203results about How to "Save cooling" patented technology

The invention relates to a high-precision and constant temperature and humidity cabinet, which is used for storing special articles. The temperature and humidity in the cabinet can be controlled within designated scope automatically and constantly. In the invention, a cooling/heating semiconductor high-temperature stacking is used as a temperature control and dehumidification executive component, an ultrasonic wave humidifier is used as a humidification executive component, and an electric temperature/humidity sensor, a series of fans, keys, a display, a controller and the like are mounted, thereby realizing constant temperature and humidity. When temperature inside the cabinet is higher than preset target temperature, the temperature control semiconductor high-temperature stacking generates forward current to reduce the temperature inside the cabinet; when temperature inside the cabinet is lower than the preset target temperature, the temperature control semiconductor high-temperature stacking generates reverse current to raise the temperature inside the cabinet to the preset target temperature; when humidity inside the cabinet is higher than preset target humidity, the dehumidification semiconductor high-temperature stacking generates forward current to reduce the temperature of a condensation block in the cabinet to be below the dew point, so as to enable moisture in the cabinet to condensate and flow into a water tank to realize dehumidification effect; and when humidity inside the cabinet is lower than preset target humidity, an ultrasonic wave humidifier sprays water mist to raise the humidity in the cabinet to the preset target humidity.

The invention relates to a method for preparing ethanol via hydrogenation of acetic ester based on recirculating of recovered hydrogen. The method comprises the steps of: recycling hydrogen in the gas phase of a product by using a pressure swing adsorption (PSA) device and then increasing the pressure for recirculating; heating the mixed gas of acetic ester, circulated hydrogen and fresh hydrogen by using reaction heat; heating the preheated raw material gas by medium-pressure steam and then importing into a reactor so as to realize high acetic ester conversion rate and high ethanol selectivity in the presence of a catalyst; and carrying out gas-liquid separation on the product gas obtained via the reaction, and liquefying and separating the reaction principal product ethanol, a small amount of byproducts and unreacted acetic ester to obtain an initial product. According to the method, hydrogen is recycled and recirculated via PSA so that the use of the raw material hydrogen can be greatly reduced, the reaction raw materials are preheated by fully utilizing the reaction heat so that the energy consumption of the heating and the cooling is decreased, the flow is simple and the control is simple and convenient.

The invention discloses a separation method for a reaction product of propane dehydrogenated propylene preparation and belongs to the field of petrochemical industry. The method comprises the following steps: (1) the reaction product of propane dehydrogenated propylene preparation is pretreated, then, the pretreated reaction product enters a propylene and ethylene cascaded refrigeration system with an expander, and then, a liquid phase is fed to a deethanizer; (2) top oil gas of the deethanizer is condensed and then enters a reflux tank of the deethanizer, tank bottom liquid of the reflux tank of the deethanizer totally returns to the deethanizer, tank top gas of the reflux tank of the deethanizer enters a top condensation section of the deethanizer and is fractionated by the condensation section, and top gas of the condensation section is condensed by a refrigerator of the top condensation section of the deethanizer under the action of a propylene refrigerating system and then enters a deep freezing tank of the deethanizer; (3) tank top gas of the deep freezing tank of the deethanizer is delivered out of a device as fuel gas, and bottom liquid of the deethanizer enters a propylene refiner; and (4) a refined propylene product is fractionated from the top of the propylene refiner, a bottom liquid phase of the propylene refiner enters a depropanizer, and a bottom product C4+ cut of the depropanizer is delivered out of the device. By adopting the separation method, the problems, i.e., large absorbent circulating rate and high energy consumption in the prior art can be solved.

The invention discloses a marine two-stage rotating-wheel dehumidifying air-conditioning system and an operating method thereof. The marine two-stage rotating-wheel dehumidifying air-conditioning system comprises a dehumidifying rotating wheel, a first-stage intercooler, a second-stage intercooler, a compression-type air-conditioner set, a humidifier, a processing fan and a regenerating fan whichare together connected in series. The adopted dehumidifying rotating wheel comprises a dehumidifying area, a regenerating area and a preprocessing area, and the preprocessing area is positioned between the regenerating area and the dehumidifying area of the dehumidifying rotating wheel. The waste heat of a ship is utilized as a heat source in the regenerating process of the dehumidifying rotatingwheel, and a waste-heat heater or a waste-gas heat-exchanging rotating wheel is adopted to heat regenerative air; and the dehumidified processed air is preliminarily cooled by utilizing seawater witha lower temperature. Because the preprocessing area is additionally arranged in the dehumidifying rotating wheel, the high-temperature high-humidity air remaining in the regenerating process of a dryer can be blown out of a rotating-wheel air passage at the preprocessing area, and the marine two-stage rotating-wheel dehumidifying air-conditioning system is favorable to the proceeding of the dehumidifying process at the dehumidifying area.

