1023results about "Flash distillation" patented technology

The utility model discloses a waste heat steam boiler based on integration of a sulfur combustion furnace and nitrogen heat extraction, and belongs to the technical field of salt chemical engineering and waste heat recovery. In order to solve the problem of waste of waste heat of high-temperature SO2 flue gas in the SO2 preparation process of the sulfur combustion furnace, a layer of enclosure shell is additionally arranged outside a heat-preservation-free shell of the sulfur combustion furnace, an annular area between the enclosure shell and the heat-preservation-free shell serves as a heat exchange area, nitrogen or air serves as a heat exchange medium, dividing wall type heat exchange is carried out through the shell of the combustion furnace, the temperature of the nitrogen is increased, and the heat exchange efficiency is improved. The flue gas in the furnace is discharged after the temperature is gradually reduced; after being heated, the nitrogen is fed into the miniature high-temperature waste heat hot water boiler and exchanges heat with high-temperature waste heat water through the heat exchanger, and the cooled nitrogen is returned and circularly exchanges heat. The heated high-temperature waste heat supplied water is sent to downstream heat consumers and is continuously and circularly heated; the pressure of the flash steam is 0.1-0.6 MPa, and the flash steam is supplied as process steam, so that the flue gas waste heat can be greatly recovered when the normal operation of sulfur combustion is maintained.

The utility model relates to a sludge drying system coupled with a heat storage system. The sludge drying system comprises a heat storage module, a sludge drying module, a waste heat collecting module and a waste heat upgrading module, the heat storage module is used for storing peak regulation steam energy of the power plant; the sludge drying module is connected with the heat storage module, comprises a plurality of drying machines which are connected in parallel, and is used for drying sludge by utilizing low-pressure steam; the waste heat collecting module is connected with the sludge drying module and is used for recycling high-temperature waste gas waste heat; the waste heat quality improving module is connected with the waste heat collecting module and used for improving the quality of the waste heat and recycling the waste heat. The utility model has the beneficial effects that the drying technology is coupled with a boiler system, so that steam energy which is difficult to store is converted into storable and combustible fuel, the deep peak regulation of a power plant is facilitated, the scale of a heat storage system is reduced, and the economical efficiency of the system is improved.

A brine concentration system may include a closed-cycle heat pump, a brine heater configured to heat brine, a flash tank to evaporate a portion of heated brine to steam, and a steam condenser in which to condense the steam to distilled water. The system may include an electric vacuum pump in connection with the flash tank and the steam condenser. The electric vacuum pump may reduce a pressure within the flash tank and the steam condenser to reduce a boiling point of the brine. The system may include a controller that dynamically adjusts operations of the closed-cycle heat pump and / or the electric vacuum pump.

The utility model discloses a heat source optimizing device for a reboiler of a methanol pre-rectifying tower, which comprises the pre-rectifying tower and the reboiler, and is characterized in that a branch pipeline is separated from the crude methanol discharge of a tower kettle and is connected with a negative pressure flash tank, and the crude methanol in the negative pressure flash tank is subjected to gas-liquid separation through flash evaporation; the bottom of the negative-pressure flash tank is connected with a methanol circulating pump, and a liquid-phase material is conveyed to a first heat exchanger at the top of the tower and returns to the negative-pressure flash tank after exchanging heat with steam at the top of the tower; a gas-phase material in the negative-pressure flash tank enters a compressor, is compressed and heated and then returns to the tower kettle of the pre-rectifying tower; according to the utility model, the process is improved by combining flash evaporation of a tower kettle discharge part with heat pump rectification, and meanwhile, the flash evaporation liquid is recycled to recycle steam heat at the top of the tower, so that the steam consumption of a reboiler of the methanol pre-rectifying tower and the use amount of circulating water at the top of the tower are effectively reduced, meanwhile, the reboiler does not need to be added, and the compression ratio of a heat pump compressor can be reduced.

