Patent Publication Number: US-2019177625-A1

Title: Method for processing viscous oil or oil products and a plant for their refining.

Description:
This application claims priority to provisional application #62/348,129 for METHOD FOR PROCESSING VISCOUS Oil OR OIL PRODUCTS AND THE PLANT FOR THEIR REFINING, filed on Jun. 9, 2016 
    
    
     FIELD OF THE INVENTION 
     The invention relates to oil producing, oil refining, chemical and petrochemical industries, particularly to changing the initial feedstock properties, that is, to processing viscous oil or oil products, including viscosity reduction, refining and cracking. 
     BACKGROUND OF THE INVENTION 
     A number of approaches for processing of viscous oil and oil products exist and are described below. However, all currently-existing solutions are characterized by low efficiency of the process, high energy consumption and/or require the application of additional heating or the use of chemical agents. 
     One method of vortex cracking of oil and oil products (see patent RU 2305699 C1, 2007. 09. 10), includes a separation of oil or oil products into fractions. This method is implemented by feeding oil or oil products into a vortex hydrocavitation facility, after processing in which the product is returned into a tank for oil and oil products, from where they are fed into a vortex tube for separation into fractions. 
     Among the known methods is a method for separating emulsions, particularly high-viscosity stable emulsions (see patent RU 2286194 C2, 2006. 10. 27), which includes a jet supply of an emulsion carried out in the form of a vortex swirling flow. In its central zone, through the use of centrifugal forces, a reduced pressure equal to the pressure of a saturated vapor of a low-boiling liquid is created. And in its peripheral zone, a pressure is produced, which pressure provides displacement of a low-boiling liquid to the central zone of the vortex swirling flow. Part of the peripheral flow is withdrawn into the initial emulsion for circulation; the emulsion vortex flow is heated to the temperature of a saturated vapor by means of shock diffusion, and after applying shock diffusion, the heated central and peripheral flows are withdrawn into the initial emulsion for recirculation. 
     As stated above, disadvantages of these known methods are insufficient efficiency as well as high energy consumption of processing viscous oil or oil products, including viscosity reduction, refining and cracking. Processing facilities known in the art also have a number of other deficiencies that are resolved by the present invention. 
     For example, a processing facility is described in the patent related to the method for separating emulsions, particularly high-viscosity stable emulsions (see patent RU 2286194 C2, 2006. 10. 27). The processing facility contains a catcher tank, pump, vortex generator, shock diffusion device. The intake fitting of the pump is connected by pipelines to the source of the initial emulsion, with the catcher tank and with the peripheral flow extraction fitting located behind the shock diffusion device; the pump&#39;s discharge fitting is connected to the vortex generator; the near-axial flow extraction fitting located behind the shock diffusion device as well as the fitting located in front of the shock diffusion device are both connected by pipelines to the catcher tank. 
     Also known in the art are facilities for vortex cracking of oil and oil products (see patent RU 2305699 C1, 2007. 09. 10), which contains a tank for oil and oil products, rectifying chamber and reaction modules, a tank for extracted products. The tank for oil and oil products is connected to rectifying chamber and reaction modules by means of a double-position valve and oil pumps. The rectifying chamber is designed as a vortex hydrocavitation facility, which contains, located in sequence, an input device, swirler, vortex tube, unswirler and an output device; a reaction module is designed as a vortex tube with a tangential inlet nozzle, collection chamber and a flow control valve; the vortex tube is connected to the tanks for collecting extracted fractions. 
     The numerous disadvantage of the known processing facilities include the impossibility of the given design to provide sufficient efficiency and low energy consumption in the course of processing viscous oil, including viscosity reduction, refining and cracking. 
     The technical problem solved by the proposed invention involves the improvement of efficiency of the process with regards to specific performance, decrease of the energy consumption of the viscous oil and oil products processing, including viscosity reduction, refining and cracking without applying any additional heating or using chemical agents. 
     SUMMARY OF THE PRESENT INVENTION 
     The present invention is defined by the following claims and nothing in this section should be taken as a limitation on those claims. 
     The present invention describes and claims a plant and a method for processing viscous oil and oil products. The plant comprises a plurality of reaction modules, a plurality of rectifying chambers, pipelines, and a plurality of hydrocavitation generators. Each reaction module comprises a reaction module&#39;s tank, a pump and at least one (and in some embodiments, several) hydrocavitation generator. Each reaction module further comprises a plurality of intermediate reaction stages. These intermediate reaction stages further comprise a last intermediary reaction stage. 
     Each rectifying chamber comprises a rectifying chamber tank, a rectifying pump, at least one of the plurality of hydrocavitation generators. Each rectifying chamber comprises a plurality of intermediate rectifying stages. 
     The reaction module and the rectifying chamber are interconnected. The plurality of intermediate reaction stages are connected by pipelines. The last intermediary reaction stage is connected by the pipelines to a rectifying chamber; 
     Each of the plurality of intermediate reaction stages comprises a tank, a pump and at least one of hydrocavitation generators; said hydrocavitation generator comprising an outlet pipe. The outlet pipe of a hydrocavitation generator is connected via the inlet pipe to the reaction module&#39;s tank. 
     The method comprises the steps of providing viscous oil products into the plant of the present invention. The viscous oil products are then processed in a reaction module. Processing in a reaction module comprises the steps of: feeding the viscous oil products into the hydrocavitation generator to obtain a product, supplying the product to the fractionation device, and continuously and consecutively delivering and processing the feedstock in a recirculation mode at one or more subsequent stages within the reaction modules. 
     Preferred embodiments of the method of the present invention further comprise the step of carrying out the intermediary processing between the stages in an intermediary reaction module. Processing in the intermediary reaction stages comprises the steps of directing recirculated oil products (following a heat-mass exchange in the preceding tank) by way of a pump into the hydrocavitation generator of the interim module to obtain further reduction of the treated product viscosity, and subsequent delivery of the processed product to the next stage of the reaction module. 
     Kinematic viscosity of processed oil product is preferably measured at the output of the reaction module to ascertain whether the viscosity requirement is met. The level of viscosity at the output of one of the plurality of the hydrocavitation generators may be measured. If the level of viscosity has not reached the preset value, the under-processed oil product may be directed back to the tank of the preceding stage. If the level of viscosity has reached the preset value, treated oil product is preferably forwarded for final processing into a rectifying chamber. 