A process and apparatus for pressure purifying of trichlorosilane is disclosed. Said process includes such steps as distilling the mixed liquid of trichlorosilane, SiCl4 and chlorosilane at 70-200 deg.C under 0.15-1.5 MPa, sending the vapor derived from distilled into purifying tower for the exchange and separation of heat and components at 40-150 deg.C, enriching the low-boiling-point trichlorosilane in vapor phase and the high-boiling-point SiCl4 in liquid phase, evaporating and condensaing several times to obtain trichlorosilane vapor, and condensing to obtain liquid-phase trichlorosilane.

The invention discloses a recovery system and a recovery method of a by-product in polycrystalline silicon production. The system and the method are used for recycling the hydrogen, chlorosilane and chlorine hydride gas in the reducing tail gas produced during the polycrystalline silicon production. The recovery method comprises the following steps: a condensing step for separating most of chlorosilane from the reducing tail gas; an adsorption step for removing all chlorine hydride and the rest chlorosilane from the reducing tail gas by using an absorption unit after the condensing step to obtain the pure hydrogen; a regenerating step for regenerating the absorption unit by using the hydrogen so as to remove the chlorosilane and chlorine hydride absorbed by the absorption unit, and obtaining the regenerative gas containing hydrogen, chlorosilane and chlorine hydride; and a cold hydrogenating step for directly feeding the regenerative gas as the raw material of the cold hydrogenation reaction to a cold hydrogenation reactor. According to the system and method provided by the invention, the HCl can be singly separated from the tail gas without an adsorption-de-adsorption device so as to prevent the HCl from being condensedly separated and gasified, and a great number of heat and cooling capacity is saved.

A compact, countertop cooler for use in dispensing cold, energy-shot beverages at point-of-purchase retail locations. The cooler comprises a housing operative to store and selectively dispense individual containers of beverages through a gravity feed system. Preferably, the cooler will include an outwardly-facing window to facilitate the consumer's ability to see the contents and further, will preferably include a ratchet-type dispensing system to selectively dispense each beverage container individually so as to serve as an anti-theft mechanism, and further dispense at least one and preferably two containers of dissimilar size. The housing will further include a cooling system to provide cooling for the beverages and further, may be provided with decorative indicia to facilitate advertising and the display of product information.

The invention relates to an energy-saving gas washing process, comprising the following steps: subjecting raw gas to countercurrent contact with methanol in an absorbing column, and washing out acidic gas from the raw gas; delivering obtained carbon-rich methanol to the upper portion of a medium-pressure flashing column, and delivering rich methanol to the lower segment of the medium-pressure flashing column; delivering via an ejector, liquid carbon-rich methanol in the medium-pressure flashing column to the upper part of a re-absorbing column, and delivering sulfur-rich methanol at the bottom of the medium-pressure flashing column to the lower part of the re-absorbing column for flashing; returning two parts of liquid flashed from the upper part of the re-absorbing column respectively to the re-absorbing column and a negative-pressure flashing column; using flashed liquid rich methanol as main washing methanol, delivering flashed gas to a suction ejector, and delivering flashed sulfur-rich methanol to a subsequent heat regeneration system.

The invention discloses a method for separation of products of reaction for preparation of propylene from propane by dehydrogenation, and belongs to the field of petrochemical industry, by the way of combination of a propylene and ethylene cascade refrigeration process with an expansion machine and a deethanization process with a deethanizer top condensation section, the products of reaction for preparation of propylene from propane by dehydrogenation can be separated, propane can be obtained by fractional distillation on depropanizator top, and is used as a reaction cycle material flow to return to the part of the reaction for preparation of propylene from propane by dehydrogenation for further reaction, and a depropanizator bottom product C4 + fraction is sent out of a device. The method can overcome the problems of a large circulation amount of an absorbent and high energy consumption in the prior art.

The invention relates to a front-end deethanizing separation process method for an ethylene device. Liquid phase material flow from pyrolysis gas condensate drier is heated for evaporating in a condensate preheater by using chilled water at the evaporating temperature of between 25 and 35 DEG C, a small amount of evaporated gaseous phase material flow containing hydrogen, methane and carbon-2-components is merged with gaseous phase material flow formed by part of pre-cooled gaseous phase pyrolysis gas at the temperature of between -10 DEG C and -12 DEG C which flows into a plate heat exchanger directly from the pyrolysis gas drier, and the mixed material flow is conveyed to the plate heat exchanger to be pre-cooled; and after being subjected to throttling through a valve under the reducedpressure, condensate material flow from the bottom of the condensate preheater is heated again in the condensate heater by using the chilled water, and gas-liquid phase material flow at the temperature of between 45 and 65 DEG C is conveyed to the middle part of a deethanizing tower. Through the method, the low-pressure steam consumption of a reboiler at the tower bottom of the low-pressure deethanizing tower is reduced, the circulating water volume of the cooling chilled water is reduced, and the comprehensive energy consumption of ethylene per ton produced by the ethylene device is reduced by 125 to 190 MJ.