The invention belongs to the field of industrial flue gas purification technology and energy conservation, and relates to a system and a method for removing condensable particulate matters through multi-field coupling synergistic enhanced condensation, the system comprises a desulfurization tower, a flash tank, a condensation structure, a liquid collecting tank and a cold water spraying layer, a slurry distribution layer of the flash tank is connected with a tower kettle of the desulfurization tower, and a flash slurry pool of the flash tank is connected with the slurry spraying layer; the liquid collecting tank, the condensation structure and the cold water spraying layer are sequentially arranged from bottom to top and are integrated in the same shell to form a secondary removal device capable of condensing particles, the secondary removal device is communicated with the top of the desulfurization tower, and flue gas channels are uniformly distributed on the liquid collecting tank; the condensation structure is formed by combining a plurality of obliquely-arranged wave-shaped condensation plates in parallel, the surfaces of the wave-shaped condensation plates are arranged in a hydrophobic mode, a plurality of protrusions and pits are arranged on the faces, facing flue gas, of the wave-shaped condensation plates, and condensable particles in the flue gas can be effectively removed.

The invention discloses a high-viscosity polymerization solution devolatilization system. The high-viscosity polymerization solution devolatilization system comprises a first-stage flash heater, a first-stage flash tank distributor, a first-stage flash tank, a second-stage flash heater, a second-stage flash tank distributor, a second-stage flash tank, a third-stage flash tank distributor and a third-stage flash tank. The invention also provides a high-viscosity polymerization solution devolatilization process which is operated in the system. According to the high-viscosity polymerization solution devolatilization system and process provided by the invention, through static flash devolatilization, dynamic flash does not need to be introduced, and the energy consumption is relatively low; in the high-viscosity polymerization solution devolatilization process provided by the invention, the glue solution content in the polymer solution at the liquid phase outlet of the first-stage flash tank is 50-75% wt, the glue solution content in the polymer solution at the liquid phase outlet of the second-stage flash tank is 85-93% wt, the glue solution content in the polymer solution at the liquid phase outlet of the third-stage flash tank can reach 99.9% wt or more, and the devolatilization efficiency is high.

The invention discloses a method and a device for removing alcamines in NMP (N-Methyl Pyrrolidone), which comprises the following steps: reacting anhydride substances with NMP containing the alcamines substances to generate NMP containing amide substances; the NMP solution containing the amide substances is rectified to remove the amide substances, and NMP with the alcohol amine substances removed is obtained; the boiling point of the product is increased in a manner that anhydride substances react with alcohol amine substances in NMP to generate amide, so that the difference value between the reacted product and the boiling point of NMP is greater than the difference value between the alcohol amine substances and the boiling point of NMP, high-purity NMP is more easily separated in a subsequent rectifying tower, the energy consumption of the rectifying tower for separating the product and impurities can be reduced, and the production cost is reduced. In addition, due to the fact that different alcohol amine additives do not need to be added additionally, universality is improved, meanwhile, the anhydride reaction belongs to amidation reaction, reaction products are more stable, free amine cannot be decomposed in the high-temperature heating process, and therefore the purity of the separated NMP can be further improved.

The invention provides a gas purification and separation method and device, and belongs to the technical field of gas purification. The method comprises the following steps: mixing process gas and methanol, and sequentially carrying out condensation treatment and gas-liquid separation treatment to obtain gas-liquid separation process gas and acidic gas condensate; carrying out methanol washing on the gas-liquid separation process gas to realize desulfurization and decarbonization so as to obtain purified gas and rich methanol (including first sulfur-containing methanol and carbon-rich methanol); carrying out first flash separation treatment on the acidic gas condensate to respectively obtain acidic gas, second sulfur-containing methanol and solid carbon dioxide; washing the solid carbon dioxide with methanol, dissolving the solid carbon dioxide in methanol, and carrying out second flash separation treatment on the obtained methanol rich in carbon dioxide to respectively obtain gas carbon dioxide and cold methanol containing carbon dioxide; the carbon dioxide-containing cold methanol can be reused for dissolving the washed solid carbon dioxide after being heated; heat exchange is carried out between the second flash separation treatment and the condensation treatment. The method has a good process gas purification and separation effect, and has the advantages of energy conservation and consumption reduction.