     In some of the preferred embodiments, the processing is carried out in a plurality of parallel-operating hydrocavitation generators at each stage of the reaction modules. The mass flow of the product fed into the one or more hydrocavitation generators is preferably equal to a multiple of the mass flow of the product fed into a reaction module. 
    
    
     
       BRIEF DESCRIPTION OF THE DRAWINGS 
         FIG. 1  illustrates a schematic structure of the preferred embodiment of the plant of the present invention. 
         FIG. 2  depicts highly-detailed schematic structure of one of the preferred embodiments of the plant of the present invention. 
         FIG. 3  is a flowchart, illustrating a preferred embodiment of the method of the present invention. 
     
    
    
     DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENTS 
     The technical issues resolved by the present invention involve the improvements to efficiency of the process with regards to specific performance, decrease of the energy costs of processing of the viscous oil and oil products, including viscosity reduction, refining and cracking. All of the above is achieved without application of additional heating or use of chemical agents. 
     The technical issues are resolved due to novel distinctive features of the proposed plant and method for processing of viscous oil or oil products, including viscosity reduction, refining and cracking. One of these features is characterized by the fact that oil or oil products are continuously and consecutively fed into and processed in a recirculation mode at one or more subsequent stages within reaction modules (also known and referred to as “reaction cells”). Between those stages the intermediary processing is carried out, which is completed (if necessary) in a fractionation device; in this case the processing in each reaction module includes the heat-mass exchange provided in the tank, delivery by a pump and processing in one or more hydrocavitation generators connected by a parallel hydraulic connection as well as its further feeding into the initial tank. From this tank the product is supplied to an intermediate stage for further processing, which includes feeding by a pump and treatment in a hydrocavitation generator as well as subsequent delivery to the next stage, in which case the raw material mass flow is chosen to be equal to the mass flow of the processed product. 
     Another of the many distinctive novel features of the proposed plant for processing viscous oil or oil products, (including viscosity reduction, refining and cracking) is illustrated by the fact that the plant comprises one or more reaction modules&#39; stages connected by pipelines and a provision of the intermediary reaction stages in between. The last intermediary stage is (if necessary) connected by a pipeline to a rectifying chamber or directly to a consumer of the processed oil or oil products. Each reaction module contains a tank, a pump and one or more hydrocavitation generators connected by a parallel hydraulic connection and pipelines, and the outlet pipe of the hydrocavitation generators is connected to the reaction module&#39;s tank; the intermediary reaction modules contain a pump and a hydrocavitation generator. 
     The processing plant and method of the present invention will now be illustrated by reference to the accompanying drawings. Preferred embodiments of the present invention have been assigned reference numeral  1000 . Other elements have been assigned the reference numerals referred to below. 
     The proposed invention  1000  is illustrated by the drawings, where  FIG. 1  shows the schematic structure of the plant, where each reaction module comprises several hydrocavitation generators, connected by a parallel hydraulic connection, using their own pumps. 
     The proposed plant ( FIG. 1 ) comprises one or more stages of reaction modules  1  and  2  connected in sequence by pipelines to one or more intermediary reaction modules  3  and  4 ; reaction module  4  is connected by a pipeline to a rectifying chamber  5 ; each of reaction modules  1  and  2  comprises tanks  6  and  7  correspondingly, hydrocavitation generators  8  and  9  with pumps  10  and  11 , and each of intermediary reaction modules  3  and  4  comprises hydrocavitation generators  12  and  13  with pumps  14  and  15 . 
     Tank  6  of reaction module  1  comprises inlet fitting  16  connected to the source of the processed oil or oil products, and outlet pipe  17  connected to the input of pump  14  of reaction module  3 ; the outlet fitting of pump  14  is connected by pipeline  18  to the inlet fitting of hydrocavitation generator  12  of reaction module  3  and by pipeline  19  is connected to tank  7  of reaction module  2 ; the outlet fitting  20  of tank  7  is connected to pump  15  of reaction module  4 ; the outlet fitting of pump  15  is connected by pipeline  21  to hydrocavitation generator  13  of reaction module  4 ; and generator  13  is connected by outlet pipe  22  to rectifying chamber  5 . 
     Tank  6  of reaction module  1  is connected by pipeline  23  to pumps  10 , which have a parallel hydraulic connection, with their outlet fittings  24  connected to the inlet fittings of hydrocavitation generators  8  correspondingly, and the outlet fittings of generators  8  are connected by pipeline  25  to tank  6  of reaction module  1 . Tank  7  of reaction module  1  is connected by pipeline  26  to pumps  11 , which have parallel hydraulic connection; their outlet fittings  27  are connected correspondingly to the inlet fittings of hydrocavitation generators  9 , outlet fittings of which are connected by pipeline  28  to tank  7  of reaction module  2 . 
     Tanks  6  and  7  of reaction modules  1  and  2  correspondingly comprise fittings  29  and  30  for gaseous fraction discharge as well as for noncondensing gases extraction. 
     The proposed method is as follows. Tank  6  of reaction module  1  is filled with oil or oil products. After filling tank  6 , circulating pumps  10  are turned on; they feed oil or oil products into hydrocavitation generators  8  providing recirculation mode in tank  6  of reaction module  1 . 
     After reaching the preset parameters of oil in tank  6 , continuous feeding of oil or oil products is provided through fitting  16  into tank  6  and through pipeline  17 —to the input of pump  14  of intermediate reaction module  3 , from where it is fed into hydrocavitation generator  12 , where intermediate hydrocavitation processing of oil or oil products is carried out. In this case the flow of oil or oil products fed for processing into tank  6  and their flow into reaction module  3  are maintained equal. 
     The oil or oil products processed in the intermediary reaction module are fed into tank  7  of reaction module  2  from where it is fed into pumps and hydrocavitation generators  9 . 
     From tank  7  of reaction module  2  oil or oil products are fed into reaction module  4  for the final hydrocavitation processing; the processing is completed (if necessary) in a fractionation device or oil or oil products are delivered directly to their consumer. 
     Processing in each reaction module (whether it is module  1  or module  2  includes heatmass exchange in a tank, delivery by a pump or pumps to one or more hydrocavitation generators for processing and further feeding into the initial tank. From this tank part of the oil or oil products are fed into pumps for recirculation while the other part is delivered to the intermediary stage for further processing, which includes delivery by a pump and processing in a hydrocavitation generator as well as further feeding into a reaction module of the next stage and so on; from there oil or oil products are fed into a rectifying chamber or delivered directly to their consumer. 
