503results about "Extractive distillation" patented technology

The invention discloses a continuous synthesis and purification method of hexafluoropropylene oxide, which comprises the following steps: introducing hexafluoropropylene, oxygen and a fluorine-containing solvent into a supergravity reactor to carry out oxidation reaction at the reaction temperature of 100-200 DEG C under the reaction pressure of 1.0-2.5 Mpa for 10-120 seconds, and after the reaction is finished, overflowing and leading out reaction liquid to obtain the hexafluoropropylene oxide. And purifying to obtain the hexafluoropropylene oxide. According to the method, the problems of mass transfer and heat transfer can be effectively solved by using the supergravity reactor, the reaction selectivity is remarkably improved, meanwhile, the productivity is effectively improved, and the supergravity reactor is combined with extractive distillation treatment, so that the conversion rate of the hexafluoropropylene reaches 79% or above, the selectivity of the hexafluoropropylene oxide is 85% or above, and the purity of the hexafluoropropylene oxide after extractive distillation reaches 99%. The invention further discloses a device used in the continuous synthesis and purification method, and cyclic utilization of hexafluoropropylene and the fluorine-containing solvent can be achieved.

The invention discloses a crude phenol continuous refining device and method, the device comprises a crude phenol storage tank, a dehydrating tower, a primary tower, a phenol fraction tower, an o-cresol fraction tower, a m-cresol and p-cresol tower, an extractive distillation tower and a p-cresol fraction tower which are connected in sequence, and the top of each tower is independently connected with a cooler; the method specifically comprises the following steps: (1) discharging phenol water; (2) discharging a heavy fraction; (3) discharging phenol; (4) discharging o-cresol; (5) discharging residual oil at the bottom of the tower; (6) carrying out extractive distillation, and discharging m-cresol; and (7) discharging p-cresol, and recycling the extraction agent. Compared with a traditional continuous rectification process, the method has the advantages that all components are separated by adopting vacuum rectification, the separation degree of the obtained product is higher, the number of theoretical plates and energy consumption are lower, high-purity phenol products are produced with low energy consumption, low cost and high efficiency, and economic benefits and environmental benefits are greatly improved.

The invention relates to the technical field of chemical waste liquid rectification separation, in particular to a solvent rectification device for chemical waste liquid treatment, which comprises a frame, two mounting boxes, a tower body and the like, the frame is connected with the two mounting boxes, the tower body is mounted on the two mounting boxes, and the mounting boxes are communicated with the tower body. Chemical waste liquid can be injected into the tower body through the waste liquid pipe, a high-boiling-point solvent can be injected into the tower body through the solvent pipe, the original azeotropic condition is broken, and the relative volatility among components is changed, so that rectification separation is realized, the filler can be conveyed upwards through the spiral conveyor, the filler is conveyed into the tower body for loading, and the production efficiency is improved. The sliding plate can be driven by the lead screw motor to move rightwards, so that the discharge hole corresponds to the tower body, old filler falls onto the material guide plate through the discharge hole and rolls leftwards to be discharged, the filler is automatically cleaned and replaced, manpower and material resources can be saved, and the safety can be improved.

The invention provides a method and a device for separating azeotrope of ethanol and dimethyl carbonate, and the method comprises the following steps: adding raw materials into an extractive distillation tower for extractive distillation, and then carrying out first heat exchange and condensation on a compressed top gas phase of the extractive distillation tower and a bottom liquid phase of the extractive distillation tower to obtain a dimethyl carbonate product; sequentially carrying out first reboiling, first flash evaporation, two times of heat exchange, second reboiling and second flash evaporation on the heat-exchanged bottom liquid phase of the extractive distillation tower to obtain a second flash evaporation gas phase and a second flash evaporation liquid phase; carrying out second heat exchange on the second flash liquid phase and the first flash liquid phase, condensing, and returning to the extractive distillation tower; and pressurizing the second flash evaporation liquid phase, performing third heat exchange with the first flash evaporation liquid phase after primary heat exchange, and condensing to obtain an ethanol product. The method is low in energy consumption, the solvent is not easy to volatilize, and the ethanol and the dimethyl carbonate in the azeotrope can be effectively separated.

