Abstract:
A method is provided of recycling and decontaminating oil-based waste drilling mud and cuttings contaminated with oil-based waste drilling mud. A facility for performing the method is also provided. The method includes removing the coarse solids from the mud, breaking the emulsion, and separating the hydrophobic phase from the water phase and the solid phase. The solids may then be treated by either or both of two approaches. One approach involves vaporizing all residual oil and water from the solids, and burning off the vaporized oil. Another approach involves at least partially vaporizing the residual oil from the solids and recondensing the oil. The method produces a solid “soil” product that is free from oil contamination (or is sufficiently decontaminated to allow reuse), an oil product that is fit for reuse, and clean air emissions. A thermal desorber or a soil dryer can be used to efficiently vaporize the oil at low temperature. Optionally the water fraction of the mud can be vaporized, solutes and salts can be captured as evaporite and then be mixed with the soil product. The method has the unique advantage of producing no persistent hazardous waste. The method has the further advantage of requiring no external input of energy if the reclaimed oil is used to provide energy for the process. The method has the further advantage of recycling portions of the drilling mud that would otherwise be subject to disposal.

Description:
CROSS-REFERENCE TO RELATED APPLICATIONS 
       [0001]    This application is a continuation-in-part of U.S. application Ser. No. 12/313,750, which was filed on Nov. 24, 2008, and which is currently pending. U.S. application Ser. No. 12/313,750 is incorporated by reference in its entirety into this application. 
     
    
     FIELD OF THE DISCLOSURE 
       [0002]    The field of the disclosure is environmental protection. More specifically, the field of the disclosure is technology directed to the treatment and recycling of drilling muds. 
       BACKGROUND 
       [0003]    Drilling through rock generally requires the use of some type of fluid to clear cuttings from the bore hole formed by the drill. In some applications, the drilling fluid can be as simple as compressed air. However, when drilling is conducted to tap fossil fuel resources, the drilling fluid used is usually a “drilling mud.” Drilling muds are generally placed in three categories, depending on the major fluid component: water-based, oil-based, and pneumatic. In the natural gas industry, oil-based muds predominate. 
         [0004]    Oil-based muds serve several functions during drilling: removing cuttings from the well, suspending the cuttings, controlling formation pressure, sealing permeable formations, stabilizing the wellbore, reducing formation damage, cooling the drill, lubricating the drill, transmitting hydraulic energy to tools and the bit, and reducing corrosion. Oil-based drilling muds typically comprise a hydrocarbon-water emulsion, an emulsifier, and clay. Bentonite is the most widely used clay in drilling muds, although other clays can be used. Other ingredients are often present. Barite, for example, is often used as a weighting agent to increase the outward hydrostatic pressure in the borehole. 
         [0005]    Typically, used drilling mud will be recirculated through a drill and borehole at the drill site. The larger cuttings are removed from the mud prior to recirculation. This is generally achieved by running the used mud over a shaker screen. This collects the drill cuttings, which are mixed with drilling mud and groundwater. The waste drilling mud and the cuttings are then subject to disposal, either with or without some form of treatment. In some situations an unused drill mud must be subject to disposal. This can occur for example if a mud is stored for too long, and loses some of its beneficial properties. All such muds, used or unused, are referred to in this disclosure as “waste drilling mud.” 
         [0006]    Disposal of waste drilling muds is a major problem in the art. Diesel is commonly used as an oil in drilling muds. Diesel poses environmental hazards, so diesel-based mud must be deposited in special landfills constructed with an impermeable lining. This is expensive, and the possibility remains that the hazardous components of the mud could leak from the landfill, damaging the environment and exposing all parties involved to toxic cleanup liability. Used drilling muds may also contain groundwater with high salt concentrations. Such saline water can also be environmentally harmful if not disposed of properly; its disposal is similarly expensive and can constitute a continuing threat to the environment with attendant legal liabilities. The task of disposal of drilling muds is complicated by the complex, multi-phase nature of the muds, which makes it difficult to isolate the hazardous components to reduce disposal volumes. 
         [0007]    Even when the bulk oil fraction of a drilling mud is separated and purified, residual organic compounds often remain tightly associated with solids in the mud (either the clay or drill cuttings), requiring disposal as a hazardous substance. Methods for completely removing hydrocarbons from the solid phase, such as steam distillation, are energy-intensive and inefficient. Solvent-based methods of hydrocarbon separation from the solid phase merely compound the problem by the introduction of hazardous solvent. Combustion of the liquid hydrocarbon in emulsion requires very high operating temperatures and can be a source of air pollution. Combustion of liquid hydrocarbon when mixed with the solid phase is problematic, as it requires the facility be licensed as an incinerator. 
         [0008]    If the hydrocarbon fraction is effectively removed, the remaining components of most waste drilling muds (water, clay, and possibly cuttings) are not hazardous, and may be disposed of without special protective measures or reused for muds or other purposes. When waste mud contains saline water, disposal of the aqueous fraction may pose a problem. Although salt concentrations in “saline” groundwaters are low compared to marine waters, they are often sufficiently high to damage soils and bodies of freshwater. Saline water may be disposed of by storage in a lagoon, in which the water slowly evaporates and the salt precipitates. Although this method greatly reduces the volume of the waste material, the concentrated salt evaporite that remains can be highly damaging to soil and groundwater, and requires either alternative disposal or further treatment. Another method of disposal is permanent storage of the saline water in an impermeable landfill. This method is expensive, may result in leaks, and is not available in every location. 
         [0009]    Consequently, there is a long-felt need in the art for a method of waste drilling mud disposal that requires no disposal of hydrocarbons and creates no persistent pollution. There is another long-felt need in the art for a method of waste drilling mud disposal that requires no disposal of saline water. There is another long-felt need in the art for a method of treatment of waste drilling mud that requires no disposal of hazardous pollutants. There is a further long-felt need in the art for a method of cost-effective diesel recycling from drilling mud. 
       SUMMARY 
       [0010]    The disclosure teaches a method of treating waste drilling muds that produces substantially no persistent pollution, its only products being either non-hazardous or fully reusable. The method generally includes a crude separation of larger solid particles from the liquid phase, the separation of the aqueous and oil sub-phases of the liquid phase, and the recovery of the hydrophobic phase as a reusable oil product (such as diesel). These steps may be followed by the removal of pollutants from the solid particles. 
         [0011]    In some embodiments of the method, a residual organic phase is at least partially vaporized from the solid particles and recondensed. Any non-recondensed gaseous organics may then be combusted. The condensate can then be recycled as a component of drilling mud or as fuel. In some embodiments of the method, substantially all organics are removed from the solid particles (either after the above described vaporization and recondensation step or in the absence of that step) by vaporization and combustion of all of the vaporized organics, and emission of the clean combustion products. The only products of the method are water, a clean solid product, flue gasses, and reusable organic product (in some cases, a reusable diesel product). The solid product and flue gasses are substantially free of pollutants, and the organic product can be safely reused, for example in new drilling mud or as a fuel. The methods disclosed serve the additional purposes of recycling drilling muds, recycling diesel fuel, disposing of saline water, and preventing pollution. 
         [0012]    Optionally the method also includes disposing of the aqueous phase through vaporization. Some solutes in the aqueous phase, notably salts, will form an evaporite upon vaporization of the aqueous phase. The evaporite can then be captured and disposed of for example by dilution in the clean solid product. The water vapor can then be harmlessly emitted to the atmosphere. 
