Patent Abstract:
A system and method for treating feedstocks containing solids, sludges or slurries that contain organics includes introducing the feedstock into a desorption chamber. In the desorption chamber, the temperature and pressure of the feedstock are elevated to volatilize a portion of the feedstock and thereby separate the feedstock into a volatile portion containing organics and a residue portion. Steam, water or oxidants can be injected into the desorption chamber to aid in the volatilization process. From the desorption chamber, the volatile portion of the feedstock is transferred to a reactor for hydrothermal treatment to oxidize or reform the organics in the volatile portion. In the hydrothermal reactor, the volatile portion may be reacted with excess oxidant and auxiliary fuel at a temperature between approximately 1000° F. and approximately 1800° F. and a pressure of between approximately 20 atmospheres and approximately 200 atmospheres.

Full Description:
FIELD OF THE INVENTION 
     The present invention pertains generally to methods and systems for accomplishing hydrothermal treatment for the purposes of either waste destruction, energy generation, or the production of chemicals. More specifically, the present invention pertains to methods and systems for the hydrothermal treatment of solids having organic constituents. The present invention is particularly, but not exclusively, useful as a method and system for volatilizing a portion of a material and subsequently treating the volatilized portion hydrothermally. 
     BACKGROUND OF THE INVENTION 
     The present invention pertains to a process for converting materials at supercritical temperature and pressure conditions, or at supercritical temperatures and elevated, yet subcritical, pressures. Supercritical and subcritical are defined here with reference to the critical point of pure water, 705° F. and 218 atm. For example, U.S. Pat. No. 4,338,199, which issued on Jul. 6, 1982 to Modell, discloses a hydrothermal process known as supercritical water oxidation (SCWO) because in some implementations oxidation in the aqueous/steam matrix occurs essentially entirely at conditions supercritical in temperature and pressure. The SCWO process has been shown to give rapid and complete oxidation of virtually any organic compound in a matter of seconds at 1000-1250° F. and 250 atm. 
     Under SCWO conditions, carbon and hydrogen form the conventional combustion products CO 2  and H 2 O, while chlorinated hydrocarbons (CHC&#39;s) give rise to hydrochloric acid (HCl). If cations are available, they will react with the hydrochloric acid to form chloride salts. Alkali may be intentionally added to the reactor to avoid high, corrosive concentrations of hydrochloric acid in the reactor and especially in the cooldown equipment following the reactor. One advantage of the SCWO process is that the conversion of material can be accomplished without producing the environmentally harmful by-products that are produced when the same material is combusted in air. For example, the final product of sulfur oxidation in SCWO is sulfate anion, in contrast to normal combustion, wherein sulfur oxidation forms gaseous SO 2 . As in the case of chloride, alkali may be intentionally added to avoid high concentrations of sulfuric acid. Similarly, the SCWO product of phosphorus oxidation is phosphate anion. 
     A hydrothermal process related to SCWO known as supercritical temperature water oxidation (STWO) can provide similar oxidation effectiveness for certain feedstocks but at lower pressure. This process has been described in U.S. Pat. No. 5,106,513 issued Apr. 21, 1992 to Hong, and utilizes temperatures in the range of 1200° F. and pressures between 25 and 218 atm. Like SCWO, the overall goal of the process may be waste destruction, energy generation, or production of chemicals. For convenience, the processes of SCWO and STWO will both be referred to herein as hydrothermal oxidation (HTO). 
     A key advantage of the hydrothermal processes described above is the cleanliness of the liquid and gaseous effluents. In particular, the gaseous emissions are far cleaner than those obtained by the conventional practice of incineration. EPA&#39;s Maximum Achievable Control Technology (MACT) standards for hazardous waste incineration took effect on Sep. 30, 1999. Current operating facilities were given until Mar. 31, 2003 to comply with the regulations. New facilities are required to comply with the new regulations at start-up. Table 1 shows that HTO emissions meet the MACT standards with little or no post-treatment, while incinerators require extensive emissions cleanup. 
     