The invention provides a fused salt extractive distillation separation method of zirconium-hafnium tetrachloride, which is particularly suitable for a fused salt extractive distillation separation device. When the fused salt extractive distillation separation is carried out, main components such as a distillation tower, a sublimator, a reflux tank, a condenser, a reboiler and a circulating tank are connected, then a zirconium and hafnium chloride raw material to be separated and chloride salt for distillation are filled, and finally the device is started to realize the separation of zirconium and hafnium chlorides under the distillation condition. The separation device and method have good usability and process adaptability, the prepared zirconium tetrachloride and hafnium tetrachloride meet the use requirements in the fields of atomic energy, aerospace, high-power laser, integrated circuits and the like, and reference and guidance are provided for research, development and application of zirconium and hafnium tetrachloride molten salt rectification separation technology and equipment.

The invention provides a continuous rectification recovery process of 1, 2-butadiene, which comprises the following steps: preheating a heavy C4 raw material and an extraction agent, feeding the preheated heavy C4 raw material and extraction agent into an extractive distillation tower, steaming out a light component A from the tower top, condensing, and returning to the tower top as reflux; the heavy component A is rectified in an extractant separation tower, a light component B is distilled out from the tower top, part of the light component B returns to serve as reflux, and the other part of the light component B enters a heavy component removal tower; the heavy component B returns to the extractive distillation tower through the heat exchanger. After heavy components of the light component B are removed in the heavy component removal tower, the light component C is evaporated out from the tower top, condensed and fed into a 1, 2-butadiene storage tank. And the heavy component C finally flows into a waste liquid tank. Wherein the heavy C4 raw material and the extraction agent are preheated by a heat exchanger, and the heat exchanger uses the heavy component B as a heat source. By providing a simple, feasible, economical and efficient continuous extractive distillation process, high-purity 1, 2-butadiene can be efficiently recovered from heavy C4 byproducts of a 1, 3-butadiene extraction device, and the content of the 1, 2-butadiene can reach 97%.

The invention belongs to the technical field of octafluoropropane purification, particularly relates to a device and a method for purifying octafluoropropane, and provides the following scheme aiming at the problems that gas flows to easily generate bubbles and the bubbles wrap impurities in the processes of octafluoropropane rectification and the like: the device comprises a rectifying tower, the bottom of the rectifying tower is fixedly connected with an extraction liquid box, and a round hole is formed in the outer side of the rectifying tower; a purification outlet is fixedly connected to the interior of the round hole, a spraying head is arranged in the rectifying tower, and an input pipe is fixedly connected to the top end of the spraying head. According to the device and method for purifying the octafluoropropane, the bubble breaking piece accurately breaks bubbles, impurities and the octafluoropropane are thoroughly separated, the spoiler strengthens the separation effect, the impurities are evenly enriched, the liftable suction outlet is matched, the impurities are accurately sucked away, impurity residues in a finished product are greatly reduced, and the product quality is improved. And the purity of the perfluoropropane is assisted to stably reach a high standard.

The invention relates to a venturi separator, which is characterized in that the venturi separator comprises a venturi tube and a liquid phase collecting tube surrounding at least one part of structure of the venturi tube, and the venturi tube comprises the following sections which are communicated in sequence: an optional equal-diameter section, a reducing section, a throat part and an expanding section, the venturi separator is provided with a gas phase inlet, a liquid phase inlet, a liquid phase outlet and a gas phase outlet, an opening is formed in the side wall or the tail end of the expanding section of the venturi tube, and the opening leads to the liquid phase collecting tube, so that a liquid phase leaves the venturi tube and enters the liquid phase collecting tube under the action of centrifugal force. The invention also relates to the use of such a Venturi separator in a chemical process.

Methods and systems for recuperating power from a pressurized fluid stream of a carbon capture system are disclosed. A compressor pressurizes the carbon dioxide containing feed fluid and passes this fluid stream through a carbon capture process. The pressurized stream is expanded across a turbine where power is recovered.

The utility model provides a six-tower thermal coupling refining device for crude methanol, which comprises a pre-rectifying tower, a normal-pressure rectifying tower, a negative-pressure rectifying tower, a medium-pressure rectifying tower, a pressurized rectifying tower I and a pressurized rectifying tower II, the tower top of the pre-rectifying tower is connected with a normal-pressure tower reboiler I, and the tower top of the normal-pressure rectifying tower is connected with a negative-pressure tower reboiler; the top of the medium-pressure rectifying tower is connected with a pre-tower reboiler, the top of the pressurized rectifying tower I is respectively connected with a medium-pressure tower reboiler and a pressurized tower II reboiler, and the top of the pressurized rectifying tower II is connected with an atmospheric tower reboiler II; in the application, methanol steam at the top of a pressurized rectifying tower I provides heat for a medium-pressure rectifying tower and a pressurized rectifying tower II; methanol steam at the top of the medium-pressure rectifying tower provides heat for the pre-rectifying tower; top steam of the pre-rectifying tower and top methanol steam of the pressurized rectifying tower II provide heat for the normal-pressure rectifying tower; the tower top steam of the normal-pressure rectifying tower provides heat for the negative-pressure rectifying tower; the steam at each tower top is utilized, and the unit consumption of the methanol rectification process is 0.36-0.50 t steam / t refined alcohol.

