Provided is a method capable of manufacturing high-purity 1,3-butylene glycol having a high potassium permanganate test value, a very low content of low boiling point components, and a high initial boiling point with a high recovery rate.

The method for manufacturing 1,3-butylene is a method for obtaining purified 1,3-butylene glycol from a crude reaction liquid containing 1,3-butylene glycol. In a dehydration column used in a dehydration step, a liquid feed containing 1,3-butylene glycol and water with an acetaldehyde content of 1000 ppm or lower and a crotonaldehyde content of 400 ppm or lower is distilled under a condition of a reflux ratio of higher than 0.3, and a liquid concentrated with a low boiling point component containing water is distilled off from above a feed tray. In a product column used in a product distillation step, a 1,3-butylene glycol liquid feed with an acetaldehyde content of 500 ppm or lower and a crotonaldehyde content of 200 ppm or lower is distilled under a condition of a reflux ratio of higher than 0.1.

Commercially beneficial carbon-containing fractions can be recovered from hydrothermal liquefaction reactions in various types of processors. Feedstock slurry from waste solids is placed into a pressurized processor where it is maintained at temperature and pressure for a predetermined period. On discharge from the processor the processed discharge is separated into liquid and solid fractions. Gaseous fractions including carbon dioxide can also be removed or off-taken from the processor. New molecular structures are created in this reaction, resulting in fractions including biogas, biofuels, biosolids and biocrude. Silica, phosphates, potash and low concentration nitrogen based fertilizer, along with carbonaceous material can also be recovered.

Commercially beneficial carbon-containing fractions can be recovered from hydrothermal liquefaction reactions in various types of processors. Feedstock slurry from waste solids is placed into a pressurized processor where it is maintained at temperature and pressure for a predetermined period. On discharge from the processor the processed discharge is separated into liquid and solid fractions. Gaseous fractions including carbon dioxide can also be removed or off-taken from the processor. New molecular structures are created in this reaction, resulting in fractions including biogas, biofuels, biosolids and biocrude. Silica, phosphates, potash and low concentration nitrogen based fertilizer, along with carbonaceous material can also be recovered.

Provided are a method and device for preparing adiponitrile. The method of the present disclosure comprises the steps of a first hydrocyanation reaction, an isomerization reaction and a second hydrocyanation reaction, wherein online Raman spectroscopy is used for detecting the content of a specific component in the system; and the reaction conditions are regulated based on the detection results, so as to achieve precise control of the materials in each step of the reaction system. The method of the present disclosure can reduce an amount of butadiene, thereby reducing the subsequent energy consumption needed for recycling butadiene and equipment investment after reaction; by monitoring the content of hydrocyanic acid in real time, the residue of hydrocyanic acid is reduced to a lower level, and the operation safety and the stability of a catalyst during reaction are improved; and the loss of the catalyst is reduced.

Provided is a method capable of yielding high-purity 1,3-butylene glycol having a very low content of a low boiling point component and a high initial boiling point, with a high recovery ratio. A reaction crude liquid containing 1,3-butylene glycol is subjected to product distillation to yield purified 1,3-butylene glycol, through dehydration including removing water by distillation and performing high boiling point component removal including removing a high boiling point component by distillation. A method for producing 1,3 butylene glycol, the method including: distilling a charged liquid having a water content of 1.2 wt.% or less in a product column for use in the product distillation under a condition of a reflux ratio of greater than 0.1; distilling off a liquid in which a low boiling point component is concentrated from above a charging plate; and extracting 1,3-butylene glycol from below the charging plate.

A system of interlocks for controlling flow of low temperature process streams in a manufacturing process through a cold box to equipment or piping not specified for such temperatures by opening and closing valves and starting and stopping pumps. At least one interlock affects streams heated in the cold box. At least one interlock affects the streams cooled in the cold box. The interlocks are activated by temperatures of process lines to prevent exposure of equipment and piping to low temperatures while preventing the shutdown of the cold box. An override controller including a predictive failure capability is also provided.

The present application relates to processing of cannabis material, particularly on a large scale, such as at an industrial level. Cannabis is typically a controlled and regulated substance, and has traditionally been processed in low quantities. A human-based manual and/or labour-intensive processing implementation is not scalable, and is therefore infeasible at an industrial level. Disclosed herein are systems and methods for facilitating industrial-scale processing of cannabis material.

A high-purity 1,3-butylene glycol product that is colorless and odorless (or almost colorless and odorless), unlikely to cause coloration and odor over time, and/or unlikely to cause an acid concentration increase over time when the product is left in a state containing water is provided. A 1,3-butylene glycol product containing 1,3-butylene glycol, wherein, after the 1,3-butylene glycol product has been kept at 180° C. for 3 hours in air atmosphere, at least one of contents of compounds represented by the following Formula (A) or (B) is less than 8 ppm. In the following formula, R.sup.1 to R.sup.4 are the same as or different from each other, and each of R.sup.1 to R.sup.4 is a hydrogen atom, an alkyl group which has from 1 to 4 carbon atoms and may be substituted with a hydroxy group, or an alkenyl group which has from 2 to 4 carbon atoms and may be substituted with a hydroxy group.

A water vapor distillation system. The system includes a water vapor distillation device configured to receive a volume of source water from a fluid source and produce distillate, the device comprising: a concentrate flow path comprising a concentrate output; a distillate flow path comprising a distillate output; at least one source proportioning valve; a first heat exchanger comprising at least a portion of the distillate flow path; a second heat exchanger including at least a portion of the concentrate flow path, wherein the first heat exchanger and the second heat exchanger in fluid flow communication with the fluid source; a distillate sensor assembly in communication with the distillate flow path and located downstream the first heat exchanger, the distillate sensor assembly configured to generate a distillate temperature measurement; and a controller configured to control the source proportioning valves, the controller configured to: receive the distillate temperature measurement; determine the difference between a first target temperature and the distillate temperature measurement; and split the source water from the fluid source between the first heat exchanger and the second heat exchanger based on the difference between the first target temperature and the distillate temperature measurement.

A water vapor distillation system. The system includes a water vapor distillation device configured to receive a volume of source water from a fluid source and produce distillate, the device comprising: a concentrate flow path comprising a concentrate output; a distillate flow path comprising a distillate output; at least one source proportioning valve; a first heat exchanger comprising at least a portion of the distillate flow path; a second heat exchanger including at least a portion of the concentrate flow path, wherein the first heat exchanger and the second heat exchanger in fluid flow communication with the fluid source; a distillate sensor assembly in communication with the distillate flow path and located downstream the first heat exchanger, the distillate sensor assembly configured to generate a distillate temperature measurement; and a controller configured to control the source proportioning valves, the controller configured to: receive the distillate temperature measurement; determine the difference between a first target temperature and the distillate temperature measurement; and split the source water from the fluid source between the first heat exchanger and the second heat exchanger based on the difference between the first target temperature and the distillate temperature measurement.