Abstract:
A method for contaminant and water removal from crude oil. The method involves recirculating at least a portion of the dewatered crude into a dehydrator. The dehydrator contains a heated dehydrated crude oil and the surface or adjacent thereto is maintained at a temperature sufficient to vaporize any water contacting the surface from crude oil to be treated in the dehydrator. It has been found important to maintain a substantially uniform temperature at or below the vaporizing surface in order to effectively treat crude oil for dewatering purposes. Significant temperature fluctuations are typically realized by dehydrators since heat enthalpy is removed in order to vaporize the water in the crude oil. Such fluctuations lead to process complications and upset and are therefore undesirable. The instant invention recognizes this limitation and substantially reduces foaming and provides for a smoothly running and efficient dehydration process.

Description:
CROSS-REFERENCE TO RELATED APPLICATIONS 
     This is a CIP application of U.S. application Ser. No. 10/011,319, filed Dec. 11, 2001 now U.S. Pat. No. 6,849,175, which in turn, is a CIP application of U.S. application Ser. No. 09/604,577, filed Jun. 27, 2000, now U.S. Pat. No. 6,372,123. 
    
    
     FIELD OF THE INVENTION 
     The present invention is directed to an enhanced crude oil dehydration process and apparatus, and more particularly the present invention is directed to a crude oil dehydration and decontamination process which can overcome the instability problems encountered with prior art for treating high water cut heavy oil streams, provide enhanced thermal energy input and recovery methods, remove suspended and dissolved compounds from inlet feed and recover diluent from oil treatment units in an efficient manner. 
     BACKGROUND OF THE INVENTION 
     Throughout many regions of the world, heavy oil, a hydrocarbon material having much higher viscosity or lower API gravity (less than 20° API, typically 7° to 12° API) than conventional petroleum crude, is being economically recovered for commercial sale. During the recovery process and prior to the transport to refineries for upgrading, the heavy oil receives preliminary treatment for water and solids removal to generally achieve basic sediment and water (BS &amp; W) content less than 0.5% by volume and chloride content less than 30 ppm (wt), more recently, the chloride content has been decreased to less than 10 ppm. Water content of the treated heavy oil typically is required to be 0.3% by volume or less. 
     Conventional crude oil treatment methods were proven to be ineffective with respect to heavy oil until the advent of the technology set forth in U.S. Pat. Reissue No. 33,999, Clare et al., reissued Jul. 21, 1992 and Canadian Patent 1,302,937, Clare et al., reissued on Jun. 9, 1992. These patents describe a simple apparatus which can be located in remote oil producing areas for dehydrating heavy oil with low risk of foaming and unstable operating, while continuously achieving dry oil which exceeds requisite specifications. These dehydrators were found to be restricted to feed oil water content of less than 5% water cuts and susceptible to foaming and process instability during high water feed rates. Throughout the operation of several of these dehydrators known from practicing the technology in Pat. Re No. 33,999 and U.S. Pat. No. 1,302,937, areas for improvement were discovered to overcome the limitations of feed oil water content and unstable operation caused by pretreatment upsets. 
     Further refinements in the crude oil processing were developed by Kresnyak and Shaw in U.S. Pat. No. 6,372,123, issued Apr. 16, 2002. 
     In the dehydration of crude, significant fluctuations in the temperature in the dehydrator can be experienced since heat enthalpy is continuously removed in order to vaporize the water in the crude oil. Kresnyak and Shaw recognized that this heat enthalpy needed to be restored in order to stabilize the temperature within the dehydrator and more particularly, the temperature of the heated dehydrated crude oil within the dehydrator. By recirculating at least a portion of the dehydrated crude and contacting this with the source of crude oil immediately below the vaporizing surface in the dehydrator, a substantially uniform temperature of the vaporizing surface in the dehydrator was realized. Accompanying advantages were immediately realized in terms of reduced foaming within the dehydrator and less process impediments. 
     Further, additional problems have been experienced in dehydration techniques in that although dehydrated heavy oil is achieved, high concentrations of suspended solids, such as clay and silica and dissolved compounds such as chlorides remain in the treated oil. These undesirable compounds continue to create many problems in pipeline transportation systems and refinery facilities to the extent that they depreciate the commercial valve of heavy oil. 
     It has been found in field applications that mineral salts, silica, clay inter alia that remain in the dehydrated crude promote corrosion cracking in stainless steel components and induce scale accretion and/or fouling of surfaces critical to efficient and consistent operation of the apparatus in the refiner and pipeline systems. Generally speaking, the salt crystals mix with the oil and coalescence results to form larger crystals which can pass through the refinery desalination equipment. 
     In view of the fact that the dehydration process is a water removal system for the crude oil, it then follows that mineral concentration is a distinct drawback. Advances have been made in respect of this limitation and in particular, dehydrators have been modified to include a demineralization/solid removal unit operation to avoid any concentration of the latter within the treatment circuit. 
