METHOD AND APPARATUS FOR TREATING SALT STREAMS

Abstract: A method for avoiding the precipitation of salts from a salt containing water stream prior to the stream reaching a supercritical water reactor is presented. The salt containing water stream is preferably kept at temperatures below supercritical conditions as the stream is transferred to the reactor. After the salt stream reaches the reactor the temperature of the salt stream is preferably raised to the appropriate temperature by mixing the salt stream, within the reactor, with a second stream that has been heated above the supercritical temperature of water. Alternatively, a method for preventing the clogging of the conduits upstream from the reactor may involve the mixing of two subcritical waste streams. One stream may include salts, the other preferably includes oxidizable material. The heat produced by the reaction of the oxidizable materials within the reactor preferably allows the mixture to remain at supercritical conditions for a time sufficient to oxidize substantially all of the oxidizable material.

Description: TITLE: METHOD AND APPARATUS FOR TREATING SALT STREAMS BACKGROUND OF THE INVENTION 1 Field of the Invention This invention generally relates to the inhibition of plugging in supercritical water reaction systems More particularly, the invention relates to the inhibition of pluggmg m components upstream from a supercntical water reactor 2 Descnption of the Related Art Mateπals that are reacted m supercritical waste oxidization ("SCWO") systems typically operate at relatively high pressures and high temperatures (e g , at least about 700 °F and 3200 psia (about 370 °C and 220 bar)) Other systems may operate in the vicinity of supercritical conditions for water (1 e , at least about 500 °F and about 2000 psia (about 260 °C and 138 bar) Inorganic salts tend to have a low solubility within supercritical water At a constant pressure, the solubility of salts typically mcreases as the temperature of the water mcreases As the temperature approaches within about 10 °F (about 5 °C) of the supercritical temperature of water, the solubility of inorganic salts tends to drop to low values Concurrently, the solubility of organic compounds, normally relatively insoluble in water, increases This increase in solubility tends to assist the oxidation of the organic compounds Oxidizable matter that is reacted or oxidized m SCWO systems may cause solids or char to form withm the reactor due to the low insolubility of the oxidation products within supercntical water Alternately, the streams themselves (especially hazardous waste streams) may contain salts or solids, which tend to be insoluble at supercritical conditions The presence of salts or solids m the reaction zone of the reactor tends to cause problems For instance, if significant amounts of salts or solids are generated, the salts or solids may either partially or fully plug the reactor, thereby reducmg reactor efficiency and/or causing expensive reactor shut downs for maintenance purposes Given the particularly high temperatures and pressures at which these systems operate, the replacement and/or mamtenance of equipment in such systems tends to be expensive Therefore, plugging in these systems tends to be a particularly difficult problem to address The plugging problem may be accentuated if additives are mixed with the stream to be treated For instance, additives may be mixed with a given stream to raise or lower its pH (e g , for the purpose of reducing corrosion) or to neutralize corrosive elements m the stream These additives, or compounds produced from the additives, may in turn cause pluggmg in the system By way of example, if a stream has a low pH, a piactitioner may wish to add sodium hydroxide (NaOH) to the stream to raise the pH If the-waste stream contains chlonnated compounds oxidation of these compounds will typically produce hydrochloric acid (HCl) To inhibit the corrosion due to HCl, as well as other acidic compounds, NaOH is typically added to neutralize these acidic products The reaction of NaOH with HCl typically produces the salt sodium chlonde (NaCl) The formed salt may cause plugging of the reactor Thus the additives available to control stream pH, and/or system corrosion, have necessanly been limited by practical considerations related to system pluggmg Dunng at least one treatment procedure water is heated to supercritical conditions before entering the reactor, typically before oxidants are added. For salt containmg waste streams, the nse to supercritical conditions may cause precipitation to occur prior to reachmg the reactor Thus pluggmg of the system may occur within the heater and conduits upstream from the reactor. While a number of reactor designs are known to prevent pluggmg of the waste stream withm the reactor, little has been done to prevent pluggmg in the heater or conduits leadmg to the reactor. It is therefore desirable to devise a method and system for preventing the precipitation of salts withm the system upstream from the reactor due to the rise to supercntical conditions. Such a method may-help prevent the plugging of the system. Conventional reactor assemblies operating m the vicinity of supercritical conditions for water are described in detail in the following patents or patent applications: U.S. Patent No. 5,403,533 to Hazlebeck et al., U.S. Patent No 4,141,829 to Thiel et al., U.S. Patent No. 4,292,953 to Dickinson, U.S. Patent No. 4,338,199 to Modell, U S. Patent No. 4,377,066 to Dickmson, U.S Patent No. 4,380,960 to Dickinson, U.S. Patent No. 4,543,190 to Modell, U.S. Patent No. 4,564,458 to Burleson. U.S. Patent No. 4,593,202 to Dickinson, U.S. Patent No 4,594.164 to Titmas, U.S. Patent No. 4,792,408 to Titmas, U.S. Patent No. 4,822,394 to Zeigler et al, U.S Patent No 4,822,497 to Hong et al , U.S Patent No. 4,861,497 to Welch et al., U.S. Patent No. 4,891,139 to Zeigler et al., U S. Patent No 4, 113,446 to Modell et al, U.S. Patent No. 5,106,513 to Hong, U.S. Patent No. 4,898,107 to Dickmson, U.S. Patent No 4,983,296 to McMahon et al., U.S. Patent No. 5,011,614 to Gresser et al, U.S. Patent No. 5,053,142 to Sorensen et al, U.S. Patent No. 5,057,231 to Mueller et al, U.S Patent No 5,133,877 to Rofer et al, U.S. Patent No. 5,183,577 to Lehmann, U.S. Patent No. 5,192,453 to Keckler et al , U.S. Patent No. 5,221,486 to Fassbender, U.S. Patent No. 5,232,604 to Swallow et al, U.S. Patent No. 5,232,605 to Baur et al, U.S. Patent No. 5,240,619 to Copa et al, U.S. Patent No. 5,250,193 to Sawicki et al , U.S. Patent No 5,252,224 to Modell et al, U.S. Patent No. 4,822,497 to Hong et al, U.S. Patent No. 5,551 ,472 to McBrayer et al, U.S. patent application senal no. 08/399,703 to McBrayer et al, U.S. Patent No. 5,620,606 to McBrayer et al, U.S. Patent No 5,582,715 to McBrayer et al, U.S. patent No. 5,591,415 to McBrayer et al , U S Patent No 5,552,039 to McBrayer et al, and U.S. patent application serial no. 08/254,956 to Eller et al, U S. patent application serial no. 08/657,899 to McBrayer et al. The above-referenced patents and patent applications are hereby incoφorated by reference. SUMMARY OF THE INVENTION A method for avoidmg the precipitation of salts from a salt containing solution prior to the solution reaching the reactor is presented. A first waste stream, which includes a salt and oxidizable matter, is preferably introduced into a supercritical water oxidation system. The first stream is preferably conducted to a first pump. The first pump preferably bnngs the first stream to a pressure in the vicinity of supercritical conditions for water (i.e., at least about 2000 psia (about 138 bar)), more preferably to a pressure above about 3200 psia (about 220 bar). After pressuπzation, the first stream is preferably conducted through a heat exchanger The first stream is preferably heated by passage through the heat exchanger to a temperature and pressure such that the salts in the first stream remain substantially soluble in the first stream The temperature of the first stream is preferably maintained below about 700 °F (about 370 °C) The first stream is preferably maintained at a pressure of at least about 3200 psia (about 220 bar) At temperatures above about 700 °F (about 370 °C), the solubility of the salts m the first stream may become lower If the concentration of salts in the first stream is greater than the solubility limit of the heated first stream, a portion of the salts may precipitate out of the first stream These precipitates may cause plugging of the system components After passing through a heat exchanger the first stream is preferably conducted to a supercntical water reactor A second stream is preferably introduced mto the system The second stream is preferably a water stream which is substantially free of salts The second stream may include water only Preferably, the second stream is a water stream which includes oxidizable material The oxidizable material preferably mcludes organic compounds The second stream is preferably passed to a second pump The second pump preferably bnngs the second stream to a pressure in the vicinity of supercritical conditions for water The stream is preferably brought to a pressure above about 3200 psia (about 220 bar) After pressurizing the second stream, the second stream is preferably conducted through a heat exchanger The heat exchanger is preferably used to pre-heat the second stream After passing through the heat exchanger, the second stream is transferred to a heater The heater preferably heats the second stream to a temperature greater than about 700 °F (about 370 °C) Preferably, the second stream is heated to a temperature such that, when the second stream is mixed with the first stream, the resultmg mixture has a temperature that is above about 700 °F (about 370 °C)) After the second stream is pressunzed and heated, the second stream is preferably conducted to a mixer An oxidant from an oxidant feeder may be added to the second stream as it passes to or through the mixer, or after it passes through the mixer The oxidant may be any source of oxygen Liquid oxygen, hydrogen peroxide, air. and or mixtures thereof are prefened Preferably, the amount of oxidant added is sufficient to oxidize substantially all of the contaminates within the first and second streams After addition of the oxidant, the second stream is preferably transfened to the supercritical water reactor The second stream is preferably introduced mto the reactor inlet and passes through the reactor, and then exits out of the reactor outlet In one embodiment, the first stream, which mcludes a mixture of water, salt and oxidizable matenals, is preferably mixed with the second stream pnor to entenng the reactor The first stream may be mixed with the second stream before the oxidant is added to the second stream Alternatively, the first stream may be mixed with the second stream after the oxidant has been added to the second stream, pnor to the second stream reaching the reactor In another embodiment, the first stream may