         [0013]    The disclosure also teaches a method of treating a waste drilling mud. In some embodiments of the method, the waste drilling mud comprises a bulk emulsion and a drilling mud solid, wherein the bulk emulsion comprises a hydrophobic phase and an aqueous phase. Such embodiments of the method comprise: separating a fraction of the drilling mud solid from the waste drilling mud, the fraction comprising a residual organic phase; demulsifying the bulk emulsion, to form a demulsified hydrophobic phase and a demulsified aqueous phase; and separating the demulsified hydrophobic phase from the demulsified aqueous phase, to create an aqueous product and an oil product, wherein the oil product is suitable for reuse. Some embodiments of the method further comprise vaporizing the residual organic phase from said fraction of the drilling mud solids, to create an organic vapor and a first solid product. 
         [0014]    Some embodiments of the method further comprise a vaporization/combustion step. The vaporization/combustion step may be performed on either or both of the fraction of the drilling mud solids or the first solid product. When the solid material is the fraction of the drilling mud solids, embodiments of the method comprise removing substantially all the residual organic phase from said fraction of the drilling mud solids, to create an organic residue vapor and a second solid product (regardless of whether the method produces the first solid product) which is a clean solid product by a process comprising vaporizing the residual organic phase; wherein the second solid product is substantially free from organic pollutants; combusting substantially all of the organic residue vapor under conditions sufficient to ensure substantially complete combustion, to create a clean gaseous product; and discharging the clean gaseous product to create a clean gaseous discharge, wherein the clean gaseous discharge is substantially free from solids, organics, or pollutants. When the solid material is the first solid product, embodiments of the method comprise removing substantially all of an organic residue from the first solid product by a process comprising vaporizing the organic residue to form an organic residue vapor, and combusting substantially all organic residue vapor to create a clean gaseous product that may be discharged. 
         [0015]    The disclosure also teaches a method of producing a reusable oil product from the waste drilling mud. Some embodiments of the method comprise: removing a first fraction of the drilling mud solids, the first fraction comprising particles above a first diameter; removing a second fraction of the drilling mud solids, the second fraction comprising particles above a second diameter; adjusting the viscosity of the drilling mud to below about 45 seconds Marsh funnel at 150° F.; demulsifying the bulk emulsion to create a hydrophobic phase and an aqueous phase in the waste drilling mud; at least partially separating the hydrophobic phase from the aqueous phase; and removing a third fraction of drilling mud solids to create a reusable oil product, the third fraction comprising particles above a third diameter. 
         [0016]    The disclosure also teaches a method of disposing of a saline groundwater of a waste drilling mud. Some embodiments of the method are a method of disposing of a saline groundwater of a waste drilling mud, the waste drilling mud comprising a bulk emulsion and a drilling mud solid, the bulk emulsion comprising an oil and the saline groundwater, the method comprising: removing a first fraction of the drilling mud solids, the first fraction comprising particles above a first diameter; removing a second fraction of the drilling mud solids, the second fraction comprising particles above a second diameter; adjusting the viscosity of the drilling mud to below about 45 seconds Marsh funnel at 150° F.; demulsifying the emulsion to create a hydrophobic phase and an aqueous phase; at least partially separating the hydrophobic phase from the aqueous phase to form a reusable oil product; and removing a third fraction of drilling mud solids, the third fraction comprising particles above a third diameter; vaporizing the aqueous phase to form a water vapor and an evaporite; capturing the evaporite; and releasing the water vapor substantially free from pollutants. 
         [0017]    The disclosure also provides a method of removing organic pollutants from a drilling mud solid. Some embodiments of the method comprise: obtaining a waste drilling mud comprising a bulk emulsion and the drilling mud solid, the bulk emulsion comprising an oil and water; and removing a first solid fraction of the drilling mud solid from the waste drilling mud, the first solid fraction comprising a residual organic phase. Some embodiments of the method further comprise vaporizing the residual organic phase from said fraction of the drilling mud solids, to create an organic vapor and a first solid product, and recondensing the residual organic phase. Some embodiments of the method further comprise removing substantially all of the residual organic phase from the first solid product by a removal process comprising vaporizing the residual organic phase to create an organic residue vapor. 
         [0018]    The disclosure also teaches a facility for treating waste drilling muds. Some embodiments of the facility comprise: a dryer; and a three phase centrifuge linked to receive material from the dryer. Some embodiments of the facility further comprise a low-temperature thermal desorber; an oxidizer linked to receive material from the low-temperature thermal desorber, the oxidizer comprising an oxidant inlet and a fuel inlet; a baghouse linked to receive material from the oxidizer; and a flue linked to receive material from the baghouse. Some embodiments of the facility further comprise a soil dryer and a condenser linked to receive vapor from the soil dryer. 
     
    
     
       BRIEF DESCRIPTION OF THE FIGURES 
         [0019]      FIG. 1 . Schematic of an embodiment of the facility showing elements of the first stages of processing, wherein the waste drilling mud is separated into an oil product, a demulsified aqueous phase, and a solid fraction. 
           [0020]      FIG. 2 . Schematic of an embodiment of the facility showing elements of the second stages of processing, wherein the solid fraction is processed to form a first solid product and a distilled oil product. 
           [0021]      FIG. 3 . Schematic of an embodiment of the facility showing elements of a stage of processing that may follow either of the first and second stages of processing, wherein a solid fraction or product is processed to product a second clean solid product and a clean gaseous discharge. Wastewater may also be treated. 
           [0022]      FIG. 4 . Detailed schematic of an embodiment of the facility. 
       
    
    
     DETAILED DESCRIPTION 
       [0023]    This description illustrates and describes the processes, machines, manufactures, compositions of matter, and other teachings of the present disclosure. Additionally, the disclosure shows and describes only certain embodiments of the processes, machines, manufactures, compositions of matter, and other teachings disclosed, but it is to be understood that the teachings of the present disclosure are capable of use in various other combinations, modifications, and environments and are capable of changes or modifications within the scope of the teachings as expressed herein, commensurate with the skill and knowledge of a person having ordinary skill in the relevant art. The embodiments described are further intended to explain certain best modes known of practicing the processes, machines, manufactures, compositions of matter, and other teachings of the present disclosure and to enable others skilled in the art to utilize the teachings of the present disclosure in such, or other, embodiments and with the various modifications required by the particular applications or uses. Accordingly, the processes, machines, manufactures, compositions of matter, and other teachings of the present disclosure are not intended to limit the exact embodiments and examples disclosed herein. 
       A. DEFINITIONS 
       [0024]    All terms used in this disclosure should be construed as encompassing both the singular and the plural form of the term, unless specified otherwise. 
         [0025]    The term “including” as used herein is non-exclusive, and can be read as synonymous with “including but not limited to.” 
         [0026]    The term “cutting” as used herein refers to mineral material that is dislodged from rock strata during drilling. 
         [0027]    The term “aqueous phase” as used herein refers to a liquid having a relatively high polarity and being substantially immiscible with oils; the aqueous phase may exist as a mixture (including an emulsion) with oils or other non-aqueous liquids. 
         [0028]    The term “water” as used herein refers to liquid H 2 O substantially free of any immiscible solvents, and which may or may not contain solutes. 
         [0029]    The term “pollutant” as used herein refers to any substance the release of which is either legally regulated or is generally known to be harmful to human health and the environment, either directly through toxic effects or indirectly; whether a substance is a pollutant is partially determined by extrinsic properties, such as the amount of the substance. 
