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WO2018068765A1 - 一种有害气体净化剂及其制备和净化方法 - Google Patents

一种有害气体净化剂及其制备和净化方法 Download PDF

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Publication number
WO2018068765A1
WO2018068765A1 PCT/CN2017/106121 CN2017106121W WO2018068765A1 WO 2018068765 A1 WO2018068765 A1 WO 2018068765A1 CN 2017106121 W CN2017106121 W CN 2017106121W WO 2018068765 A1 WO2018068765 A1 WO 2018068765A1
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Prior art keywords
sulfate
carbonate
hydroxide
gas
basic
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PCT/CN2017/106121
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English (en)
French (fr)
Inventor
黄华丽
黄立维
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Priority claimed from CN201610901765.1A external-priority patent/CN106474910A/zh
Priority claimed from CN201610906056.2A external-priority patent/CN106474911A/zh
Priority claimed from CN201610906058.1A external-priority patent/CN106377997A/zh
Priority claimed from CN201610939180.9A external-priority patent/CN106474889A/zh
Priority to JP2019519365A priority Critical patent/JP7120650B2/ja
Priority to CA3038760A priority patent/CA3038760C/en
Priority to US16/336,099 priority patent/US11911740B2/en
Application filed by Individual filed Critical Individual
Priority to CN201780010197.9A priority patent/CN109715269B/zh
Priority to AU2017344205A priority patent/AU2017344205B2/en
Publication of WO2018068765A1 publication Critical patent/WO2018068765A1/zh
Anticipated expiration legal-status Critical
Priority to US18/332,712 priority patent/US12478945B2/en
Ceased legal-status Critical Current

