US20120085095A1 - Utilization of process heat by-product - Google Patents

Utilization of process heat by-product Download PDF

Info

Publication number: US20120085095A1
Authority: US; United States
Prior art keywords: working fluid; fluid stream; heat; stream; product
Prior art date: 2010-10-06
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.): Abandoned

Application number

US13/267,635

Other languages

English (en)

Inventor

John David Penton

Leonore R. Rouse

Jerry M. Rovner

Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)

Chevron USA Inc

Chevron Corp

Original Assignee

Chevron USA Inc

Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)

2010-10-06

Filing date

2011-10-06

Publication date

2012-04-12

2011-10-06 Application filed by Chevron USA Inc filed Critical Chevron USA Inc

2011-10-06 Priority to US13/267,635 priority Critical patent/US20120085095A1/en

2011-10-06 Assigned to CHEVRON CORPORATION reassignment CHEVRON CORPORATION ASSIGNMENT OF ASSIGNORS INTEREST (SEE DOCUMENT FOR DETAILS). Assignors: PENTON, JOHN DAVID, ROUSE, LEONORE R., ROVNER, JERRY M.

2012-04-12 Publication of US20120085095A1 publication Critical patent/US20120085095A1/en

2013-03-08 Assigned to CHEVRON U.S.A. INC. reassignment CHEVRON U.S.A. INC. ASSIGNMENT OF ASSIGNORS INTEREST (SEE DOCUMENT FOR DETAILS). Assignors: PENTON, JOHN DAVID, ROUSE, LEONORE R., ROVNER, JERRY M.

2013-03-15 Assigned to CHEVRON U.S.A. INC. reassignment CHEVRON U.S.A. INC. CORRECTIVE ASSIGNMENT TO CORRECT THE RECEIVING PARTY FROM CHEVRON CORPORATION TO CHEVRON U.S.A. INC. PREVIOUSLY RECORDED ON REEL 029947 FRAME 0858. ASSIGNOR(S) HEREBY CONFIRMS THE SELL, ASSIGNMENT, TRANSFER AND SET OVER UNTO SAID CHEVRON U.S.A. INC. Assignors: PENTON, JOHN DAVID, ROUSE, LEONORE R., ROVNER, JERRY M.

Status Abandoned legal-status Critical Current

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Classifications

- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F01—MACHINES OR ENGINES IN GENERAL; ENGINE PLANTS IN GENERAL; STEAM ENGINES
- F01K—STEAM ENGINE PLANTS; STEAM ACCUMULATORS; ENGINE PLANTS NOT OTHERWISE PROVIDED FOR; ENGINES USING SPECIAL WORKING FLUIDS OR CYCLES
- F01K23/00—Plants characterised by more than one engine delivering power external to the plant, the engines being driven by different fluids
- F01K23/02—Plants characterised by more than one engine delivering power external to the plant, the engines being driven by different fluids the engine cycles being thermally coupled
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F01—MACHINES OR ENGINES IN GENERAL; ENGINE PLANTS IN GENERAL; STEAM ENGINES
- F01K—STEAM ENGINE PLANTS; STEAM ACCUMULATORS; ENGINE PLANTS NOT OTHERWISE PROVIDED FOR; ENGINES USING SPECIAL WORKING FLUIDS OR CYCLES
- F01K25/00—Plants or engines characterised by use of special working fluids, not otherwise provided for; Plants operating in closed cycles and not otherwise provided for
- F01K25/08—Plants or engines characterised by use of special working fluids, not otherwise provided for; Plants operating in closed cycles and not otherwise provided for using special vapours
- F01K25/10—Plants or engines characterised by use of special working fluids, not otherwise provided for; Plants operating in closed cycles and not otherwise provided for using special vapours the vapours being cold, e.g. ammonia, carbon dioxide, ether
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F01—MACHINES OR ENGINES IN GENERAL; ENGINE PLANTS IN GENERAL; STEAM ENGINES
- F01K—STEAM ENGINE PLANTS; STEAM ACCUMULATORS; ENGINE PLANTS NOT OTHERWISE PROVIDED FOR; ENGINES USING SPECIAL WORKING FLUIDS OR CYCLES
- F01K13/00—General layout or general methods of operation of complete plants
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F01—MACHINES OR ENGINES IN GENERAL; ENGINE PLANTS IN GENERAL; STEAM ENGINES
- F01K—STEAM ENGINE PLANTS; STEAM ACCUMULATORS; ENGINE PLANTS NOT OTHERWISE PROVIDED FOR; ENGINES USING SPECIAL WORKING FLUIDS OR CYCLES
- F01K19/00—Regenerating or otherwise treating steam exhausted from steam engine plant
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F22—STEAM GENERATION
- F22B—METHODS OF STEAM GENERATION; STEAM BOILERS
- F22B33/00—Steam-generation plants, e.g. comprising steam boilers of different types in mutual association
- F22B33/18—Combinations of steam boilers with other apparatus