         [0030]    The term “linked to receive material from” indicates an element or structure arranged such that a material can be transported from another element or structure. Such transport can be suitable for liquids, solids, gasses, or mixtures thereof. Elements so linked may be connected by pipes, channels, conduits, conveyors, or any other means known in the art. The linkage need not be direct, and additional structures or elements may intervene between the linked elements. 
         [0031]    The term “linked to transmit material to” indicates an element or structure arranged such that a material can be transported to another element or structure. Such transport can be suitable for liquids, solids, gasses, or mixtures thereof. Elements so linked may be connected by pipes, channels, conduits, conveyors, or any other means known in the art. The linkage need not be direct, and additional structures or elements may intervene between the linked elements. 
         [0032]    The term “waste drilling mud” indicates a drilling mud intended for disposal, whether used or unused. 
       B. WASTE DRILLING MUD PROCESSING FACILITY 
       [0033]    The disclosure provides facilities for providing any of the methods disclosed herein. The disclosure provides a waste drilling mud processing facility comprising: a dryer  2 , a three phase centrifuge  10  linked to receive material from the dryer  2 . The facility may further comprise an oil product collection tank  26  linked to receive material from the three phase centrifuge  10 , and a water conduit  25  linked to receive material from the three phase centrifuge  10 . Some embodiments of the facility further comprise a low-temperature thermal desorber  15 , an oxidizer  21  comprising an oxidant inlet  28  and a fuel inlet  29  linked to receive material from the low-temperature thermal desorber  15 , a baghouse  24  comprising a baghouse filter  25  linked to receive material from the oxidizer  21 , and a flue  31  linked to receive material from the baghouse  24 . Some embodiments of the facility further comprise a soil dryer  61  and a condenser  55  linked to receive vapor from the soil dryer  61 . Some embodiments of the facility comprise at least one of the following: a debris screen  32  linked to transmit material to the dryer  2 ; a receiving tank  33  linked to transmit material to the dryer  2 ; a dryer liquid tank  6  linked to receive material from the dryer  2  and linked to transmit material to the three phase centrifuge  10 ; a decanter centrifuge  7  linked to receive material from the dryer  2  and linked to transmit material to the three phase centrifuge  10 ; a raw stock holding tank  34  linked to receive material from the dryer  2  and linked to transmit material to the three phase centrifuge  10 ; a soil conditioner  18  linked to receive material from the thermal desorber  15 ; a cyclonic separator  20  linked to receive material from the low temperature thermal desorber  15  and linked to transmit material to the oxidizer  21 ; and a quench chamber  22  linked to receive material from the oxidizer  21  and linked to transmit material to the baghouse  24 . Each of the elements may be linked to receive material from or transmit material to other elements, depending on their configuration. 
         [0034]      FIG. 1  partially illustrates one such embodiment of the facility, showing the elements involved in the separation of the waste drilling mud  44  into a solid fraction  40 ,  41 ,  42 , and demulsified aqueous phase  43  and an oil product  50 . In the illustrated embodiment the waste drilling mud  44  is passed through a debris screen  32  into a receiving tank  33 . Waste drilling mud is then transported to the dryer  2 , where a fraction of the drilling mud solids  40  is removed. The remaining waste drilling mud  44  is then transported to the dryer liquid tank  6 , and then to a decanter centrifuge  7 . The decanter centrifuge removes a second fraction  41  of drilling mud solids. The remaining waste drilling mud  44  is then transported to a second decanter centrifuge  35 . The second decanter centrifuge  35  removes a third fraction  52  of drilling mud solids. The remaining waste drilling mud  44  is then transported to an additional decanter centrifuge  51 . The additional decanter centrifuge  51  removes an additional fraction  42  of drilling mud solids. The remaining waste drilling mud  44  (now referred to as “raw stock”) is transported to a raw stock holding tank  34 . Depending on the viscosity of the waste drilling mud  44 , the waste drilling mud  44  is then transported to one of an emulsion treatment tank  36  or the decanter centrifuge  7 . Agents are added to demulsify the emulsion, including an acid  47 , an oxidant  48 , and a demulsifier  49 . The waste drilling mud  44  is then transported to a three-phase centrifuge  10 . The three-phase centrifuge  10  separates the waste drilling mud  44  into three components: a fourth fraction  53  of drilling mud solids, a demulsified aqueous phase  43 , and an oil product  50 . The demulsified aqueous phase  43  is transported to a reservoir  38 . The oil product  50  is transported to one or more solids separation cells  64  and then to an oil product collection tank  26 . Oil product  50  in the oil product collection tank  26  can then be distributed by means of a pipeline  14  or a tanker vehicle  13 . 
         [0035]      FIG. 2  illustrates elements of the embodiment of the facility involved in at least partially vaporizing the residual organic phase. This section of the facility accepts the solid fractions  40 - 42   52   53 . The solid fractions  40 - 42   52   53  are fed into at least one soil dryer  61 , wherein the residual organic phase is at least partially vaporized from the solids. Any residual water in the solid fractions  40 - 42   52   53  is also vaporized. A condenser  55  is linked to receive vapor from the soil dryer  61  and recondense the vaporized organics. The vaporized water may be recondensed. Recondensed water  63  may then be used in the quench chamber  22  or the soil conditioner  18 , or it may be emitted to the atmosphere. The recondensed organics may be recycled for various purposes depending on the composition of the recondensed organics. This produces a first solid product  56  containing a small amount of organic material, and substantially free from water, that can be reused for various applications, such as road base material or fill. The first solid product  56  may contain evaporite resulting from vaporization of water from the solids. Any uncondensed organic vapor  65  may be fed to scrubbers  57  (as may the water vapor  66 ), and the scrubbed gaseous product may be sent to a baghouse  24  and released. 
         [0036]      FIG. 3  partially illustrates elements of the embodiment of the facility involved in completely removing organics from solids. This section of the facility can accept any of the solid fractions  40 - 42   52   53  or the first solid product  56  (referred to collectively as the “solid desorber feed”). The solid desorber feed is introduced to a direct-fired counter-current low temperature thermal desorber  16  having a desorber fuel inlet  39 . Any organic residue is vaporized to form an organic residue vapor and run through a dual cyclone  19 . The remaining solids are fed into a soil conditioner  18  and combined with water, to form the second solid product  46 . Any solids removed by the dual cyclone  19  are also fed into the soil conditioner  18 . The organic residue vapor that passes through the dual cyclone  19  is transported into an oxidizer  21  having a fuel inlet  29 , an oxidant inlet  28 , and optionally a water inlet  27 . The organic residue vapor is completely combusted, and the hot products of combustion are fed into a quench chamber  22  having a water inlet  23 , whereby cooling water is sprayed into the quench chamber  22 . The cooled gasses then pass into a baghouse  24  and through a bag filter  25 . Any solids retained by the bag filter  25  are fed into the soil conditioner  18 . The cooled gasses are emitted through a flue  31  to form a clean gaseous discharge  45 . 
         [0037]    Some embodiments of the facility further comprise any of a debris screen  32 ; a receiving tank  33  linked to transmit material to the dryer and linked to receive material from the debris screen  32 ; a dryer liquid tank  6  linked to receive material from the dryer  2 ; a decanter centrifuge  7  linked to receive material from the dryer liquid tank  6 ; a second decanter centrifuge  35  linked to receive material from the decanter centrifuge  7 ; a raw stock holding tank  34  linked to receive material from the second decanter centrifuge  35 ; an emulsion treatment tank  36  linked to receive material from the raw stock holding tank  34  and linked to transmit material to the three phase centrifuge  10 ; a soil conditioner  18  linked to receive material from the thermal desorber  15 ; a cyclonic separator  20  linked to receive material from the thermal desorber  15  and linked to transmit material to the oxidizer  21 ; and a quench chamber  22  linked to receive material from the oxidizer  21  and linked to transmit material to the baghouse  24 . Liquid produced by the decanter centrifuges  7 ,  35  may be treated in one or more agitated and heated process tanks  62  prior to being channeled to the subsequent step. 