A process for preparing the plastic filter plate or plastic plate features that its mould is controlled by hydraulic press, its heat channel is positioned at the bottom of lower mould and communicated with said lower mould, and the plasticized plastics is injected in said mould via heat channel.

The invention provides a plant essence gradient extraction device, which comprises an evaporator with a built-in raw material bed layer, an exhaust pump, a gas condensing device, a circulating gas heating device and a product collecting tank, wherein the gas condensing device and the circulating gas heating device are formed by coupling a semiconductor cooling device; the cold side of the semiconductor cooling device serves as a gas condensing device and the hot side of the semiconductor cooling device serves as a circulating gas heating device; and the semiconductor cooling device is formed by connecting N stages of semiconductor cooling units in series; return crossing lines with valves are arranged at the cold side material outlet openings of the semiconductor cooling units from the 1st stage to the N-1th stage and are connected to the hot side material outlet openings of the semiconductor cooling units to regulate the temperature difference between the cold sides and the hot sidesof the semiconductor cooling units. Based on the requirements of the gradient extraction of the distillates of the plant essence, the device can provide cold energy and heat energy according to the required cooling and heating temperature, so that the device has high energy efficiency, is reasonable in energy utilization and low in cost.

The invention discloses neutralized crystallization system and method of preparing caprolactam through caprolactam rearrangement solution. The neutralized crystallization system is characterized in that a feeding mixer is connected with an inlet in the upper part of a neutralized crystallization reactor, an upper-layer organic phase outlet of the neutralized crystallization reactor is connected with an inlet of a caprolactam oil layer separator, a lower-layer heavy organic phase outlet of the neutralized crystallization reactor is connected with an inlet of an ammonium sulfate centrifugal machine, an outlet at one end of the caprolactam oil layer separator is connected with a caprolactam collecting tank, an outlet at the other end of the caprolactam oil layer separator is connected with an ammonium sulfate mother liquor collection tank, an outlet at the lower end of the ammonium sulfate centrifugal machine is connected with an ammonium sulfate washing dryer, an outlet at the upper end of the ammonium sulfate centrifugal machine is connected with the ammonium sulfate mother liquor collection tank which is connected with the neutralized crystallization reactor through a mother liquor circulating pump. The neutralized crystallization system and method have the advantages that the heating and cooling capacities are integrated in reaction process, the energy consumption is low, the process is simple, and the purity of the product is high.

The invention discloses a method for preparing deoiled wax. The method comprises the following steps: under a dewaxing condition, performing solvent dewaxing on a mixture of raw oil and a dewaxing diluting solvent to obtain dewaxed filtrate and dewaxed cerate; performing a first stage of solvent deoiling on a mixture of the dewaxed cerate and a first deoiling slurrying solvent at a temperature lower than a dewaxing temperature to obtain first-stage deoiled cerate and first-stage deoiled filtrate; performing a second stage of solvent deoiling on a mixture of the first-stage deoiled cerate and a second deoiling slurrying solvent at a temperature higher than the first-stage deoiling temperature to obtain second-stage deoiled cerate and second-stage deoiled filtrate; and performing a third stage of solvent deoiling on a mixture of the second-stage deoiled cerate and a third deoiling slurrying solvent at a temperature lower than the second-stage deoiling temperature to obtain third-stage deoiled cerate and third-stage deoiled filtrate. The method disclosed by the invention has the advantages of increasing the yield of deoiled wax and the yield of dewax oil on the premise of satisfying the standard requirements of oil content of the deoiled wax, reducing the amount of a used fresh solvent and reducing the energy consumption.

The invention discloses a solution total heat recovery and condensation dehumidification compound fresh air processing device, which comprises a return air processing system and a fresh air processing system, wherein a sensible heat exchange device is adopted, supply air with lower temperature is utilized for lowering the temperature of indoor return air, meanwhile, the supply air temperature of fresh air is also raised, and the fresh air can be directly supplied into a room. The state point of return air before entering a total heat recovery device approaches to a saturation line, the return air and the fresh air are subjected to total heat recovery in the solution total heat recovery device, the recovered energy of the return air is fully utilized, the input cold quantity of a cold source is reduced, and the energy efficiency of the fresh air processing device is improved. In addition, the fresh air processing device has the advantage that through work condition switching, the return air heat recovery and fresh air heating and dehumidification functions in winter can be realized.

