5results about How to "Reduce backmixing" patented technology

The present application relates to a kind of for aromatic hydrocarbon combined plant adsorption separation unit extract partition wall rectification system, including partition wall rectification tower, toluene separation flow path, p-xylene separation flow path and p-diethylbenzene separation flow path;Partition wall rectification tower includes the partition wall being arranged in tower interior, one end of partition wall is fixed in tower bottom, the other end of partition wall extends upwards and is kept a certain distance from tower top, and partition wall separates the space in tower interior into first separation chamber and second separation chamber being arranged left and right, and common rectification chamber being located above partition wall, first separation chamber, second separation chamber and common rectification chamber are in fluid communication;Toluene separation flow path is connected with the top of common rectification chamber;P-diethylbenzene separation flow path is connected with the bottom of first separation chamber;P-xylene separation flow path is connected with the bottom of second separation chamber.Compared with double-tower rectification process, investment is greatly reduced, tower top gas cooling load is less, system waste heat is fully recycled, energy consumption and cost are reduced, and economic benefit is generated.

The invention discloses a vertical-flow single-kettle type extraction machine, an adjusting method, a multi-stage counter-current extraction system connected in series with the vertical-flow single-kettle type extraction machine and a control adjusting method. The extraction machine is of a vertical single-kettle structure, a combination of a mixing cylinder, a guide cylinder and a container outer shell is formed in the extraction machine, and the extraction machine further comprises a variable-speed stirrer, a phase clarification functional filler, a two-phase liquid inlet pipe orifice, a two-phase liquid outlet pipe orifice and the like. The variable-speed stirrer drives the two-phase materials to be fully blended in the mixing chamber in a lower plug flow mode and form stable pressurized conveying, the blended materials are returned and then enter the annular clarifying chamber in a horizontal radiation flow mode to achieve efficient layering, and a pressurizing pressure head is reserved for discharging. A plurality of stages of single-kettle type extractors are connected in series according to a countercurrent mass transfer mode, and interstage connection and regulation assemblies are configured to form a countercurrent extraction system capable of supporting extraction under pressure. The system is operated according to a specific method, the whole line can be started and stopped at any time with lossless efficiency, the processing capacity can be greatly adjusted on line, the two-phase flow ratio can be adjusted on the whole line, the system can be conveniently started to distribute materials, and the system can be conveniently stopped and discharged according to quality.

The invention relates to the technical field of catalysts, and discloses a heteropolyacid catalyst as well as a preparation method and application thereof. The roundness P of the heteropolyacid catalyst is more than or equal to 0 and less than or equal to 0.8, meanwhile, the stacking density rho of the heteropolyacid catalyst is limited, and the relationship between the roundness P and the average radius Ravg is more than or equal to 0 and less than or equal to 0.95, namely (2 * rho * P) / Ravg; the catalyst can be efficiently stacked and arranged in the tube nest of the reactor, so that the catalyst is arranged more tightly, channeling and reverse mixing of feed gas among catalyst particles are effectively reduced, the utilization rate of methylacrolein can be increased in the reaction of producing methacrylic acid by oxidizing methylacrolein, and meanwhile, the occurrence of excessive reaction is reduced; therefore, the catalyst can keep high methylacrolein conversion rate and methacrylic acid selectivity at the same time. Meanwhile, the specific structure of the outer surface of the catalyst can enable the catalyst to obtain good mechanical strength, the cracking and crushing conditions of the catalyst are reduced, and the service life of the catalyst is prolonged.

This invention discloses a gas-liquid mass transfer unit, comprising: an upper tray channel extending downward from an opening in the upper tray; a swirl vane array at the top of the upper tray channel, with a first through-hole on the channel wall at a fixed position of the swirl vanes, for allowing only gas phase flow during the gas phase flow stage, forming a swirling flow through the swirl vane array, and for allowing only liquid phase flow during the liquid phase flow stage; a first constriction at the bottom of the upper tray channel, with a second through-hole along the upper edge of the first constriction for liquid phase overflow; a lower tray channel with a third through-hole at its upper part, for allowing only gas phase flow during the gas phase flow stage and only liquid phase flow during the liquid phase flow stage; a fourth through-hole in the lower middle part of the lower tray channel; a second constriction at the top of the lower tray channel; and a movable component that can slide entirely within the upper and lower tray channels; the movable component includes an upper circular surface and a lower circular surface fixedly connected; when the movable component moves to the top under the lifting action of the gas phase, it is in the gas phase flow stage; when the movable component moves downward under the gravity action of the liquid phase, it is in the liquid phase flow stage.

The present application belongs to the technical field of petroleum chemical industry, and discloses a condensate oil separation process and device. The core of the condensate oil separation process is to improve the 'light and heavy gradual separation' process into a 'light, medium and heavy simultaneous separation' new process, and to open the side line production in the primary distillation column and the fractionating column of the condensate oil separation device. Part of the intermediate components are separated in advance, so that the back mixing of the intermediate component light naphtha in the primary distillation column and the back mixing of the intermediate component heavy naphtha in the fractionating column can be reduced, repeated rectification can be avoided, the separation difficulty of the system and the energy consumption can be effectively reduced; the C5 separation tower of the old original process is used for separating the mixed fraction of light naphtha and heavy naphtha after the pressure reduction transformation of the C5 separation tower; the heat pump technology is used in the debutanizer, the low-grade heat at the top of the tower is upgraded to serve as the reboiling heat source at the bottom of the debutanizer, part of the steam at the bottom of the tower is replaced, and the consumption of the cold utility at the top of the tower is reduced.