         [0038]    Some embodiments of the facility further comprise an additional decanter centrifuge  51  linked to receive material from at least one of the dryer  2 , the liquid dryer tank  6 , the decanter centrifuge  7 , and the second decanter centrifuge  35 . 
         [0039]    In some embodiments of the facility, a flocculant inlet  53 , feeds flocculant  52  into at least one of the additional decanter centrifuge  51 , the decanter centrifuge  7 , and the second decanter centrifuge  35 . 
         [0040]    As explained herein, the dryer  2  may be any dryer known in the art to be suitable for separating solids from waste drilling mud, high-viscosity liquids, emulsions, or oils including a processing centrifugal dryer  37  or a vertical centrifugal dryer  4 . 
         [0041]    The three phase centrifuge  10  linked to receive material from the dryer  2  can be any such apparatus known to those skilled in the art suitable for separating an hydrophobic phase from an aqueous phase and solids of up to a given diameter. In some cases the given diameter will be predetermined, for example during design or operation. 
         [0042]    The oil product  50  collection tank  26  linked to receive material from the three phase centrifuge  10  can be any suitable vessel or tank. 
         [0043]    The water conduit  27  linked to receive material from the three phase centrifuge  10  may be any suitable conduit, for example a pipe. The water conduit  27  may be linked to transmit water to a reservoir  38 . In some embodiments of the facility, the water conduit  27  is linked to transmit water to at least one of the following: the thermal desorber  15 , the soil conditioner  18 , the oxidizer  21 , and the quench chamber  22 . 
         [0044]    Some embodiments of the soil dryer  61  is a screw heat exchanger  54 . The screw heat exchanger  54  is a screw conveyer in which the drive screw itself is heated. Generally the heat is supplied internally to the drive screw, for example by circulating a hot fluid through the shaft. The heat may be supplied for example by a circulating fluid heated by a boiler, and the boiler in turn may be fueled by the oil product of the process (or by any other suitable fuel). The heated fluid could also be the clean gaseous product of the process. The temperature of the screw heat exchanger  54  may be varied along its length. Alternatively, multiple screw heat exchangers  54  may be employed to expose the material to a variety of temperatures. The screw heat exchanger  54  will be maintained at a temperature that is at least the boiling temperature (or sublimation temperature) of the component to be removed. For example, a first screw heat exchanger  54  could be maintained at or above the boiling point of water, but below the boiling point of the residual organic phase, to dry the solid fraction prior to the vaporization of the residual organic phase. Water vapor  66  can then be discharged, and the remaining solid and organic material fed into a higher temperature screw heat exchanger  54  to at least partially vaporize the residual organic phase. The temperature of each heat exchanger  54  (or each section of heat exchanger) can be set to vaporize only a certain desired fraction of the residual organic based on the known vapor pressures and boiling points of such fractions, as is understood by those skilled in the art. Such fractions may include drilling mud additives that improve the properties of the drilling mud. Recovery of such additives can increase the value of the recondensed organic fraction. 
         [0045]    In an exemplary embodiment, the screw heat exchanger  54  either maintains a temperature gradient, or multiple screw heat exchangers  54  are used to vary the temperature of the process. A first heat exchanger temperature of about 180-220° F. selectively vaporizes water, which can be discharged without further treatment; in some embodiments of the method, the first heat exchanger temperature is about 200° F. A second heat exchanger temperature of about 500-750° F. at least partially vaporizes the residual organic phase. A third heat exchanger temperature of about 300° F. cools the first solid product. 
         [0046]    Although many types of soil dryer  61  can adequately remove residual hydrocarbon pollutants from solids, it has been unexpectedly discovered that the screw heat exchanger  54  has numerous advantages in the recovery of the organic fraction from drilling muds. A screw heat exchanger  54  has the advantage of maintaining a low volume of air, which allows for precise control of temperature and concentrates the gaseous products of heating. Screw heat exchangers  54  produce high temperatures without subjecting their contents to combustion, preventing valuable components of the drilling mud from being oxidized. Oxygen concentrations can be reduced or minimized to prevent oxidation at high temperatures, owning to the aforementioned low volume of air within a screw heat exchanger  54 . The temperature of a screw heat exchanger  54  can vary with the location within the screw-auger structure, and the temperature can be precisely controlled. As a result, very specific fractions of the drilling mud can be recovered, such as commercially valuable additives. Previously, there was no known method of recycling such components selectively. 
         [0047]    The condenser  55  can be any suitable condenser known in the art. The condenser  55  will cool the organic vapor  65  to below its boiling point, causing the organic vapor  65  to condense as a liquid. If only a certain component or fraction of the organic vapor  65  is desired, the condenser temperature may set according to the boiling point of the certain component or fraction. 
         [0048]    In some embodiments of the facility, uncondensed organic vapor is transmitted to a second oxidizer  59 . The second oxidizer  59  may be of any kind that is suitable as the first oxidizer  21  (often referred to in this description mere as “the oxidizer”) as described below. Optionally water from any source may be transmitted to the second oxidizer  59  for the purpose of controlling the temperature of the oxidizer  59  or to allow separation of solutes from the water as evaporite. 
         [0049]    The low-temperature thermal desorber  15  can be of any type known to those skilled in the art, as explained herein, including a direct-fired countercurrent rotary dryer  16 . The low-temperature thermal desorber  15  may comprise a desorber fuel inlet  39 . In some embodiments of the facility the fuel inlet  39  of the desorber is linked to receive material from the oil product  50  collection tank  26  or linked to receive the hydrophobic phase (or demulsified hydrophobic phase) from the three-phase centrifuge  10 . 
         [0050]    The oxidizer  21  linked to receive material from the low-temperature thermal desorber  15  comprises an oxidant inlet  28  and a fuel inlet  29 . As explained elsewhere herein, the oxidizer  21  must be capable of performing under operating conditions to assure substantially complete combustion of the organic vapor. 
         [0051]    The quench chamber  22  may be configured to allow the clean gaseous product to expand and undergo expansive cooling. In some embodiments of the facility the quench chamber  22  is linked to receive quench water from the water conduit  27 . 
         [0052]    The soil conditioner  18  may be linked to receive conditioning water from the water conduit  27 . 
         [0053]    The baghouse  24  linked to receive material from the oxidizer  21  comprises a bag filter  30 . The baghouse  24  can be of any design understood by those skilled in the art. 
       C. METHODS OF TREATING WASTE DRILLING MUD 
       [0054]    The instant disclosure provides methods for processing a waste drilling mud  44 . The waste drilling mud  44  may be used or unused. A used drilling mud may comprise drilling mud solids, such as a plurality of drill cuttings, clay, and barite. In fact, a used drilling mud may comprise over 50% drill cuttings by weight, or be nearly entirely drill cuttings by weight. Such a composition is still referred to as a drilling mud. Some, but not all, drilling muds contemplated by this disclosure comprise at least one of the following: an oil, water, oil and water in a bulk emulsion, an emulsifier, additives, solutes, and solids. 