The invention relates to a process and a device for distilling and separating isoamylol isomeride by a heat pump. The device comprises a distilling tower, the heat pump, a reboiler, a buffer tank, a driving heat exchanger and a reflux pump. The distilling tower is provided with a tower top vapor phase port and a tower top discharge outlet, the tower top vapor phase port is hermetically connected with an inlet of the heat pump through a pipeline, the reboiler is provided with a shell pass inlet, a shell pass outlet, a pipe pass inlet and a pipe pass outlet, the shell pass inlet is hermetically connected with the heat pump through a pipeline, the pipe pass inlet of the reboiler is hermetically connected with a tower bottom of the distilling tower, the pipe pass outlet is connected with a vapor phase port on the lower portion of the distilling tower through a pipeline, and the shell pass outlet is connected with the buffer tank. The bottom of the buffer tank is provided with a liquid phase discharge outlet which is connected with an inlet of the reflux pump. An outlet of the reflux pump is divided into two material flows, one is connected with a tower top reflux port of the distilling tower through a pipeline, and the other one is used as discharge on the tower top.

The invention discloses a fresh air treatment device for indirect evaporative cooling return air total heat recovery. The fresh air treatment device is composed of a sensible heat recovery device for supply air and return air, a return air total heat recovery device, an air treatment device and the like. The sensible heat recovery device is adopted for the fresh air treatment device, the supply air low in temperature is used for cooling the indoor return air, a state point of the return air is close to a saturation line before the return air enters the total heat recovery device, and therefore the total heat recovery process of fresh air and the return air is close to the saturation line, and the efficiency of the total heat recovery device is improved. Meanwhile, the supply air temperature of the fresh air is increased, and the fresh air can be fed indoors directly. Through the fresh air treatment device, recoverable energy of the return air is fully used, the input cooling capacity of a cold source is reduced, and the energy efficiency of the fresh air treatment device is improved. In addition, through working condition switching, the fresh air treatment device can have the functions of recovering heat of the return air and heating and humidifying the fresh air in winter.

The invention discloses a purification and separation method of a syngas by FTrPSA, and relates to the technical field of H2 production, CO production and purification and separation for a PSA gas. Compared with the prior art, the purification and separation method of the syngas by FTrPSA disclosed by the invention separates coarse removal and refined removal of impurities of acidic components and the like in the syngas purification process, an intermediate gas is refined by the syngas and subjected to an intermediate temperature PSA separation process to obtain a qualified syngas product or H2 and CO products, the operating temperature and operating pressure are the same as those of an intermediate temperature PSA concentration process, so that the load and energy consumption of the syngas in the refining and intermediate temperature PSA separation are reduced, the integration degree of purification and separation process and the purity of the produces are improved, furthermore, a concentrated gas is subjected to a membrane separation process to obtain further recycled syngas and remove the acidic components, so that the load of the membrane separation process is reduced and the yield of the products is improved.

The invention relates to a regeneration process for washing and spraying methanol by low-temperature methanol, which comprises the following steps of: spraying the methanol by virgin gas, cooling the virgin gas, carrying out gas-liquid separation on the virgin gas, carrying out flash evaporation on the methanol and a water condensate, reheating the methanol and the water condensate, rectifying and regenerating the methanol, carrying out flash evaporation on the methanol sprayed by the virgin gas and the water condensate by a flash tank, delivering the flashed vapor of the condensate into an H2S concentration tower, delivering into tail gas finally, carrying out heat exchange between the decompressed methanol, the decompressed water condensate and H2S gas at an outlet of an H2S distillate heat exchanger, delivering the reheated methanol and the reheated water condensate into a methanol water knockout tower for separation, delivering methanol gas at the top of the methanol water knockout tower into a methanol regeneration tower and carrying out rectification and regeneration. Compared with the prior art, the invention has the advantages of low energy consumption, low operating pressure of the heat exchanger, high concentration of H2S in acid gas and the like.

The invention discloses a natural gas pipe network pressure energy power generation and refrigeration house method and device. The device comprises an expansion power generation system and a coolant refrigeration system, wherein the expansion power generation system and the coolant refrigeration system realize power generation and refrigeration integration; the expansion power generation system is that high-pressure natural gas generates power through an expander, then exchanges heat with a coolant, and enters an urban gas pipe network; after exchanging heat with low temperature natural gas, the coolant in the coolant system passes through a distributor; and one stream is directly supplied to a high temperature refrigeration house, and the other stream is supplied to a low temperature refrigeration house after being throttled, so as to realize refrigeration house freshness retaining at different temperature levels. According to the device disclosed by the invention, the expander, a power generator and a compressor operate continuously, so that pressure energy of the pipe network is recycled for generating power and driving the compressor to rotate, externally required energy during independent use of the compressor is reduced, and cooling of two refrigeration houses at different temperature levels is realized; and the device has extremely high economical and social benefits.