Definitions

the present application generally relates to heat recovery and utilization. More particularly, the present application relates to the utilization of process heat by-product to generate electricity and/or mechanical power.
the present invention is directed to processes for heat recovery from process heat by-product, wherein such heat recovery is realized by channeling thermal energy from a process heat by-product stream to an organic Rankine cycle—from which electricity can be derived through a turbine-driven generator.
the present invention is also directed to systems for implementing such processes.
a process for indirectly utilizing process heat by-product from refinery operations includes three sub-processes that occur simultaneously.
the first and second sub-processes are linked via a first heater, and the second and third sub-processes are linked via a second heater.
a process heat by-product stream is directed to the first heater and is utilized to heat a first working fluid stream to produce a cooled by-product stream and a heated working fluid stream.
the cooled by-product stream is then exhausted to atmosphere.
the process heat by-product stream includes flue gas from a fluid catalytic cracking unit or recovered heat from a high temperature reactor, such as a fired heater, incinerator, hydrotreater, catalytic reformer, or isomerization unit.
a high temperature reactor such as a fired heater, incinerator, hydrotreater, catalytic reformer, or isomerization unit.
the first working fluid stream is heated by the process heat by-product stream in the first heater to form a first heated working fluid stream.
the first heated working fluid stream is directed to the second heater, and is utilized to heat a working fluid stream of an organic Rankine cycle to produce a cooled working fluid stream and a second heated working fluid stream.
the cooled working fluid stream is then passed through a pump to form the first working fluid stream.
the working fluid stream of the organic Rankine cycle is heated to form the second heated working fluid stream.
the second heated working fluid stream is vaporized.
the second heated working fluid stream is passed through a turbine-generator set to form an expanded working fluid stream and produce electricity and/or mechanical power.
the expanded working fluid stream is then directed to another heat exchanger to form a condensed working fluid stream.
the condensed working fluid stream is then passed through a pump to form the working fluid stream that enters the second heater.
a process for indirectly utilizing waste heat by-product includes three sub-processes that occur simultaneously.
the first and second sub-processes are linked via a first heater, and the second and third sub-processes are linked via a second heater.
a waste heat by-product stream is directed to the first heater and is utilized to heat a first working fluid stream to produce a cooled by-product stream and a heated working fluid stream.
the cooled by-product stream is then exhausted to atmosphere.
the cooled by-product stream is directed to an incinerator, a scrubber, or a stack prior to being exhausted to the atmosphere.
the waste heat by-product stream includes waste heat from a steam generator, gas turbine, or diesel generator.
the first working fluid stream is heated by the waste heat by-product stream in the first heater to form a first heated working fluid stream.
the first heated working fluid stream is directed to the second heater, and is utilized to heat a working fluid stream of an organic Rankine cycle to produce a cooled working fluid stream and a second heated working fluid stream.
the cooled working fluid stream is then passed through a pump to form the first working fluid stream.
the working fluid stream of the organic Rankine cycle is heated to form the second heated working fluid stream.
the second heated working fluid stream is vaporized.
the second heated working fluid stream is passed through a turbine-generator set to form an expanded working fluid stream and produce electricity and/or mechanical power.
the expanded working fluid stream is then directed to another heat exchanger to form a condensed working fluid stream.
the condensed working fluid stream is then passed through a pump to form the working fluid stream that enters the second heater.
a system for utilizing a heat by-product includes a process heat by-product stream and an organic Rankine cycle subsystem.
the organic Rankine cycle subsystem includes a heat exchanger in thermal communication with the heat by-product stream, an organic Rankine cycle flow line having a working fluid, whereby the flow line is in thermal communication with the heat exchanger, and whereby the heat exchanger transfers thermal energy from the heat by-product stream to the working fluid so as to heat the working fluid to form a heated working fluid, a turbine-based generator for generating electricity and/or mechanical power from the heated working fluid passing through, one or more condensers for condensing the heated working fluid to form a condensed working fluid, and a pump for pumping the condensed working fluid to a higher pressure to form the working fluid that enters the heat exchanger.
FIG. 1 is a schematic diagram of a heat recovery system for utilization of waste heat from a fluid catalytic cracking unit, according to an exemplary embodiment.
FIG. 2 is a schematic diagram of a heat recovery system for utilization of waste heat from a fluid catalytic cracking unit, according to another exemplary embodiment.
FIG. 3 is a schematic diagram of a heat recovery system for utilization of waste heat from a fluid catalytic cracking unit, according to yet another exemplary embodiment.
FIG. 4 is a schematic diagram of a heat recovery system for utilization of waste heat from a fluid catalytic cracking unit, according to yet another exemplary embodiment.
FIG. 5 is a schematic diagram of a heat recovery system for utilization of process heat by-product from a fired heater unit, according to an exemplary embodiment.
FIG. 6 is a schematic diagram of a heat recovery system for utilization of process heat by-product from a fired heater unit, according to another exemplary embodiment.
FIG. 7 is a schematic diagram of a heat recovery system for utilization of process heat by-product from a fired heater unit, according to yet another exemplary embodiment.
FIG. 8 is a schematic diagram of a heat recovery system for utilization of process heat by-product from a fired heater unit, according to yet another exemplary embodiment.
FIG. 9 is a schematic diagram of a heat recovery system for utilization of an exhaust gas stream from a steam generator unit, according to an exemplary embodiment.
FIG. 10 is a schematic diagram of a heat recovery system for utilization of an exhaust gas stream from a steam generator unit, according to another exemplary embodiment.
FIG. 11 is a schematic diagram of a heat recovery system for utilization of an exhaust gas stream from a steam generator unit, according to yet another exemplary embodiment.
FIG. 12 is a schematic diagram of a heat recovery system for utilization of an exhaust gas stream from a steam generator unit, according to yet another exemplary embodiment.
FIG. 13 is a schematic diagram of a heat recovery system for utilization of an exhaust gas stream from a gas turbine unit, according to an exemplary embodiment.
FIG. 14 is a schematic diagram of a heat recovery system for utilization of an exhaust gas stream from a gas turbine unit, according to another exemplary embodiment.
FIG. 15 is a schematic diagram of a heat recovery system for utilization of an exhaust gas stream from a gas turbine unit, according to yet another exemplary embodiment.
FIG. 16 is a schematic diagram of a heat recovery system for utilization of an exhaust gas stream from a gas turbine unit, according to yet another exemplary embodiment.
FIG. 17 is a schematic diagram of a heat recovery system for utilization of a process heat stream, according to an exemplary embodiment.
FIG. 18 is a schematic diagram of a heat recovery system for utilization of a process heat stream, according to another exemplary embodiment.
FIG. 19 is a schematic diagram of a heat recovery system for utilization of a process heat stream, according to yet another exemplary embodiment.
FIG. 20 is a schematic diagram of a heat recovery system for utilization of a process heat stream, according to yet another exemplary embodiment.
FIG. 1 shows a direct heat recovery system 100 for utilization of a flue gas stream 102 from a fluid catalytic cracking regenerator unit 101 .
the flue gas stream 102 is a high temperature heat stream that is generated by the combustion of coke in the fluid catalytic cracking regenerator unit 101 .
the flue gas stream 102 has a temperature in the range of from about 1100 to about 1800° F.
when the combustion of coke is complete at least a portion 102 a of the flue gas stream 102 enters a waste heat steam generator 103 .
a boiler feed water stream 104 also enters the waste heat steam generator 103 , and heat from the flue gas stream 102 is utilized to heat the boiler feed water stream 104 to produce a steam stream 105 .
the waste heat steam generator 103 generates steam at pressures in the range of from about 15 to about 1100 pound-force per square inch gauge (psig).
a reduced heat flue gas stream 106 then exits the waste heat steam generator 103 and enters an electrostatic precipitator 107 , which removes any catalyst fines 108 present in the reduced heat flue gas stream 106 to produce a reduced fines flue gas stream 109 .
the reduced fines flue gas stream 109 has a temperature in the range of from about 350 to about 800° F.
the flue gas stream 102 when the combustion of coke is incomplete and the flue gas stream 102 contains significant amounts of carbon monoxide, at least a portion 102 b of the flue gas stream 102 enters a carbon monoxide boiler 110 .
a fuel stream 111 and an air stream 112 also enter the boiler 110 to combust the carbon monoxide in the flue gas stream 102 .
a boiler feed water stream 114 also enters the boiler 110 , and heat from the combustion process and the flue gas stream 102 is utilized to heat the boiler feed water stream 114 to produce a steam stream 115 .
the boiler 110 operates at a pressure in the range of from about 15 to about 1100 psig.
a reduced heat flue gas stream 116 then exits the boiler 110 and enters an electrostatic precipitator 117 to remove any catalyst fines 118 present in the reduced heat flue gas stream 116 to produce a reduced fines flue gas stream 119 .
the reduced fines flue gas stream 119 has a temperature in the range of from about 350 to about 800° F.
a portion 102 a of the flue gas stream 102 can be routed through the waste heat steam generator 103 , and the resulting reduced fines flue gas stream 109 can be combined with a remainder portion 102 c of the flue gas stream 102 afterwards prior to entering a heat exchanger 120 .
the heat exchanger 120 is a part of the organic Rankine cycle.
the heat exchanger 120 may be any type of heat exchanger capable of transferring heat from one fluid stream to another fluid stream. Suitable examples of heat exchangers include, but are not limited to, heaters, vaporizers, economizers, and other heat recovery heat exchangers.
the heat exchanger 120 may be a shell-and-tube heat exchanger, a plate-fin-tube coil type of exchanger, a bare tube or finned tube bundle, a welded plate heat exchanger, and the like.
the present invention should not be considered as limited to any particular type of heat exchanger unless such limitations are expressly set forth in the appended claims.
