Recovery and re-use of waste energy in industrial facilities

Patent metadata

Field	Value
Publication number	US-10119764-B2
Application number	US-201615241989-A
Country	US
Kind code	B2
Filing date	Aug 19, 2016
Priority date	Aug 24, 2015
Publication date	Nov 6, 2018
Grant date	Nov 6, 2018

Abstract

Configurations and related processing schemes of direct or indirect (or both) inter-plants 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 (or both) inter-plants 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, a low temperature shift (LTS) converter product stream and a diesel hydro-treating plant stream of a hydrocracking plant, a steam reforming hydrogen plant and a diesel hydro-treating plant, respectively, of the plurality of oil refining plants to one or more heat exchangers, the hydrocracking plant stream comprising at least one of a feed stream to a first reaction stage cold high pressure separator, a feed stream to a second reaction stage cold high pressure separator, a product stripper overhead stream, a diesel product stream, a kerosene pumparound stream, and a kerosene product stream;
flowing a stream from a first oil refining plant of the plurality of oil refining plants to the one or more heat exchangers, the first oil refining plant being different from the hydrocracking plant, the steam reforming hydrogen plant and the diesel hydro-treating plant and comprising a naphtha hydro-treating plant, a sour water stripper plant, an amine regeneration plant separation section, a sulfur recovery plant and a gas separation plant through which a gas separation plant stream comprising at least one of C2 to C4 flows, wherein the one or more heat exchangers transfer heat from one or more of the hydrocracking plant stream, the low temperature shift (LTS) converter product stream and the diesel hydro-treating plant stream to the stream from the first oil refining plant; and
utilizing the stream from the first oil refining plant heated by one or more of the hydrocracking plant stream, the low temperature shift (LTS) converter product stream and the diesel hydro-treating plant stream in an oil refining process at the first oil refining plant.

2. The method claim 1 , wherein the one or more heat exchangers indirectly transfer heat from one or more of the hydrocracking plant stream, the low temperature shift (LTS) converter product stream and the diesel hydro-treating plant stream to the stream from the first oil refining plant.

3. The method of claim 2 , wherein the one or more heat exchangers indirectly transfer heat through a buffer fluid using one or more of the hydrocracking plant stream, the low temperature shift (LTS) converter product stream and the diesel hydro-treating plant stream.

4. The method of claim 3 , wherein the buffer fluid comprises at least one of oil or water.

5. The method of claim 3 , wherein the one or more heat exchangers indirectly transfer heat through the buffer fluid using one or more of the hydrocracking plant stream, the low temperature shift (LTS) converter product stream and the diesel hydro-treating plant stream by:
heating, in a first heat exchanger, a first buffer fluid stream using the hydrocracking plant diesel product stream in the hydrocracking plant;
heating, in a second heat exchanger, a second buffer fluid stream using the feed stream to the second reaction stage cold high pressure separator in the hydrocracking plant;
heating, in a third heat exchanger, a third buffer fluid stream using the feed stream to the first reaction stage cold high pressure separator in the hydrocracking plant;
heating, in a fourth heat exchanger, a fourth buffer fluid stream using the product stripper overhead stream in the hydrocracking plant;
heating, in a fifth heat exchanger, a fifth buffer fluid stream using the kerosene pumparound stream in the hydrocracking plant;
heating, in a sixth heat exchanger, a sixth buffer fluid stream using the kerosene product stream in the hydrocracking plant;
heating, in a seventh heat exchanger, a seventh buffer fluid stream using the low temperature shift converter product stream in the steam reforming hydrogen plant;
heating, in an eighth heat exchanger, an eight buffer fluid stream using a diesel stripper overhead stream in the diesel hydro-treating plant; and
heating, in a ninth heat exchanger, a ninth buffer fluid stream using a diesel stripper bottoms stream in the diesel hydro-treating plant.

6. The method of claim 5 , further comprising combining the heated first buffer fluid stream exiting the first heat exchanger, the heated second buffer fluid stream exiting the second heat exchanger, the heated third buffer fluid stream exiting the third heat exchanger, the heated fourth buffer fluid stream exiting the fourth heat exchanger, the heated fifth buffer fluid stream exiting the fifth heat exchanger, the heated sixth buffer fluid stream exiting the sixth heat exchanger, the heated seventh buffer fluid stream exiting the seventh heat exchanger, the heated eight buffer fluid stream exiting the eighth heat exchanger, and the heated ninth buffer fluid stream exiting the ninth heat exchanger resulting in a combined heated buffer fluid.

7. The method of claim 6 , further comprising:
flowing the combined heated buffer fluid to the naphtha hydro-treating plant;
heating, in a tenth heat exchanger, a naphtha splitter bottoms stream in the naphtha hydro-treating plant using the combined heated buffer fluid;
flowing the combined heated buffer fluid to a sour water stripper bottoms in the sour water stripper plant;
heating, in an 11 th heat exchanger, a sour water stripper bottoms stream in the sour water stripper plant using the combined heated buffer fluid;
flowing the combined heated buffer fluid to the sulfur recovery plant;
heating, in a 12 th heat exchanger, an amine regenerator bottoms stream in the sulfur recovery plant using the combined heated buffer fluid;
flowing the combined heated buffer fluid to the amine regeneration plant separation section;
heating, in a 13 th heat exchanger, an acid gas regenerator bottoms stream in the amine regeneration plant separation section using the combined heated buffer fluid;
flowing the combined heated buffer fluid to the gas separation plant;
heating, in a 14 th heat exchanger, a C3/C4 splitter bottoms stream in the gas separation plant using the combined heated buffer fluid; and
heating, in the 14 th heat exchanger, a de-ethanizer bottoms stream using the combined heated buffer fluid.

8. The method of claim 7 , wherein the first heat exchanger, the second heat exchanger, the third heat exchanger, the fourth heat exchanger, the fifth heat exchanger, the sixth heat exchanger, the seventh heat exchanger, the eighth heat exchanger and the ninth heat exchanger are fluidically coupled to each other in parallel.

9. The method of claim 8 , wherein the tenth heat exchanger is fluidically coupled in series with a combination of the first heat exchanger, the second heat exchanger, the third heat exchanger, the fourth heat exchanger, the fifth heat exchanger, the sixth heat exchanger, the seventh heat exchanger, the eighth heat exchanger and the ninth heat exchanger.

10. The method of claim 9 , wherein the tenth heat exchanger, 11 th heat exchanger, the 12 th heat exchanger, the 13 th heat exchanger, the 14 th heat exchanger and the 15 th heat exchanger are fluidically coupled to each other in series.

11. The method of claim 9 , wherein the combined heated buffer fluid from the naphtha hydro-treating plant is flowed to the sour water stripper plant, then to the sulfur recovery plant, then to the amine regeneration plant separation section, and then to the gas separation plant.

Assignees

• Saudi Arabian Oil Co

Inventors

• Mahmoud Noureldin Mahmoud Bahy
• Al Saed Hani Mohammed

Classifications

• C01B3/34 Primary

  by reaction of hydrocarbons with gasifying agents · CPC title

• C01B2203/043

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

• C01B2203/0283

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

• C01B2203/0227

  containing a catalytic reforming step · CPC title

• C01B2203/127

  Catalytic desulfurisation · CPC title