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Definitions

  • the invention relates to a harmful gas purifying agent and a preparation and purification method thereof, and belongs to the technical field of air pollution control and related environmental protection.
  • Nitrogen oxides and sulfur dioxide are toxic to humans, and a large amount of nitrogen oxides and sulfur dioxide emissions are one of the main causes of atmospheric photochemical fog and acid rain.
  • Statistics show that the contribution of nitrogen oxides in urban acid rain is increasing. In recent years, the state has newly enacted some new laws and regulations to make more relevant pollutants emitted by combustion processes such as nitrogen oxides and sulfur dioxide, especially thermal power. Strict control and emission reduction regulations.
  • the concentration of nitrogen oxides in flue gas generated by combustion of fossil fuels in a thermal power plant or the like is about several hundred to several thousand ppm, and more than 90% of them are nitric oxide.
  • selective catalytic conversion is one of the main methods for controlling NOx in flue gas or exhaust gas of the fossil fuel.
  • the catalyst requires strict operating conditions, and ammonia or urea is required as a reducing agent.
  • the gas stream contains sulfide and dust. It has a great influence on the life of the catalyst, especially for coal-fired thermal power plants.
  • the wet method uses various liquids to absorb NOx, which is the main treatment method for low-temperature emission sources, but Exhaust gas with more nitrogen oxides has low solubility due to the low solubility of nitric oxide in solution.
  • the method of oxidizing or reducing absorption requires consumption of related chemicals, and the operating cost is high.
  • Hazardous substances such as nitrogen oxides, sulfur dioxide, carbon monoxide and hydrocarbons emitted by exhaust gas from automobiles and ships, which are powered by internal combustion engines, are one of the main causes of atmospheric haze. With the increasing amount of car reservations, the resulting air pollution problem is becoming more and more serious. In particular, the treatment of pollutants such as nitrogen oxides emitted from exhaust gas using diesel internal combustion engines is difficult and costly. At present, most of the processing technologies are concentrated on the catalytic reduction of nitrogen oxides. Therefore, research and development of new fuel combustion flue gas or exhaust gas purification technology such as nitrogen oxides in exhaust gas is an urgent problem to be solved in industrial applications.
  • the object of the present invention is to provide a harmful gas purifying agent and a method for preparing and purifying the same, which are used for removing harmful gases such as nitrogen oxides, sulfur dioxide, carbon monoxide and hydrocarbon VOCs, respectively, from a gas stream.
  • the primary technical problem to be solved by the present invention is to provide a harmful gas purifying agent (hereinafter referred to as a purifying agent) and a preparation method thereof for separately or simultaneously removing nitrogen oxides, sulfur dioxide, carbon monoxide and hydrocarbon VOCs from a gas stream. Such as harmful gases, with high activity and high removal efficiency.
  • a purifying agent a harmful gas purifying agent
  • Another technical problem to be solved by the present invention is to provide a purification method and apparatus for the above-mentioned purifying agent, which has the characteristics of simple operation, high processing efficiency, large processing amount, and low running cost.
  • a purifying agent comprising one or any two or more elements of A component iron, cobalt, manganese or copper; B component hydroxyl or water One or two of the components C; one or any two or more elements of sodium, potassium, lithium, calcium, barium or magnesium; one or both of the components D, sulfate, chlorine or carbonate and Above or; a solid compound or a mixed compound composed of E-component oxygen, the E-component oxygen does not contain sulfate, carbonate, hydroxyl, and oxygen in water, wherein the mass percentage of each component is A-component 4-96 %, B component 1-75%, C component 1-75%, D component 1-75%, E component 0-35%.
  • the main function of the removal of nitrogen oxides is iron or manganese or cobalt or copper elements and their hydroxy compounds or oxides or corresponding composite compounds contained in the compounds, sodium, potassium and lithium are brought in when the materials are added, It can play a certain catalytic role in the purification of purifying harmful substances.
  • Calcium, barium and magnesium and their oxides or hydroxy compounds or related salts can be used as a forming agent and a component for adsorbing harmful substances, and the oxygen contains oxygen in the metal oxide. And oxygen in the oxy compound.
  • a preparation method of the above-mentioned purifying agent which is characterized in that the material A, the material B and the water (the A is a liquid crystal solid with no water, no water or less water, the same below) is mixed in a certain proportion in the reactor
  • the materials A, B and water described in this process react (depending on the different materials to be heated to accelerate the reaction), the above mixing reaction process is generally an exothermic process, so that the material has a certain temperature rise.
  • the obtained product is dried and activated, and the obtained solid product is a purifying agent of the present invention.
  • material A is ferrous (II) or iron (III), manganese (II), cobalt (II), copper (I) or copper (II) sulfate, chloride (hydrochloride), One or any combination of two or more of carbonates, nitrates or nitrites, organic acid salts, mainly ferrous sulfate and ferric sulfate, ferrous chloride and ferric chloride, ferrous carbonate and iron carbonate , ferrous nitrate and ferric nitrate, ferrous acetate and iron acetate, manganese sulfate, manganese chloride, manganese carbonate, manganese nitrate, manganese acetate, cobalt sulfate, cobalt chloride, cobalt carbonate, cobalt nitrate, cobalt acetate, copper sulfate, Copper chloride, copper carbonate, copper nitrate and copper acetate.
  • the material A may also be one or any combination of two or more materials corresponding to the salt including a basic or acid or double salt and a related derivative compound such as a polymer or a coordination compound, mainly ferrous sulfate.
  • Feed A is preferably related to the sulfates, chlorides and carbonates and related derivatives thereof.
  • Material B is one or a combination of two or more materials of an alkali or a basic substance or a related derivative, and is mainly composed of alkali metal hydroxides and carbonates, alkaline earth metal hydroxides, oxides and carbonates. And related acid salts, basic salts, double salts, polymeric compounds, coordination compounds, and ammonium hydroxide (ammonia).
  • the hydroxide mainly comprises sodium hydroxide, potassium hydroxide, lithium hydroxide, calcium hydroxide, barium hydroxide, magnesium hydroxide and ammonia water
  • the oxide mainly comprises calcium oxide, barium oxide and magnesium oxide.
  • the carbonate is mainly sodium carbonate or sodium hydrogencarbonate, Potassium carbonate or potassium hydrogencarbonate, lithium carbonate or lithium hydrogencarbonate, calcium carbonate or calcium hydrogencarbonate or basic calcium carbonate, barium carbonate or barium hydrogencarbonate, magnesium carbonate or magnesium hydrogencarbonate or basic magnesium carbonate, ammonium carbonate or hydrogencarbonate Ammonium or aluminum magnesium carbonate.
  • the material B is preferably an alkali metal hydroxide and a carbonate, an alkaline earth metal hydroxide and an oxide. When the material B is ammonia or an ammonium salt, the material is easily decomposed by heating, and generally should be combined with other compounds or materials in the material B. The agent is used together.
  • the drying method of the present invention can adopt heating mode, and the heating temperature is generally 40° C. or higher, preferably 60° C.-450° C., the maximum temperature can be the same as the activation temperature, and the heating can be performed under the condition of negative pressure or vacuum, and the heating time can be shorter.
  • the separated moisture in the material is about 10% or less.
  • the activation is carried out at a certain temperature, generally above 100 ° C, preferably from 150 ° C to 750 ° C, up to 1200 ° C or more, depending on the type of material, the general material contains iron and cobalt elements, activated
  • the temperature can be higher, and the activation temperature of the cleaning agent based on manganese or copper can be lower.
  • the decomposition temperature of the alkali metal and alkaline earth metal is higher than the activation temperature, and the activation temperature of the product containing chloride, carbonate, ammonium salt or nitrate in the material may exceed the decomposition temperature of the salt, and the corresponding salt is decomposed. Converted to oxides. Drying and activation can be carried out in one step at the same time, or in steps, with comparable results.
  • the product may be pre-compressed and then dried and activated, and a certain amount of a molding agent may be added.
  • the product contains more water and is not easily formed, a certain amount of the molding agent is added, and after preliminary drying (general The moisture is about 15-30%) and then press-molded to form various shapes such as honeycomb, plate or granules, and then further dried and activated. Drying and activation can be carried out under inert gas such as air or nitrogen or under negative pressure, or in the presence of reducing agent to reduce the oxidation of low-valent metals in the product.
  • the reducing agents are mainly hydrocarbons such as hydrogen and methane. Carbonic acid hydroxide such as formaldehyde, ammonia, carbon monoxide and nitrogen monoxide have the same effect.
  • the product is allowed to reach the set temperature as a whole, and is maintained for a period of time.
  • the gas component in the gas stream is no longer changed, the activation is completed, and the obtained solid product is a kind of the present invention.
  • the purifying agent has no special requirement for the amount of the reducing agent to be added, and the reducing dose is small, and the activation time is longer.
  • the heating can be carried out by various heating means such as electric furnace, heat conducting medium, electromagnetic and microwave, and the effect is equivalent.
  • the preparation method of the above-mentioned purifying agent characterized in that one or two or more kinds of sulfate or chloride or carbonate of the material A are combined, sodium hydroxide or potassium hydroxide or hydrogen in the material B
  • the product obtained by reacting one or two or more kinds of lithium oxide and water after mixing is obtained by drying and activation, and the effect of using different materials B is substantially equivalent.
  • the hydroxide is excessive in the material, the sodium hydroxide, potassium hydroxide or lithium hydroxide that does not participate in the reaction tends to melt when the heating and activation temperature is high.
  • the lithium hydroxide has the highest melting point and hydrogen. Potassium oxide is the second, sodium hydroxide is the lowest, and the melting of the material has little effect on the performance of the prepared scavenger.
  • the preparation method of the above-mentioned purifying agent characterized in that one or two or more kinds of sulfate or chloride or carbonate of the material A are combined, calcium hydroxide, calcium oxide and hydroxide in the material B are A product obtained by reacting one or any combination of two or more kinds of cerium, cerium oxide, magnesium hydroxide and magnesium oxide with water, obtained by drying and activation, and using the material B in the obtained purifying agent
  • the effect of the calcium and barium compounds as materials is good.
  • a sulfate or a chloride or a carbonate of the material A is used.
  • the reaction molar ratio of the material A and the material B according to the present invention is about 1:0.5-1:3, which varies depending on the metal valence of the material.
  • the molar ratio of the actual materials to the addition is not particularly required, and is generally 1:0.1 or more, preferably 1:0.3 to 1:10.
  • the material A may also be one or any of the related derivative compounds including the basic or acid or double salt and the polymer or the coordination compound.
  • Two or more material compositions mainly ammonium ferrous sulfate, ammonium ferrous chloride, basic ferric sulfate, basic ferric chloride, oxy basic ferric sulfate, ferric ammonium sulfate, cuprous sulfate, chloride Copper, basic copper sulfate, basic copper chloride, copper ammonium sulfate, copper ammonium chloride, basic manganese sulfate, basic manganese chloride, ammonium manganese sulfate, ammonium manganese chloride, basic cobalt sulfate, basic chlorine Cobalt, ammonium cobalt sulfate, ammonium cobalt chloride, polyferric aluminum sulfate, polyaluminum ferric chloride, potassium iron sulfate,
  • the material B can also be replaced by a corresponding carbonate, including an acid or basic or multiple carbonate, and a polymer and a coordination compound such as sodium carbonate or hydrogen carbonate.
  • a corresponding carbonate including an acid or basic or multiple carbonate, and a polymer and a coordination compound such as sodium carbonate or hydrogen carbonate.
  • the preparation method is the same as the above, wherein when the material B is an acid salt, it should be used together with other alkaline materials or paired with the basic salt in the material A.
  • the carbonate in the carbonate has a less effective effect on the reaction with the material A.
  • the preparation method of the purifying agent of the present invention may also be composed of the metal element iron or manganese of the material A or the hydroxide of cobalt or copper and related coordination compounds, including ferrous hydroxide, iron hydroxide and manganese hydroxide.
  • the sulfate includes sodium sulfate, potassium sulfate, lithium sulfate, calcium sulfate, barium sulfate, and magnesium sulfate
  • the chloride includes sodium chloride, potassium chloride, lithium chloride, calcium chloride, barium chloride, and magnesium chloride.
  • the carbonate includes sodium carbonate, potassium carbonate, lithium carbonate, calcium carbonate, barium carbonate, magnesium carbonate, etc., and the acid or base or double salt and the polymer compound mainly have sodium hydrogen sulfate and potassium hydrogen sulfate.
  • lithium hydrogen sulfate, calcium hydrogen sulfate, barium hydrogen sulfate and magnesium hydrogen sulfate sodium hydrogencarbonate, potassium hydrogencarbonate, lithium hydrogencarbonate, calcium hydrogencarbonate, barium hydrogencarbonate and magnesium hydrogencarbonate, basic calcium carbonate, basic magnesium carbonate And potassium iron sulfate and the like.
  • the hydroxide of the metal element of the material A and the related coordination compound material and the sulfate, chloride, carbonate and the corresponding acid or base or double salt or polymer or coordination compound Dosing
  • the metal salt of the material B should generally be used together with the alkali or alkaline material when the acid salt is used.
  • the preparation process is the same as described above, and is obtained after drying and activation. Among them, the purification effect of the obtained purifying agent is slightly inferior to the above-mentioned scavenger prepared by the corresponding materials A and B.
  • the material is a crystalline water solid, no water or less water may be added.
  • the metal element of the material A may also be replaced by a corresponding carbonate or basic or basic or basic chloride, including ferrous carbonate and iron carbonate.
  • manganese carbonate, cobalt carbonate, basic cobalt carbonate, copper carbonate, basic copper carbonate, basic iron sulfate or polyferric chloride, basic oxysulfate, basic copper sulphate or basic copper chloride, basic Materials such as manganese sulfate or basic manganese chloride, basic cobalt sulfate and basic cobalt chloride, and other preparation processes are the same as described above.
  • the purifying effect of the prepared purifying agent is substantially equivalent to the purifying agent obtained by the above preparation.
  • the materials may be replaced by a combination of related materials.
  • the various salts or hydroxides of the material A may be replaced by a ratio of a corresponding metal or an oxide or a salt thereof (including organic and inorganic) to a solution such as hydrochloric acid, sulfuric acid and alkali, such as ferrous sulfate or may be iron or oxidized.
  • the ferrous iron or ferrous sulfide is reacted with dilute sulfuric acid;
  • the manganese chloride can be obtained by reacting manganese oxide with hydrochloric acid;
  • the ferric chloride can be obtained by reacting iron phosphate with hydrochloric acid, and then adding calcium hydroxide to filter off the clear water layer.
  • the iron hydroxide is obtained; the alkali metal hydroxide in the material B can also be obtained by reacting the corresponding metal oxide with water, and the alkaline earth metal oxide can be obtained by decomposing a compound such as the corresponding carbonate.
  • the effect of the purifying agent prepared after the combination of the above materials is replaced by the corresponding material is the same as the above preparation method.
  • the same type of materials may be used in combination or in combination, and the effect of the obtained product is substantially equivalent.
  • the main action of the added water enables the material to be wet, and the materials are thoroughly mixed and reacted, and the amount of the addition has no special requirement, generally 1 of the total amount of the materials. Up to 20 times (molar ratio), preferably 3-10 times, adding a large amount of water, the drying and dehydration process consumes a large amount of energy, and when the material is a crystalline water solid, no water or less water is added.
  • the mixing reaction is carried out in the liquid phase of the aqueous solution; when the material A is the organic acid salt, the nitrate salt or the nitrite solid, the material A should be dissolved in the water first.
  • the metal hydroxide solid precipitate of the material A is obtained, and the clear water layer is filtered (may also be washed several times) to remove ammonium, nitrate, nitrite, acetate and the like in the solution, and then After the addition of the molding agent, the cleaning agent described in the present invention can also be obtained by drying and activating according to the aforementioned preparation process.
  • the materials such as carbonate
  • the effect of the obtained purifying agent is the same as the preparation method described above.
  • a certain amount of a molding agent may be added to the material, and the molding agent includes oxides, hydroxides, sulfates and carbonates of alkaline earth metals in the material B. And all related derivatives (including acid or basic or polymeric compounds or double salts or coordination compounds, etc.), as well as clays and silicates (such as calcium silicate, magnesium silicate or aluminum silicate)
  • the main purpose is to absorb moisture in the product and easy to form, and can play an auxiliary adsorption.
  • the dosage of the molding agent can be added simultaneously with each material, or in the mixing reaction of the materials.
  • the dosage is determined according to the need, generally 1-85% of the total volume of the material, and other preparation processes are basically the same as the foregoing.
  • the purifying agent can be preformed into a shape such as a sphere, a plate or a honeycomb ceramic, and the preparation process is similar to the preparation of an industrial catalyst or an adsorbent. For details, refer to the relevant chemical manual.
  • one or any combination of two or more metals of iron, manganese, cobalt, copper or the like in the material A may be added to the material as a compounding agent.
  • the compounding agent generally accounts for less than 95% of the total mass of the purifying agent, and the compounding agent generally does not participate in the reaction in the preparation process of the purifying agent, and can play a certain catalytic role in removing harmful gases in the gas stream. Among them, the effect of adding the oxide of the relevant material is good.
  • a certain amount of organic solvent may be added before the drying and dehydration and activation process of the material, mainly acetone, methyl ethyl ketone, ethanol or propanol, etc., the addition amount has no special requirement, the volume ratio Generally, it is 1:1 or less, stirred and mixed, and the solvent is volatilized after heating, thereby increasing the specific surface area of the purifying agent and improving the purification efficiency of the purifying agent.
  • transition element oxide such as titanium dioxide, tungsten trioxide, vanadium pentoxide, rare earth or palladium, platinum or the like may be added as a catalytic auxiliary in the material, and the transition metal oxide may be added.
  • the rare earth mass content is generally less than 10%
  • the precious metal is generally less than 0.5% to promote the adsorption and conversion of harmful substances such as nitrogen oxides, sulfur dioxide, carbon monoxide and VOCs in the gas stream, and the effects of these metal oxides or precious metals are substantially equivalent.
  • the purifying agent may also be supported on a carrier of a general-purpose catalyst such as alumina particles and honeycomb ceramics, and the preparation process is also similar to the preparation of the related catalyst.
  • a general-purpose catalyst such as alumina particles and honeycomb ceramics
  • the purifying agent purifying method of the present invention is to introduce the purifying agent obtained by the above preparation method into a gas-solid reactor purifying device, in which the nitrogen gas, sulfur dioxide, carbon monoxide and VOCs contained in the gas stream are respectively harmful.
  • the substance and the scavenger are removed by various reactions such as adsorption, absorption, and redox, thereby achieving gas purification purposes.
  • the nitrogen oxides are adsorbed and purified by the purifying agent, the sulfur dioxide is adsorbed and absorbed by the purifying agent to be purified, and the carbon monoxide and VOCs are catalytically oxidized to be purified.
  • the temperature of the gas stream is high (greater than 300 ° C)
  • the removal of nitrogen oxides and VOCs is dominant.
  • the sulfur dioxide in the gas stream can be removed while removing the nitrogen oxides, and the sulfur dioxide is removed and purified.
  • the amount of material B added is related to the amount of addition, and the removal rate of sulfur dioxide is high.
  • the gas-solid reactor of the present invention can adopt a gas-solid contact reactor such as a fixed bed, a moving bed, a fluidized bed, a fluidized bed and a circulating fluidized bed which are commonly used in chemical unit operations, and can adopt a forward flow, a reverse flow and a wrong flow.
  • a gas-solid contact reactor such as a fixed bed, a moving bed, a fluidized bed, a fluidized bed and a circulating fluidized bed which are commonly used in chemical unit operations, and can adopt a forward flow, a reverse flow and a wrong flow.
  • the relevant reactor structure can refer to the relevant chemical equipment manual.
  • a circulating fluidized bed gas-solid reactor harmful gas purification device wherein the gas-solid reactor is provided with a gas inlet connected to the gas flow in the lower portion of the cylinder, and a purifying agent particle is arranged in the middle portion.
  • the method of adding the purifying agent particles may be mechanical feeding or pneumatic feeding, and the effect is equivalent.
  • a gas flow distributor is arranged above the lower gas inlet of the cylinder, so that the gas solid in the reactor is fully mixed and contacted.
  • the upper part of the body is provided with a connecting pipe, and the airflow is communicated with the gas-solid separator through the connecting pipe.
  • the purified gas stream is discharged from the upper part of the gas-solid separator, and the purifying agent particles are gas-extracted.
  • the lower part of the solid separator is discharged, and some of the purifying agent can be returned to the reactor to participate in the reaction (or not Return), specifically, according to the degree of reaction, the proportion of the materials in the return cylinder to participate in the reaction can be adjusted (the range can be 0-100%).
  • a countercurrent moving bed gas-solid reactor harmful gas purifying device comprises a cylinder body, a gas inlet is arranged at a lower portion of the cylinder body, a purifying agent inlet port and a gas outlet are arranged at the upper portion, and a purifying agent is arranged at the bottom portion.
  • the gas outlet is connected to the gas outlet through the gas-solid reaction zone in the cylinder, and the purifying agent is connected to the gas-solid reaction zone and the purifying agent recovery zone of the mouth through the cylinder to communicate with the purifying agent particle discharge port.
  • the treatment process is that the gas stream to be treated is introduced into the reactor from the gas inlet and the purifying agent added by the purifying agent inlet port is subjected to gas-solid adsorption and redox reaction in the gas-solid reaction zone, and the purified gas stream is discharged from the gas outlet, and the reaction is carried out.
  • the post-solid particles are discharged through the purifying agent discharge port after passing through the solid scavenger recovery zone.
  • a fixed bed gas-solid reactor harmful gas purifying device comprising a cylinder body, a gas inlet is arranged at a lower portion of the cylinder body, a gas flow distributor is arranged above the gas inlet, and a purifying agent is filled above the gas flow distributor
