Recovery and re-use of waste energy in industrial facilities

Patent metadata

Field	Value
Publication number	US-9851153-B2
Application number	US-201615241998-A
Country	US
Kind code	B2
Filing date	Aug 19, 2016
Priority date	Aug 24, 2015
Publication date	Dec 26, 2017
Grant date	Dec 26, 2017

Abstract

Configurations and related processing schemes of direct or indirect inter-plants (or both) heating systems synthesized for grassroots medium grade crude oil semi-conversion refineries to increase energy efficiency from specific portions of low grade waste heat sources are described. Configurations and related processing schemes of direct or indirect inter-plants (or both) heating systems synthesized for integrated medium grade crude oil semi-conversion refineries and aromatics complex for increasing energy efficiency from specific portions of low grade waste sources are also described.

First claim

The invention claimed is:

1. A method implemented in a crude oil refining facility, the method comprising:
in a crude oil refining facility comprising a plurality of oil refining plants, each oil refining plant configured to perform at least one oil refining process, each oil refining plant comprising a plurality of interconnected oil refining sub-systems, wherein a plurality of streams at respective temperatures flow between the plurality of oil refining sub-systems:
flowing a hydrocracking plant stream from a hydrocracking plant of the plurality of oil refining plants to a first heat exchanger, the hydrocracking plant stream comprising at least one of a first stage reaction section feed to a first stage cold high pressure separator stream, a diesel product stream, a kerosene product stream, a second reaction stage feed stream to a second cold high pressure separator stream, a product stripper overheads stream, a kerosene pumparound stream;
flowing a stream from a first oil refining plant of the plurality of oil refining plants to the first heat exchanger, the first oil refining plant being different from the hydrocracking plant and comprising at least one of a sulfur recovery plant, a sour water stripper plant, a gas separation plant through which a gas separation plant stream comprising at least one of C2 to C4 flows, a naphtha hydro-treating plant, an amine regeneration plant separation section, wherein an acid gas regenerator bottoms stream comprising a weak amine salt flows through the amine regeneration plant, wherein the first heat exchanger transfers heat from the hydrocracking plant stream to the stream from the first oil refining plant; and
utilizing the stream from the first oil refining plant heated by the hydrocracking plant stream in an oil refining process at the first oil refining plant.

2. The method of claim 1 , wherein the first oil refining plant is the sulfur recovery plant, the stream is an amine regenerator bottoms stream, the hydrocracking plant stream is the first stage reaction section feed to the first stage cold high pressure separator stream, and wherein utilizing the stream from the first oil refining plant heated by the hydrocracking plant stream in an oil refining process at the first oil refining plant further comprises:
heating the amine regenerator bottoms stream using the first stage reaction section feed to a first stage cold high pressure separator stream; and
flowing the heated amine regenerator bottoms stream through a sulfur recovery plant amine regenerator bottoms of the sulfur recovery plant.

3. The method of claim 1 , wherein the first oil refining plant is the sour water stripper plant, the stream is a sour water stripper bottoms stream, wherein the hydrocracking plant stream comprises the diesel product stream, the first stage reaction section feed to the first stage cold high pressure separator stream and the kerosene product stream, and wherein utilizing the stream from the first oil refining plant heated by the hydrocracking plant stream in an oil refining process at the first oil refining plant comprises:
heating the sour water stripper bottoms stream using the diesel product stream in the first heat exchanger;
heating the sour water stripper bottoms stream using the first stage reaction section feed to the first stage cold high pressure separator stream in a second heat exchanger;
heating the sour water stripper bottoms using the kerosene product stream in a third heat exchanger; and
flowing the heated sour water stripper bottoms stream through the sour water stripper plant.

4. The method of claim 3 , wherein the first heat exchanger, the second heat exchanger and the third heat exchanger are fluidically coupled to each other in parallel.