       
         
               
             
               
               
               
               
             
           
               
                 TABLE 1 
               
             
             
               
                   
               
               
                 Comparison of Incineration and HTO 
               
               
                 with Respect to MACT/Air Standards 
               
             
          
           
               
                   
                   
                 Typical incinerator 
                 HTO Inherent 
               
               
                 Type of Emissions 
                   
                 emissions controls 
                 Performance 
               
               
                 in Effluent Gas 
                   
                 needed to meet new 
                 (with no gas cleanup 
               
               
                 Stream 
                 MACT/Air Standards 
                 MACT Standards 
                 devices) 
               
               
                   
               
               
                 Dioxins/difurans, 
                  &lt;0.2 
                 Rapid quench, powdered 
                  &lt;0.006 
               
               
                 ng/DSCM (TEQ) 
                   
                 activated carbon (PAC) 
               
               
                   
                   
                 with fabric filter 
               
               
                   
                   
                 baghouse 
               
               
                 Particulate Matter, 
                  &lt;34 
                 Fabric filter baghouse or 
                  &lt;4 
               
               
                 mg/DSCM 
                   
                 electrostatic precipitator 
               
               
                 Toxic Metals, 
                  &lt;0.024 for Cd + Pb 
                 Wet electrostatic 
                  &lt;0.015 for Cd + Pb 
               
               
                 mg/DSCM 
                  &lt;0.097 for 
                 precipitator 
                  &lt;0.015 for Sb + As + Be + Cr 
               
               
                   
                 Sb + As + Be + Cr 
               
               
                 Destruction and 
                  &gt;99.99 
                 Afterburner 
                 &gt;99.999 
               
               
                 removal efficiency, 
               
               
                 % 
               
               
                 HCI, ppmv 
                  &lt;21 
                 Packed tower wet 
                  &lt;0.4 
               
               
                   
                   
                 scrubber 
               
               
                 NOx, ppm 
                 depends on air 
                 Only local regulations 
                  &lt;1 
               
               
                   
                 district - can be 
                 apply. Ammonia or urea 
               
               
                   
                 &lt;100 ppm 
                 injection may be 
               
               
                   
                   
                 required. 
               
               
                 CO, ppm 
                 &lt;100 
                 Afterburner 
                  &lt;2 
               
               
                 Hydrocarbons, ppm 
                  &lt;10 
                 Afterburner 
                  &lt;0.03 
               
               
                   
               
             
          
         
       
     