         [0055]    The drilling mud contemplated is an oil-based drilling mud. The oil may be a fuel oil. If the oil is a fuel oil, it can be any class of fuel oil, including numbers 1, 2, 3, 4, 5 or 6 fuel oil (alone or in any combination). In some embodiments the fuel oil is a bunker fuel or a heating oil. In some embodiments, the oil is diesel. Oil-based drilling muds based on diesel are commonly based on petroleum derived diesel (“petrodiesel”), but a mud based on diesel derived from plant oils (“biodiesel”) will work in some embodiments of the method also. The oil may be present in an emulsion or a “reverse emulsion” (in which an aqueous phase is emulsified within a hydrophobic phase). The oil may contain organic additives to improve the properties of the drilling mud. 
         [0056]    Some embodiments of the methods and facilities of this disclosure can be applied to a used drilling mud that also contains drilling mud solids other than cuttings. Such drilling mud solids may include a clay; that clay may be a Bentonite, another clay, or a combination of clays. Barite may also be included. 
         [0057]    If the used drilling mud contains drilling mud solids (cuttings or otherwise) with high organic content, additional treatment may be required to achieve the desired separation and cleanup of the different fractions of the used drilling mud. If the drilling mud solids contain inorganic pollutants, such as radionuclides or heavy metals, additional treatment may be necessary to adequately address the inorganic pollutants. Ideally the used drilling mud solids are free from inorganic pollutants. 
         [0058]    Some embodiments of the methods and facilities of this disclosure can be applied to a used drilling mud that also contains water, including water in an emulsion or a reverse emulsion. The water is also referred to as an “aqueous phase.” The water may be present at any concentration. The water may contain solutes at any concentrations. In some embodiments, the water contains salts. The water may contain salts up to their saturation concentrations. In some drilling muds, the salts will be salts common in groundwater. Such groundwater salts include hypochlorides, chlorides, chlorates, perchlorates, sulfates, sulfites, sulfides, nitrates, nitrites, phosphates, carbonates, bicarbonates, carbides, borates, oxides, fluorides, silicates, arsenates, arsenides, selenates, selenides, bromates, bromides, and iodides. These may be present in high concentrations in old groundwaters. For example, chloride may be present at up to about 3000 ppm in certain groundwaters, or up to exactly 3000 ppm. The water may also contain dissolved organics. Ideally the water does not contain significant organic solutes. 
         [0059]    Some embodiments of the methods and facilities of this disclosure can be applied to a used drilling mud that also contains an emulsifier. Embodiments of the methods and facilities may be applied generally to mud containing any emulsifier known in the art, including organic emulsifiers. 
         [0060]    1. Screening 
         [0061]    Certain embodiments of the method comprise screening the waste drilling mud  44  to remove any debris. In this context “debris” refers to trash or other large contaminating objects present in the waste drilling mud  44 , and does not include drilling mud solids. 
         [0062]    The debris can be removed with a coarse screen  1  as familiar to those skilled in the art. After screening, the waste drilling mud  44  can be conveyed directly to a dryer  2  or it can be held in a receiving tank  3  prior to drying. 
         [0063]    2. Drying 
         [0064]    Certain embodiments of the method include separating a fraction of the drilling mud solid  40  from the waste drilling mud  44 , the fraction  40  comprising particles above a predetermined diameter, the fraction  40  further comprising a residual organic phase (“drying”). The separation may be achieved by use of a dryer  2 . Any dryer known in the art to be suitable for separating solids from waste drilling mud  44 , high-viscosity liquids, emulsions, or oils may be used. Such dryers include for example a centrifugal dryer  3 . In some embodiments, the dryer is a vertical centrifugal dryer  4 , or a processing centrifuge  5 . The dryer  2  may be operated to effect the separation of a fraction  40  of the drilling mud solid from the waste drilling mud  44 , wherein the fraction  40  of the drilling mud solid comprises particles below a first diameter. The first predetermined diameter may be any diameter of solid. In some embodiments of the method, the first diameter is about 15/1000″, or exactly 15/1000″ (3.81 mm). In some embodiments of the method, the first diameter is from zero to about 15/1000″, or from zero to exactly 15/1000″. The diameters of particles of the various fractions may in some cases be predetermined, for example during the design of the system or by varying conditions of operation of the system. 
         [0065]    The remainder of the waste drilling mud  44  will have a reduced solids concentration at this point. In some embodiments of the method, the waste drilling mud  44  after separating a fraction of the drilling mud solid  40  from the waste drilling mud  44  has a solids concentration of one or more of the following: 10-40%, 15-35%, 20-30%, 25%, or about these values. 
         [0066]    Subsequent to drying, the remainder of the waste drilling mud  44  may be conveyed to a dryer liquid tank  6 . If the remainder of the waste drilling mud  44  is conveyed to a dryer liquid tank  6 , the waste drilling mud  44  can then be conveyed to subsequent steps in the method. 
         [0067]    3. De-Solidification 
         [0068]    Some embodiments of the method comprise removing a second fraction  41  of the drilling mud solids, the second fraction  41  comprising particles above a second diameter. In certain of these embodiments the second diameter is less than the first diameter of the first separation step. In various embodiments of the method, the second diameter is one or more of the following: 5-15 μm, 6-14 μm, 7-13 μm, 8-12 μm, 9-11 μm, 10 μm, and about these values. 
         [0069]    In some embodiments of the method, the second fraction  41  is removed by centrifugation. In certain of these embodiments, the second fraction  41  is removed using a decanter centrifuge  7 . 
         [0070]    The process may be repeated on the remainder of the waste drilling mud  44 , by removing a third fraction  52  of the drilling mud solids, the third fraction  52  comprising particles above a second pre-determined diameter. In some embodiments the third fraction  52  of the drilling mud solids is removed using a second decanter centrifuge  35 . In various embodiments of the method, the third diameter is one or more of the following: 5-15 μm, 6-14 μm, 7-13 μm, 8-12 μm, 9-11 μm, 10 μm, and about these values. 
         [0071]    Some embodiments of the method further comprise treating the liquid product of a decanter centrifuge  7 ,  35  in a process tank  62 . Conditions in the process tank will aid in solid separation. Examples of such condition include elevated temperature (for example, about 180° F.) and agitation. 
         [0072]    The diameters of particles of the various fractions may in some cases be predetermined, for example during the design of the system or by varying conditions of operation of the system. 
         [0073]    The process may be repeated on the remainder of the waste drilling mud  44 , by removing additional fractions  42  of the drilling mud solids, the additional fractions  42  comprising particles above an additional pre-determined diameter. In some embodiments additional fractions  42  of the drilling mud solids are removed using one or more additional decanter centrifuges  51 . In various embodiments of the method, the additional pre-determined diameter is one or more of the following: 5-15 μm, 6-14 μm, 7-13 μm, 8-12 μm, 9-11 μm, 10 μm, and about these values. 
         [0074]    Some embodiments of the method comprise the addition of a flocculant  52  through a flocculant inlet  53 . The flocculant promotes aggregation of solids in the waste drilling mud, and increases the efficiency of removal of the solids. 
         [0075]    4. Preparation for Demulsification 
         [0076]    The waste drilling mud  44  may be stored prior to demulsification in an agitator tank  8 . The agitator tank  8  has the advantage of maintaining a homogeneous emulsion prior to demulsification. The agitator tank  8  may be heated to further aid in maintaining a homogeneous emulsion. 
         [0077]    In some embodiments of the method, the viscosity of the waste drilling mud  44  is adjusted to a certain value or range prior to demulsification. Viscosity of the waste drilling mud  44  may be measured, and the waste drilling mud  44  viscosity adjusted if the viscosity is not within the certain range or at the certain value. The viscosity may be adjusted for example by diluting the waste drilling mud  44  and returning it to one of the earlier separation steps. The viscosity may also be adjusted by diluting the waste drilling mud  44  with diesel and carrying out the demulsification step. 