The invention relates to an acetylene purification system and method, in particular to a method for removing impurities in acetylene to an electronic-grade acetylene level through a membrane separation technology coupled rectification process, and belongs to the field of gas separation. Aiming at the characteristics of an industrial grade acetylene material, the invention provides a technology for preparing electronic grade acetylene based on membrane separation coupling rectification, the membrane separation technology and the rectification technology are organically coupled, and a safe solvent is introduced into a rectification tower, so that the thermal stability of liquid acetylene is effectively improved, and the explosion risk is remarkably reduced. According to the technology, efficient preparation of the electronic-grade acetylene (the purity is greater than or equal to 99.9999%) is realized, and the method has a good industrial application prospect and popularization value.

The disclosure relates to a process for separating a hydrocarbon-containing feedstock stream by extractive distillation, wherein the feedstock stream is contacted with a water-soluble solvent for aromatics in countercurrent. An aliphatics fraction is distillatively removed as aliphatics product stream from the mixture obtained. The aromatics are stripped from the aromatics-enriched solvent that remains and the aromatics-depleted solvent is recycled in a solvent circuit, with compounds having a lower boiling point compared to the solvent accumulating in the solvent circuit as impurities. At least a substream of the solvent circuit is purified for removal of the impurities, wherein the substream for the purifying is subjected to a thermal separation process, in which the impurities are at least partly discharged in a top product and the purified solvent that remains is recycled into the solvent circuit. An apparatus for carrying out the process is also disclosed.

The present application provides a molten salt extraction and distillation separation device for zirconium and hafnium tetrachloride, comprising a distillation tower, a reboiler, a reflux tank, a circulation tank, a sublimator, a gas preheater, and a condenser. During installation, the various components are connected in sequence to obtain a complete molten salt extraction and distillation separation device for zirconium and hafnium tetrachloride. The device has a simple structure, is easy to operate, and is convenient to connect, and is suitable for the molten salt extraction and distillation separation of zirconium and hafnium tetrachloride.

The utility model provides an aromatic hydrocarbon extraction device. The aromatic hydrocarbon extraction device comprises a de-heavy tower, an extraction tower, a recovery tower, a first rectifying tower and a second rectifying tower which are connected in sequence, a tower top steam outlet of the de-heavy tower is connected with a heat source inlet of an extraction tower reboiler, and a heat source outlet of the extraction tower reboiler is connected with a feed port of the extraction tower through a de-heavy tower return tank. A discharge port of the extraction tower is connected with a feed port of the recovery tower, a tower top steam outlet of the recovery tower is connected with a feed port of the first rectifying tower through a recovery tower return tank, and a discharge port of the first rectifying tower is connected with a feed port of the second rectifying tower. The aromatic hydrocarbon extraction device disclosed by the utility model has the characteristics of high aromatic hydrocarbon extraction rate, high purity, energy conservation and high efficiency.

This application provides a five-tower thermally coupled refining apparatus for crude methanol, comprising a pre-distillation tower, an atmospheric distillation tower, a medium-pressure distillation tower, a pressure distillation tower I, and a pressure distillation tower II connected in sequence. The top of the pre-distillation tower is connected to the reboiler of the atmospheric distillation tower I, the top of the medium-pressure distillation tower is connected to the reboiler of the pre-distillation tower, the top of the pressure distillation tower I is connected to the reboilers of the medium-pressure distillation tower and the reboiler of the pressure distillation tower II, and the top of the pressure distillation tower II is connected to the reboiler of the atmospheric distillation tower II through a top outlet pipeline of the pressure distillation tower II. In this application, the top steam of the pressurized distillation column one provides heat to the medium-pressure distillation column and the pressurized distillation column two. The top steam of the medium-pressure distillation column provides heat to the pre-distillation column. The top steam of the pre-distillation column and the pressurized distillation column two provide heat to the atmospheric distillation column, thus making full use of the heat at the top of each distillation column. Through this application, the unit consumption of the methanol distillation process can be reduced from 1.2t steam / t refined methanol to 0.50-0.60t steam / t refined methanol, achieving a significant reduction in energy consumption.

