WO2013134910A1 - 一种矿热熔融电炉尾气催化氧化净化的方法 - Google Patents

一种矿热熔融电炉尾气催化氧化净化的方法 Download PDF

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WO2013134910A1
WO2013134910A1 PCT/CN2012/072193 CN2012072193W WO2013134910A1 WO 2013134910 A1 WO2013134910 A1 WO 2013134910A1 CN 2012072193 W CN2012072193 W CN 2012072193W WO 2013134910 A1 WO2013134910 A1 WO 2013134910A1
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gas
tail gas
catalyst
hours
electric furnace
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PCT/CN2012/072193
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French (fr)
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宁平
王学谦
王向宇
田森林
唐晓龙
郜华萍
易红宏
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昆明理工大学
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Priority to PCT/CN2012/072193 priority Critical patent/WO2013134910A1/zh
Priority to US14/384,716 priority patent/US20150041722A1/en
Publication of WO2013134910A1 publication Critical patent/WO2013134910A1/zh

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    • C01B3/50—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification
    • C01B3/56—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification by contacting with solids; Regeneration of used solids
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Definitions

  • the invention relates to a method for catalytic oxidation purification of tail gas of a mine hot melt electric furnace.
  • Carbon-based products are important organic chemical raw materials. With the reduction of petroleum resources and the rising price, the scope and quantity of carbon-based products replacing petrochemical products are expanding, and the status of carbon-based chemicals in various countries' economies is becoming more and more important. At present, carbon-chemical has become a hot spot for research and development in many countries around the world. New products, new processes, and new catalysts are emerging one after another. Carbon monoxide has almost become a chemical raw material with the same amount of basic chemical materials such as ethylene and propylene in petrochemical industry.
  • the industrial waste gas is rich in carbon monoxide, and the CO in the ore-melting electric furnace is worthy of being utilized.
  • Mineral hot melt When the electric furnace is used in chemical industry, it should be purified and purified first. If a 30 to 90% reduction of carbon monoxide containing carbon monoxide is used as a raw material for the production of a single carbon chemical product, high purity CO gas must first be obtained. Obviously, the presence of impurities in the tail gas of the ore-melting electric furnace greatly limits the effective utilization of the gas. In order to ensure the smooth progress of product quality and subsequent comprehensive utilization processes, it must be purified and pretreated.
  • ore hot melt electric furnace exhaust gas as a raw material gas to produce a single carbon chemical product can also change the current high cost of the ore hot melt electric furnace production, and the situation in the market is weak, to achieve energy saving, energy saving, clean production.
  • precious resources such as ore-melting electric furnace exhaust gas, which is rich in carbon monoxide, have been limited to drying raw materials, and most of the hot-melt electric furnace exhaust gas is directly burned and vented. The limiting factor is that the tail gas of the hot-melt electric furnace contains influences on it.
  • the impurities of oxo synthesis that is, the problem of tail gas purification in the ore-melting electric furnace, have not been solved, especially the removal of phosphorus in the tail gas of the ore-melting electric furnace, which has a serious influence on the carbon monoxide carbonylation catalyst.
  • the reaction is a reduction reaction occurring at a high temperature when the ore is reduced by the ore-melting electric furnace
  • the impurities in the tail gas of the ore-melting electric furnace are mainly present in a reduced state.
  • Phosphorus is mainly elemental phosphorus (P 4 ) and phosphine (PH 3 )
  • sulfur is mainly hydrogen sulfide (H 2 S) and organic sulfur
  • fluorine is mainly hydrogen fluoride (HF), silicon fluoride (SiF 4 ), etc.
  • the current industry mainly uses water washing and alkaline washing to purify: 1.
  • washing The reducing exhaust gas is cooled and dedusted, and fluoride and a part of elemental phosphorus, phosphine, hydrogen fluoride and hydrogen sulfide are removed. Since the vapor pressure of phosphorus rapidly decreases as the temperature decreases, some of the phosphorus in the exhaust gas is removed by condensation after the water wash is cooled, and a part of the hydrogen sulfide can be removed by dissolving in water.
  • Alkali washing A large amount of acid gas such as carbon dioxide (co 2 ), hydrogen sulfide or hydrogen fluoride is removed by a chemical reaction using a 0.8 to 10% sodium hydroxide (NaOH) solution.
  • acid gas such as carbon dioxide (co 2 )
  • hydrogen sulfide or hydrogen fluoride is removed by a chemical reaction using a 0.8 to 10% sodium hydroxide (NaOH) solution.
  • the main problems in the above methods are as follows: the removal efficiency of the elemental material is low, the removal is incomplete, and the use of various catalysts may cause poisoning of the catalyst, which cannot meet the requirements of the raw material gas of a carbon chemical.
  • the invention overcomes the deficiencies of the prior art, aims to solve the problem of purification and pretreatment of the tail gas of the ore-melting electric furnace, and provides a method for catalytic oxidation purification of the tail gas of the ore-melting electric furnace, so that after purifying the tail gas of the ore-melting electric furnace, sulfur,
  • concentration of typical impurities such as phosphorus and fluorine is less than 1 mg/m 3 , which makes it meet the requirements of high-value-added raw material gas for one-carbon chemical products.