         [0078]    More than one approach to viscosity adjustment may be employed in the method. In some embodiments of the method, the viscosity is adjusted by a certain method if it falls within one range, and adjusted by another method if it falls within another range. For example, if the viscosity is measured to be in a higher range, the viscosity may be adjusted by diluting the waste drilling mud  44  and returning it to one of the earlier separation steps. If the viscosity is measured to be in a middle range, the viscosity may be adjusted by diluting the waste drilling mud  44  and transmitting it to the demulsification step. 
         [0079]    In some embodiments of the method, the waste drilling mud  44  is subjected to the demulsification step if its viscosity is below 45 seconds Marsh funnel at 150° F. or about this value. If the waste drilling mud&#39;s  44  viscosity is measured to be between about 45-50 seconds Marsh funnel at 150° F., the waste drilling mud  44  is diluted with diesel and then is subjected to the demulsification step. If the waste drilling mud&#39;s  44  viscosity is above about 50 seconds Marsh funnel at 150° F., the waste drilling mud  44  is diluted with diesel and returned to one of the previous separation steps. 
         [0080]    5. Demulsification 
         [0081]    Certain embodiments of the method include demulsifying the bulk emulsion, to form a demulsified hydrophobic phase and a demulsified aqueous phase  43 . Demulsifying the bulk emulsion can be achieved by any means known in the art. Emulsions in drilling muds are idiosyncratic, based on the emulsifier used (if any) and the composition of the mud. When an organic emulsifier is used, the emulsion can be demulsified by any of the following alone or in combination: heating the emulsion, adjusting the pH of the emulsion, adding an oxidant to the emulsion, adding a de-emulsifier to the emulsion, and centrifuging the emulsion. 
         [0082]    If the emulsion is heated in the process of demulsification, it can be heated to any temperature up to about the boiling temperature of the emulsion. In various embodiments of the method, the emulsion is heated to at least one of the following: 140-200° F., 150-190° F., 160-180° F., 165-175° F., 170° F., and about these values 
         [0083]    If the pH is adjusted in the process of demulsification, it can be acidified or made alkaline; typically the final pH will not be neutral if the pH is adjusted. Acidification below about pH 5 often increases the efficiency of demulsification when an organic emulsifier is used. In various embodiments of the method, the pH is adjusted to at least one of the following: 0.0-5.0, 4-6, 4.5-5.5, 4.5-5.3, 4.6, and about these values. The pH can be adjusted by the addition of any acid  47  or base. If the emulsion is acidified, some embodiments of the method comprise adding a strong acid  47  to the emulsion. Some embodiments of the method comprise adding a strong inorganic acid  47  to the emulsion. Some embodiments of the method comprise the addition of at least one of the following acids to the emulsion: hydrochloric acid, sulfuric acid, nitric acid, chromic acid, perchloric acid, hydroiodic acid, hydrobromic acid, fluoroantimonic acid, “magic acid” (an equimolar mixture of HSO 3 F and SbF 5 ), carborane superacid H(CHB 11 Cl 11 ), fluorosulfuric acid, and triflic acid. Hydrochloric acid, for example, has the advantage of low cost and a high dissociation constant. In some embodiments of the method, a weak acid  47  is used to adjust the pH, although larger volumes are needed. 
         [0084]    In some embodiments of the method, an oxidant  48  is added to achieve demulsification. The oxidant  48  functions to degrade an organic emulsifying agent, which then breaks the emulsion (alone or in combination with other means). Any oxidant can be used, but ideally the oxidant  48  will be chosen based on its oxidizing power, potential to contaminate the waste stream, cost, and possible side reactions. Commonly used oxidants include salts, oxides and acids of the following anions: hypochlorite, halogens, chlorite, chlorate, perchlorate, permanganate, chromate, dichromate, chromium trioxide, pyridinium chlorochromate, peroxide, Tollen&#39;s reagent, sulfoxides, and persulfate. Gasses such as nitrous oxide, ozone and O 2  are also excellent oxidants. Other potentially useful oxidants include osmium tetroxide, and nitric acid. For example, 1.5% sodium hypochlorite is an inexpensive and effective oxidant that aids in demulsification without the addition of unduly polluting hazardous material to the waste stream. 
         [0085]    In some embodiments of the method, an additional demulsifier  49  is used, for example: acid-catalyzed phenol-formaldehyde resins, base-catalyzed phenol-formaldehyde resins, polyamines, di-epoxides, and polyols. 
         [0086]    Some embodiments of the method comprise demulsifying the emulsion by centrifugation. This may involve centrifuging the emulsion in a two-phase centrifuge  9 , in which case separation will occur between the demulsified hydrophobic phase and the demulsified aqueous phase  43 . This may involve centrifuging the emulsion in a three-phase centrifuge  10 , in which case separation will occur between the demulsified hydrophobic phase, the demulsified aqueous phase  43 , and the solid in one step. 
         [0087]    6. Demulsified Separation 
         [0088]    Embodiments of the method comprise separating the demulsified hydrophobic phase from the demulsified aqueous phase  43 , to create an aqueous product and an oil product  50 , wherein the oil product  50  is suitable for reuse. In some embodiments of the method, the demulsified phases are separated by centrifugation. This may occur simultaneously with the demulsifying step, or it may occur subsequent to the demulsifying step. In some embodiments of the method, the demulsified aqueous phase  43  is separated from the demulsified hydrophobic phase by centrifuging in a two-phase centrifuge  9 . In some embodiments of the method, the demulsified aqueous phase  43  is separated from the demulsified hydrophobic phase by centrifuging in a three phase centrifuge  10 . If a three-phase centrifuge is used, a fourth fraction  53  of the drilling mud solid may be removed simultaneously. In some embodiments of the method, the fourth fraction  53  of the drilling mud solid removed comprises particles above a certain diameter. In various embodiments of the method, the diameter is one or more of the following: 0-100 μm, 0-75 μm, 0-50 μm, 0-25 μm, 0-20 μm, 0-15 μm, 0-10 μm, 100 μm, 75 μm, 50 μm, 25 μm, 20 μm, 15 μm, 10 μm, and about each of these values. The lower the diameter, the higher the quality of the oil product  50  and aqueous product will be. Higher diameters have the advantage of requiring less energetic centrifugation. In some embodiments of the method, substantially all solids are removed. In some embodiments the fourth fraction  53  of the drilling solids removed comprises particles above a certain density. In various embodiments of the method, the fourth fraction  53  of the drilling mud solid may comprise one or more of the following: a residual organic phase, and a residual aqueous phase. 
         [0089]    In some embodiments of the method, the oil product  50  is suitable for reuse as a fuel, a drilling mud oil, or both. In some embodiments in which the oil product  50  is suitable for reuse as an oil, the oil product  50  is suitable as one or more of the following: a boiler fuel, a desorber fuel, and an oxidizer fuel. A desorber fuel is a fuel suitable to power a thermal desorber. An oxidizer fuel is a fuel suitable to power an oxidizer. A boiler fuel is a fuel suitable to power a boiler. It is generally advantageous that the oil product  50  have a low water content and a low solids content. 
