# US 10,480,864 B2 · Recovery and re-use of waste energy in industrial facilities

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- Number: US 10,480,864 B2
- Document ID: US10480864B2
- Status: Granted
- Kind: B2
- Application number: 15/833,088
- Filed: 2017-12-06
- Published: 2018-04-05
- Granted: 2019-11-19
- Earliest claimed: 2015-08-24
- Assignees: Saudi Arabian Oil Company
- Applicants: Saudi Arabian Oil Company
- Inventors: Mahmoud Bahy Mahmoud Noureldin; Hani Mohammed Al Saed
- Web page: https://patentgrep.com/patent/US10480864B2

## CPC

- F28D 7/0083: {with units having particular arrangement relative to a supplementary heat exchange medium, e.g. with interleaved units or with adjacent units arranged in common flow of supplementary heat exchange medium}
- B01D 3/007: {Energy recuperation; Heat pumps}
- B01D 3/32: Other features of fractionating columns {; Constructional details of fractionating columns not provided for in groups B01D3/16 - B01D3/30}
- B01D 51/10: Conditioning the gas to be cleaned
- B01D 53/047: Pressure swing adsorption
- B01D 53/1462: {Removing mixtures of hydrogen sulfide and carbon dioxide}
- B01D 53/185: {Liquid distributors}
- B01D 53/343: {Heat recovery}
- B01D 53/48: Sulfur compounds
- B01D 53/8603: {Removing sulfur compounds}
- B01D 53/96: Regeneration, reactivation or recycling of reactants
- C01B 3/24: of hydrocarbons
- C01B 3/34: by reaction of hydrocarbons with gasifying agents
- C02F 1/586: {by removing ammoniacal nitrogen (for biological methods C02F3/00)}
- C07C 7/08: by extractive distillation
- C10G 33/06: with mechanical means, e.g. by filtration
- C10G 35/04: Catalytic reforming
- C10G 45/00: Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds
- C10G 45/02: to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbons; Hydrofinishing
- C10G 45/44: Hydrogenation of the aromatic hydrocarbons
- C10G 47/00: Cracking of hydrocarbon oils, in the presence of hydrogen or hydrogen- generating compounds, to obtain lower boiling fractions (C10G15/00 takes precedence; destructive hydrogenation of non-melting solid carbonaceous or similar materials C10G1/06)
- C10G 65/00: Treatment of hydrocarbon oils by two or more hydrotreatment processes only
- C10G 65/12: including cracking steps and other hydrotreatment steps
- C10G 69/00: Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process (C10G67/00 takes precedence)
- C10K 3/04: reducing the carbon monoxide content {, e.g. water-gas shift [WGS]}
- C10L 3/101: {Removal of contaminants}
- C10L 3/103: {Sulfur containing contaminants}
- C10L 3/104: {Carbon dioxide}
- F01D 17/145: {by means of valves, e.g. for steam turbines (valves in general F16K)}
- F01K 3/185: {using waste heat from outside the plant (F02G5/00 takes precedence)}
- F01K 13/00: General layout or general methods of operation of complete plants
- F01K 13/02: Controlling, e.g. stopping or starting
- F01K 23/06: combustion heat from one cycle heating the fluid in another cycle
- F01K 23/064: {in combination with an industrial process, e.g. chemical, metallurgical}
- F01K 25/06: using mixtures of different fluids (plants using mixtures of steam and gas F01K21/04)
- F01K 25/08: using special vapours
- F01K 27/00: Plants for converting heat or fluid energy into mechanical energy, not otherwise provided for
- F01K 27/02: Plants modified to use their waste heat, other than that of exhaust, e.g. engine-friction heat
- F28F 9/26: Arrangements for connecting different sections of heat-exchange elements, e.g. of radiators (connecting different sections in water heaters F24H9/14 {, connecting headers with inlet or outlet fittings F28F9/0246})
- H02K 7/1823: {structurally associated with turbines or similar engines}
- B01D 2252/204: Amines
- C01B 2203/0227: containing a catalytic reforming step
- C01B 2203/0233: the reforming step being a steam reforming step
- C01B 2203/0283: containing a CO-shift step, i.e. a water gas shift step
- C01B 2203/043: Regenerative adsorption process in two or more beds, one for adsorption, the other for regeneration
- C01B 2203/127: Catalytic desulfurisation
- C02F 2101/10: Inorganic compounds
- C02F 2101/101: {Sulfur compounds}
- C02F 2101/16: Nitrogen compounds, e.g. ammonia
- C02F 2103/18: from the purification of gaseous effluents
- C02F 2103/36: from the manufacture of organic compounds
- C10G 2300/202: Heteroatoms content, i.e. S, N, O, P
- C10G 2300/207: Acid gases, e.g. H2S, COS, SO2, HCN
- C10G 2300/4006: Temperature
- C10G 2300/4056: Retrofitting operations
- C10G 2400/04: Diesel oil
- C10G 2400/30: Aromatics
- C10L 2290/06: Heat exchange, direct or indirect
- C10L 2290/541: Absorption of impurities during preparation or upgrading of a fuel
- Y02P 20/129: Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines
- Y02P 30/00: Technologies relating to oil refining and petrochemical industry
- F28D: HEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA DO NOT COME INTO DIRECT CONTACT (fluid heaters having heat generating means and heat transferring means F24H; furnaces F27; details of heat-exchange apparatus of general)
- B01D: SEPARATION (separating solids from solids by wet methods B03B, B03D; by pneumatic jigs or tables B03B; by other dry methods B07; magnetic or electrostatic separation of solid materials from solid materials or fluids, separation by high-voltage electric fields B03C; centrifuges, vortex apparatus B04; presses per se for squeezing-out liquid from liquid-containing material B30B9/02; treatment of water C02F, e.g. softening by ion-exchange C02F1/42; {arrangements of air intake cleaners in gas turbine plants F02C7/05} ; arrangements or mounting of filters in air-conditioning, air-humidification or ventilation F24F13/28)
- C01B: NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; {METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C}
- C02F: TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE (separation in general B01D; special arrangements on waterborne vessels of installations for treating water, waste water or sewage, e.g. for producing fresh water, B63J; adding materials to water to prevent corrosion C23F; treating radioactively-contaminated liquids G21F9/04; regeneration of reactants for recirculation into processes, see the relevant places for the processes)
- C07C: ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C10G: CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION (cracking to hydrogen or synthesis gas C01B; cracking or pyrolysis of hydrocarbon gases to individual hydrocarbons or mixtures thereof of definite or specified constitution C07C; cracking to cokes C10B); RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10K: PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
- C10L: FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G OR C10K; LIQUIFIED PETROLEUM GAS; USE OF ADDITIVES TO FUELS OR FIRES; FIRE-LIGHTERS
- F01D: NON-POSITIVE DISPLACEMENT MACHINES OR ENGINES, e.g. STEAM TURBINES (machines or engines for liquids F03; non-positive displacement pumps F04D)
- F01K: STEAM ENGINE PLANTS; STEAM ACCUMULATORS; ENGINE PLANTS NOT OTHERWISE PROVIDED FOR; ENGINES USING SPECIAL WORKING FLUIDS OR CYCLES (gas-turbine or jet-propulsion plants F02; nuclear power plants, engine arrangements therein G21D)
- F28F: DETAILS OF HEAT-EXCHANGE AND HEAT-TRANSFER APPARATUS, OF GENERAL APPLICATION (water and air traps, air venting F16)
- H02K: DYNAMO-ELECTRIC MACHINES (dynamo-electric relays H01H53/00; conversion of DC or AC input power into surge output power {H03K3/53})
- Y02P: CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS

## 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.

## Claims

### Claim 1

A system comprising:
a hydrocracking plant of a crude oil refining facility, the hydrocracking plant comprising feed furnaces, a first stage reaction section comprising a fixed-bed reactor vessel, a second reaction stage comprising another fixed-bed reactor vessel, and a fractionator column, wherein the hydrocracking plant is configured to perform at least one crude oil refining process and to flow a hydrocracking plant stream comprising at least one of a first stage reaction section feed stream to a first stage cold high pressure separator, a diesel product stream, a kerosene product stream, a second reaction stage feed stream to a second cold high pressure separator, a product stripper overheads stream, a kerosene pumparound stream;
an oil refining plant of the crude oil refining facility, the oil refining plant being different from the hydrocracking plant, the oil refining plant comprising at least one of a sulfur recovery plant comprising an amine regenerator distillation column, a sour water stripper plant comprising a sour-water stripper distillation column, a gas separation plant comprising a de-ethanizer distillation column and a propane-butane splitter distillation column and through which a gas separation plant stream comprising at least one of C2 to C4 flows in the gas separation plant, a naphtha hydro-treating plant comprising a naphtha splitter distillation column, an amine regeneration plant separation section comprising an acid gas absorber vessel and an acid gas regenerator vessel, wherein an acid gas regenerator bottoms stream comprising a weak amine salt flows through the amine regeneration plant;
a flow control system connected to the hydrocracking plant and the oil refining plant, the flow control system comprising one or more flow pumps, one or more flow pipes, and one or more valves, wherein the flow control system is configured to:
flow the hydrocracking plant stream from the hydrocracking plant to a heat exchanger, and
flow a stream from the oil refining plant to the heat exchanger; and
the heat exchanger configured to transfer a portion of heat flowed through the hydrocracking plant stream to the stream from the oil refining plant.

### Claim 2 (depends on 1)

The system of claim 1, wherein the oil refining plant is the sulfur recovery plant,
wherein the stream is an amine regenerator bottoms stream,
wherein the hydrocracking plant stream comprises the first stage reaction section feed stream to the first stage cold high pressure separator,
wherein the heat exchanger is configured to transfer the portion of the heat flowed through the first stage reaction section feed stream to the amine regenerator bottoms stream, and
wherein the flow control system is configured to flow the heated amine regenerator bottoms stream to an amine regenerator bottoms of the sulfur recovery plant.

### Claim 3 (depends on 1)

The system of claim 1, wherein the heat exchanger is a first heat exchanger,
wherein the oil refining plant comprises the sour water stripper plant,
wherein 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 stream to the first stage cold high pressure separator, and the kerosene product stream, and
wherein the first heat exchanger is configured to transfer the portion of the heat carried by the diesel product stream,
wherein the system comprises:
a second heat exchanger configured to transfer a portion of heat carried by the first stage reaction section feed stream to the sour water stripper bottoms stream; and
a third heat exchanger configured to transfer a portion of heat carried by the kerosene product stream to the sour water stripper bottoms stream, and
wherein the flow control system is configured to flow the heated sour water stripper bottoms stream through the sour water stripper plant.