be added to the second stream as the second stream is passed through the reactor A plurality of injection ports downstream from the reactor mlet may be used to mtroduce the first stream mto the reactor Preferably, a first portion of the first stream is mixed with the second stream pnor to the reactor inlet A second portion of the first stream may also be injected into the leactor as the second stream passes through the reactor The mixture of the first and second stream preferably forms a mixed stream. The temperature of the mixed stream is preferably determined by the temperature of both the first and second streams, as well as the flow rates of the two streams. Preferably, the temperature and flow rate of the second stream are predetermined such that the peak temperature of the mixed stream within the reactor is preferably substantially greater than the supercritical temperature of water (e.g., greater than about 700 °F (about 370 °C)), more preferably greater than about 1000 °F (about 540 °C), more preferably still between about 1000 °F to 1200 °F (about 540 °C to 650 °C). As the mixed stream passes through the reactor, the oxidizable material is preferably oxidized. Substantially complete oxidation of all of the oxidizable materials may, in some instances, occur if the mixed stream is preferably maintained at a temperature above the supercritical temperature of water (i.e., above about 700 °F (about 370 °C)) as the mixed stream passes through the reactor. When the first and second streams are mixed together, a mixed stream having a temperature that is at least about 700 °F (about 370 °C) is preferably formed. At temperatures above about 700 °F (about 370 °C), the salts dissolved within the mixed stream may precipitate out of the mixed stream. These salts may become redissolved within the mixed stream as the mixed stream cools to temperatures below the supercritical temperature of water (e.g., during passage of the mixed stream through a heat exchanger). In another embodiment, the precipitated salts may be removed from the mixed stream by a separator. The separator is preferably configured to substantially separate the salt particles from the mixed stream. After passing through the reactor, the mixed stream is preferably conducted to the heat exchanger. The heat exchanger preferably allows the mixed stream from the reactor to pass through in such a way that the heat from the mixed stream will preheat the first and or second streams passing through the heat exchanger. The mixed stream may then be transferred to a cooler. The cooler preferably lowers the temperature and pressure of the mixed stream to subcritical conditions. Gases and condensed water are preferably transferred from the system via the cooler. Cooling of the mixed stream in either the heat exchanger or the cooler may cause any precipitated salts to become redissolved within the mixed stream. An automatic controller may be used to monitor the system and alter the reaction conditions. The controller may adjust the flow rate of the first and/or second streams such that the oxidizable materials are treated within the reactor for a sufficient time to allow the oxidizable material to be substantially oxidized. The controller may also adjust the flow rates of the first and/or second streams to maintain a specified temperature within the reactor. For example, the controller may adjust the flow rate of the first and/or second streams to control the peak reactor temperature. Additionally, the controller may adjust the amount of oxidant added to the second stream prior to, in or after the mixer. In another embodiment, a method for preventing the clogging of the conduits upstream from the reactor may involve the mixing of two subcritical streams. A first stream (e.g., a waste stream) which includes a salt and oxidizable matter is preferably introduced into the system. The first stream is preferably conducted to a first pump. The first pump preferably brings the first stream to a pressure above about 3200 psia (about 220 bar). After pressurization, the first stream is preferably conducted through a heat exchanger. The first stream is preferably heated by passage through a heat exchanger and/or a heater to a temperature such that the salts in the first stream remain substantially soluble in the first stream The temperature of the first stream is preferably mamtamed below about 700 °F (about 370 °C) The first stream is preferably maintained at a pressure of at least about 3200 psia (about 220 bar) A second stream is preferably introduced into the system Preferably, the second stream is a water stream which mcludes oxidizable material The second stream may also include salts The second stream preferably contams a sufficient amount of oxidizable material such that, when mixed with the first stream, the amount of oxidizable matenal present in the mixed stream is sufficient to obtain supercntical conditions as a result of reaction ofthe oxidizable material The second stream is preferably passed to a second pump The second pump preferably brings the second stream to a pressure in the vicinity of supercritical conditions for water The stream is preferably biought to a pressure above about 3200 psia (about 220 bar) After pressurizing the second stream, the second stream is preferably conducted through a heat exchanger The second stream is preferably heated by passage through a heat exchanger and/or a heater to a temperature such that the salts in the second stream remain substantially soluble in the second stream The temperatuie of the second stream is preferably maintained below about 700 °F (about 370 °C) The second stream is preferably mamtamed at a pressure of at least about 3200 psia (about 220 bar) After the first and second streams are pressurized and heated, either the first stream, the second stream, or both streams are preferably conducted to a mixer, where an oxidant from an oxidant feeder may be added to the stream Preferably, the amount of oxidant added is sufficient to oxidize substantially all of the contaminates withm the first stream and the second stream The first stream is preferably introduced into the reactor at the reactor mlet The first stream preferably passes through the reactor, exitmg out of the reactor through the reactor outlet As the first stream is passed through the reactor, the second stream is preferably injected mto the reactor Preferablv, the second stream is injected into the reactor at a position downstream from the reactor mlet As the second stream is injected mto the reactor, a mixed stream is preferably formed The mixed stieam preferably includes a mixture of the first stream and the second stream The oxidizable matenal content of the mixed stream may be dependent on the concentration of oxidizable material in the first and second streams Preferably, the second stream contams a sufficient amount of oxidizable material such that, when the second stream is combmed with the first stream, a mixed stream is formed that mcludes greater than about 5 to 7% by volume of oxidizable material Preferably, the mixed stream includes greater than about 6% by volume ot oxidizable matenal When the mixed stream is conducted through the reactor, the oxidizable material is preferably reacted to form oxidation products The reaction of the oxidizable matenals within the reactor may cause the temperature ofthe mixed stream to rise Preferably, the oxidation ofthe oxidizable material causes the temperature ofthe mixed stream to rise above about 700 °F (about 370 °C) Since the mixed stream is preferably at a pressure above about 3200 psia (about 220 bar), the increase in temperature may create supercritical conditions withm the reactor After the oxidation of the oxidizable materials has begun, the temperature ofthe mixed stream may rise above about 700 °F (about 370 °C) At temperatures above about 700 °F (about 370 °C), the salts dissolved within the mixed stream may precipitate out of the mixed stream These salts are preferably conducted out of the reactor along with the mixed stream The mixed stream and the precipitated salts are preferably conducted trom the reactor into a separator After separation ofthe salts from the mixed stream, the stream is preferably conducted to a cooler An automatic controller may be used to monitor the system and alter the reaction conditions BRIEF DESCRIPTION OF THE DRAWINGS Fig 1 depicts a block diagram illustrating a reactor assembly for the mixing of a hot waste stream with a cooler waste stream, Fig 2 depicts a block diagram illustrating a reactor assembly for the mixing of a waste stream containing oxidizable material with a salt containing waste stream, DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENTS The critical point of a solvent is the temperature and pressure above which the solvent cannot be liquefied by increasing the pressure When heated above its cntical temperature, water attains a supercntical state in which the density of water drops to about 0 15 to 0 2 grams/cm 3 As used in this patent, the term "supercntical water" is taken to mean water which is in this supercritical state Supercritical water tends to have significantly different solubility properties than subcntical water As used in this patent, the term "subcritical water" is taken to mean water at a temperature and pressure below the critical point Organic substances, which are normally substantially insoluble within subcntical water, tend to become highly soluble within supercritical water Alternatively, inorganic substances, which are typically soluble withm subcntical water, tend to become substantially insoluble withm supercritical water As used m this patent, the term "supercritical conditions for water" is taken to mean a temperature higher than about 700 °F (about 370 °C) and a pressure higher than about 3200 psia (about 220 bar) As used in this patent, the term "vicinity of supercntical conditions for water" is taken to mean temperatures from about 550 °F to 1200 °F (about 288 °C to 650 °C) and pressures from about 2000 psia to 5000 psia (about 138 bar to 345 bar) As used in this patent, the term "subcntical conditions for water" is taken to mean temperatures below about 700 °F (about 370 °C) and pressures below about 3200 psia (about 220 bar) The insolubility of inorganic materials withm supercntical water tends to present problems for reactors operating on water hav g a high salt content (e g , sea water) Under typical processmg conditions, the contaminated water is typically heated to supercntical conditions before entering the reactor Typically, as the salt containing solution approaches within about 10 °F (about 5 °C) ofthe cntical point of water, the solubility ot the dissolved salts drops to very low levels It appears that the salts dissolved withm the water tend to precipitate out when the water is heated near to supercritical conditions This precipitation may cause the formation of salt deposits withm the heater and the conduits leading to the reactor Eventually, the reactor may become clogged