     Having set forth the background of the dehydration technology, one of the remaining process limitations that was discovered relates to the use of diluent in the system. Unfortunately, within the processes and particularly the first generation dehydration technology, a significant amount of diluent was required. Typically, 20% to 50% by volume diluent was required in order to effect the first generation processes. Clearly, this has significant impact on the available volume within the pipeline and as a natural consequence, pipelines either had to be 50% larger in order to have the same efficiency in the absence of the diluent or, the process was inherently 20% to 50% less efficient. Although a detriment, first generation systems had inherent advantages such as good separation and operated at significantly cooler temperatures. 
     In flash treatment systems subsequently developed, the process produced dry oil, did not involve the extensive use of many pieces of equipment to handle different unit operations and therefore was more affordable and more importantly, did not require any diluent. Despite the significant advantages, flash treatment systems were not equipped to handle chloride problems as indicated above. 
     It would be advantageous if methodology could be developed which unifies all of the positive attributes of first generation processes with flash treatment process without the disadvantages and in particular, without the requirement for a diluent make up. The present invention is directed to a union of all of the positive attributes of existing systems and conveniently provides for high diluent recycle. 
     Accordingly, one object of the present invention is to provide advances to overcome the limitations encountered by the previous art. 
     SUMMARY OF THE INVENTION 
     One object of the present invention is to provide a dehydration method for dehydrating crude oil containing water and recycling diluent used in the method. 
     A further object of one embodiment of the present invention is to provide a method of removing water and solids from crude oil containing water and solids to provide a clean dry oil, comprising: 
     A separation phase, a dehydration phase and a diluent recovery phase, the dehydration phase including:
         providing a source of crude oil containing water;   adding a diluent to the source of crude oil;   a separation phase to remove at least a portion of the water;   dehydrating the crude oil containing water in a dehydrator having a vaporizing surface of dry crude oil at a temperature sufficient to vaporize water contacting the surface;   exposing the source of crude oil to the dry crude oil to vaporize the water and at least a portion of diluent in the source;       

     the diluent recovery phase including:
         heating the dehydrated crude to liberate diluent;   stripping the diluent; and   recirculating recovered diluent to the crude oil containing water in the separation phase.       

     One of the attractive benefits of the methodology as set forth herein relates to the fact that it can be easily retrofitted on to existing first generation dehydration systems in order to provide for high diluent recovery. This is advantageous since the oil processing industry is experiencing difficulty in obtaining a diluent due to a shortage of suitable diluent materials. 
     The method set forth herein is designed to recover and recycle a high proportion of the diluent (at least 90%) and in some cases, 99% or greater recovery is achievable. As an example, for a typical 30,000 BOPD (barrels of oil per day) commercial SAGD (steam assisted gravity drainage) operation, this recovery translates to less than one truck load of diluent makeup within a system on a daily basis. In the present technologies available, this insignificant diluent makeup has not been achievable. As those skilled in the art will appreciate, this significantly adds to the efficiency of the overall method which, in turn, immediately translates to a significant increase in profitability of the overall process. 
     Conveniently, when at least a portion of the dry crude oil recycle stream around the dehydrator enters the dehydrator and is distributed below the surface of the hot crude oil in the dehydrator a consistent temperature is maintained at or above the vaporization temperature of water and at or below the surface of the oil and throughout the contained oil, thereby providing a means to mitigate the risk of process upsets and instability due to foaming. 
     A further object of the present invention is to provide a dry crude recycle stream around the dehydrator to mix with the feed stream, to allow an input of supplemental heat energy (external or waste heat energy) to remove a portion of diluent to result in an energetically efficient and balanced process. 
     This process effectively unifies the best aspects of blend treatment and flash treatment to provide a process which can remove unwanted solid and salt compounds, dehydrate the crude oil and maximize the efficiency of the diluent that is used in the system. Accordingly, in the methodology of the instant invention a dry clean oil product is formulated and this is done while providing a maximum efficiency on the recovery of diluent used in the process. In terms of the make up diluent, commercially available diluents may be employed such as synthetic crude oil (SCO), naphtha and natural gas condensates. 
     The overall method unifies all of the best attributes of the existing technologies to provide a cooler process which operates in a stable manner to produce clean dry oil. As a further very significant advantage, the pipelines employed for transportation can be anywhere from 20% to 50% smaller in capacity in view of the fact that no diluent is added into the system. This feature alone, presents a significant savings and when taken into account with the fact that the operation of the primary treatment plant may be decoupled and operated independently from the pipeline and the SAGD well pads independently operated, the overall methodology clearly has significant ramifications in terms of efficiency, profitability and utility. 
     As a further advantage of the present invention, the process is arranged simultaneously to recover from a source of crude oil diluent fluids that have been added to a reservoir with SAGD injection steam. These diluent fluids can be simultaneously recovered with the method and returned back to injection steam. This method provides a significant reduction in injection steam (20-40%); for a fixed steam injection rate there will be 20-40% more bitumen produced. 
