TECHNOLOGY FOCUS - BIOLOGY - Preferred Process: In the process (P1), the recovery step includes a bioreactor for the production of biomass such as algae and/or bacteria such as cyano bacteria. The algae and/or bacteria in the recovery step are concentrated and recycled to the feed mixture.    TECHNOLOGY FOCUS - INSTRUMENTATION AND TESTING - Preferred Apparatus: The pretreatment apparatus is provided prior to the feed pump. The pretreatment apparatus comprises a device adapted to divide particles in the feedstock and to mix the feedstock and the water and the liquid organic compound to a feed mixture with the specified feed mixture properties for the process. The conversion device comprises a vertically oriented reactor having a conically shaped inlet for introducing the feed mixture in the top and a conically shaped outlet in the bottom, and where the angle of the walls of the conical inlet to the centerline of the reactor is below 60 degrees , and where the angle of the walls of the conical outlet to the centerline of the reactor is below 30 degrees . The vertically positioned cyclone shaped mixing chamber is provided for the introduction of the supercritical fluids and/or oxidizing agent is performed in, and where an inlet tangential to the mixing chamber is provided for introducing the superheated supercritical fluid and/or oxidizing agent into the chamber and a bottom outlet is provided for withdrawing the fully converted feed mixture from the cyclone shaped mixing chamber. The mixing chamber having a conically shaped inlet and a conically shaped outlet is provided for the introduction of the supercritical fluids and/or oxidizing agent, the walls of conical shaped inlet and outlet having angle to the centerline of the mixing chamber of maximum 60 degrees , and where an inlet is provided with an angle, alpha , in the flow direction of at least 20 degrees for the introduction of the superheated supercritical fluid and/or oxidizing agent into the mixing chamber, and where an outlet is provided at the bottom for withdrawing the partially or fully converted feed mixture from the mixing chamber.    TECHNOLOGY FOCUS - ORGANIC CHEMISTRY - Preferred Process: The process (P1) is related to palm oil production from fresh fruit bunches and involves: a) a sterilization step; b) a stripping step; c) a digestion step; d) a pressing step; e) a clarification and purification step of the liquor; f) a nut and fiber separation step for separating the fibers and nuts from the pressing cake; g) a nut drying, cracking and separation step producing palm kernels and palm shells; h) feeding the waste product in the form of fiber, oil palm fronds, oil palm trunks, shells, empty fruit bunches, POME and/or decanter cakes into a continuous process for converting carbonaceous material in the waste product into a liquid hydrocarbon product; and i) extracting a liquid hydrocarbon product. The process (P1) is related to olive oil production from olives and involves: a first step of washing the olives; a step of milling the olives; a step of centrifugation separating the milled olives into an olive oil fraction and a Pomace fraction and/or a vegetable water fraction; feeding the waste product in the form of Pommac into a continous process for converting carbonaceous material in the waste product in the form of Pomace and/or vegetable water into a liquid hydrocarbon product; and extracting a liquid hydrocarbon product. The process (P1) is related to sugar production from sugar cane and involves: a milling step; a first clarification step; an evaporation step; a second clarification step; a vacuum pan step; a crystallization step; a centrifugation step; a washing step; a drying step, where a sugar product is produced and a bagasse product, a filtercake product, a molasses product and a water effluent and where at least part of one of the streams of bagasse product and/or filtercake product and/or molasses product and/or water effluent and/or sugarcane agricultural residues (SCAR) is fed into a continuous conversion process, and at least one liquid hydrocarbon product is extracted. The process (P1) involves: feeding at least part of the extracted liquid hydrocarbon product into the processing step for the prepared food base product, as a fuel for power generation and/or heating purposes. The continuous process for converting carbonaceous material contained in the waste material into a liquid hydrocarbon product, waste material including the carbonaceous material being in a feed mixture including at least one fluid, where the fluid includes water and further liquid organic compounds at least partly produced by the process in a concentration of at least 1 wt.