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WO2010129298A2 - Centrale hydrothermique - Google Patents

Centrale hydrothermique Download PDF

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Publication number
WO2010129298A2
WO2010129298A2 PCT/US2010/032608 US2010032608W WO2010129298A2 WO 2010129298 A2 WO2010129298 A2 WO 2010129298A2 US 2010032608 W US2010032608 W US 2010032608W WO 2010129298 A2 WO2010129298 A2 WO 2010129298A2
Authority
WO
WIPO (PCT)
Prior art keywords
expander
brine
scwor
compressor
exhaust
Prior art date
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.)
Ceased
Application number
PCT/US2010/032608
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English (en)
Other versions
WO2010129298A3 (fr
Inventor
Thomas G. Mcguinness
Gary Carr
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.)
Individual
Original Assignee
Individual
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.)
Filing date
Publication date
Application filed by Individual filed Critical Individual
Priority to US13/266,451 priority Critical patent/US20120042653A1/en
Publication of WO2010129298A2 publication Critical patent/WO2010129298A2/fr
Publication of WO2010129298A3 publication Critical patent/WO2010129298A3/fr
Anticipated expiration legal-status Critical
Ceased 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
    • F01K23/06—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 combustion heat from one cycle heating the fluid in another cycle
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J3/00—Processes of utilising sub-atmospheric or super-atmospheric pressure to effect chemical or physical change of matter; Apparatus therefor
    • B01J3/008—Processes carried out under supercritical conditions
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E20/00—Combustion technologies with mitigation potential
    • Y02E20/14—Combined heat and power generation [CHP]