     In the prior art, there has always been the requirement for diluent transportation and concomitant equipment with the technology set forth herein, there is no requirement whatsoever for a diluent facility or any pipeline or other transportation means for handling large volumes of the diluent. 
     In respect of the demineralization/solid removal, many of the standard techniques used to produce clean oil can be employed in this system which renders the overall process operationally simplistic relative to existing blend operations which experience complications such as process upsets and oil treatment instability. 
     The dry crude oil surface may be selectively heated by reintroduction of dry crude oil, auxiliary heat addition, etc. The important aspect is that the heat used for vaporization is replaced so that a uniform or substantially uniform surface temperature is maintained. This is one important unit operation to maintain. 
     Enhancements have been developed to eliminate the limits imposed by water cut of the source crude oil feed and to provide a very clean and dry heavy oil product relatively free of water, solids and chlorides. 
     The present invention relates to process enhancements to an apparatus used for dehydrating crude oil containing water, comprising a casing, means for admitting and distributing the liquid crude oil into the casing and onto the host surface of the dry crude oil, means for controlling the level of crude oil and a means to transfer heat energy sufficient to maintain the liquid oil at or above the distillation temperature for evaporating water, light hydrocarbons and at least a portion of diluent. 
     A further embodiment of the present invention is to recycle and blend the condensed light hydrocarbon produced from the dehydrator, with the raw source crude oil, to provide a blend treating oil/water separation pretreatment step. The light hydrocarbons can optionally be combined with additional diluent solvents to achieve both the volume and composition of diluent required to treat the emulsions. The diluent acts as a solvent for the oil, reducing the viscosity and density of the heavy crude oil and creates the density difference to separate the heavy oil from the produced water and solids. The separation step can be performed at the temperature and pressure conditions of the raw well effluent or source oil. Any heavy portion of additional diluent will pass through the dehydrator and be retained in the sales oil as shipping diluent. 
     The light hydrocarbons and water exiting the casing are condensed by any suitable means known in the art, and collected and separated into water and light hydrocarbon liquid phases. Any non-condensable vapors are released from the apparatus for disposition by any safe means. Dry crude oil meeting pipeline BS &amp; W specifications is pumped from the dehydrator to the stripper for final diluent recovery prior to transport for refining and upgrading. 
     Typically, the dehydrator taught in the current art performed well to produce dry crude oil, however several problems have been encountered: 
     1. The dehydrator was limited to crude oil feed water cuts (wc) of less than 10% water to oil, and more specifically less than 5% wc to reduce the risk of unstable operation with foaming tendencies. This required the need for a conventional treater means upstream of the dehydrator to reduce raw crude oil water cuts from 50 to 20% wc down to less than 5% wc prior to feeding the dehydrator. 
     2. The dry crude oil exiting the dehydrator contains high chloride content, causing metallurgy and corrosion problems with downstream refineries facilities and transportation pipelines. 
     3. It was found that by flash evaporating off the water and by effectively eliminating all emulsions, solids such as clays and silica compounds, concentrated in the dry oil phase, had a tendency to buildup, plug and/or cause heat element damage. 
     4. It has been further experienced that the dehydrator is susceptible to unstable operations and foaming tendencies causing dehydration temperature swings and wet oil production. 
     The present invention seeks to address these concerns by providing methodology and apparatus to exceed the performance of the dehydrator beyond the prior art. 
     In one embodiment of the invention, at least a portion of the dry crude oil exiting the dehydrator is recycled and mixed with the inlet crude oil feed prior to entering the dehydrator casing. By increasing recycle flow, a consistent and stable inlet water cut composition can be maintained at the entrance to the casing to control the tendency to foam and create operational complications. With greater recycle rates, the raw water cut levels can be increased above the 10% wc stable level and continuous stable operation is maintained. This eliminates the need for conventional treatment ahead of the dehydrator and can avoid dehydrator process upset if an upstream treater is used and a treater upset occurs. 
     A further embodiment of the invention requires that at least a portion of the recycled dry crude oil be recycled and distributed immediately below the dry crude oil evaporating surface. This method ensures that the temperature of the surface of the dry oil in the dehydrator is maintained at or above the flash evaporating temperature of water. Water and other flashing liquids droplets from the feed are not permitted to penetrate the surface of the crude oil, thereby preventing the cooling below the surface and creating surface breakdown foaming and unstable dehydrator operation. 
     Advantageously, external heat transfer means can be added to the recycle circuit supra to regulate the precise temperature of the feed stream to the dehydrator casing. This method enhancement will regulate the precise level of pre-flashing of water and other flashing liquids vapor in the feed oil to control the residual water level contacting the hot dry oil surface. This step can be used to prevent the overcooling of the bath and eliminate the foaming effects caused by excessive evaporation surface breakdown. 