the flue gas stream 102 can be entirely routed through the waste heat steam generator 103 .
a portion 102 b of the flue gas stream 102 can be routed through the through the boiler 110 , and the resulting reduced fines flue gas stream 119 can be combined with the remainder portion 102 c of the flue gas stream 102 afterwards prior to entering the heat exchanger 120 .
the flue gas stream 102 can be entirely routed through the boiler 110 .
a first portion 102 a of the flue gas stream 102 can be routed through the waste heat steam generator 103 , a second portion 102 b of the flue gas stream 102 can be routed through the boiler 110 , and the resulting reduced fines flue gas streams 109 , 119 can be combined with a third portion 102 c of the flue gas stream 102 afterwards prior to entering the heat exchanger 120 .
the flue gas stream 102 can directly enter heat exchanger 120 .
the flue gas stream 102 can be treated any number of ways and in any combination to produce an input flue gas stream 125 prior to entering the heat exchanger 120 .
At least a portion 125 a of the input flue gas stream 125 is then utilized to heat a working fluid stream 126 in the heat exchanger 120 .
the portion 125 a of the input flue gas stream 125 thermally contacts the working fluid stream 126 to transfer heat to the working fluid stream 126 .
the phrase “thermally contact” generally refers to the exchange of energy through the process of heat, and does not imply physical mixing or direct physical contact of the materials.
the working fluid stream 126 includes any working fluid suitable for use in an organic Rankine cycle.
the portion 125 a of the input flue gas stream 125 and the working fluid stream 126 enter the heat exchanger 120 to produce a heated working fluid stream 128 and a reduced heat flue gas stream 129 .
the working fluid stream 126 has a temperature in the range of from about 80 to about 150° F.
the heated working fluid stream 128 has a temperature in the range of from about 160 to about 450° F.
the heated working fluid stream 128 is vaporized.
the heated working fluid stream 128 is vaporized within a supercritical process, with conditions at a temperature and pressure above the critical point for the heated working fluid stream 128 .
the heated working fluid stream 128 is superheated.
the working fluid stream 126 enters as a high pressure liquid and the heated working fluid stream 128 exits as a superheated vapor.
the reduced heat flue gas stream 129 has a temperature in the range of from about 300 to about 750° F.
the reduced heat flue gas stream 129 is cooled to a temperature just above its dew point. The reduced heat flue gas stream 129 can then be vented to the atmosphere.
a portion 125 b of the input flue gas stream 125 is diverted through a bypass valve 130 and then combined with the reduced heat flue gas stream 129 to produce an exhaust flue gas stream 131 to be vented to the atmosphere.
the exhaust flue gas stream 131 has a temperature in the range of from about 300° F. to about 800° F.
the entire portion 125 a of the input flue gas stream 125 is directed through the heat exchanger 120 , and is exhausted to the atmosphere at a temperature of about 300° F.
At least a portion 128 a of the heated working fluid stream 128 is then directed to a turbine-generator system 150 , which is a part of the organic Rankine cycle.
turbine will be understood to include both turbines and expanders or any device wherein useful work is generated by expanding a high pressure gas within the device.
the portion 128 a of the heated working fluid stream 128 is expanded in the turbine-generator system 150 to produce an expanded working fluid stream 151 and generate power.
the expanded working fluid stream 151 has a temperature in the range of from about 80 to about 440° F.
the turbine-generator system 150 generates electricity or electrical power.
the turbine-generator system 150 generates mechanical power.
a portion 128 b of the heated working fluid stream 128 is diverted through a bypass valve 152 and then combined with the expanded working fluid stream 151 to produce an intermediate working fluid stream 155 .
the intermediate working fluid stream 155 has a temperature in the range of from about 85 to about 445° F.
the intermediate working fluid stream 155 is then directed to one or more air-cooled condensers 157 .
the air-cooled condensers 157 are a part of the organic Rankine cycle.
the organic Rankine cycle includes two air-cooled condensers 157 in series. Suitable examples of air-cooled condensers include, but are not limited to, air coolers and evaporative coolers.
each of the air-cooled condensers 157 is controlled by a variable frequency drive 158 .
the air-cooled condensers 157 cool the intermediate working fluid stream 155 to form a condensed working fluid stream 159 .
the condensed working fluid stream 159 has a temperature in the range of from about 80 to about 150° F.
the condensed working fluid stream 159 is then directed to a pump 160 .
the pump 160 is a part of the organic Rankine cycle.
the pump 160 may be any type of commercially available pump sufficient to meet the pumping requirements of the systems disclosed herein.
the pump 160 is controlled by a variable frequency drive 161 .
the pump 160 returns the condensed working fluid stream 159 to a higher pressure to produce the working fluid stream 126 that is directed to the heat exchanger 120 .
FIG. 2 shows a direct heat recovery system 200 according to another exemplary embodiment.
the heat recovery system 200 is the same as that described above with regard to heat recovery system 100 , except as specifically stated below. For the sake of brevity, the similarities will not be repeated hereinbelow.
the intermediate working fluid stream 155 is then directed to one or more water-cooled condensers 257 .
the water-cooled condensers 257 are a part of the organic Rankine cycle.
the organic Rankine cycle includes two water-cooled condensers 257 in series. The water-cooled condensers 257 cool the intermediate working fluid stream 155 to form a condensed working fluid stream 259 .
the condensed working fluid stream 259 has a temperature in the range of from about 80 to about 150° F.
the condensed working fluid stream 259 is then directed to the pump 160 and is returned to a higher pressure to produce the working fluid stream 126 that is directed to the heat exchanger 120 .
FIG. 3 shows an indirect heat recovery system 300 for utilization of an input flue gas stream 325 .
the input flue gas stream 325 is the same as that described above with regard to input flue gas stream 125 , and for the sake of brevity, the similarities will not be repeated hereinbelow.
at least a portion 325 a of the input flue gas stream 325 is utilized to heat a working fluid stream 326 in a heat exchanger 320 .
the portion 325 a of the input flue gas stream 325 thermally contacts the working fluid stream 326 and transfers heat to the working fluid stream 326 .
Suitable examples of the working fluid stream 326 include, but are not limited to, water, glycols, therminol fluids, alkanes, alkenes, chlorofluorocarbons, hydrofluorocarbons, carbon dioxide (CO2), refrigerants, and mixtures of other hydrocarbon components.
the portion 325 a of the input flue gas stream 325 and the working fluid stream 326 enter the heat exchanger 320 to produce a heated working fluid stream 328 and a reduced heat flue gas stream 329 .
the working fluid stream 326 has a temperature in the range of from about 85 to about 160° F.
the heated working fluid stream 328 has a temperature in the range of from about 165 to about 455° F.
the reduced heat flue gas stream 329 has a temperature in the range of from about 300 to about 750° F. In certain embodiments, the reduced heat flue gas stream 329 is cooled to a temperature just above its dew point. The reduced heat flue gas stream 329 can then be vented to the atmosphere. In certain exemplary embodiments, a portion 325 b of the input flue gas stream 325 is diverted through a bypass valve 330 and then combined with the reduced heat flue gas stream 329 to produce an exhaust flue gas stream 331 to be vented to the atmosphere. In certain exemplary embodiments, the exhaust flue gas stream 331 has a temperature in the range of from about 300 to about 800° F. In certain exemplary embodiments, the input flue gas stream 325 is entirely directed through the heat exchanger 320 , and is exhausted to the atmosphere at a temperature of about 300° F.
a portion 328 a of the heated working fluid stream 328 enters a heat exchanger 335 to heat a working fluid stream 336 to produce a heated working fluid stream 337 and a reduced heat working fluid stream 338 .
the portion 328 a of the heated working fluid stream 328 thermally contacts the working fluid stream 336 and transfers heat to the working fluid stream 336 .
the working fluid stream 336 includes any working fluid suitable for use in an organic Rankine cycle.
the working fluid stream 336 has a temperature in the range of from about 80 to about 150° F.
the heated working fluid stream 337 has a temperature in the range of from about 160 to about 450° F.
the heated working fluid stream 337 is vaporized. In certain exemplary embodiments, the heated working fluid stream 337 is vaporized within a supercritical process. In certain exemplary embodiments, the heated working fluid stream 337 is superheated. In certain exemplary embodiments, the reduced heat working fluid stream 338 has a temperature in the range of from about 85 to about 155° F. In certain embodiments, a portion 328 b of the heated working fluid stream 328 is diverted through a bypass valve 339 and then combined with the reduced heat working fluid stream 338 to produce an intermediate working fluid stream 340 . In certain exemplary embodiments, the intermediate working fluid stream 340 has a temperature in the range of from about 85 to about 160° F.
the intermediate working fluid stream 340 is then directed to a pump 342 .
the pump 342 is controlled by a variable frequency drive 343 .
the pump 342 returns the intermediate working fluid stream 340 to produce the working fluid stream 326 that enters the heat exchanger 320 .
At least a portion 337 a of the heated working fluid stream 337 is then directed to a turbine-generator system 350 , which is a part of the organic Rankine cycle.
the portion 337 a of the heated working fluid stream 337 is expanded in the turbine-generator system 350 to produce an expanded working fluid stream 351 and generate power.
the expanded working fluid stream 351 has a temperature in the range of from about 80 to about 440° F.
the turbine-generator system 350 generates electricity or electrical power. In certain other embodiments, the turbine-generator system 350 generates mechanical power.
a portion 337 b of the heated working fluid stream 337 is diverted through a bypass valve 352 and then combined with the expanded working fluid stream 351 to produce an intermediate working fluid stream 355 .
the intermediate working fluid stream 355 has a temperature in the range of from about 85 to about 445° F.
the intermediate working fluid stream 355 is then directed to one or more air-cooled condensers 357 .
the air-cooled condensers 357 are a part of the organic Rankine cycle.
the organic Rankine cycle includes two air-cooled condensers 357 in series.
each of the air-cooled condensers 357 is controlled by a variable frequency drive 358 .
the air-cooled condensers 357 cool the intermediate working fluid stream 355 to form a condensed working fluid stream 359 .
the condensed working fluid stream 359 has a temperature in the range of from about 80 to about 150° F.
the condensed working fluid stream 359 is then directed to a pump 360 .
