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US20120042653A1 - Hydrothermal Power Plant - Google Patents

Hydrothermal Power Plant Download PDF

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Publication number
US20120042653A1
US20120042653A1 US13/266,451 US201013266451A US2012042653A1 US 20120042653 A1 US20120042653 A1 US 20120042653A1 US 201013266451 A US201013266451 A US 201013266451A US 2012042653 A1 US2012042653 A1 US 2012042653A1
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Prior art keywords
expander
brine
fluid
gas
scwor
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Abandoned
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US13/266,451
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English (en)
Inventor
Thomas G. McGuinness
Cary Carr
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TURBOSYSTEMS ENGR Inc
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TURBOSYSTEMS ENGR Inc
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Priority to US13/266,451 priority Critical patent/US20120042653A1/en
Publication of US20120042653A1 publication Critical patent/US20120042653A1/en
Abandoned legal-status Critical Current

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    • 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 Water Oxidation Reactor (SCWOR).
  • SCWOR Supercritical 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.
  • Biofuels 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.
  • It is still another object of the invention to provide such a plant is capable of accept multiple and diverse fuel sources for the recovery of useful energy with high thermal efficiency.
  • 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 air compressor-ex
  • 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 fifth embodiment of the HTPP.
  • FIG. 7 is a schematic diagram of a sixth embodiment of the HTPP.
  • FIG. 8 is a schematic diagram of a seventh embodiment of the HTPP.
  • FIG. 9 is a schematic cross-sectional elevation view of a gravity separator for use with any of the above embodiments.
  • 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 U.S. Pat. Nos. 5,558,783 (issued to McGuinness on Sep. 24, 1996) and 5,384,051 (issued to McGuinness on Jan. 24, 1995), which are incorporated herein by reference.
  • This oxidation reaction generates heat that is used to generate electrical power in the HTTP 100 as described further below.
  • the 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.
  • various combinations of biomass and organic materials are co-injected with water or in an aqueous suspended state into the top of the SCWOR 110 at the injector 1405 .
  • Hot exhaust and reaction products from the SCWOR 110 are controllably cooled in the quench cooler 120 by direct mixing with cooled re-circulated brine that circulates in line 1300 from the bottom of the gravity separator 130 .
  • Gravity separator then received this cooled reaction product from the quench cooler 120 via inlet portal 131 .
  • the gravity separator 130 receives the output of the SCWOR 100 after passing through the quench cooling section 120 .
  • an important aspect of the current invention is the extraction of heat from the hot liquid recirculation stream of the brine in line 1300 .
  • This is both a more efficient way to extract and more effectively deploy heat from gases as proposed in U.S. Pat. No. 5,485,728 (which issued to Norman L. Dickinson on Jan. 23, 1996 for “EFFICIENT UTILIZATION OF CHLORINE AND MOISTURE-CONTAINING FUELS”) and U.S. Pat. No. 5,000,099 (which is a continuation in part of a series of patents to Dickinson), and also enables other routes for heat and energy recovery that would otherwise be lost in a prior art system.
  • Other important and alternative aspects of the invention are described further below.
  • Waste water 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 U.S. Pat. Nos. 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 2-phase vapor-liquid mixture.
  • This 2-phase stream then enters a gravity or brine 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 brine, as it contains some dissolved inorganic salts.
  • the hot liquid phase or brine leaves the bottom of the separator 130 at a lower exit portal 132 and then enters the line forming loop 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 the stream of loop 1300 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.
  • the blowdown water containing the dissolved solids is then directed back to the WWTF headworks. This 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 gravity separator 130 at exit portal 133 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 SCWOR combustor 110 .
  • 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 one or more 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. One stream goes 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.
  • Such expanders are generally, but not exclusively turbine devices.
  • 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 .
  • the exact nature of the drive mechanism will depend on the structure and type of the expander and compressor, which although both are preferably turbine devices, as other types of compressors known in the art can be deployed in the embodiments described herein.
  • 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 non-condensable gases upstream of each interstage reheater. This reduces the total preheat required upstream of each stage of expansion, providing more efficient production of energy from the biomass feed. 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. However, the 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 , which 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 heat exchangers 3118 , 3218 and 3318 which respectively receive either the re-circulating brine, or a heat transfer fluid heated there from, as a heat source to 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.
  • another aspect of the invention is the steam generator 270 located in the hot brine recirculation loop 1300 , which 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 are 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 steam condenser 311 to the heat exchanger 220 that pre-cool that mixture entering the moisture condenser 240 , while a second recirculation pump 105 returns 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 300 .
  • Overall HTPP thermal efficiency is approximately 38% based on higher heating value of the wet feed.
  • the present invention will always incorporate a Brayton power generation cycle it may or may not include an optional Rankine (steam) co-generation cycle.
  • 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 .
  • the superheater 400 acts as a heat exchanger that heats the output of the steam generator 270 before it reaches the steam turbine 314 .
  • a condenser 240 does 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 around the condenser 240 , 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.