Definitions

  • the present invention relates to an improved means of electric power generation via the oxidation of various organic materials in a Supercritical
  • SCWOR Water Oxidation Reactor
  • SCWOR have an inherent utility as the most of efficient means to completely oxidize organic waste of all types, including toxic chemical, as well as wet biomass, such as sludge.
  • an SCWOR can also use conventional fuels without creating harmful by-products, other than CO2, the conventional fuels need not be heavily refined and can even be contaminated with water, organic and organo- inter-metallic and metallic compounds.
  • Bio fuels in particular ethanol, has gained popularity as an automotive gasoline additive in the US, as well as a direct fuel in other countries.
  • AS ethanol is generally produced from corn or such cane, a significant non- fermentable biomass is created in these processes. These biomasses are sometimes burnt as fuel, but being somewhat wet, are an inefficient and particulate polluting heat source.
  • the first object is achieved by providing a power generating plant that comprises a super critical water oxidation reactor (SCWOR) having a feed port for reactants and an exit port for exhaust, a brine separator having an inlet for receiving the exhaust of the SCWOR and at least one outlet for gases, two or more pairs of air compressors and expanders coupled in rotary motion by a common axle, at least one heat exchanger associated with each of said one or more pairs of compressors and expanders, wherein the hot exhaust gas exiting the brine separator enters a first expander, and the cooled exhaust gas exiting the first expander enters a first heat exchanger that cools hot compressed air from the air compressor while reheating the cooled exhaust gas exiting the first expander prior to a second stage of expansion, and the cooled air exiting the heat exchanger enters a downstream compressor stage in said 2 or more pairs of air compressor and expanders, a motor or motor/generator with a rotary coupling to at least one common drive mechanism of the
  • SCWOR super critical water
  • FIG. 1 is a schematic diagram the generically discloses the operative principles of the HTPP in a first embodiment.
  • FIG. 2 is a schematic diagram of the power generation system in the HTPP of FIG. 1.
  • FIG. 3 is a schematic diagram of a second embodiment of the HTPP.
  • FIG. 4 is a schematic diagram of a third embodiment of the HTPP.
  • FIG. 5 is a schematic diagram of a fourth embodiment of the HTPP.
  • FIG. 6 is a schematic diagram of a firth embodiment of the HTPP.
  • HTPP Hydro-Thermal Power Plant
  • FIG. 1 illustrates a HTPP 100 that comprises a super critical water oxidation reactor (SCWOR) 110.
  • SCWOR super critical water oxidation reactor
  • the organic materials that enter the SCWOR 110 are oxidized, as are described for example in US Pat. No. 5,558,783 issued to McGuinness on Sep.24, 1996) and 5,384,051 (issued to McGuinness on Jan.
  • SCWOR 100 preferably incorporates a permeable- wall or transpiring wall 115.
  • the SCWOR 110 may be operated at pressures above or below the critical pressure or water.
  • an important aspect of the current invention is the extracts of heat from the hot liquid recirculation stream of the brine. This is more both a more efficient way to extract heat from gases as proposed in US Pat. no. 5,485,728 issued to Norman L. Dickinson on Jan. 23, 1996 for "EFFICIENT UTILIZATION OF CHLORINEAND MOISTURE- CONTAINING FUELS" and US Pat. no. 5,000,099 (which is a continuation in part of a series of patents to Dickinson), but also enables other routes for heat and energy recovery that would otherwise be lost in a prior art system.
  • Waste water treatment facility (WWTF) sludge
  • WWTF Waste water treatment facility
  • many high moisture renewable fuel sources and non-renewable fuel sources such as coal may be used to generate power in the inventive HTPP 100.
  • Wastewater sludge will preferably be taken off the bottom of the existing WWTF gravity thickeners at approx 3% biosolids (BS) concentration.
  • the sludge can be ground as necessary to improve pumpability, and then pumped at low pressure to the HTPP 100.
  • the sludge is preferably centrifuged to approx 10% biosolids concentration. Filtrate water from the centrifuge is sent back to the WWTF headworks.
  • the concentrated sludge is then pumped to combustor pressure via pump 260.
  • SCWOR 110 which is preferably a hydrothermal transpiring-wall combustor (such as are disclosed in US Pat. No. 5,558,783 and 5,384,051) where it is turbulently combined with a preheated mixture of superheated steam and compressed air.
  • the combustor will normally operate at subcritical pressures (below the critical pressure of water), but may also be designed to operate above the critical pressure of water. Spontaneous oxidation of the sludge occurs upon mixing within the combustor.
  • Superheated reaction products (CO 2 , N 2 , excess O 2 , water vapor and inorganic residuals) exit the bottom of the combustor and enter the quench cooler 120
  • the quench cooler 120 partially cools the stream, thereby forming a saturated
  • This 2-phase stream then enters a gravity separator 130 for separation into liquid and vapor streams.
  • This gravity separator 130 operates below the local saturation temperature of water and will contain what will be referred to as a brine, as it contains some dissolved inorganic slats.
  • the hot liquid phase or brine leaves the bottom of the separator 130 via line 1300 carrying with it all of the suspended and dissolved inorganic constituents of the sludge.