A system and method for continuously purifying contaminated polymers, such as polypropylene, at a commercial scale. In one embodiment, the system and method involves obtaining reclaimed plastic, mixing the reclaimed plastic with a solvent, purifying the mixture through decanting and devolatilization steps, and recycling the reclaimed solvent back into the system.

The present application relates to a kind of heat pump rectification systems based on heat shock flash circulation lift heat exchange, including rectifying tower, lift membrane reboiler, first throttling valve and heat shock heater, the secondary steam outlet of rectifying tower is connected with the heating steam import of lift membrane reboiler, the discharge port of the bottom of rectifying tower is connected with the cold side flow channel import of heat shock heater, and the cold side flow channel export of heat shock heater is connected with the feed inlet of lift membrane reboiler by first throttling valve;The vapor-liquid mixture outlet of lift membrane reboiler is connected with the column still liquid reflux port of rectifying tower, and the steam condensate outlet of lift membrane reboiler is connected with condensate tank, and the liquid outlet of condensate tank is connected with the condensate reflux port of rectifying tower side wall.The present application is combined by heat shock pressurization energy storage and throttling flash kinetic energy release, provides independent and stable lift membrane kinetic energy for lift membrane heat exchange, so that the flow pattern in the tube of lift membrane reboiler directly enters the efficient annular flow stage, improves the industrial applicability of lift membrane heat exchange technology in heat pump rectification system.

The present application relates to a kind of hot exciting flash evaporation loop lift heat exchanger, including upper head, lower head, cylinder, several heat exchange tubes, the upper end surface of cylinder and the upper head form cavity I between, the lower end surface of cylinder and the lower head form cavity II between, cavity I, cavity II and the inner cavity of cylinder are not communicated with each other between, heat exchange tube is fixed in the inside of cylinder by tube sheet, the upper end of heat exchange tube is placed in cavity I and is communicated with cavity I, lower end and cavity II are communicated, cylinder includes lift section cylinder and hot exciting section cylinder, heat exchange tube includes lift section heat exchange tube and hot exciting section heat exchange tube, lift section heat exchange tube and hot exciting section heat exchange tube are communicated by throttling component between, the inner diameter of throttling component is less than the inner diameter of hot exciting section heat exchange tube.The heat exchanger of the present application is provided with a kind of hot exciting flash evaporation loop lift, will hot exciting pressurization energy storage, throttling flash evaporation kinetic energy release, loop lift heat exchange and vapor-liquid separation function integration in same equipment, solve the problem of traditional lift section heat exchanger dependence big temperature difference.

The invention belongs to the technical field of separation and recovery, and particularly relates to separation and recovery equipment and process for an R410A mixed refrigerant based on a deep eutectic solvent. The separation and recovery equipment for the R410A mixed refrigerant based on the eutectic solvent comprises an absorption tower, a first flash tank and a second flash tank, the liquid outlet end and the liquid inlet end of the absorption tower are communicated and connected through a circulating pipe; the first flash tank and the second flash tank are arranged on the circulating pipe; a first heat exchanger is arranged on the circulating pipe and between the first flash tank and the second flash tank, and a second heat exchanger is arranged on the circulating pipe and between the second flash tank and the liquid inlet end of the absorption tower; the gas outlet end of the first flash tank is communicated with the gas inlet end of the absorption tower through a communicating pipe; a third heat exchanger is arranged on the communicating pipe. By adopting the equipment and the process provided by the invention, the recovery rates of R32 and R125 in the R410A mixed refrigerant both reach 95% or above.

A fly ash prevention device for treating high-concentration water relates to the technical field of petrochemical engineering and comprises a flash evaporation concentration tower, a flash steam outlet is formed in the top of the flash evaporation concentration tower, and a black water outlet is formed in the bottom of the flash evaporation concentration tower; the tower wall of the flash concentration tower is connected with a black water connecting pipe, and black water tangentially enters the tower through the black water connecting pipe; a black water concentration chamber is arranged at the bottom in the flash evaporation concentration tower, the bottom of the black water concentration chamber is communicated with a black water outlet, an ascending pipe is arranged above the black water concentration chamber, a steam ascending cap is arranged on the ascending pipe, a fly ash prevention filler washing assembly is arranged above the steam ascending cap, and a gas distributor is arranged above the fly ash prevention filler washing assembly; a high-efficiency demister is arranged at the top in the flash evaporation concentration tower and is arranged on the flash steam outlet; according to the technical scheme, coal gasification and heavy oil gasification water systems are optimized, black water is concentrated, the washing environment is improved, and fly ash is prevented from being carried into a rear system.