%, involves: converting at least part of the carbonaceous material by: pressurizing the feed mixture to a pressure of 50-400 bar; heating the feed mixture to a temperature of 250-500 degrees C; maintaining the pressurized and heated feed mixture in the desired pressure and temperature ranges in a reaction zone for a predefined time; cooling the feed mixture to a temperature of 25-200 degrees C; expanding the feed mixture to a pressure of 1-70 bar, thereby causing the carbonaceous material to be converted to a liquid hydrocarbon product; and separating a fraction comprising liquid hydrocarbon product. The pressure during the conversion step is 275-350 bar, preferably 290-330 bar, more preferably 300-325 bar. The temperature during the conversion step is 380-430 (preferably 385-430, more preferably 390-430, especially 400-430) wt.%. The feed mixture at entry temperature is pressurized essentially to the desired process pressure before heating to process temperature is initiated. The pH during the conversion is greater than or equal to 7, preferably 8-12, and more preferably 8-11, where the pH of the feed mixture is measured during and/or after the conversion and when the pH measurement is outside the preferred range, the composition of the feed mixture is altered to correct the pH in the conversion. The heating of the feed mixture is taking place at a rate of at least 50 (preferably 75, more preferably 100, especially 150) degrees C/minute in the temperature of 140-300 degrees C. The residence time in the reactor is 10-40 (preferably 10-30, especially 10-25) minutes. The average flow velocity in pipes in the process and/or at the entry of the conversion zone/reactor, is at least 0.2 (preferably 0.2-5, especially 0.5-3) meter/second. The process further involves recovery of substances from the residual fraction remaining after separation of the fraction comprising a liquid hydrocarbon product, and where the recovery is performed in at least one evaporator and condenser, and where the first of the evaporator is adapted to perform a vapor recompression technique, including mechanical vapor recompression and/or thermal recompression. The evaporators are heated by steam and the steam is at least partly produced by the process, where at least the first evaporator comprises at least two condensers operating decreasing condensation temperatures. The condensation temperature of first condenser is 85-110 (preferably 90-105) degrees C and where the temperature of the last condenser is preselected so as to condense compounds having a boiling point lower than water, such as a condensation temperature of 20-80 (preferably 30-70, especially 40-60) degrees C. The recovered substances are at least partly recirculated in a concentrated form and introduced into the feed mixture. The concentration factor, as defined as the mass ratio of the residual fraction fed to the recovery step to the mass of concentrate, is at least 4, preferably at least 5, more preferably at least 7. The treated waste water from the bioreactor is used as process water in the initial process for organic food production. The heating for the conversion is at least partly performed by introducing at least one supercritical fluid, such as a superheated supercritical fluid, into the feed mixture. The heating performed for the conversion is at least partly performed by introducing an oxidizing agent into the feed mixture. The introduction of the supercritical fluids and/or oxidizing agent is performed in a vertically positioned cyclone shaped mixing chamber, and where the feed mixture is introduced in the center from top with a ratio of the average linear velocity in the inlet pipe to the minimum average linear velocity of the mixed fluids in the mixing chamber of at least 2, and where the superheated supercritical fluid and/or oxidizing agent is introduced into the chamber tangentially to the mixing chamber at a velocity ratio of at least 4, and where the partially or fully converted feed mixture is withdrawn from the cyclone shaped mixing chamber from the bottom. The introduction of the supercritical fluid and/or oxidizing agent is performed in a mixing chamber having a conically shaped inlet and a conically shaped outlet, the walls of conical shaped inlet and outlet having angle to the centerline of the mixing chamber of maximum 60 degrees , and where the feed mixture is introduced from the top with a ratio of the average linear velocity in the inlet pipe to the minimum average linear velocity of the mixed fluids in the mixing chamber of at least 2, and where the superheated supercritical fluid and/or oxidizing agent is introduced into the mixing chamber with an angle, alpha , in the flow direction of at least 20 degrees , and where the average linear velocity ratio of the superheated supercritical fluid and/or oxidizing agent is at least 4, and where the partially or fully converted feed mixture is withdrawn from the mixing chamber from the bottom. The