The present system is for simultaneous recovery of purified water and dissolved solids from impure high TDS water (1) which is achieved in a single step and eliminates the use of external thermal energy for making the system significantly efficient. It eliminates the use of boiler, cooling tower that reduces the overall capital cost and continuous requirement of external thermal energy for making system efficient. The simultaneous recovery of the purified water and solids from high TDS input effluent reduce the energy intensity of the system. Said system provides a vacuum system as heat pump which enables the system to be self-sufficient in thermal energy requirements for evaporation process and reduces GHG emissions significantly.

The present system is for simultaneous recovery of purified water and dissolved solids from impure high TDS water (1) which is achieved in a single step and eliminates the use of external thermal energy for making the system significantly efficient. It eliminates the use of boiler, cooling tower that reduces the overall capital cost and continuous requirement of external thermal energy for making system efficient. The simultaneous recovery of the purified water and solids from high TDS input effluent reduce the energy intensity of the system. Said system provides a vacuum system as heat pump which enables the system to be self-sufficient in thermal energy requirements for evaporation process and reduces GHG emissions significantly.

Continuous photochemical production of high purity linear mercaptan and sulfide-containing compositions.

Continuous photochemical production of high purity linear mercaptan and sulfide-containing compositions.

The present disclosure relates to a heat exchange system which is capable of saving energy consumed in a whole process by exchanging heat of different streams from each other, included in a continuous preparation system of a diester-based composition.

A hydrocracking process is disclosed. The hydrocracking process comprises hydrocracking a hydrocarbon feed stream in a hydrocracking reactor in the presence of a hydrogen stream and a hydrocracking catalyst to produce a hydrocracked effluent stream. The hydrocracked effluent stream is separated in a separator to provide a vapor hydrocracked stream and a liquid hydrocracked stream. The liquid hydrocracked stream is fractionated to provide a naphtha stream, a kerosene stream having a T90 temperature of about 204° C. (399° F.) to about 238° C. (460° F.), a diesel stream having a T90 temperature of about 360° C. (680° F.) to about 383° C. (721° F.) and an unconverted oil stream. The kerosene stream, the unconverted oil stream, and a portion of the diesel stream is recycled to the hydrocracking reactor for hydrocracking.

A hydrocracking process is disclosed. The hydrocracking process comprises hydrocracking a hydrocarbon feed stream in a hydrocracking reactor in the presence of a hydrogen stream and a hydrocracking catalyst to produce a hydrocracked effluent stream. The hydrocracked effluent stream is separated in a separator to provide a vapor hydrocracked stream and a liquid hydrocracked stream. The liquid hydrocracked stream is fractionated to provide a naphtha stream, a kerosene stream having a T90 temperature of about 204° C. (399° F.) to about 238° C. (460° F.), a diesel stream having a T90 temperature of about 360° C. (680° F.) to about 383° C. (721° F.) and an unconverted oil stream. The kerosene stream, the unconverted oil stream, and a portion of the diesel stream is recycled to the hydrocracking reactor for hydrocracking.

The hybrid desalination and energy production system includes a desalination system for separating seawater into purified water and brine, an electrodialysis system for treating the brine and outputting low salinity water, a hypersaline brine solution, and H.sub.2 gas; an evaporator for treating the hypersaline brine solution and outputting salt and water vapor; a superheater for treating the water vapor and outputting a superheated water vapor; a turbine for receiving the superheated water vapor to generate energy; a gas scrubber for receiving the H.sub.2 gas from the electrodialysis system and producing dry hydrogen; and a hydrogen cell for receiving the dry hydrogen and outputting energy. A condenser converts the vapor into condensate and low salinity water. A desalinated water collection tank receives the desalinated or low salinity water. A pressure retarded osmosis system receives the brine, the low salinity water, and condensate from the condenser to produce dilute brine.

A process for producing one or more of benzene, toluene, or mixed xylenes may include combining one or more aromatic feed chemicals, one or more aromatic-based polymers, hydrodearylation catalyst, and hydrogen in a hydrodearylation unit to form a chemical product. The process may also include passing the chemical product out of the hydrodearylation unit, where the chemical product comprises one or more of benzene, toluene, and mixed xylenes. Additionally, a system for producing one or more of benzene, toluene, or mixed xylenes may include a mixing unit and a hydrodearylation unit. An aromatic feed stream and an aromatic-based polymer stream may be in fluid communication with a mixing unit. A mixing unit effluent stream may be in fluid communication between the mixing unit and the hydrodearylation unit. A chemical product stream may be in fluid communication with the hydrodearylation unit.

A process for producing one or more of benzene, toluene, or mixed xylenes may include combining one or more aromatic feed chemicals, one or more aromatic-based polymers, hydrodearylation catalyst, and hydrogen in a hydrodearylation unit to form a chemical product. The process may also include passing the chemical product out of the hydrodearylation unit, where the chemical product comprises one or more of benzene, toluene, and mixed xylenes. Additionally, a system for producing one or more of benzene, toluene, or mixed xylenes may include a mixing unit and a hydrodearylation unit. An aromatic feed stream and an aromatic-based polymer stream may be in fluid communication with a mixing unit. A mixing unit effluent stream may be in fluid communication between the mixing unit and the hydrodearylation unit. A chemical product stream may be in fluid communication with the hydrodearylation unit.