     As a further feature, a solid/liquid separation device, examples of which include a filter, hydro cyclone, centrifugal separators, gravity separators, centrifuge or any combination thereof, etc., may be employed in the circuit of the recycle stream continuously or on a batch basis to-remove suspended solids from the hot dry oil. 
     Additionally, a clean water washing circuit may be added to the dehydrator feed to reduce undesirable dissolved compounds, such as chlorides, from the dry crude oil. The entire contaminated water stream, or a portion thereof, is treated by a suitable treatment method to create a clean water stream and a highly concentrated brine, slurry or solid product. The recovered clean water is recycled back to the raw crude oil for oil pretreatment. Generally water or any aqueous solution containing compounds for enhancing the extraction of chloride is most desirable, otherwise any regenerable fluid with a suitable aggressive solubility for chlorides may be considered. 
     It is preferable that in addition to achieving a dehydrated oil, having a BS&amp;W content of less than 0.5% wc by volume and greater than 90% diluent recovery, the embodiments of the invention in combination, or separately applied, can produce a dry clean crude oil, substantially free of solids and diluent, containing less than 10 ppm (wt) chlorides, in a continuous and stable operation, with low risk of foaming and process upsets. The oil produced by the present process is readily vendible and is most desirable, particularly in the case of heavy crude oils with gravities in the 7° API, to 20° API range. 
     Having thus described the invention, reference will now be made to the accompanying drawings illustrating preferred embodiments. 
    
    
     
       BRIEF DESCRIPTION OF THE DRAWINGS 
         FIG. 1  is a schematic flow diagram which illustrates the dry oil recycle to the dehydrator feed stream and dehydrator; 
         FIG. 2  is an additional schematic flow diagram showing external heat exchange on the recycle for temperature adjustment of the feed or surface of the dehydrator or both; 
         FIG. 3  is a further schematic flow diagram showing a solid/liquid separator for removal of suspended solids; 
         FIG. 4  is a schematic flow diagram illustrating the addition of water washing for removal of dissolved compounds such as chlorides; 
         FIG. 5  is a schematic flow diagram illustrating a further embodiment of the present invention; 
         FIG. 6  is a section along line  6 — 6  of  FIG. 5 ; 
         FIG. 7  is a schematic flow diagram illustrating a further embodiment of the present invention; 
         FIG. 8  is a schematic flow diagram illustrating yet another embodiment of the present invention; 
         FIG. 9  is a schematic flow diagram illustrating a further embodiment of the present invention; 
         FIG. 10  is a schematic flow diagram illustrating another embodiment of the present invention; 
         FIG. 11  is a schematic flow diagram illustrating a still further embodiment of the present invention; and 
         FIG. 12  is a schematic flow diagram illustrating a diluent recovery circuit. 
     
    
    
     Similar numerals employed in the Figures denote similar elements. 
     DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENT 
     With reference to  FIG. 1 , heavy oil with a viscosity of between 7° API and 20° API denoted by numeral  10 , typically includes a mixture of crude oil, water, oil/water emulsion, dissolved compounds such as chlorides and solid particles such as clay, metals and silicas and may contain diluent. The crude oil is mixed with diluent of 30-50% by volume and generally received in a gravity separator, heated or non heated treater  12 , under pressure from between atmospheric pressure to 100 psig (700 kPag). This will depend on the quantity of diluent present in the oil. Heated treaters typically operate from 170° F. to 285° F. (77° C. to 141° C.). In the treaters, solid particles and bulk brackish water is separated and removed from the raw crude oil at  14 . Water cuts of less than 10%, to more typically between 5% and 1% by volume can be achieved in the raw crude/diluent feed  18  exiting the primary treatment through a valve member  20 . The water stream  22  generally contains dissolved compounds such as sodium chloride, (5,000 to 50,000 ppm (wt)) and silica, and suspended compounds such as clay and sand. 
     The raw crude oil/diluent mix at approximately between 5% and 1% water cut in the emulsion form, containing no free water, enters the dehydrator  24  where the crude oil and emulsions are evenly distributed onto the hot surface of dry crude oil (not shown), operating at or above the evaporation temperatures of the water and other flashing liquids. Water and other flashing liquids are flashed off the oil or separated by distillation, with water and low boiling temperature hydrocarbon and diluent components from the oil exiting through the column  26  and passing through line  28 . If desired, the water and lower boiling components may be sent to a condenser  30  and subsequently to a vapor liquid separator  32 . Dehydrated higher boiling point crude oil is discharged from the dehydrator  24  through line  34 . 
     In the separator  32 , water and light hydrocarbons are separated by differences in specific gravity. The water is discharged through line  36  and pump  38 . The light hydrocarbons are transferred from the separator  32  using pump  40  via line  42 , and can be removed for disposal at line  44  or at least a portion recycled and mixed with the inlet crude oil  10  via line  46 , to dilute the incoming crude oil and thereby facilitate its further treatment. Non condensable, i.e. light hydrocarbons, inert gases (nitrogen, carbon dioxides, hydrogen sulfide) are vented from separator  32  and disposed of or recovered by any suitable safe means. 