  • the upper part of the cleaning agent filling layer is provided with a purifying agent inlet port
  • the lower part is provided with a purifying agent discharging port
  • the upper part of the barrel body is further provided with a gas outlet
  • the gas inlet passes through the air gap distributor and the purifying agent filling layer of the gap gas passage and the gas outlet
  • the purifying agent inlet and the purifying agent outlet are respectively connected to the purifying agent filling layer.
  • the treatment process is to introduce a gas stream of a harmful gas such as nitrogen oxides to be treated from a gas inlet through a gas flow distributor into a purifying agent filling layer, in the purifying agent filling layer, a harmful gas such as nitrogen oxides and a purifying agent.
  • a harmful gas such as nitrogen oxides and a purifying agent.
  • the gas-solid adsorption and redox reactions are removed, and the purified gas stream is discharged from the gas outlet at the upper portion of the reactor, and the purified purifying agent can be periodically discharged from the purifying agent discharge port.
  • the purification temperature range of the purifying agent of the invention is generally above 60 ° C, the highest purification temperature is the same as the highest activation temperature of the purifying agent, preferably the temperature range is from 200 ° C to 500 ° C, generally using a purifying agent containing iron or cobalt.
  • the purification temperature is higher, and the purification temperature containing manganese and copper is lower. If the temperature of the gas stream entering the gas-solid reactor is lower than 60 ° C, the temperature of the purifying agent is preheated to above 100 ° C in advance, so that the purifying agent is activated and then added to the gas-solid reactor.
  • the gas-solid contact time of the nitrogen oxide in the reaction process in the reactor is generally 0.05 s or more, the contact time is long, and the removal rate is high, preferably 0.2 s to 20 s.
  • the molar ratio of adsorption and reaction with nitrogen oxides and sulfur dioxide is calculated by the metal content in the material A, which is about 1:0.5-1:2, and is also related to the material B and the structure of the purifying agent, and the actual operation process is purified.
  • the dosage of the agent can be determined after actual testing according to different purifying agent characteristics, gas flow temperature, gas-solid contact time and removal rate requirements.
  • the molar ratio of the purifying agent to the nitrogen oxide is generally 1 or more, and the larger the molar ratio, the better the removal effect of the nitrogen oxides, but the energy consumption is increased, preferably 5-100.
  • reactors such as fixed bed, moving bed and ebullating bed, there are no special requirements, and they are added as needed.
  • the particle size and structure of the purifying agent can be selected according to different reactors, and a solid particle purifying agent can be used for fluidized bed, moving bed and bubbling bed, and the particle size is selected according to the chemical design manual of the corresponding reactor, generally 0.01 mm. -20mm, the fixed bed can be formed into a spherical, flat or honeycomb ceramic shape, and the size can be prepared and selected according to the size of the reactor structure.
  • the purifying agent of the present invention uses the compound of manganese or copper in the material A to have the best effect, and the iron or cobalt is slightly inferior.
  • the gas stream contains a relatively high concentration of carbon dioxide, it is preferred to use a product prepared from carbonate as a material to reduce the associated effects.
  • the used purifying agent can be regenerated by a gas-solid desorption and reduction reaction at a certain temperature, and the regeneration can generally be in the air or It can be carried out in an inert gas such as nitrogen or under a negative pressure, or it can be regenerated in the presence of a reducing agent.
  • Hydrogens such as hydrogen, methane, carbonic acid hydroxide such as formaldehyde, ammonia, carbon monoxide and nitrogen monoxide are used in the reduction.
  • the effect of the agent is roughly equivalent.
  • the regeneration temperature is usually 150 ° C or higher, and may be lower under a negative pressure.
  • the maximum temperature is equivalent to the purification agent activation temperature, and may be higher than the activation temperature, preferably 450 ° C to 850 ° C.
  • the regeneration temperature of the iron-containing and cobalt-purifying agents can be higher, and the regeneration temperature of the manganese-containing and copper-purifying agents can be lower.
  • the purifying agent after adsorbing nitrogen oxides alone can be regenerated by gas-solid desorption, and the regeneration temperature of the purifying agent after absorbing sulfur dioxide can be higher, and is generally regenerated by a reduction reaction.
  • the airflow according to the present invention is mainly a flue gas containing harmful gases such as nitrogen oxides and sulfur dioxide generated by combustion of fossil fuels, such as thermal power generation, building materials and smelting, including mobile source exhaust gases of various types of motor vehicles and marine internal combustion engines, and the like. Relevant airflow generated by industrial processes.
  • the invention has the advantages that: the purifying agent is subjected to gas-solid adsorption and redox reaction with harmful substances such as nitrogen oxides in the gas stream at a certain temperature, and the nitrogen gas contained in the gas stream is separately or simultaneously contained. Various harmful substances such as substances, sulfur dioxide and VOCs are removed to achieve gas purification purposes, and the purification agent can be used in the regeneration cycle after the reaction.
  • FIG. 1 is a schematic view showing the structure of a harmful gas purification device for a circulating fluidized bed gas-solid reactor.
  • FIG. 2 is a schematic view showing the structure of a countercurrent moving bed gas-solid reactor harmful gas purifying device.
  • FIG 3 is a schematic view showing the structure of a harmful gas purification device for a fixed bed gas-solid reactor.
  • the invention is further described in detail below with reference to the accompanying drawings and embodiments.
  • the examples are illustrated by using the ferrous sulfate compound in the material A, and other similar compounds in the material A are exemplified.
  • the material B is represented by an alkali metal hydroxide or an alkaline earth metal oxide and hydroxide, and other compounds in the material B are exemplified.
  • Embodiment 1 A method for preparing the purifying agent: adding ferrous sulfate, sodium hydroxide and water to a mixing reactor at a ratio of about 1:0.1:2 (molar ratio, the same below), so that the materials are uniformly mixed. After the reaction is completed (about 10-30 minutes, the same material, the materials are different), dried and activated in the air, the drying temperature is about 40-60 ° C, the time is about 3 hours, the moisture in the material is removed, then The activation is carried out at an activation temperature of about 100 ° C. When the gas component in the gas stream is no longer changed, the activation is completed, and the obtained solid product is a purifying agent according to the present invention.
  • Embodiment 2 A preparation method of the purifying agent: adding cobalt sulfate heptahydrate and sodium hydroxide to a mixing reactor at a ratio of about 1:1, and after the reaction is completed, drying and activating in air, heating temperature It is 60-95 ° C, the time is about 2 hours, the moisture in the material is removed, and then activated, the activation temperature is about 150 ° C. When the gas component in the gas stream is no longer changed, the activation is completed, and the obtained solid product is A cleaning agent according to the invention.
  • Embodiment 3 A method for preparing the purifying agent: adding ferrous sulfate heptahydrate and sodium hydroxide to a mixing reactor at a ratio of about 1:2 to uniformly mix the materials, and drying in nitrogen after the reaction is completed. And activation, drying temperature is about 250 ° C (including activation), time is about 2 hours, when the gas component in the gas stream is no longer changed, drying and activation is completed, the obtained solid product is a kind of the present invention purifier.
  • Embodiment 4 A method for preparing the purifying agent: adding manganese sulfate tetrahydrate and lithium hydroxide to a mixing reactor at a ratio of about 1:3, stirring and mixing, and drying and activating in nitrogen after the reaction is completed.
  • the drying temperature is about 60-95 ° C
  • the time is about 2 hours
  • the water in the material is volatilized and then activated
  • the activation temperature is about 350 ° C.
  • the solid product is a purifying agent according to the invention.
  • Embodiment 5 A method for preparing the purifying agent: adding copper sulfate pentahydrate and potassium hydroxide to a mixing reactor at a ratio of about 1:2 to uniformly mix the materials, and after drying, drying in air and Activation, drying temperature is about 450 ° C (including activation), time is about 1 hour, when the gas component in the gas stream no longer changes, drying and activation is completed, the obtained solid product is a purification according to the present invention Agent.
  • Embodiment 6 A preparation method of the purifying agent: adding ferrous sulfate heptahydrate, sodium carbonate and water to a mixing reactor at a ratio of about 1:1:2, stirring and heating appropriately, after the reaction is completed, obtaining The solid product is dried and activated in nitrogen at a temperature of about 60-95 ° C for about 2 hours and an activation temperature of about 450-500 ° C. When the gas component in the gas stream is no longer changed, the activation is completed.
  • the solid product obtained is a purifying agent according to the invention.
  • Embodiment 7 a preparation method of the purifying agent: adding ferrous hydroxide, sodium sulfate and water to a mixing reactor at a ratio of about 1:1:3, stirring and mixing, and after the reaction is completed, evacuating and heating the material under reduced pressure , the heating temperature is about 60-95 ° C, the time is about 1 hour, the obtained solid product is activated in nitrogen, the activation temperature is about 450 ° C, when the gas component in the gas stream is no longer changed, the activation is completed, and the obtained
  • the solid product is a purifying agent according to the invention.
  • Embodiment 8 A method for preparing the purifying agent: adding ferrous carbonate, potassium hydroxide, sodium sulfate and water to a mixing reactor at a ratio of about 1:2:1:5, stirring and mixing, after the reaction is completed , drying and activation in nitrogen, drying temperature About 60-95 ° C, the time is about 2 hours, and then the material is activated, the temperature is about 550 ° C, when the gas component in the gas stream no longer changes, the activation is basically completed, the obtained solid product is a kind The purifying agent of the invention.
  • Embodiment 9 a method for preparing the purifying agent: adding manganese carbonate, sodium hydroxide, calcium sulfate and water to a mixing reactor at a ratio of about 1:2:1:5, stirring and mixing, after the reaction is completed, The material is dried in nitrogen at a temperature of about 60-95 ° C for about 2 hours to remove the moisture in the material, and then the material is activated, the activation temperature is about 500 ° C, and the activation is carried out in the air. When the gas component in the composition is no longer changed, the activation is substantially completed, and the obtained solid product is a purifying agent according to the present invention.
  • Embodiment 10 A method for preparing the purifying agent: adding basic copper carbonate, sodium sulfate and water to a mixing reactor at a ratio of about 1:1:5, stirring and mixing, and after the reaction is completed, drying in nitrogen.
  • the material is heated at a temperature of about 60-95 ° C for about 2 hours, and then the material is activated.
  • the activation temperature is about 500 ° C.
  • the activation is carried out in the air. When the gas component in the gas stream is no longer changed, the activation is basically Upon completion, the solid product obtained is a purifying agent according to the present invention.
  • Example 11 A method for preparing the purifying agent: adding about 20% of the volume of the material to the material obtained by reacting manganese sulfate tetrahydrate and potassium hydroxide in the above Example 4, the other processes are the same
  • the solid product obtained is a purifying agent according to the invention.
  • Embodiment 12 A method for preparing the purifying agent: adding ferrous sulfate, ammonia water (concentration about 35%) and calcium sulfate to a mixing reactor at a ratio of about 1:1:2, stirring and mixing, and after the reaction is completed, precipitating The fresh water layer is removed, dried and activated in air, dried at a temperature of 40-60 ° C for about 3 hours, and then activated at a temperature of about 450 ° C. When the gas component in the gas stream is no longer changed, the activation is completed.
  • the solid product obtained is a purifying agent according to the invention.
  • Example 13 A method for preparing the purifying agent: respectively, ferric sulfate, ferrous chloride, ferric chloride, cobalt chloride, manganese chloride, and copper chloride solution (all of which are about 50%) and hydroxide Sodium is mixed in a ratio of about 1:1.5. After the reaction is completed, about 30% (mass ratio) of calcium carbonate as a molding agent is added, and drying and activation are carried out in nitrogen at a drying temperature of about 60-95 ° C for about 2 hours. After an hour, the activation is carried out, and the activation temperature is about 450 ° C. When the gas component in the gas stream is no longer changed, the activation is completed, and the obtained solid product is the purifying agent of the present invention.
  • Embodiment 14 A method for preparing the purifying agent: ferrous sulfate heptahydrate, cobalt sulfate heptahydrate, manganese sulfate tetrahydrate, copper sulfate pentahydrate and potassium hydroxide according to about 1:1:1:1:8
  • the mixture is added to the mixing reactor in a ratio, and the mixture is thoroughly stirred to uniformly mix the materials.
  • drying and activation are carried out in nitrogen gas at a drying temperature of about 60-95 ° C for about 2 hours.
  • the moisture in the material is removed, and then the material is activated at a temperature of about 550 ° C.
  • the gas component in the gas stream is no longer changed, the activation is completed, and the obtained solid product is a purifying agent according to the present invention.
  • Embodiment 15 A method for preparing the purifying agent: adding, to a material obtained by reacting ferrous sulfate heptahydrate and sodium hydroxide in the above-mentioned Embodiment 3, about 10% by mass of the total amount of titanium dioxide Solid powder (anatase type), stirred and mixed, then evacuated and heated to dry the material at a temperature of about 40-60 ° C for about 2 hours, then activated in nitrogen at a temperature of about 350 ° C, when in the gas stream When the gas component is no longer changed, the activation is completed, and the obtained solid product is a purifying agent according to the present invention.
  • titanium dioxide Solid powder anatase type
  • Embodiment 16 A method for preparing the purifying agent: adding kaolin (clay) as a molding agent and a compounding agent to a material obtained by reacting ferrous sulfate heptahydrate and sodium hydroxide in the above Example 3 Iron powder, the kaolin (clay) dosage is about 20% (mass, the same below), iron powder is about 95%, and evenly stirred to make a honeycomb of ⁇ 50mm ⁇ 50mm (small hole is ⁇ 3mm, 15 Uniformly) cylindrical, then dried and activated in nitrogen, heated at a temperature of about 60-95 ° C for about 2 hours, then activated again, at a temperature of about 350 ° C, when the gas composition in the gas stream no longer changes When the activation is completed, the obtained honeycomb ceramic-like product is a purifying agent according to the present invention.
  • kaolin (clay) dosage is about 20% (mass, the same below)
  • iron powder is about 95%
  • evenly stirred to make a honeycomb of ⁇ 50mm
  • Embodiment 17 A method for preparing the purifying agent: adding 0.1% (by mass) of precious metal palladium powder to the material obtained by reacting ferrous sulfate heptahydrate and sodium hydroxide in the above Example 3 And an equal volume of porous alumina particles having a diameter of about 3 mm with the total material, stirred and mixed, supported on the surface of the support, and then dried and activated in nitrogen, the drying temperature is about 60-95 ° C, and the time is about 2 hours. The activation is further carried out at a temperature of about 300 ° C. When the gas component in the gas stream is no longer changed, the activation is substantially completed, and the obtained solid particulate product is a purifying agent according to the present invention.
  • Embodiment 18 A method for preparing the purifying agent: adding calcium sulfate dihydrate as a forming agent to a material obtained by the reaction in the above-mentioned Example 14, the mass of the calcium sulfate dihydrate is about After 15%, the mixture was uniformly stirred to make a honeycomb of ⁇ 50 mm ⁇ 50 mm (the pores were ⁇ 3 mm, 15 uniform), and then dried and activated under nitrogen. The drying temperature was about 60-95 ° C for about 1 hour. Then, the activation is carried out at a temperature of about 350 ° C. When the gas component in the gas stream is no longer changed, the activation is substantially completed, and the obtained honeycomb ceramic-like product is a purifying agent according to the present invention.
  • Example 19 A circulating fluidized bed gas-solid reactor harmful gas purification device is shown in FIG.
  • the device comprises a cylinder body (4).
  • the lower part of the cylinder body (4) is provided with a gas inlet (1) for connecting the airflow, and the airflow distributor (2) is arranged above the lower airflow inlet to fully mix the gas and solid in the cylinder.
  • a solid purifying agent inlet port (3) There is a solid purifying agent inlet port (3), and the upper portion is connected to the gas-solid separator (7) through a connecting pipe (5) provided; a gas outlet (6) is disposed at an upper portion of the gas-solid separator (7), and the gas-solid separator
  • the lower part of (7) is provided with a solid purifying agent discharge port (9), and the purifying agent return port (8) is in communication with the barrel body (4), and the upper part and the bottom part of the barrel body (4) are respectively provided with an inspection port (10) And the bottom of the cartridge cleaning agent discharge port (11).
  • the purifying process is to introduce the gas stream to be treated from the gas inlet (1) into the cylinder body (4), and after the gas distributor (2) is mixed with the purifying agent added by the purifying agent inlet port (3), gas-solid adsorption oxidation occurs.
  • the reduction reaction the purified gas stream enters the gas-solid separator (7) from the connecting pipe (5) in the upper part of the cylinder for gas-solid separation, the gas stream is discharged from the gas outlet (6), and some unreacted purifying agent can be returned through the purifying agent.
  • the mouth (8) returns to the cylinder (4) to continue to participate in the reaction, and the rest is discharged through the purifying agent discharge port (9), and the bottom of the cylinder is also provided with a bottom purifying agent discharge port (11) for discharging excess purifying agent.
  • the circulating fluidized bed gas-solid reactor has a diameter of ⁇ 60 mm, a height of 2500 mm, and a cylindrical material of 316L stainless steel.
  • the concentration of nitrogen oxides (nitrogen monoxide is about 95%) in the gas stream is 500 ppm, the oxygen content is about 8% by volume, the moisture content is about 10% by volume, and the rest is nitrogen.
  • the gas flow rate is about 5 m 3 /h. (The gas-solid contact time in the reactor is about 0.05-3 s).
  • the purifying agents prepared in Examples 1-15 were respectively used, and the average particle diameter of the purifying agent was about 0.5 mm, and the amount added was about 2-3 kg/h.
  • the purifier feed is a mechanical metering feed, and the temperature after the material is imported is the same as the temperature of the gas in the reactor.
  • the solid particles after the reaction separated by the gas-solid separator (using the cyclone separator) are not returned to the inside of the cylinder.
  • Example 1 was scavenger embodiment, 461, 422, 381, 390 and 423; the cleaning agents prepared in Example 2 were 442, 323, 193, 101 and 283; the cleaning agents prepared in Example 3 were 423, 235, 71, 57 and 225; 4, the prepared purifying agents are 416, 215, 65, 56 and 245; the purifying agents prepared in Example 5 are 395, 154, 55, 43 and 265; the purifying agent prepared in Example 6 is 422, 147, 60, 56 and 216; the cleaning agents prepared in Example 7 were 466, 234, 197, 239 and 296; the cleaning agents prepared in Example 8 were 419, 193, 45, 29 and 231; 9 obtained purifying agents, 396, 149, 53, 47 and 263; the purifying agents prepared in Example 10
  • cobalt chloride materials they are 442, 247, 76, 81 and 293. 412, 207, 66, 78, and 305, 395, 177, 56, 80, and 335 for the copper chloride material; 461, 177, 56, 48, and 231 for the cleaning agents prepared in Example 14; The purifying agents prepared in Example 15 were 415, 217, 67, 54 and 212.
  • Example 20 A countercurrent moving bed gas-solid reactor harmful gas purification device is shown in FIG.
  • the device comprises a cylinder body (4), a gas inlet (1) is arranged at a lower portion of the cylinder body (4), a purifier inlet port (3) and a gas outlet port (6) are arranged at the upper portion, and a purifier discharge port (9) is arranged at the bottom portion.
  • the gas inlet (1) is in communication with the gas outlet (6) via the gas-solid reaction zone (12) in the cylinder (4), and the gas-solid reaction of the purifier addition port (3) through the cylinder (4)
  • the zone (12) and the scavenger recovery zone (13) are in communication with the scavenger particle discharge port (9).
  • the cylinder (4) has a diameter of ⁇ 60 mm and a height of 1500 mm.
  • the body material is 316L stainless steel, and the effective height of the gas-solid reaction zone (12) is about 1000 mm.
  • the purifying process is a gas-solid redox chemical reaction in which the gas stream to be treated enters the cylinder (4) from the gas inlet (1) and the purifying agent added by the purifying agent inlet (3) in the gas-solid reaction zone (12).
  • the purified gas stream is discharged from the gas outlet (6), and the solid particles are discharged through the purification agent discharge port (9) after passing through the solid purifier recovery zone (13).
  • the carrier gas is air, the relative humidity is about 70%, the concentration of nitrogen monoxide in the gas stream is 450 ppm, the gas flow rate is about 1 m 3 /h, and the gas-solid contact time in the reactor is about 3-15 s.
  • the purifying agent prepared in Example 5 was used, and the average particle diameter was about 0.5 mm, and the scavenger was added in an amount of about 2 kg/h.
  • the gas flow temperatures in the reactor were about 60 ° C, 250 ° C, 350 ° C and 450 ° C, respectively, the experimental results showed that the gas outlet NO concentration (ppm) was 435, 43, 12 and 35, respectively.
  • Example 21 The purification apparatus was the same as in Example 19.
  • the concentration of sulfur dioxide in the gas stream is 500ppm
  • the oxygen content is about 8% by volume
  • the moisture content is about 10% by volume
  • the rest is nitrogen.
  • the gas flow rate is about 2-3m 3 /h (the gas-solid contact time in the reactor) About 0.5-5s).
  • Other conditions are the same as in the embodiment 19.
  • the purifying agent prepared in Example 12 was used.
  • the inlet gas flow temperatures were 60 ° C, 150 ° C, 250 ° C, 350 ° C and 450 ° C, respectively
  • the experimental results showed that the gas outlet SO 2 concentrations (ppm) were 423, 178, 135, 343 and 465, respectively.
  • Example 22 A fixed bed gas-solid reactor harmful gas purification device is shown in FIG.
  • the device comprises a cylinder body (4), a gas inlet (1) is arranged at a lower portion of the cylinder body (4), a gas flow distributor (2) is arranged above the gas inlet (1), and a purifier filling layer is arranged above the gas flow distributor (2) (14)
  • the upper portion of the purifying agent filling layer (14) is provided with a purifying agent inlet port (3)
  • the lower portion is provided with a purifying agent discharging port (9)
  • the upper portion of the barrel body (4) is further provided with a gas outlet (6), the gas
  • the inlet (1) communicates with the gas outlet (6) via the gas flow distributor (2) and the scavenger filling layer (14), and the purifying agent inlet port (3) and the purifying agent discharge port (9) are respectively It is in communication with the scavenger filling layer (14).
  • the cylinder (4) has a diameter of ⁇ 60 mm, a height of 1500 mm
  • the purifying process is to introduce a gas stream of a harmful gas such as nitrogen oxides to be treated from the gas inlet (1) through the gas distributor (2) into the purifying agent filling layer (14), in the purifying agent filling layer (14).
  • a harmful gas such as nitrogen oxides
  • the purifying agent are removed by a gas-solidification reaction, and the purified gas stream is discharged from the gas outlet (6) at the upper portion of the reactor, and the purified purifying agent can be periodically discharged from the purifying agent discharge port (9).
