33results about How to "Increase water vapor content" patented technology

The invention relates to a method for reducing emission of CO2 by circulating fluidized bed temperature flue gas circulation oxygen combustion, which is a method for realizing CO2 emission reduction applied in a circulating fluidized bed boiler based on the technology of temperature flue gas circulating oxygen combustion. The method comprises the following steps: feeding fuel and desulfurater into the circulating fluidized bed boiler, taking the gas mixture of O2 and circulating flue gas as combustion agent, passing through the heating surface at the tail by the flue gas generated by combustion, heating O2 (concentration is 96.5%-98.5%) from an air separation unit, generating temperature flue gas at the temperature of 140-150 DEG C, taking the gas mixture composed of 30%-70% of the temperature flue gas and O2 as oxidant to delivery to a furnace for combustion, carrying out dedusting by a deduster, multi-level condensation and dehydration and compression on the residual flue gas (volume concentration of CO2 is larger than 95%), and realizing resource utilization or storing in a sealing manner. The circulating glue gas is rich in vapor, entrainment unburned carbon and active desulfurater; the method enhances radiant heat exchange in the furnace, solves the problem of insufficient amount of convection heat transfer, improves combustion efficiency and desulfuration efficiency of the furnace, and can realize near-zero emission of gas pollutant; besides, the method can also lower comprehensive power consumption of space division and CO2 compression, and improve generating efficiency.

The invention relates to a seawater desalination process with low cost, which utilizes the condensate of the vapor cycle of a thermal power plant or a nuclear power station as a heat source, heats seawater to the temperature of 60-80 DEG C and atomizes the seawater in an atomizing chamber. On the other hand, natural air is heated after being washed and humidified, enters the atomizing chamber and contacts the atomized high-temperature seawater mist flow so as to enable part of the atomized high-temperature seawater mist flow to be instantaneously vaporized; fresh water mist droplets generated by the atomization of the high-temperature seawater are lifted by the kinetic energy of air to move upwards; moreover, because the density of water is different from the density of salt, the water and the salt are separated in the movement process; the two blasts of fresh water airflow are cooled by the raw material of cold seawater simultaneously and condensed into fresh water, the heated raw material of the cold seawater is used for washing and humidifying the natural air, and clean air carrying water vapor is recycled after the clean air carrying the water vapor is cooled; and the entire process flow does not consume extra heat energy and only consumes the air and less electric energy required by the transportation of the seawater. The process recovers energy in the condensate of the vapor cycle of the thermal power plant or the nuclear power station, produces the fresh water in large amounts and also produces a by-product of concentrated seawater.

Carbon monoxide (CO) is selectively reacted with hydrogen (H₂) over a ruthenium (Ru) on alumina catalyst at a temperature of about 210 to about 290° C. To be a viable option for micro catalytic fuel processing devices, highly active, selective, and stable catalysts must be demonstrated with as large a temperature window for feasible operation as possible. We have studied the effects of metal loading, preparation method, pretreatment conditions, and choice of support on the performance of Ru-based catalysts for such applications. Catalyst testing results and catalyst characterization using XRD and BET are discussed. In one example, operating at a gas hourly space velocity (GHSV) of 13,500 hr⁻¹, a 3% Ru/Al₂O₃ catalyst yielded CO outputs less than 100 ppm in a temperature range from 240° C. to 285° C., while not exceeding a hydrogen consumption of 10%. This catalyst was further successfully demonstrated in a microchannel device.

This invention relates to the recovery of energy in the manufacture of sulfuric acid, and more particularly to enhanced recovery of energy from the absorption of wet SO₃ in sulfuric acid. The invention is further directed to control of mist formation during SO₃ absorption, and of the sulfuric acid mist content of the gas stream leaving the SO₃ absorption step in a process wherein SO₃ absorption energy is recovered from absorption acid in useful form.

The invention relates to a flue gas desulfurization and desulfurization wastewater treatment method. According to the flue gas desulfurization and desulfurization wastewater treatment method, a flue gas pre-treatment tower comprises a flue gas/desalted water heat exchanger and a spraying unit; liquid-state desalted water is converted into gas-state desalted water by using flue gas in the flue gas/desalted water heat exchanger, and the gas-state desalted water enters a gas-liquid separator and is separated; the gas phase is compressed, the compressed gas phase enters the gas discharge cylinderon the top of a desulfurization tower to heat and purify the flue gas; the spraying unit is used for spraying a NaOH solution to reduce the flue gas temperature to below the dew point temperature of an acid, the cooled flue gas enters a bag type dust removing device and is treated, and the treated flue gas enters the desulfurization tower; and on the bottom of the desulfurization tower, a proper amount of desulfurization wastewater is subjected to spraying drying by using the flue gas, and the flue gas enters a desulfurization zone and is subjected to desulfurization purification. The invention further relates to a treatment apparatus of the treatment method. With the method and the apparatus of the present invention, the purified flue gas meets the discharge requirement, and the zero discharge of the flue gas desulfurization wastewater is achieved, the white smoke and the blue smoke are simultaneously eliminated, and the flue gas desulfurization and desulfurization wastewater comprehensive treatment cost is reduced.