     A useful variation on the HTO process is that in which no oxidant, or a sub-stoichiometric amount of oxidant, is added to the reactor. In this case, rather than converting to CO 2  and H 2 O, the organic material can reform into useful organic products. This process will be referred to as hydrothermal gasification (HTG), while HTO and HTG will be jointly referred to as hydrothermal processing (HTP). 
     A conventional limitation of HTP has been its application to bulk solids. The pressurized nature of the process typically requires that bulk solids be ground to a fine particle size to allow pumping into a high pressure reactor. Both grinding and pumping can require specialty equipment. In particular, a different device is generally required for different materials such as wood, plastic, or friable solids. Once the material has been ground, introduction into a pressurized reactor usually requires slurrying the material at a high concentration to minimize the size of the HTP reactor and associated process equipment. Thus, expensive, high pressure slurry pumps for viscous streams are typically required. For other solids such as metals, glass or ceramics, suitable size-reduction for introduction into an HTP reactor vessel is completely impractical. 
     A large amount of hazardous waste is generated each year that cannot be placed in a typical landfill unless it is pre-treated. Among this hazardous waste is a large amount of mixed waste consisting of non-hazardous solids that are contaminated with hazardous constituents. The hazardous constituents in these mixed-waste streams are generally suitable for direct feeding into a HTP reactor if they can be first separated from the solid portion of the waste stream. Once the hazardous constituent is extracted from the solid portion, the solid portion is generally considered non-hazardous and can be disposed of without further treatment in a conventional landfill. 
     Examples of such mixed-wastes include soils, inorganic adsorbents and other solids that are contaminated with hazardous organic or radioactive materials. Another such mixed waste consists of conventional and chemical munitions as well as munition dunnage. Protective suits, munition bodies and equipment contaminated with energetics, biological or chemical warfare agents is another mixed waste in which the solids portion could be disposed of conventionally if the hazardous contamination was removed and treated. Similarly, PCB contaminated transformers, pesticide contaminated bags and containers, and medical/biohazard waste such as contaminated needles and glass containers are all mixed wastes that could be disposed of efficiently by first separating the waste into hazardous and non-hazardous components. 
     Another category of waste that can pose difficulty for treatment by HTP is a concentrated acid, base or salt solution contaminated with an organic material. Treatment could be facilitated if the hazardous organic constituents could be separated for HTP while the residual inorganic solution could be handled by simpler means. 
     In the preceding examples, the organic to be treated may be a minor constituent or contaminant, or it may constitute a major portion of the feedstock. 
     In light of the above, it is an object of the present invention to provide methods suitable for the purposes of treating hazardous waste streams containing bulk solid materials and slurries that are difficult to size-reduce and pump to elevated pressure. It is another object of the present invention to provide methods for the removal and destruction of organic constituents from viscous materials such as bulk solids, sludges and slurries without having to pump the viscous material to high pressure. It is another object of the present invention to provide methods for the removal and destruction of organic constituents from acidic, alkaline, or salt-bearing waste streams or feedstocks. Yet another object of the present invention is to provide a method for chemically converting feedstocks containing solids using hydrothermal treatment which is robust, simple, and economical. 
     SUMMARY OF THE PREFERRED EMBODIMENTS 
     The present invention is directed to a system and method for treating feedstocks that include large solid objects, dissolved or undissolved solids, sludges or slurries that contain organics that may be volatilized. For the present invention, the feedstock is first fed into a desorption chamber to volatilize a portion of the feedstock and thereby separate the feedstock into a volatile portion and a residue portion. The feedstock can be continuously fed into the desorption chamber, or the feedstock can be introduced into the desorption chamber in batches. In the desorption chamber, the feedstock is heated to a temperature between approximately 300° F. and approximately 1500° F. and pressurized to a pressure of between approximately 20 atmospheres and approximately 200 atmospheres in an atmosphere that is overall net reducing. 
     In accordance with the present invention, steam, water or oxidants can be introduced into the desorption chamber to aid in the volatilization process. Specifically, these materials can be introduced to serve as reactants for localized partial oxidation and gasification reactions that assist in the overall volatilization of organic constituents. For the present invention, solids handling equipment can be installed in the desorption chamber to mix the steam with the feedstock and thereby increase the rate of volatilization. When continuous feed systems are employed, the solids handling equipment can also be utilized to transport the feedstock from the entrance to the exit of the desorption chamber. Examples of solids handling equipment that can be installed within the desorption chamber for use in conjunction with the present invention include augers, rotary kilns and drum or container breaching equipment. 
     Inside the desorption chamber, several mechanisms can be employed that operate alone or in combination to heat the feedstock. Sources of heat can include the use of conventional heating elements to heat the walls or solids handling equipment, the introduction of heated steam into the desorption chamber, and the heat generated from any exothermic reactions that occur in the desorption chamber. 
     From the desorption chamber, the volatile portion of the feedstock is transferred to a reactor for hydrothermal treatment, while the residue portion of the feedstock is removed from the desorption chamber for disposal. Preferably, a transfer pipe is used to establish fluid communication between the desorption chamber and the hydrothermal reactor to thereby transfer the volatile portion of the feedstock to the hydrothermal reactor. For the present invention, the volatile portion can be fed into a pipe reactor, downflow reactor or any other type of reactor suitable for hydrothermal treatment. 
     In the hydrothermal reactor, the volatile portion may be combined with an excess (20-100%) of oxidant and auxiliary fuel (if required). The reaction between the volatile portion, oxidant and auxiliary fuel is maintained at a temperature between approximately 1000° F. and approximately 1800° F. and a pressure of between approximately 20 atmospheres and approximately 200 atmospheres. The throughput of the reactor is controlled to cause the volatile portion of the feedstock to remain in the reactor for a sufficient residence time (10-60 seconds) to ensure complete oxidation of all organic species. After reaction, the effluent from the reactor can be further processed and then disposed. 
     Alternatively, addition of oxidant to the hydrothermal reactor may be reduced or eliminated, to allow organic reforming reactions to occur. Reactor temperature and pressure condition are again maintained at 1000-1800° F. and 20-200 atmospheres. 
    
    
     BRIEF DESCRIPTION OF THE DRAWINGS 
     The novel features of this invention, as well as the invention itself, both as to its structure and its operation, will be best understood from the accompanying drawings, taken in conjunction with the accompanying description, in which similar reference characters refer to similar parts, and in which: 
     FIG. 1 is a schematic diagram of a system in accordance with the present invention having a batch desorption chamber and a pipe reactor; and 
     FIG. 2 is a schematic diagram of a system in accordance with the present invention having a continuous desorption chamber and a vessel reactor. 
    