  • the alumina carrier purifying agent and the honeycomb forming purifying agent prepared in Examples 16-18 were respectively used, the bulk density of the purifying agent was about 1500 kg/m 3 , and the filling height of the purifying agent in the reactor was about 200 mm, and the outer wall of the reactor was insulated. .
  • the test gas flow is a gas flow simulating automobile exhaust gas, wherein the inlet concentration of the pollutants is about 350 ppm of nitrogen monoxide, about 50 ppm of sulfur dioxide, 10% of carbon dioxide (volume, the same below), carbon monoxide and hydrocarbon of about 150 mg/m 3 , The oxygen content is about 1%, the gas flow rate is about 1.5 m 3 /h, and the gas residence time in the reactor is about 0.3 s - 3 s.
  • Example 16 when using honeycomb type scavenger embodiment, the gas outlet concentrations of NO x (ppm) to about 322,275 , 265 and 285, SO 2 (ppm) are about 42, 55, 43 and 46, carbon monoxide and hydrocarbon concentrations (mg/m 3 ) are about 66, 25, 0 and 0; using Example 17 supported on alumina when the cleaning agent on the carrier, a gas outlet concentrations of NO x (ppm) to about 276,125,106 and 202, SO 2 (ppm) of about 15,18,40 and 47, carbon monoxide and hydrocarbon concentration (mg / m 3 ) is approximately 57, 4, 0 and 0.
  • Example 18 When using the honeycomb molded scavenger embodiment, the gas outlet concentrations of NO x (ppm) and about 182,33,42 175, SO (ppm) and 45, the concentration of carbon monoxide and hydrocarbons of about 2 9,12,35 (mg/m 3 ) is approximately 31, 1, 0 and 0. Since the amount of the scavenger added to the fixed bed reactor is fixed, the removal rate of the harmful substances in the gas stream varies with the reaction consumption of the purifying agent in the reactor, and the measured concentration of the gas outlet contaminant is the maximum removal rate. concentration.
  • Example 23 In the apparatus used in Example 22, the powdery particle purifying agent of Example 14 after use in Example 19 was regenerated in air at a gas flow rate of about 1 m 3 /h, and the gas flow temperature in the reactor was about The reaction time was about 1 hour at 600 °C. When the gas composition in the gas stream no longer changes, the regeneration is completed.
  • Example 24 In the apparatus employed in Example 22, the honeycomb shaped cleaning agent of Example 18 after use in Example 22 was regenerated in nitrogen gas at a gas flow rate of about 1 m 3 /h and the reducing agent was 1% carbon monoxide gas. The temperature of the gas stream in the reactor was about 750 ° C, and the reaction time was about 1 hour. When the gas composition in the gas stream no longer changes, the regeneration is completed.
  • Embodiment 25 A method for preparing the purifying agent: adding ferrous sulfate heptahydrate, calcium oxide and water to a mixing reactor at a ratio of about 1:2:1, stirring and mixing, and after the reaction is completed, drying in nitrogen And activation, drying temperature is about 60-95 ° C, time is about 2 hours, and then activation, activation temperature is about 750 ° C, adding about 0.5% of methane as a reducing agent, when the gas component in the gas stream no longer changes The activation is completed, and the obtained solid product is a purifying agent according to the present invention.
  • Embodiment 26 A method for preparing the purifying agent: adding copper sulfate pentahydrate, barium hydroxide and water to a mixing reactor at a ratio of about 1:1.5:1, stirring and mixing, and after the reaction is completed, in air
  • the material is dried and activated, the drying temperature is about 60-95 ° C, the time is about 2 hours, and then the activation is carried out at a temperature of about 500 ° C.
  • the gas component in the gas stream is no longer changed, the activation is completed, and the obtained solid product is obtained. It is a purifying agent according to the present invention.
  • Embodiment 27 A method for preparing the purifying agent: adding manganese sulfate, calcium carbonate and water to a mixing reactor at a ratio of about 1:1:2, stirring well and heating appropriately, after the reaction is completed, in the air
  • the material is dried and activated, the drying temperature is about 60-95 ° C, the time is about 2 hours, and then the activation is about 450 ° C.
  • the gas component in the gas stream is no longer changed, the activation is completed, and the obtained solid is obtained.
  • the product is a purifying agent according to the invention.
  • Embodiment 28 A method for preparing the purifying agent: adding ferrous carbonate, manganese carbonate and basic copper carbonate to a mixed reaction with magnesium hydroxide, sodium sulfate and water respectively at a ratio of about 1:2:1:6 , stirring and mixing, after the reaction is completed, drying and activation in nitrogen, drying temperature is about 60-95 ° C, time is about 2 hours, and then activation, temperature is about 550 ° C, when the gas component in the gas stream When it is no longer changed, the activation is completed and the obtained solid product is the purifying agent.
  • Embodiment 29 A method for preparing the purifying agent: respectively, ferric sulfate, ferrous chloride, ferric chloride, cobalt chloride, manganese chloride and copper chloride solution (each content of about 50%) and calcium oxide respectively Mixing in a ratio of about 1:3. After the reaction is completed, drying and activation are carried out in nitrogen at a temperature of about 60-95 ° C for about 2 hours, followed by activation at a temperature of about 500 ° C. When the gas component is no longer changed, the activation is completed, and the obtained solid product is the purifying agent.
  • Embodiment 30 A method for preparing the purifying agent: ferrous sulfate heptahydrate, cobalt sulfate heptahydrate, manganese sulfate tetrahydrate, copper sulfate pentahydrate and calcium oxide according to about 1:1::1:1:6
  • the mixture is added to the mixing reactor and stirred and mixed. After the reaction is completed, drying and activation are carried out in nitrogen.
  • the drying temperature is about 60-95 ° C, the time is about 2 hours, and then the activation is carried out at a temperature of about 550 ° C. When the gas component is no longer changed, the activation is completed and the obtained solid product is the purifying agent.
  • Embodiment 31 A method for preparing the purifying agent: adding the clay as a molding agent to the material obtained after the reaction in the above embodiment 30, the dosage of the clay is 30% of the total mass of the material. Mix and uniformly make a ⁇ 50mm ⁇ 50mm honeycomb (small hole is about ⁇ 3mm, 15 holes evenly distributed) cylinder, then dry and activate in nitrogen, drying temperature is about 150 ° C, time is about 1 hour, activation temperature is about 550 ° C When the gas component in the gas stream is no longer changed, the activation is completed, and the obtained honeycomb ceramic-like product is the purifying agent of the present invention.
  • Example 32 Purification apparatus Same as Example 19, using the purifying agent prepared in Examples 25-30, the average particle diameter of the purifying agent is about 0.5 mm, and the adding amount is about 2-3 kg/h, and other operating conditions are the same as in the examples. 19.
  • the inlet gas stream temperatures were 250 °C, 350,450 °C and 550 deg.] C
  • the purifying agents prepared in Example 26 were 310, 102, 75 and 380; the purifying agents prepared in Example 27 were 336, 149, 105 and 392; the purifying agent prepared in Example 28, gas the outlet of the NO x concentration 416,155,97 and 323, respectively; prepared in Example 28 scavenger embodiment, when ferrous carbonate mass, of 305,123,71 and 315, when manganese carbonate material, as 295,113,65 And 285, basic copper carbonate materials, 285, 103
  • Example 33 The purification apparatus was the same as Example 20.
  • the harmful gas carrier gas is air, the relative humidity is about 70%, the concentration of nitrogen monoxide in the gas stream is about 450ppm, the concentration of sulfur dioxide is about 500ppm, and the gas flow rate is about 1m 3 /h.
  • the scavenger has an average particle diameter of about 0.5 mm and an addition amount of about 2-3 kg/h. Other operating conditions are the same as those in Example 20.
  • the experimental results When the inlet gas stream temperatures were 150 °C, 300 °C, 450 °C and 600 °C, the experimental results: the gas outlet of the NO x concentration (in ppm) are 190,62,45 and 335; a gas SO 2 concentration (in ppm ) is divided into 169, 265, 355 and 475.
  • Example 34 The purification apparatus was the same as in Example 22.
  • the purifying agent prepared in Example 31 was used, and the other operating conditions were the same as those in Example 22.
  • the reactor inlet gas stream temperature of about 150 °C, 300 °C, at 450 °C and 600 °C, results were as follows: minimum outlet concentration of contaminants after purification are NO x (ppm) and about 195,72,65 225, SO 2 (ppm) is about 10, 17, 35 and 46, and the carbon monoxide and hydrocarbon concentrations (mg/m 3 ) are about 65, 8, 0 and 0.
  • Example 35 In the apparatus used in Example 22, the powdery particle purifying agent of Example 30 after use in Example 19 was regenerated in air at a gas flow rate of about 1 m 3 /h, and the gas flow temperature in the reactor was about The reaction time was about 1 hour at 600 °C. When the gas composition in the gas stream no longer changes, the regeneration is completed.
  • Example 36 In the apparatus used in Example 22, the purifying agent of Example 31 after use was regenerated, the carrier gas was nitrogen, the gas flow rate was about 1 m 3 /h, and the reducing agent was 0.5% methane gas in the reactor. The gas stream temperature was about 700 ° C and the reaction time was about 2 hours. The regeneration is complete when the reducing agent and other gas components in the gas stream no longer change.
  • Example 37 A preparation method of the purifying agent: ferrous sulfate heptahydrate, cobalt sulfate heptahydrate, manganese sulfate tetrahydrate, copper sulfate pentahydrate and potassium hydroxide and calcium oxide respectively, about 1:1:3
  • the mixture is added to the mixing reactor and stirred and mixed. After the reaction is completed, drying and activation are carried out in nitrogen. The drying temperature is about 40-60 ° C, the time is about 3 hours, and then the activation is carried out at a temperature of about 550 ° C. When the composition is no longer changed, the activation is completed, and a solid product is obtained as the purifying agent.
  • Embodiment 38 A preparation method of the purifying agent: ferrous sulfate heptahydrate, cobalt sulfate heptahydrate, manganese sulfate tetrahydrate, copper sulfate pentahydrate and sodium hydroxide and calcium carbonate respectively 1:1:3
  • the mixture is added to the mixing reactor and stirred and mixed. After the reaction is completed, drying and activation are carried out in the air. The drying temperature is about 60-95 ° C, the time is about 2 hours, and then the activation is about 600 ° C. When the gas component in the gas stream is no longer changed, the activation is completed, and the solid product is obtained as the purifying agent.
  • Embodiment 39 A method for preparing the purifying agent: respectively, ferrous carbonate, manganese carbonate and basic copper carbonate with hydrogen and oxygen Potassium, calcium carbonate and water are separately added to the mixing reactor at a ratio of about 1:2:2:6, and the mixture is stirred and mixed. After the reaction is completed, drying and activation are carried out in nitrogen, and the drying temperature is about 60-95 ° C. After 2 hours, and then activated, the temperature is about 550 ° C. When the gas component in the gas stream is no longer changed, the activation is completed, and the obtained solid product is the purifying agent.
  • Embodiment 40 A method for preparing the purifying agent: adding iron sulfate, cobalt sulfate heptahydrate, manganese sulfate tetrahydrate and copper sulfate pentahydrate to a mixing reactor with potassium carbonate and water at a ratio of about 1.5:1:3, respectively. Stir and heat appropriately. After the reaction is completed, add about 10% of the total amount of calcium oxide powder and mix well. Dry and activate in nitrogen. The drying temperature is about 60-95 ° C for about 2 hours. The activation, the temperature is about 550 ° C, when the gas component in the gas stream is no longer changed, the activation is completed, and the obtained solid product is a purifying agent according to the present invention.
  • Embodiment 41 A method for preparing the purifying agent: ferrous chloride, ferric chloride, cobalt chloride, manganese chloride and copper chloride solution (each content of about 50%) are respectively combined with sodium hydroxide and carbonic acid Calcium is added to the mixing reactor at a ratio of about 1:2:2 and mixed uniformly. After the reaction is completed, drying and activation are carried out in nitrogen, the drying temperature is about 60-95 ° C, the time is about 2 hours, and then the activation temperature is about At 500 ° C, when the gas component in the gas stream no longer changes, the activation is completed, and the obtained solid product is the purifying agent.
  • Embodiment 42 A method for preparing the purifying agent: the products obtained in the above Example 38 are respectively made into a honeycomb of ⁇ 50 mm ⁇ 50 mm (small pores are about ⁇ 3 mm, 15 uniformly distributed), and then in a nitrogen gas. Drying and activation, the drying temperature is about 60-95 ° C, the time is about 2 hours, the water in the material is volatilized and removed, and then activated, the activation temperature is about 650 ° C, and the obtained solid product is an invention.
  • Example 43 Purifying apparatus Same as Example 19, using the purifying agent prepared in Examples 37-41, the scavenger has an average particle diameter of about 0.5 mm, the amount of addition is about 2-3 kg/h, and the carbon dioxide concentration in the gas stream is increased. 10% by volume, the other operating conditions are the same as in Example 19.
  • Example 37 using a cleaning agent prepared embodiment, when the mass of ferrous sulfate heptahydrate, 251, 65 and 93, when the cobalt sulfate heptahydrate material is 276, 85 and 103, the manganese sulfate tetrahydrate material is 191, 55 and 123, and the copper sulfate pentahydrate material is 201, 52 and 115;
  • the prepared scavenger, the effect of each material is substantially the same as that of the material used in Example 37, but lasts for a longer period of time; using the purifying agent prepared in Example 39, the ferrous carbonate material is 195, 55 and 82, manganese carbonate materials, 172, 49 and 113, copper carbonate materials, 167, 42 and 95; using the cleaning agent prepared in Example 40, ferrous sulfate materials, 265, 85
  • Example 44 The purification apparatus was the same as Example 20.
  • the harmful gas carrier gas is simulated boiler flue gas.
  • the concentration of nitrogen monoxide in the gas stream is about 450ppm
  • the concentration of sulfur dioxide is about 500ppm
  • the concentration of carbon dioxide is about 10%
  • the water content is about 10%
  • the gas flow rate is about 1.5m 3 /h.
  • the purifying agent prepared in Example 38 was used.
  • the scavenger had an average particle diameter of about 0.5 mm and an addition amount of about 2-3 kg/h. Other operating conditions were the same as those in Example 20.
  • Example 45 The purification apparatus was the same as in Example 22.
  • the purifying agent prepared in Example 42 was used, and the other operating conditions were the same as those in Example 22.
  • the reactor gas inlet temperature of about 150 °C, 250 °C, 350 °C and 450 °C
  • each of the purified material after the minimum outlet concentration of contaminants results are as follows: ferrous sulfate heptahydrate material, NO x (ppm) to about 172, 75, 55 and 65, SO 2 (ppm) is about 7, 16, 36 and 46, and carbon monoxide and hydrocarbon concentrations (mg/m 3 ) are about 52, 10, 0 and 0.
  • Cobalt sulfate heptahydrate material NO x (ppm) and about 205,145,95 85, SO 2 (ppm) and about 47 8,18,37, carbon monoxide and hydrocarbon concentration (mg / m 3) is about 55 , 15,0 and 0, of manganese sulfate tetrahydrate material, NO x (ppm) to about 162,55,45 and 65, SO 2 (ppm) and about 5,10,26, carbon monoxide and hydrocarbon concentration of 45 (mg / m 3) and about 0 37,5,0; copper sulfate pentahydrate material, NO x (ppm) to about 152,45,35 and 45, SO 2 (ppm) and about 46 6,15,30, CO And the hydrocarbon concentration (mg/m 3 ) is about 32, 5, 0 and 0.
  • Example 46 In the apparatus used in Example 22, each of the honeycomb forming purifying agents prepared in Example 42 after use was regenerated, the carrier gas was nitrogen, the gas flow rate was about 1 m 3 /h, and the reducing agent was 1%. For methane gas, the temperature of the gas stream in the reactor is about 750 ° C, and the reaction time is about 2 hours. When the reducing agent and other gas components in the gas stream no longer change, regeneration is substantially complete.
  • Example 47 In the apparatus used in Example 22, each of the particulate purifying agents prepared in Example 41 after use in Example 19 was regenerated in air at a gas flow rate of about 1 m 3 /h, and the gas flow temperature was about 500-700 ° C, depending on the purifying agent, the reaction time is about 1 hour. When the gas composition in the gas stream no longer changes, the regeneration is completed.
  • Embodiment 48 A method for preparing the purifying agent: dissolving ferrous acetate, ferric nitrate, manganese nitrate and cobalt acetate in water, respectively, and adding sodium hydroxide at about 1:2 to obtain corresponding metal hydrogens respectively.
  • Oxide solid precipitate after filtration, the clear water layer is filtered off, the nitrate, acetate and the like in the solution are removed, and then the calcium oxide is added in an equimolar amount with sodium hydroxide, and the mixture is uniformly mixed according to the above preparation process.
  • Embodiment 49 A method for preparing the purifying agent: pressing ferrous hydroxide, iron hydroxide, manganese hydroxide, cobalt hydroxide, copper hydroxide and cuprous hydroxide with sodium sulfate, calcium oxide and water, respectively A ratio of about 1:1:3:6 is added to the mixing reactor, stirred and mixed uniformly, and then dried and activated in nitrogen.
  • the drying heat temperature is about 60-95 ° C for about 2 hours, so that most of the materials are made.
  • the water is volatilized and then activated, and the activation temperature is about 550 ° C. When the gas component in the gas stream is no longer changed, the activation is completed, and the obtained solid product is the purifying agent of the present invention.
  • Example 50 Purification apparatus Same as Example 19, using the purifying agent prepared in Example 49, the scavenger having an average particle diameter of about 0.5 mm and an addition amount of about 2-3 kg/h, and other operating conditions were the same as those in Example 19.
  • the inlet gas stream temperatures were 250 °C, 350 °C and 450 °C
  • the gas outlet of the experimental results obtained the NO x concentration (in ppm) are: ferrous hydroxide when using the material, and 93 to 241,145; using ferric hydroxide
  • the materials are 262, 160 and 85; when using manganese hydroxide materials, they are 181, 72 and 96; when using cobalt hydroxide materials, they are 267, 155 and 136; when using copper hydroxide materials, they are 191, 65 and 112; when using cuprous hydroxide materials, it is 187, 57 and 119.
  • Embodiment 51 A method for preparing the purifying agent: pressing ferrous hydroxide, iron hydroxide, manganese hydroxide, cobalt hydroxide, copper hydroxide and cuprous hydroxide with sodium sulfate, calcium carbonate and water, respectively Approximately 1:1:3:6 ratio was added to the mixing reactor and mixed uniformly to form a honeycomb of ⁇ 50 mm ⁇ 50 mm (small pores of about ⁇ 3 mm, 15 uniform), dried and activated in nitrogen, and the drying heat temperature was about It is 60-95 ° C, the time is about 2 hours, and then the activation is carried out. The activation temperature is about 650 ° C. When the gas component in the gas stream is no longer changed, the activation is completed, and the obtained solid product is the purification described in the present invention. Agent. The experimental results show that the effect of the obtained purifying agent is substantially equivalent to the purifying agent of the corresponding material.
  • Embodiment 52 A method for preparing the purifying agent: dissolving ferrous hydroxide, iron hydroxide, manganese hydroxide, cobalt hydroxide, copper hydroxide and cuprous hydroxide with sodium chloride, calcium carbonate and water, respectively Adding to the mixing reactor at a ratio of about 1:1:3:6, mixing uniformly, making a honeycomb of ⁇ 50mm ⁇ 50mm (small holes are about ⁇ 3mm, 15 uniform) cylinders, drying and activating in nitrogen, drying heat temperature Approximately 60-95 ° C, the time is about 2 hours, and then activated, the activation temperature is about 500-600 ° C, when the gas component in the gas stream no longer changes, the activation is completed, the obtained solid product is the said purifier.
  • Example 53 The purification apparatus was the same as in Example 22.
  • the purifying agent prepared in Example 52 was used.
  • the other operating conditions were the same as those in Example 22.
  • the reactor gas inlet temperatures were about 250 ° C, 350 ° C and 450 ° C
  • the minimum concentrations of the gas outlet pollutants were measured as follows: when ferrous hydroxide material, NO x concentration (ppm, same below) are about 191,76 and 85, SO 2 concentration (ppm, same below) of about 16, 26 and 46, carbon monoxide and hydrocarbon concentration (mg / m 3, the same below) and about 25,0 0; with iron hydroxide material, NO x concentration of about 205,81 and 95, SO 2 is about 17, 29 and 47, about the concentration of carbon monoxide and hydrocarbons and 0 to 27,0; with manganese hydroxide material, NO x concentration of about 115,45 and 65, SO 2 is about 11, 25 and 42, the concentration of carbon monoxide and hydrocarbons and approximately 15,0 0; using when co
  • Example 54 In the apparatus used in Example 22, after the use of Example 53, the honeycomb forming purifying agent was used for regeneration, the carrier gas was nitrogen, the gas flow rate was about 1 m 3 /h, and the reducing agent was 1% methane gas. The temperature of the gas in the reactor is about 750 ° C, and the reaction time is about 2-3 hours. When the gas composition in the gas stream no longer changes, the regeneration is completed.
  • Embodiment 55 A method for preparing the purifying agent: the ratio of iron hydroxide, manganese hydroxide, tetraammine copper hydroxide and tetraammine cobalt hydroxide to calcium carbonate and water respectively of about 1:3:4 After adding to the mixing reactor and mixing uniformly, a honeycomb of ⁇ 50 mm ⁇ 50 mm (small pores of about ⁇ 3 mm, 15 uniform) is prepared, and dried and activated in nitrogen, and the drying heat temperature is about 60-95 ° C, and the time is about After 2 hours, the activation is carried out at an activation temperature of about 500 ° C. When the gas component in the gas stream is no longer changed, the activation is completed, and the obtained solid product is the purifying agent of the present invention.
  • Example 56 The purification apparatus was the same as in Example 22.
  • the purifying agent prepared in Example 55 was used.
  • the other operating conditions were the same as those in Example 22.
  • the gas inlet gas inlet temperatures of the reactor were about 250 ° C, 350 ° C and 450 ° C, the minimum concentration of the gas outlet pollutants after purification was measured.
  • Embodiment 57 A method for preparing the purifying agent: respectively, ferrous hydrogen carbonate, iron carbonate, oxy basic ferric sulfate, basic manganese chloride, basic cobalt sulfate, and polyaluminium ferric chloride, respectively, and sodium carbonate Calcium silicate and water are added to the mixing reactor at a ratio of about 1:2:1:6, and stirred and mixed uniformly to form a honeycomb of ⁇ 50 mm ⁇ 50 mm (small holes are about ⁇ 3 mm, 15 uniform)
  • the cylinder, dried and activated in nitrogen has a drying heat temperature of about 60-95 ° C for about 2 hours, and then is activated, and the activation temperature is about 650 ° C. When the gas component in the gas stream is no longer changed, the activation is performed. Upon completion, the obtained solid product is the purifying agent of the present invention.
  • Other preparation processes are the same as described above.
  • Example 58 The purification apparatus was the same as in Example 22.
  • the purifying agent prepared in Example 57 was used.
  • the other operating conditions were the same as in Example 22.
  • the reactor gas inlet temperature was about 200 ° C, 300 ° C and 400 ° C, the minimum concentrations of the gas outlet pollutants after purification were experimentally measured.
  • Embodiment 59 A method for preparing the purifying agent: respectively, ammonium ferrous sulfate, ammonium cobalt chloride, ammonium manganese chloride, cuprous chloride, polyaluminum sulphate, potassium sulphate and tetraammine sulphate Adding sodium hydroxide, calcium oxide and water to the mixing reactor at a ratio of about 1:1:3:6 and mixing them uniformly to form a honeycomb of ⁇ 50mm ⁇ 50mm (small pores are about ⁇ 3mm, 15 uniform) cylinders, under nitrogen Drying and activation, drying heat temperature is about 60-95 ° C, time is about 2 hours, and then activation, the activation temperature is about 550 ° C, when the gas component in the gas stream no longer changes, the activation is completed, the obtained
  • the solid product is the purifying agent of the present invention.
  • Example 60 The purification apparatus was the same as in Example 22.
  • the purifying agent prepared in Example 59 was used.
  • the other operating conditions were the same as those in Example 22.
  • the reactor gas inlet temperatures were about 250 ° C, 350 ° C and 450 ° C, the minimum concentration of the reactor gas outlet pollutants after purification was experimentally determined.

