Hydrocracking process with interstage steam stripping

Patent metadata

Field	Value
Publication number	US-9803148-B2
Application number	US-201213559846-A
Country	US
Kind code	B2
Filing date	Jul 27, 2012
Priority date	Jul 29, 2011
Publication date	Oct 31, 2017
Grant date	Oct 31, 2017

Abstract

In a hydrocracking process, the product from the first stage reactor passes through a steam stripper to remove hydrogen, H 2 S, NH 3 , light gases (C 1 -C 4 ), naphtha and diesel products. The stripper bottoms are separated from hydrogen, H 2 S, NH 3 , light gases (C 1 -C 4 ), naphtha, and diesel products and treated in a second stage reactor. The effluent stream from the second stage reactor, along with the stream of separated hydrogen, H 2 S, NH 3 , light gases (C 1 -C 4 ), naphtha, and diesel products, are passed to a separation stage for separating petroleum fractions. Preferably, the effluent stream from the first stage reactor is passed through a steam generator prior to the steam stripping step. In an alternate embodiment, the effluent stream from the first stage reactor is passed through a vapor/liquid separator stripper vessel prior to the steam stripping step.

First claim

The invention claimed is:

1. A process for hydrocracking a hydrocarbon feedstock comprising the steps of:
supplying the feedstock and hydrogen to an input of a first stage reactor containing a first stage hydrocracking catalyst for removal of heteroatoms and cracking of high molecular weight molecules into lower molecular weight hydrocarbons to produce a first-stage reactor effluent; thereafter
passing the first stage effluent to a steam stripper vessel to separate hydrogen, H 2 S, NH 3 , light gases (C 1 -C 4 ), naphtha, and diesel products;
passing the stripper bottoms from the stripper vessel, and hydrogen, to a second stage reactor containing a second stage hydrocracking catalyst;
combining a hydrocracked effluent stream of the second stage reactor with the hydrogen, H 2 S, NH 3 , light gases (C 1 -C 4 ), naphtha, and diesel products separated in the steam stripper vessel to form a combined product stream; and passing the combined product stream to a separation stage for separation of the components into predetermined product streams.

2. The process of claim 1 , wherein the effluent stream from the first stage reactor is passed through a heat exchange steam generator prior to being passed to the steam stripper vessel.

3. The process of claim 1 , wherein the effluent stream from the first stage reactor is passed through vapor/liquid separator stripper vessel to produce tops and bottoms, the bottoms being passed to the steam stripper vessel.

4. The process of claim 1 , wherein the first stage hydrocracking catalyst is selected from the group consisting of amorphous alumina catalysts, amorphous silica alumina catalysts, zeolite-based catalysts, and a combination comprising at least one of amorphous alumina catalysts, amorphous silica alumina catalysts, and zeolite-based catalyst.

5. The process of claim 1 , wherein the first stage hydrocracking catalyst further comprises an active phase of Ni, W, Mo, Co, or a combination comprising at least one of Ni, W, Mo, and Co.

6. The process of claim 1 , wherein 10% to 80% by volume of hydrocarbons boiling above 370° C. at a hydrogen partial pressure in the range of 100200 kg/cm 2 are converted in the first reactor to one or more light gases selected from the group consisting of methane, ethane, propane, n-butane, isobutene, hydrogen sulfide, ammonia, naphtha fractions boiling in the range of 180° C. to 375° C., diesel fractions boiling in the range of 180° C. to 375° C., and combinations comprising at least one of the foregoing light gases.

7. The process of claim 1 , wherein the first reactor is at a hydrogen partial pressure is in the range of 100-150 kg/cm 2 .

8. The process of claim 1 , wherein the flow of feedstock oil to the first reactor is in the range of 300-2000 m 3 over 1000 m 3 of hydrotreating catalyst per hour.

9. The process of claim 1 , wherein the first or second reactor is a fixed-bed, an ebullated-bed, a slurry-bed, or a combination thereof.

10. The process of claim 1 , wherein a portion of the effluent stream of hydrogen, H 2 S, NH 3 , light gases (C 1 -C 4 ), naphtha, and diesel products removed from the steam stripper vessel are directed through a separator vessel to separate water, gas, and liquids; a sour diesel stream is also supplied to the separator vessel to mix with the effluent stream; and wherein the combined effluent stream/sour diesel stream is directed through a diesel hydrotreater unit to produce ultra-low sulfur diesel fuel.

Assignees

• Koseoglu Omer Refa
• Al-Abdul'Al Ali H
• Ushio Masaru
• Nakano Koji
• Saudi Arabian Oil Co
• Japan Coop Center Petroleum
• Jgc Catalysts & Chemicals Ltd

Inventors

• Koseoglu Omer Refa
• Al-Abdul'Al Ali H
• Ushio Masaru
• Nakano Koji

Classifications

• C10G65/12

  including cracking steps and other hydrotreatment steps · CPC title

• C10G2300/301

  Boiling range · CPC title

• C10G2400/02

  Gasoline · CPC title

• C10G2400/04

  Diesel oil · CPC title

• C10G67/02 Primary

  plural serial stages only · CPC title