  • the stream in line 1300 passes through a steam generator 270, such as a shell & tube heat exchanger for example, before being recycled back to the quench cooler 120 via pump 121.
  • the steam generator 270 is thus designed to extract useful heat from the liquid brine recirculation loop 1300.
  • the brine circulation quench pump 121 supports the continued flow of brine in loop 1300.
  • Inorganic solids are continuously removed from this stream via hydrocyclone filtration at filter 500, and then removed from the system via blowdown for solids dewatering and disposal at 505.
  • a hydrocyclone 500 is optionally replaced with a filter or other means known in the art to separate and remove free solids from the liquid in brine recirculation loop 1300 .
  • “Blowdown” refers to a liquid stream leaving the process for disposal. This stream would contain any separated solids from the hydrocyclone or filter, but might only contain dissolved solids to control the total amount of dissolved solids in the brine recirculation loop. This technique is routinely used in steam boilers to prevent total dissolved solids from reaching saturation and precipitating out on the walls of the equipment as scale. Blowdown water containing the dissolved solids is directed back to the WWTF headworks. Blowdown is a small percentage of the total flow through the recirculation loop.
  • the hot vapor mixture of CO 2 , N 2 , O 2 and water vapor exits the 2-phase separator 130 and enters a condenser 220, where the water vapor is condensed and separated from the non-condensable gases.
  • the condensed water output from condenser 220 at port 242 is generally free of inorganics and organics; it is essentially distilled water but may require additional polishing. Such excess condensed water is drained from the process and returned to the WWTF, such as at moisture condenser 240, via outlet 242.
  • the remaining condensed water is heated and vaporized for mixing with the compressor air (from compressor 3317) via valve 1403 prior to injection into the combustor.
  • a portion of this condensed water is optionally recycled back to the combustor or SCWOR 110 (via circulation pump 107) for liner transpiration via liner 115 at inlet port 1406 (where it is delivered outside the permeable-wall or transpiring wall 115.)
  • the water before returning to the either the injector 1405 or the side port 1406 is preferably reheated by injector trim heaters 1401.
  • two 3 -way flow control valves 1402 and 1403 are provided for dividing the total flow of compressed air and transpiration water to separate destinations. Such flow control valves might use multiple 2-way valves instead of a single 3 -way valve to achieve same end.
  • Flow control valve 1402 divides liquid transpiration water into two streams. One stream going to the boiler to be vaporized for use in transpiration service and the balance going to the boiler to be vaporized for use in injection/mixing service with the feed.
  • Flow control valve 1403 divides the compressed air into two streams. The other stream going to the reactor annulus at port 1406 for use in transpiration service and the balance going to the feed injector 1405 for injection/mixing with the feed from pump 265.
  • the injector trim heaters 1401 are also useful in reactor start-up and control.
  • the non-condensable gases are used to generate power in generation train 3000 by being fed to one or more gas expanders wherein they drive a rotary mechanism.
  • each of the air compressor stages 3317 are coupled in rotary motion to one or more gas expansion stages 3315 by a common drive mechanism 160.
  • One or more of such coupled compressor-expander pairs or stages are arranged in a train of two or more pairs to achieve higher overall compression ratio and expansion ratio than possible with pair.
  • Two or more compressor and expander stages may be coupled in rotary motion at different rotational speeds by means of a common gearbox, as done in integrally-geared compressors known in the art.
  • the cooperative operation of the other stages of train 3000 is shown in more detail in FIG. 2.
  • the non-condensable gases leaving the condenser 240 are heated in a pre -heater 3318 by heat from the hot brine recirculation loop 1450 and then reduced to atmospheric pressure via a multi-stage hot gas expander cascade train 3000.
  • Each stage of the expander cascade drives one of the compressor stages. Should it be desired to recover carbon dioxide from this stream of non-condensable gases, it would best be done upstream of the high-pressure expander preheater at unit 245, wherein the carbon dioxide by removal is represent by the exciting arrow 246.
  • the power train 3000 preferably deploys 3 or 4 stages of compression with intercooling, while the expansion likewise requires 3 or 4 stages of expansion with interstage reheat.
  • FIG. 2 illustrates a preferred aspect of the invention with three separate expander-compressor pairs 3100, 3200 and 3300 cascaded in series.
  • heat from each compressor intercooler is used to heat and expand the noncondensable gases upstream of each interstage reheater. This reduces the total preheat required upstream of each stage of expansion, providing more efficient product of energy from the biomass. This allows each expander-compressor train to operate more closely to its optimum speed for maximum efficiency.
  • At least 2 of the 3 coupled expander - compressor pairs 3100, 3200 and 3300 have at least one associated heat exchanger 3110 and 3210 (for 3100 and 3200 respectively) that receives the compressor output as a heat source and to increase the enthalpy of the exhaust of the preceding expander in the chain.