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Abstract

一种有害气体净化剂及其制备和净化方法，特征是把铁或锰或钴或铜的盐类及相关衍生物物料与碱或碱性物质及相关衍生物物料和水及成型剂按一定比例和程序混合，得到的固体化合物或混合物，经干燥和活化后，制得的固体产物即为净化剂，把净化剂导入气－固反应器，气流中的有害物在一定温度下与净化剂发生气固反应而被去除，净化剂经再生后可循环利用。

Description

一种有害气体净化剂及其制备和净化方法 技术领域
本发明涉及一种有害气体净化剂及其制备和净化方法，属于大气污染控制和相关环境保护技术领域。
背景技术
人类活动产生的氮氧化物(NOx，主要包括NO和NO2)和二氧化硫(SO2)等有害气体，其中由燃料燃烧产生的占很大部分，其次是硝酸生产、化工制药的硝化反应、金属表面和半导体处理等工业过程。氮氧化物和二氧化硫和对人体有致毒作用，大量的氮氧化物和二氧化硫排放还是引起大气光化学雾和酸雨的主要原因之一。统计数据表明我国城市酸雨中氮氧化物的贡献在不断增加，近年来，国家新制定了一些新法律、法规，对氮氧化物和二氧化硫，特别是火电等燃烧过程排放的相关污染物作出了更加严格的控制和减排规定。
一般地，火力发电厂等以化石燃料燃烧产生的烟气中的氮氧化物浓度约为几百到几千ppm，其中90％以上是一氧化氮。目前选择性催化转化法(SCR)是目前治理化石燃料烟气或尾气中NOx的主要手段之一，但催化剂对运行条件要求严格，需要氨或尿素等作为还原剂，气流中含有硫化物和粉尘等对催化剂的寿命影响很大，特别是对以煤为燃料的火电厂的运行费用很高；湿法是采用各种液体对NOx进行吸收，是低温排放源的主要治理方法，但对含一氧化氮较多的废气，由于一氧化氮在溶液中的溶解度很小，吸收效率较低，如采用氧化或还原吸收的方法，需消耗相关的药剂，运行费用高。
汽车和船舶等采用内燃机作为动力的尾气排放的氮氧化物、二氧化硫、一氧化碳和碳氢化合物等有害物质是大气雾霾的主要成因之一。随着汽车保留量越来越多，由此引起的大气污染问题越来越严重，特别是采用柴油内燃机作为动力的尾气所排放的氮氧化物等污染物的治理难度大、成本高。目前处理技术也大都集中在氮氧化物的催化还原。因此，研究开发新型燃料燃烧烟气或尾气中氮氧化物等有害气体的净化技术，是工业应用中急需解决的问题。
本发明目的是提供一种有害气体净化剂及其制备和净化方法，用于从气流中分别或同时去除氮氧化物、二氧化硫、一氧化碳和碳氢化合物VOCs等有害气体。
发明内容
本发明所要解决的首要技术问题是提供一种有害气体净化剂(以下简称净化剂)及其制备方法，用于从气流中分别或同时去除氮氧化物、二氧化硫、一氧化碳和碳氢化合物VOCs 等有害气体，具有活性高，去除效率高的特点。本发明所要解决的另一个技术问题是提供上述净化剂的净化方法和装置，具有操作简单、处理效率高、处理量大和运行费用低的特点。
本发明解决上述技术问题所采用的技术方案为：一种净化剂，所述净化剂包括A组分铁、钴、锰或铜的一种或任意二种及以上元素；B组分羟基或水的一种或二种；C组分钠、钾、锂、钙、钡或镁的一种或任意两种及以上元素；D组分硫酸根、氯或碳酸根的一种或任意二种及以上；或E组分氧组成的固体化合物或混合化合物，所述的E组分氧不包含硫酸根、碳酸根、羟基和水中的氧，其中各组分的质量百分比为A组分4－96％，B组分1－75％，C组分1－75％，D组分1—75％，E组分0－35％。其中，脱除氮氧化物起主要作用的是化合物中含有的铁或锰或钴或铜元素及其羟基化合物或和氧化物或相应复合化合物，钠、钾和锂随物料投加时带入，对净化有害物净化可以起一定的催化作用，钙、钡和镁及其氧化物或羟基化合物或相关盐等可作为成型剂和吸附有害物的成分，所述的氧包含金属氧化物中的氧和氧基化合物中的氧。
一种所述的净化剂的制备方法，其特征是把物料A、物料B和水(所述的A为带结晶水固体时，可不加水或少加水，下同)按一定比例在混合反应器中混合，这个过程所述的物料A、B和水发生反应(视不同物料可适当加热以加快反应)，上述混合反应过程一般为放热过程，使物料有一定的升温。待反应完毕后，把所得到的产物进行干燥和活化，得到的固体产物即为本发明所述的一种净化剂。所述物料中，物料A是亚铁(Ⅱ)或铁(Ⅲ)、锰(Ⅱ)、钴(Ⅱ)、铜(Ⅰ)或铜(Ⅱ)的硫酸盐、氯化物(盐酸盐)、碳酸盐、硝酸盐或亚硝酸盐、有机酸盐的一种或任意二种及以上物料组合，主要有硫酸亚铁和硫酸铁、氯化亚铁和氯化铁、碳酸亚铁和碳酸铁、硝酸亚铁和硝酸铁、醋酸亚铁和醋酸铁、硫酸锰、氯化锰、碳酸锰、硝酸锰、醋酸锰、硫酸钴、氯化钴、碳酸钴、硝酸钴、醋酸钴、硫酸铜、氯化铜、碳酸铜、硝酸铜和醋酸铜等。所述的物料A也可以是所述盐相应的包括碱式或酸式或复式盐以及聚合物或配位化合物等相关衍生化合物的一种或任意二种及以上物料组合，主要有硫酸亚铁铵或氯化亚铁铵或碱式(又称聚合)硫酸铁或碱式(又称聚合)氯化铁或氧基碱式硫酸铁或硫酸铁铵、硫酸亚铜或氯化亚铜或碱式硫酸铜或碱式氯化铜或硫酸铜铵或氯化铜铵、碱式硫酸锰或碱式氯化锰或硫酸锰铵或氯化锰铵、碱式硫酸钴或碱式氯化钴或硫酸钴铵或氯化钴铵、聚合硫酸铝铁或聚合氯化铝铁、硫酸铁钾、碳酸氢亚铁和硫酸四氨合铜等。物料A优选相关的硫酸盐、氯化物和碳酸盐及其相关的衍生物。物料B是碱或碱性物质或相关衍生物的一种或任意二种及以上物料组合，主要有碱金属的氢氧化物和碳酸盐，碱土金属的氢氧化物、氧化物和碳酸盐、以及相关的酸式盐、碱式盐、复式盐、聚合化合物、配位化合物和氢氧化铵(氨水)等。所述的氢氧化物主要有氢氧化钠、氢氧化钾、氢氧化锂、氢氧化钙、氢氧化钡、氢氧化镁和氨水，所述的氧化物主要有氧化钙、氧化钡和氧化镁，所述的碳酸盐主要有碳酸钠或碳酸氢钠、 碳酸钾或碳酸氢钾、碳酸锂或碳酸氢锂、碳酸钙或碳酸氢钙或碱式碳酸钙、碳酸钡或碳酸氢钡、碳酸镁或碳酸氢镁或碱式碳酸镁、碳酸铵或碳酸氢铵或碳酸铝镁等。物料B优选碱金属的氢氧化物和碳酸盐、碱土金属的氢氧化物和氧化物，物料B采用氨水或铵盐时，因相应物料加热易分解，一般应与物料B中其他化合物或成型剂一同使用。
本发明所述的干燥可采用加热方式，加热温度一般为40℃以上，优选60℃－450℃，最高温度可同活化温度，在负压或抽真空条件下加热，加热时间可短些，一般干燥脱水后使物料中的分离水分达到约10％以下。所述的活化是在一定温度下进行，一般为100℃以上，优选150℃－750℃，最高可达1200℃以上，具体可视物料种类而定，一般物料中含有铁和钴元素的，活化温度可以高一些，以锰或铜元素为主的净化剂的活化温度可低一些。通常碱金属和碱土金属的硫酸盐分解温度高于活化温度，物料中含有氯化物、碳酸盐、铵盐或硝酸盐的产物的活化温度可以超过所述盐的分解温度，相应的盐分解后转化为氧化物。干燥和活化可同时一步进行，也可分步进行，效果相当。也可以把所述的产物预先压制成型后再进行干燥和活化，可添加一定量的成型剂，如所述产物含水较多不易成型时，添加一定量的成型剂后，经初步干燥后(一般水分在15－30％左右)再压制成型，制成蜂窝、板或颗粒等所需各种形状后，再进一步干燥和活化。干燥和活化可以在空气或氮气等惰性气体或负压下进行，也可在还原剂存在条件下的活化，以减少产物中低价态金属的氧化，还原剂主要有氢气、甲烷等碳氢化合物、甲醛等碳氢氧化合物、氨、一氧化碳和一氧化氮等，效果大体相当。在所述产物的活化过程中，使产物整体达到所设温度后，并保持一段时间，当气流中的气体组分不再变化时，活化完成，得到的固体产物即为一种本发明所述的净化剂，所述还原剂的加入量没有特殊要求，还原剂量少，活化时间就长些。加热可采用电炉、导热介质、电磁和微波等多种加热手段，效果相当。
根据所述一种净化剂的制备方法，其特征是把物料A的硫酸盐或氯化物或碳酸盐的一种或二种及以上组合、物料B中的氢氧化钠或氢氧化钾或氢氧化锂的一种或二种及以上组合和水混合后反应得到的产物，经干燥和活化后制得，采用不同物料B的效果大体相当。一般以物料A适当过量为好。如物料中所述的氢氧化物过量时，未参加反应的氢氧化钠、氢氧化钾或氢氧化锂在加热和活化温度较高时，易发生熔融现象，其中，氢氧化锂熔点最高，氢氧化钾其次，氢氧化钠最低，物料熔融对制得的净化剂性能的影响不大。
根据所述一种净化剂的制备方法，其特征是把物料A的硫酸盐或氯化物或碳酸盐的一种或二种及以上组合、物料B中的氢氧化钙、氧化钙、氢氧化钡、氧化钡、氢氧化镁和氧化镁的一种或任意二种及以上组合物料和水混合后反应得到的产物，经干燥和活化后制得，所制得的净化剂中以采用物料B中钙和钡的化合物作为物料的效果为好。
根据所述一种净化剂的制备方法，其特征是把物料A的硫酸盐或氯化物或碳酸盐的一种 或二种及以上组合、物料B中的氢氧化钠或氢氧化钾或氢氧化锂或氢氧化铵的一种或二种及以上组合、物料B中的氢氧化钙、氧化钙、氢氧化钡、氧化钡、氢氧化镁和氧化镁的一种或任意二种及以上组合和水混合后反应得到的产物，经干燥和活化后制得。
本发明所述的物料A和物料B的反应摩尔配比约为1：0.5－1：3，具体因所述的物料的金属价数不同而有所变化。实际物料的投加摩尔比无特殊要求，一般为1：0.1以上，优选1：0.3－1：10。
本发明所述净化剂的制备方法中，所述的物料A也可以是所述盐相应的包括碱式或酸式或复式盐以及聚合物或配位化合物等的相关衍生化合物的一种或任意二种及以上物料组合物，主要有硫酸亚铁铵、氯化亚铁铵、碱式硫酸铁、碱式氯化铁、氧基碱式硫酸铁、硫酸铁铵、硫酸亚铜、氯化亚铜、碱式硫酸铜、碱式氯化铜、硫酸铜铵、氯化铜铵、碱式硫酸锰、碱式氯化锰、硫酸锰铵、氯化锰铵、碱式硫酸钴、碱式氯化钴、硫酸钴铵、氯化钴铵、聚合硫酸铁铝、聚合氯化铝铁、硫酸铁钾、碳酸氢亚铁和硫酸四氨合铜等，其中采用酸式盐作为物料时，对应碱性物料B的用量应适当加大，或与其他碱性物料配合使用。按上述方法制备，所得产物的效果与前述采用物料A为相关的盐的产物大体相当。
本发明所述净化剂的制备方法中，所述的物料B也可用相应的碳酸盐替代，包括酸式或碱式或复式碳酸盐以及聚合物和配位化合物，如碳酸钠或碳酸氢钠、碳酸钾或碳酸氢钾、碳酸锂或碳酸氢锂、碳酸钙或碳酸氢钙或碱式碳酸钙、碳酸钡或碳酸氢钡、碳酸镁或碳酸氢镁或碱式碳酸镁、碳酸铵或碳酸氢铵等。制备方法同前述，其中物料B采用酸式盐时，应与其他碱性物料配合使用，或与物料A中的碱式盐配对使用。所述的碳酸盐中除水溶性较好和强碱性的碳酸钠和碳酸钾等碳酸盐外，其他不溶性的碳酸盐与物料A反应的效果要差一些。
本发明所述净化剂的制备方法，也可由所述物料A的金属元素铁或锰或钴或铜的氢氧化物以及相关的配位化合物，包括氢氧化亚铁、氢氧化铁、氢氧化锰(Ⅱ)、氢氧化钴(Ⅱ)、氢氧化铜、氢氧化亚铜、氢氧化四氨合铜和氢氧化四氨合钴等的一种或任意两种及以上物料组合，与物料B的金属元素钠或钾或锂或钙或钡或镁的硫酸盐、氯化物、碳酸盐以及相应的酸式或碱式或复式盐或聚合物或配位化合物等物料的一种或任意两种及以上物料组合，与水和成型剂(或)混合制备得到。所述的硫酸盐包括硫酸钠、硫酸钾、硫酸锂、硫酸钙、硫酸钡和硫酸镁，所述氯化物包括氯化钠、氯化钾、氯化锂、氯化钙、氯化钡和氯化镁，所述的碳酸盐包括碳酸钠、碳酸钾、碳酸锂、碳酸钙、碳酸钡和碳酸镁等，所述的酸式或碱式或复式盐和聚合化合物主要有硫酸氢钠、硫酸氢钾、硫酸氢锂、硫酸氢钙、硫酸氢钡和硫酸氢镁，碳酸氢钠、碳酸氢钾、碳酸氢锂、碳酸氢钙、碳酸氢钡和碳酸氢镁，碱式碳酸钙、碱式碳酸镁和硫酸铁钾等。所述物料A的金属元素的氢氧化物以及相关的配位化合物物料与所述硫酸盐、氯化物、碳酸盐以及相应的酸式或碱式或复式盐或聚合物或配位化合物等物料的投加量以物 料中的各组分摩尔比计算时，同前述物料A和物料B的投加摩尔配比，所述物料B的金属盐采用酸式盐时一般也应与碱或碱性物料配合使用，其他制备工艺同前述，经干燥和活化后制得。其中，得到的净化剂的净化效果与上述以相应的物料A和B制备的净化剂效果稍差一些，所述物料为带结晶水固体时，可不加水或少加水。
所述物料A的金属元素铁或锰或钴或铜的氢氧化物也可由相应的碳酸盐或碱式碳酸盐或碱式硫酸盐或碱式氯化物替代，包括碳酸亚铁、碳酸铁、碳酸锰、碳酸钴、碱式碳酸钴、碳酸铜、碱式碳酸铜、碱式硫酸铁或聚合氯化铁、氧基碱式硫酸铁、碱式硫酸铜或碱式氯化铜、碱式硫酸锰或碱式氯化锰、碱式硫酸钴和碱式氯化钴等物料，其他制备工艺同前述。所制得的净化剂的净化效果与上述制备得到的净化剂效果大体相当。
本发明所述的净化剂的制备方法中，所述各物料可由相关物料的组合替代。所述的物料A的各类盐或氢氧化物可由相应金属或其氧化物或盐(包括有机和无机)等与盐酸、硫酸和碱等溶液配比替代，如硫酸亚铁或可由铁或氧化亚铁或硫化亚铁和稀硫酸反应制得；氯化锰可由锰的氧化物与盐酸反应制得；氯化铁可由磷酸铁与盐酸反应得到，再加入氢氧化钙，滤去清水层，可得到氢氧化铁；物料B中的碱金属氢氧化物也可由相应的金属氧化物与水反应得到，碱土金属氧化物可由其相应碳酸盐等化合物分解得到。以上各物料的组合替代相应物料后所制得的净化剂的效果同前述制备方法。
本发明所述的净化剂的制备方法中，所述的同一类物料可以混合或组合配合使用，所得产物的效果大体相当。本发明所述的净化剂的制备过程中，所述加入的水的主要作用使物料能够湿润，物料之间充分混合和反应即可，加入量无特殊要求，一般为所述物料总量的1到20倍(摩尔比)，优选3－10倍，加入水量多，干燥脱水过程就能耗大，物料为带结晶水固体时，可不加水或少加水。
本发明所述净化剂的制备方法中，物料B为氨水时，混合反应在水溶液液相进行；采用物料A为有机酸盐、硝酸盐或亚硝酸盐固体时，应把物料A先溶解于水后再混合，得到物料A的金属氢氧化物固体沉淀物，滤去清水层(也可经多次洗涤)，去除溶液中铵、硝酸根、亚硝酸根、醋酸根等及相关离子后，再加入成型剂混合后，按前述的制备工艺，进行干燥和活化，也可以制得本发明所述的净化剂。采用其他物料时，也可以把所述的物料(如碳酸盐)先溶解于水后，按上述过程制备，所得净化剂的效果同前述的制备方法。
本发明所述净化剂的制备过程中，在物料中均可投加一定量的成型剂，所述的成型剂包括物料B中的碱土金属的氧化物、氢氧化物、硫酸盐和碳酸盐及所有相关的衍生物(含酸式或碱式或聚合化合物或复盐或配位化合物等)，还有黏土和硅酸盐(如硅酸钙、硅酸镁或硅酸铝等)等相关物料的一种或二种及以上组合，主要目的是吸收产物中水分和易于成型，并可起辅助吸附作用。成型剂的投加方式可与各物料同时加入，也可在所述物料混合反应中和反 应后，干燥和活化前加入，效果相当，投加量视需要而定，一般为物料总体积的1－85％，其他制备工艺基本同前述。可以把所述的净化剂预制成型后，制成如球、板或蜂窝陶瓷等形状，其制备工艺类似于工业催化剂或吸附剂的制备，具体可参看相关化工手册。
本发明所述净化剂的制备过程中，也可以在物料中加入与物料A中的铁、锰、钴、铜元素的金属或其氧化物的一种或任意两种及以上物料组合作为配合剂，所述配合剂占净化剂的总质量含量一般为95％以下，所述配合剂在净化剂制备过程中一般不参加反应，在去除气流中有害气体过程中能起到一定的催化作用。其中，以添加相关物料的氧化物的效果为好。
本发明所述的净化剂的制备过程中，也可在物料干燥脱水和活化工艺前加入一定量的有机溶剂，主要有丙酮、丁酮、乙醇或丙醇等，加入量无特殊要求，体积比一般为1：1以下，搅拌混合，加热后所述的溶剂挥发，能增加所述净化剂的比表面积，提高净化剂的净化效率。
本发明所述净化剂的制备过程中，也可以在物料中添加少量过渡元素氧化物如二氧化钛、三氧化钨、五氧化二钒、稀土或钯、铂等贵金属作为催化助剂，过渡金属氧化物或稀土质量含量一般为10％以下，贵金属一般为0.5％以下，以促进气流中的氮氧化物、二氧化硫、一氧化碳和VOCs等有害物的吸附和转化，这些金属氧化物或贵金属的效果大体相当。
本发明所述净化剂的制备过程中，也可以把净化剂负载在氧化铝颗粒、蜂窝陶瓷等通用催化剂的载体上，制备工艺也类同相关催化剂的制备，具体可参看相关化工手册。
本发明所述净化剂的净化方法是把上述制备方法得到的净化剂导入气－固反应器净化装置，在净化装置内，气流中分别和同时含有的氮氧化物、二氧化硫、一氧化碳和VOCs等有害物与所述的净化剂发生吸附、吸收和氧化还原等各种反应而被去除，从而达到气体净化目的。其中氮氧化物被所述的净化剂吸附得到净化，二氧化硫被净化剂吸附和吸收得到净化，一氧化碳和VOCs被催化氧化而得到净化。一般在气流温度较高的时(大于300℃)，以氮氧化物和VOCs去除为主，气流温度较低时，在去除氮氧化物的同时可以去除气流中的二氧化硫，二氧化硫的去除与净化剂中物料B的投加量有关，投加量大，二氧化硫的去除率就高。
本发明所述的气－固反应器可采用化工单元操作常用的固定床、移动床、沸腾床、流化床和循环流化床等气－固接触反应器，可采用顺流、逆流和错流等多种形式，效果大体相当，有关反应器结构具体可参看相关化工设备手册。
一种本发明所述的循环流化床气－固反应器有害气体净化装置，所述的气－固反应器的筒体侧下部设置有连接所述气流的气体进口，中部设置有净化剂颗粒加入口，所述净化剂颗粒加入方式可采用机械进料或气力进料等方式，效果相当，在筒体的下部气体进口上方设置有气流分布器，使反应器内气固充分混合接触，筒体的上部设置有连接管，所述的气流通过连接管与气固分离器连通，经气固分离器气固分离后，净化后的气流从气固分离器的上部排出，净化剂颗粒从气固分离器下部排出，其中部分净化剂可返回反应器内参加反应(也可不 返回)，具体可根据反应程度调节所述物料返回筒内参加反应的比例(范围可为0-100％)。
一种本发明所述的逆流移动床气－固反应器有害气体净化装置，该装置包括筒体，筒体下部设置有气体进口，上部设置有净化剂加入口和气体出口，底部设置有净化剂排出口，气体进口经筒体内的气固反应区与气体出口连通，所述的净化剂加入口经筒体内的气固反应区及净化剂回收区与净化剂颗粒排出口连通。其处理工艺流程是把待处理的气流由气体进口进入反应器与由净化剂加入口加入的净化剂在气固反应区发生气固吸附和氧化还原反应，净化后的气流从气体出口排出，反应后固体颗粒经固体净化剂回收区后通过净化剂排出口排出。
一种本发明所述的固定床气－固反应器有害气体净化装置，该装置包括筒体，筒体下部设置有气体进口，气体进口上方设置有气流分布器，气流分布器上方为净化剂充填层，净化剂充填层的上部设置有净化剂加入口、下部设置有净化剂排出口，筒体的上部还设置气体出口，气体进口经气流分布器和净化剂充填层的空隙气体通道与气体出口连通，所述的净化剂加入口和净化剂排出口分别与净化剂充填层连通。其处理工艺流程是把待处理的含氮氧化物等有害气体的气流由气体进口经过气流分布器导入净化剂充填层，在所述的净化剂充填层内，氮氧化物等有害气体与净化剂发生气固吸附和氧化还原等反应而被去除，净化后的气流从反应器上部的气体出口排出，反应后的净化剂可由净化剂排出口定期排出。
本发明所述的净化剂的净化温度范围一般为60℃以上，最高净化温度与所述净化剂的最高活化温度相同，优选温度范围为200℃－500℃，一般以含有铁或钴的净化剂的净化温度高一些，含有锰和铜的净化温度低一些。如进入气-固反应器的气流温度低于60℃，需预先把所述的净化剂温度预热到100℃以上，使净化剂得到活化后再加入气－固反应器。所述的氮氧化物在所述反应器内反应过程的气固接触时间一般为0.05s以上，接触时间长，去除率高，优选为0.2s－20s。净化剂中以物料A中的金属含量计算，与氮氧化物和二氧化硫的吸附和反应摩尔比约为1：0.5－1：2，具体还与物料B以及净化剂结构有关，实际操作过程，净化剂的投加量可根据不同净化剂特性、气流温度、气固接触时间和去除率要求等操作参数经实际试验后确定。对于循环流化床气－固反应器，净化剂与氮氧化物的摩尔比一般为1以上，摩尔比越大，氮氧化物的去除效果越好，但能耗增加，优选为5－100，对于固定床、移动床和沸腾床等反应器，无特定要求，视需要投加。所述的净化剂的粒径及结构可根据不同反应器选用，流化床、移动床和沸腾床等可采用固体颗粒净化剂，粒径依据相应反应器的化工设计手册选取，一般为0.01mm－20mm，固定床可采用球形、平板形或蜂窝陶瓷状等成型净化剂，大小可根据反应器结构尺寸制备和选用。