The utility model relates to the technical field of hydrochloric acid desorption, in particular to a hydrochloric acid desorption device which comprises a hydrochloric acid desorption tower, and the top of the hydrochloric acid desorption tower is sequentially communicated with a primary condensing device, a secondary condensing device, a freezing device, a demister and a hydrogen chloride buffer tank; one side wall of the hydrochloric acid desorption tower is communicated with a hydrochloric acid storage tank; the side wall of the hydrochloric acid desorption tower is also communicated with a calcium chloride solution storage tank; a bottom liquid outlet of the hydrochloric acid desorption tower is communicated with a first inlet of the thermosyphon reboiler, the thermosyphon reboiler is provided with a first outlet and a second outlet, the first outlet is communicated with a liquid inlet of the hydrochloric acid desorption tower, and the second outlet is sequentially communicated with the multi-effect evaporation device and the flash separation tank; and the flash separation tank is respectively communicated with a calcium chloride solution storage tank and a second inlet of the thermosyphon type reboiler. According to the utility model, the equipment investment is reduced, the concentration efficiency of the calcium chloride solution is improved, the energy consumption is reduced, and calcium chloride is prevented from flowing back into the desorption tower to cause blockage.

The invention belongs to the field of chemical purification, and discloses a method and equipment for separating carbon tetrafluoride in nitrogen trifluoride through pressurized absorption of a deep eutectic solvent, and the method comprises the following steps: (1) increasing the pressure of nitrogen trifluoride crude gas to 0.5 MPa or above; (2) cooling the crude gas to below 40 DEG C through a crude gas feeding heat exchanger; (3) through the absorption tower, the crude gas entering from the tower kettle is in countercurrent contact with the eutectic solvent entering from the tower top, and the content of carbon tetrafluoride in the crude gas is reduced to 5 ppm or below; (4) reducing the content of carbon tetrafluoride in the eutectic solvent to be less than 1ppm through a two-stage flash tank; and (5) reducing the temperature of the eutectic solvent to be below 30 DEG C through a eutectic solvent discharging heat exchanger and a eutectic solvent cooler, and circulating the eutectic solvent back to the absorption tower from the bottom of the absorption tower. According to the method, the quality of the nitrogen trifluoride product can be improved, the carbon tetrafluoride impurity in the nitrogen trifluoride purity can be reduced to 5ppm, and the cost is low.

The utility model discloses a styrene tail gas runner adsorption concentration coupling solvent absorption treatment system, which comprises a runner unit, an absorption tower and a flash evaporation analysis unit which are sequentially connected, a waste gas pipeline is connected with a tail gas inlet of the runner unit, and a concentrated gas outlet of the runner unit is connected with a gas phase inlet at the bottom of the absorption tower; the flash evaporation analysis unit comprises a flash evaporation kettle and a rich liquor reflux washing tower, a rich liquor outlet of the absorption tower is divided into two paths, one path is connected with the flash evaporation kettle through a rich liquor intermediate tank, a lean-rich liquor heat exchanger, a rich liquor-flue gas heat exchanger and a rich liquor electric auxiliary heating heater, and the other path is connected with the flash evaporation kettle through the rich liquor reflux washing tower; a gas phase outlet of the flash kettle is connected with a gas phase inlet of the pregnant solution reflux washing tower; a barren liquor outlet of the flash kettle is connected with an absorbent inlet in the top of the absorption tower. The device is low in investment and operation cost, good in tail gas purification effect, energy-saving, consumption-reducing and high in styrene recovery rate.