the pump 360 is a part of the organic Rankine cycle.
the pump 360 is controlled by a variable frequency drive 361 .
the pump 360 returns the condensed working fluid stream 359 to a higher pressure to produce the working fluid stream 336 that is directed to the heat exchanger 335 .
FIG. 4 shows an indirect heat recovery system 400 according to another exemplary embodiment.
the heat recovery system 400 is the same as that described above with regard to heat recovery system 300 , except as specifically stated below. For the sake of brevity, the similarities will not be repeated hereinbelow.
the intermediate working fluid stream 355 is directed to one or more water-cooled condensers 457 .
the water-cooled condensers 457 are a part of the organic Rankine cycle.
the organic Rankine cycle includes two water-cooled condensers 457 in series.
the water-cooled condensers 457 cool the intermediate working fluid stream 355 to form a condensed working fluid stream 459 .
the condensed working fluid stream 459 has a temperature in the range of from about 80 to about 150° F.
the condensed working fluid stream 459 is then directed to the pump 360 and is returned to a higher pressure to produce the working fluid stream 336 that is directed to the heat exchanger 335 .
a direct heat recovery system 500 for utilizing heat from a high temperature reactor such as a convection section of a fired heater 502
the high temperature reactor is an incinerator, hydrotreater, catalytic reformer, or isomerization unit.
the fired heater 502 is used in a refinery to heat a feedstock stream 503 going to a refinery unit. Suitable examples of refinery units include, but are not limited to, crude distillation units and vacuum distillation units.
a fuel stream 505 and an air stream 506 enter a burner section of the fired heater 502 and heat the feedstock stream 503 to produce a heated feedstock stream 507 .
the heat from the resulting flue gas stream 508 can then be used to heat a steam stream 509 to produce a saturated or superheated steam stream 510 and a flue gas stream 511 .
the flue gas stream 511 has a temperature in the range of from about 350 to about 800° F.
the flue gas stream 511 can then be utilized to heat a portion 512 a of a working fluid stream 512 .
the working fluid stream 512 includes any working fluid suitable for use in an organic Rankine cycle.
the flue gas stream 511 and the portion 512 a of the working fluid stream 512 enter a heater 513 to produce a heated working fluid stream 514 and a reduced heat flue gas stream 515 .
the flue gas stream 511 thermally contacts the working fluid stream 512 and transfers heat to the working fluid stream 512 .
the heater 513 is a part of the organic Rankine cycle, and can be integrated into the convection section of the fired heater 502 .
the portion 512 a of the working fluid stream 512 has a temperature in the range of from about 80 to about 150° F. In certain exemplary embodiments, the heated working fluid stream 514 has a temperature in the range of from about 160 to about 450° F. In certain exemplary embodiments, the heated working fluid stream 514 is vaporized. In certain exemplary embodiments, the heated working fluid stream 514 is vaporized within a supercritical process. In certain exemplary embodiments, the heated working fluid stream 514 is superheated. In certain exemplary embodiments, the reduced heat flue gas stream 515 has a temperature in the range of from about 300 to about 750° F. In certain embodiments, the reduced heat flue gas stream 515 has a temperature of about 300° F.
the reduced heat flue gas stream 515 can then be vented to the atmosphere.
a portion 512 b of the working fluid stream 512 is diverted through a bypass valve 517 and then combined with the heated working fluid stream 514 to produce a working fluid stream 518 .
the working fluid stream 518 has a temperature in the range of from about 155 to about 455° F.
the working fluid stream 512 is entirely directed through the heater 513 .
the intermediate working fluid stream 555 is then directed to one or more air-cooled condensers 557 .
the air-cooled condensers 557 are a part of the organic Rankine cycle.
the organic Rankine cycle includes two air-cooled condensers 557 in series.
each of the air-cooled condensers 557 is controlled by a variable frequency drive 558 .
the air-cooled condensers 557 cool the intermediate working fluid stream 555 to form a condensed working fluid stream 559 .
the condensed working fluid stream 559 has a temperature in the range of from about 80 to about 150° F.
the condensed working fluid stream 559 is then directed to a pump 560 .
the pump 560 is a part of the organic Rankine cycle.
the pump 560 is controlled by a variable frequency drive 561 .
the pump 560 returns the condensed working fluid stream 559 to a higher pressure to produce the working fluid stream 512 that is directed to the heater 513 .
FIG. 6 shows a direct heat recovery system 600 according to another exemplary embodiment.
the heat recovery system 600 is the same as that described above with regard to heat recovery system 500 , except as specifically stated below. For the sake of brevity, the similarities will not be repeated hereinbelow.
the intermediate working fluid stream 555 is then directed to one or more water-cooled condensers 657 .
the water-cooled condensers 657 are a part of the organic Rankine cycle.
the organic Rankine cycle includes two water-cooled condensers 657 in series. The water-cooled condensers 657 cool the intermediate working fluid stream 555 to form a condensed working fluid stream 659 .
the condensed working fluid stream 659 has a temperature in the range of from about 80 to about 150° F.
the condensed working fluid stream 659 is then directed to the pump 560 and is returned to a higher pressure to produce the working fluid stream 512 that is directed to the heater 513 .
FIG. 7 shows an indirect heat recovery system 700 for utilization of a flue gas stream 711 .
the flue gas stream 711 is the same as that described above with regard to flue gas stream 511 , and for the sake of brevity, the similarities will not be repeated hereinbelow.
the flue gas stream 711 is utilized to heat a working fluid stream 712 in a heater 713 .
the flue gas stream 711 thermally contacts the working fluid stream 712 and transfers heat to the working fluid stream 712 .
Suitable examples of the working fluid stream 712 include, but are not limited to, water, glycols, therminol fluids, alkanes, alkenes, chlorofluorocarbons, hydrofluorocarbons, carbon dioxide (CO2), refrigerants, and mixtures of other hydrocarbon components.
the flue gas stream 711 and the portion 712 a of the working fluid stream 712 enter the heater 713 to produce a heated working fluid stream 714 and a reduced heat flue gas stream 715 .
the heater 713 can be integrated into the convection section of a fired heater 702 .
the portion 712 a of the working fluid stream 712 has a temperature in the range of from about 85 to about 160° F.
the heated working fluid stream 714 has a temperature in the range of from about 165 to about 455° F.
the reduced heat flue gas stream 715 has a temperature in the range of from about 300 to about 750° F.
the reduced heat flue gas stream 715 can then be vented to the atmosphere.
a portion 712 b of the working fluid stream 712 is diverted through a bypass valve 717 and then combined with the heated working fluid stream 714 to produce a working fluid stream 718 .
the working fluid stream 718 has a temperature in the range of from about 165 to about 455° F.
the working fluid stream 712 is entirely directed through the heater 713 .
a portion 718 a of the working fluid stream 718 enters a heater 735 to heat a working fluid stream 736 to produce a heated working fluid stream 737 and a reduced heat working fluid stream 738 .
the portion 718 a of the working fluid stream 718 thermally contacts the working fluid stream 736 and transfers heat to the working fluid stream 736 .
the working fluid stream 736 includes any working fluid suitable for use in an organic Rankine cycle.
the working fluid stream 736 has a temperature in the range of from about 80 to about 150° F.
the heated working fluid stream 737 has a temperature in the range of from about 160 to about 450° F.
the heated working fluid stream 737 is vaporized. In certain exemplary embodiments, the heated working fluid stream 737 is vaporized within a supercritical process. In certain exemplary embodiments, the heated working fluid stream 737 is superheated. In certain exemplary embodiments, the reduced heat working fluid stream 738 has a temperature in the range of from about 85 to about 155° F. In certain embodiments, a portion 718 b of the working fluid stream 718 is diverted through a bypass valve 739 and then combined with the reduced heat working fluid stream 738 to produce an intermediate working fluid stream 740 . In certain exemplary embodiments, the intermediate working fluid stream 740 has a temperature in the range of from about 85 to about 160° F.
At least a portion 737 a of the heated working fluid stream 737 is then directed to a turbine-generator system 750 , which is a part of the organic Rankine cycle.
the portion 737 a of the heated working fluid stream 737 is expanded in the turbine-generator system 750 to produce an expanded working fluid stream 751 and generate power.
the expanded working fluid stream 751 has a temperature in the range of from about 80 to about 440° F.
the turbine-generator system 750 generates electricity or electrical power. In certain other embodiments, the turbine-generator system 750 generates mechanical power.
a portion 737 b of the heated working fluid stream 737 is diverted through a bypass valve 752 and then combined with the expanded working fluid stream 751 to produce an intermediate working fluid stream 755 .
the intermediate working fluid stream 755 has a temperature in the range of from about 80 to about 445° F.
the intermediate working fluid stream 755 is then directed to one or more air-cooled condensers 757 .
the air-cooled condensers 757 are a part of the organic Rankine cycle.
the organic Rankine cycle includes two air-cooled condensers 757 in series.
each of the air-cooled condensers 757 is controlled by a variable frequency drive 758 .
the air-cooled condensers 757 cool the intermediate working fluid stream 755 to form a condensed working fluid stream 759 .
the condensed working fluid stream 759 has a temperature in the range of from about 80 to about 150° F.
the condensed working fluid stream 759 is then directed to a pump 760 .
the pump 760 is a part of the organic Rankine cycle.
the pump 760 is controlled by a variable frequency drive 761 .
the pump 760 returns the condensed working fluid stream 759 to a higher pressure to produce the working fluid stream 736 that is directed to the heater 735 .
FIG. 8 shows an indirect heat recovery system 800 according to another exemplary embodiment.
the heat recovery system 800 is the same as that described above with regard to heat recovery system 700 , except as specifically stated below. For the sake of brevity, the similarities will not be repeated hereinbelow.
the intermediate working fluid stream 755 is directed to one or more water-cooled condensers 857 .
the water-cooled condensers 857 are a part of the organic Rankine cycle.
the organic Rankine cycle includes two water-cooled condensers 857 in series.
the water-cooled condensers 857 cool the intermediate working fluid stream 755 to form a condensed working fluid stream 859 .
the condensed working fluid stream 859 has a temperature in the range of from about 80 to about 150° F.