     As shown by  FIG. 1 , dry oil can be recycled from  48  and recycled as stream  50  to mix with the inlet feed  18 , prior to being distributed onto the hot oil surface in the dehydrator  24 . 
     In order to maintain the temperature of the hot oil surface, at least a portion of the recycle stream  50  can be recycled directly to the dehydrator  24  and be distributed at or immediately below the surface of the hot dry crude oil. It has been found that by recycling the dry crude oil to inlet stream  18 , and separately or in combination with recycling dry crude oil to the surface of the hot bath by using stream  52  (dashed lines), the following significant benefits can be realized: 
     a) The water cut of the raw crude oil at stream  18  can be increased to greater than 10%, and even greater than 20% by volume. This enhancement means that the requirement for conventional treatment denoted as  12  can be eliminated, without risk of process instability and foaming of the dehydrator. 
     b) If a conventional primary treatment  12  is used, the recycle stream can be used to isolate the dehydrator from unstable or operational complications if the pretreatment becomes unstable. This means that the dry crude oil sales specification is not at risk, and rerun of off spec sales oil from sales oil storage tanks and pipelines is avoided. 
     The ratio of recycle at  50  to inlet feed can vary depending on the actual temperature and rate of the recycle  52  and the level of feed conditioning and water cut reduction required at the inlet to the dehydrator. Similarly, the ratio of recycle  52  to recycle  50  will vary for each application in order to establish a balance between dehydrator feed conditioning and dehydrator surface temperature. Depending on the relative size of oil recycle  50  to dry sales oil  34 , common pumps or separate pumps may be used, as known to those skilled in the art. Recycle  52  can also be provided by separate pumping means. 
     Referring to  FIG. 2 , shown is an enhancement to the recycle variation of  FIG. 1 , where a heat exchanger means  54  is added-to the recycle circuit to condition the temperature for steams  56  and  52 . The streams,  56  and  52  can be heated or cooled to the same temperature or independently to separate temperatures in order to seek the thermal balance of the feed stream and hot crude oil bath surface. Any form of suitable heat source, such as direct fired heaters, indirect fired heaters, heat exchangers or heat recovery or cooling apparatus may be selected. A further consideration for temperature at the streams  56  and  52  is whether the feed is from a heated primary treatment means at 170° F. to 285° F. (77° C. to 141° C.) or from a raw crude storage tank at 60° F. to 100° F. (16° C. to 38° C.) 
       FIG. 3  illustrates an additional enhancement to include a solid/liquid separator means  62 , used to remove suspended solids such as clay, sand, and precipitated salts from the dehydrated crude oil. The solid/liquid separator  62  may be selected from any suitable separator device known to those skilled in the art, such as gravity separators, clarifiers, filter, screens, cyclones and centrifuges. The recycle stream from  50 , is sized to satisfy the range of operation of the solid/liquid separator device  62  and specifically sized to accommodate a solids removal rate at  64  greater or equal to the solids content entering the dehydrator  24  at  18  and being produced in the dehydration process. 
     The removal of the solids can be performed on a continuous or batch basis and primarily allow for the ongoing removal of solids from the dehydrator  24  to prevent buildup and plugging. Buildup of solids on the heating elements contained in  24  or external to  24  is detrimental to the elements performance and can become a safety issue. 
     Turning to  FIG. 4 , shown is a further variation of the invention showing the addition of a water wash means to the dehydrator to remove dissolved solids. The raw crude oil can contain high concentrations of sodium, calcium, magnesium, chlorides, sulfur, carbonates, silica, etc. All, these compounds, especially the chloride are currently undesirable in the dry crude sales product and may have significant commercial impact on the price for the crude oil, or even restrict sales. Typically, refineries are currently requiring less than 30 ppm (wt) chlorides in the sales crude oil. 
     Using the enhancement shown by  FIG. 4 , clean water  66  is injected and intimately mixed with the raw crude oil  10  at  68 . The feed mixture  10  is passed through primary treatment separator at  12 . The bulk of the brine contaminated water is separated from the oil and discharged through line  22  to a water treatment unit  70 . 
     The washed crude oil is discharged at  18  and becomes the feed stream to the dehydrator. The feed can be conditioned either in the primary treatment  12  or by using the recycle stream  50  and  52  to ensure stable dehydrator  24  operation. The washed crude at  18  contains significantly reduced levels of dissolved compounds, meeting or exceeding the sales oil specification requirements. 
     The water treatment scheme selected for each application must ensure that the undesirable compounds in stream  22  are sufficiently removed to satisfy the process removal requirements at  18 . Typical water treatment practices, are microfiltration, reverse osmosis, distillation, flocculation, clarification and coagulation. 
     Treated water  72  enters the treated water surge vessel  74  and is transferred by pump  76  for reinjection at  68  using line  66 . 
