking unit, the fluid catalytic cracking additive comprising a shape-selective zeolite, wherein an average pore size of the shape-selective zeolite is smaller than an average pore size of the base cracking catalyst;
wherein the base cracking catalyst and the fluid catalytic cracking additive are present in an amount of between 55 to 95% by weight of the base cracking catalyst and between 5 and 45% by weight of the fluid catalytic cracking additive; and
wherein the base cracking catalyst and the fluid catalytic cracking additive are each added separately to the reaction zone of the fluid catalytic cracking unit;
contacting the petroleum oil feedstock, the base cracking catalyst, and the fluid catalytic cracking additive in the reaction zone of the fluid catalytic cracking unit for a reaction zone contact time of between 0.05 and 3 seconds to obtain a mixed hydrocarbon stream, said mixed hydrocarbon stream comprising a desulfurized hydrocarbon product stream, unreacted petroleum oil feedstock, and spent catalyst, wherein the reaction zone is maintained at a temperature of between 500° C. and 630° C.;
separating and collecting the desulfurized hydrocarbon product stream from the spent catalyst and the unreacted petroleum oil feedstock in a stripping zone;
withdrawing a stream comprising the desulfurized hydrocarbon product and the unreacted petroleum oil feedstock from the stripping zone;
separating the desulfurized hydrocarbon product stream to produce the full-range low-sulfur gasoline product stream;
recycling at least a portion of the desulfurized hydrocarbon product from the stream withdrawn from the stripping zone, through a first separation zone before sending the recycled portion of the desulfurized hydrocarbon product to the reaction zone; and
controlling feed rates of the petroleum oil feedstock, the base cracking catalyst, and the fluid catalytic cracking additive to the reaction zone with a process control, using a distributed control system, wherein the step of controlling the feed rates comprises the steps of:
continuously monitoring and collecting data corresponding to a composition of the petroleum oil feedstock, a composition of the full-range low-sulfur gasoline product stream, the feed rates of the base cracking catalyst and the fluid catalytic cracking additive, and operating conditions of the fluid catalytic cracking unit, measured directly from sensors of the fluid catalytic cracking unit;
providing the data corresponding to the petroleum oil feedstock, the full-range low-sulfur gasoline product stream, the feed rates of the base cracking catalyst and the fluid catalytic cracking additive, and the operating conditions of the fluid catalytic cracking unit to the distributed control system and comparing the results against historical data; and
adjusting the feed rate of the fluid catalytic cracking additive using the distributed control system, to optimize desulfurization of the petroleum oil feedstock,

wherein the distributed control system comprises a network of controllers configured to process the data measured directly from the sensors of the fluid catalytic cracking unit, to predict how adjustment of one or more of the data affects the optimization of the desulfurization of the petroleum oil feedstock, and to adjust the feed rate of the fluid catalytic cracking additive based on the predicted adjustment of the one or more of the data affecting the optimization of the desulfurization of the petroleum oil feedstock.

2. The method of claim 1 further comprising the steps of:
determining a sulfur content in the full-range low-sulfur gasoline product stream;
adjusting at least one parameter selected from a rate of feed of the petroleum oil feedstock to the reaction zone of the fluid catalytic cracking unit, the fluid catalytic cracking unit reaction zone temperature, or the reaction zone contact time between the petroleum oil feedstock, the base cracking catalyst, and the fluid catalytic cracking additive to achieve an adjusted operating condition; and
determining the sulfur content of the full-range low-sulfur gasoline product stream when the fluid catalytic cracking unit is operating under the adjusted operating condition.

3. The method of claim 1 further comprising:
determining an initial real-time sulfur content in the full-range low-sulfur gasoline product stream;
calculating a simulated sulfur content in the full-range low-sulfur gasoline product stream based upon an adjustment of at least one operating parameter, wherein the at least one operating parameter is selected from a feed rate of the petroleum oil feedstock to the reaction zone of the fluid catalytic cracking unit, a feed rate of the base cracking catalyst to the reaction zone, a feed rate of the fluid catalytic cracking additive to the reaction zone, the temperature of the reaction zone of the fluid catalytic cracker unit, or the contact time between the petroleum oil feedstock, the base cracking catalyst, and the fluid catalytic cracking additive;
repeating the step of calculating a simulated sulfur content until a maximum simulated desulfurization is achieved;
comparing the maximum simulated desulfurization with the an initial sulfur content in the full-range low-sulfur gasoline product stream; and
if the sulfur content in the maximum simulated desulfurization is less than the initial sulfur content in the full-range low-sulfur gasoline product stream, then adjusting at least one operating parameter to reduce sulfur content of the full-range low-sulfur gasoline product stream.

4. The method of claim 1 wherein the fluid catalytic cracking unit is a down-flow or riser type fluid catalytic cracking reactor.

5. The method of claim 1 wherein the fluid catalytic cracking unit comprises a regeneration zone, a second separation zone, and the stripping zone.

6. The method of claim 5 wherein the fluid catalytic cracking unit further comprises the first separation zone coupled to the second separation zone.

7. The method of claim 1 further comprising recycling at least a portion of unreacted oil feedstock to the reaction zone.

8. The method of claim 1 wherein the reaction zone contact time of the base cracking catalyst, the fluid catalytic cracking additive, and the petroleum oil feedstock is between 0.1 and 1.5 seconds.

9. The method of claim 1 wherein the reaction zone contact time of the base cracking catalyst, the fluid catalytic cracking additive, and the petroleum oil feedstock is between 0.2 and 0.9 seconds.

10. The method of claim 1 wherein a ratio of the base cracking catalyst and the fluid catalytic cracking additive to the petroleum oil feedstock in the fluid catalytic cracking unit is between 10 to 50 wt/wt.

11. The method of claim 1 wherein the fluid catalytic cracking additive comprises ZSM-5.

12. The method of claim 1 wherein the petroleum oil feedstock is selected from the group consisting of an oil selected from the group consisting of naphtha, crude oil, deasphalted oil, vacuum gas oil, gas oil, petroleum residue, hydrotreated petroleum oil products, and mixtures thereof.

Assignees

• Al-Alloush Saeed Saad
• Taha Othman A
• Khan M Rashid
• Saudi Arabian Oil Co

Inventors

• Al-Alloush Saeed Saad
• Taha Othman A
• Khan M Rashid

Classifications

• G05D21/02

  characterised by the use of electric means · CPC title

• C10G2300/4093

  Catalyst stripping · CPC title

• C10G2300/1059

  Gasoil having a boiling range of about 330 - 427 °C · CPC title

• B01J29/084

  Y-type faujasite · CPC title

• B01J29/088

  Y-type faujasite · CPC title