    
     DESCRIPTION OF THE PREFERRED EMBODIMENT 
     Referring to FIG. 1, a system in accordance with the present invention is shown and generally designated  10 . As shown in FIG. 1, the system  10  includes a desorption chamber  12  for volatilizing a portion of a feedstock  13 . For the present invention, the feedstock  13  can be any material having a volatile component that can be separated from the remaining feedstock and oxidized or reformed hydrothermally. Specifically applicable for the present invention are feedstocks having a viscous component (i.e. a component such as a solid, slurry or sludge that is not readily processable directly into a hydrothermal reactor). The feedstock  13  will also be contaminated with or partially or wholly composed of a volatile component that is hydrothermally treatable. Although the volatile component will typically be organic, it is to be appreciated that feedstocks having a volatile inorganic component that can be oxidized in the hydrothermal reactor are also ideal candidates for the present invention. Also suitable for the present invention are feedstocks  13  having contaminated liquids with high dissolved inorganic content, such as dense brines, acids or bases. These liquid streams can cause problems when fed directly into a hydrothermal reactor due to excessive salt buildup or corrosivity in the reactor. With the present invention, the organic constituents of such streams may be volatilized at a relatively low temperature, where salt buildup or corrosion are not an issue. 
     As shown in FIG. 1, the desorption chamber  12  can be covered with insulation  14  to allow retention of process heat. Additional desorption chambers  16  and  18 , similar to the desorption chamber  12 , can be provided to allow at least one desorption chamber  12 ,  16 , or  18  to be on line while the others are being loaded and unloaded with feedstock  13 . Heaters (not shown) can be used to heat the feedstock  13  in the desorption chambers  12 ,  16 ,  18  to facilitate volatilization of a portion of the feedstock  13 , at a typical operating temperature of 300-1500° F. Alternatively, steam can be introduced into desorption chambers  12 ,  16 ,  18  to heat the feedstock  13  and facilitate volatilization of a portion of the feedstock  13 . As shown, water can be withdrawn from tank  20  and raised to the system operating pressure of 20-200 atm by high pressure pump  22 . The pressurized water can be passed through a regenerative heat exchanger  24 , which heats the water by heat exchange with hot reactor effluent from pipe reactor  26 . Subsequent to the heat exchanger  24 , additional heating of the steam may be accomplished in preheater  28 . Preheat may be accomplished by an electrical heater as shown for preheater  28 , by a fired heater, by a combination of these methods, or by other suitable means known in the art. The temperature of the steam leaving the preheater  28  is preferably in the range of 300-1500° F. It is to be appreciated that the temperature of the feedstock  13  can be elevated by heaters in the desorption chambers  12 ,  16 ,  18 , the steam from preheater  28 , or the steam and heaters in combination. Further, for some feedstocks  13 , the heaters in the desorption chambers  12 ,  16 ,  18  can be employed during process startup and subsequently deactivated during steady state operation. 
     During operation of the system  10 , steam from the preheater  28  can be directed through one of the valves  30 ,  32  or  34  and into one of the desorption chambers  12 ,  16  or  18  to volatilize a portion of the feedstock  13  and thereby create a volatile portion and a residue portion of the feedstock  13 . The volatile portion combines with the steam and exits a desorption chamber  12 ,  16  or  18  into conduit  36  and flows toward pipe reactor  26 . Additionally, as shown in FIG. 1, steam from the preheater  28  can be caused to bypass the desorption chambers  12 ,  16 ,  18  directly through valve  38  for use in the pipe reactor  26 . 
     The volatile portion of feedstock  13  can be oxidized or reformed in the pipe reactor  26 . To carry out the oxidation reaction, liquid oxygen (LOX) can be supplied from tank  40  and pressurized by the high pressure cryogenic pump  42 . The pressurized liquid can be vaporized in vaporizer  44  and then passed to the reactor via line  46 . Optionally, some oxygen may be supplied to the desorption chambers  12 ,  16 , and  18  via line  48 . In some cases, oxygen may improve the volatilization of the organics and the oxidation reaction can supplement the heat needed for volatilization in the desorption chamber  12 ,  16 ,  18 . As shown, valves  50  and  52  can be used to split the oxygen between the desorption chamber  12 ,  16 ,  18  and the pipe reactor  26 . 