the condensed working fluid stream 859 is then directed to the pump 760 and is returned to a higher pressure to produce the working fluid stream 736 that is directed to the heater 735 .
a direct heat recovery system 900 for utilizing a waste heat by-product stream 901 from a steam generator 902 is shown.
the steam generator 902 is used wherever a source of steam is required.
a fuel stream 905 and an air stream 906 enter a burner section 902 a of the steam generator 902 and heat a water stream 903 to produce a steam stream 907 and the waste heat by-product stream 901 .
the waste heat by-product stream 901 has a temperature in the range of from about 400 to about 1000° F.
the waste heat by-product stream 901 is directed to a diverter valve 908 and can be separated into an exhaust stream 909 and a discharge stream 910 .
the discharge stream 910 can be directed to a bypass stack 911 and then discharged to the atmosphere.
a portion 909 a of the exhaust stream 909 can be utilized to heat a working fluid stream 912 .
the portion 909 a of the exhaust stream 909 thermally contacts the working fluid stream 912 and transfers heat to the working fluid stream 912 .
the working fluid stream 912 includes any working fluid suitable for use in an organic Rankine cycle.
the portion 909 a of the exhaust stream 909 and the working fluid stream 912 enter a heater 913 to produce a heated working fluid stream 914 and a reduced heat exhaust stream 915 .
the heater 913 is a part of the organic Rankine cycle.
the working fluid stream 912 has a temperature in the range of from about 80 to about 150° F.
the heated working fluid stream 914 has a temperature in the range of from about 160 to about 450° F.
the heated working fluid stream 914 is vaporized.
the heated working fluid stream 914 is vaporized within a supercritical process.
the heated working fluid stream 914 is superheated.
the reduced heat exhaust stream 915 has a temperature in the range of from about 300 to about 900° F.
the reduced heat exhaust stream 915 can then be directed to a primary stack 916 and discharged to the atmosphere.
the steam generator 902 and the heater 913 can be integrated into the primary stack 916 .
the reduced heat exhaust stream 915 can be directed to an incinerator or a scrubber prior to being discharged to the atmosphere.
a portion 909 b of the exhaust stream 909 is diverted through a bypass valve 917 and then combined with the reduced heat exhaust stream 915 to produce an exhaust stream 918 .
the exhaust stream 918 has a temperature in the range of from about 300 to about 905° F.
the exhaust stream 909 is entirely directed through the heater 913 .
At least a portion 914 a of the heated working fluid stream 914 is then directed to a turbine-generator system 950 where the portion 914 a of the heated working fluid stream 914 is expanded to produce an expanded working fluid stream 951 and generate power.
the expanded working fluid stream 951 has a temperature in the range of from about 80 to about 440° F.
a portion 914 b of the heated working fluid stream 914 is diverted through a bypass valve 952 and then combined with the expanded working fluid stream 951 to produce an intermediate working fluid stream 955 .
the intermediate working fluid stream 955 has a temperature in the range of from about 80 to about 445° F.
the intermediate working fluid stream 955 is then directed to one or more air-cooled condensers 957 .
the air-cooled condensers 957 are a part of the organic Rankine cycle.
the organic Rankine cycle includes two air-cooled condensers 957 in series.
each of the air-cooled condensers 957 is controlled by a variable frequency drive 958 .
the air-cooled condensers 957 cool the intermediate working fluid stream 955 to form a condensed working fluid stream 959 .
the condensed working fluid stream 959 has a temperature in the range of from about 80 to about 150° F.
the condensed working fluid stream 959 is then directed to a pump 960 .
the pump 960 is a part of the organic Rankine cycle.
the pump 960 is controlled by a variable frequency drive 961 .
the pump 960 returns the condensed working fluid stream 959 to a higher pressure to produce the working fluid stream 912 that is directed to the heater 913 .
FIG. 10 shows a direct heat recovery system 1000 according to another exemplary embodiment.
the heat recovery system 1000 is the same as that described above with regard to heat recovery system 900 , except as specifically stated below. For the sake of brevity, the similarities will not be repeated hereinbelow.
the intermediate working fluid stream 955 is then directed to one or more water-cooled condensers 1057 .
the water-cooled condensers 1057 are a part of the organic Rankine cycle.
the organic Rankine cycle includes two water-cooled condensers 1057 in series.
the water-cooled condensers 1057 cool the intermediate working fluid stream 955 to form a condensed working fluid stream 1059 .
FIG. 11 shows an indirect heat recovery system 1100 for utilization of an exhaust stream 1109 from a steam generator 1102 .
the exhaust stream 1109 is the same as that described above with regard to exhaust stream 909 , and for the sake of brevity, the similarities will not be repeated hereinbelow.
a portion 1109 a of the exhaust stream 1109 can be utilized to heat a working fluid stream 1112 .
the portion 1109 a of the exhaust stream 1109 thermally contacts the working fluid stream 1112 and transfers heat to the working fluid stream 1112 .
Suitable examples of the working fluid stream 1112 include, but are not limited to, water, glycols, therminol fluids, alkanes, alkenes, chlorofluorocarbons, hydrofluorocarbons, carbon dioxide (CO2), refrigerants, and mixtures of other hydrocarbon components.
the portion 1109 a of the exhaust stream 1109 and the working fluid stream 1112 enter a heater 1113 to produce a heated working fluid stream 1114 and a reduced heat exhaust stream 1115 .
the working fluid stream 1112 has a temperature in the range of from about 85 to about 160° F.
the heated working fluid stream 1114 has a temperature in the range of from about 165 to about 455° F.
the reduced heat exhaust stream 1115 has a temperature in the range of from about 300 to about 900° F.
the reduced heat exhaust stream 1115 can then be directed to a primary stack 1116 and discharged to the atmosphere.
the steam generator 1102 and the heater 1113 can be integrated into the primary stack 1116 .
the reduced heat exhaust stream 1115 can be directed to an incinerator or a scrubber prior to being discharged to the atmosphere.
a portion 1109 b of the exhaust stream 1109 is diverted through a bypass valve 1117 and then combined with the reduced heat exhaust stream 1115 to produce an exhaust stream 1118 .
the exhaust stream 1118 has a temperature in the range of from about 300 to about 905° F.
the exhaust stream 1109 is entirely directed through the heater 1113 .
At least a portion 1114 a of the heated working fluid stream 1114 enters a heater 1135 to heat a working fluid stream 1136 to produce a heated working fluid stream 1137 and a reduced heat working fluid stream 1138 .
the portion 1114 a of the heated working fluid stream 1114 thermally contacts the working fluid stream 1136 and transfers heat to the working fluid stream 1136 .
the working fluid stream 1136 includes any working fluid suitable for use in an organic Rankine cycle.
the working fluid stream 1136 has a temperature in the range of from about 80 to about 150° F.
the heated working fluid stream 1137 has a temperature in the range of from about 160 to about 450° F.
the heated working fluid stream 1137 is vaporized. In certain exemplary embodiments, the heated working fluid stream 1137 is vaporized within a supercritical process. In certain exemplary embodiments, the heated working fluid stream 1137 is superheated. In certain exemplary embodiments, the reduced heat working fluid stream 1138 has a temperature in the range of from about 85 to about 155° F. In certain embodiments, a portion 1114 b of the working fluid stream 1114 is diverted through a bypass valve 1139 and then combined with the reduced heat working fluid stream 1138 to produce an intermediate working fluid stream 1140 . In certain exemplary embodiments, the intermediate working fluid stream 1140 has a temperature in the range of from about 85 to about 160° F.
the intermediate working fluid stream 1140 is directed to a pump 1142 .
the pump 1142 is controlled by a variable frequency drive 1143 .
the pump 1142 returns the intermediate working fluid stream 1140 to produce the working fluid stream 1112 that enters the heater 1113 .
At least a portion 1137 a of the heated working fluid stream 1137 is then directed to a turbine-generator system 1150 , which is a part of the organic Rankine cycle.
the portion 1137 a of the heated working fluid stream 1137 is expanded in the turbine-generator system 1150 to produce an expanded working fluid stream 1151 and generate power.
the expanded working fluid stream 1151 has a temperature in the range of from about 80 to about 440° F.
the turbine-generator system 1150 generates electricity or electrical power. In certain other embodiments, the turbine-generator system 1150 generates mechanical power.
a portion 1137 b of the heated working fluid stream 1137 is diverted through a bypass valve 1152 and then combined with the expanded working fluid stream 1151 to produce an intermediate working fluid stream 1155 .
the intermediate working fluid stream 1155 has a temperature in the range of from about 80 to about 445° F.
the intermediate working fluid stream 1155 is then directed to one or more air-cooled condensers 1157 .
the air-cooled condensers 1157 are a part of the organic Rankine cycle.
the organic Rankine cycle includes two air-cooled condensers 1157 in series.
each of the air-cooled condensers 1157 is controlled by a variable frequency drive 1158 .
the air-cooled condensers 1157 cool the intermediate working fluid stream 1155 to form a condensed working fluid stream 1159 .
the condensed working fluid stream 1159 has a temperature in the range of from about 80 to about 150° F.
the condensed working fluid stream 1159 is then directed to a pump 1160 .
the pump 1160 is a part of the organic Rankine cycle.
the pump 1160 is controlled by a variable frequency drive 1161 .
the pump 1160 returns the condensed working fluid stream 1159 to a higher pressure to produce the working fluid stream 1136 that is directed to the heater 1135 .
FIG. 12 shows an indirect heat recovery system 1200 according to another exemplary embodiment.
the heat recovery system 1200 is the same as that described above with regard to heat recovery system 1100 , except as specifically stated below. For the sake of brevity, the similarities will not be repeated hereinbelow.
the intermediate working fluid stream 1155 is directed to one or more water-cooled condensers 1257 .
the water-cooled condensers 1257 are a part of the organic Rankine cycle.
the organic Rankine cycle includes two water-cooled condensers 1257 in series.
the water-cooled condensers 1257 cool the intermediate working fluid stream 1155 to form a condensed working fluid stream 1259 .
the condensed working fluid stream 1259 has a temperature in the range of from about 80 to about 150° F.
the condensed working fluid stream 1259 is then directed to the pump 1160 and is returned to a higher pressure to produce the working fluid stream 1136 that is directed to the heater 1135 .
a direct heat recovery system 1300 for utilizing a waste heat by-product stream 1301 from a gas turbine 1302 is shown.
the gas turbine is replaced with a diesel generator (not shown).
a fuel stream 1305 and an air stream 1306 enter the gas turbine 1302 and is combusted to produce energy and the waste heat by-product stream 1301 .