         [0090]    As the content of water decreases in the oil product  50 , the energy yield of the fuel upon combustion increases. Acceptable diesel fuels can have relatively high water contents (up to about 40%) and still function as fuels for example in boilers. Various embodiments of the method produce oil products  50  with water contents of one or more of the following: 0-40%, 0-30%, 0-20%, 0-10%, 0-5%, below 5%, and about each of these values. 
         [0091]    As the content of solids decreases, the energy yield of the fuel upon combustion increases and the ash production of combustion decreases. Fuels with high water or solids content have the advantage of low production cost. Various embodiments of the method create oil products  50  suitable as fuels with solids contents up to 20%, 15%, 6%, 1%, and about these values. In some embodiments of the method, the oil product  50  has a solids content of about 4-6%. 
         [0092]    Embodiments of the method yield oil products  50  suitable for reuse in drilling muds with solids contents up to about 4-6%. In particular embodiments of the method, the oil product  50  suitable for reuse in drilling mud comprises a solids content of one or more of: 0-6%, 0-5%, 0-4%, 0-3%, 0-2%, 0-1%, 0%, and about each of these values. 
         [0093]    The oil product  50  can be stored on-site in an oil storage facility  11 , such as a tank  12 . Alternatively, the oil product  50  can be delivered off-site by means such as tanker vehicles  13  or pipelines  14 . 
         [0094]    7. Vaporization/Recondensation of Organics 
         [0095]    Embodiments of the method comprise vaporizing a residual organic phase from the solid fraction  40   41   42   52   53  of the drilling mud, to create an organic vapor  65  and a first solid product  56 ; and condensing the organic vapor  65  to produce a second oil product  58 . Vaporization can be achieved by any means known in the art. For example, it has unexpectedly been discovered that feeding the solid fraction  40   41   42   52   53  of the drilling mud through a soil dryer  61  (particularly when the soil dryer  61  is a screw heat exchanger  54 ) is an efficient and effective means of vaporizing the residual organic phase from the solid fraction  40   41   42   52   53 . Water may be co-vaporized with the residual organic phase. Alternatively, water may be vaporized prior to or subsequent to the vaporization of the residual organic phase. In some embodiments of the method, water is not vaporized from the solid fraction  40   41   42   52   53 . 
         [0096]    The organic vapor  65  may be recondensed and collected as a liquid. This has the advantage of preventing the release of the organic vapor  65 , which contains pollutants. Condensation may be achieved by cooling the vapor or increasing the pressure of the vapor. Any non-recondensed organic vapor  67  may be routed to the second oxidizer  59  and completely combusted, to produce clear air emissions substantially free from volatile organic compounds. 
         [0097]    The temperature of the soil dryer  61  will determine which fractions of the residual organic phase are vaporized. This in turn will control the composition and quality of the second oil product  58 . The composition of the second oil product  58  will also be affected by the temperature and pressure of the condenser  55 . If the drilling mud contains organic additives of high value, it will be advantageous to set the parameters of the soil dryer  61  and condenser  55  to vaporize and recondense the additives selectively. 
         [0098]    Water that is vaporized in the soil dryer may be recondensed and collected as recondensed water  63 , it may be routed to the second oxidizer  59  for temperature control. Of course, vaporized water in the absence of any gaseous hydrocarbons can be released to the atmosphere. 
         [0099]    The first solid product will not be completely free of organic compounds. However, the first solid product will in some cases be suitable for reuse with further processing, for example as road base or fill. In a typical embodiment of the method, the first solid product is from 2-5% hydrocarbon. 
         [0100]    8. Vaporization/Combustion of Organics 
         [0101]    Embodiments of the method comprise the sequential vaporization and combustion of either the residual organic phase from the solid fraction separated from the drilling mud, or of an organic residue present in the first solid product (both solid/organic materials referred to in this section as having an “organic phase” and a “solid phase”). Such embodiments comprise removing substantially all the organic phase from the solid phase, to create an organic residue vapor and a second solid product  46 , removing the organic phase comprising vaporizing the organic phase (some of the organic phase may be combusted); wherein the second solid product  46  is substantially free from organic pollutants. Vaporization can be achieved by any means known by those skilled in the art. For example, it has been unexpectedly discovered that vaporization can be achieved very efficiently using a low-temperature thermal desorber  15 . In some embodiments of the method, solid material  40   41   42   52   53   56  separated from the waste drilling mud  44  is introduced to a thermal desorber, in which substantially all organic carbon is vaporized. In some embodiments, residual water associated with the solid phase is co-vaporized. In some embodiments, water separated from the drilling mud is introduced and co-vaporized. The degree to which the organic phase is vaporized will be determined by various factors including residence time, temperature, pressure, and composition of the organic phase. 
         [0102]    The solid fraction  40   41   42   52   53   56  may be any solid fraction that has been separated from the waste drilling mud  44  as described herein. 
         [0103]    In embodiments in which organic carbon is vaporized in a thermal desorber  15 , the thermal desorber  15  can be of any type known to those skilled in the art. It has unexpectedly been discovered that the organic phase can be efficiently removed using a direct-fired counter-current low temperature thermal desorber  16 . If a direct-fired thermal desorber  16  is used, some amount of the residual organic carbon is likely to be combusted, and the remainder vaporized. 
         [0104]    In some embodiments of the method, the thermal desorber  15  is powered by a thermal desorber fuel, such as a combustible hydrocarbon fuel. In certain embodiments of the method, the oil product  50  is reused as the thermal desorber fuel. This approach has the advantage of both reusing the oil product  50  without creating any lasting pollutant and avoiding the need to purchase additional energy to power the desorber. Depending on the composition of the organic phase and depending on the operating conditions of the thermal desorber, a portion of the organic phase may also serve as fuel in a direct-fueled thermal desorber  17 . This has the advantage of requiring less input of energy from outside the process. In some embodiments of the method, the thermal desorber fuel is autoignited. 
         [0105]    In various embodiments of the method, the organic phase is vaporized using a direct-fired countercurrent thermal desorber  16  operating at one or more of the following temperatures: 500-650° F., 525-625° F., 550° F., or about these values. Higher temperatures have the advantage of ensuring complete vaporization and requiring shorter residence times, while lower temperatures have the advantage of less fuel consumption. In some embodiments, the thermal desorber  15  is operated at or about atmospheric pressure. In some embodiments, the thermal desorber  15  is operated at sub-atmospheric pressure. In various embodiments of the method the thermal desorber  15  is operated at one or more of the following pressures: 2-14″ of water negative pressure, 4-12″ of water negative pressure, 6-10″ of water negative pressure, 8″ of water negative pressure, or about these values. Residence time can also be varied to optimize vaporization, with longer residence times ensuring a better yield; shorter residence time provides for higher throughput. 
         [0106]    9. Treatment and Disposal of the Solid Product 
         [0107]    The second solid product  46  created in the vaporization step may be combined with the solids collected from filtration of the gaseous product and the solids collected from cyclonic separation of the organic residue vapor; in such embodiments the second solid product  46  comprises solids separated from the drilling mud, solids collected from filtration of the gaseous product and the solids collected from cyclonic separation of the organic vapor. 
         [0108]    In some embodiments of the method, the second solid product  46  is cooled and moistened by the addition of conditioning water. This may be achieved using a standard soil conditioner  18 , for example. The conditioning water may comprise at least a portion of the aqueous phase (or the demulsified aqueous phase  43 ) of the waste drilling mud  44 . The conditioning water may be saline groundwater. If the conditioning water is saline groundwater, then the second solid product  46  will comprise a salt. The water may be used in any amount that will cool the second solid product  46  for handling and condition the second solid product  46  for particular uses. In some embodiments a portion of the water is discharged as steam. 