and require servicing Water containing halogenated organic materials, such as chloroform, methylene chlonde, dichloroethylene and others, and/or sulfur containmg compounds, can also present similar problems During the processmg of solutions containing halogenated and or sulfur containing compounds, pH adjustmg additives (e g , NaOH or NaHC0 3 ) may be added to the solutions to neutralize the acidic products produced withm the reactor These additives are typically added before the solution is introduced into the reactor The preheating of the water which includes halogenated solvents and/or sulfur containing compounds and additives may cause precipitation ofthe additives This precipitation may cause cloggmg within the heater and the conduits leading to the reactor An embodiment of a method for avoiding the precipitation of salts from a salt containing stream pnor to the stream reachmg a reactor mvolves keepmg the salt containing water stream at temperatures below supercritical conditions as the salt stream is transferred to the reactor After the salt stream reaches the reactor, the temperature ofthe salt stream is preferably raised to the appropnate temperature by mixmg the salt stream, withm the reactor, with a second stream that has been heated above the supercntical temperature of water The temperature of the second stream is preferably high enough such that the mixing of the second stream with the salt stream produces a mixture having a temperature above the supercritical temperature of water (I e , above about 700 °F (about 370 °C)) Withm the reactor, the inorganic salts may precipitate out, however, this is a well known problem that is readily controlled through the use of various reactor designs known in the art Referring to the system 100, depicted m Fig 1, an embodiment of a method for the destruction of contaminants in salt streams is described in more detail A first stream (e g , a waste stream, a process stream, a sea water stream, etc ) which includes a salt and oxidizable matter is preferably introduced mto the system via conduit 112 Examples of oxidizable matter may include various organic compounds dissolved or suspended in the water, as well as inorganic compounds An example of a salt stream is sea water contaminated with organic compounds In another embodiment, supply source 110 may contain an inorganic salt for neutralizing oxidation products Dunng the reaction of halogenated or sulfur containing organic compounds within a supercntical water reactor, the organic compounds are oxidized to produce acidic products These acidic products tend to corrode the components ofthe system if not neutralized Typically, a basic salt (e g , NaOH or NaHC0 3 ) may be added to the contaminated stream, preferably prior to the reaction of the organic compounds, to neutralize the acidic oxidation products formed A first stream which mcludes oxidizable material may be introduced mto the system via conduit 112 As the first stream is introduced mto the system, a neutralizing salt from salt supply source 110 may be added to form a salt containing first waste stream The first stream, made of a mixture of oxidizable matenal and salt, is preferably conducted through conduit 112 to first pump 122 First pump 122 preferably bnngs the first stream to a pressure in the vicinity of supercritical conditions for water A positive displacement pump is preferably used to pressurize the first stream A positive displacement pump is commercially available from Feluwa, Germany The first stream is brought to a pressure preferably in the range of about 2000 psia to 5000 psia (about 138 bar to 345 bar); more pieferably, above about 3200 psia (about 220 bar). After pressurizing the first stream with pump 122, the first stream is conducted through heat exchanger 130. Heat exchanger 130 is preferably used to heat the first stream. After the operation of reactor 150 has started, hot effluent coming out of the reactor may be passed through heat exchanger 130 via conduit 155. The hist stream is preferably heated by passage through the heat exchanger to a temperature such that the salts in the first stream remain substantially soluble in the first stream. The temperature of the first stream is preferably mamtamed below about 700 °F (about 370 °C). The first stream is preferably mamtamed at a pressure of at least about 3200 psia (about 220 bar). At temperatures above about 700 °F (about 370 °C), the solubility of the salts m the first stream may become lower. If the concentration of salts in the first stream is greater than the solubility limit of the heated first stream, a portion of the salts may precipitate out of the first stream. These piecφitates may cause pluggmg of the system components, especially the conduits. An advantage of the described method is that the salt containing first stream is preferably mamtamed below a temperature that would cause precipitation of the salts (I e, about 700 °F (about 370 °C)) before the first stream reaches the reactor. After passing through heat exchanger 130, the first stream is preferably conducted to reactor 150 Optionally, the first stream may be conducted to a heater (not shown). The heater may be used to heat the first stieam to temperatures below about 700 °F (about 370 °C). A heater may be used to raise the temperature of the first stream when the heat exchanger 130 fails to heat the first stream to the appropriate temperature level A second stream is preferably introduced into the system via conduit 116. The second stream is pieferably a water stream which is substantially free of salts. The second stream may include water only. Preferably, the second stream is a water stream which mcludes oxidizable matenal. The oxidizable material preferably includes organic compounds Alternatively, the second stream may contam salts. When the second stream contains salts the concentration or chemical composition of the salts is preferably selected such that the salts substantially remam m solution when the second stream is brought to supercntical conditions. The second stream is preferably passed via conduit 116 to second pump 120. Second pump 120 pieferably brmgs the second stream to a pressure m the vicinity of supercritical conditions for water. A positive displacement pump is preferably used to pressunze the second stream. The stream is brought to a pressure pieferably m the range of about 2000 psia to 5000 psia (about 138 bar to 345 bar), more preferably, above about 3200 psia (about 220 bar). After pressurizing the second stream with pump 120, the second stream is preferably conducted through heat exchanger 130. Heat exchanger 130 is preferably used to heat the second stream. After the operation of reactor 150 has started, hot effluent coming out ofthe reactor may be passed through heat exchanger 130 via conduit 155 The passage of the hot effluent over the conduit 124 preferably increases the temperature of the second stream to the vicinity of supercritical conditions. After passmg through heat exchanger 130, the second stream is transferred to heater 134. Heater 134 may be used to heat the second stream to temperatures in the vicinity of supercritical conditions. Heater 134 is preferably a gas heater. Heater 134 preferably heats the second stream to a temperature between about 550 °F to about 1200 °F (about 290 °C to 650 °C), more preferably, in the range of about 700 °F to about 1000 °F (about 370 °C to 540 °C) Preferably, the second stream is heated to a temperature such that, when the second stieam is mixed with the first stream, the resulting mixture may achieve a peak reactor temperature above about 700 °F (about 370 °C), preferably above about 1000 °F (about 540 °C), and more preferably between about 1000 °F to 1200 °F (about 540 °C to 650 °C) The peak reactor temperature is the temperature of the stream as it is reacted with a supercritical reactor at supercntical conditions An advantage ofthe described method is that little or no precipitation occurs when the second stream is heated above 700 °F (about 370 °C) smce the second stream is substantially free of salts An oxidant supply system includes an oxidant feeder 140, oxidant feeder conduit 137, and oxidant feeder valve 138 The oxidant supply system may be coupled to deliver oxidant to the first stream upstream trom the reactor, the second stream upstream from the reactor, and or to the reactor Oxidant feeder valve 138 may be used to control the amount of oxidant added to the system components In an embodiment, the oxidant supply system is preferably coupled to mixer 136 The second stream is pieferably conducted through conduit 135 to mixer 136, where it may be mixed with oxidant from the oxidant supply system The oxidant supply system may also be configured to add oxidant to the second stream upsneam and/or downstream from the mixer The oxidant may be any conventional source of oxygen Examples of oxygen sources mclude, but are not limited to, liquid oxygen, air, hydrogen peroxide, ozone, persulfates, permanganates, nitrates and their corresponding acids, oxyacids of chlorine and theu corresponding salts, hypochloπtes, chlorus acid and chlorites, chlorates, perchlorates and their corresponding acids Mixtures of oxidants may be used m substantial oi even catalytic quantities Liquid oxygen, hydrogen peroxide, and/or mixtures thereof are preferred Preferably, the amount of oxidant added is sufficient to oxidize a substantial amount or substantially all ofthe contaminates withm the first stream and the second stream The second stream is preferably transferred to reactor 150 through conduit 139 Reactor 150 is preferably configured to allow passage of salts which may precipitate from a stream passing through the reactor at supercntical conditions The second stream is preferably introduced mto reactor 150 at inlet 151 of the reactor The second stream is preferably passed through reactor 150, exiting out of reactor outlet 153 In one embodiment, the first stream, which includes a mixture of water, salt and oxidizable matenals, is preferably mixed with the second stream pnor to entenng reactor 150 The first stream may be mixed with the second stream before the oxidant is added to the second stream The first stream may be conducted via conduit 141 to conduit 135 where the first stream is mixed with the second stream In another embodiment, the first stream may be mixed with the second stream after the oxidant has been added to the second stream, prior to the second stream reachmg the reactor The first stream may be conducted via conduit 143 to conduit 139 where the first stream is mixed with the second stream In another embodiment, the first stream may be added to the second stream as the second stream is passed through reactor 150 The first stream may be injected into reactor 150 at a position downstream from inlet 151 of the reactor At least one injection port 157 downstream from reactor mlet 151 is preferably used to allow the introduction ofthe first stream mto reactor 150. A plurality of injection ports 157 downstream from reactor