  • the output gas from the first compressor 3117 is fed to the next compressor 3217 in pair 3200, and the output of compressor 3217 is feed to the next compressor 3317.
  • An intercooler such as 3110 for compressor - expander pair 3100 cools the gas before the next stage of compression.
  • intercooler receives the cooler exit gas from each expander as the heat transfer fluid such that heat or enthalpy in the gas from compression is transferred to the gas before the next stage of expansion.
  • the input to the last expander 3115 in coupled compressor- expander pair 3100 is heated first by the output of compressor 3117 via air compressor intercooler 3110 that acts as a heat exchanger.
  • the input of the second expander 3215 in coupled pair 3200 is heated first by the output of compressor 3217 via air compressor intercooler 3210 that acts as a heat exchanger.
  • each of expanders 3150, 3250, and 3350 are thus associated with a heat exchangers 3118, 3218 and 3318 respectively that receives either the re-circulating brine, or a heat transfer fluid heated therefrom, as a heat source and further increase the enthalpy of the exhaust of the preceding expander.
  • the final low-pressure expander-compressor pair 3100 is connected to a motor/generator 3001.
  • motor operation is generally required drive the air compressors.
  • the low-pressure expander will gradually supply power to the compressor and eventually produce enough power to generate surplus electric power to the grid.
  • the intermediate-pressure and high-pressure expander-compressor trains 3300 and 3200 may or may not have a connected motor/generator 3002 and 3003 respectively.
  • FIG. 3-6 another aspect of the invention is the steam generator 270 located in the hot brine recirculation loop 1300 generates steam supplying a conventional steam turbine system 300 for additional power recovery.
  • the steam turbine 314 may drive a dedicated electric generator 312, or may be connected to the low pressure expander-compressor-motor/generator train via a conventional overrunning clutch, these alternative coupling means being designated 1450 in FIG. 5-6.
  • the effluent from the steam powered turbine 314 then enter the steam condenser 311, which has a water cooling inlet 313.
  • the steam turbine re-circulation pump 106 is used to return the output of the moisture separator 240 to the heat exchanger 220 that pre-cool that mixture entering the moisture condenser 240, while a second recirculation pump 105 return the water exiting this heat exchanger 220 to the steam generator 270.
  • the total net power produced by the HTPP 100 is roughly evenly split between the expander-compressor cascade 3000 and the steam turbine system
  • an optional steam superheater 400 is disposed at least partially within the SCWOR 110 to further improve the efficiency of the steam turbine system 300.
  • FIG. 5 and FIG. 6 there is a mode of operation whereby a condenser 240 need not be disposed in the vapor outlet from the brine separator 130 to directly inject the hot vapor mixture into the expander- compressor.
  • a condenser 240 need not be disposed in the vapor outlet from the brine separator 130 to directly inject the hot vapor mixture into the expander- compressor.
  • FIG. 5 and FIG. 6 illustrate the optional bypass line 5001 having valves valve around the condenser, which allows HTPP operation without the condenser in the loop.
  • the reason for condensing and cooling the hot vapor exhaust stream is to cool the gas to facilitate removal of CO 2 from the high-pressure exhaust gas stream, which is most easily done cool.
  • a dashed line 166 is intended to illustrate the optional gear box or clutch coupling between the generators
  • the oxidizer to the SCWOR 1000 may be air, oxygen enriched air, or oxygen.
  • Air separation technology may optionally be installed upstream of the SCWOR 110 to separate air into oxygen-rich and nitrogen-rich streams.
  • the nitrogen-rich stream may optionally be used to drive a gas expander as part of the power generation train 3000.
  • Such oxidizer may or may not be mixed with the transpiration water entering at portal 1401.
  • the motor 3003 might be required for start-up, but then once the system is up to pressure and temperature, the compressor is driven solely by the expander. We will endeavor to start the system up without using motors on the higher pressure expander-compressors.
  • a clutch coupling 3116 and 3216 typically an overrunning clutch, such that when the expander-compressor comes up to speed it automatically disengages from the motor 3003 allowing the motor to be switched off.
  • Such clutches are commonly employed in industry.
  • a hydrodynamic centrifugal or axial type compressor is shown in the diagram, for smaller plants a reciprocating compressor as known in the art may also be similarly employed in which all stages are driven via a common drive mechanism and motor/generator.
  • a reciprocating or axial gas expanders are shown in the diagram, for smaller flows a reciprocating or other positive displacement type expansion engine may also be similarly employed whereby all stages of expansion may be connected via a common drive mechanism.
  • the air compressor stages may be driven independently from the gas expander stages.
  • Gas expander stages are capable of generating mechanical power to directly drive electric generators, air compressors, pumps, chillers or any other type of driven equipment.