### Claim 4 (depends on 3)

The system 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.

### Claim 5 (depends on 1)

The system of claim 1, wherein the heat exchanger is a first heat exchanger,
wherein the 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 section feed stream to the first stage cold high pressure separator stream, and the kerosene product stream,
wherein the first heat exchanger is configured to transfer the portion of the heat from the second reaction stage feed stream to the C3/C4 splitter bottoms stream in the gas separation plant,
wherein the system further comprises:
a second heat exchanger configured to transfer a portion of heat from the first stage reaction section feed stream to the sulfur recovery plant bottom cold stream in the sulfur recovery plant, and
a third heat exchanger configured to transfer a portion of heat carried by the kerosene product stream to the de-ethanizer bottoms stream in the gas separation plant, and
wherein the flow control system is configured to:
flow the heated sulfur recovery plant bottom cold stream to the sulfur recovery plant,
flow the heated de-ethanizer bottoms stream to the gas separation plant, and
flow the heated C3/C4 splitter bottoms stream to the gas separation plant.

### Claim 6 (depends on 1)

The system of claim 1, wherein the heat exchanger is a first heat exchanger,
wherein the 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 comprises the diesel product stream, the product stripper overheads stream, the kerosene pumparound stream, the kerosene product stream, and
the first stage reaction section feed stream to the first stage cold high pressure separator, and
wherein the first heat exchanger is configured to transfer the portion of the heat from the diesel product stream to the naphtha splitter bottoms stream in the naphtha hydro-treating plant, and
wherein the system further comprises:
a second heat exchanger configured to transfer a portion of heat from the product stripper overheads stream to the naphtha splitter bottoms stream in the naphtha hydro-treating plant,
a third heat exchanger configured to transfer a portion of heat from the kerosene pumparound stream to the naphtha splitter bottoms stream in the naphtha hydro-treating plant,
a fourth heat exchanger configured to transfer a portion of heat from the kerosene product stream to the naphtha splitter bottoms stream in the naphtha hydro-treating plant, and
a fifth heat exchanger configured to transfer a portion of heat from the first stage reaction section feed stream to the amine regenerator bottoms stream in the sulfur recovery plant, and
wherein the flow control system is configured to:
flow the heated naphtha splitter bottoms stream to the naphtha hydro-treating plant; and
flow the heated amine regenerator bottoms stream to the sulfur recovery plant.

### Claim 7 (depends on 6)

The system 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.

### Claim 8 (depends on 1)

The system of claim 1, wherein the heat exchanger is a first heat exchanger,
wherein the oil refining plant comprises the sour water stripper plant and the gas separation plant,
wherein the stream comprises a sour water stripper bottoms 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 stage feed stream to the second cold high pressure separator, the first stage reaction section feed stream to the first stage cold high pressure separator, the product stripper overhead stream and the kerosene product stream,
wherein the first heat exchanger is configured to transfer the portion of the heat from the second reaction stage feed stream to the C3/C4 splitter bottoms stream in the gas separation plant,
wherein the system further comprises:
a second heat exchanger configured to transfer a portion of heat from the first stage reaction section feed stream to a first branch of the sour water stripper bottoms stream in the sour water stripper plant,
a third heat exchanger configured to transfer a portion of heat from the product stripper overhead stream to a second branch of the sour water stripper bottoms stream, and
a fourth heat exchanger configured to transfer a portion of heat from the kerosene product stream to the de-ethanizer bottoms stream in the gas separation plant, and
wherein the flow control system is configured to:
flow the heated first branch and the heated second branch to the sour water stripper plant, and
flow the heated de-ethanizer bottoms stream and the heated C3/C4 splitter bottoms stream to the gas separation plant.

### Claim 9 (depends on 8)

The system of claim 8, wherein the second heat exchanger and the third heat exchanger are fluidically coupled to each other in parallel.

### Claim 10 (depends on 1)

The system of claim 1, wherein the heat exchanger is a first heat exchanger,
wherein the oil refining plant comprises the amine regeneration plant separation section,
wherein the stream comprises the acid gas regenerator bottoms stream in the amine regeneration plant separation section,
wherein the hydrocracking plant stream comprises the diesel product stream, the first stage reaction section feed stream to the first stage cold high pressure separator, and the kerosene product stream,
wherein the first heat exchanger is configured to transfer the portion of the heat from the diesel product stream to a first branch of the acid gas regenerator bottoms stream in the amine regeneration plant separation section,
wherein the system further comprises:
a second heat exchanger configured to transfer a portion of heat from the first stage reaction section feed stream to a second branch of the acid gas regenerator bottoms stream, and
a third heat exchanger configured to transfer a portion of heat from the kerosene product stream to a third branch of the acid gas regenerator bottoms stream, and
wherein the flow control system is configured to flow the first branch, the second branch and the third branch to the amine regeneration plant separation section acid gas regenerator bottom.

### Claim 11 (depends on 10)

The system of claim 10, wherein the first heat exchanger, the second heat exchanger and the third heat exchanger are coupled to each other in parallel.