inlet 151 may be used to introduce the first stream into reactor 150. Preferably, a first portion of the first stream is mixed with the second stream prior to reactor mlet 151 The first portion of the first stream is preferably conducted via conduit 141 and/or 143 to conduits 135 and 139, lespectively, such that the first portion ofthe first stream is mixed with the second stream. A second portion of the first stream may also be injected into reactor 150 as the second stream passes through the reactor At least one injection point, preferably a plurality of injection points 157, may be used to introduce the second portion of the first stream into the reactor. Mixing ofthe first and second streams preferably forms a mixed stream. The temperature ofthe mixed stream is preferably determined by the temperature of both the first stream and the second stream, as well as the flow rates of the two streams. Preferably, these temperatures and flow rates are predetermined such that the temperature of the mixed stream is substantially greater than the supercntical temperature of water (e.g., greater than about 700 °F (about 370 °C) As the mixed stream passes through reactor 150, the oxidizable matenal is preferably oxidized. For substantially complete oxidation of all of the oxidizable mateπals, the mixed stream preferably achieves a peak reactor temperature above the supercritical temperature of water (e.g., above about 700 °F (about 370 °C)) as the mixed stream passes through reactor 150. Preferably, the initial temperature ofthe mixed stream is piedetermined such that the peak reactor temperature is between about 1000 °F to 1200 °F (about 540 °C to 650 U C) As the mixed stream passes through reactor 150, cooling ofthe mixed stream to below 700 °F (about 370 °C) may occur due to heat loss from reactor 150 to the surroundings This heat loss may be offset by heat produced during the oxidation ofthe oxidizable matenals. The supercntical water oxidation of oxidizable materials, especially organic compounds, is typically an exothermic reaction (i.e , a chemical reaction that produces heat). This production of heat during the oxidation of organic compounds may cause the temperature of the surroundings (i.e., the reactor) to rise. Preferably the heat produced by the reaction of the oxidizable material will maintain the mixed stream at a temperature between about 1000 °F to 1200 °F (about 540 °C to 650 °C). When a sufficient amount of oxidizable matenal is present, this heating ofthe reactor may be sufficient to prevent cooling of the mixed stream. If the amount of oxidizable material is relatively low, the heat generated by the oxidation ofthe oxidizable material may be insufficient to mamtam the mixed stream at temperatures above about 700 °F (about 370 °C). In such cases, the mixed stream is preferably formed such that the mixed stream has an initial temperature which is significantly higher than 700 °F (about 370 °C). The initial temperature ofthe mixed stream is the temperature ofthe mixed stream when the mixed stream is formed. As the mixed stream passes through reactor 150, the mixed stream may cool due to loss of heat from reactor 150 to the surroundings Because the reaction ofthe oxidizable material may be insufficient to mamtain the initial temperature, the temperature of the mixed stream typically drops as it passes through reactor 150 To ensure that the final temperature (l e, the temperature of the mixed stream as it exits reactor 150) is maintained above 700 °F (about 370 °C) the mixed stream is preferably formed such that the initial temperature of the mixed stream is significantly greater than about 700 °F (about 370 °C). This higher initial temperature ofthe mixed stream pieferably inhibits the final temperature ofthe mixed stream from dropping below about 700 °F (about 370 °C). For example, mixed streams that contain relatively high concentrations of oxidizable materials may only require an initial temperature that is slightly above about 700 °F (about 370°F) to achieve an adequate peak reactor temperature. As the mixed stream passes through reactor 150, the oxidizable material may be oxidized causing the temperature of the mixed stream to increase. This temperature increase may be offset, to some extent, by the loss of heat from reactor 150 to the surroundings. When the concentration of oxidizable material is relatively high (e.g., at least greater than about 5% by volume of oxidizable material), the oxidation of this material will preferably maintain the mixed stream at temperatures substantially above about 700 °F (about 370 °C). Preferably, the initial temperature ofthe mixed stream is at or above about 750 °F (about 400 °C) when the concentration of oxidizable materials is less than about 5% by volume. If the concentration of oxidizable material is relatively low, the oxidation ofthe oxidizable material may be insufficient to maintain the mixed stream at a temperature above about 700 °F (about 370 °C). As the mixed stream passes through reactor 150 the temperature ofthe mixed stream may become lower due to the loss of heat from reactor 150 to the surroundings. When the concentration of oxidizable material is relatively low the oxidation of this material may be insufficient to maintain the mixed stream at temperatures substantially above about 700 °F (about 370 °C). Preferably, the initial temperature of the mixed stream is at or above about 950 °F (about 510 °C) when the concentration of oxidizable materials is at about 1% by volume. Table 1 further illustrates this concept, based on a series of computer simulations ofthe mixing of a hot stream with a colder salt containing stream in a supercritical reactor. The simulations were based on the introduction of a salt containing stream which is at a temperature of about 680 °F (about 360 °C) to a hot stream which is at a temperature of 1000 °F (about 540 °C). The salt containing stream was introduced into the reactor at a flow rate of about 100 lb./hr. The concentration of oxidizable material within the mixed stream was varied from 1% to 6% by volume. The temperature ofthe mixed stream represents the theoretical temperature of the mixed stream which is required to produce a 1000 °F peak temperature in the reactor after oxidation. The heater power refers to the amount of heat required to produce a 1000 °F (about 540 °C) hot stream having the hot stream flow rate given. All streams are maintained at a pressure of about 3200 psia (about 220 bar). Table 1 Refemng to the simulations, simulation 1 shows that an initial mixed stream temperamre of about 976 °F (about 524 °C) would be requued to substantially oxidize the oxidizable matenal at a peak reactor temperamre of about 1000 °F (about 540 °C) when the oxidizable material is present at a concentration of 1% by \ olume To produce a mixture having a temperature of about 976 °F (about 524 °C), it was determined that a hot stream at about 1000 °F (about 540 °C) would need to be added at a rate of about 358 lb. hr to a salt stream at about 680 °F (about 360 °C) flowing at a rate of about 100 lb. hr. The amount of heat required to produce a hot stream having a temperature of about 1000 °F (about 540 °C) and a flow rate of about 358 lb /hr was determined to be about 253,000 b.t.u./hr. As the concentration of oxidizable material is increased, the temperature ofthe mixed stream may be decreased while still allowing complete oxidation of the oxidizable materials at a peak reactor temperature of about 1000 °F (about 540 °C) To lower the temperature ofthe mixed stream, the flow rate ofthe hot stream may be reduced while holding the flow rate and temperamre of the salt contammg stream constant Thus, when the concentration of oxidizable material is at about 6% by volume the temperature ofthe mixed stream needs to be at about 743 °F (about 395 °C) or higher (see simulation 6) To produce a mixed stream having a temperature of about 743 °F (about 395 °C), it is was determined that the flow rate of a 1000 °F (about 540 °C) hot stream should be about 47 lb /hr When the concentration of oxidizable material is greater than about 6% by volume, the salt containing stieam may have an initial temperature that is below about 700 °F (about 370 °C) when introduced into the leactor Oxidation of the oxidizable material will preferably increase the temperature ofthe waste stream such that supercritical conditions are achieved withm the reactor. A salt contammg stream hav g a concentration of oxidizable material greater than about 6% may be introduced mto the reactor at about 680 °F (about 360 °C) The heat produced by the oxidation of the oxidizable materials may be sufficient to raise the temperature ofthe salt containing stream above about 700 °F (about 370 °C) and mamtam the temperature of the salt stream at this level until the oxidizable material is substantially all reacted. For this situation a second stream, having a higher temperature than the salt contammg stream, may not be requued The initial temperature of the mixed stream, formed by mixing the salt contammg stream with the a second stream having a higher temperature than the salt contammg stream, may be controlled by varying the flow rates of the first and second streams and/or the temperature ofthe second stream. For example, to raise the initial temperature ofthe mixed stream, either the flow rate ofthe first stream may be lowered or the flow rate of the second stream may be increased To lower the initial temperature of the mixed stream, either the flow rate of the first stream may be increased or the flow rate of the second stream may be decreased Additionally, the initial temperamre of the mixed stream may be altered by varying the temperature of the second stream. Preferably, the temperamre ofthe first stream is mamtamed as high as possible without causing the precipitation of salts from the first stream To adjust the initial temperamre ofthe mixed stream, the temperamre of the second stream may be altered. To increase the initial temperamre ofthe mixed stream, the temperature of the second stream may be increased while the flow rate of the first and second streams remains constant. To decrease the initial temperature of the mixed stream, the temperamre of the second stream may be decreased while the flow rate ofthe first and second stream is held constant. When the first and second streams are mixed together, a mixed stream having a temperature that is at least about 700 °F (about 370 °C) is preferably formed. At temperatures above about 700 °F (about 370 °C) the salts dissolved within the mixed stream may precipitate out of the mixed stream. Reactor 150 is preferably configured to allow the precipitated salts to flow through the reactor without substantially inhibiting the flow of the mixed stream. Reactors configured to allow the flow of solids along with supercritical fluids typically include reaction zones which may have a relatively large diameter. One such reactor is descnbed m "SCWRO Process for Regeneration of Activated Carbon and Destruction