     Referring still to FIG. 1, a supplementary fuel stream may be provided to pipe reactor  26  to attain reactor temperatures sufficient for high destruction efficiency of the volatile portion of the feedstock  13 . Generally, the heating value of the steam with the volatile portion of the feedstock  13  is low, necessitating supplementary fuel. As shown in FIG. 1, supplementary fuel can be supplied from tank  54  and pumped to the pipe reactor  26  by high pressure pump  56 . The fuel, oxidant, steam, and volatile portion of feedstock  13  mix at the head of the pipe reactor  26 . Within the pipe reactor  26 , temperatures as high as 1800° F. are attained due to heat liberated by the oxidation reactions. Preferably, the temperature within the pipe reactor  26  is maintained between approximately 1000° F. and approximately 1800° F. and the pressure within the pipe reactor  26  is maintained between approximately 20 atmospheres and approximately 200 atmospheres. Feed rates of supplementary fuel, oxidant, and steam may be varied to accommodate varying concentrations of the volatile portion of feedstock  13  that may be entering the pipe reactor  26 . Residence time in the pipe reactor  26  is typically less than 30 seconds. 
     The reaction in the pipe reactor  26  creates a hot effluent that exits the pipe reactor  26  and is fed to a regenerative heat exchanger  24  for cooling. The resulting cool, high pressure stream can then be separated into liquid and gaseous streams in a separator  58 . Preferably, the gas and liquid are depressurized separately through valves  60  and  62 , respectively. The use of separate depressurization of the gas and liquid streams helps to minimize erosion of the pressure letdown valves  60  and  62 . 
     The depressurized gas and liquid can be fed to a collection tank  64 , as shown in FIG.  1 . From the collection tank  64 , the gas is passed to atmosphere through line  66 . If desired, a sampling port (not shown) can be installed in line  66 . If required, a carbon filter  68  can be installed in line  66  to remove any unoxidized organic material in the gas. The liquid from collection tank  64  may be sampled, released, or otherwise collected through line  70 . 
     Referring now to FIG. 2, an alternative embodiment of the present invention is shown. In this embodiment, contaminated feedstock  13 , as described above, can be fed into a lockhopper  72 . The feedstock  13  can be added to lockhopper  72  as a single batch, or added in a continuous or semicontinuous fashion. Lockhopper valve  74  is provided to intermittently introduce a portion of the feedstock  13  from the lockhopper  72  and into the head of the pressurized desorption chamber  76 . It is to be appreciated that lockhopper valve  74  operates as an airlock, allowing the pressure within the desorption chamber  76  to be maintained while feedstock  13  is introduced. 
     As shown in FIG. 2, an auger  78  can be installed in the desorption chamber  76  to move the feedstock  13  through the desorption chamber  76 . The wall of the desorption chamber  76  and/or the auger  78  can be heated to elevate the temperature of the feedstock  13  to a temperature of between approximately 300° F. and approximately 1500° F. Alternatively, a rotating drum (not shown) can be installed in the desorption chamber  76  to move and mix the feedstock  13  with the steam. For the present invention, it is contemplated that drums full of material may be used as a feedstock  13 . In this case, a pusher-feeder (not shown) may be installed in the desorption chamber  76  for manipulating the drums or other similar containers. Further, the pressure applied in the desorption chamber  76  can be used to crush and rupture closed containers such as drums, thus allowing any contained material to be exposed within the desorption chamber  76  for volatilization. Likewise, the container contents may expand due to the temperature in the desorption chamber  76 , causing container expansion and rupture and allowing exposure of the container contents. Alternatively, an in-situ breaching device (not shown) may be installed within the feed lockhopper  72  to expose the material in containers before insertion into the desorption chamber  76 . In this manner, volatiles can be released without overpressuring the closed container in the desorption chamber  76 . This allows the shape of the container to be maintained while being transported through the desorption chamber  76 . 
     As shown in FIG. 2, the desorption chamber  76  can be covered with insulation  80  to help retain the elevated operating temperature. In the course of traversing the desorption chamber  76 , the volatile portion of the feedstock  13  (which generally consists of organic constituents and moisture) are volatilized due to the elevated operating temperature. The volatilization of the feedstock  13  results in a residue portion which is generally a viscous material such as a solid, sludge or slurry and a volatile portion. At the tail end of desorption chamber  76 , the residue portion can be transferred into lockhopper  82 . Lockhopper valve  86  is provided to intermittently discharge the residue portion into a collection drum  84 . It is to be appreciated that lockhopper valve  86  can be constructed to operate as an airlock, allowing the pressure within desorption chamber  76  to be maintained during discharge of the residue portion. The volatile portion which generally consists of volatilized organics and moisture exits the desorption chamber  76  via line  88 . 