### Claim 12 (depends on 1)

The system of claim 1, wherein the heat exchanger is the first heat exchanger,
wherein the oil refining plant comprises the amine regeneration plant separation section,
wherein the stream comprises the acid gas regenerator bottoms stream in the amine regeneration plant separation section,
wherein the hydrocracking plant stream comprises the first stage reaction section feed stream to the first stage cold high pressure separator, the product stripper overhead stream, and the kerosene product stream,
wherein the first heat exchanger is configured to transfer the portion of the heat from the first stage reaction section feed stream to a first branch of the acid gas regenerator bottoms stream in the amine regeneration plant separation section,
wherein the system further comprises:
a second heat exchanger configured to transfer a portion of heat from the product stripper overhead stream to a second branch of the acid gas regenerator bottoms stream,
a third heat exchanger configured to transfer a portion of heat from the kerosene product stream to a third branch of the acid gas regenerator bottoms stream, and
wherein the flow control system is configured to flow the first branch, the second branch and the third branch to the amine regeneration plant separation section acid gas regenerator bottom.

### Claim 13 (depends on 12)

The system of claim 12, wherein the first heat exchanger, the second heat exchanger and the third heat exchanger are coupled to each other in parallel.

### Claim 14 (depends on 1)

The system of claim 1, wherein the heat exchanger is a first heat exchanger,
wherein the oil refining plant comprises the naphtha hydro-treating plant and the sour water stripper plant,
wherein the stream comprises a naphtha splitter bottoms stream in the naphtha hydro-treating plant and a sour water stripper bottoms stream in the sour water stripper plant,
wherein the hydrocracking plant stream comprises the diesel product stream, the kerosene pumparound stream, the kerosene product stream, the first stage reaction section feed stream to the first stage cold high pressure separator and the product stripper overheads stream,
wherein the first heat exchanger is configured to transfer the portion of the heat from the diesel product stream to a first branch of the naphtha splitter bottoms stream in the naphtha hydro-treating plant,
wherein the system further comprises:
a second heat exchanger configured to transfer a portion of heat from the first stage reaction section feed stream to a first branch of the sour water stripper bottoms stream in the sour water stripper plant,
a third heat exchanger configured to transfer a portion of heat from the product stripper overheads stream to a second branch of the sour water stripper bottoms stream,
a fourth heat exchanger configured to transfer a portion of heat from the kerosene pumparound stream to a second branch of the naphtha splitter bottoms stream, and
a fifth heat exchanger configured to transfer a portion of heat from the kerosene product stream to a third branch of the naphtha splitter bottoms stream, and
wherein the flow control system is configured to:
flow the heated first branch and the heated second branch of the sour water stripper bottoms stream to the sour water stripper plant, and
flow the heated first branch, the heated second branch and the heated third branch of the naphtha splitter bottoms stream to the naphtha hydro-treating plant.

### Claim 15 (depends on 14)

The system of claim 14, wherein the first heat exchanger, the fourth heat exchanger and the fifth heat exchanger are fluidically coupled to each other in parallel.

### Claim 16 (depends on 14)

The system of claim 14, wherein the second heat exchanger and the third heat exchanger are fluidically coupled to each other in parallel.

### Claim 17 (depends on 1)

The system of claim 1, wherein the heat exchanger is a first heat exchanger,
wherein the oil refining plant comprises the sulfur recovery plant and the sour water stripper plant,
wherein the stream comprises an amine regenerator bottoms stream in the sulfur recovery plant and a sour water stripper bottoms stream,
wherein the hydrocracking plant stream comprises the kerosene product stream, the diesel product stream, the first stage reaction section feed stream to the first stage cold high pressure separator, and the product stripper overheads stream,
wherein the first heat exchanger is configured to transfer the portion of the heat from the diesel product stream to a first branch of the amine regenerator bottoms stream in the sulfur recovery plant,
wherein the system further comprises:
a second heat exchanger configured to transfer a portion of heat from the first stage reaction section feed stream to a first branch of the sour water stripper bottoms stream in the sour water stripper plant,
a third heat exchanger configured to transfer a portion of heat from the product stripper overheads stream to a second branch of the sour water stripper bottoms stream, and
a fourth heat exchanger configured to transfer a portion of heat from the kerosene product stream to a second branch of the amine regenerator bottoms stream, and
wherein the flow control system is configured to:
flow the heated first branch and the heated second branch of the amine regenerator bottoms stream to the sour water stripper plant, and
flow the heated first branch and the heated second branch of the sour water stripper bottoms stream to the sulfur recovery plant.

### Claim 18 (depends on 17)

The system of claim 17, wherein the first heat exchanger and the fourth heat exchanger are fluidically coupled to each other in parallel.

### Claim 19 (depends on 17)

The system of claim 17, wherein the second heat exchanger and the third heat exchanger are fluidically coupled to each other in parallel.