  • Water treatment systems as known in the art to control corrosion and fouling of process equipment.
  • a dashed line 166 is intended to illustrate the optional gear box or clutch coupling between the generators 3001 and 312 , or a common shaft to a single generator.
  • 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 or oxygen enriched stream may or may not be mixed with the transpiration water entering at portal 1406 .
  • additional motors 3002 and 3003 may or may not be required at all depending on the application.
  • 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. It is preferable to start the system up without using motors on the higher pressure expander-compressors.
  • a clutch coupling 3116 and 3216 typically an overrunning clutch, is deployed 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.
  • FIG. 7 illustrates yet another embodiment of the invention in which the fluid phase the output of the gravity or brine separator 130 is directed from the bottom thereof at portal 132 through level control valve 706 causing a pressure drop with expansion device or flash drum 701 .
  • the flash drum 701 generates steam and condensed water having some dissolved or suspended solids.
  • output gas of the SCWOR 110 also exits the gravity separator 130 at the upper portal 133 , and is directed in line 710 toward a system pressure control valve 705 . Line 710 then directs this gas to the input port 3712 of the first or higher pressure expander 3710 , which is mechanically coupled to a second or lower pressure expander 3720 .
  • the low pressure output gas exiting portal 733 of the flash drum 701 is feed to the input port 3722 of the second or lower pressure expander 3720 via line 720 .
  • the lower pressure expander 3720 can also receives at inlet port 3722 the output from exit portal 3711 of the higher pressure expander 3710 , which is mixed into line 720 .
  • the rotary mechanical coupling from the expanders 3710 and 3720 drives generator 3710 to produce electric power or other useful energy. It should be appreciated that this embodiment does not require to expanders, as the gas output of either the gravity separator or flash drum can drive a single expander, with the gas output of the other device being used to power an unrelated expander, such as for example in the other embodiments of the invention.
  • Liquid output from the bottom of the flash drum 701 will contain a mixture of suspended and dissolved solids.
  • This liquid stream is preferably separated in brine loop 1300 ′ by hydrocyclone filtration at filter 500 , within recirculation or return to loop 1300 ′.
  • the liquid effluent from the solid separator or filter 500 thus returns to the quench cooler 120 , via a brine circulation pump 121 .
  • the hot brine may be used in heat exchanger 7401 to pre-heat the feed from pump 260 before it reaches the main heater 265 .
  • loop 1300 ′ returns water back to the gravity separator 130 , preferably by mixing in quench cooler 120 with the direct effluent from SCWOR 110 .
  • the output of the SCWOR 110 can be cooled by other means than the quench cooler, with the same effect of the output thereof entering the gravity separator.
  • the output of the gravity circulator can return thereto via the brine circulation loop 1300 or 1300 ′, without the need to enter an equivalent cooling means.
  • Water from the gas streams or steam that drives the expanders can also be returned in a re-pressurized state to the SCWOR 110 as in other embodiments.
  • the low pressure side output at portal 3721 of the low pressure expander 3720 is directed to a moisture condenser 7240 .
  • the condensate there from is stored in a condensate recovery tank 7241 . Liquid condensate is drawn from the bottom of this tank and optionally feed by a pump 261 back to the injector 1405 or between the transpiring wall and inner chamber wall of the SCWOR 110 , but preferably after being re-heated and re-pressurized via the high pressure heaters 707 and 708 respectively.
  • the output of a second feed air compressor 702 which is driven by motor 703 , is directed toward valve 1407 and 709 to pressurize and drive the water or steam generated by heaters 707 and 708 .
  • the output of fluid from heater 707 is controlled by valve 709 to direct water to the SCWOR chamber or reactor annulus at port 1406 for use in transpiration service.
  • the output of fluid from heater 708 is controlled by valve 1407 to direct water to the feed injector 1405 for injection/mixing with the feed from pump 265 .
  • Make up water is optionally fed to the condensate separator or recovery tank 7241 via port 7012 .
  • the condensate separator or recovery tank 7241 externally vents non combustible exhaust gases at line 7301 .
  • an optional steam superheater 400 is disposed at least partially within the SCWOR 110 to further improve the efficiency of the generation of electric power at generator 3730 , by pre-heating the gas output of the gravity or brine separator 130 in line 710 before or after it reach pressure control valve 705 .
  • the output of the gravity brine separator 130 travels via line 411 , and returning to feed the expander 3710 via line 412 .
  • the superheater 400 can receive and pre-heat gas exiting the flash drum 701 that travels in line 720 , as shown by broken lines at 411 and 412 .
  • FIG. 9 illustrates a common and representative structure for a gravity separator 130 .
  • the gravity separator 130 has an inlet port 131 for receiving effluent, such as from the quench cooler 120 of the SCWOR 110 .
  • the influent hits deflection plate 134 which directs liquid downward toward the bottom, where upon prompt gravity separation it can exit via portal 132 .
  • Mist and vapor that expands upward in the separator 130 reaches a mist removal device or water vapor coalesce means 135 situated below the upper vapor exit portal 133 .
  • the mist removal device 135 is optionally a mist mat, vane pack, hydrocyclone and the like, so that liquid from the mist is collected and flows downward, and the vapor phase exits at portal 133 .
  • U.S. Pat. No. 7,654,397 (issued to Allouche on Feb. 2, 201), which is incorporated herein by reference, also discloses the construction of a particular type of gravity separator that separates a liquid phase and a gas

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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
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
CN111894689A (zh) * 2020-08-06 2020-11-06 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
US20210276888A1 (en) * 2020-03-05 2021-09-09 John Troy Kraczek Conversion of supercritical water energy into electrical power
US11274629B2 (en) * 2016-12-05 2022-03-15 Orean Energy AG System and method for energy recovery in industrial faciliiies
US20230227336A1 (en) * 2019-06-28 2023-07-20 Battelle Memorial Institute Destruction of PFAS Via an Oxidation Process and Apparatus Suitable for Transportation to Contaminated Sites

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