of Pollutants m Supercntical Water" by M.J. Cocero et al. The precipitated salts are preferably conducted out of reactor 150 along with the mixed stream. After passing through separator 154 the mixed stream is preferably conducted to heat exchanger 130 through conduit 155. Heat exchanger 130 preferably allows the mixed stream from reactor 150 to pass through m such a way that the heat from the mixed stream will preheat the first and second streams passing through conduits 124 and 126. Cooling of the mixed stream in the heat exchanger may cause the temperamre of the mixed stream to drop below about 700 °F (370 °C). If the mixed stream drops below 700 °F (370 °C) any precipitated salts may become redissolved within the mixed stream Thus, plugging ofthe reactor may be avoided by lowering the temperature of the mixed stream after passage through reactor 150 In another embodiment, the precipitated salts may be removed from the mixed stream by a separator. The separator is preferably configured to substantially separate the salt particles from the mixed stream. Conduit 152 preferably conducts the mixed stream and the precipitated salt from reactor 150 mto a separator 154. Separator 154 may be a hydrocyclone separator or a gravity separator. Alternatively, the separator may be incorporated into the reactor. Separator 154 is preferably configured to substantially separate the salt particles horn the mixed stream. The separated salt particles are preferably conducted out ofthe system via conduit 170 The mixed stream is preferably transferred to cooler 156 via conduit 159 Cooler 156 preferably lowers the temperamre and pressure ofthe mixed stream to subcntical conditions. Gases are preferably released to the atmosphere through conduit 158. Condensed water is preferably transfened from the system 100 through conduit 160. A controller 144 may be used to monitor system 100 and alter the reaction conditions. Controller 144 may be a computer, programmable logic controller, or any of other known controller systems known m the art. These systems may include a proportional-integral ("PI") controller or a proportional-integral-denvative ("PID") controller. Controller 144 may be part of an electronic, digital, or pneumatic system. Controller 144 may also send, and optionally receive, signals to and/or from the system components that may be electromc, digital, or pneumatic. Controller 144 may ad j ust the flow rate ofthe first and second streams through reactor 150. The flow late ofthe streams may be adjusted by altering the pump displacement or speed ofthe first and second pumps. C ontroller 144 may send signals to the pumps to control the flow rate ofthe streams The flow rate is pieferably adjusted such that the oxidizable matenals are treated withm reactor 150 for a sufficient time to allow the oxidizable matenal to be substantially oxidized. The controller may also adjust the flow rates ofthe first and second streams to maintam a specified temperamre withm the reactor Controller 144 may also adjust the temperamre of the second stream Controller 144 may send signals to heater 134 m response to changes in temperamre from reactor 150. Additionally, controller 144 may adjust the amount of oxidant added to the second stream in mixer 136 by controlling the oxidant feeder valve 138 The amount of oxidant added is preferably controlled in response to changes in temperamre and/or pressure of reactor 150 Additionally, the controller may vary the amount of oxidant as a function ofthe concentration of oxidizable material contained in the streams ~ In another embodiment, a method for preventing the cloggmg of the conduits upstream from the leactor may involve the mixing of two subcntical streams. As m the previous method, a salt stream is preferably mamtamed at temperatures below supercntical conditions as the solution is transfened to a reactor A second stream is also added to the reactor to form a mixture of the two streams The second stream pieferably mcludes a relatively high amount of oxidizable matenal. The mixed stream formed by mixmg the first stream with the second stream preferably includes a sufficient amount of oxidizable matenal to cause an exothermic reaction withm the reactor, The heat produced by the reaction is preferably sufficient to raise the temperamre of the mixed stream above about 700 °F (about 370 °C) The heat produced by the reaction ofthe oxidizable matenals within the reactor preferably allows the mixture to remain at a temperamre above about 700 °F (about 370 °C) for a time sufficient to oxidize a substantial amount or substantially all of the oxidizable material Typically, the concentration of oxidizable material within the mixed stream is above about 6%. In this manner clogging may be prevented upstream from the reactor. Referring to the system 200 depicted in Fig 2, an embodiment of a method for the destruction of contaminants in salt streams is descnbed m more detail A first stream, which includes a salt and oxidizable matter, is preferably introduced into the system via conduit 216 Examples of oxidizable matter may include \ anous organic compounds dissolved or suspended in the water, as well as some inorganic compounds. An example of a salt stream is sea water which mcludes organic compounds In another embodiment, supply source 210 may contam a pH adjustmg additive for neutralizing oxidation products. Typically, a pH adjusting additive (e.g., NaOH or NaHCOj) may be added to the first stieam to neutralize the oxidation products formed. A first stream which includes oxidizable matenal may be introduced into the system via conduit 216. As the first stream is introduced mto the system, a pH adjustmg additive from supply source 210 may be added to form a first stream which mcludes a salt. The first stream made of a mixture of oxidizable matenal and a salt is preferably conducted through conduit 216 to first pump 220. First pump 220 preferably bnngs the first stream to a pressure in the vicinity of supercritical conditions for water. A positive displacement pump is preferably used to pressurize the first stieam. The first stream is brought to a pressure preferably m the range of about 2000 psia to 5000 psia (about 138 bar to 345 bar), more preferably, above about 3200 psia (about 220 bar). After pressurizing the first stream with pump 220, the first stream is preferably conducted through heat exchanger 230. Heat exchanger 230 is preferably used to heat the first stream. After the operation of reactor 250 has started, hot effluent commg out of the reactor may be passed through heat exchanger 230 via conduit 255 The first stream is preferably heated by passage through the heat exchanger to a temperamre such that the salts m the first stream remain substantially soluble in the first stream The temperamre ofthe first stream is pieterably mamtamed below about 700 °F (about 370 °C) At temperamres above about 700 °F (about 370 °C), the solubility of the salts m the first stream may become lower. An advantage of the descnbed method is that the stream is not heated above a temperamre (i.e., above about 700 °F (about 368 °C)) that would cause substantial precipitation of the salts before the first stream reaches the reactor The first stream may be conducted to heater 232. Heater 232 may be used to heat the first stream to temperamres up to about 700 °F (about 368 °C) Heater 232 may be used before the operation ofthe reactor 250 has begun to heat the first stream Heater 232 may also be used to raise the temperamre ofthe first stream when heat exchanger 230 fails to heat the waste stream to the appropnate temperamre level A second stream is preferably introduced mto the system via conduit 212. Preferably, the second stream is a stream which includes oxidizable material The second stream may also include salts The oxidizable material preferably mcludes organic compounds The second stream preferably contains a sufficient amount of oxidizable material such that, when mixed with the first stream, the amount of oxidizable matenal piesent in the mixed stream is sufficient to sustain supercntical conditions dunng the reaction of the oxidizable material In another embodiment, supply source 214 may contam oxidizable material The oxidizable material pieferably is an organic compound or group of compounds which may be added to the second stream to mciease the concentration of oxidizable matenals withm the stream A second stream, which may include oxidizable material, may be introduced mto the system via conduit 216 As the second stream is introduced mto the system, additional oxidizable material from supply source 214 may be added to form a second stream containing sufficient oxidizable matenal to sustain supercritical conditions during the reaction of the oxidizable material The second stream is passed via conduit 212 to second pump 222 Second pump 222 preferably brings the waste stream to a pressure m the vicinity of supercntical conditions for water. The second stream is brought to a pressure preferably m the range of about 2000 psia to 5000 psia (about 138 bar to 345 bar); more preferably, above about 3200 psia (about 220 bar). After pressurizing the second stream with pump 222, the second stream is conducted through heat exchanger 230. Heat exchanger 230 is preferably used to heat the second stream After the operation ofthe leactor 250 has started, hot effluent commg out ofthe reactor may be passed through the heat exchanger 230 via conduit 255. The hot effluent preferably is used to heat the second stream as it passes through conduit 225 After passing through heat exchanger 230, the second stream may be conducted to a heater 234 The second stream is preferably heated by passage through heater 234 to a temperamre such that the salts in the second stream remam substantially soluble in the second stream The heater may be used to heat the stream to temperamres up to about 700 °F (about 370 °C) Heater 234 may be used before the operation ofthe reactor 250 has begun to heat the second stream Heater 234 may also be used to raise the temperamre of the second stream when heat exchanger 230 fails to heat the second stream to the appropriate temperamre level After the first stream is pressurized and heated, the stream is preferably conducted through conduit 235 to mixer 236, where it may be mixed with oxidant from oxidant feeder 240 through oxidant feeder line 237 Alternatively, the oxidant may be fed into the first stream upstream from or downstream from mixer 136 In another embodiment, the second stream may be passed through mixer 236 to allow an oxidant to be added, rather than the first stream In another embodiment, both the first and second streams may pass through mixer 236 where an oxidant may be added to the streams An oxidant feeder valve 238 may be used to control the amount ot oxidant added to the passing stream The oxidant may be any conventional source of oxygen Liquid oxygen, hydrogen peroxide, and/or mixtures thereof are prefened Preferably, the amount of oxidant added is sufficient to oxidize