### Claim 20 (depends on 1)

The system of claim 1, wherein the heat exchanger is a first heat exchanger,
wherein the oil refining plant comprises the naphtha hydro-treating plant, the sour water stripper plant, and the gas separation plant,
wherein the stream comprises a naphtha splitter bottoms stream in the naphtha hydro-treating plant, a sour water stripper bottoms stream in the sour water stripper plant, a de-ethanizer bottoms stream in the gas separation plant and a C3/C4 splitter bottoms stream in the gas separation plant,
wherein the hydrocracking plant stream comprises the diesel product stream, the kerosene pumparound stream, the first stage reaction section feed stream to the first stage cold high pressure separator, the product stripper overheads stream, and the kerosene product stream,
wherein the first heat exchanger is configured to transfer the portion of the heat from the diesel product stream to a first branch of the naphtha splitter bottoms stream in the naphtha hydro-treating plant,
wherein the system further comprises:
a second heat exchanger configured to transfer a portion of heat from the first stage reaction section feed stream to a first branch of the sour water stripper bottoms stream in the sour water stripper plant,
a third heat exchanger configured to transfer a portion of heat from the product stripper overheads stream to a second branch of the sour water stripper bottoms stream,
a fourth heat exchanger configured to transfer a portion of heat from the kerosene pumparound stream to a second branch of the naphtha splitter bottoms stream,
a fifth heat exchanger configured to transfer a portion of heat from the kerosene product stream to the de-ethanizer bottoms stream in the gas separation plant, and
a sixth heat exchanger configured to transfer a portion of heat from the kerosene product stream to the C3/C4 splitter bottom stream in the gas separation plant, and
wherein the flow control system is configured to:
flow the heated first branch and the heated second branch of the sour water stripper bottoms stream to the sour water stripper plant,
flow the heated first branch and the heated second branch of the naphtha splitter bottoms stream to the naphtha hydro-treating plant, and
flow the heated de-ethanizer bottoms stream and the heated C3/C4 splitter bottom streams to the gas separation plant.

### Claim 21 (depends on 20)

The system of claim 20, wherein the first heat exchanger and the fourth heat exchanger are fluidically coupled to each other in parallel.

### Claim 22 (depends on 20)

The system of claim 20, wherein the second heat exchanger and the third heat exchanger are fluidically coupled to each other in parallel.

### Claim 23 (depends on 1)

The system of claim 1, wherein the heat exchanger is a first heat exchanger,
wherein the oil refining plant comprises the amine regeneration plant separation section and the gas separation plant,
wherein the stream comprises the acid gas regenerator bottoms stream in the amine regeneration plant separation section, a de-ethanizer bottoms stream and a C3/C4 splitter bottoms stream in the gas separation plant,
wherein the hydrocracking plant stream comprises the diesel product stream, the first stage reaction section feed stream to the first stage cold high pressure separator, and the kerosene product stream,
wherein the first heat exchanger is configured to transfer the portion of the heat from the diesel product stream to a first branch of the acid gas regenerator bottoms stream in the amine regeneration plant separation section,
wherein the system further comprises:
a second heat exchanger configured to transfer a portion of heat from the first stage reaction section feed stream to a second branch of the acid gas regenerator bottoms stream,
a third heat exchanger configured to transfer a portion of heat from the kerosene pumparound stream to the C3/C4 splitter bottoms stream in the gas separation plant,
a fourth heat exchanger configured to transfer a portion of heat from the kerosene product stream to a third branch of the amine regeneration bottoms stream, and
a fifth heat exchanger configured to transfer a portion of heat from the kerosene product stream to the de-ethanizer bottoms stream in the gas separation plant, and
wherein the flow control system is configured to:
flow the heated first branch, the heated second branch and the heated third branch to the acid gas removal plant, and
flow the heated C3/C4 splitter bottoms stream and the heated de-ethanizer bottoms stream to the gas separation plant.

### Claim 24 (depends on 23)

The system of claim 23, wherein the first heat exchanger, the second heat exchanger and the fourth heat exchanger are fluidically coupled to each other in parallel.

### Claim 25 (depends on 1)

The system of claim 1, wherein the heat exchanger is a first heat exchanger,
wherein the oil refining plant comprises the amine regeneration plant separation section and the sulfur recovery plant,
wherein the stream comprises an amine regenerator bottoms stream in the sulfur recovery plant and an acid gas regenerator bottoms stream in the amine regeneration plant separation section,
wherein the hydrocracking plant stream comprises the diesel product stream, the kerosene product stream, the second reaction stage feed stream to the second cold high pressure separator, the product stripper overheads stream, and the first stage reaction section feed stream to the first stage cold high pressure separator,
wherein the first heat exchanger is configured to transfer the portion of the heat from the diesel product stream to a first branch of the amine regenerator bottoms stream in the sulfur recovery plant,
wherein the system further comprises:
a second heat exchanger configured to transfer a portion of heat from the second reaction stage feed stream to a first branch of the acid gas regenerator bottoms stream in the amine regeneration plant separation section,
a third heat exchanger configured to transfer a portion of heat from the first stage reaction section feed stream to a third branch of the acid gas regenerator bottoms stream, and
a fourth heat exchanger configured to transfer a portion of heat from the product stripper overheads stream to a second branch of the acid gas regenerator bottoms stream, and
wherein the flow control system is configured to:
flow the heated first branch and the heated second branch of the sulfur recovery plant streams to the sulfur recovery plant, and
flow the heated first branch, the heated second branch and the heated third branch of the acid gas regenerator bottoms stream to the amine regeneration plant separation section.

### Claim 26 (depends on 25)

The system of claim 25, wherein the first heat exchanger and the fifth heat exchanger are fluidically coupled to each other in parallel.

### Claim 27 (depends on 25)

The system of claim 25, wherein the second heat exchanger, the third heat exchanger and the fourth heat exchanger are fluidically coupled to each other in parallel.