     If the goal is only to reduce the level of viscosity, then the process is limited to processing in one or more reaction modules depending on the level of viscosity of initial oil or oil products, the required output level of viscosity after processing and the method of implementation of a hydrocavitation generator&#39;s operation; in this case the mass flow of the oil or oil products delivered for processing is chosen to be equal to the mass flow of the processed oil or oil products. The mass flow of oil or oil products fed into hydrocavitation generators operating in a recirculation mode, shall be set to be equal to a multiple of the mass flow of oil or oil products, which are fed into a reaction module, and in case of using several parallel operating hydrocavitation generators, the mass flow in each of hydrocavitation generators shall be chosen to be equal to the mass flow of the product delivered for processing. 
     Under steady-state conditions the temperature in a tank at each reaction module stage is configured and maintained constant and equal to a mass-averaged temperature of the product in a tank. 
     During the processing, noncondensing gases are removed from each tank. 
     The proposed plant operates as follows ( FIG. 1 ). Tank  6  of reaction module  1  is filled with oil or oil products through fitting  16 . After filling tank  6 , circulating pumps  10  are turned on; they are connected by pipeline  23  to tank  6 , which provides feeding of oil or oil products along pipelines  24  into hydrocavitation generators  8 ; the processed oil or oil products are fed from them into tank  6  providing a recirculation mode in reaction module  1 . 
     After reaching the preset parameters of oil in tank  6 , continuous supply of oil or oil products is provided into tank  6  and through pipeline  17 —to the input of pump  14  of intermediate reaction module  3 , from where it is fed through pipeline  18  into hydrocavitation generator  12 , where intermediate hydrocavitation processing of oil or oil products is carried out. In this case the flow of oil or oil products fed for processing into tank  6  and their flow into reaction module  3  are maintained equal. 
     The oil or oil products processed in the intermediary reaction module  3  are fed through pipeline  19  into tank  7  of reaction module  2 , after filling which they are fed through pipeline  26  into pumps  11 , from where they are fed through pipeline  27  into hydrocavitation generators  9 , and through pipeline  28  the processed oil or oil products are returned to tank  7  of reaction module  2 . 
     From tank  7  of reaction module  2  oil or oil products are fed through pipeline  20  into pump  15  of reaction module  4 , from where they are fed through pipeline  21  into hydrocavitation generators  9 ; from there they are fed through pipeline  22  into rectifying chamber  5 , where the processing is completed by fractionation or oil, or oil products are delivered directly to their consumer. 
     During the processing, noncondensing gases are removed from tanks  6  and  7  through fittings  29  and  30 . 
     Application of hydrocavitation generators, which are forming strongly whirling counter-flows with high radial pressure gradient and highly developed anisotropic turbulence along with generated intensive acoustic vibrations, allows for influencing the flow of the processed oil or oil products by means of acoustic vibrations at sonic and ultrasonic frequencies, which in its turn leads to intensification of flow heating, enhancement of cavitation effects, formation of strong pressure pulses and intensification of heat-mass exchange processes. These factors account for destruction of paraffin, decomposition of chemical bonds (C—C) with free radicals and of carbamides formation in long molecules, separation of the mixture into light and heavy fractions, which in turn results in changing physical and chemical properties of oil, density decrease, viscosity reduction, etc. 
     Application of two and more stages&#39; scheme for implementation of the operational process performed in main and intermediary reaction modules placed in sequence, which contains hydrocavitation generators, when carried out in recirculation mode in main reaction modules, allows: to increase the speed of viscosity reduction; to increase specific mass performance with regards to the processed oil or oil products, i.e. the performance related to the plant&#39;s mass, and to decrease the number of reaction modules&#39; stages. 
     The use of parallel operating hydrocavitation generators in main reaction modules allows for applying hydrocavitation generators and their feeding pumps with the same geometric dimensions and technical specifications. 
     Thus the use of the proposed method and the plant  1000  for processing viscous oil and oil products, including viscosity reduction, refining and cracking, allows for improving the efficiency of the process with regards to specific performance, reducing energy consumption of the processing without applying any additional heating or using chemical agents. 
       FIG. 2  depicts highly-detailed schematic structure of one of the preferred embodiments of the plant  1000  of the present invention.  FIG. 2  illustrates the positioning and function of the following elements of the present invention:
     I—First Stage Tank;   II—Second Stage Tank;   III—Third Stage Tank;     1 —Feedstock Tank;     2 —Feeding Pump;     3 —Stop Valve;     4 —Feeding Pipeline;     5 ,  6  and  7 —Hydro-generators of the First Stage;     8 ,  9  and  10 —Transfer Pumps of the First Stage;     11 ,  24  and  37 —Feed Pipeline;     12 ,  13 ,  14 ,  25 ,  26 ,  27 ,  38 ,  39  and  40 —Stop Valves;     15 ,  28  and  41 —Offlake Pipeline;     16 ,  17 ,  29 ,  30 ,  42  and  43 —Stop Valves;     18 ,  31  and  44 —Flushing Tank;     19 ,  20 ,  32 ,  33 ,  45  and  46 —Stop Valves;     21 ,  34  and  47 —Flushing Pipeline;     22 ,  23 ,  35 ,  36 ,  48  and  49 —Pressure Sensors (manometer);     50 —Temperature Sensor (thermocouple probe);     51 —Drainage Pipe;     51   a —Stop Valve;     52 —Feed Pipeline;     52   a —Stop Valve;     53 —Viscometer,     54 —Drainage Pipe;     55 ,  56  and  58 —Stop Valves;     57 —Drain Connection;     59 —Hydro-generator of the Interim Stage;     60 —Transfer Pump of the Interim Stage;     61 ,  62  and  63 —Stop Valves;     64 —Offtake Pipeline;     65 —Stop Valve;     66 —Flushing Tank;     67  and  68 —Stop Valves;     69 —Flushing Pipeline;     70  and  71 —Pressure Sensors (manometers);     72  and  73 —Temperature Sensors (thermocouple probes);     74 ,  75  and  76 —Hydro-Generators of the Second Stage;     77 ,  78  and  79 —Transfer Pumps of the Second Stage;     80 ,  93  and  106 —Feeding Pipeline;     81 ,  82 ,  83 ,  94 ,  95 ,  96 ,  107 ,  108  and  109 —Stop Valves;     84 ,  97  and  110 —Offlake Pipeline;     85 ,  86 ,  98 ,  99 ,  111  and  112 —Stop Valves;     87 ,  100  and  113 —Flushing Tank;     88 ,  89 ,  101 ,  102 ,  114  and  115 —Stop Valves;     90 ,  103  and  116 —Flushing Pipeline;     91 ,  92 ,  104 ,  105 ,  117  and  118 —Pressure Sensors (manometers);     119 —Temperature Sensor (thermocouple probe);     120 —Drainage Pipe;     121 —Stop Valve;     122 —Feed Pipeline;     123 —Stop Valve;     124 —Viscometer;     125 —Drainage Pipe;     126 ,  127  and  129 —Stop Valves;     128 —Drain Connection;     130 —Hydro-generator of the Interim Stage;     131 —Transfer Pup of the Interim Stage;     132 ,  133  and  134 —Stop Valves;     135 —Offtake Pipeline;     136 —Stop Valve;     137 —Flushing Tank;     138  and  139 —Stop Valves;     140 —Flushing Pipeline;     141  and  142 —Pressure Sensors (manometers);     143  and  144 —Temperature Sensors (thermocouple probes);     145 ,  146  and  147 —Hydro-generators of the Third Stage;     148 ,  149  and  150 —Transfer Pumps of the Second Stage;     151 ,  164  and  177 —Feeding Pipeline;     152 ,  153 ,  154 ,  165 ,  166 ,  167 ,  177 ,  179  and  180 —Stop Valves;     155 ,  168  and  181 —Offtake Pipeline;     156 ,  157 ,  169 ,  170 ,  182  and  183 —Stop Valves;     158 ,  171  and  184 —Flushing Tank;     159 ,  160 ,  172 ,  173 ,  185  and  186 —Stop Valves;     161 ,  174  and  187 —Flushing Pipeline;     162 ,  163 ,  175 ,  176 ,  188  and  189 —Pressure Sensors (manometers);     190 —Temperature Sensor (thermocouple probe);     191 —Drainage Pipe;     192 —Stop Valve;     193 —Viscometer;     194 ,  195  and  196 —Drainage Pipe;     197 ,  198  and  199 —Stop Valve;     200 —Drainage Pipe;     201 —Stop Valve;     202 ,  203     204 —Drainage Pipe;     205 ,  206  and  207 —Stop Valve;     208 —Drainage Pipe;     209 —Stop Valve;     210 ,  211  and  212 —Drainage Pipe;     213 ,  214  and  215 —Stop Valve;     216 ÷ 233 —Temperature Sensors (thermocouple probes);     234 —Feeding Pipeline of the Final Stage;     235  and  236 —Stop Valves;     237 —Flushing Pipeline;     238 —Hydro-generators of the Final Stage;     239 —Transfer Pumps of the Final Stage;     240 ,  241  and  242 —Stop Valves;     243 —Flushing Tank;     244  if  245 —Stop Valves;     246 —Flushing Pipeline;     247 —Offtake Pipeline;     248 —Stop Valve;     249 —Drain Connection;     250 —Stop Valve;     251  and  252 —Pressure Sensors (manometers);     253  and  254 —Temperature Sensors (thermocouple probes);     255 —Drainage Pipe;     256 —Flushing Tank of the Feeding Pump;     257  and  258 —Stop Valves;     259 —Flushing Pipeline;     260 —Drain Connection;     261 —Stop Valve;   

     The description of the preferred embodiment depicted on  FIG. 2  is as follows: 
     1. First Stage 
     A feedstock of a very high viscosity is fed into a tank of the first stage I from the feedstock tank I by way of screw injection pump  2  through valve  3  via pipeline  4 . Tangentially to the surface of the tank in the first stage I there are three hydro-generators  5 ,  6  and  7 , where the cavitation treatment of the feedstock is carried out. 
     The feedstock to be processed is delivered to hydro-generator  5  by way of and through the first stage transfer pump  8  via feeding pipeline  11  through valves  12 ,  13  and  14 . The feedstock processed in hydro-generator  5  is fed into the tank of the first stage I via offtake pipeline  15  through valves  16  and  17 . Flushing of hydro-generator  5  and transfer pump  8  is carried out with a diesel fuel from flushing tank  18  through valves  19  and  20  via flushing pipeline  21 . Control over the pressure level is carried out using pressure sensor  22  at the outlet of transfer pump  8  by means of the pressure sensor  23  at the outlet of hydro-generator  5 . 
     The process in hydro-generator  5  is carried out as follows. Valves  19  and  20  on flushing pipeline  21  are closed. The supply of the feedstock to be processed is provided through the use of transfer pump  8  through opened valves  12 ,  13  and  14 . After it has been processed, the feedstock is carried off to first stage tank I via offtake pipeline  15  through opened valves  16  and  17 . For flushing hydro-generator  5  valves  12  and  17  are closed and valves  19  and  20  on flushing pipeline  21  are opened; as the result transfer pump  8  pumps diesel fuel over through hydro-generator  5  from flushing tank  18 . Valves  13 ,  14  and  16  during the flushing process are opened. When the flushing process is over, valves  19  and  20  are closed, and, if necessary, valve  17  is opened simultaneously; as the result the flushing fuel is fed into first stage tank I. In case of failure of the transfer pump  8 , valves  12 ,  13 ,  14 ,  16  and  17  are closed and the pump is replaced. 
     In the same way the feedstock to be processed is delivered to hydro-generator  6  by way of first stage transfer pump  9  via feeding pipeline  24  through valves  25 ,  26  and  27 . The feedstock processed in hydro-generator  6  is fed into the tank of the first stage I via offtake pipeline  28  through valves  29  and  30 . Flushing of hydro-generator  6  and transfer pump  9  is carried out with a diesel fuel from flushing tank  31  through valves  32  and  33  via flushing pipeline  34 . Control over the pressure level is carried out using pressure sensor  35  at the outlet of transfer pump  9  and by means of the pressure sensor  36  at the outlet of hydro-generator  6 . 
     The process in hydro-generator  6  is carried out as follows. Valves  32  and  33  on flushing pipeline  34  are closed. The supply of the feedstock to be processed is provided way of transfer pump  9  through opened valves  25 ,  26  and  27 . After it has been processed, the feedstock is carried off to the tank of the first stage I via offtake pipeline  28  through opened valves  29  and  30 . For flushing hydro-generator  6  valves  25  and  30  are closed and valves  32  and  33  on flushing pipeline  34  are opened; as the result, transfer pump  9  delivers diesel fuel over by way of the hydro-generator  6  from flushing tank  31 . Valves  26 ,  27  and  29  during the flushing process are opened. When the flushing process is over, valves  32  and  33  are closed, and, if necessary, valve  30  is opened simultaneously; as the result. the flushing fuel is fed into the tank of the first stage I. In case of failure of the transfer pump  9 , valves  25 ,  26 ,  27 ,  29  and  30  are closed and the pump is replaced. 