5. The method of claim 1 , wherein the first oil refining plant comprises the gas separation plant and the sulfur recovery plant, wherein the stream comprises a C3/C4 splitter bottoms stream in the gas separation plant, a sulfur recovery plant bottom cold stream in the sulfur recovery plant and a de-ethanizer bottoms stream in the gas separation plant, wherein the hydrocracking plant stream is the second reaction stage feed stream to the second cold high pressure separator stream, the first stage reaction feed stream to the first stage cold high pressure separator stream and the kerosene product stream, and wherein utilizing the stream from the first oil refining plant heated by the hydrocracking plant stream in an oil refining process at the first oil refining plant comprises:
heating the C3/C4 splitter bottoms stream in the gas separation plant using the second reaction stage feed stream to the second cold high pressure separator stream in the first heat exchanger;
heating the sulfur recovery plant bottom cold stream in the sulfur recovery plant using the first stage reaction feed stream to the first stage cold high pressure separator stream in a second heat exchanger;
heating the de-ethanizer bottoms stream in the gas separation plant using the kerosene product stream in a third heat exchanger;
flowing the heated sulfur recovery plant bottom cold stream to the sulfur recovery plant;
flowing the heated de-ethanizer bottoms stream to the gas separation plant; and
flowing the heated C3/C4 splitter bottoms stream to the gas separation plant.

6. The method of claim 1 , wherein the first oil refining plant comprises the naphtha hydro-treating plant and the sulfur recovery plant, wherein the stream comprises a naphtha splitter bottoms stream in the naphtha hydro-treating plant and an amine regenerator bottoms stream in the sulfur recovery plant, wherein the hydrocracking plant stream the diesel product stream, the product stripper overheads stream, the kerosene pumparound stream, the kerosene product stream, and the first reaction stage feed stream to a first stage cold high pressure separator, and wherein utilizing the stream from the first oil refining plant heated by the hydrocracking plant stream in an oil refining process at the first oil refining plant comprises:
heating a naphtha splitter bottoms stream in the naphtha hydro-treating plant using the diesel product stream, the product stripper overheads stream, the kerosene pumparound stream and the kerosene product stream in a first heat exchanger, a second heat exchanger, a third heat exchanger and a fourth heat exchanger, respectively;
heating the amine regenerator bottoms stream in the sulfur recovery plant using the first reaction stage feed stream to the first stage cold high pressure separator in a fifth heat exchanger;
flowing the heated naphtha splitter bottoms stream to the naphtha hydro-treating plant; and
flowing the heated amine regenerator bottoms stream to the sulfur recovery plant.

7. The method of claim 6 , wherein the first heat exchanger, the second heat exchanger, the third heat exchanger and the fourth heat exchanger are fluidically coupled to each other in parallel.

8. The method of claim 1 , wherein the first oil refining plant comprises the sour water stripper plant and the gas separation plant, wherein the stream comprises a sour water stripper bottom cold stream, a C3/C4 splitter bottoms stream and a de-ethanizer bottoms stream in the gas separation plant, wherein the hydrocracking plant stream comprises the second reaction section second stage cold high pressure separator feed stream, the first reaction stage feed stream to the first stage cold high pressure separator, the product stripper overhead stream and the kerosene product stream, and wherein utilizing the stream from the first oil refining plant heated by the hydrocracking plant stream in an oil refining process at the first oil refining plant comprises:
heating the C3/C4 splitter bottoms stream in the gas separation plant

Assignees

• Saudi Arabian Oil Co

Inventors

• Noureldin Mahmoud Bahy Mahmoud
• Al Saed Hani Mohammed

Classifications

• C01B2203/0227

  containing a catalytic reforming step · CPC title

• C01B2203/0283

  containing a CO-shift step, i.e. a water gas shift step · CPC title

• C01B2203/127

  Catalytic desulfurisation · CPC title

• C01B2203/043

  Regenerative adsorption process in two or more beds, one for adsorption, the other for regeneration · CPC title

• C01B3/34 Primary

  by reaction of hydrocarbons with gasifying agents · CPC title