本发明所述净化剂采用物料A中以锰或铜的化合物的效果最好，铁或钴稍差一些。气流中含有较高浓度的二氧化碳时，优选采用以碳酸盐为物料制备的产物，以减少相关的影响。
使用后的净化剂可在一定温度下通过气固脱吸及还原等反应再生，再生一般可在空气或 氮气等惰性气体或负压中进行，也可在有还原剂存在下再生，常用的还原剂有氢气、甲烷等碳氢化合物、甲醛等碳氢氧化合物、氨、一氧化碳和一氧化氮等，还原剂效果大体相当。再生温度通常为150℃以上，在负压下可低一些，最高温度与所述净化剂活化温度相当，可高于活化温度，优选450℃－850℃。其中含铁和钴净化剂的再生温度可高一些，含锰和铜净化剂的再生温度可低一些。单独吸附氮氧化物后的净化剂可通过气固脱吸的再生，吸收二氧化硫后的净化剂的再生温度可高些，一般通过还原反应再生。
本发明所述的气流主要为火力发电、建材和冶炼等以化石燃料燃烧产生的含有氮氧化物、二氧化硫等有害气体的烟气，包括各类机动车、船舶内燃机等移动源尾气，也可是其他工业过程产生的相关气流。
与现有技术相比，本发明优点在于：采用所述净化剂在一定温度下与气流中的氮氧化物等有害物发生气固吸附和氧化还原反应，使气流中分别或同时含有的氮氧化物、二氧化硫和VOCs等各种有害物得到去除，从而达到气体净化目的，反应后净化剂可通过再生循环使用。
附图说明
图1是一种循环流化床气－固反应器有害气体净化装置结构示意图。
图2是一种逆流移动床气－固反应器有害气体净化装置结构示意图。
图3是一种固定床气－固反应器有害气体净化装置结构示意图。
图中：1气体进口；2气体分布器；3净化剂加入口；4筒体；5连接管；6气体出口；7气固分离器；8净化剂返回口；9净化剂排出口；10检修口；11筒底净化剂排出口；12气固反应区；13净化剂回收区；14净化剂充填层。
具体实施方式
以下结合附图和实施例对本发明作进一步详细描述。实施例以采用物料A中的硫酸亚铁化合物作为代表说明，物料A中其他同类化合物举例说明。物料B采用碱金属的氢氧化物或碱土金属的氧化物和氢氧化物作为代表说明，物料B中其他化合物举例说明。
实施例1：一种所述净化剂的制备方法：把硫酸亚铁、氢氧化钠和水按约1：0.1：2(摩尔比，下同)比例加入混合反应器，使物料混合均匀，待反应完毕后(约10－30分钟，下同，物料不同有所不同)，在空气中进行干燥和活化，干燥温度约为40－60℃，时间约为3小时，除去物料中的水分，然后进行活化，活化温度约为100℃，当气流中的气体组分不再变化时，活化完成，得到的固体产物即为一种本发明所述的净化剂。
实施例2：一种所述净化剂的制备方法：把七水硫酸钴和氢氧化钠按约1：1比例加入混合反应器混合，待反应完毕后，在空气中进行干燥和活化，加热温度为60－95℃，时间约为2小时，除去物料中的水分，然后进行活化，活化温度约为150℃，当气流中的气体组分不再变化时，活化完成，得到的固体产物即为一种本发明所述的净化剂。
实施例3：一种所述净化剂的制备方法：把七水硫酸亚铁和氢氧化钠按约1：2比例加入混合反应器，使物料混合均匀，待反应完毕后，在氮气中进行干燥和活化，干燥温度约为250℃(含活化)，时间约为2小时，当气流中的气体组分不再变化时，干燥和活化完成，得到的固体产物即一种为本发明所述的净化剂。
实施例4：一种所述净化剂的制备方法：把四水硫酸锰和氢氧化锂按约1：3比例加入混合反应器，搅拌混合，待反应完毕后，在氮气中进行干燥和活化，干燥温度约为60－95℃，时间约为2小时，使物料中的水分挥发除去，然后进行活化，活化温度约为350℃，当气流中的气体组分不再变化时，活化完成，得到的固体产物即为一种本发明所述的净化剂。
实施例5：一种所述净化剂的制备方法：把五水硫酸铜和氢氧化钾按约1：2比例加入混合反应器，使物料混合均匀，待反应完毕后，在空气中进行干燥和活化，干燥温度约为450℃(含活化)，时间约为1小时，当气流中的气体组分不再变化时，干燥和活化完成，得到的固体产物即为一种本发明所述的净化剂。
实施例6：一种所述净化剂的制备方法：把七水硫酸亚铁、碳酸钠和水按约1：1：2比例加入混合反应器，搅拌并适当加热，待反应完毕后，把得到的固体产物在氮气中进行干燥和活化，干燥温度约为60－95℃，时间约为2小时，活化温度约为450－500℃，当气流中的气体组分不再变化时，活化完成，得到的固体产物即为一种本发明所述的净化剂。
实施例7：一种所述净化剂的制备方法：把氢氧化亚铁、硫酸钠和水按约1：1：3比例加入混合反应器，搅拌混合，待反应完毕后，抽空减压加热物料，加热温度约为60－95℃，时间约为1小时，得到的固体产物在氮气中进行活化，活化温度约为450℃，当气流中的气体组分不再变化时，活化完成，得到的固体产物即为一种本发明所述的净化剂。
实施例8：一种所述净化剂的制备方法：把碳酸亚铁、氢氧化钾、硫酸钠和水按约1：2：1：5比例分别加入混合反应器，搅拌混合，待反应完毕后，在氮气中干燥和活化，干燥温度 约为60－95℃，时间约为2小时，然后对物料进行活化，温度约为550℃，当气流中的气体组分不再变化时，活化基本完成，得到的固体产物即为一种本发明所述的净化剂。
实施例9：一种所述净化剂的制备方法：把碳酸锰、氢氧化钠、硫酸钙和水按约1：2：1：5比例分别加入混合反应器，搅拌混合，待反应完毕后，在氮气中干燥物料，加热温度约为60－95℃，时间约为2小时，使物料中的水分挥发除去，然后对物料进行活化，活化温度约为500℃，活化在空气中进行，当气流中的气体组分不再变化时，活化基本完成，得到的固体产物即为一种本发明所述的净化剂。
实施例10：一种所述净化剂的制备方法：把碱式碳酸铜、硫酸钠和水按约1：1：5比例分别加入混合反应器，搅拌混合，待反应完毕后，在氮气中干燥物料，加热温度约为60－95℃，时间约为2小时，然后对物料进行活化，活化温度约为500℃，活化在空气中进行，当气流中的气体组分不再变化时，活化基本完成，得到的固体产物即为一种本发明所述的净化剂。
实施例11：一种所述净化剂的制备方法：把在上述实施例4中四水硫酸锰和氢氧化钾反应后得到的物料中，加入约20％所述物料体积的丙酮，其他工艺相同，得到的固体产物即为一种本发明所述的净化剂。
实施例12：一种所述净化剂的制备方法：把硫酸亚铁、氨水(浓度约35％)和硫酸钙按约1：1：2比例加入混合反应器搅拌混合，待反应完毕后，沉淀除去清水层，在空气中进行干燥和活化，干燥温度为40－60℃，时间约为3小时，再进行活化，温度约为450℃，当气流中的气体组分不再变化时，活化完成，得到的固体产物即为一种本发明所述的净化剂。
实施例13：一种所述净化剂的制备方法：把硫酸铁、氯化亚铁、氯化铁、氯化钴、氯化锰和氯化铜溶液(含量均约50％)分别与氢氧化钠按约1：1.5比例混合，待反应完毕后，加入作为成型剂的碳酸钙约30％(质量比)，在氮气中进行干燥和活化，干燥温度约为60－95℃，时间约为2小时，然后进行活化，活化温度均约为450℃，当气流中的气体组分不再变化时，活化完成，得到的固体产物即为本发明所述的净化剂。
实施例14：一种所述净化剂的制备方法：把七水硫酸亚铁、七水硫酸钴、四水硫酸锰、五水硫酸铜和氢氧化钾按约1：1：1：1：8比例加入混合反应器，并充分搅拌，使物料混合均匀，待反应完毕后，在氮气中进行干燥和活化，干燥温度约为60－95℃，时间约为2小时， 除去物料中的水分，然后再对物料进行活化，温度约为550℃，当气流中的气体组分不再变化时，活化完成，得到的固体产物即为一种本发明所述的净化剂。
实施例15：一种所述净化剂的制备方法：把在上述实施例3中七水硫酸亚铁和氢氧化钠反应后得到的物料中，加入约占总物料10％(质量比)的二氧化钛固体粉末(锐钛型)，搅拌混合，然后抽空减压加热干燥物料，温度约为40－60℃，时间约为2小时，然后在氮气中进行活化，温度约为350℃，当气流中的气体组分不再变化时，活化完成，得到的固体产物即为一种本发明所述的净化剂。
实施例16：一种所述净化剂的制备方法：把在上述实施例3中七水硫酸亚铁和氢氧化钠反应后得到的物料中，加入作为成型剂的高岭土(黏土)以及配合剂还原性铁粉，所述高岭土(黏土)的投加量约为20％(质量，下同)，铁粉约为95％，并搅拌均匀后制成Φ50mm×50mm的蜂窝(小孔为Φ3mm，15个均布)圆柱，然后在氮气中干燥和活化，加热温度约为60－95℃，时间约为2小时，然后再进行活化，温度约为350℃，当气流中的气体组分不再变化时，活化完成，得到的蜂窝陶瓷状产物，即为一种本发明所述的净化剂。
实施例17：一种所述净化剂制备方法：把上述实施例3中七水硫酸亚铁和氢氧化钠反应后得到的物料中，加入约占总物料0.1％(质量比)的贵金属钯粉末，和与总物料等体积的直径约为3mm的多孔氧化铝颗粒，搅拌混合后负载在所述载体表面，然后在氮气中干燥和活化，干燥温度约为60－95℃，时间约为2小时，再进行活化，温度约为300℃，当气流中的气体组分不再变化时，活化基本完成，得到的固体颗粒产物即为一种本发明所述的净化剂。
实施例18：一种所述净化剂的制备方法：把在上述实施例14中反应后得到的物料中，加入作为成型剂的二水硫酸钙，所述二水硫酸钙的质量投加量约为15％，搅拌均匀后制成Φ50mm×50mm的蜂窝(小孔为Φ3mm，15个均布)圆柱，然后在氮气中干燥和活化，干燥温度约为60－95℃，时间约为1小时，然后再进行活化，温度约为350℃，当气流中的气体组分不再变化时，活化基本完成，得到的蜂窝陶瓷状产物，即为一种本发明所述的净化剂。
实施例19：一种循环流化床气－固反应器有害气体净化装置如图1所示。该装置包括筒体(4)，筒体(4)的侧下部设置有连接气流的气体进口(1)，下部气流入口上方设置有气流分布器(2)使筒内气固充分混合，中部设置有固体净化剂加入口(3)，上部通过设置的连接管(5)与气固分离器(7)连通；气固分离器(7)的上部设置有气体出口(6)，气固分离器 (7)的下部设置有固体净化剂排出口(9)，并且净化剂返回口(8)与筒体(4)连通，筒体(4)中下部和底部还分别设置有检修口(10)和筒底净化剂排出口(11)。
其净化工艺流程是把待处理气流由气体进口(1)导入筒体(4)，经过气体分布器(2)与由净化剂加入口(3)加入的净化剂混合后，发生气固吸附氧化还原反应，净化后的气流从筒体上部的连接管(5)进入气固分离器(7)进行气固分离，气流从气体出口(6)排出，部分未反应的净化剂可通过净化剂返回口(8)返回筒体(4)内继续参加反应，其余部分通过净化剂排出口(9)排出，同时筒底部也设置有筒底净化剂排出口(11)排出多余的净化剂。
所述循环流化床气－固反应器直径为Φ60mm，高为2500mm，筒体材料为316L不锈钢。气流中氮氧化物(一氧化氮约为95％)的浓度为500ppm，氧气为约8％(体积)，水分含量约为10％(体积)，其余为氮气，气体流量约为5m3/h(反应器内气固接触时间约为0.05－3s)。分别采用实施例1－15制得的净化剂，净化剂平均粒径约为0.5mm，加入量约为2－3kg/h。净化剂进料为机械计量进料，物料进口后的温度同反应器内的气体温度。经气固分离器(采用旋风分离器)分离的反应后固体颗粒不返回筒内。当进口气流温度分别为100℃、250℃、350℃、450℃和550℃时，实验结果得到气体出口NOx浓度(单位ppm，下同)：实施例1制得的净化剂，为461、422、381、390和423；实施例2制得的净化剂，为442、323、193、101和283；实施例3制得的净化剂，为423、235、71、57和225；实施例4制得的净化剂，为416、215、65、56和245；实施例5制得的净化剂，为395、154、55、43和265；实施例6制得的净化剂，为422、147、60、56和216；实施例7制得的净化剂，为466、234、197、239和296；实施例8制得的净化剂，为419、193、45、29和231；实施例9制得的净化剂，为396、149、53、47和263；实施例10制得的净化剂，为392、187、53、42和255；实施例11制得的净化剂，为393、194、57、51和235；实施例12制得的净化剂，为436、210、73、87和263；实施例13制得的净化剂，硫酸铁物料时，为425、233、64、66和252，氯化亚铁物料时，为195、223、54、61和222，氯化铁物料时，为215、243、74、91和262，氯化钴物料时，为442、247、76、81和293，氯化锰物料时，为412、207、66、78和305，氯化铜物料时，为395、177、56、80和335；实施例14制得的净化剂，为411、177、56、48和231；实施例15制得的净化剂，为415、217、67、54和212。
实施例20：一种逆流移动床气－固反应器有害气体净化装置如图2所示。该装置包括筒体(4)，筒体(4)下部设置有气体进口(1)，上部设置有净化剂加入口(3)和气体出口(6)，底部设置有净化剂排出口(9)；气体进口(1)经筒体(4)内的气固反应区(12)与气体出口(6)连通，所述的净化剂加入口(3)经筒体(4)内的气固反应区(12)及净化剂回收区(13)与净化剂颗粒排出口(9)连通。所述的筒体(4)管径为Φ60mm，高为1500mm，筒 体材料为316L不锈钢，气固反应区(12)的有效高度约为1000mm。
其净化工艺流程是把待处理的气流由气体进口(1)进入筒体(4)与由净化剂加入口(3)加入的净化剂在气固反应区(12)发生气固氧化还原化学反应，净化后的气流从气体出口(6)排出，反应后固体颗粒经固体净化剂回收区(13)后通过净化剂排出口(9)排出。
载气为空气，相对湿度约为70％，气流中一氧化氮的浓度为450ppm，气体流量约1m3/h，反应器内气固接触时间约为3－15s。采用实施例5制得的净化剂，平均粒径约为0.5mm，净化剂加入量约为2kg/h。反应器内气流温度分别约为60℃、250℃、350℃和450℃时，实验结果得到气体出口NO浓度(ppm)分别为435、43、12和35。
实施例21：净化装置同实施例19。气流中二氧化硫的浓度为500ppm，氧气含量约为8％(体积)，水分含量约为10％(体积)，其余为氮气，气体流量约为2－3m3/h(反应器内气固接触时间约为0.5―5s)。其他条件同实施例19。采用实施例12所制得的净化剂。当进口气流温度分别为60℃、150℃、250℃、350℃和450℃时，实验结果得到气体出口SO2浓度(ppm)分别为423、178、135、343和465。
实施例22：一种固定床气－固反应器有害气体净化装置如图3所示。该装置包括筒体(4)，筒体(4)下部设置有气体进口(1)，气体进口(1)上方设置有气流分布器(2)，气流分布器(2)上方为净化剂充填层(14)，净化剂充填层(14)的上部设置有净化剂加入口(3)、下部设置有净化剂排出口(9)，筒体(4)的上部还设置气体出口(6)，气体进口(1)经气流分布器(2)和净化剂充填层(14)的空隙气体通道与气体出口(6)连通，所述的净化剂加入口(3)和净化剂排出口(9)分别与净化剂充填层(14)连通。所述的筒体(4)直径为Φ60mm，高为1500mm，材料为316L不锈钢。
其净化工艺流程是把待处理的含氮氧化物等有害气体的气流由气体进口(1)经过气流分布器(2)导入净化剂充填层(14)，在所述的净化剂充填层(14)内，有害气体与净化剂发生气固化学反应而被去除，净化后的气流从反应器上部的气体出口(6)排出，反应后的净化剂可由净化剂排出口(9)定期排出。
分别采用实施例16－18制备的氧化铝载体净化剂和蜂窝成型净化剂，净化剂的堆积密度均约为1500kg/m3，反应器内净化剂的充填高度均约为200mm，反应器外壁保温。
试验的气流为模拟汽车尾气的气流，其中污染物的进口浓度分别为一氧化氮约350ppm、二氧化硫约50ppm、二氧化碳10％(体积，下同)、一氧化碳和碳氢化合物约为150mg/m3，氧气含量约为1％，气体流量约1.5m3/h，气体在反应器内停留时间约为0.3s－3s。反应器气流气体进口温度约为150℃、300℃、400℃和550℃时，实验结果如下：采用实施例16蜂窝成 型的净化剂时，气体出口浓度分别为NOx(ppm)约322、275、265和285，SO2(ppm)约为42、55、43和46，一氧化碳和碳氢化合物浓度(mg/m3)约为66、25、0和0；采用实施例17负载在氧化铝载体上的净化剂时，气体出口浓度分别为NOx(ppm)约276、125、106和202，SO2(ppm)约为15、18、40和47，一氧化碳和碳氢化合物浓度(mg/m3)约为57、4、0和0。采用实施例18蜂窝成型净化剂时，气体出口浓度分别为NOx(ppm)约182、33、42和175，SO2(ppm)约为9、12、35和45，一氧化碳和碳氢化合物浓度(mg/m3)约为31、1、0和0。由于固定床反应器加入的净化剂的量是固定的，因此气流中有害物的去除率随反应器内净化剂的反应消耗而有所变化，测得的气体出口污染物浓度为最大去除率时的浓度。
实施例23：在实施例22采用的装置中，在空气中对在实施例19使用后的实施例14的粉状颗粒净化剂进行再生，气体流量约1m3/h，反应器内气流温度约为600℃，反应时间约1小时。当气流中的气体组分不再变化时，再生完成。
实施例24：在实施例22采用的装置中，在氮气中对在实施例22使用后的实施例18的蜂窝成型净化剂进行再生，气体流量约1m3/h，还原剂为1％一氧化碳气体，反应器内气流温度约为750℃，反应时间约1小时。当气流中的气体组分不再变化时，再生完成。
实施例25：一种所述净化剂的制备方法：把七水硫酸亚铁、氧化钙和水按约1：2：1比例加入混合反应器，搅拌混合，待反应完毕后，在氮气中干燥和活化，干燥温度约为60－95℃，时间约为2小时，再进行活化，活化温度约为750℃，加入约0.5％的甲烷作为还原剂，当气流中的气体组分不再变化时，活化完成，得到的固体产物即为一种本发明所述的净化剂。
实施例26：一种所述净化剂的制备方法：把五水硫酸铜、氢氧化钡和水按约1：1.5：1比例加入混合反应器，搅拌混合，待反应完毕后，在空气中对物料进行干燥和活化，干燥温度约为60－95℃，时间约为2小时，再进行活化，温度约为500℃，当气流中的气体组分不再变化时，活化完成，得到的固体产物即为一种本发明所述的净化剂。
实施例27：一种所述净化剂的制备方法：把四水硫酸锰、碳酸钙和水按约1：1：2比例加入混合反应器，充分搅拌并适当加热，待反应完毕后，在空气中对物料进行干燥和活化，干燥温度约为60－95℃，时间约为2小时，然后活化，温度约为450℃，当气流中的气体组分不再变化时，活化完成，得到的固体产物即为一种本发明所述的净化剂。
实施例28：一种所述净化剂的制备方法：把碳酸亚铁、碳酸锰和碱式碳酸铜分别与氢氧化镁、硫酸钠和水按约1：2：1：6比例分别加入混合反应器，搅拌混合，待反应完毕后，在氮气中进行干燥和活化，干燥温度约为60－95℃，时间约为2小时，然后进行活化，温度约为550℃，当气流中的气体组分不再变化时，活化完成，得到的固体产物即为所述的净化剂。
实施例29：一种所述净化剂的制备方法：把硫酸铁、氯化亚铁、氯化铁、氯化钴、氯化锰和氯化铜溶液(含量均约50％)分别与氧化钙按约1：3比例混合，待反应完毕后，在氮气中进行干燥和活化，干燥温度约为60－95℃，时间约为2小时，然后进行活化，温度均约为500℃，当气流中的气体组分不再变化时，活化完成，得到的固体产物即为所述的净化剂。