The invention relates to a production technology of corn pulp addition fibers. The production technology sequentially comprises the following steps of separating corn fibers in a corn starch plant into dehydrated corn fibers and dehydrated fluid, conveying the dehydrated corn fibers into a first pipe bundle drier for first-stage drying, and controlling a product return ratio; after the first-stage drying, performing primary pulp addition with thick corn pulp, performing uniform mixing to obtain a first mixture, conveying the first mixture into a second pipe bundle drier for second-stage drying, and controlling a product return ratio; after the second-stage drying, performing secondary pulp addition with thick corn pulp, performing uniform mixing to obtain a second mixture, conveying the second mixture into a third pipe bundle drier for third-stage drying, and controlling a product return ratio; enabling discharged corn fibers after the third-stage drying, namely corn pulp addition fibers to enter a multi-stage countercurrent cooling tower for cooling; and respectively performing dust removal and residual heat recover on the high-quality tail gas of the first pipe bundle drier, the high-quality tail gas of the second pipe bundle drier, and the low-quality tail gas of the third pipe bundle drier, and gradually concentrating thin corn pulp into the thick corn pulp through recovered heat. The production technology of the corn pulp addition fibers disclosed by the invention is low in steam consumption and power consumption, high in drying efficiency and good in product quality.

The invention provides a refrigerator. The refrigerator comprises an inner container, an air supply fan, a storage container and an oxygen removal assembly; a storage chamber as well as an evaporator cavity and an air supply duct which are located on the back side of the storage chamber and used for containing an evaporator is formed in the inner container; the air supply fan is arranged in the air supply duct and is configured to promote formation of air flow circulating among the evaporator cavity, the air supply duct and the evaporator cavity; the storage container is arranged in the storage chamber; the oxygen removal assembly is arranged above the storage container and is provided with an electrolysis part which faces the outside of the storage container and is used for electrolyzing water vapor outside the storage container through electrochemical reaction and an oxygen consumption part which faces the inside of the storage container and is used for consuming oxygen through electrochemical reaction; and the air supply fan is further configured to continuously operate at the first preset rotating speed after a refrigeration system of the refrigerator completes refrigeration to supplement the storage chamber with the water vapor, so that enough water vapor can be provided for the oxygen removal assembly to serve as a reactant, and the electrolytic oxygen removal efficiency can be improved.

The invention relates to a cracking furnace tube for inhibiting catalytic coking of a hydrocarbon cracking furnace tube, and a manufacturing method thereof. The furnace tube comprises a substrate and an oxide film combined with the substrate, wherein the oxide film is an oxide film obtained by compounding three layers of oxides, the inner layer oxide near the substrate contains at least one selected from SiO2, CeO2 and Y2O3, the middle layer oxide comprises at least one selected from Cr2O3, FeO, Fe2O3 and NiO, the surface layer oxide comprises at least one selected from MnO and MnxCr3-xO4, and x is 0.5-1.5. The cracking furnace tube is manufactured by the following steps: carrying out a step-by-step heating treatment on a nickel-chrome alloy furnace tube material in low oxygen partial pressure gas, and generating an oxide film obtained by compounding three layers of oxides on the inner surface. According to the present invention, Fe content and Ni content in the oxide film of the cracking furnace tube are low, such that catalytic coking of the radiation-section furnace tube of the cracking furnace can be significantly inhibited when the cracking furnace tube is used for production of low carbon number olefin by the hydrocarbon cracking furnace tube.

The invention belongs to the field of chemical engineering and particularly relates to a process of a series quenching adiabatic fixed bed methanation reactor. The process comprises the following steps: (1) dividing synthesis gas passing through an ultra-fine reactor into N paths, enabling divided synthesis gas to enter the upper end of each catalyst bed layer of the reactor; (2) mixing fresh synthesis gas entering a section of catalyst bed layer with water vapor and circulating gas and then enabling the mixed gas to enter a section of bed layer; (3) mixing fresh synthesis gas entering the Mth section of catalyst bed layer with quenched gas coming from the outlet of the (M-1)th section of bed layer, and then enabling the mixed gas to enter the Mth section of catalyst bed layer; (4) pressurizing desalted water with a desalting water pump and then enabling the desalted water to enter the lower end of each bed layer of the reactor, wherein the desalted water can be used for quenching high-temperature gas at the outlet of each bed layer of the reactor.

The invention discloses an under-pressure oxygen-enriched circulating fluidized bed gasification process method and system. The system comprises a feed coal bunker, a screw feeder, a pressurized oxygen-enriched circulating fluidized bed gasifier and a deslagging belt, wherein the feed coal bunker is connected with a coal washer; a slag lock hopper is connected with a roller slag cooler; the deslagging belt is arranged beside the roller slag cooler; the top of a high-temperature cyclone separator is connected with the top of a gasifying agent preheater, the gasifying agent preheater is connected with a steam superheater, an economizer is connected with a cyclone dust collector, the cyclone dust collector is connected with a high-temperature filter body, and the high-temperature filter bodyis connected with a humidifying dust removal tower. According to the under-pressure oxygen-enriched circulating fluidized bed gasification process method and system, a novel structural design is adopted, so that the process flow is simple, the gasification pressure is easy to improve, the system operation cost and the investment cost are low, the dust removal efficiency is high, and the content ofwater vapor in produced coal gas is high.

The invention belongs to the technical field of distributed energy and air conditioning, and discloses a PEMFC combined supply fresh air purification, dehumidification and humidification device and a control method thereof.In the PEMFC combined supply fresh air purification, dehumidification and humidification device, the fresh air purification and humidification device is provided with a box body, a shaft is installed in the box body through a shaft hole, the shaft penetrates through a heat insulation and preservation material, and the heat insulation and preservation material is arranged in the box body; one end is connected with the motor; fins are arranged on the upper side of the heat insulation material and coated with an MOFs adsorption material; the upper side of the box body is provided with an upper half air inlet and outlet, and the lower side of the box body is provided with a lower half air inlet and And the fresh air purifying and humidifying device is connected with the first heat exchanger. The PEMFC provides electric quantity needed by the device and heat needed by solid adsorbent regeneration, and compared with a traditional fresh air dehumidification device, the situation that cold and heat are counteracted can be effectively avoided, the unit cost is effectively reduced, and the purposes of energy conservation and environment protection are achieved; the application requirements of the solid adsorbent can be met.