     As an option, condensed water from the separator  32  can be transferred directly by pump  78  to either the treated water surge tank  74  by line  80  or to a water treatment unit  70  by line  82  if water treatment is required. The net water production would discharge from the separator  32  at stream  84 , or from the water treatment unit  70  by means of stream  88 . Fresh water makeup can be introduced to the treated water storage tank  74  at  90  if a water balance deficit is encountered. 
     Referring now to  FIG. 5 , shown is a further embodiment of the present invention where the dehydrator  24  is divided into zones for solids separation. As is illustrated in  FIG. 5 , there is a solid separation zone, generally denoted by numeral  100  within the dehydrator  24  and a clean, dry oil zone denoted by numeral  102 . Zones  100  and  102  are separated by a separation baffle  104 , which baffle  104  may be composed of any suitable baffle structure known to those skilled in the art for isolation of a liquid containing suspended solids such that the baffle facilitates sufficient residence time to permit gravity settlement of the existing solid or solids which are in a growth phase. The baffle  104  therefore provides a weir where hot/dry oil may flow into zone  102  substantially free of any solids. 
     The solid (not shown) may be collected in a pan structure denoted by numeral  106  and shown best in FIG.  6 . 
     The dry oil recirculation loop, denoted by numeral  108  containing suspended solids from between 0 weight percent and 30 weight percent and more particularly, near 0 (0.5 weight percent) to 5 weight percent are pumped through line  50  to a solids/liquid separation means  62 ; The solids may be removed by simple purge stream (either batch or continuous) or by a solid/liquid separation device such as a gravity settling tank or vessel, filter device, filter press, hydrocyclone, centrifugal separator or centrifuge or any combination of these components (none of which is shown). A flushing recycle loop (not shown) is commonly included between line  50  and pans  106  to assist with flushing of the solids and prevents solids build up. A washing solvent, such as a portion of the diluent created by the flash treating process, denoted by numeral  110  may be used to wash the solids free of any hydrocarbon compounds. 
     The hot dehydrated oil, now substantially free of suspended solids is recycled from separation device  62  to the dehydrator bath surface  52  (just beneath the surface as shown in the drawing) and/or the source oil inlet, denoted in this Figure by numeral  53 . The hot dry oil surface circulates internally along the dehydrator and accumulates into the dehydrated oil zone  102  for further transfer by a line  34 . Further heat energy may be added to the recycle stream  51  to maintain a level of vaporization in the source oil inlet and the desired temperature of the hot dry oil surface. Where the temperature of the source oil at  18  is sufficiently high to meet the energy balance of the dehydrator for a given source oil water content, then stream  53  may be deleted entirely. Heat energy may be added in the recycle streams and/or internally of the bath of the dehydrator  24  as discussed herein previously. Common practices of internal heating, well known to those skilled, consist of fire tubes or other heating devices (not shown). 
     The solids, sludge and other wash diluent as well as hydrocarbon carryover from separation device  62  may be disposed of directly or redissolved/slurried into the source water with a mixing device, globally denoted by numeral  112 . Diluent and hydrocarbon fluids can be skimmed from tank  112  through circuit  114  and recycled via line  46  to the source  10 . 
     The recycle rate for a circuit  50  may be set by the process heating requirements of the streams  52  and  53  or the minimum rate required by the solid liquid separation device  62  to remove the level of source suspended and produce solids on a continuous or batch processing basis. The recycle streams may also be separate with different pumping devices to meet specific needs. The size of the solids and particle distribution of the solids will vary depending on the solid composition, the level of solid residence time and the final solids concentration designed into the dehydrator and the methodology selected for removal. 
     Referring now to  FIG. 7 , shown is a further variation of the arrangement shown in FIG.  5 . In this embodiment, the baffle  104  is absent from the internal volume of the dehydrator  24 . In this configuration, solids collect in the entire bottom of the dehydrator  24  and collect at the pans  106  illustrated in FIG.  7  and in cross section in FIG.  6 . Recycle stream  50  supplies necessary thermal energy as discussed herein previously and may also be employed for flushing pans  106 . 
     A separate stream  116  can be drawn from the bottom of dehydrator  24  and passed through a solid liquid separation device  118 . Dry crude, substantially free of solids can then be transferred from the separation device  118  via line  34 . Any surplus dry oil can be recycled to provide a defoaming function to flash gases (not shown), the surplus oil indicated from separation device  118  via line  120 . 
     With respect to  FIG. 8 , the treater  24 , in this embodiment, is reconfigured from the longitudinally disposed arrangement shown in the previous Figures to a conical version as illustrated in FIG.  8 . This arrangement is useful for higher solids loading in the material to be treated, to accommodate space restriction or alternate distillation configurations. 