According to the fructus viticis extract tool, an upper rail is arranged in the horizontal direction, a lower rail inclines upwards by 5-35 degrees, the upper rail and the lower rail are arranged in a matched mode in the vertical direction, the upper rail and the lower rail are each in a disc shape, a groove is formed in the inner side of each disc, each groove is in a circular ring shape, each circular ring is in an oval shape, and a telescopic rod slides on the inner side of each groove. The telescopic rods are I-shaped and located at the two ends of the butt joint cylinder, the telescopic rods are in sliding connection with the butt joint cylinder in the vertical direction, and the telescopic rods rotate and move at the two ends of the butt joint cylinder, so that when the telescopic rods slide between the upper rail and the lower rail, the telescopic rods stretch out and draw back in the vertical direction relative to the butt joint cylinder, and at the moment, the distance between the blades on the outer sides of the telescopic rods is shortened; the distance between the blades in the vertical direction is shortened, and the blades can extrude and distill the fructus viticis and purified water in the distillation tank in the vertical direction, so that the blades can extrude the fructus viticis in the vertical direction while moving and stirring in the horizontal direction, and quick distillation and extraction of the fructus viticis are assisted.

Inhibitor compositions for abating undesirable emulsion polymerization during processing of hydrocarbon stream laden with reactive vinylic monomers are provided. The polymerization inhibitor compositions include at least a first inhibitor compound having a stable nitroxide radical and a second inhibitor including phenylenediamine. Methods of inhibiting the polymerization of monomers using the compositions of the disclosure are also provided. The methods of inhibiting polymerization of monomers include a step of adding a composition of the disclosure to a process stream. The process stream includes an ethylenically unsaturated monomer that is suspended in the bulk-phase and highly polar solvents as distractive distillation solvents.

The utility model discloses a separation device for ethyl acetate and cyclohexane, which belongs to the technical field of separation and purification, solves the problems of incapability of large-scale separation, high process difficulty and poor separation effect in the prior art, and comprises an extractive distillation tower, the upper part is provided with a polyol solvent inlet, the top is connected with a first condenser, the outlet of the first condenser is connected with a cyclohexane outlet on the other side of the upper part of the extractive distillation tower, and the cyclohexane outlet is connected with a re-separation device. According to the device disclosed by the utility model, the problem of azeotropy of ethyl acetate and cyclohexane is solved by adding polar polyol, the relative volatility of the ethyl acetate and the cyclohexane is changed, and large-scale efficient separation of a mixture of the ethyl acetate and the cyclohexane is realized; the dissolubility of cyclohexane, sodium acetate and ethanol in water is different, so that the separation effect of cyclohexane is further improved, and the whole device is simple in structure.

The utility model relates to the technical field of extraction devices, and discloses a zirconium and hafnium fractional extraction device which comprises a separation box, a fractionation cavity is formed in the upper portion of the interior of the separation box, a first rotating shaft is arranged in the fractionation cavity, a plurality of sets of first stirring blades are fixedly arranged on the first rotating shaft, and a cleaning plate is fixedly installed at the bottom of the first rotating shaft. The cleaning plate is attached to the sealing plate, the sealing plate is arranged in the middle of the interior of the separation box, the cleaning plate is arranged, the cleaning plate is attached to the sealing plate, liquid materials remaining on the sealing plate can be pushed into the circulating groove in the sealing plate when the cleaning plate rotates, the circulating groove is in a long strip shape, and therefore the liquid materials can be separated from the circulating groove. According to the cleaning plate, liquid materials can flow into the mixing cavity at the bottom of the circulating groove more quickly and intensively, meanwhile, in the rotating process of the cleaning plate, the strip shape is well matched with the rotating path, the liquid materials can be continuously and effectively collected, and omission is reduced.