the waste heat by-product stream 1301 has a temperature in the range of from about 450 to about 1400° F.
the waste heat by-product stream 1301 is directed to a diverter valve 1308 and can be separated into an exhaust stream 1309 and a discharge stream 1310 .
the discharge stream 1310 can be directed to a bypass stack 1311 and then discharged to the atmosphere.
a portion 1309 a of the exhaust stream 1309 can be utilized to heat a working fluid stream 1312 .
the portion 1309 a of the exhaust stream 1309 thermally contacts the working fluid stream 1312 and transfers heat to the working fluid stream 1312 .
the working fluid stream 1312 includes any working fluid suitable for use in an organic Rankine cycle.
the portion 1309 a of the exhaust stream 1309 and the working fluid stream 1312 enter a heater 1313 to produce a heated working fluid stream 1314 and a reduced heat exhaust stream 1315 .
the heater 1313 is a part of the organic Rankine cycle.
the working fluid stream 1312 has a temperature in the range of from about 80 to about 150° F.
the heated working fluid stream 1314 has a temperature in the range of from about 160 to about 450° F.
the heated working fluid stream 1314 is vaporized.
the heated working fluid stream 1314 is vaporized within a supercritical process.
the heated working fluid stream 1314 is superheated.
the reduced heat exhaust stream 1315 has a temperature in the range of from about 250 to about 1000° F.
the reduced heat exhaust stream 1315 can then be directed to a primary stack 1316 and discharged to the atmosphere.
the reduced heat exhaust stream 1315 can be directed to an incinerator or a scrubber prior to being discharged to the atmosphere.
a portion 1309 b of the exhaust stream 1309 is diverted through a bypass valve 1317 and then combined with the reduced heat exhaust stream 1315 to produce an exhaust stream 1318 .
the exhaust stream 1318 has a temperature in the range of from about 250 to about 1100° F.
the exhaust stream 1309 is entirely directed through the heater 1313 .
At least a portion 1314 a of the heated working fluid stream 1314 is then directed to a turbine-generator system 1350 where the portion 1314 a of the heated working fluid stream 1314 is expanded to produce an expanded working fluid stream 1351 and generate power.
the expanded working fluid stream 1351 has a temperature in the range of from about 80 to about 440° F.
a portion 1314 b of the heated working fluid stream 1314 is diverted through a bypass valve 1352 and then combined with the expanded working fluid stream 1351 to produce an intermediate working fluid stream 1355 .
the intermediate working fluid stream 1355 has a temperature in the range of from about 80 to about 445° F.
the intermediate working fluid stream 1355 is then directed to one or more air-cooled condensers 1357 .
the air-cooled condensers 1357 are a part of the organic Rankine cycle.
the organic Rankine cycle includes two air-cooled condensers 1357 in series.
each of the air-cooled condensers 1357 is controlled by a variable frequency drive 1358 .
the air-cooled condensers 1357 cool the intermediate working fluid stream 1355 to form a condensed working fluid stream 1359 .
the condensed working fluid stream 1359 has a temperature in the range of from about 80 to about 150° F.
the condensed working fluid stream 1359 is then directed to a pump 1360 .
the pump 1360 is a part of the organic Rankine cycle.
the pump 1360 is controlled by a variable frequency drive 1361 .
the pump 1360 returns the condensed working fluid stream 1359 to a higher pressure to produce the working fluid stream 1312 that is directed to the heater 1313 .
FIG. 14 shows a direct heat recovery system 1400 according to another exemplary embodiment.
the heat recovery system 1400 is the same as that described above with regard to heat recovery system 1300 , except as specifically stated below. For the sake of brevity, the similarities will not be repeated hereinbelow.
the intermediate working fluid stream 1355 is then directed to one or more water-cooled condensers 1457 .
the water-cooled condensers 1457 are a part of the organic Rankine cycle.
the organic Rankine cycle includes two water-cooled condensers 1457 in series.
the water-cooled condensers 1457 cool the intermediate working fluid stream 1355 to form a condensed working fluid stream 1459 .
the condensed working fluid stream 1459 has a temperature in the range of from about 80 to about 150° F.
the condensed working fluid stream 1459 is then directed to the pump 1360 and is returned to a higher pressure to produce the working fluid stream 1312 that is directed to the heater 1313 .
FIG. 15 shows an indirect heat recovery system 1500 for utilization of an exhaust stream 1509 .
the exhaust stream 1509 is the same as that described above with regard to exhaust stream 1309 , and for the sake of brevity, the similarities will not be repeated hereinbelow.
a portion 1509 a of the exhaust stream 1509 can be utilized to heat a working fluid stream 1512 .
the portion 1509 a of the exhaust stream 1509 thermally contacts the working fluid stream 1512 and transfers heat to the working fluid stream 1512 .
Suitable examples of the working fluid stream 1512 include, but are not limited to, water, glycols, therminol fluids, alkanes, alkenes, chlorofluorocarbons, hydrofluorocarbons, carbon dioxide (CO2), refrigerants, and mixtures of other hydrocarbon components.
the portion 1509 a of the exhaust stream 1509 and the working fluid stream 1512 enter a heater 1513 to produce a heated working fluid stream 1514 and a reduced heat exhaust stream 1515 .
the working fluid stream 1512 has a temperature in the range of from about 85 to about 160° F.
the heated working fluid stream 1514 has a temperature in the range of from about 165 to about 455° F.
the reduced heat exhaust stream 1515 has a temperature in the range of from about 250 to about 1000° F.
the reduced heat exhaust stream 1515 can then be directed to a primary stack 1516 and discharged to the atmosphere.
the reduced heat exhaust stream 1515 can be directed to an incinerator or a scrubber prior to being discharged to the atmosphere.
a portion 1509 b of the exhaust stream 1509 is diverted through a bypass valve 1517 and then combined with the reduced heat exhaust stream 1515 to produce an exhaust stream 1518 .
the exhaust stream 1518 has a temperature in the range of from about 250 to about 1100° F.
the exhaust stream 1509 is entirely directed through the heater 1513 .
At least a portion 1514 a of the heated working fluid stream 1514 enters a heater 1535 to heat a working fluid stream 1536 to produce a heated working fluid stream 1537 and a reduced heat working fluid stream 1538 .
the portion 1514 a of the heated working fluid stream 1514 thermally contacts the working fluid stream 1536 and transfers heat to the working fluid stream 1536 .
the working fluid stream 1536 includes any working fluid suitable for use in an organic Rankine cycle.
the working fluid stream 1536 has a temperature in the range of from about 80 to about 150° F.
the heated working fluid stream 1537 has a temperature in the range of from about 160 to about 450° F.
the heated working fluid stream 1537 is vaporized. In certain exemplary embodiments, the heated working fluid stream 1537 is vaporized within a supercritical process. In certain exemplary embodiments, the heated working fluid stream 1537 is superheated. In certain exemplary embodiments, the reduced heat working fluid stream 1538 has a temperature in the range of from about 85 to about 155° F. In certain embodiments, a portion 1514 b of the working fluid stream 1514 is diverted through a bypass valve 1539 and then combined with the reduced heat working fluid stream 1538 to produce an intermediate working fluid stream 1540 . In certain exemplary embodiments, the intermediate working fluid stream 1540 has a temperature in the range of from about 85 to about 160° F.
the intermediate working fluid stream 1540 is directed to a pump 1542 .
the pump 1542 is controlled by a variable frequency drive 1543 .
the pump 1542 returns the intermediate working fluid stream 1540 to produce the working fluid stream 1512 that enters the heater 1513 .
At least a portion 1537 a of the heated working fluid stream 1537 is then directed to a turbine-generator system 1550 , which is a part of the organic Rankine cycle.
the portion 1537 a of the heated working fluid stream 1537 is expanded in the turbine-generator system 1550 to produce an expanded working fluid stream 1551 and generate power.
the expanded working fluid stream 1551 has a temperature in the range of from about 80 to about 440° F.
the turbine-generator system 1550 generates electricity or electrical power. In certain other embodiments, the turbine-generator system 1550 generates mechanical power.
a portion 1537 b of the heated working fluid stream 1537 is diverted through a bypass valve 1552 and then combined with the expanded working fluid stream 1551 to produce an intermediate working fluid stream 1555 .
the intermediate working fluid stream 1555 has a temperature in the range of from about 80 to about 445° F.
the intermediate working fluid stream 1555 is then directed to one or more air-cooled condensers 1557 .
the air-cooled condensers 1557 are a part of the organic Rankine cycle.
the organic Rankine cycle includes two air-cooled condensers 1557 in series.
each of the air-cooled condensers 1557 is controlled by a variable frequency drive 1558 .
the air-cooled condensers 1557 cool the intermediate working fluid stream 1555 to form a condensed working fluid stream 1559 .
the condensed working fluid stream 1559 has a temperature in the range of from about 80 to about 150° F.
the condensed working fluid stream 1559 is then directed to a pump 1560 .
the pump 1560 is a part of the organic Rankine cycle.
the pump 1560 is controlled by a variable frequency drive 1561 .
the pump 1560 returns the condensed working fluid stream 1559 to a higher pressure to produce the working fluid stream 1536 that is directed to the heater 1535 .
FIG. 16 shows an indirect heat recovery system 1600 according to another exemplary embodiment.
the heat recovery system 1600 is the same as that described above with regard to heat recovery system 1500 , except as specifically stated below. For the sake of brevity, the similarities will not be repeated hereinbelow.
the intermediate working fluid stream 1555 is directed to one or more water-cooled condensers 1657 .
the water-cooled condensers 1657 are a part of the organic Rankine cycle.
the organic Rankine cycle includes two water-cooled condensers 1657 in series.
the water-cooled condensers 1657 cool the intermediate working fluid stream 1555 to form a condensed working fluid stream 1659 .
the condensed working fluid stream 1659 has a temperature in the range of from about 80 to about 150° F.
the condensed working fluid stream 1659 is then directed to the pump 1560 and is returned to a higher pressure to produce the working fluid stream 1536 that is directed to the heater 1535 .
a direct heat recovery system 1700 for utilizing a heat by-product stream 1701 from a process column 1702 is shown.
Suitable examples of process columns include, but are not limited to, distillation columns and strippers.
the heat by-product stream 1701 has a temperature in the range of from about 170 to about 700° F.
a portion 1701 a of the heat by-product stream 1701 can be utilized to heat a working fluid stream 1712 .
the portion 1701 a of the heat by-product stream 1701 thermally contacts the working fluid stream 1712 and transfers heat to the working fluid stream 1712 .
the working fluid stream 1712 includes any working fluid suitable for use in an organic Rankine cycle.