The invention relates to the technical field of aluminum oxide production, and discloses evaporation forced-effect jet flash evaporation equipment which comprises a storage tank, a heating box is arranged outside the storage tank, an air guide pipe is arranged on the side wall of the storage tank, a flash evaporator is arranged outside the air guide pipe, a conveying pipe is arranged in the heating box, and a flash evaporator is arranged in the conveying pipe. A discharging table is fixedly connected to the lower side of the flash evaporator, a mounting block is fixedly connected to the side wall of the flash evaporator, a flow dividing pipe is fixedly connected to one end of the mounting block, a guiding assembly is arranged on the side wall of the flow dividing pipe, and a flow guiding block is fixedly connected to the interior of the flow dividing pipe. The steam pushes the cleaning assembly to rotate, meanwhile, the steam firstly passes through the flow guide block, and tiny crystals mixed in the steam are preliminarily filtered under the filtration of the flow guide block, so that the effects of preheating the mother liquor in advance, realizing self-circulation of the mother liquor, reducing the use of a circulating pump and further reducing the power consumption of the device can be achieved.

The utility model relates to the technical field of flash evaporation, in particular to a flash evaporation tank which comprises a flash evaporation tank body, a base fixedly installed at the lower end of the flash evaporation tank body, an exhaust pipe arranged at the upper end of the flash evaporation tank body, a liquid collecting hopper arranged on the inner side of the flash evaporation tank body, a supporting plate arranged at the lower end of the liquid collecting hopper, and a feeding valve arranged on the left side of the flash evaporation tank body. A driving motor is arranged on the inner side of the base; a scraping plate I is arranged on the inner side of the flash tank body and located at the upper end of the liquid collecting hopper; a scraping plate II is arranged at the upper end of the scraping plate I; and a discharging valve is communicated with the lower end of the right side of the flash tank body. The driving motor drives the rotating shaft to rotate, so that the first scraper and the second scraper are driven to rotate, liquid drops on the inner wall of the flash tank body are scraped and guided, and the gathering efficiency of the liquid drops is improved.

The utility model discloses evaporation flash evaporation crystallization equipment, which is cylindrical closed equipment consisting of a cylindrical evaporator, a flash evaporation chamber, an upper crystallizer structure, a middle crystallizer structure and a lower crystallizer structure, has the functions of evaporation, flash evaporation and crystallization, can be used for evaporation, flash evaporation and crystallization of solutions, and can be widely applied to the flow of industrial production. Detachable connecting piece flanges are arranged at the raw material inlet A, the steam inlet C, the condensed water outlet D, the gas phase outlet F, the exhaust inlet G, the target product outlet J, the exhaust outlet L and the circulating material outlet M and are detachably connected with the whole production system. The device is reasonable in layout, simple in structure, small in fluid resistance, uniform in fluid distribution, easy to install, overhaul, maintain and clean, wide in application range and suitable for evaporation, flash evaporation and crystallization production systems of various specifications and models.

The invention relates to the technical field of chemical recovery, and particularly discloses a carbon tetrachloride removal system and process, the system comprises a washing tower and a carbon tetrachloride removal assembly, the washing tower is used for introducing a solvent and a phosgene material; the tower top of the washing tower is used for outputting treated substances; a tower kettle of the washing tower is communicated with the carbon tetrachloride removal assembly, and the carbon tetrachloride removal assembly is used for removing carbon tetrachloride in materials from the washing tower. The solvent is introduced into the washing tower to wash the phosgene material, and after the solvent is introduced, the washing tower is not pure phosgene equipment, so that the safety performance is improved; and compared with the prior art that carbon tetrachloride is removed by utilizing a phosgene rectifying tower and a solvent refining tower, the combination of the washing tower and the carbon tetrachloride removal assembly is beneficial to reducing the energy consumption.