     In the same way the feedstock to be processed is delivered to hydro-generator  7  by way of the first stage transfer pump  10  via feeding pipeline  37  through valves  38 ,  39  and  40 . The feedstock processed in hydro-generator  7  is fed into the tank of the first stage I via offtake pipeline  41  through valves  42  and  43 . Flushing of hydro-generator  7  and transfer pump  10  is carried out with a diesel fuel from flushing tank  44  through valves  45  and  46  via flushing pipeline  47 . Control over the pressure level is carried out using pressure sensor  8  at the outlet of transfer pump  10  and by means of the pressure sensor  49  at the outlet of hydro-generator  7 . 
     The process in hydro-generator  7  is carried out as follows. Valves  45  and  46  on flushing pipeline  47  are closed. The supply of the feedstock to be processed is provided by way of the transfer pump  10  through opened valves  38 ,  39  and  40 . After it has been processed, the feedstock is carried off to the tank of the first stage I via offtake pipeline  41  through opened valves  42  and  43 . For flushing hydro-generator  7  valves  38  and  43  are closed and valves  45  and  46  on the flushing pipeline  47  are opened; as the result, transfer pump  10  delivers diesel fuel over by way of the hydro-generator  7  from flushing tank  44 . Valves  39 ,  40  and  42  during the flushing process are opened. When the flushing process is over, valves  45  and  46  are closed, and, if necessary, valve  43  is opened simultaneously; as the result, the flushing fuel is fed into the tank of the first stage I. In case of failure of the transfer pump  10 , valves  38 ,  39 ,  40 ,  42  and  43  are closed and the pump is replaced. 
     The processes in hydro-generators  5 ,  6  and  7  are carried out simultaneously and are repeated not less than 2÷3 times. Temperature control in first stage tank I is carried out by means of the thermocouple probe  50 . 
     Drainage of the flushing fuel from the tank of the first stage I is carried out via drainage pipe  51  through valve  51   a.    
     After processing in hydro-generators  5 ,  6  and  7  the feedstock from the tank of the first stage I is removed via pipeline  52  through valve  52   a . The viscometer  53  is installed on a pipeline  52 ; the needs for further processing of the feedstock are determined according to this viscometer&#39;s readings. To the extent that the processing in the tank of the first stage I turns out to be sufficient and the viscosity value meets the stated requirements, the final product is drained via pipeline  54  through opened valves  55  and  56  through drain connection  57  with valve  58  closed. 
     To the extent that the viscosity value does not meet the stated requirements, the feedstock to be processed is supplied to hydro-generator  59  by way of the interim stage&#39;s transfer pump  60  via feeding pipeline  53  through valves  61 ,  62  and  63 . The feedstock processed in hydro-generator  59  is fed into the tank of the second stage II via offtake pipeline  64  through valve  65 . Flushing of hydro-generator  59  and transfer pump  60  is carried out with a diesel fuel from flushing tank  66  through valves  67  and  68  via flushing pipeline  69 . Control over the pressure level is carried out using the pressure sensor  70  at the outlet of transfer pump  60  and by means of the pressure sensor  71  at the outlet of hydro-generator  59 . Control over the temperature level is carried out using the temperature sensor  72  at the outlet of transfer pump  60  and by means of the temperature sensor  73  at the outlet of hydro-generator  59 . 
     The process in hydro-generator  59  is carried out as follows. Valves  55  and  58  on drainage pipe  54  as well as valves  67  and  68  on flushing pipeline are closed. The supply of the feedstock to be processed is provided by way of the transfer pump  60  through opened valves  61 ,  62  and  63 . After it has been processed, the feedstock is carried off to the tank of the second stage II via offtake pipeline  64  through opened valve  65 . For flushing hydro-generator  59  valves  61  and  63  are closed and valves  67  and  68  on flushing pipeline  69  are opened; as the result, the transfer pump  60  delivers diesel fuel over by way of the hydro-generator  59  from flushing tank  66 . Valve  62  during the flushing process is opened. When the flushing process is over, valves  67  and  68  are closed, and valves  55  and  58  are opened; as the result, the flushing fuel is drained via pipeline  54  through valve  56  of the drain connection  57 . In case of failure of the transfer pump  60 , valves  55 ,  58 ,  61 ,  62  and  63  are closed and the pump is replaced. 
     2. Second Stage 
     The feedstock to be processed is fed into the tank of the second stage  11  through valve  65  via pipeline  64 . Three hydro-generators  74 ,  75  and  76 , where the cavitation processing of the feedstock is carried out, are placed tangentially to the surface of the tank of the second stage II. 
     The feedstock to be processed is supplied to hydro-generator  74  by way of the second stage transfer pump  77  via feeding pipeline  78  through valves  80 ,  81  and  82 . The feedstock processed in hydro-generator  74  is fed into the tank of the second stage II via offtake pipeline  84  through valves  85  and  86 . Flushing of hydro-generator  74  and transfer pump  77  is carried out with a diesel fuel from flushing tank  87  through valves  88  and  89  via flushing pipeline  90 . Control over the pressure level is carried out using the pressure sensor  91  at the outlet of the transfer pump  77  and by means of the pressure sensor  92  at the outlet of the hydro-generator  74 . 
     The process in hydro-generator  74  is carried out as follows. Valves  88  and  89  on flushing pipeline  90  are closed. The supply of the feedstock to be processed is provided by way the transfer pump  77  through opened valves  81 ,  82  and  83 . After it has been processed, the feedstock is carried off to the tank of the second stage  11  via offtake pipeline  84  through opened valves  85  and  86 . For flushing hydro-generator  77  valves  81  and  86  are closed and valves  88  and  89  on flushing pipeline  90  are opened; as the result, the transfer pump  77  delivers diesel fuel over by way of the hydro-generator  74  from flushing tank  87 . Valves  82 ,  83  and  85  during the flushing process are opened. When the flushing process is over, valves  88  and  89  are closed, and, if necessary, valve  86  is opened simultaneously; as the result, the flushing fuel is fed into the tank of the second stage II. In case of failure of the transfer pump  77 , valves  81 ,  82 ,  83 ,  85  and  86  are closed and the pump is replaced. 