the portion 1701 a of the heat by-product stream 1701 and the working fluid stream 1712 enter a heater 1713 to produce a heated working fluid stream 1714 and a reduced heat exhaust stream 1715 .
the heater 1713 is a part of the organic Rankine cycle.
the working fluid stream 1712 has a temperature in the range of from about 80 to about 150° F.
the heated working fluid stream 1714 has a temperature in the range of from about 160 to about 450° F.
the heated working fluid stream 1714 is vaporized.
the heated working fluid stream 1714 is vaporized within a supercritical process.
the heated working fluid stream 1714 is superheated.
the reduced heat exhaust stream 1715 has a temperature in the range of from about 90 to about 500° F.
the reduced heat exhaust stream 1715 can then be vented to the atmosphere.
a portion 1701 b of the heat by-product stream 1701 is diverted through a bypass valve 1717 and then combined with the reduced heat exhaust stream 1715 to produce an exhaust stream 1718 .
the exhaust stream 1718 has a temperature in the range of from about 90 to about 510° F.
the heat by-product stream 1701 is entirely directed through the heater 1713 .
At least a portion 1714 a of the heated working fluid stream 1714 is then directed to a turbine-generator system 1750 where the portion 1714 a of the heated working fluid stream 1714 is expanded to produce an expanded working fluid stream 1751 and generate power.
the expanded working fluid stream 1751 has a temperature in the range of from about 80 to about 440° F.
a portion 1714 b of the heated working fluid stream 1714 is diverted through a bypass valve 1752 and then combined with the expanded working fluid stream 1751 to produce an intermediate working fluid stream 1755 .
the intermediate working fluid stream 1755 has a temperature in the range of from about 80 to about 455° F.
the intermediate working fluid stream 1755 is then directed to one or more air-cooled condensers 1757 .
the air-cooled condensers 1757 are a part of the organic Rankine cycle.
the organic Rankine cycle includes two air-cooled condensers 1757 in series.
each of the air-cooled condensers 1757 is controlled by a variable frequency drive 1758 .
the air-cooled condensers 1757 cool the intermediate working fluid stream 1755 to form a condensed working fluid stream 1759 .
the condensed working fluid stream 1759 has a temperature in the range of from about 80 to about 150° F.
the condensed working fluid stream 1759 is then directed to a pump 1760 .
the pump 1760 is a part of the organic Rankine cycle.
the pump 1760 is controlled by a variable frequency drive 1761 .
the pump 1760 returns the condensed working fluid stream 1759 to a higher pressure to produce the working fluid stream 1712 that is directed to the heater 1713 .
FIG. 18 shows a direct heat recovery system 1800 according to another exemplary embodiment.
the heat recovery system 1800 is the same as that described above with regard to heat recovery system 1700 , except as specifically stated below. For the sake of brevity, the similarities will not be repeated hereinbelow.
the intermediate working fluid stream 1755 is then directed to one or more water-cooled condensers 1857 .
the water-cooled condensers 1857 are a part of the organic Rankine cycle.
the organic Rankine cycle includes two water-cooled condensers 1857 in series.
the water-cooled condensers 1857 cool the intermediate working fluid stream 1755 to form a condensed working fluid stream 1859 .
the condensed working fluid stream 1859 has a temperature in the range of from about 80 to about 150° F.
the condensed working fluid stream 1859 is then directed to the pump 1760 and is returned to a higher pressure to produce the working fluid stream 1712 that is directed to the heater 1713 .
FIG. 19 shows an indirect heat recovery system 1900 for utilization of heat by-product stream 1901 .
the heat by-product stream 1901 is the same as that described above with regard to heat by-product stream 1701 , and for the sake of brevity, the similarities will not be repeated hereinbelow.
a portion 1901 a of the heat by-product stream 1901 can be utilized to heat a working fluid stream 1912 .
the portion 1901 a of the heat by-product stream 1901 thermally contacts the working fluid stream 1912 and transfers heat to the working fluid stream 1912 .
Suitable examples of the working fluid stream 1912 include, but are not limited to, water, glycols, therminol fluids, alkanes, alkenes, chlorofluorocarbons, hydrofluorocarbons, carbon dioxide (CO2), refrigerants, and mixtures of other hydrocarbon components.
the portion 1901 a of the heat by-product stream 1901 and the working fluid stream 1912 enter a heater 1913 to produce a heated working fluid stream 1914 and a reduced heat exhaust stream 1915 .
the working fluid stream 1912 has a temperature in the range of from about 85 to about 160° F.
the heated working fluid stream 1914 has a temperature in the range of from about 165 to about 455° F.
the reduced heat exhaust stream 1915 has a temperature in the range of from about 90 to about 500° F.
the reduced heat exhaust stream 1915 can then be vented to the atmosphere.
a portion 1901 b of the heat by-product stream 1901 is diverted through a bypass valve 1917 and then combined with the reduced heat exhaust stream 1915 to produce an exhaust stream 1918 .
the exhaust stream 1918 has a temperature in the range of from about 90 to about 510° F.
the heat by-product stream 1901 is entirely directed through the heater 1913 .
At least a portion 1914 a of the heated working fluid stream 1914 enters a heater 1935 to heat a working fluid stream 1936 to produce a heated working fluid stream 1937 and a reduced heat working fluid stream 1938 .
the portion 1914 a of the heated working fluid stream 1914 thermally contacts the working fluid stream 1936 and transfers heat to the working fluid stream 1936 .
the working fluid stream 1936 includes any working fluid suitable for use in an organic Rankine cycle.
the working fluid stream 1936 has a temperature in the range of from about 80 to about 150° F.
the heated working fluid stream 1937 has a temperature in the range of from about 160 to about 450° F.
the heated working fluid stream 1937 is vaporized.
the heated working fluid stream 1937 is vaporized within a supercritical process. In certain exemplary embodiments, the heated working fluid stream 1937 is superheated. In certain exemplary embodiments, the reduced heat working fluid stream 1938 has a temperature in the range of from about 85 to about 155° F. In certain embodiments, a portion 1914 b of the working fluid stream 1914 is diverted through a bypass valve 1939 and then combined with the reduced heat working fluid stream 1938 to produce an intermediate working fluid stream 1940 . In certain exemplary embodiments, the intermediate working fluid stream 1940 has a temperature in the range of from about 85 to about 160° F. The intermediate working fluid stream 1940 is directed to a pump 1942 . In certain exemplary embodiments, the pump 1942 is controlled by a variable frequency drive 1943 . The pump 1942 returns the intermediate working fluid stream 1940 to produce the working fluid stream 1912 that enters the heater 1913 .
At least a portion 1937 a of the heated working fluid stream 1937 is then directed to a turbine-generator system 1950 , which is a part of the organic Rankine cycle.
the portion 1937 a of the heated working fluid stream 1937 is expanded in the turbine-generator system 1950 to produce an expanded working fluid stream 1951 and generate power.
the expanded working fluid stream 1951 has a temperature in the range of from about 80 to about 440° F.
the turbine-generator system 1950 generates electricity or electrical power. In certain other embodiments, the turbine-generator system 1950 generates mechanical power.
a portion 1937 b of the heated working fluid stream 1937 is diverted through a bypass valve 1952 and then combined with the expanded working fluid stream 1951 to produce an intermediate working fluid stream 1955 .
the intermediate working fluid stream 1955 has a temperature in the range of from about 80 to about 445° F.
the intermediate working fluid stream 1955 is then directed to one or more air-cooled condensers 1957 .
the air-cooled condensers 1957 are a part of the organic Rankine cycle.
the organic Rankine cycle includes two air-cooled condensers 1957 in series.
each of the air-cooled condensers 1957 is controlled by a variable frequency drive 1958 .
the air-cooled condensers 1957 cool the intermediate working fluid stream 1955 to form a condensed working fluid stream 1959 .
the condensed working fluid stream 1959 has a temperature in the range of from about 80 to about 150° F.
the condensed working fluid stream 1959 is then directed to a pump 1960 .
the pump 1960 is a part of the organic Rankine cycle.
the pump 1960 is controlled by a variable frequency drive 1961 .
the pump 1960 returns the condensed working fluid stream 1959 to a higher pressure to produce the working fluid stream 1936 that is directed to the heater 1935 .
FIG. 20 shows an indirect heat recovery system 2000 according to another exemplary embodiment.
the heat recovery system 2000 is the same as that described above with regard to heat recovery system 1900 , except as specifically stated below. For the sake of brevity, the similarities will not be repeated hereinbelow.
the intermediate working fluid stream 1955 is directed to one or more water-cooled condensers 2057 .
the water-cooled condensers 2057 are a part of the organic Rankine cycle.
the organic Rankine cycle includes two water-cooled condensers 2057 in series.
the water-cooled condensers 2057 cool the intermediate working fluid stream 1955 to form a condensed working fluid stream 2059 .
the condensed working fluid stream 2059 has a temperature in the range of from about 80 to about 150° F.
the condensed working fluid stream 2059 is then directed to the pump 1960 and is returned to a higher pressure to produce the working fluid stream 1936 that is directed to the heater 1935 .
the present invention may employ any number of working fluids in the organic Rankine cycle.
working fluids for use in the organic Rankine cycle include, but are not limited to, ammonia (NH3), bromine (Br2), carbon tetrachloride (CCl4), ethyl alcohol or ethanol (CH3CH2OH, C2H60), furan (C4H40), hexafluorobenzene or perfluoro-benzene (C6F6), hydrazine (N2H4), methyl alcohol or methanol (CH3OH), monochlorobenzene or chlorobenzene or chlorobenzol or benzine chloride (C6H5C1), n-pentane or normal pentane (nC5), i-hexane or isohexane (iC5), pyridene or azabenzene (C5H5N), refrigerant 11 or freon 11 or CFC-11 or R-11 or t
the working fluid may include a combination of components.
one or more of the compounds identified above may be combined or with a hydrocarbon fluid, for example, isobutene.
a hydrocarbon fluid for example, isobutene.
the present invention is not limited to any particular type of working fluid or refrigerant. Thus, the present invention should not be considered as limited to any particular working fluid unless such limitations are clearly set forth in the appended claims.
the present application is generally directed to various heat recovery systems and methods for producing electrical and/or mechanical power from a heat source.
the exemplary systems may include a heat exchanger, a turbine-generator set, a condenser heat exchanger, and a pump.
the present invention is advantageous over conventional heat recovery systems and methods as it utilizes heat that would otherwise be rejected to the atmosphere to produce electricity and/or mechanical power, thus increasing process efficiency