The invention discloses a drainage flash heat supply system of a once-through boiler under low load and an operation method of the drainage flash heat supply system. The drainage flash heat supply system comprises a drainage flash control valve, a drainage flash tank, a heat supply steam throttle valve, an electric heater and a condensation drainage recirculation pump which are sequentially arranged behind a water storage tank. When a unit undertakes a peak regulation task and a boiler enters a wet state operation mode under an ultra-low load working condition, drain water generated by a steam-water separator is introduced into a flash evaporation heat supply system, generated high-pressure steam is used for industrial heat supply, the steam meets the requirements of pressure and superheat degree of industrial steam through a throttling valve and an electric heater, and the heat supply efficiency is improved. The drain water produced in the flash tank is re-introduced into the feed line through a condensed drain water recirculation pump. According to the system, power supply and heat supply can be decoupled during low-load operation of a unit, meanwhile, the stable combustion requirement of boiler operation is met, and the hydrodynamic safety of each water cooling wall is protected.

The invention discloses flash tank equipment which comprises a flash tank, a feeding pipe, an exhaust pipe, a conical first heating flow guide body, a first oil way, an annular second heating flow guide body and a second oil way. And a tank wall convex part is arranged on the inner surface of the tank wall of the flash tank. A first oil cavity is formed in the first heating flow guide body, the first heating flow guide body is suspended below the spraying head at the lower end of the feeding pipe and is positioned above the convex part of the tank wall, and the first oil way is connected with the first heating flow guide body and is communicated with the first oil cavity. A second oil cavity is formed in the second heating flow guide body, the second heating flow guide body is arranged below the tip of the convex part of the tank wall, and the second oil way is connected with the second heating flow guide body and communicated with the second oil cavity, so that the heat transfer mode is improved, the heat transfer area and the heat transfer intensity are effectively increased, and the retention time of fluid materials is prolonged; the temperature of the lower half part of the flash tank is increased, so that the flash efficiency is improved, and the quality and the performance of polymer products are ensured.

The utility model relates to the technical field of ammonia distillation equipment, in particular to a microwave indirect heating ammonia distillation tower. Comprising a tower body, a wastewater atomization device, a microwave heating device, a liquid sealing disc, a tower disc and a dephlegmator, an atomizing nozzle of the wastewater atomizing device is mounted in the tower body and located at the middle lower part, and the atomizing nozzle downwards sprays atomized wastewater; the microwave heating device is installed outside the tower body and located below the wastewater atomization device, and atomized wastewater is flashed and vaporized through microwave heating of the microwave heating device; the liquid seal disc and the tower disc are mounted in the tower body, the liquid seal disc is positioned above the wastewater atomization device, and the tower disc is positioned above the liquid seal disc; and the dephlegmator is fixedly connected to the top of the tower body. The method has the advantages of high efficiency, low energy consumption, low cost and small environmental pollution.

The utility model provides a caprolactam rectification heat energy coupling utilization system, which comprises a cyclohexane refining tower, a cyclohexene separation tower and a debenzolization tower which are communicated in sequence, in the system, high-temperature gas-phase materials generated by the cyclohexane refining tower and the cyclohexene separation tower and kettle bottom liquid in the next tower are subjected to heat exchange treatment through a falling film evaporator, and the cyclohexene separation tower and the kettle bottom liquid in the next tower are separated; the feeding temperature of the next tower is increased, so that the heat utilization of high-temperature steam is improved, the use of steam is reduced, and the production cost is reduced; meanwhile, the use of fire coal is reduced, the emission of waste gas is reduced, and the environment is protected.

The utility model provides a synthetic tail gas separation device based on a liquid nitrogen washing mode. The tail gas separation device comprises a TSA adsorption unit, a liquefaction separation unit, a mixed refrigeration circulation unit, a nitrogen circulation unit and a natural gas storage unit, the input end of the TSA adsorption unit is connected with the liquefaction separation unit; the output end of the liquefaction separation unit is respectively connected with the nitrogen-rich out-of-bound area, the hydrogen-rich out-of-bound area and the natural gas storage unit; the mixed refrigeration cycle unit and the nitrogen cycle unit are connected in parallel with the liquefaction separation unit; one path of the output end of the cold box is connected with the dehydrogenation tower; one path of the output end of the dehydrogenation tower is connected with a hydrogen-rich gas outlet area through a cold box; the other path is connected with the denitrification tower; one path of the output end of the denitrification tower is connected with the nitrogen-rich gas out-of-bound area through the return tank and the cold box in sequence; the other path of the output end of the cold box is connected with a liquid nitrogen cooling device through a liquid nitrogen flash tank and a liquid nitrogen booster pump in sequence; according to the device, a mixed refrigerant and liquid nitrogen are used as refrigerating media, and hydrogen-rich gas, nitrogen-rich gas and liquefied natural gas are obtained by separating synthetic tail gas through rectification.