The invention provides a coarse methanol five-tower thermal coupling refining process and a refining device.The device comprises a pre-rectifying tower, a normal-pressure rectifying tower, a medium-pressure rectifying tower, a first pressurized rectifying tower and a second pressurized rectifying tower which are sequentially connected, the top of the pre-rectifying tower is connected with a first normal-pressure tower reboiler, and the top of the medium-pressure rectifying tower is connected with a pre-tower reboiler; the top of the pressurized rectifying tower I is connected with a medium-pressure tower reboiler and a pressurized tower II reboiler; the top of the pressurized rectifying tower II is connected with an atmospheric tower reboiler II through a top extraction pipeline of the pressurized tower II; tower top steam of the first pressurized rectifying tower provides heat for the medium-pressure rectifying tower and the second pressurized rectifying tower, tower top steam of the medium-pressure rectifying tower provides heat for the pre-rectifying tower, tower top steam of the pre-rectifying tower and the second pressurized rectifying tower provides heat for the normal-pressure rectifying tower, and heat of the tower tops of all the rectifying towers is fully utilized; through the application, the unit consumption of the methanol rectification process can be reduced from 1.2 t steam / t refined alcohol to 0.50-0.60 t steam / t refined alcohol, so that the energy consumption is greatly reduced.

The present invention relates to the technical field of rectification separation of chemical waste liquid, and particularly relates to a solvent rectification device for treating chemical waste liquid, including a frame, an installation box, a tower body, etc. Two installation boxes are connected to the frame, and the tower body is jointly installed on the two installation boxes, and the installation box and the tower body are communicated. In the present invention, chemical waste liquid can be injected into the tower body through a waste liquid pipe, and a high-boiling solvent can be injected into the tower body through a solvent pipe, breaking the original azeotropic condition and changing the relative volatility between components, so as to achieve rectification separation. The packing can be conveyed upward through a screw conveyor and conveyed into the tower body for loading. The slide plate can be driven to move to the right by a lead screw motor, so that the discharge hole corresponds to the tower body. The old packing falls onto the guide plate through the discharge hole and rolls leftward for discharge, automatically cleaning and replacing the packing, which can save human and material resources and improve safety.

The invention relates to the technical field of extractive distillation, in particular to a plant essence extractive distillation method, device and system, and the method comprises the following steps: acquiring temperature data, pressure data and flow data; acquiring average temperature data at each moment, respectively recording the average temperature data, the pressure data and the flow data as related data, and acquiring oscillation degree values of various related data in the monitoring time period; respectively acquiring a first influence coefficient and a second influence coefficient of the monitoring time period; acquiring a coupling disturbance index in the current monitoring time period; acquiring an unbalance coefficient of temperature distribution in the current monitoring time period according to the temperature data at each moment; and the rectification abnormal coefficient of the current monitoring time period is obtained by combining the coupling disturbance index in the current monitoring time period, so that the prediction range parameter in the model prediction control technology in the next monitoring time period is obtained, and the reflux quantity of the next monitoring time period is adjusted. According to the method, the extractive distillation purity of the plant extract is improved by optimizing the prediction range parameters.

The utility model discloses ammonia nitrogen removal equipment for anaerobic fermentation biogas slurry, and belongs to the field of ammonia nitrogen removal and recycling of anaerobic fermentation biogas slurry. All deaminated biogas slurry flows back to the anaerobic fermentation system by virtue of a steam stripping flash evaporation deamination technology, an ammonia absorption technology, an evaporative crystallization technology, a mud-mud heat exchange technology and the like. An adopted flash evaporation deamination tower (3) is internally divided into a plurality of areas, ammonia-containing biogas slurry sequentially flows through the areas and is in countercurrent contact with circulating steam and fresh steam in the areas, ammonia nitrogen in the biogas slurry is removed through steam stripping and flash evaporation, and the generated deaminated biogas slurry completely flows back to an anaerobic fermentation system; ammonia in the ammonia-containing steam is absorbed by dilute sulfuric acid in an ammonia gas absorption tower (9), an ammonium sulfate solution is generated and sent to an evaporative crystallization tank (16), indirect heating and circulating evaporative crystallization are adopted, and solid ammonium sulfate is transported outwards; the mud-mud heat exchanger (2) is suitable for heat exchange between non-Newtonian fluid materials. Biogas slurry is no longer discharged, and fixed asset investment of anaerobic fermentation projects with the same gas production scale is reduced.

The utility model relates to a solvent regeneration system which comprises a solvent regenerator, a distillation column, a solvent cooler and a vapor-liquid separation chamber, a solvent inlet is formed in the top of the solvent regenerator, a heating device is arranged in the solvent regenerator, the top of the solvent regenerator is communicated with the bottom of the distillation column, and filler and a nozzle are arranged in the distillation column; a vapor phase outlet of the distillation column is connected with a vapor phase inlet of a solvent cooler, a cooling device is arranged in the solvent cooler, the top of the solvent cooler is communicated with the bottom of a vapor-liquid separation chamber, and a non-condensed vapor outlet is formed in the top of the vapor-liquid separation chamber and connected with a vacuum vapor exhaust system; and a liquid phase outlet at the bottom of the solvent cooler is connected with a spray head in the distillation column and a regenerated solvent return pipeline. According to the utility model, the regeneration of solvents such as N-formylmorpholine and the like can be realized, the regeneration quality of the N-formylmorpholine solvent which is recycled in a production system is improved, and the extraction operation efficiency is improved.