         [0109]    Regardless whether the second solid product  46  is treated, the second solid products  46  of the method comprise no substantial amount of organic pollutant, and may be disposed of or reused without special measures. In some embodiments in which saline water is used to condition the second solid product  46 , the concentration of salt in the second solid product  46  is sufficiently low that it does not constitute a pollutant. 
         [0110]    As stated above, in some embodiments of the method the first solid product  56  is not fit for disposal absent further processing, but may be used as fill or road base. Testing may be conducted of the first  56  or second solid product  46  to determine the organic content. As organic compounds are potential pollutants, the organic content will dictate whether the solid product can be disposed of without further treatment and for which applications the solid product can be reused. 
         [0111]    10. Particulate Removal 
         [0112]    In some embodiments of the method, particulate matter (such as evaporite, soot, or dust) is removed from the organic residue vapor or organic vapor  65  and steam produced by the vaporization step. Removal may be achieved by any means known in the art. In some embodiments, cyclonic separation is used to efficiently collect the particulate matter. In such embodiments the characteristics of the cyclone may be varied to remove particulates based on density or size. In some embodiments of the method, removal is achieved using a dual cyclone  19 . The dual cyclone  19  may comprise two cyclonic separators  20  in parallel, or in series. In additional embodiments more cyclonic separators  20  may be used. In some embodiments the solid particles are added to the first solid product  56  or the second solid product  46 , either before cooling or conditioning. 
         [0113]    11. Combustion of Organic Vapor 
         [0114]    Embodiments of the method comprise combusting substantially all the organic residue vapor or non-recondensed organic vapor  67  under conditions sufficient to ensure substantially complete combustion, to create a clean gaseous product. In some embodiments of the method, combustion is carried out in an oxidizer  21  or a second oxidizer  59 , for example by comingling the organic residue vapor or non-recondensed organic vapor  67  with oxidizer fuel and an oxidant (such as O 2 ). Complete combustion can be achieved by varying conditions such as temperature, oxygen concentration, oxidizer fuel concentration, organic vapor  65 /organic residue vapor concentration, residence time, and by adding various concentrations of atomized water. In various embodiments of the method, the temperature is maintained at one or more of the following temperatures: 1400-2000° F., 1500-1900° F., 1600-1800° F., 1700° F., and thereabouts. Oxygen concentration can be controlled by forcing air into the oxidizer  21  or second oxidizer  59  using a blower or other means. Alternatively, concentrated or pure oxygen gas can be introduced into the oxidizer  21  or second oxidizer  59 . Under conditions in which the concentration of organic residue vapor is high, it is desirable to increase the concentration of oxygen. In various embodiments of the method, the partial pressure of air in the oxidizer  21  or second oxidizer  59  is at least one of 12-20 psi, 13-19 psi, 14-18 psi, 15-17, 16 psi, and about these values. In various embodiments of the method, the partial pressure of oxygen in the oxidizer is at least one of 2.4-4.0 psi, 2.6-3.8 psi, 2.8-3.6 psi, 3.0-3.4 psi, 3.2 psi, and about these values. Under some conditions the oxidizer fuel will be ignited by autoignition. 
         [0115]    Water may also be injected into the chamber. Waste water can be disposed of by vaporization this way, creating an aerosolized evaporite if the water contains solutes. Under some conditions it may be desirable to reduce the temperature in the oxidizer  21  or second oxidizer  59  by introducing water, for example atomized water. In some embodiments of the method the water comprises at least a portion of the aqueous phase (or demulsified aqueous phase  43 ) or recondensed water  63 . Introducing water also serves the purpose of disposing of saline water, the salt forming an evaporite upon vaporization of the water. 
         [0116]    The oxidizer fuel can be any combustible gas or liquid, or even a fine combustible solid. In some embodiments of the method, the oxidizer fuel is the oil product  50 . Using the oil product  50  as the oxidizer fuel has the advantage of reusing one of the products of the process on-site. It does not require that fuel be purchased and transported to the site. It provides a means of clean disposal of the oil product  50 . The concentration of the oxidizer fuel in the oxidizer  21  or second oxidizer  59  will affect the efficiency of combustion. In various embodiments of the method the partial pressure of the oxidizer fuel in the oxidizer is one or more of the following: 120-240 psi, 140-220 psi, 160-200 psi, 180 psi, and thereabouts. High fuel concentrations have the advantage of providing higher temperatures and more complete combustion of the organic residue vapor. Low fuel concentrations have the advantage of preventing un-combusted fuel from leaving the oxidizer and low fuel consumption. 
         [0117]    Depending on operating conditions, combustion may create a solid soot, dust, or aerosol, in addition to a clean gaseous product. The clean gaseous product may be substantially free from solids, organics, or pollutants at this point. Even a gaseous product that is substantially free from pollutants will likely contain a trace of carbon monoxide. The trace of carbon monoxide in some embodiments is below concentrations that are legally regulated; in other embodiments the trace of carbon monoxide is a legally regulated concentration that requires a discharge permit. In some embodiments the trace of carbon monoxide is less than 500 ppm, or about that amount. 
         [0118]    12. Quenching 
         [0119]    In some embodiments of the method, the clean gaseous product is cooled in a quench chamber  22 . In certain of these embodiments, the quench chamber comprises a water inlet  23 . The clean gaseous product may be cooled for example by spraying water into the quench chamber  22 ; the water will vaporize, cooling the gas. In some embodiments, the water is atomized water. In some embodiments, the water is saline water. In some embodiments of the method, the water is saline groundwater. In some embodiments of the method, the water comprises at least a portion of the aqueous phase (or the demulsified aqueous phase  43 ). If the water is saline, then a saline evaporite will be created upon vaporization of the water. 
         [0120]    If a quench chamber  22  is used, it may be any type of quench chamber familiar to those skilled in the art. The quench chamber may facilitate cooling by expanding along its length, allowing the hot gas to expand and cool. 
         [0121]    In embodiments of the method that involve a baghouse  24 , the exit temperature of the clean gas product will be below about 400° F.; temperatures in this range have the advantage of not damaging the baghouse  24 . In some embodiments of the method, the exit temperature will be above about 250° F.; temperatures in this range have the advantage of ensuring the quench water is fully vaporized. In various embodiments of the method, the exit temperature will be one or more of 250-400° F., 300-400° F., 325-375° F., 350° F. and about any of these values. 
         [0122]    13. Filtration 
         [0123]    In some embodiments of the method, the evaporite is captured subsequent to at least one of removing the organic residue or residual organic phase from the drilling mud solid fraction, oxidization of the organic residue vapor, or quenching of the clean gaseous product. The evaporite may be captured by any conventional separation method. In some embodiments of the method, the evaporite is captured by filtration. In certain of these embodiments, the evaporite is captured in a baghouse filter  25 , in a baghouse  24 . 
         [0124]    14. Discharge 
         [0125]    Embodiments of the method comprise discharging the clean gaseous product to create a clean gaseous discharge  45 , wherein the clean gaseous discharge  45  is substantially free from solids, organics, or pollutants. The clean gaseous discharge  45  may contain traces of solids, organics, or pollutants. In some embodiments of the method, the clean gaseous discharge  45  contains solids, organics, or pollutants at or below legally regulated levels. In some embodiments of the method, the clean gaseous discharge  45  contains carbon monoxide at a legally regulated level. In some embodiments, carbon monoxide is present below 500 ppm or about this value. In some embodiments of the method, at least one of the following is either absent or present below legally regulated levels: solids and organics.