实施例30：一种所述净化剂的制备方法：把七水硫酸亚铁、七水硫酸钴、四水硫酸锰、五水硫酸铜和氧化钙按约1：1：：1：1：6比例加入混合反应器搅拌混合，待反应完毕后，在氮气中进行干燥和活化，干燥温度约为60－95℃，时间约为2小时，再进行活化，温度约为550℃，当气流中的气体组分不再变化时，活化完成，得到的固体产物即为所述的净化剂。
实施例31：一种所述净化剂的制备方法：把在上述实施例30中反应后得到的物料中，加入作为成型剂的黏土，所述黏土的投加量占总物料质量的30％，混合均匀制成Φ50mm×50mm的蜂窝(小孔约为Φ3mm,15孔均布)圆柱，然后在氮气中干燥和活化，干燥温度约为150℃，时间约为1小时，活化温度约为550℃，当气流中的气体组分不再变化时，活化完成，得到的蜂窝陶瓷状产物，即为本发明所述的净化剂。
实施例32：净化装置同实施例19，采用实施例25－30所制得的净化剂，净化剂平均粒径约为0.5mm，加入量约为2－3kg/h，其他操作条件同实施例19。当进口气流温度分别为250℃、350、450℃和550℃时，实验结果得到气体出口NOx浓度(单位ppm)：采用实施例25所制得的净化剂，为320、122、81和393；实施例26所制得的净化剂，为310、102、75和380；实施例27所制得的净化剂，为336、149、105和392；实施例28所制得的净化剂，气体出口NOx浓度分别为416、155、97和323；实施例28所制得的净化剂，碳酸亚铁物料时，为305、123、71和315，碳酸锰物料时，为295、113、65和285，碱式碳酸铜物料时，为285、103、51和290；实施例29所制得的净化剂，采用硫酸铁物料时，为325、143、94和320，氯化亚铁物料时，为312、127、89和313，氯化铁物料时，为321、135、92和331，氯化钴物料时，为341、167、121和335，氯化锰物料时，为290、87、89和333，氯化铜物料时，为289、83、95和353；采用实施例30所制得的净化剂，为285、68、66和315。
实施例33：净化装置同实施例20。有害气体载气为空气，相对湿度约为70％，气流中一氧化氮浓度约为450ppm，二氧化硫浓度约为500ppm，气体流量约1m3/h。采用实施例30所制得的净化剂，净化剂平均粒径约为0.5mm，加入量约为2－3kg/h，其他操作条件同实施例20。当进口气流温度分别为150℃、300℃、450℃和600℃时，实验结果得到：气体出口NOx浓度(单位ppm)分别为190、62、45和335；气体出SO2浓度(单位ppm)分为169、265、355和475。
实施例34：净化装置同实施例22。采用实施例31所制得的净化剂，其他操作条件同实施例22。当反应器气流气体进口温度约为150℃、300℃、450℃和600℃时，实验结果如下：净化后污染物最小出口浓度分别为NOx(ppm)约195、72、65和225，SO2(ppm)约为10、17、35和46，一氧化碳和碳氢化合物浓度(mg/m3)约为65、8、0和0。
实施例35：在实施例22采用的装置中，在空气中对在实施例19使用后的实施例30的粉状颗粒净化剂进行再生，气体流量约1m3/h，反应器内气流温度约为600℃，反应时间约1小时。当气流中的气体组分不再变化时，再生完成。
实施例36：在实施例22采用的装置中，对使用完后实施例31的净化剂进行再生，载气为氮气，气体流量约1m3/h，还原剂为0.5％甲烷气体，反应器内气流温度约为700℃，反应时间约2小时。当气流中的还原剂和其他气体组分不再变化时，再生完成。
实施例37：一种所述净化剂的制备方法：把七水硫酸亚铁、七水硫酸钴、四水硫酸锰、五水硫酸铜分别与氢氧化钾和氧化钙按约1：1：3比例加入混合反应器搅拌混合，待反应完毕后，在氮气中进行干燥和活化，干燥温度约为40－60℃，时间约为3小时，然后活化，温度约为550℃，当气流中的气体组分不再变化时，活化完成，得到固体产物即为所述净化剂。
实施例38：一种所述净化剂的制备方法：把七水硫酸亚铁、七水硫酸钴、四水硫酸锰、五水硫酸铜分别与氢氧化钠和碳酸钙按约1：1：3比例加入混合反应器搅拌混合，待反应完毕后，在空气中进行干燥和活化。干燥温度约为60－95℃，时间约为2小时，然后活化，温度约为600℃，当气流中的气体组分不再变化时，活化完成，得到固体产物即为所述净化剂。
实施例39：一种所述净化剂的制备方法：把碳酸亚铁、碳酸锰和碱式碳酸铜分别与氢氧 化钾、碳酸钙和水按约1：2：2：6比例分别加入混合反应器，搅拌混合，待反应完毕后，在氮气中进行干燥和活化，干燥温度约为60－95℃，时间约为2小时，然后活化，温度约为550℃，当气流中的气体组分不再变化时，活化完成，得到的固体产物即为所述的净化剂。
实施例40：一种所述净化剂的制备方法：把硫酸铁、七水硫酸钴、四水硫酸锰和五水硫酸铜分别与碳酸钾和水按约1.5：1：3加入混合反应器并搅拌和适当加热，待反应完毕后，再加入总物料量约10％的氧化钙粉混合均匀后，在氮气中进行干燥和活化，干燥温度约为60－95℃，时间约为2小时，然后活化，温度约为550℃，当气流中的气体组分不再变化时，活化完成，得到的固体产物即为一种本发明所述的净化剂。
实施例41：一种所述净化剂的制备方法：把氯化亚铁、氯化铁、氯化钴、氯化锰和氯化铜溶液(含量均约50％)分别与氢氧化钠和碳酸钙按约1：2：2比例加入混合反应器混合均匀，待反应完毕后，在氮气中进行干燥和活化，干燥温度约为60－95℃，时间约为2小时，然后活化，活化温度约为500℃，当气流中的气体组分不再变化时，活化完成，得到的固体产物即为所述净化剂。
实施例42：一种所述净化剂的制备方法：把在上述实施例38中得到的产物分别制成Φ50mm×50mm的蜂窝(小孔约为Φ3mm，15个均布)圆柱，然后在氮气中干燥和活化，干燥温度约为60－95℃，时间约为2小时，使物料中的水分挥发除去，然后进行活化，活化温度约为650℃，得到的固体的产物即为一种本发明所述的净化剂。
实施例43：净化装置同实施例19，采用实施例37－41所制得的净化剂，净化剂平均粒径约为0.5mm，加入量约为2－3kg/h，气流中增加二氧化碳浓度约10％(体积)，其他操作条件同实施例19。当气体进口温度分别为250℃、350℃和450℃时，实验结果得到气体出口NOx浓度(ppm)：采用实施例37所制得的净化剂，七水硫酸亚铁物料时，为251、65和93，七水硫酸钴物料时，为276、85和103，四水硫酸锰物料时，为191、55和123，五水硫酸铜物料时，为201、52和115；采用实施例38所制得的净化剂，各物料的效果与实施例37所采用的物料大体相当，但持续时间更长；采用实施例39所制得的净化剂，碳酸亚铁物料时，为195、55和82，碳酸锰物料时，为172、49和113，碳酸铜物料时，为167、42和95；采用实施例40所制得的净化剂，硫酸铁物料时，为265、85和143，七水硫酸钴物料时，为286、95和163，四水硫酸锰物料时，为201、65和133，五水硫酸铜物料时，为191、62和145；采用实施例41所制得的净化剂，各物料的效果与实施例38所采用的物料大体相当。
实施例44：净化装置同实施例20。有害气体载气为模拟锅炉烟气，气流中一氧化氮浓度约为450ppm，二氧化硫浓度约为500ppm，二氧化碳浓度约10％，水分约为10％，气体流量约为1.5m3/h。采用实施例38所制得的净化剂，净化剂平均粒径约为0.5mm，加入量约为2－3kg/h，其他操作条件同实施例20。当进口气流温度分别为200℃、300℃和400℃时，实验结果得到气体出口NOx和SO2浓度(ppm)分别为：七水硫酸亚铁物料时，NOx为220、85和95，SO2为151、105和343，四水硫酸锰物料时，NOx为195、55和90，SO2为145、95和325，五水硫酸铜物料时，NOx为165、45和86，SO2为171、125和363。
实施例45：净化装置同实施例22。采用实施例42所制得的净化剂，其他操作条件同实施例22。当反应器气体进口温度约为150℃、250℃、350℃和450℃时，各物料净化后污染物的最小出口浓度实验结果如下：七水硫酸亚铁物料，NOx(ppm)约172、75、55和65，SO2(ppm)约为7、16、36和46，一氧化碳和碳氢化合物浓度(mg/m3)约为52、10、0和0。七水硫酸钴物料，NOx(ppm)约205、145、95和85，SO2(ppm)约为8、18、37和47，一氧化碳和碳氢化合物浓度(mg/m3)约为55、15、0和0，四水硫酸锰物料，NOx(ppm)约162、55、45和65，SO2(ppm)约为5、10、26和45，一氧化碳和碳氢化合物浓度(mg/m3)约为37、5、0和0；五水硫酸铜物料，NOx(ppm)约152、45、35和45，SO2(ppm)约为6、15、30和46，一氧化碳和碳氢化合物浓度(mg/m3)约为32、5、0和0。
实施例46：在实施例22采用的装置中，对使用完后实施例42所制得的各蜂窝成型净化剂进行再生，载气为氮气，气体流量约1m3/h，还原剂为1％甲烷气体，反应器内气流温度约为750℃，反应时间约2小时。当气流中的还原剂和其他气体组分不再变化时，再生基本完成。
实施例47：在实施例22采用的装置中，在空气中对在实施例19使用后的实施例41所制得的各颗粒净化剂进行再生，气体流量约1m3/h，气流温度约为500-700℃，根据净化剂不同有所区别，反应时间约1小时。当气流中的气体组分不再变化时，再生完成。
实施例48：一种所述净化剂的制备方法：把醋酸亚铁、硝酸铁、硝酸锰和醋酸钴分别溶于水后，再按约1：2加入氢氧化钠，分别得到相应的金属氢氧化物固体沉淀物，沉淀后滤去清水层，去除溶液中硝酸根、醋酸根等及相关盐后，再按与氢氧化钠等摩尔投加氧化钙，按前述的制备工艺，混合均匀，制成Φ50mm×50mm的蜂窝(小孔约为Φ3mm，15个均布)圆柱，在空气中进行干燥和活化，干燥热温度约为60－95℃，时间约为2小时，然后进行活化，活化 温度约为600℃，当气流中的气体组分不再变化时，活化完成，得到的固体产物即为本发明所述的净化剂。所制得的净化剂的效果与同类相应物料的净化剂效果相当。
实施例49：一种所述净化剂的制备方法：把氢氧化亚铁、氢氧化铁、氢氧化锰、氢氧化钴、氢氧化铜和氢氧化亚铜分别与硫酸钠、氧化钙和水按约1：1：3：6比例加入混合反应器，并搅拌混合均匀后，在氮气中进行干燥和活化，干燥热温度约为60－95℃，时间约为2小时，使物料中的大部水分挥发除去，然后进行活化，活化温度约为550℃，当气流中的气体组分不再变化时，活化完成，得到的固体产物即为本发明所述的净化剂。
实施例50：净化装置同实施例19，采用实施例49所制得的净化剂，净化剂平均粒径约为0.5mm，加入量约为2－3kg/h，其他操作条件同实施例19。当进口气流温度分别为250℃、350℃和450℃时，实验结果得到气体出口NOx浓度(单位ppm)分别为：采用氢氧化亚铁物料时，为241、145和93；采用氢氧化铁物料时，为262、160和85；采用氢氧化锰物料时，为181、72和96；采用氢氧化钴物料时，为267、155和136；采用氢氧化铜物料时，为191、65和112；采用氢氧化亚铜物料时，为187、57和119。
实施例51：一种所述净化剂的制备方法：把氢氧化亚铁、氢氧化铁、氢氧化锰、氢氧化钴、氢氧化铜和氢氧化亚铜分别与硫酸钠、碳酸钙和水按约1：1：3：6比例加入混合反应器混合均匀后，制成Φ50mm×50mm的蜂窝(小孔约为Φ3mm，15个均布)圆柱，在氮气中进行干燥和活化，干燥热温度约为60－95℃，时间约为2小时，然后进行活化，活化温度约为650℃，当气流中的气体组分不再变化时，活化完成，得到的固体产物即为本发明所述的净化剂。实验结果得到所制得的净化剂的效果与同类相应物料的净化剂大体相当。
实施例52：一种所述净化剂的制备方法：把氢氧化亚铁、氢氧化铁、氢氧化锰、氢氧化钴、氢氧化铜和氢氧化亚铜分别与氯化钠、碳酸钙和水按约1：1：3：6比例加入混合反应器混合均匀后，制成Φ50mm×50mm的蜂窝(小孔约为Φ3mm，15个均布)圆柱，在氮气中进行干燥和活化，干燥热温度约为60－95℃，时间约为2小时，然后进行活化，活化温度约为500-600℃，当气流中的气体组分不再变化时，活化完成，得到的固体产物即为所述的净化剂。
实施例53：净化装置同实施例22。采用实施例52所制得的净化剂，其他操作条件同实施例22，当反应器气体进口温度约为250℃、350℃和450℃时，实验测得气体出口污染物最小浓度分别为：采用氢氧化亚铁物料时，NOx浓度(ppm，下同)分别约为191、76和85， SO2浓度(ppm，下同)约为16、26和46，一氧化碳和碳氢化合物浓度(mg/m3，下同)约为25、0和0；采用氢氧化铁物料时，NOx浓度约为205、81和95，SO2约为17、29和47，一氧化碳和碳氢化合物浓度约为27、0和0；采用氢氧化锰物料时，NOx浓度约为115、45和65，SO2约为11、25和42，一氧化碳和碳氢化合物浓度约为15、0和0；采用氢氧化钴物料时，NOx浓度约为195、81和85，SO2约为21、36和47，一氧化碳和碳氢化合物浓度约为25、1和0；采用氢氧化铜物料时，NOx浓度约为93、35和58，SO2约为21、35和46，一氧化碳和碳氢化合物浓度约为15、0和0；采用氢氧化亚铜物料时，NOx浓度约为85、26和55，SO2约为20、31和46，一氧化碳和碳氢化合物浓度约为16、0和0。
实施例54：在实施例22采用的装置中，对实施例53中使用完后采用各蜂窝成型净化剂进行再生，载气为氮气，气体流量约1m3/h，还原剂为1％甲烷气体，反应器内气流温度约为750℃，反应时间约2-3小时。当气流中的气体组分不再变化时，再生完成。
实施例55：一种所述净化剂的制备方法：把氢氧化铁、氢氧化锰、氢氧化四氨合铜和氢氧化四氨合钴分别与碳酸钙和水按约1：3：4比例加入混合反应器混合均匀后，制成Φ50mm×50mm的蜂窝(小孔约为Φ3mm，15个均布)圆柱，在氮气中进行干燥和活化，干燥热温度约为60－95℃，时间约为2小时，然后进行活化，活化温度约为500℃，当气流中的气体组分不再变化时，活化完成，得到的固体产物即为本发明所述的净化剂。
实施例56：净化装置同实施例22。采用实施例55所制得的净化剂，其他操作条件同实施例22，当反应器气流气体进口温度约为250℃、350℃和450℃时，实验测得净化后气体出口污染物最小浓度分别为：采用氢氧化铁物料时，NOx(ppm,下同)约为225、110和145，SO2(ppm，下同)约为25、31和45，一氧化碳和碳氢化合物(mg/m3，下同)约为36、7和0；采用氢氧化锰物料时，NOx浓度约为195、69和115，SO2约为15、30和43，一氧化碳和碳氢化合物浓度约为25、6和0；采用氢氧化四氨合钴物料时，NOx浓度约为255、161和185，SO2约为15、27和45，一氧化碳和碳氢化合物浓度约为31、10和0；采用氢氧化四铵合铜物料时，NOx浓度约为193、85和188，SO2约为20、32和46，一氧化碳和碳氢化合物浓度约为23、5和0。所述净化剂的再生过程同前述
实施例57：一种所述净化剂的制备方法：把碳酸氢亚铁、碳酸铁、氧基碱式硫酸铁、碱式氯化锰、碱式硫酸钴和聚合氯化铝铁分别与碳酸钠、硅酸钙和水按约1：2：1：6比例加入混合反应器，并搅拌混合均匀后，制成Φ50mm×50mm的蜂窝(小孔约为Φ3mm，15个均布) 圆柱，在氮气中进行干燥和活化，干燥热温度约为60－95℃，时间约为2小时，然后进行活化，活化温度约为650℃，当气流中的气体组分不再变化时，活化完成，得到的固体产物即为本发明所述的净化剂。其他制备工艺同前述。
实施例58：净化装置同实施例22。采用实施例57所制得的净化剂，其他操作条件同实施例22，当反应器气体进口温度约为200℃、300℃和400℃时，实验测得净化后气体出口污染物最小浓度分别为：采用碳酸氢亚铁物料时，NOx(ppm，下同)浓度分别约为147、61和85，SO2浓度(ppm，下同)约为21、37和45，一氧化碳和碳氢化合物浓度(mg/m3，下同)约为55、35和10；采用碳酸铁物料时，NOx浓度约175、90和108，SO2约为25、38和46，一氧化碳和碳氢化合物浓度约为65、36和12；采用氧基碱式硫酸铁物料时，NOx浓度约为155、54和77，SO2约为20、34和43，一氧化碳和碳氢化合物浓度约为55、35和10；采用碱式氯化锰物料时，NOx浓度约为138、51和75，SO2约为15、25和39，一氧化碳和碳氢化合物浓度约为35、20和0；采用碱式硫酸钴物料时，NOx浓度约为168、73和90，SO2约为29、36和46，一氧化碳和碳氢化合物浓度约为53、30和12；采用聚合氯化铝铁物料时，NOx浓度约为263、105和176，SO2约为25、40和48，一氧化碳和碳氢化合物浓度约为87、53和220。所述净化剂的再生过程同前述。
实施例59：一种所述净化剂的制备方法：把硫酸亚铁铵、氯化钴铵、氯化锰铵、氯化亚铜、聚合硫酸铁铝、硫酸铁钾和硫酸四氨合铜分别与氢氧化钠、氧化钙和水按约1：1：3：6比例加入混合反应器混合均匀后，制成Φ50mm×50mm的蜂窝(小孔约为Φ3mm，15个均布)圆柱，在氮气中进行干燥和活化，干燥热温度约为60－95℃，时间约为2小时，然后进行活化，活化温度约为550℃，当气流中的气体组分不再变化时，活化完成，得到的固体产物即为本发明所述的净化剂。
实施例60：净化装置同实施例22。采用实施例59所制得的净化剂，其他操作条件同实施例22，当反应器气体进口温度约为250℃、350℃和450℃时，实验测得净化后反应器气体出口污染物最小浓度分别为：采用硫酸亚铁铵物料时，NOx(ppm，下同)浓度分别约为248、73和83，SO2浓度(ppm，下同)约为22、25和45，一氧化碳和碳氢化合物浓度(mg/m3，下同)约为55、20和1；采用氯化钴铵物料时，NOx浓度约为265、88和92，SO2约为25、31和46，一氧化碳和碳氢化合物浓度约为49、21和1；采用氯化锰铵物料时，NOx浓度约为191、54和79，SO2约为23、30和41，一氧化碳和碳氢化合物浓度约为41、15和0；采用氯化亚铜物料时，NOx浓度约为185、52和78，SO2约为27、35和45，一氧化碳和碳氢 化合物浓度约为35、12和0；采用聚合硫酸铁铝物料时，NOx浓度约为278、161和155，SO2约为29、37和47，一氧化碳和碳氢化合物浓度约为65、33和5；采用硫酸铁钾物料时，NOx浓度约为258、143和160，SO2约为29、39和48，一氧化碳和碳氢化合物浓度约为63、35和7；采用聚合氯化铝铁物料时，NOx浓度约为261、158和156，SO2约为28、36和47，一氧化碳和碳氢化合物浓度约为77、35和10；采用硫酸四氨合铜物料时，NOx浓度约为191、67和86，SO2约为25、33和45，一氧化碳和碳氢化合物浓度约为56、25和0。所述净化剂的再生过程同其前述。
应该说明的是，以上实施例仅用于说明本发明的技术方案，本发明的保护范围不限于此。对于本领域的技术人员来说，凡在本发明的精神和原则之内，对各实施例所记载的技术方案进行修改，或者对其中的部分技术特征进行任何等同替换、修改、变化和改进等，均应包含在本发明的保护范围之内。