process involves upgrading, where the liquid hydrocarbon product from the separation is heated to a temperature of 350-600 degrees C, at a pressure of 0.5-30 bar, thereby producing at least one liquid hydrocarbon fraction and/or at least one solid residue fraction and/or at least one gas fraction and/or at least one aqueous fraction. The at least part of the aqueous fraction is recycled to the recovery step and mixed with the residual fraction from the separation. The upgrading by heating is performed in at least 2 steps. The temperature in the first heating step of heating is maintained less than or equal to 200 (preferably less than or equal to 180, more preferably less than or equal to 160, especially 140, particularly 100-140) degrees C. The heat for the first evaporation step is recovered from the cooling and expanding the converted feed mixture. The residual fraction comprising liquid hydrocarbons and/or solids is withdrawn from the first heating step and fed to a second heating step, where it is heated to a temperature of up to 600 (preferably 400-550, preferably 425-500) degrees C. The pressure is maintained in 2.5-10 bar. At least a fraction of the heated residual fraction comprising liquid hydrocarbons is fed to a fractionator. The evaporated fraction is condensed and fractionated in at least two condensing steps having predefined and decreasing condensation temperatures. The outlet temperature of the non-condensed liquid hydrocarbons in the first condensation step is 340-400 (preferably 350-390, more preferably 360-380) degrees C. The outlet temperature from the second condensation step is 120-300 (preferably 150-250), where a fraction not being condensed in the condensing steps comprises a combustible gas and where the gas is combusted to produce heat for heating in the process. The cooling medium is used in the condensation, and the heat transferred to the cooling medium is used for at least partly supplying the heat required in the conversion. The second heating step involves at least two vessels or drums operating in a sequential cycle, and where the solid residue is allowed to accumulate within the vessels or drums for a predefined period. Preferred Components: The concentration of at least one liquid organic compound contained in the feed mixture is at least 5 wt.%, preferably at least 10 wt.%, especially at least 20 wt.%. The feed mixture contains at least one homogeneous catalyst in the form of a compound of potassium and/or sodium so as to ensure a total concentration of potassium and sodium of at least 0.5 wt.%, preferably 1-10 wt.%, more preferably 2-5 wt.%. The ratio of weight of the liquid organic compounds to the dry weight of carbonaceous material in the feed mixture is 0.1-2, preferably 0.15-1, especially 0.2-0.5. The substances being recovered comprise water soluble organics and/or homogeneous catalyst in the form of potassium and/or sodium. In the process (P2), the feedstock material added has a maximum particle size of 15 (preferably 5, more preferably 1, especially 0.5) mm. The process (P2) further involves: a division of the particles in the feedstock, to obtain the desired maximum particle size. The liquid organic compound is added in an amount of at least 5 (preferably at least 10, especially at least 20) wt.%. The homogeneous catalyst is added in the form of a compound of potassium and/or sodium so as to ensure a total concentration of potassium and/or sodium of at least 0.5 (preferably 1-10, especially 2-5) wt.%. The first step of pre-treating further involves: chemical pulping; and heating of the feed mixture to a temperature of 50-200 (preferably 90-160) degrees C, at a pressure of 1-20 (preferably 4-20) bar to avoid boiling. The pretreatment has duration of 5 minutes to 24 hours, preferably 10 minutes to 12 hours, more preferably 15 minutes to 6 hours, especially 20 minutes to 3 hours. The dry solid content of the carbonaceous material is at least 20 wt.% such at least 25 wt.%, preferably the dry solid content of the carbonaceous material is at least 30 wt.% such as at least 40 wt.%. The dry solid content of the carbonaceous material is 20-70 (preferably 30-60) wt.%. Preferred Feed Mixture: The feed mixture contains at least one homogeneous catalyst in the form of a compound of potassium and/or sodium so as to ensure a total concentration of potassium and sodium of at least 0.5 (preferably 1-10, more preferably 2-5) wt.%. The ratio of weight of the liquid organic compounds to the dry weight of carbonaceous material in the feed mixture is 0.1-2. The feed mixture comprises a dry solid content of carbonaceous material of 20-70 (preferably 30-60) wt.%. The feed mixture comprises particles with a maximum diameter of 30 (preferably 15, more preferably 5, especially 1, particularly 0.5) mm. EXAMPLE - No suitable example given.