     In the same way the feedstock to be processed is supplied to the hydro-generator  75  by way of the second stage transfer pump  78  via feeding pipeline  93  through valves  94 ,  95  and  96 . The feedstock processed in hydro-generator  75  is fed into the tank of the second stage II via offtake pipeline  97  through valves  98  and  99 . Flushing of the hydro-generator  75  and transfer pump  78  is carried out with a diesel fuel from flushing tank  100  through valves  101  and  102  via flushing pipeline  103 . Control over the pressure level is carried out using the pressure sensor  104  at the outlet of the transfer pump  78  and by means of the pressure sensor  105  at the outlet of the hydro-generator  75 . 
     The process in hydro-generator  75  is carried out as follows. Valves  101  and  102  on flushing pipeline  103  are closed. The supply of the feedstock to be processed is provided by way of the transfer pump  78  through opened valves  94 ,  95  and  96 . After it has been processed, the feedstock is carried off to the tank of the second stage II via offtake pipeline  97  through opened valves  98  and  99 . For flushing hydro-generator  75  valves  94  and  99  are closed and valves  101  and  102  on flushing pipeline  103  are opened; as the result, the transfer pump  78  delivers diesel fuel over by way of the hydro-generator  75  from flushing tank  100 . Valves  95 ,  96  and  98  during the flushing process are opened. When the flushing process is over, valves  101  and  102  are closed, and, if necessary, valve  99  is opened simultaneously; as the result, the flushing fuel is fed into the tank of the second stage II. In case of failure of the transfer pump  78 , valves  94 ,  95 ,  96 ,  98  and  99  are closed and the pump is replaced. 
     In the same way the feedstock to be processed is supplied to hydro-generator  76  by way of the second stage transfer pump  79  via feeding pipeline  106  through valves  107 ,  108  and  109 . The feedstock processed in hydro-generator  76  is fed into the tank of the second stage II via offtake pipeline  110  through valves  111  and  112 . Flushing of the hydro-generator  76  and transfer pump  79  is carried out with a diesel fuel from flushing tank  113  through valves  114  and  115  via flushing pipeline  116 . Control over the pressure level is carried out using the pressure sensor  117  at the outlet of transfer pump  79  and by means of the pressure sensor  118  at the outlet of the hydro-generator  76 . 
     The process in hydro-generator  76  is carried out as follows. Valves  114  and  115  on flushing pipeline  116  are closed. The supply of the feedstock to be processed is provided by way of the transfer pump  79  through opened valves  107 ,  108  and  109 . After it has been processed, the feedstock is carried off to the tank of the second stage II via of take pipeline  110  through opened valves  111  and  112 . For flushing the hydro-generator  76  valves  107  and  112  are closed and valves  114  and  115  on flushing pipeline  116  are opened; as the result, the transfer pump  79  delivers diesel fuel over by means of the hydro-generator  76  from flushing tank  113 . Valves  108 ,  109  and  111  during the flushing process are opened. When the flushing process is over, valves  114  and  115  are closed, and, if necessary, valve  112  is opened simultaneously; as the result, the flushing fuel is fed into the tank of the second stage II. In case of failure of the transfer pump  79 , valves  107 ,  108 ,  109 ,  111  and  112  are closed and the pump is replaced. 
     The processes in hydro-generators  74 ,  75  and  76  are carried out simultaneously and are repeated not less than 2÷3 times. Temperature control in the tank of the second stage II is carried out by means of the thermocouple probe  119 . 
     Drainage of the flushing fuel from the tank of the second stage II is carried out via pipeline  120  through valve  121 . 
     After processing in hydro-generators  74 ,  75  and  76  the feedstock from second stage tank II is removed via pipeline  122  through valve  123 . The viscometer  124  is installed on the pipeline  122 ; the needs for further processing of the feedstock is determined according to that viscometer&#39;s readings. To the extent that the processing in the tank of the second stage  11  turns out to be sufficient and the viscosity value meets the stated requirements, the final product is drained via pipeline  125  through opened valves  126  and  127  through drain connection  128  with valve  129  closed. 
     To the extent that the viscosity value does not meet the stated requirements, the feedstock to be processed is directed to the hydro-generator  130  by way of the interim stage&#39;s transfer pump  131  via feeding pipeline  122  through valves  132 ,  133  and  134 . The feedstock processed in hydro-generator  130  is fed into the tank of the third stage III via offtake pipeline  135  through valve  136 . Flushing of the hydro-generator  130  and transfer pump  131  is carried out with a diesel fuel from flushing tank  137  through valves  138  and  139  via flushing pipeline  140 . Control over the pressure level is carried out using the pressure sensor  141  at the outlet of the transfer pump  131  and by means of the pressure sensor  142  at the outlet of the hydro-generator  130 . Control over the temperature level is carried out using the temperature sensor  143  at the outlet of the transfer pump  131  and by means of the temperature sensor  144  at the outlet of the hydro-generator  130 . 
     The process in the hydro-generator  130  is carried out as follows. Valves  126  and  129  on drainage pipe  125  as well as valves  138  and  139  on flushing pipeline  140  are closed. The supply of the feedstock to be processed is provided by means of the transfer pump  131  through opened valves  132 ,  133  and  134 . After it has been processed, the feedstock is carried off to the tank of the third stage  111  via offtake pipeline  135  through opened valve  136 . For flushing the hydro-generator  130  valves  132  and  134  are closed and valves  138  and  139  on flushing pipeline  140  are opened; as the result, the transfer pump  131  delivers diesel fuel over by way of the hydro-generator  130  from the flushing tank  137 . Valve  133  during the flushing process is opened. When the flushing process is over, valves  138  and  139  are closed, and valves  126  and  129  are opened; as the result, the flushing fuel is drained via pipeline  125  through valve  127  of drain connection  128 . In case of failure of the transfer pump  131 , valves  126 ,  129 ,  132 ,  133  and  134  are closed and the pump is replaced. 
     3. Third Stage 
     The feedstock to be processed is fed into the tank of the third stage Ill through valve  136  via pipeline  135 . Three hydro-generators  145 ,  146  and  147 , where the cavitation processing of the feedstock is carried out, are placed tangentially to the surface of the tank of the third stage III. 
     The feedstock to be processed is supplied to hydro-generator  145  by way of the third stage&#39;s transfer pump  148  via feeding pipeline  151  through valves  152 ,  153  and  154 . The feedstock processed in hydro-generator  145  is fed into the tank of the third stage III via offtake pipeline  155  through valves  156  and  157 . Flushing of the hydro-generator  145  and transfer pump  148  is carried out with a diesel fuel from flushing tank  158  through valves  159  and  160  via flushing pipeline  161 . Control over the pressure level is carried out using the pressure sensor  162  at the outlet of the transfer pump  148  and by means of the pressure sensor  163  at the outlet of the hydro-generator  145 . 