a substantial portion of or substantially all ofthe oxidizable matenals withm the fust and second streams The first stream is preferably transferred to reactor 250 through conduit 239 Reactor 250 is preferably configured to maintain reactor conditions in the vicinity of supercritical conditions for water More preferably, reactor 250 is configured to maintain reactor conditions at supercritical conditions for water The first stream is pieterablv introduced into reactor 250 at inlet 251 ofthe reactor The first stream preferably passes through the leactor exiting out of through reactor outlet 253 As the first stream is passed through reactor 250, the second stream, which includes a mixture of water and oxidizable materials, is preferably injected mto the reactor Preferably, the second stream is injected mto the reactor at a position downstream from mlet 251 of reactor 250 At least one injection port downstream from leactor inlet 251 is preferably used A plurality of injection pomts downstream from the reactor mlet may be used to introduce the second stream mto reactor 250 As the second stream is injected into reactor 250, a mixed stream is preferably formed The mixed stieam preferably includes a mixture of the first stream and the second stream The oxidizable material content ot the mixed stream may be dependent on the concentration of oxidizable material in the first and second stieams Preferably, the second stream contams a sufficient amount of oxidizable material such that when the second stream is combined with the first stream a mixed stream is formed that includes greater than about 6% by volume of oxidizable material When the mixed stream is conducted through reactor 250, the oxidizable material is preferably reacted to form oxidation products The oxidation ofthe oxidizable material may produce exothermic reactions The exothermic reactions ofthe oxidizable matenals may cause the temperamre of the mixed stream to nse Preferably, the oxidation ofthe oxidizable material causes the temperamre of the mixed stream to nse above about 700 °F (about 370 °C) Since the mixed stream is preferably at a pressure above about 3200 psia (about 220 bar), the increase in temperamre may create supercritical conditions withm the reactor By msunng a concentration of oxidizable material above about 6% by volume, the heat ofthe oxidation reactions should be sufficient to maintain supercritical conditions while the mixture is passed through reactor 250 An advantage of this method is that plugging ofthe components upstream from reactor 250 may be reduced Pluggmg of the conduits and other components typically occurs when a waste stream is heated to supercritical temperamre before reaching the reactor The heatmg of a waste stream to these temperamres may cause the dissolved salts to precipitate out of the waste stream Since neither the first nor the second streams need to be heated to supercritical temperamres (1 e , greater than about 700 °F (about 370 °C) before reachmg reactor 250, the precipitation of salts from the waste stream may be avoided After the oxidation of the oxidizable matenals has begun, the temperamre ofthe mixed stream may rise above about 700 °F (about 370 °C) At temperamres above about 700 °F (about 370 °C), the salts dissolved withm the mixed stream may precipitate out ofthe mixed stream These salts are preferably conducted out of teactor 250 along with the mixed stream Conduit 252 preferably conducts the mixed stream and the piecipitated salt from reactor 250 into a separator 254 Separator 254 may be a hydrocyclone separator or a lty separator Alternatively, the separator may be incorporated into the reactor Separator 254 is preferably configured to substantially separate the salt particles from the mixed stream The separated salt particles are pi eferably conducted out of the system via conduit 270 After passing through separator 254, the mixed stream is preferably conducted to heat exchanger 230 through conduit 255 Heat exchanger 230 preferably allows the mixed stream from reactor 250 to pass through m such a way that the heat from the mixed stream will preheat the first and second streams passmg through conduits 224 and 225 The mixed stream may then be transfened to cooler 256 via conduit 259 Cooler 256 pieterably lowers the temperamre and pressure ofthe mixed stream to subcntical conditions Gases are pieferably released to the atmosphere through conduit 258 Condensed water is preferably transferred from the system 200 through conduit 260 \ controller 244 may be used to monitor system 200 and alter the reaction conditions Controller 244 mav adjust the flow rate ofthe first and second streams through reactor 250 Controller 244 may send signals to the pumps to control the flow rate ofthe streams Controller 244 may also adjust the temperature ofthe first sUeam, the second stream or both streams Controller 244 may send signals to heaters 232 and 234 in response to changes in temperamre from reactor 250 Additionally, controller 244 may adjust the amount of oxidant added to the waste stream passmg through mixer 236 by controlling the oxidant feeder valve 238 The amount of oxidant added is preferably controlled in response to changes m temperamre and pressure of reactor 250 and as a function ofthe concentration of oxidizable material contained m the streams Further modifications and alternative embodiments of vanous aspects of the invention will be apparent to those skilled in the art in view of this description Accordmgly, this description is to be construed as illustrative only and is for the purpose of teachmg those skilled in the art the general manner of carrying out the invention It is to be understood that the forms ofthe mvention shown and descnbed herem are to be taken as the presently prefeπed embodiments Elements and mateπals may be substimted for those illustrated and described herein, parts and processes may be reversed, and certain features ofthe invention may be utilized independently, all as would be apparent to one skilled m the art after havmg the benefit of this descnption ofthe invention Changes may be made in the elements descnbed herein or m the steps or in the sequence of steps of the methods described herein without departing from the sp t and scope ofthe invention as descnbed m the following claims

Claims: What is claimed is 1 A method for treating a first stream compnsmg oxidizable material, a salt and water m a reactor at a temperamre of at least about 700 °F (about 370 °C) and a pressure of at least about 3200 psia (about 220 bar), comprising conducting a second stream compnsmg water to the reactor, wherein the second stream is at a pressure of at least about 3200 psia (about 220 bar) and a temperamre of at least about 700 °F (about 370 °C), mixing the first stream with the second stream upstream from the reactor to form a mixed stream, the mixed stream compnsmg the oxidizable material ofthe first stream, wherem the first stream is at a pressure and temperamre such that the salt in the first stream remains substantially dissolved withm the first stream, and wherem the mixed stream is at a temperamre of at least about 700 °F (about 370 °C) and a pressure of at least about 3200 psia (about 220 bar), introducing the mixed stream into the reactor, and reacting at least a portion of the oxidizable matter of the mixed stream withm the reactor The method of claim 1 , wherem the first stream is at a pressure of at least about 3200 psia (about 220 bar) and a temperamre below about 700 °F (about 370 °C) 3 The method of claim 1 , further compnsmg addmg a pH adjusting additive to the first stream pnor to mixing the first stream with the second stream The method of claim 1, further compnsmg heatmg the first stream m a heat exchanger such that the temperamre ofthe first stream is about 650-695 °F (about 343-368 °C) The method of claim 1 , further compnsmg adding an oxidant to the second stream prior to mixmg the first stream with the second stream The method of claim 1, further comprising passing the second stream through a heat exchanger and a heater pnor to mixing the first stream with the second stream, wherem the heat exchanger and the heater together bring the temperamre ofthe second stream to at least about 700 °F (about 370 °C) The method of claim 1, wherein the mixed stream is introduced to the reactor at an mlet ofthe reactor, and wherein the first stream is mixed with the second stream at a position upstream from the mlet of the reactor The method of claim 1, further compnsmg heating the second stream to a temperamre of between about 1000 °F (about 540 °C) to about 1200 °F (about 650 °C) The method of claim 1 , further comprising varying a flow rate of the second stream as a function of a concentration ofthe oxidizable material in the mixed stream The method of claim 1 , further compnsmg varying a flow rate of the second stream as a function of a temperamre of the mixed stream The method of claim 1. further compnsmg varying a flow rate ofthe second stream to maintain a predetermined temperamre of the mixed stream, and wherem the temperamre of the mixed stream is maintained at a value which produces a predetermined peak reactor temperamre The method of claim 1 , wherein formation of the mixed stream is accompanied by precipitation of a portion of the salt, and further comprising passing the mixed stream through a separator to remove the precipitated salt from the mixed stream The method of claim 1, further comprising passing the mixed stream from the reactor through a heat exchanger, and wherein the passage of the mixed stream through the heat exchanger substantially heats the first and second streams prior to the first and second streams bemg mixed together The method of claim 1 , further compnsmg passmg the mixed stream mto a cooler subsequent to reacting the oxidizable matter, wherein the cooler is configured to bnng the mixed stream to subcntical conditions The method of claim 1, further comprising varying the temperamre ofthe second stream to control the temperamre ofthe mixed stream. The method of claim 1 , wherein the second stream further compnses oxidizable material The method of claim 1, wherein the oxidizable material compnses organic compounds The method of claim 1. wherein the oxidizable material comprises halogenated solvents, and further comprising adding pH adjusting additives to the first stream prior to introducing the first stream mto the reactor The method of claim 1 , wherein the oxidizable material comprises sulfur containing compounds, and further comprising adding pH adjusting additives to the first stream prior to mtroducing the first stream into the reactor The method of claim 1 , further comprising adding an oxidant to the second stream pnor to introducing the second stream into the reactor, wherem a concentration of oxidant is substantially greater than a concentration of oxidizable matenal in the mixed stream The method of claim 1, wherem the second stream further comprises oxidizable matenal A method for treating a first stream comprising