The continuous production heat pump assisted integrated extractive distillation device is adopted to realize high-purity separation and recovery of the diethyl ether-methyl formate-n-pentane azeotrope, and separation is realized by utilizing the characteristic that the extraction agent has great influence on the relative volatility of the diethyl ether-methyl formate-n-pentane azeotrope. The purity of the separated diethyl ether, n-pentane and methyl formate reaches 99.9% or above, high-purity recycling of the extraction agent can be achieved, the separation cost is greatly reduced, and the method is low in energy consumption and flexible to operate.

The invention relates to an extractive distillation device and a waste liquid recovery method. The extractive distillation device comprises an evaporator, a primary tower, an impurity removal tower, an extractive distillation tower and a product recovery tower which are sequentially communicated through pipelines; the evaporator is provided with a raw material inlet, a first liquid phase inlet, a first liquid phase outlet, a first gas phase outlet, a first steam inlet and a first steam condensate outlet, and the primary distillation tower is provided with a primary distillation gas phase inlet and a primary distillation liquid phase outlet; the first gas phase outlet is communicated with the primary distillation gas phase inlet through a pipeline, the first liquid phase inlet is communicated with the primary distillation liquid phase outlet through a pipeline, and the first liquid phase outlet is used for flowing out impurities. According to the device and the recovery method, MDG and NMF in the waste liquid are further separated by adopting the extraction agent, MDG and NMF products can be respectively recovered, and thus the industrial utilization value of the MDG and NMF mixture is expanded.

The invention provides a fused salt extractive distillation separation device for zirconium and hafnium tetrachloride, which comprises a rectifying tower, a reboiler, a reflux tank, a circulating tank, a sublimator, a gas preheater and a condenser, and during installation, all the parts are sequentially connected to obtain the complete zirconium and hafnium tetrachloride fused salt extractive distillation separation device. The device is simple in structure, easy and convenient to operate, convenient to connect and suitable for molten salt extractive distillation separation of zirconium-hafnium tetrachloride.

The embodiment of the invention provides an extractive distillation system, a control method and an extractive distillation process, and belongs to the technical field of chemical separation and purification. The extractive distillation system comprises an extractive distillation tower, a first condenser, a first reboiler, a first reflux tank, an extraction agent recovery tower, a second condenser, a second reboiler, a second reflux tank, a raw material preheater, a plurality of regulating valves, a plurality of material conveying pumps and control equipment, the control equipment comprises a first pressure controller, a second pressure controller, a first reflux tank liquid level controller, a first reboiler liquid level controller, a second reflux tank liquid level controller, a second reboiler liquid level controller, a first reflux ratio controller, a first cascade control loop and a second cascade control loop, a third cascade control loop and a fourth cascade control loop. The extractive distillation system has the technical effect of improving the purity of the obtained product.

A Cannabis processing system comprises a grinding apparatus and a cell disruption apparatus. The grinding apparatus is configured to grind wet Cannabis cuttings to from a ground, wet Cannabis material comprising wet Cannabis particles having an average particle size within a range of from about 1 mm to about 3 mm. The cell disruption apparatus is downstream of the grinding apparatus and is configured to disrupt cell walls of plant cells of the wet Cannabis particles through one or more of flash freezing, a cellulose solvent, applied negative pressure, and vacuum distillation to facilitate removal of one or more cannabinoids within the plant cells of the wet Cannabis particles. Methods of processing Cannabis are also described.

A process for preparing a purified benzene composition from a crude hydrocarbon stream containing at least 10% by volume of benzene is provided. The process comprises subjecting the crude hydrocarbon stream and a further recycled benzene containing stream to a solvent-based extraction so as to produce a benzene enriched aromatic stream and a benzene depleted non-aromatic stream, subjecting the benzene enriched aromatic stream to a hydrodesulfurization so as to obtain a desulfurized aromatic stream, subjecting the desulfurized aromatic stream to a distillation producing a purified benzene stream and a further benzene containing stream having a benzene concentration of between less than 100% by weight and the azeotropic benzene concentration, and at least partially recycling the further benzene containing stream.