The invention relates to the technical field of product selectivity adjustment in a vinylamine production process, in particular to a piperazine and diethylenetriamine high-selectivity co-production system and process, the piperazine and diethylenetriamine high-selectivity co-production system comprises a raw material storage unit, a reaction unit, an ammonia recovery unit, a product refining unit and a product storage unit, the raw material storage unit is provided with an NH3 storage area and an MEA storage area, a mass flow meter I, a mass flow meter II and a flow proportion control module I are arranged; a stream I is connected between the ammonia recovery unit and the NH3 storage area; the product storage unit comprises an MEA product intermediate tank, an EDA product intermediate tank and an AEA product intermediate tank which are connected with a second stream, a third stream and a fourth stream respectively, and a third mass flow meter, a fourth mass flow meter, a second flow proportion control module and a third flow proportion control module are arranged on the third stream and the fourth stream respectively. The selectivity of piperazine and diethylenetriamine is improved, and the operation benefit of the device is maximized.

The invention relates to the technical field of chemical equipment, and discloses a sodium carbonate production system adopting an ammonia-soda process. The system for producing sodium carbonate by the ammonia-soda process comprises a thin liquid distillation tower and a flash evaporation module. The thin liquid distillation tower is used for discharging waste thin liquid; the flash evaporation module comprises a second flash evaporation device and a water injection assembly; a steam outlet of the second flash tank is communicated with a steam inlet of the thin liquid distillation tower; the water inlet end of the water injection assembly is communicated with the thin liquid distillation tower, and the water outlet end of the water injection assembly is located in the second flash tank and used for discharging waste thin liquid to flush flash steam in the second flash tank. According to the invention, by arranging the water injection assembly, the waste thin liquid discharged from the thin liquid distillation tower is introduced into the second flash tank for flushing flash steam in the second flash tank so as to flush away droplets in the flash steam, and the content of calcium ions introduced into the thin liquid distillation tower can be reduced, so that the calcium ions in the waste thin liquid are reduced and even eliminated; and the waste thin liquid discharged from the thin liquid distillation tower can be used as filtering washing water.

To disclose a pitch production system using coal tar or decant oil for coal-based or petroleum-based pitch.SOLUTION: Total pitch production yields are increased by heat treating distillate fractions from a pitch production process. A heat treatment system and process are disclosed in embodiments. A heaviest distillate having a highest molecular weight is subjected to heat treatment, though other embodiments contemplate heat treating a variety of combined distillate fractions. The heat treatment system requires heat soaking distillates at elevated temperatures of 459 to 535°C at a near-constant temperature with near-uniform flow. A fraction of the heat-treated distillate may be re-introduced to the pitch production system as a part of a continuous process.SELECTED DRAWING: Figure 2A

The utility model discloses a J-T valve dehydration and dealkylation device which comprises a skid-mounted frame, a pretreatment module, a dehydration and dealkylation module and a three-phase separation module are arranged on the skid-mounted frame, and the dehydration and dealkylation module is connected with the pretreatment module through a J-T valve. According to the utility model, the pretreatment module, the dehydration and dealkylation module and the three-phase separation module are all integrated in the compact skid-mounted frame, so that the occupied area is greatly reduced, the installation, transportation and relocation of the device are more convenient and faster, and the operation cost is reduced. Meanwhile, a J-T valve is arranged to be connected with the pretreatment module and the dealkylation module, and condensation and separation of moisture and hydrocarbons in the feed gas are further promoted based on the Joule-Thomson throttling expansion principle. And the efficient and stable dehydration and dealkylation effects are ensured while the occupied area is reduced.