     In the example, the dehydrator  24  is reconfigured to a vertically disposed cylindrical design with a conical bottom section. An advantage associated with this arrangement have been the possibility of introducing the recycle oil and or source oil via a centrifugal entry. This has energy ramifications since it is known that mechanical agitation, particularly by a centrifuge, will result in solid particles being disassociated from the liquid within which they are contained. At the same time gravity settling is achieved in the bottom conical section of the dehydrator. By combining the two separation techniques, i.e. the mechanical agitation and the gravity separation, a dry clean oil zone develops approximately in the middle region of the dehydrator, broadly denoted by numeral  122  and solids are prevented from entering this zone due to the motion of the fluid and the introduction of a coaxial baffle  124 . Dry oil, substantially devoid of any solids is removed via line  48  and transferred for subsequent unit operations or sales or further recycled back to dehydrator  24  for any other suitable purpose (defoaming, temperature control, etc.). Dry oil with solids entrained therein is transferred to separation device  62  as indicated herein previously where a substantial amount of the solids are removed by simply purging or by suitable separation as discussed herein previously. 
     Turning to  FIG. 9 , shown is a further variation on the conical dehydrator system. In this embodiment, dry oil with solids entrained therein is collected entirely within the conical section denoted by numeral  109  of dehydrator  24 . Once within the conical section  109 , the fluid is circulated to provide the necessary energy requirement at loops  52  and  53  as discussed herein previously. 
     In  FIG. 10 , further modifications to the dehydrator  24  are illustrated in the process flow diagram depicted. In this embodiment, a distillation tower extends from the dehydrator  24 , with the distillation tower being broadly denoted by numeral  126 . This is a particularly convenient feature since the distillation portion  126  can be employed to selectively separate and distill any hydrocarbon fraction desired. 
     Operational parameters for the distillation tower  126  will be appreciated by those skilled in the art. The distillation apparatus may be attached directly to the unit or provided separately. 
     Turning to  FIG. 11 , shown is a dehydration, separation and upgrading process flow diagram where the dehydration circuit shown herein previously is joined with an overall processing scheme for upstream heavy oil production such as SAGD or CSS. 
     In this embodiment, the source is well effluent, sharing a common numeral with the source from previous flow diagrams. The effluent  10 , which is typically at a temperature of greater than 285° F. and at approximately 350 psig (140° C. and 2400 kPa) is introduced for pretreatment at  12  where bulk water, solids, dissolved compounds, inter alia are removed. The hot emulsion, generally containing less than 5 weight percent BS and W is flashed in dehydrator  24  at atmospheric pressure and temperatures of greater than 220° F. (105° C.) where the water and light hydrocarbons are distilled and suspended-solid contaminants are removed. The dry heavy oil exiting the system at  34  is a particularly useful stream for heavy oil partial upgrading processes (such as distillation, vacuum distillation and solvent deasphalting) where the crude oil product quality is upgraded from approximately 7 to 10 API to about 21 API with a viscosity-of less than 350 CSt at 10° C., primarily for pipeline transport to refineries. 
     As an alternative, the cleansed dry heavy oil is also suitable as a precursor material for full upgrading conversion such as visbreaking, hydro processing, and thermal cracking. In the absence of the upgrading process, the cleansed dry crude requires blending with about 20% to 30% by volume diluent and subsequently must be shipped as dilute crude product by pipeline to a refinery capable of treating the blended heavy oil. 
     By following the enhancements independently or in combination, the process methods as described by this invention, will result with dry clean crude oil meeting or exceeding new sales specifications for commercial sale. 
     As a further variation,  FIGS. 9 and 10  illustrate an optional diluent makeup stream  130  which can be mixed with the light hydrocarbon stream  46  and blended with the source crude oil  10  prior to the pretreatment step  12 . The addition of the diluent reduces the density and viscosity of the heavy oil and creates the density difference and separation motive force between the heavy oil and the produced water, thereby breaking down the oil emulsion and producing a lower water cut oil feed to the dehydrator at  18 . A further advantage of this embodiment is that the pretreatment separation step can be performed at the source crude oil inlet pressures and temperatures, typically less than 284° F. (140° C.), thereby requiring no additional heat energy input. The diluent makeup stream can primarily contain heavier molecular weight components, such as pentane and heavier, and perform the separation function and generally pass through the dehydrator with the sales oil and form part of the shipping diluent volume required. 
     A further advantage of the blend treating pretreatment step is that only the low water cut dehydrator feed  18  is heated to above 212° F. (100° C.) for flash treating. The dehydrator operating temperature and pressure are selected, by those skilled in the art, to match the required diluent  130  and light hydrocarbon  46  volume and composition and perform the basic water distillation function. By carefully selecting the dehydrator distillation and hydrocarbon recycling conditions, a specific hydrocarbon distillation cut can be achieved for the sales oil, thus providing a controlled feed composition  34  for further downstream full or partial upgrading operations  120 . 