oxidizable matenal, salt and water m a reactor at a temperamre of at least about 700 °F (about 370 °C) and a pressure of at least about 3200 psia (about 220 bar), comprising conducting a second stream comprising oxidizable material and water to the reactor, wherein the second stream is at a pressure of at least about 3200 psia (about 220 bar) and a temperamre of at least about 700 °F (about 370 °C), mixing the first stream with the second stream to form a mixed stream upstream from the reactor, the mixed stream comprising the oxidizable material from the first and the second streams, wherem the fust stream is at a pressure of at least about 3200 psia (about 220 bar) and a temperamre up to about 7 00 °F (about 370 °C), and wherein the mixed stream is at a temperamre of at least about 700 °F (about 370 °C) and a pressure of at least about 3200 psia (about 220 bar), introducing the mixed stream into the reactor, and reacting at least a portion of the oxidizable material ofthe mixed stream within the reactor The method of claim 22, further comprising adding a pH adjusting additive to the first stream pnor to mixing the first stream with the second stream 1 he method of claim 22, further comprising heating the first stream in a heat exchanger such that the temperamre of the first stream is about 650-695 °F (about 340 - 370°C) The method of claim 22, further compnsmg adding an oxidant to the second stream pnor to mixing the first stream with the second stream 1 he method of claim 22, further comprising passing the second stream through a heat exchanger and a heater prior to mixing the first stream with the second stream, wherein the heat exchanger and the heater together bring the temperamre ofthe second stream to at least about 700 °F (about 370 °C) The method of claim 22, wherein the mixed stream is conducted to the reactor at an mlet ofthe reactor, and wherem the first stream is mixed with the second stream upstream from the mlet ofthe reactor The method of claim 22, further compnsmg heating the second stream to a temperamre of at least about 1000 °F (about 540 °C) The method of claim 22, further comprising varying a flow rate and or temperamre of the second stream as a function of a concentration of the oxidizable material in the mixed stream The method of claim 22, further comprising varying a flow rate and/or temperamre of the second stieam as a function of a temperamre of the mixed stream The method of claim 22, further comprising varying a flow rate of the second stream to mamtam a predetermined temperamre ofthe mixed stream, and wherein the temperamre ofthe mixed stream is maintained at a value which is sufficient to generate a predetermined peak reactor temperamre The method of claim 22, wherein formation of the mixed stream is accompanied by precipitation of a portion ofthe salt, and further compnsmg passing the mixed stream through a separator to remove the precipitated salt from the mixed stream The method of claim 22, further comprising passing the mixed stream from the reactor through a heat exchanger, and wherem the passage ofthe mixed stream through the heat exchanger substantially heats the first and second streams pnor to these streams bemg mixed The method of claim 22, further compnsmg passing the mixed stream into a cooler subsequent to leading the oxidizable matter, wherein the cooler is configured to brmg the mixed stream to subcntical conditions The method of claim 22, further compnsmg varying the temperamre ofthe second stream to control the temperamre ofthe mixed stream The method of claim 22, wherem the second stream further comprises oxidizable matenal. The method of claim 22, wherein the oxidizable material comprises organic compounds The method of claim 22, wherein the oxidizable matenal comprises halogenated solvents, and further comprising adding a pH adjusting additive to the first stream prior to mixing the first stream with the second stream The method of claim 22, wherein the oxidizable matenal comprises sulfur containing compounds, and further comprising addmg a pH adjusting additive to the first stream pnor to mixing the first stream with the second stream The method of claim 22, further compnsmg addmg an oxidant to the second stream prior to mixing the first stream with the second stream, wherem a concentration of oxidant is substantially greater than a concentration of oxidizable material in the mixed stream A method for treating a mixed stream comprising oxidizable material, a salt and water in a reactor at a temperamre of at least about 700 °F (about 370 °C) and a pressure of at least about 3200 psia (about 220 bar), comprising introducing a first stream comprising oxidizable material, the salt and water into the reactor, wherein the first stream is at a pressure of at least about 3200 psia (about 220 bar) and a temperamre substantially less than about 695 °F (about 368 °C), introducing a second stream mto the reactor subsequent to the introduction of the first stream, the second stream comprising oxidizable material and water, wherein the second stream is at a pressure of at least about 3200 psia (about 220 bar) and a temperamre substantially less than about 695 °F (about 368 °C), mixmg the second stream with the first stream to form the mixed stream withm the reactor such that the mixed stream is at a pressure of at least about 3200 psia (220 bar) and a temperamre substantially less than about 695 °F (about 368 °C), and reacting at least a portion ofthe oxidizable matenal withm the reactor, wherem the reaction of the oxidizable material causes a temperamre of the mixed stream to rise substantially above about 700 °F (about 370 °C) The method of claim 41 , further compnsmg addmg a pH adjustmg additive to the first stream pnor to introducing the first stream into the reactor The method of claim 41 , further compnsmg heating the first stream in a heat exchanger such that the temperamre ofthe first stream is about 650-695 °F (about 343-368 °C) The method of claim 41, further compnsmg adding an oxidant to the first stream prior to introducing the first stream mto the reactor The method of claim 41 , further compnsmg addmg an oxidant to the second stream prior to introducing the first stream into the reactor The method of claim 41, further compnsmg passing the second stream through a heat exchanger and a heater prior to introducing the second stream into the reactor, wherem the heat exchanger and the heater together bring the temperamre of the second stream to below about 700 °F (about 370 °C) The method of claim 41 , wherem the first stream is mtroduced mto the reactor at an mlet of the reactor, and wherein the second stream is mtroduced to the reactor at a position downstream from the inlet of the reactor The method of claim 41 , wherein reaction of the mixed stream is accompanied by precipitation of a portion ofthe salt, and further compnsmg passmg the nuxed stream through a separator to remove the precipitated salt from the mixed stream The method of claim 41 , further compnsmg passmg the mixed stream from the reactor through a heat exchanger, and wherein the passage ofthe mixed stream through the heat exchanger substantially heats the first and second streams The method of claim 41, further compnsmg passing the mixed stream mto a cooler subsequent to reacting the oxidizable matter, wherem the cooler is configured to brmg the mixed stream to subcntical conditions The method of claim 41 , wherein the first stream further compnses oxidizable matenal The method of claim 41, wherein the oxidizable matenal comprises organic compounds The method of claim 41, wherem the oxidizable matenal comprises halogenated solvents, and further comprising adding a salt to the first stream pnor to mtroducing the first stream mto the reactor The method of claim 41 , wherein the oxidizable matenal comprises sulfur and/or phosphate contammg compounds, and further compnsmg adding a pH adjustmg additive to the first stream pnor to introducing the first stream into the reactor The method of claim 41 , further comprising addmg an oxidant to the first stream prior to introducing the first stream into the reactor, wherein a concentration of oxidant is substantially greater than a concentration of oxidizable material in the mixed stream A system for treating a mixed stream comprising oxidizable matter, a salt and water m a reactor at a temperamre of at least about 700 °F (about 370 °C) and a pressure of at least about 3200 psia (about 220 bar), compnsmg a reactor comprising an inlet and an outlet, the reactor configured to contain the mixed stream as it flows at a temperamre of at least about 700 °F (about 370 C C) and a pressure of at least about 3200 psia (about 220 bar) from the mlet to the outlet dunng use, and wherem the reactor is configured to allow particles to flow through the reactor, a first stream conduit configured to convey a first stream to the first let ofthe reactor during use, a second stream conduit connected to convey a second stream to the first stream conduit durmg use, a heating system, wherein the first stream conduit and the second stream conduits pass through the heatmg system, and wherein the heating system is configured to increase a temperamre of streams passmg through the first conduit and second conduits such that the mixmg ofthe streams produces a mixed stream havmg a temperamre that is at least about 700 °F (about 370 °C), and an oxidant supply source coupled to the system, wherein the oxidant supply source is configured to supply an oxidant to the mixed stream The system of claim 56, wherein the first stream conduit is configured to contain the first stream at a piessure of about 3200 psia (about 220 bar), and wherem the second stream conduit is configured to contain the second stream at a pressure of about 3200 psia (about 220 bar) The system of claim 56, wherein the heatmg system comprises a first heater, and a second heater, the first heater coupled to the first conduit, the second heater coupled to the second conduit The system of claim 56, further compnsmg a controller configured to adjust a flowrate of the first stieam and a flow rate and/or temperature ofthe second stream to achieve a mixed stream temperamre of at least about 700 C F (about 370 °C) as the mixed stream is flowed through the reactor dunng use. The system of claim 56, further compnsmg a first pump, the first pump configured to raise the pressme of the first stream passmg through the first conduit to a pressure of at least about 3200 psia (about 220 bar) during use, and further compnsmg a second pump, the second pump configured to raise the pressure ofthe second stream passing through the second conduit to a pressure of at least about 3200 psia (about 220 bar) dunng use The system of claun 56, further compnsmg a separator, wherem the separator is configured to substantially remove undissolved particles from a stream passing out ofthe reactor dunng use The system of claim 56, further compnsmg a cooler, wherem the cooler is configured to substantially cool a stream passing out