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Engineering & Computer Science (AREA)
Mechanical Engineering (AREA)
General Engineering & Computer Science (AREA)
Chemical & Material Sciences (AREA)
Combustion & Propulsion (AREA)
Physics & Mathematics (AREA)
Thermal Sciences (AREA)
Engine Equipment That Uses Special Cycles (AREA)

US13/267,635 2010-10-06 2011-10-06 Utilization of process heat by-product Abandoned US20120085095A1 (en)

Priority Applications (1)

Application Number	Priority Date	Filing Date	Title
US13/267,635 US20120085095A1 (en)	2010-10-06	2011-10-06	Utilization of process heat by-product

Applications Claiming Priority (2)

Application Number	Priority Date	Filing Date	Title
US39039710P	2010-10-06	2010-10-06
US13/267,635 US20120085095A1 (en)	2010-10-06	2011-10-06	Utilization of process heat by-product

Publications (1)

Publication Number	Publication Date
US20120085095A1 true US20120085095A1 (en)	2012-04-12

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ID=45924039

Family Applications (2)

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US13/267,635 Abandoned US20120085095A1 (en)	2010-10-06	2011-10-06	Utilization of process heat by-product
US13/267,595 Abandoned US20120085097A1 (en)	2010-10-06	2011-10-06	Utilization of process heat by-product

Family Applications After (1)

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US13/267,595 Abandoned US20120085097A1 (en)	2010-10-06	2011-10-06	Utilization of process heat by-product

Country Status (7)

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US (2)	US20120085095A1 (fr)
KR (2)	KR20130099959A (fr)
AU (2)	AU2011311963A1 (fr)
CA (2)	CA2812796A1 (fr)
SG (2)	SG189003A1 (fr)
WO (2)	WO2012048132A2 (fr)
ZA (1)	ZA201301931B (fr)

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Also Published As

Publication number	Publication date
ZA201301931B (en)	2014-05-28
AU2011311963A1 (en)	2013-03-14
CA2813420A1 (fr)	2012-04-12
WO2012048132A3 (fr)	2012-07-19
SG189003A1 (en)	2013-05-31
CA2812796A1 (fr)	2012-04-12
WO2012048132A2 (fr)	2012-04-12
US20120085097A1 (en)	2012-04-12
WO2012048135A2 (fr)	2012-04-12
SG188593A1 (en)	2013-04-30
AU2011311966A1 (en)	2013-02-28
KR20140000219A (ko)	2014-01-02
WO2012048135A3 (fr)	2012-07-19
KR20130099959A (ko)	2013-09-06

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