### Claim 28 (depends on 1)

The system claim 1, wherein the heat exchanger is a first heat exchanger,
wherein the oil refining plant comprises the amine regeneration plant separation section and the naphtha hydro-treating plant,
wherein the stream comprises a naphtha splitter bottoms stream in the naphtha hydro-treating plant and an acid gas regenerator bottoms stream in the amine regeneration plant separation section and an acid gas removal stream in the amine regeneration plant separation section,
wherein the hydrocracking plant stream comprises the diesel product stream, the product stripper overhead stream, the kerosene pumparound stream, the kerosene product stream, the first stage reaction feed stream to the first stage cold high pressure separator, the product stripper overhead stream, and the kerosene product stream,
wherein the first heat exchanger is configured to transfer the portion of the heat from the diesel product stream to a first branch of the naphtha splitter bottoms stream in the naphtha hydro-treating plant,
wherein the system further comprises:
a second heat exchanger configured to transfer a portion of heat from the product stripper overhead stream to a second branch of the naphtha splitter bottom streams in the naphtha hydro-treating plant,
a third heat exchanger configured to transfer a portion of heat from the kerosene pumparound stream to a third branch of the naphtha splitter bottoms stream in the naphtha hydro-treating plant, and
a fourth heat exchanger configured to transfer a portion of heat from the kerosene product stream to a fourth branch of the naphtha splitter bottoms stream in the naphtha hydro-treating plant,
a fifth heat exchanger configured to transfer a portion of heat from the first stage reaction section feed stream to a first branch of the acid gas regenerator bottoms stream in the amine regeneration plant separation section,
a sixth heat exchanger configured to transfer a portion of heat from the product stripper overhead stream to a second branch of the acid gas regenerator bottoms stream, and
a seventh heat exchanger configured to transfer a portion of heat from the kerosene product stream to an acid gas removal branch stream in the amine regeneration plant separation section, and
wherein the flow control system is configured to:
flow the heated first branch, the heated second branch, the heated third branch and the heated fourth branch of the naphtha splitter bottoms stream to the naphtha hydro-treating plant, and
flow the heated first branch and the heated second branch of the acid gas regenerator bottoms stream, and the heated acid gas removal branch stream to the amine regeneration plant separation section.

### Claim 29 (depends on 28)

The system of claim 28, wherein the fifth heat exchanger, the sixth heat exchanger and the seventh heat exchanger are fluidically coupled to each other in parallel.

### Claim 30 (depends on 28)

The system of claim 28, 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.

### Claim 31 (depends on 28)

The system of claim 28, wherein the second heat exchanger and the sixth heat exchanger are fluidically coupled to each other in series.

### Claim 32 (depends on 1)

The system of claim 1, wherein the heat exchanger is a first heat exchanger, and
wherein the system further comprises a diesel hydro-treating plant of the crude oil refining facility, the diesel hydro-treating plant comprising a diesel stripper column and configured to perform at least one crude oil refining process, the diesel hydro-treating plant flowing a diesel hydro-treating plant stream.

### Claim 33 (depends on 32)

The system of claim 32, wherein the diesel hydro-treating plant stream comprises a diesel hydro-treating plant diesel product stream and a stripper overhead stream,
wherein the oil refining plant comprises the amine regeneration plant separation section, the sulfur recovery plant and the sour water stripper plant,
wherein the stream comprises an amine regenerator bottoms stream in the sulfur recovery plant, an acid gas regenerator bottoms stream in the amine regeneration plant separation section and a bottom stream in the sour water stripper plant,
wherein the hydrocracking plant stream comprises the diesel product stream, the kerosene product stream, the first stage reaction section feed stream to the first stage cold high pressure separator, the diesel product stream, the stripper overhead stream, the kerosene pumparound stream and the diesel stripper overhead stream,
wherein the first heat exchanger is configured to transfer the portion of the heat from the diesel product stream to a first branch of the amine regenerator bottoms stream in the sulfur recovery plant,
wherein the system further comprises:
a second heat exchanger configured to transfer a portion of heat from the first stage reaction section feed stream to a first branch of the acid gas regenerator bottoms stream in the amine regeneration plant separation section,
a third heat exchanger configured to transfer a portion of heat from the stripper overhead stream to a first branch of the bottom stream in the sour water stripper plant,
a fourth heat exchanger configured to transfer a portion of heat from the kerosene pumparound stream to a second branch of the bottom stream in the sour water stripper plant,
a fifth heat exchanger configured to transfer a portion of heat from the kerosene product stream to a second branch of the amine regenerator bottoms stream,
a sixth heat exchanger configured to transfer a portion of heat from the stripper overhead stream of the diesel hydro-treating plant to a third branch of the bottom stream in the sour water stripper plant, and
a seventh heat exchanger configured to transfer a portion of heat from the diesel hydro-treating plant diesel product stream to a second branch of the acid gas regenerator bottoms stream, and
wherein the flow control system is configured to:
flow the heated first branch of the acid gas regenerator bottoms stream and the heated second branch of the acid gas regenerator bottoms stream to the amine regeneration plant separation section,
flow the heated first branch of the amine regenerator bottoms stream and the heated second branch of the amine regenerator bottoms stream to the sulfur recovery plant, and
flow the heated first branch of the bottom stream, the heated second branch of the bottom stream and the heated third branch of the bottom stream to the sour water stripper plant.

### Claim 34 (depends on 32)

The system of claim 32, wherein the first heat exchanger and the fifth heat exchanger are fluidically coupled to each other in parallel.