     Referring still to FIG. 2, steam can be introduced into the desorption chamber  76  to heat the feedstock  13  and facilitate desorption. As shown, water from tank  90  can be withdrawn and raised to the system operating pressure of between approximately 20 atmospheres and 200 atmospheres by high pressure pump  92 . The pressurized water can be passed through preheater  94  and raised to a temperature between approximately 300° F. and approximately 1500° F. Preheat may be accomplished by an electrical heater such as preheater  94 , by a fired heater, by a combination of these methods, or by other suitable means known in the art. Preheater  94  is also used to heat the desorption chamber  76  during startup from a cold condition. 
     During operation, steam from the preheater  94  can be directed through valve  96  and into the desorption chamber  76  for interaction with the feedstock  13 . As shown in FIG. 2, the feedstock  13  and steam are introduced at the same end of the desorption chamber  76  and subsequently flow within the desorption chamber  76  in the same direction (i.e. the feedstock  13  and steam are in co-current flow). In some implementations of the present invention, the steam and feedstocks  13  can be introduced at opposite ends of the desorption chamber  76  causing the feedstock  13  and steam to flow in opposite directions (i.e., countercurrent flow). Countercurrent flow can result in the production of a cleaner residue portion for some feedstocks  13 . Additionally, steam from the preheater  94  can be allowed to bypass the desorption chamber  76  through line  100  using valve  98 . The bypass steam flowing through line  100  can be introduced into reactor  102  for use in controlling the temperature within the reactor  102 . 
     Referring still to FIG. 2, a supplementary fuel stream may be provided for introduction into reactor  102  to attain reactor temperatures sufficient for high destruction efficiency of the volatilized organics in the volatile portion of the feedstock  13 . Generally, the heating value of the steam with the entrained organics in line  88  is low. As shown in FIG. 2, supplementary fuel can be supplied from tank  104  and pumped to the reactor  102  by high pressure pump  106 . From the pump  106 , the supplementary fuel passes through line  108  for mixture with the volatile portion of the feedstock  13  and steam from line  88  and the optional steam from line  100 . The mixed stream enters line  110  and proceeds toward the reactor  102 . 
     Regardless of whether the volatile portion of the feedstock  13  is to be completely oxidized or only reformed in vessel reactor  102 , an oxidant may be required. For the present invention, the oxidant used can be oxygen as described above, air, enriched air or any other oxidant known in the pertinent art such as hydrogen peroxide. As shown in FIG. 2, ambient air can be compressed to high pressure using a high pressure air compressor  112 . From the compressor  112 , the air enters line  114  and proceeds toward the reactor  102 . In addition, it is sometimes desirable to add alkali to the reactor  102  to neutralize acidic constituents such as hydrogen chloride or sulfuric acid that can be formed when organic material containing heteroatoms is oxidized. FIG. 2 shows alkali supply tank  116 , from which alkali such as sodium hydroxide solution can be introduced to the process via high pressure pump  118 . From the pump  118 , the alkali solution can be passed through line  120 , mixing with air from line  114  and the volatile portion of feedstock  13 /steam mixture from line  110 . The mixed stream then enters the reactor  102  via line  122 . The order of mixing the various feeds to the reactor  102  can vary depending on feed. In some cases, the streams can be mixed before entering the main reactor  102 . 
     Feed rates of supplementary fuel, oxidant, and steam may be varied to accommodate varying concentrations of organics or other oxidizable materials in the volatile portion of the feedstock  13  that is entering the reactor  102 . Alternatively, a control device such as a hot valve (not shown) may be incorporated to regulate the flow of volatiles from the desorption chamber  76  to the reactor  102  to aid steady reactor operation. In another embodiment of the present invention, a control circuit (not shown) can be used to vary either the temperature within the desorption chamber  76  or the feed rate that feedstock  13  is introduced in the desorption chamber  76 . Specifically, a control circuit can be employed to vary the heating rate or feed rate in response to the measured flow rate of volatiles entering the reactor  102 . 