     Turning to the embodiment of the invention shown schematically  FIG. 12 , a diluent recycle system is shown as a further unit operation in the dehydration and solid removal method. Effluent stream  10  undergoes pretreatment  12  as indicated with previous embodiments. The temperature at which the effluent is contacted for pretreatment is between 284° F. (140° C.) and 356° F. (180° C.). Prior to contacting the pretreatment phase of the operation, the stream is cooled by a heat exchanger which may comprise a boiler feed water heat exchanger as an example to less than 212° F. (100° C.) and more desirably between 176° F. (80° C.) and 203° F. (95° C.) for atmospheric downstream processing. 
     Recycled diluent (discussed in greater detail herein after) is mixed with the effluent material at  142  prior to contact with the pretreatment phase. 
     As generally described herein previously, pretreatment, although indicated in  FIG. 12  as a single unit operation may comprise several operations including free water knockout, desalination, filtration or any combination of operations to facilitate reduced water content and salt content in the effluent stream (bitumen emulsion). Produced water recovered from the pretreatment operation is recovered and recycled through stream  22  to be used as boiler feed water for, example, a SAGD steam generation operation. 
     Once pretreated, the emulsion exiting the pretreatment operation  12  contains significantly lower concentrations of salts, solids and water. In particular, the water content is less than 10% by volume and more desirably less than 2% by volume. This pretreated emulsion is pumped by pump  144  and passed through heat exchanger  146  prior to entering the dehydrator  24 , the latter having been discussed thoroughly herein previously. Additional heat is added to the stream  148  from heat exchanger  146  with the quantity of heat being sufficient to vaporize at least some of the water in the stream and the light diluent hydrocarbons. Typically, the temperature of the stream is between 266° F. (130° C.) and 356° F. (180° C.). As a further efficient provision, further heat can be added by heat exchanger  54  from stream  51  to recover substantially all of the water and a significant portion of the light hydrocarbon diluent. 
     Having been exposed to the dehydrator, the emulsion exits as a dry bitumen via stream  34  and is elevated in temperature to between 392° F. (200° C.) and 662° F.(350° C.) by heat exchanger  150 . This assists in full diluent recover. Having been exposed to heat exchanger  150 , the stream  152  (now elevated in temperature to approximately 392° F. (200° C.)) enters a steam stripping tower  154  where steam, denoted by numeral  153  is used to strip the diluent from the bitumen. The quantity of steam required and the temperature of streams  18 ,  51  and  152  are optimized for the type of diluent being used. Typical diluents include synthetic crude oil (SCO), naphtha and natural gas condensates. In terms of the quantity of recycled diluent, this is determined by the bitumen water separation parameters required in the pretreatment phase  12 . 
     The vapor recovered from dehydrator  24  and stripping tower  154  may be either independently or commonly collected and condensed in a cooler  30  and vessel  32 . A portion of the light hydrocarbon diluent may be transferred as reflux back to the stripper  154 , denoted by numeral  156 . The remaining amount and major amount of the condensed diluent is recycled to the onset of the process at  142 . Preheating may be applied using exchanger  158  to control the inlet conditions at the pretreatment phase  12 . Any water  36  and non-condensable vapors separated in vessel  32  are disposed of in an efficient manner. 
     Dry crude exiting stripper  154 , denoted by numeral  155  may be recirculated through heat exchanger  146  for heat recovery and subsequently discharged. A further heat exchanger  160  may be provided for temperature reduction. 
     The solvent to bitumen ratio which establishes the rate of diluent recycle and injection at  142  is generally optimized between 0.1 and 1.0. As an example, it is typical to have a ratio of about 0.3 to 0.6 diluent to bitumen. Optimization of this parameter avoids the onset of asphaltene precipitation and minimizes overall energy consumption. Further, optimization of the actual composition of the diluent recycle stream is important; a great amount of aromatic as opposed to paraffinic hydrocarbons in the recycled diluent may be desirable in order to avoid asphalt precipitation and optimize recycle rate of the diluent. Composition of the diluent can be adjusted by changing composition of the diluent make up and by process parameter adjustment. 
     By the methodology followed in  FIG. 12 , it has been found that extremely high recycle rate (greater than 90% and in some cases greater than 98%) recovery of the diluent is possible. This provision eliminates the requirement for major processing units at the refinery/upgrader and alleviates the burden in the industry currently realized by a lack of diluent and further avoids unnecessary expenditure typically associated with resupplying diluent at a site. This inherently makes the process more efficient and cost effective. 
     In terms of the stripping operation, although a stripping tower has been set forth in  FIG. 12 , it will be readily appreciated that any separation technique which achieves the desired result may be employed. Such suitable techniques include multiple flashing, distillation, vacuum flashing, super critical separation and any other unit operation in combination with or without a stripping tower known to achieve the desired result and apparent to those skilled in the art. 
     Although embodiments of the invention have been described above, it is not limited thereto and it will be apparent to those skilled in the art that numerous modifications form part of the present invention insofar as they do not depart from the spirit, nature and scope of the claimed and described invention.