### Claim 35 (depends on 32)

The system of claim 32, wherein the second heat exchanger and the seventh heat exchanger are fluidically coupled to each other in parallel.

### Claim 36 (depends on 32)

The system of claim 32, wherein the third heat exchanger, the fourth heat exchanger and the sixth heat exchanger are fluidically coupled to each other in parallel.

### Claim 37 (depends on 32)

The system of claim 32, wherein the diesel hydro-treating plant stream comprises a diesel stripper bottom product stream, and a stripper overhead stream and a hot stream to be cooled in a hydrogen plant in the crude oil refining facility, the hydrogen plant comprising a steam reforming furnace or a pressure swing adsorption (PSA) vessel,
wherein the oil refining plant comprises the amine regeneration plant separation section, the sulfur recovery plant, the gas separation plant and the sour water stripper plant,
wherein the stream comprises an amine regenerator bottoms stream in the sulfur recovery plant, an acid gas regenerator stream in the amine regeneration plant separation section, a bottom stream in the sour water stripper plant, a C3/C4 splitter bottoms stream in the gas separation plant and a de-ethanizer bottoms stream in the gas separation plant,
wherein the hydrocracking plant stream comprises the diesel product stream, the kerosene product stream, the first stage reaction section feed stream to the first stage cold high pressure separator, the product stripper overheads stream, and the kerosene pumparound stream,
wherein the first heat exchanger is configured to transfer the portion of the heat from the diesel product stream to a first branch of the amine regenerator bottoms stream in the sulfur recovery plant,
wherein the system further comprises:
a second exchanger configured to transfer a portion of heat from the first stage reaction section feed stream to a first branch of the acid gas regenerator bottoms stream in the amine regeneration plant separation section,
a third heat exchanger configured to transfer a portion of heat from the product stripper overheads stream to a first branch of the bottom stream in the sour water stripper plant,
a fourth heat exchanger configured to transfer a portion of heat from the kerosene pumparound stream to a first branch of the C3/C4 splitter bottoms stream in the gas separation plant,
a fifth heat exchanger configured to transfer a portion of heat from the kerosene product stream to a second branch of the amine regenerator bottoms stream,
a sixth heat exchanger configured to transfer a portion of heat from the stripper overhead stream of the diesel hydro-treating plant to a second branch of the bottom stream in the sour water stripper plant,
a seventh heat exchanger configured to transfer a portion of heat from the diesel stripper bottom product stream of the diesel hydro-treating plant to a second branch of the acid gas regenerator bottoms stream,
an eighth heat exchanger configured to transfer a portion of heat from the diesel stripper bottom product stream of the diesel hydro-treating plant to a second branch of the C3/C4 splitter bottoms stream, and
a ninth heat exchanger configured to transfer a portion of heat from the diesel stripper bottom product stream of the diesel hydro-treating plant to the de-ethanizer bottoms stream in the gas separation plant,
a tenth heat exchanger configured to transfer a portion of heat from the hot stream to be cooled in the hydrogen plant to a fourth branch of the bottom stream in the sour water stripper plant, and
wherein the flow control system is configured to:
flow the heated first branch of the amine regenerator bottoms stream and the heated second branch of the amine regenerator bottoms stream to the sulfur recovery plant,
flow the heated first branch of the acid gas regenerator bottoms stream and the heated second branch of the acid gas regenerator bottoms stream to the amine regeneration plant separation section,
flow the heated first branch of the bottom stream, the heated third branch of the bottom stream and the heated fourth branch of the bottom stream to the sour water stripper plant, and
flow the heated first branch of the C3/C4 splitter bottoms stream, the heated second branch of the C3/C4 splitter bottoms stream and the heated de-ethanizer bottoms stream to the gas separation plant.

### Claim 38 (depends on 37)

The system of claim 37, wherein the first heat exchanger and the fifth heat exchanger are fluidically coupled to each other in parallel.

### Claim 39 (depends on 38)

The system of claim 38, wherein the second heat exchanger and the seventh heat exchanger are fluidically coupled to each other in parallel.

### Claim 40 (depends on 38)

The system of claim 38, wherein the third heat exchanger, the sixth heat exchanger and the tenth heat exchanger are fluidically coupled to each other in parallel.

### Claim 41 (depends on 38)

The system of claim 38, wherein the seventh heat exchanger and the eighth heat exchanger are fluidically coupled to each other in series.

### Claim 42 (depends on 38)

The system of claim 38, wherein the fourth heat exchanger and the eighth heat exchanger are fluidically coupled to each other in parallel.

### Claim 43 (depends on 38)

The system of claim 38, wherein the eighth heat exchanger and the ninth heat exchanger are fluidically coupled to each other in series.