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  • Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Combustion & Propulsion (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Physical Or Chemical Processes And Apparatus (AREA)
  • Engine Equipment That Uses Special Cycles (AREA)

Abstract

L'invention porte sur un réacteur à oxydation super critique de l'eau (SCWOR), servant de source d'énergie extrêmement efficace dans une centrale, par couplage des différents courants de sortie en communication thermique avec des compresseurs-détendeurs à plusieurs étages ou en cascade, qui eux-mêmes sont mécaniquement couplés à un moteur ou à une génératrice. Dans une forme de réalisation, la chaleur provenant d'une boucle de saumure liquide en recirculation préchauffe directement ou indirectement les effluents gazeux du SCWOR avant la détente. Dans une autre forme de réalisation, la chaleur de compression est utilisée pour préchauffer l'effluent d'un détendeur avant l'étage ultérieur de détente. La boucle de saumure en recirculation va également de préférence préchauffer l'effluent du détendeur avant un étage ultérieur de détente.
PCT/US2010/032608 2009-04-28 2010-04-27 Centrale hydrothermique Ceased WO2010129298A2 (fr)

Priority Applications (1)

Application Number Priority Date Filing Date Title
US13/266,451 US20120042653A1 (en) 2009-04-28 2010-04-27 Hydrothermal Power Plant

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
US17349809P 2009-04-28 2009-04-28
US61/173,498 2009-04-28

Publications (2)

Publication Number Publication Date
WO2010129298A2 true WO2010129298A2 (fr) 2010-11-11
WO2010129298A3 WO2010129298A3 (fr) 2011-03-03

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PCT/US2010/032608 Ceased WO2010129298A2 (fr) 2009-04-28 2010-04-27 Centrale hydrothermique

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WO (1) WO2010129298A2 (fr)

Families Citing this family (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20140166263A1 (en) * 2012-12-17 2014-06-19 Conocophillips Company Brine based indirect steam boiler
CN106242019A (zh) * 2016-09-14 2016-12-21 西安热工研究院有限公司 超临界二氧化碳布雷顿循环发电‑废水处理的耦合系统
EP3330499B1 (fr) * 2016-12-05 2023-08-23 Orcan Energy AG Système et procédé de récupération d'énergie dans des installations industrielles
CN107935287A (zh) * 2017-12-08 2018-04-20 陕西科技大学 一种超临界水氧化能量回收系统
CA3141768A1 (fr) * 2019-06-28 2020-12-30 Battelle Memorial Institute Destruction de pfas par l'intermediaire d'un procede d'oxydation et appareil approprie pour le transport vers des sites contamines
US11738314B2 (en) * 2020-03-05 2023-08-29 Sreus Energy, Llc Conversion of supercritical water energy into electrical power
CN111894689B (zh) * 2020-08-06 2021-07-09 西安交通大学 一种基于超临界水氧化的热-电-清洁水联产系统

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US5147564A (en) * 1991-08-22 1992-09-15 Titmas And Associates Incorporated Method for recovering energy from a wet oxidation products stream flow using rotational energy
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Publication number Publication date
US20120042653A1 (en) 2012-02-23
WO2010129298A3 (fr) 2011-03-03

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