ofthe reactor to subcntical conditions durmg use The system of claim 56, further compnsmg a pH adjustmg additive supply source, wherem the salt supply source is configured to add a salt to the first stream passmg through the first conduit dunng use The system of claim 56, further compnsmg a controller, wherein the controller is configured to monitor a temperamre ofthe mixed stream dunng use, and wherem the controller is configured to adjust the temperamre ofthe second stream passmg through the second conduit in response to changes in the temperamre of the reactor dunng use. The system of claim 56, wherein the separator is a hydrocyclone separator The system of claim 56, further compnsmg a controller, the controller configured to maintain a concentration of the oxidant withm the reactor dunng use, the concentration bemg sufficient to substantially oxidize the organic contaminant dunng use. The system of claun 56, wherein the oxidant supply source is coupled to the first conduit, and wherein the oxidant supply source introduces the oxidant mto a stream passmg through the first conduit dunng use The system of claim 56, wherein the oxidant supply source is coupled to the second conduit, and wherem the oxidant supply source introduces the oxidant mto a stream passing through the second conduit durmg use 69 The system of claim 56, wherem the oxidant supply source is coupled to the reactor, and wherem the oxidant supply source introduces the oxidant into the mixed stream as the mixed stream passes through the reactor dunng use. 70 The system of claim 56, wherein the heating system comprises a heat exchanger, a first heater and a second heater. 71. A system for treating a mixed stream compnsmg oxidizable matter, a salt and water m a reactor at a temperamre of at least about 700 °F (about 370 °C) and a pressme of at least about 3200 psia (about 220 bar), compnsmg: a reactor comprising a first mlet, a second mlet and an outlet, the reactor configured to contain the mixed stream as it flows at a temperamre of at least about 700 °F (about 370 °C) and a pressure of at least about 3200 psia (about 220 bar) from the mlet to the outlet dunng use, and wherein the reactor is configured to allow particles to flow through the reactor, and wherem the second mlet is downstream from the first mlet; a first stream conduit configured to convey a first stream to the first mlet of the reactor dunng use; a second stream conduit connected to convey a second stream to the second mlet ofthe reactor durmg use; a first heating system, wherem the first stream conduit passes through the first heating system, and wherem the first heatmg system is configured to increase the temperamre of a stream passmg through the first conduit to a temperamre of up to about 700 °F (about 370 °C) dunng use; a second heatmg system, wherem the second stream conduit passes through the heatmg system, and wherein the heatmg system is configured to heat a stream passmg through the second stream conduit to a temperamre of at least about 700 °F (about 370 °C) dunng use; and an oxidant supply source coupled to the system, wherein the oxidant supply source is configured to supply an oxidant to the mixed stream. A system for treatmg a mixed stream compnsmg oxidizable matter, a salt and water in a reactor at a temperamre of at least about 700 °F (about 370 °C) and a pressure of at least about 3200 psia (about 220 bar), compnsmg a reactor compnsmg a first inlet, a second inlet and an outlet, the reactor configured to contam the mixed stream as it flows at a temperature of at least about 700 °F (about 370 °C) and a pressure of at least about 3200 psia (about 220 bar) from the mlet to the outlet dunng use, and wherein the reactor is configured to allow particles to flow through the reactor, and wherem the second mlet is downstream from the first mlet, a first stream conduit configured to convey a first stream to the first mlet ofthe reactor dunng use, a second stream conduit connected to convey a second stream to the second mlet ofthe reactor during use, a first heating system, wherein the first stream conduit passes through the first heatmg system, and wherein the first heatmg system is configured to mcrease the temperamre of a stream passmg through the first conduit to a temperamre of up to about 700 °F (about 370 °C) duπng use; a second heatmg system, wherem the second stream conduit passes through the heatmg system, and wherein the heatmg system is configured to heat a stream passmg through the second stream conduit to a temperamre of at least about 700 °F (about 370 °C) during use, and an oxidant supply source coupled to the system, wherein the oxidant supply source is configured to supply an oxidant to the mixed stream a controller configured to adjust a flowrate of the first stream and a flow rate ofthe second stream to achieve a mixed stream temperamre of at least about 700 °F (about 370 °C) as the mixed stream is flowed through the reactor durmg use A system for treatmg a mixed stream compnsmg oxidizable matter, a salt and water m a reactor at a temperamre of at least about 700 °F (about 370 °C) and a pressure of at least about 3200 psia (about 220 bar), compnsmg a reactor compnsmg a first inlet, a second mlet and an outlet, the reactor configured to contain the mixed stream as it flows at a temperature of at least about 700 °F (about 370 °C) and a pressure of at least about 3200 psia (about 220 bar) from the mlet to the outlet dunng use, and wherein the reactor is configured to allow particles to flow through the reactor, and wherein the second inlet is downstream from the first mlet, a first stream conduit configured to convey a first stream to the first mlet ofthe reactor duπng use, a second stream conduit connected to convey a second stream to the second mlet of the reactor dunng use, a first heatmg system, wherem the first stream conduit passes through the first heatmg system, and wherein the first heatmg system is configured to mcrease the temperamre of a stream passmg through the first conduit to a temperamre of up to about 700 °F (about 370 °C) durmg use, a second heatmg system, wherem the second stream conduit passes through the heatmg system, and wherein the heatmg system is configured to heat a stream passing through the second stream conduit to a temperamre of at least about 700 °F (about 370 °C) dunng use, and an oxidant supply source coupled to the system, wherein the oxidant supply source is configured to supply an oxidant to the mixed stream a controller, wherein the controller is configured to monitor a temperamre ofthe mixed stream dunng use, and wherein the controller is configured to adjust the temperamre ofthe second stream passmg through the second conduit in response to changes in the temperamre ofthe reactor durmg use A method for treating a waste stream compnsmg oxidizable matenal, salt and water m a reactor at a temperamre of at least about 700 °F (about 370 °C) and a pressure of at least about 3200 psia (about 220 bar), comprising pressurizing the waste stream to a pressure of at least about 3200 psia (about 220 bar), heating the waste stream to a temperamre m the vicinity of supercntical conditions for water such that the salt remains substantially dissolved withm the waste stream, and wherem the temperamre ofthe waste stream is substantially less than about 695 °F (about 368 °C), conducting a heating stream comprising oxidizable material and water to the reactor, wherein the heatmg stream is at a pressure of at least about 3200 psia (about 220 bar) and a temperamre of at least about 700 °F (about 370 °C), mixmg the waste stream with the heatmg stream to form a mixed stream upstream from the reactor, the mixed stream compnsmg the oxidizable matenal from the waste stream and the heatmg streams, wherem the mixed stream is at a temperamre of at least about 700 °F (about 370 °C) and a pressure of at least about 3200 psia (about 220 bar), and reacting at least a portion ofthe oxidizable matenal ofthe mixed stream withm the reactor A method for treating a first stream compnsmg oxidizable matenal, a salt and water m a reactor at a temperamre of at least about 700 °F (about 370 °C) and a pressure of at least about 3200 psia (about 220 bar), compnsmg introducing a second stream compnsmg water into the reactor, wherem the second stream is at a pressure of at least about 3200 psia (about 220 bar) and a temperamre of at least about 700 °F (about 370 °C), mtroducing the first stream mto the reactor subsequent to the introduction ofthe second stream, wherein the first stream is at a pressure and temperamre such that the salt in the first stream remains substantially dissolved withm the first stream, mixmg the first stream with the second stream to form a mixed stream withm the reactor, the mixed stream compnsmg the oxidizable material ofthe first stream, and wherem the mixed stream is at a temperamre of at least about 700 °F (about 370 °C) and a pressure of at least about 3200 psia (about 220 bar), and reactmg at least a portion ofthe oxidizable matter ofthe mixed stream withm the reactor The method of claim 75, wherein the second stream is introduced to the reactor at an mlet of the reactor, and wherem the first stream is introduced to the reactor at a position downstream from the mlet of the reactor A method for treatmg a first stream compnsmg oxidizable matenal m a reactor at a temperamre of at least about 700 °F (about 370 °C) and a pressure of at least about 3200 psia (about 220 bar), comprising. conducting a second stream comprising water to the reactor, wherem the second stream is at a pressure of at least about 3200 psia (about 220 bar) and a temperamre of at least about 700 °F (about 370 °C); mixmg the first stream with the second stream upstream from the reactor to form a mixed stream, mtroducing the mixed stream mto the reactor, and reactmg at least a portion of the oxidizable matter of the mixed stream withm the reactor. A system for treating a mixed stream compnsmg oxidizable matter m a reactor at a temperamre of at least about 700 °F (about 370 °C) and a pressure of at least about 3200 psia (about 220 bar), compnsmg a reactor compnsmg an mlet and an outlet; a first stream conduit configured to convey a first stream to the first inlet ofthe reactor dunng use; a second stream conduit connected to convey a second stream to the first stream conduit duπng use; and a heating system, wherem the first stream conduit and the second stream conduits pass through the heatmg system, and wherem the heatmg system is configured to mcrease a temperamre of streams passmg through the first conduit and second conduits such that the mixing ofthe streams produces a mixed stream havmg a temperatare that is at least about 700 °F (about 370 °C).

Inventors: MCBRAYER ROY NELSON JR, STENMARK LARS BERTIL, TIDLUND LARS HENNING, MCBRAYER, ROY, NELSON, JR., STENMARK, LARS, BERTIL, TIDLUND, LARS, HENNING
Applicants: CHEMATUR ENG AB, CHEMATUR ENGINEERING AB
Application year: 1999
Main classification: A62D3
IPC codes: A62D3, A62D101, B01J3, C02F11