### Claim 44 (depends on 32)

The method of claim 32, wherein the diesel hydro-treating plant stream comprises a diesel stripper bottom product stream, and a stripper overhead stream, and a hot stream to be cooled in a hydrogen plant in the crude oil refining facility,
wherein the oil refining plant comprises the acid gas removal plant, the sulfur recovery plant, the gas separation plant, the naphtha hydro-treating plant and the sour water stripper plant, wherein the stream comprises a naphtha splitter bottoms stream in the naphtha hydro-treating plant, a bottom stream in the acid gas removal plant, a sulfur plant amine regenerator bottoms stream in the acid gas removal plant, a sour water stripper bottoms stream in the sour water stripper plant, a C3/C4 splitter bottoms stream in the gas separation plant, a de-ethanizer bottoms stream in the gas separation plant,
wherein the hydrocracking plant stream comprises the diesel product stream, the kerosene pumparound stream, the kerosene product stream, the product stripper overheads stream, the second reaction stage feed stream to the second cold high pressure separator, the first stage reaction section feed stream to the first stage cold high pressure separator, and
wherein the first heat exchanger is configured to transfer the portion of the heat from the hydrocracking plant product stream to a first branch of the naphtha splitter bottoms stream in the naphtha hydro-treating plant,
wherein the system further comprises:
a second heat exchanger configured to transfer a portion of heat from the hydrocracking plant product stream to a first branch of the amine regenerator bottoms stream in the sulfur recovery plant,
a third heat exchanger configured to transfer a portion of heat from the second reaction stage feed stream to a second branch of the amine regenerator bottoms stream,
a fourth heat exchanger configured to transfer a portion of heat from the first stage reaction section feed stream to the bottom stream in the amine regeneration plant separation section,
a fifth heat exchanger configured to transfer a portion of heat from the hydrocracking plant stripper overhead stream to a first branch of the sour water stripper bottoms stream in the sour water stripper plant,
a sixth heat exchanger configured to transfer a portion of heat from the kerosene pumparound stream to a second branch of the naphtha splitter bottoms stream,
a seventh heat exchanger configured to transfer a portion of heat from the kerosene pumparound stream to a first branch of the C3/C4 splitter bottoms stream in the gas separation plant,
an eighth heat exchanger configured to transfer a portion of heat from the kerosene product stream to a third branch of the naphtha splitter bottoms stream,
a ninth heat exchanger configured to transfer a portion of heat from the kerosene product stream to a first branch of the amine regenerator bottoms stream in the sulfur plant,
a tenth heat exchanger configured to transfer a portion of heat from the diesel stripper bottom product stream to a fourth branch of the naphtha splitter bottoms stream,
an eleventh heat exchanger configured to transfer a portion of heat from the stripper overhead stream to a second branch of the sour water stripper bottoms stream,
a twelfth heat exchanger configured to transfer a portion of heat from the diesel stripper bottom product stream to a second branch of the amine regenerator bottoms stream,
a thirteenth heat exchanger configured to transfer a portion of heat from the diesel stripper bottom product stream to a second branch of the C3/C4 splitter bottoms stream,
a fourteenth heat exchanger configured to transfer a portion of heat from the diesel stripper bottom product stream to the de-ethanizer bottoms stream in the gas separation plant, and
a fifteenth heat exchanger configured to transfer a portion of heat from the hot stream to be cooled in the hydrogen plant to a third branch of the sour water stripper bottoms stream, and
wherein the flow control system is configured to:
flow the heated first branch of the naphtha splitter bottoms stream, the heated second branch of the naphtha splitter bottoms stream, the heated third branch of the naphtha splitter bottoms stream and the heated fourth branch of the naphtha splitter bottoms stream to the naphtha hydro-treating plant,
flow the heated first branch of the amine regenerator bottoms stream, the heated second branch of the amine regenerator bottoms stream and the heated third branch of the amine regenerator bottoms stream to the sulfur recovery plant,
flow the heated first branch of the acid gas removal plant amine regenerator bottom stream and the heated second branch of the acid gas removal plant amine regenerator bottom stream to the acid gas removal plant,
flow the heated first branch of the sour water stripper bottoms stream, the heated second branch of the sour water stripper bottoms stream and the heated third branch of the sour water stripper bottoms stream to the sour water stripper plant, and
flow the heated first branch of the C3/C4 splitter bottoms stream, the heated second branch of the C3/C4 splitter bottoms stream and the heated de-ethanizer bottoms stream to the gas separation plant.

### Claim 45 (depends on 44)

The system of claim 44, wherein the first heat exchanger, the sixth heat exchanger, the eighth heat exchanger and the tenth heat exchanger are fluidically coupled to each other in parallel.

### Claim 46 (depends on 44)

The system of claim 44, wherein the first heat exchanger and the second heat exchanger are fluidically coupled to each other in series.

### Claim 47 (depends on 44)

The system of claim 44, wherein the eighth heat exchanger and the ninth heat exchanger are coupled to each other in series.

### Claim 48 (depends on 44)

The system of claim 44, wherein the fourth heat exchanger and the twelfth heat exchanger are fluidically coupled to each other in parallel.

### Claim 49 (depends on 44)

The system of claim 44, wherein the tenth heat exchanger and the eleventh heat exchanger are fluidically coupled to each other in series.

### Claim 50 (depends on 44)

The system of claim 44, wherein the fifth heat exchanger, the eleventh heat exchanger and the fifteenth heat exchanger are fluidically coupled to each other in parallel.

### Claim 51 (depends on 44)

The system of claim 44, wherein the sixth heat exchanger and the seventh heat exchanger are fluidically coupled to each other in series.

### Claim 52 (depends on 44)

The system of claim 44, wherein the seventh heat exchanger and the thirteenth heat exchanger are fluidically coupled to each other in parallel.

### Claim 53 (depends on 44)

The system of claim 44, wherein the twelfth heat exchanger and the thirteenth heat exchanger are fluidically coupled to each other in series.