     The process in the hydro-generator  145  is carried out as follows. Valves  159  and  160  on flushing pipeline  161  are closed. The supply of the feedstock to be processed is provided by way of the transfer pump  148  through opened valves  152 ,  153  and  154 . After it has been processed, the feedstock is carried off to the tank of the third stage II via offtake pipeline  155  through opened valves  156  and  157 . For flushing the hydro-generator  145  valves  152  and  157  are closed and valves  159  and  160  on flushing pipeline  161  are opened; as the result, the transfer pump  148  delivers diesel fuel over by way of the hydro-generator  145  from flushing tank  158 . Valves  153 ,  154  and  156  during the flushing process are opened. When the flushing process is over, valves  159  and  160  are closed, and, if necessary, valve  157  is opened simultaneously; as the result, the flushing fuel is fed into the tank of the third stage III. In case of failure of the transfer pump  148 , valves  152 ,  153 ,  154 ,  156  and  157  are closed and the pump is replaced. 
     In the same way the feedstock to be processed is supplied to the hydro-generator  146 , which is provided by means of the third stage&#39;s transfer pump  149  via feeding pipeline  164  through valves  165 ,  166  and  167 . The feedstock processed in hydro-generator  146  is fed into the tank of the third stage III via offtake pipeline  168  through valves  169  and  170 . Flushing of the hydro-generator  146  and transfer pump  149  is carried out with a diesel fuel from flushing tank  171  through valves  172  and  173  via flushing pipeline  174 . Control over the pressure level is carried out using the pressure sensor  175  at the outlet of the transfer pump  149  and by means of the pressure sensor  176  at the outlet of the hydro-generator  146 . 
     The process in hydro-generator  146  is carried out as follows. Valves  172  and  173  on flushing pipeline  174  are closed. The supply of the feedstock to be processed is provided by way of the transfer pump  149  through opened valves  165 ,  166  and  167 . After it has been processed, the feedstock is carried off to the tank of the third stage II via offtake pipeline  168  through opened valves  169  and  170 . For flushing the hydro-generator  146  valves  165  and  170  are closed and valves  172  and  173  on flushing pipeline  174  are opened; as the result, the transfer pump  149  delivers a diesel fuel over by means of the hydro-generator  146  from the flushing tank  171 . Valves  166 ,  167  and  169  during the flushing process are opened. When the flushing process is over, valves  172  and  173  are closed, and, if necessary, valve  170  is opened simultaneously; as the result, the flushing fuel is fed into the tank of the third stage III. In case of failure of the transfer pump  149 , valves  165 ,  166 ,  167 ,  169  and  170  are closed and the pump is replaced. 
     In the same way the feedstock to be processed is supplied to the hydro-generator  147 , which is provided by means of the of the third stage&#39;s transfer pump  150  via feeding pipeline  177  through valves  178 ,  179  and  180 . The feedstock processed in the hydro-generator  147  is fed into the tank of the third stage III via the offtake pipeline  181  through valves  182  and  183 . Flushing of the hydro-generator  147  and transfer pump  150  is carried out with a diesel fuel from the flushing tank  184  through valves  185  and  186  via flushing pipeline  187 . Control over the pressure level is carried out using the pressure sensor  188  at the outlet of the transfer pump  150  and by means of the pressure sensor  189  at the outlet of the hydro-generator  147 . 
     The process in the hydro-generator  147  is carried out as follows. Valves  185  and  186  on flushing pipeline  187  are closed. The supply of the feedstock to be processed is provided by way of the transfer pump  150  through opened valves  178 ,  179  and  180 . After it has been processed, the feedstock is carried off to the tank of the third stage  111  via the offtake pipeline  181  through opened valves  182  and  183 . For flushing the hydro-generator  147  valves  178  and  183  are closed and valves  185  and  186  on flushing pipeline  187  are opened; as the result, the transfer pump  150  delivers a diesel fuel over by way of the hydro-generator  147  from flushing tank  184 . Valves  179 ,  180  and  182  during the flushing process are opened. When the flushing process is over, valves  185  and  186  are closed, and, if necessary, valve  183  is opened simultaneously; as the result, the flushing fuel is fed into the tank of the third stage III. In case of failure of the transfer pump  150 , valves  178 ,  179 ,  180 ,  182  and  183  are closed and the pump is replaced. 
     The processes in hydro-generators  145 ,  146  and  147  are carried out simultaneously and are repeated not less than 2÷3 times. Temperature control in the tank of the third stage III is carried out by means of the thermocouple probe  190 . 
     After processing in hydro-generators  145 ,  146  and  147  the feedstock from the tank of the third stage III is removed via pipeline  191  through valve  192 . The viscometer  193  is installed on the pipeline  191 ; the needs for further processing of the feedstock are determined according to that viscometer&#39;s readings. To the extent that all the carried out processing is sufficient and the viscosity value meets the stated requirements, the drainage of the final product is carried out. To the extent that the viscosity value does not meet the predetermined values, the feedstock being processed is returned to the tank of the first stage I. 
     Drainage of the flushing fuel from flushing tanks  18 ,  31  and  44  of the first stage I is carried out via drainage pipes  194 ,  195  and  196  respectively and correspondingly by ways of valves  197 ,  198  and  199 . 
     Drainage of the flushing fuel from the flushing tank  66  of the interim stage is carried out via drainage pipe  200  through valve  201 . 
     Drainage of the flushing fuel from flushing tanks  87 ,  100  and  113  of the second stage II is carried out via drainage pipes  202 ,  203  and  204  respectively and correspondingly by ways of valves  205 ,  206  and  207 . 
     Drainage of the flushing fuel from the flushing tank  137  of the interim stage is carried out via drainage pipe  208  through valve  209 . 
     Drainage of the flushing fuel from flushing tanks  158 ,  171  and  184  of the third stage III is carried out via drainage pipes  210 ,  211  and  212  respectively and correspondingly by ways of valves  213 ,  214  and  215 . 
     Control over the temperature level at the outlets of the first stage&#39;s transfer pumps  8 ,  9  and  10  is carried out using temperature sensors  216 ,  217  and  218  correspondingly. Control over the temperature level at the outlets of first stage hydro-generators  5 ,  6  and  7  is carried out using temperature sensors  219 ,  220  and  221  correspondingly. 