Claims (15)

  1. 一种有害气体净化剂，其特征在于所述的净化剂包括A组分铁、钴、锰或铜的一种或任意二种及以上元素；B组分羟基或水的一种或二种；C组分钠、钾、锂、钙、钡或镁的一种或任意两种及以上元素；D组分硫酸根、氯或碳酸根的一种或任意二种及以上；或E组分氧组成的固体化合物或混合化合物，所述的E组分氧不包含硫酸根、碳酸根、羟基和水中的氧，其中各组分的质量百分比为A组分4－96％，B组分1－75％，C组分1－75％，D组分1—75％，E组分0－35％。
  2. 根据权利要求1所述的一种净化剂的制备方法，其特征在于把物料A、物料B和水混合后的产物，经干燥和活化后，制得的固体产物，所述物料中，物料A是亚铁(Ⅱ)或铁(Ⅲ)、锰(Ⅱ)、钴(Ⅱ)、铜(Ⅰ)或铜(Ⅱ)的硫酸盐、氯化物、碳酸盐、硝酸盐或亚硝酸盐、有机酸盐的一种或任意二种及以上物料组合，或是所述盐相应的碱式、酸式、复式盐、聚合物、配位化合物及相关衍生化合物的一种或任意二种及以上物料组合，包括硫酸亚铁铵、氯化亚铁铵、碱式硫酸铁、碱式氯化铁、氧基碱式硫酸铁、硫酸铁铵、硫酸亚铜、氯化亚铜、碱式硫酸铜、碱式氯化铜、硫酸铜铵、氯化铜铵、碱式硫酸锰、碱式氯化锰、硫酸锰铵、氯化锰铵、碱式硫酸钴、碱式氯化钴、硫酸钴铵、氯化钴铵、聚合硫酸铁铝、聚合氯化铝铁、硫酸铁钾、碳酸氢亚铁和硫酸四氨合铜；物料B为钠、钾、锂的氢氧化物或碳酸盐，钙、钡、镁的氧化物、氢氧化物或碳酸盐，氨水，以及相关的酸式盐、碱式盐、复式盐的一种或任意二种及以上物料组合，包括氢氧化钠、氢氧化钾、氢氧化锂、氧化钙、氧化钡、氧化镁、氢氧化钙、氢氧化钡、氢氧化镁、氨水、碳酸钠、碳酸氢钠、碳酸钾、碳酸氢钾、碳酸锂、碳酸氢锂、碳酸钙、碳酸氢钙、碱式碳酸钙、碳酸钡、碳酸氢钡、碳酸镁、碳酸氢镁、碱式碳酸镁、碳酸铵、碳酸氢铵和碳酸铝镁。
  3. 根据权利要求2所述的一种净化剂的制备方法，其特征在于把物料A的硫酸盐、氯化物或碳酸盐，物料B中的氢氧化钠、氢氧化钾或氢氧化锂的一种或任意二种及以上组合和水混合后得到的产物，经干燥和活化后制得；或把物料A的硫酸盐、氯化物或碳酸盐，物料B中的氢氧化钙、氧化钙、氢氧化钡、氧化钡、氢氧化镁或氧化镁的一种或二种及以上组合物料和水混合后得到的产物，经干燥和活化后制得。
  4. 根据权利要求2所述的一种净化剂的制备方法，其特征在于把物料A的硫酸盐、氯化物或碳酸盐，物料B中的氢氧化钠、氢氧化钾、氢氧化锂、氢氧化铵的一种或任意二种及以上物料组合，物料B中的氢氧化钙、氧化钙、氢氧化钡、氧化钡、氢氧化镁或氧氧化镁的一种或任意二种及以上物料组合和水混合后得到的产物，经干燥和活化后制得。
  5. 根据权利要求2或3或4所述的一种净化剂的制备方法，其特征在于所述物料A和物料B 的投加量为1：0.1以上。
  6. 根据权利要求1所述的一种净化剂的制备方法，其特征在于把所述金属元素铁、钴、锰、铜的氢氧化物或配位化合物的一种或任意两种及以上的物料组合，所述物料包括氢氧化亚铁、氢氧化铁、氢氧化锰(Ⅱ)、氢氧化钴(Ⅱ)、氢氧化铜、氢氧化亚铜、氢氧化四氨合铜或氢氧化四氨合钴，与所述金属元素钠、钾、锂、钙、镁、钡的硫酸盐、氯化物、碳酸盐以及相应的酸式、碱式、复式盐的一种或任意两种及以上物料组合，和水混合制备，经干燥和活化后制得，所述的酸式、碱式、复式盐包括硫酸氢钠、硫酸氢钾、硫酸氢锂、硫酸氢钙、硫酸氢钡、硫酸氢镁，碳酸氢钠、碳酸氢钾、碳酸氢锂、碳酸氢钙、碳酸氢钡、碳酸氢镁、碱式碳酸钙、碱式碳酸镁、碳酸铝镁、硫酸铝钾和硫酸铁钾；所述的氢氧化物也可由相应的碳酸盐、碱式碳酸盐、碱式硫酸盐或碱式氯化物替代，包括碳酸亚铁、碳酸铁、碳酸锰、碱式碳酸钴、碳酸铜、碱式碳酸铜、碱式碳酸铝镁、碱式硫酸铁、聚合氯化铁、氧基碱式硫酸铁、碱式硫酸铜、碱式氯化铜、碱式硫酸锰、碱式氯化锰、碱式硫酸钴、碱式氯化钴、聚合硫酸铁铝或聚合氯化铝铁中的一种或任意二种及以上物料组合。
  7. 根据权利要求2或3或4或6所述的一种净化剂的制备方法，其特征在于所述净化剂的制备过程中，所述水的加入量为所述物料总量的1到20倍，所述的物料为带结晶水固体时，可不加水或少加水。
  8. 根据权利要求2或3或4或6所述的一种净化剂的制备方法，其特征在于所述净化剂的制备过程中，在所述产物干燥工艺前加入一定量的成型剂，所述的成型剂包括物料B中的碱土金属的氧化物、氢氧化物、硫酸盐、碳酸盐和相关的酸式或碱式或聚合化合物或复盐或配位化合物、黏土和包括硅酸钙、硅酸镁和硅酸铝的硅酸盐相关物料的一种或二种及以上物料组合，添加体积量为1－85％。
  9. 根据权利要求2所述的一种净化剂的制备方法，其特征在于物料B为氨水或物料A为有机酸盐、硝酸盐或亚硝酸盐，所述物料的混合反应在液相进行，滤去清水层，再加入所述的成型剂混合后，经干燥和活化后制得。
  10. 根据权利要求2或3或4或6或9所述的一种净化剂的制备方法，其特征在于所述净化剂的制备过程中，在所述产物干燥工艺前加入溶剂，所述溶剂包括丙酮、丁酮、乙醇和丙醇，加入体积量为1：1以下；和/或添加过度金属或金属氧化物，包括二氧化钛、三氧化钨、五氧化二钒、稀土或贵金属，所述金属或金属氧化物的加入量10％以下，贵金属为0.5％以下。
  11. 根据权利要求2或3或4或6或9所述的一种净化剂的制备方法，其特征在于把净化剂制成颗粒，或制成球、板或蜂窝陶瓷形状，或负载在通用催化剂的载体上。
  12. 根据权利要求2或3或4或6或9所述的净化剂的制备方法，其特征在于所述的净 化剂制备过程中，在所述物料中加入铁、锰、钴或铜元素的金属或其氧化物的一种或任意两种及以上组合作为配合剂，加入量为95％以下。
  13. 根据权利要求2或3或4或6或9所述的一种净化剂的制备方法，其特征在于所述的净化剂的干燥温度为40℃以上，所述的活化温度为100℃以上。
  14. 根据权利要求1或2或3或4或6或9所述的一种净化剂的制备方法，其特征在于所述的净化剂在惰性气体或空气中或有还原剂存在下活化和再生，所述的还原剂包括氢气、甲烷、甲醛、氨或尿素、一氧化碳和一氧化氮，所述净化剂的再生温度为150℃以上。
  15. 一种有害气体净化剂的净化方法和装置，其特征在于把所述有害气体净化剂和含有害气体的气流分别导入气－固反应器，在所述的气－固反应器内，气流中的氮氧化物与所述的净化剂发生气固吸附反应而被去除，二氧化硫被净化剂吸附和吸收而被去除，一氧化碳和碳氢化合物等VOCs被所述净化剂催化氧化而得到净化，所述的气－固反应器包括化工单元操作通用的固定床、移动床、沸腾床、流化床或循环流化床气－固接触反应器，所述的气流在所述气－固反应器内与所述净化剂的反应温度为60℃以上。
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Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN108926989A (zh) * 2018-08-28 2018-12-04 湖北煜韩环境科技有限公司 一种分子筛除甲醛净化剂及其制备方法
CN110302670A (zh) * 2019-07-29 2019-10-08 许翠英 一种高温工业烟气脱硫脱硝处理装置
CN111547748A (zh) * 2020-06-17 2020-08-18 赣州有色冶金研究所 一种碳酸氢锂溶液高效脱碳制备电池级碳酸锂的方法

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* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
AU2020256256B2 (en) 2019-04-03 2025-06-05 Calgon Carbon Corporation Perfluoroalkyl and polyfluoroalkyl sorbent materials and methods of use
CN110252114B (zh) * 2019-06-20 2022-09-09 深圳市中拓智森环保科技有限公司 空气净化剂溶液及其制备方法
CN111151231B (zh) * 2020-01-09 2021-10-15 浙江工业大学 一种脱硝氯化铁吸附剂再生的方法
WO2022008952A1 (es) * 2020-07-06 2022-01-13 Ecological World For Life S.A.S. Sistema de captura de no 2 a partir del aire con convertidores químicos sólidos no catalíticos
EP4182071A4 (en) 2020-07-14 2024-08-14 Calgon Carbon Corporation SORBENTS HAVING HIGH VOLUMETRIC VALUES OF IODINE AND MOLASSES FOR THE REMOVAL OF PFAS FROM FLUIDS AND METHODS FOR THEIR MANUFACTURE AND USE
WO2022047499A2 (en) 2020-08-31 2022-03-03 Calgon Carbon Corporation Iron and nitrogen treated sorbent and method for making same
TW202218983A (zh) 2020-08-31 2022-05-16 美商卡爾岡碳公司 經銅與氮處理之吸附劑及其製法
MX2023002245A (es) 2020-08-31 2023-03-17 Calgon Carbon Corp Sorbente tratado con cobre, hierro y nitrogeno y metodo para hacer el mismo.
DE102021110700B3 (de) 2021-04-27 2022-06-02 Dräger Safety AG & Co. KGaA Filter für schwefelhaltige Gase
KR102585648B1 (ko) 2022-07-19 2023-10-10 한국건설기술연구원 황계열 가스오염물질의 제거를 위한 이중금속산화물 흡착제 및 그 제조 방법
CN117085666A (zh) * 2023-09-26 2023-11-21 中国科学院城市环境研究所 一种饱和吸附剂的流化再生装置与方法

Citations (10)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPS5297366A (en) * 1976-02-11 1977-08-16 Shell Int Research Simultaneous removal of nitric oxide and sulfuric oxide from gas streams
JPH0459022A (ja) * 1990-06-22 1992-02-25 Babcock Hitachi Kk 微粉脱硫剤を燃焼排ガスに噴霧する脱硫法
CN102872798A (zh) * 2012-10-22 2013-01-16 常州大学 一种常温铁系硫化氢脱除剂的制备方法
CN104117273A (zh) * 2013-04-26 2014-10-29 日本派欧尼株式会社 由氮化镓类化合物半导体的制造工序排出的废气的处理方法
CN105879603A (zh) * 2016-05-26 2016-08-24 张锐 一种优质脱硫剂及其制备方法
CN106268219A (zh) * 2016-08-31 2017-01-04 湖南环达环保有限公司 一种氧化铁精脱硫剂及其制备与应用方法
CN106377997A (zh) * 2016-10-17 2017-02-08 黄华丽 一种气流中有害气体净化剂的制备及净化方法和装置
CN106474911A (zh) * 2016-10-17 2017-03-08 黄华丽 一种气体净化剂的制备及净化方法和装置
CN106474888A (zh) * 2016-10-20 2017-03-08 黄华丽 一种气流净化剂的制备及净化方法和装置
CN106474910A (zh) * 2016-10-14 2017-03-08 黄华丽 一种有害气体净化剂的制备及净化方法和装置

Family Cites Families (27)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR1043603A (fr) * 1963-02-20 1953-11-10 Cavalier en matière élastique utilisable dans les fichiers
US3860690A (en) * 1971-11-03 1975-01-14 Inst Gas Technology Suppression of nitric oxide
NL7307675A (zh) * 1972-06-16 1973-12-18
JPS5166276A (en) * 1974-11-06 1976-06-08 Kanden Hankyu Shoji Kk Haishutsugasuchuno chitsusosankabutsuno jokyohoho
JPS523567A (en) * 1975-06-27 1977-01-12 Matsushita Electric Ind Co Ltd Process for removal of nitrogen oxides
JPS52125483A (en) * 1976-04-15 1977-10-21 Matsushita Electric Ind Co Ltd Production of catalysts for gas purification
DE2846476C3 (de) * 1977-10-26 1982-01-21 Babcock-Hitachi K.K., Tokyo Titandioxid enthaltendes Sinterprodukt und Verfahren zum Sintern von pulverförmigem Titandioxid
JPS5522305A (en) * 1978-08-04 1980-02-18 Mitsubishi Heavy Ind Ltd Catalyst composition
US4755499A (en) * 1984-10-12 1988-07-05 Noxso Corporation Sorbent for removing nitrogen oxides, sulfur oxides and hydrogen sulfide from gas streams
US4721582A (en) * 1986-03-11 1988-01-26 Sanitech, Inc. Toxic gas absorbent and processes for making same
US4977123A (en) * 1988-06-17 1990-12-11 Massachusetts Institute Of Technology Preparation of extrusions of bulk mixed oxide compounds with high macroporosity and mechanical strength
US5180703A (en) 1991-04-24 1993-01-19 W. R. Grace & Co.-Conn. Sox/nox sorbent and process of use
US5362463A (en) * 1992-08-26 1994-11-08 University Of De Process for removing NOx from combustion zone gases by adsorption
US6068824A (en) * 1993-02-04 2000-05-30 Nippon Shokubai Co., Ltd. Adsorbent for nitrogen oxides and method for removal of nitrogen oxides by use thereof
JP3095604B2 (ja) * 1993-02-04 2000-10-10 株式会社日本触媒 窒素酸化物の吸着剤およびこの吸着剤を用いた窒素酸化物の除去方法
DE69627197T2 (de) * 1995-09-26 2003-12-24 Kabushiki Kaisha Kobe Seiko Sho, Kobe Mittel zur entfernung von giftgas
JP3148155B2 (ja) * 1997-07-14 2001-03-19 株式会社日本触媒 窒素酸化物および／または硫黄酸化物の吸着剤およびその使用方法
JP3705933B2 (ja) * 1998-08-06 2005-10-12 株式会社日本触媒 窒素酸化物および／または硫黄酸化物の吸着剤、並びに該吸着剤を用いた窒素酸化物および／または硫黄酸化物の除去方法
CN1305565C (zh) * 2001-12-15 2007-03-21 北京三聚环保新材料有限公司 脱硫催化剂及其制备方法和用途
JP2007160166A (ja) 2005-12-12 2007-06-28 Toyota Motor Corp 常温ＮＯｘ吸着材
CN101134918B (zh) * 2006-08-28 2012-03-21 北京三聚环保新材料股份有限公司 具有高硫容的脱硫剂活性组分及其制备方法
ATE439903T1 (de) * 2006-10-06 2009-09-15 Umicore Ag & Co Kg Stickoxidspeicherkatalysator mit abgesenkter entschwefelungstemperatur
CN101298017A (zh) * 2008-01-23 2008-11-05 清华大学 烟气脱硫脱硝工艺
US8048818B2 (en) * 2008-03-26 2011-11-01 Babcock & Wilcox Power Generation Group, Inc. In-situ regeneration of a catalyst masked by calcium sulfate
CN103736371A (zh) * 2013-12-12 2014-04-23 芜湖中路实业有限责任公司 一种含粉煤灰的烟气脱硝脱硫剂及其制备方法
CN105032163A (zh) * 2015-07-02 2015-11-11 黄立维 一种从气流中去除氮氧化物和二氧化硫的方法及其装置
CN105771617A (zh) * 2016-03-22 2016-07-20 天津滨环化学工程技术研究院有限公司 一种烟气的脱硫脱硝方法

Patent Citations (10)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPS5297366A (en) * 1976-02-11 1977-08-16 Shell Int Research Simultaneous removal of nitric oxide and sulfuric oxide from gas streams
JPH0459022A (ja) * 1990-06-22 1992-02-25 Babcock Hitachi Kk 微粉脱硫剤を燃焼排ガスに噴霧する脱硫法
CN102872798A (zh) * 2012-10-22 2013-01-16 常州大学 一种常温铁系硫化氢脱除剂的制备方法
CN104117273A (zh) * 2013-04-26 2014-10-29 日本派欧尼株式会社 由氮化镓类化合物半导体的制造工序排出的废气的处理方法
CN105879603A (zh) * 2016-05-26 2016-08-24 张锐 一种优质脱硫剂及其制备方法
CN106268219A (zh) * 2016-08-31 2017-01-04 湖南环达环保有限公司 一种氧化铁精脱硫剂及其制备与应用方法
CN106474910A (zh) * 2016-10-14 2017-03-08 黄华丽 一种有害气体净化剂的制备及净化方法和装置
CN106377997A (zh) * 2016-10-17 2017-02-08 黄华丽 一种气流中有害气体净化剂的制备及净化方法和装置
CN106474911A (zh) * 2016-10-17 2017-03-08 黄华丽 一种气体净化剂的制备及净化方法和装置
CN106474888A (zh) * 2016-10-20 2017-03-08 黄华丽 一种气流净化剂的制备及净化方法和装置

Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN108926989A (zh) * 2018-08-28 2018-12-04 湖北煜韩环境科技有限公司 一种分子筛除甲醛净化剂及其制备方法
CN110302670A (zh) * 2019-07-29 2019-10-08 许翠英 一种高温工业烟气脱硫脱硝处理装置
CN111547748A (zh) * 2020-06-17 2020-08-18 赣州有色冶金研究所 一种碳酸氢锂溶液高效脱碳制备电池级碳酸锂的方法

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