TECHNOLOGY FOCUS - INSTRUMENTATION AND TESTING - Preferred Components: The first nozzle reactor comprises: a reactor body having an interior reactor chamber with an injection end and an ejection end; an injection passage mounted in the nozzle reactor in material injecting communication with the injection end of the interior reactor chamber, where the injection passage has (a) an enlarged volume injection section, enlarged volume ejection section and a reduced volume mid-section intermediate between the enlarged volume injection section and enlarged volume ejection section, (b) a material injection end and (c) a material ejection end in injecting communication with the interior reactor chamber; and a material feed passage penetrating the reactor body and being adjacent to the material ejection end of the injection passage and transverse to an injection passage axis extending from the material injection end to the material ejection end in the injection passage.    TECHNOLOGY FOCUS - ORGANIC CHEMISTRY - Preferred Method: The method (I) or (II) further comprises: separating the first solvent component or the secondary first solvent component, respectively from the first solvent-wet tailings by adding a second solvent to the first solvent-wet tailings, thus producing second solvent-wet tailings, where the second solvent-wet tailings comprise a second solvent component; separating the second solvent component from the second solvent-wet tailings; cracking the non-participating hydrocarbon stream inside a second nozzle reactor; and upgrading bitumen component of the bitumen-enriched solvent phase. The method (I) further comprises: separating the bitumen-enriched solvent phase into bitumen component and a first solvent phase before cracking the bitumen component inside a first nozzle reactor, where separating the bitumen-enriched solvent phase into bitumen component and the first solvent phase comprises heating the bitumen-enriched solvent phase to a temperature above the boiling point temperature of the first solvent. In the method (I) or (II) separating the bitumen-enriched solvent phase from the first mixture comprises: a first stage of separating a first quantity of the bitumen-enriched solvent phase or the first bitumen-enriched solvent phase from the first mixture by filtering, settling or draining the bitumen-enriched solvent phase from the first mixture; and a second stage of separating a second quantity of the bitumen-enriched solvent phase or the first bitumen-enriched solvent phase, respectively from the first mixture by adding a second quantity of first solvent to the first mixture. In the method (I) or (II): the second stage of separating a second quantity of the bitumen-enriched solvent phase from the first mixture comprises washing the first mixture with the second quantity of first solvent in a countercurrent process; separating the first solvent component from the first solvent-wet tailings comprises washing the first solvent-wet tailings with the second solvent in a countercurrent process; separating the second solvent from the second solvent-wet tailings comprises flashing the second solvent component from the second solvent-wet tailings; separating the bitumen-enriched solvent phase from the first mixture comprises filtering the first mixture in a plate and frame-type filter press; separating the first solvent component from the first solvent-wet tailings comprises adding the second solvent to the first solvent-wet tailings loaded in a plate and frame-type filter press; filtering the first mixture in a plate and frame-type filter press further comprises adding a gas over the first mixture loaded in the plate and frame-type filter press; and gas is added over the first solvent-wet tailings loaded in the plate and frame-type filter press. In the method (I) or (II) cracking bitumen component or asphaltene stream, respectively inside the first nozzle reactor comprises: injecting a stream of cracking material through an injection passage into an interior reactor chamber; and injecting the bitumen component or asphaltene stream, respectively into the interior reactor chamber adjacent to the injection passage and transverse to the stream of cracking material entering the interior reactor chamber from the injection passage. In the method (II) separating the first solvent from the bitumen-enriched solvent phase comprises heating the bitumen-enriched solvent phase to a temperature above the boiling point temperature of the first solvent. In the method (IV) separating the bitumen-enriched solvent phase from the first result of mixing the first solvent with the first quantity of material comprising bitumen comprises: filtering, settling or draining a first quantity of bitumen-enriched solvent phase from the first result of mixing the first solvent with the first quantity of material comprising bitumen; and displacing a second quantity of bitumen-enriched solvent phase from the first result of mixing the first solvent with the first quantity of material comprising bitumen. Preferred Components: The material comprising bitumen is tar sands. The first solvent comprises light aromatic solvent comprising kerosene, diesel, gas oil, naphtha, benzene, toluene, aromatic alcohol and/or their derivatives. The second solvent comprises a volatile hydrocarbon solvent comprising a cyclo- or iso-paraffin having 3-9C and/or their derivatives. The second solvent is liquefied petroleum gas. The light hydrocarbon liquid distillate comprises hydrocarbon having a molecular weight less than 300 Dalton's. In the method (IV), the portion of the second result comprises light hydrocarbon distillate. In the method (V), the portion of the fourth result comprises light hydrocarbon distillate. EXAMPLE - Bitumen was extracted from a Trinidad tar sand project. Sample was initially weighed and placed into a mixing container along with first solvent i.e. biodiesel in the ratio of 14:1. The first solvent and the tar sands were mixed with a standard three blade impeller. The tar sands were leached for one hour in the mixing container and filtered. The filtrate of liquids formed a bitumen-enriched solvent phase and the filter cake of solids formed first solvent-wet tailings. The first solvent-wet filtrate was weighed and measured. The first solvent-wet filter cake was subjected to addition of a second solvent. The second solvent was added by placing the first solvent-wet filter cake into a pipe extractor and introducing liquid petroleum gas (LPG) into the pipe extractor. The first solvent-wet filter cake was soaked in the liquid LPG for fifteen minutes. The liquids and solids in the mixture were separated into a first solvent-second solvent mixture and second-solvent wet tailings, respectively. The first solvent-second solvent mixture included liquid LPG, bitumen and first solvent. The LPG was removed from the bitumen and first solvent by allowing it to vaporize within the system. The bitumen and the first solvent were then captured in a flask. The weight and amount of the liquids were measured. The second solvent-wet tailings removed from the pipe extractor were analyzed to determine the amount of bitumen in the second solvent-wet tailings. The bitumen-enriched solvent phase was injected into the nozzle reactor via the material feed port of the nozzle reactor. Steam at a pressure of 20 bars was also injected into the nozzle reactor. Steam and bitumen-enriched solvent phase were injected into the nozzle reactor at a steam:bitumen-enriched solvent phase at a ratio of 2:1. The pressure inside of the nozzle reactor at injection was 1.5 bars and the injected bitumen-enriched solvent phase remained in the nozzle reactor for 1 second. A liquid product exiting the nozzle reactor was collected and analyzed. The product was separated into a non-participating hydrocarbon stream and a participating hydrocarbon stream. The participating hydrocarbon stream had an American Petroleum Institute gravity of 28-35. The participating hydrocarbon stream contained a mixture of cracked hydrocarbons including highly aromatic compounds i.e. toluene, xylene, some benzene and other ring compounds. The molecular weight of the compounds in the participating hydrocarbon stream was generally less than 300 Daltons.