     In the same way control over the temperature level at the outlets of second stage transfer pumps  77 ,  78  and  79  is carried out using temperature sensors  222 ,  223  and  224  correspondingly. Control over the temperature level at the outlets of second stage&#39;s hydro-generators  74 ,  75  and  76  is carried out using temperature sensors  225 ,  226  and  227  correspondingly. 
     In the same way control over the temperature level at the outlets of third stage transfer pumps  148 ,  149  and  150  is carried out using temperature sensors  228 ,  229  and  230  correspondingly. Control over the temperature level at the outlets of third stage&#39;s hydro-generators  145 ,  146  and  147  is carried out using temperature sensors  231 ,  232  and  233  correspondingly. 
     In order to prevent getting any unprocessed feedstock to a consumer, an additional stage is provided at the third stage outlet. In this case the feedstock being processed is supplied via pipeline  234  with closed valves  235  and  236  on drainage pipe  237  to the hydro-generator  238  by means of the final stage transfer pump  239  through valves  240 ,  241  and  242 . Flushing of the hydro-generator  238  and transfer pump  239  is carried out with a diesel fuel from flushing tank  243  through valves  244  and  245  via flushing pipeline  246 . Drainage of the flushing fuel from flushing tank  243  is carried out via drainage pipe  247  through valve  248 . 
     To the extent that the processing in the facilities turns out to be sufficient and the viscosity value meets the stated requirements, the final product is drained via pipeline  237  through opened valves  235  and  250  through drain connection  249  with valve  236  closed. 
     Control over the pressure level is carried out using pressure sensor  251  at the outlet of the transfer pump  239  and by means of the pressure sensor  252  at the outlet of the hydro-generator  238 . Control over the temperature level is carried out using temperature sensor  253  at the outlet of the transfer pump  239  and by means of the temperature sensor  254  at the outlet of the hydro-generator  238 . 
     The process in hydro-generator  238  is carried out as follows. Valves  235  and  236  on drainage pipe  237  as well as valves  244  and  245  on flushing pipeline  246  are closed. The supply of the feedstock to be processed is provided by way of the transfer pump  239  through opened valves  240 ,  241  and  242 . After it has been processed, the feedstock is carried off to a consumer via offtake pipeline  255 . For flushing hydro-generator  238  valves  241  and  242  are closed and valves  244  and  245  on flushing pipeline  246  are opened; as the result, the transfer pump  239  delivers diesel fuel over by means of the hydro-generator  238  from flushing tank  243 . Valve  240  during the flushing process is opened. When the flushing process is over, valves  244  and  245  are closed, and valve  248  is opened; as the result, the flushing fuel is drained through drain connection  247 . In case of failure of the transfer pump  239 , valves  235 ,  236 ,  240 ,  241  and  242  are closed and the pump is replaced. 
     For flushing the feeding pump  2  valve  3  is closed and valves  257  and  258  on the flushing pipeline  259  are opened; as the result, the transfer pump  2  delivers a diesel fuel over from the flushing tank  256 . When the flushing process is over, valves  257  and  258  are closed, and valve  261  is opened; as the result the flushing fuel is drained through drain connection  260 . In case of failure the transfer pump  2 , valve  3  is closed and the pump is replaced. 
     Readings of viscometers  53 ,  124  and  193  allow to determine whether it is necessary to intensify the processing of the feedstock or, vice versa, to decrease its intensity, i.e. to decrease the number of passes through each hydro-generator, or to selectively shut down hydro-generators of the first, second or third stage. 
     The principal chart shown on the  FIG. 2  combines the parallel and the sequential layouts of the hydro-generators described earlier. The advantages of the said chart are as follows: 
     1. At the starting stage a hot diesel fuel is fed into the tank of the first stage I along with the feedstock proper. Because of that an initial decrease of the feedstock&#39;s viscosity takes place due to a temperature increase, thus less power is required for directing movement of a viscous feedstock and therefore the process of cavitation in hydro-generators is achieved and carried out more easily.
 
2. With a availability of selectively locating the hydro-generators there exists a possibility to regulate the intensity of the viscosity reduction process depending on the level of viscosity of the initial feedstock and on the specified viscosity of the product at the outlet: to reduce the number of the feedstock&#39;s passes through each hydro-generator or to change the number of hydro-generators themselves.
 
3. Replacement of any malfunctioned equipment will not lead to downtime of the whole processing facilities as the replacement can be carried out during the process.
 
 FIG. 3  is a flowchart, illustrating steps of one of the preferred embodiments of the method of the present invention. The following steps are illustrated:
 
     Viscous oil products are provided into the plant ( 310 ). The viscous oil products are then processed in a reaction module ( 320 ). Processing in a reaction module comprises the steps of feeding the viscous oil products into the hydrocavitation generator ( 322 ) to obtain a product, supplying the product to the fractionation device ( 324 ), and continuously and consecutively delivering and processing the feedstock in a recirculation mode ( 326 ) at one or more subsequent stages within the reaction modules. 
     The intermediary processing is carried out ( 330 ) between the stages in an intermediary reaction module. The processing in intermediary reaction stages comprises the following. Recirculated oil products are directed ( 332 ) (following a heat-mass exchange in the preceding tank) by way of a pump into the hydrocavitation generator of the interim module to obtain further reduction of the treated product viscosity. The processed product is subsequently delivered ( 334 ) to the next stage of the reaction module. 
     Kinematic viscosity of processed oil product is then measured ( 340 ) at the output of the reaction module to ascertain whether the viscosity requirement is met ( 350 ). The viscosity requirement may be met ( 352 ) or not met ( 354 ). 
     In some embodiments of the present method, the treated oil product may be redirected back to the tank of the preceding stage ( 360 ) for further treatment. 
     In circumstances, where it is determined that the level of viscosity has reached the preset value ( 352 ), the treated oil product is forwarded for final processing into a rectifying chamber ( 370 ). 
     It is to be understood that while the plant and the method of the present invention have been described and illustrated in detail, the above-described embodiments are simply illustrative of the principles of the invention and the forms that the invention can take, and not a definition of the invention. It is to be understood also that various other modifications and changes may be devised by those skilled in the art which will embody the principles of the invention and fall within the spirit and scope thereof. It is not desired to limit the invention to the exact construction and operation shown and described. The spirit and scope of this invention are limited only by the spirit and scope of the claims below.