     As shown in FIG. 2, the reactor  102  can be covered with insulation  124  to help preserve the heat of reaction and achieve a high degree of oxidation. For the present invention, the reactor  102  may be of the type described in U.S. Pat. No. 6,054,057 to Hazlebeck, et al., entitled “Downflow Hydrothermal Oxidation,” and which is assigned to the same assignee as the present invention. As described in the &#39;057 patent, it is sometimes desirable to introduce a quench stream at the bottom of the reactor  102  to cool the reaction stream and dissolve any salts that may have formed in the reactor  102 . In FIG. 2, quench water can be supplied to the reactor  102  from tank  126  via high pressure pump  128  and line  130 . For the present invention, a scraper device (not shown) can be installed in the reactor  102  to mitigate deposition of solids on the inner wall of the reactor  102 . Alternatively, a mechanical device such as an auger (not shown) can be installed in the reactor  102  to aid solids removal from the reactor  102 . 
     In operation, the heat created by the oxidation reaction is often sufficient to maintain the temperature in the reactor  102  at the desired operation level, which is between approximately 1000° F. and approximately 1800° F. The feed rates into and out of the reactor  102  can be adjusted to obtain a desired residence time in the reactor  102  which is typically less than 30 seconds. In the reactor  102 , the intimate gas-liquid contact ensures that emissions of particulates, acid gases and metals are within the most stringent environmental regulations. Because of the rapid internal thermal quench, dioxins, difurans and other typical byproducts of conventional waste oxidation are not formed in the well-mixed HTO reactor. The feed rates and operating conditions in the reactor  102  can be adjusted to completely oxidize the volatile portion of the feedstock  13  or reform it into a fuel gas or synthesis gas. For reformation, substoichiometric or no oxygen is added to the feedstock  13  at the reactor  102 , allowing the organics to reform. Operating pressures for gasification are similar to those used for complete oxidation, however, preferred gasification temperatures can range somewhat higher than those used for oxidation, for example as high as 1800° F. 
     As shown in FIG. 2, a heat exchanger  132  is provided to cool the effluent exiting the reactor  102  through line  131 . Although a quench stream is preferably used in the reactor  102 , the quenched effluent may still exit the reactor  102  at a temperature of approximately 500° F. The cool, high pressure stream that exits from the heat exchanger  132  is forwarded to a separator  134  for separation into liquid and gaseous streams. The gas and liquid streams are depressurized separately through valves  136  and  138 , respectively. This technique of separate depressurization of the gas and liquid streams helps to minimize erosion of the pressure letdown valves  136  and  138 . 
     As shown in FIG. 2, the depressurized gas and liquid streams proceed from the letdown valves  136 ,  138  and into a collection tank  140 . From the collection tank  140 , the gas fraction passes through line  142 , and may be sampled if desired. An optional carbon filter  144  can be provided in line  142  to remove unoxidized organic material, if required. Optionally, a mechanism (not shown) for removing and liquefying carbon dioxide from the gas can be installed in line  142  to reduce greenhouse gas emissions. The liquid from collection tank  140  may be sampled, released, or otherwise collected through line  146 . If required, a mechanism (not shown) for polishing the liquid effluent can be installed in line  146  to remove dissolved or particulate metals. 
     As an alternative to the designs shown in FIGS. 1 and 2, it is also possible to use a single pressure vessel with two zones, one zone for volatilization and a second for oxidation or reforming. For example, a container having a screened opening can be used to hold the feedstock. The container can be placed inside a pressure vessel. Volatiles released from the container can be oxidized or reformed in the remaining portion of the pressure vessel. 
     While the particular devices and methods as herein shown and disclosed in detail are fully capable of obtaining the objects and providing the advantages herein before stated, it is to be understood that they are merely illustrative of the presently preferred embodiments of the invention and that no limitations are intended to the details of construction or design herein shown other than as described in the appended claims.

Technology Classification (CPC): 2