  • the tail gas of the ore-melting electric furnace is a reducing industrial waste gas.
  • the main components are: CO 85 ⁇ 95% (V/V), C0 2 3 ⁇ 7% (V/V), H 2 1 ⁇ 8% (V/V), N 2 2 ⁇ 5% (V / V ), 0 2 0. 2 ⁇ 1% (V / V), TP 1000- 5000mg / m 3, H 2 S 1000 ⁇ 5000mg / m 3, HF 300 ⁇ 4000mg / m 3 .
  • Alkaline washing can remove the typical pollutants in the elemental state in the tail gas of the ore-melting electric furnace, and convert the typical pollutants in the elemental state from the elemental state of the aerosol to the gas state, which is beneficial to the removal by the catalytic oxidation purification method;
  • the reformed gas is heated to a fixed bed of catalytic oxidation, and the typical impurities in the gaseous state are removed by oxidizing a trace amount of oxygen in the tail gas of the ore-melting electric furnace.
  • the tail gas of the hot-melt electric furnace is washed with an alkali-containing aqueous solution to remove impurities such as silicon fluoride, carbon dioxide and some elemental phosphorus in the tail gas.
  • the reaction process is as follows:
  • the washing solution containing N3 ⁇ 4C0 3 is subjected to causticization to recover NaOH and returned to the system for recycling.
  • the exhaust gas still cannot meet the requirements for preparing raw materials for chemical products.
  • the present invention adopts a high-efficiency purification technology of catalytic oxidation of tail gas in a mineral-melting electric furnace.
  • the tail gas after the alkali washing is preheated by the preheater, and passes through the reactor from bottom to top.
  • the reactor is filled with a high-efficiency catalyst, and elemental phosphorus, phosphine, and hydrogen fluoride impurities are catalytically oxidized.
  • sulfur is catalytically oxidized:
  • Phosphine has strong reducibility.
  • the low-cost P in the exhaust gas undergoes redox reaction with high-valent metal ions (Me 3+ ), P is oxidized and converted to phosphoric acid, and metal ions (Me 3+ ) are reduced and reduced.
  • the metal ions are oxidized by the 0 2 in the gas to achieve the recycling of the catalyst.
  • the main reaction equation is as follows:
  • the purified tail gas discharged from the reactor is cooled to 30 ° C by a cooling tower to obtain a qualified one carbon chemical raw material gas.
  • the volume of oxygen in the exhaust gas obtained in the step (2) is 0. 5 ⁇ 3%, and the exhaust gas is passed from bottom to top at a rate of 300 to 600 m 3 (gas volume) / m 3 (catalyst volume).
  • a catalytically oxidized fixed bed containing the high-efficiency catalyst obtained in the step (1) is subjected to a purification reaction at a reaction temperature of 50 to 100 ° C, and the purified gas is cooled to obtain a carbon chemical raw material gas.
  • the catalyst carrier of the step (1) is activated alumina, zeolite, activated carbon or diatomaceous earth.
  • the immersion liquid of the step (1) is a concentration of 0. 25 ⁇ 7% of sodium hydroxide, potassium hydroxide, sulfur A solution of ferrous iron, lead chloride, aluminum nitrate, sodium carbonate, copper acetate or cerium nitrate.
  • the catalyst carrier When the catalyst carrier is activated alumina, it is impregnated with a cerium nitrate solution having a mass concentration of 0.35%. The catalyst carrier is impregnated with a ferrous sulfate solution having a mass concentration of 0.4%.
  • the catalyst carrier When the catalyst carrier is activated carbon, it is impregnated with a potassium hydroxide solution having a mass concentration of 0.5%. When the catalyst carrier is activated carbon, it is impregnated with a sodium hydroxide solution having a mass concentration of 0.5%. The catalyst carrier is impregnated with a copper acetate solution having a mass concentration of 0.2%.
  • the catalyst carrier When the catalyst carrier is activated carbon, it is impregnated with a sodium carbonate solution having a mass concentration of 7%.
  • the leaching of the lead chloride was carried out with a solution having a mass concentration of 0.55%, and then impregnated with a lead chloride solution having a mass concentration of 0.25%.
  • the high-efficiency catalyst of the step (3) is activated by hot air for 4-8 hours, and the adsorbed but not completely oxidized substances, such as elemental phosphorus, phosphine, phosphorus trioxide, hydrogen sulfide, are completely oxidized, and then steam is used. It is activated for 2 ⁇ 4h, then washed with water, then heated to 95 ⁇ 110°C with steam, and finally activated by drying with hot air for 24 ⁇ 48h.
  • the catalytic oxidation purification can adopt two fixed bed parallel systems, wherein one fixed bed fails to be transferred to the catalyst regeneration, and the other fixed bed continues to be purified, and the catalyst regeneration time is 1/2 of the catalytic oxidation purification time of the ore heat melting electric furnace exhaust gas. 1/3, the entire system can be guaranteed to run continuously.
  • the invention firstly removes typical pollutants existing in the elemental state in the tail gas of the ore heat-melting electric furnace by caustic cleaning of the tail gas of the ore-melting electric furnace, and converts the typical pollutants in the elemental state into a gas state from the elemental state of the aerosol, after the alkali washing
  • the reformed gas enters the catalytic oxidation fixed bed after being heated, and the typical impurities in the gaseous state are removed by oxidizing a trace amount of oxygen in the tail gas of the ore-melting electric furnace.
  • the typical impurity content in the tail gas of the ore hot-melting electric furnace is Less than 1 mg/m 3 .
  • the catalyst used in the invention can greatly improve the purification efficiency of the tail gas of the ore melting electric furnace, the catalyst is easy to be regenerated, the utilization rate is high, the process flow is simple, and the purification cost is low.
  • the main factors affecting the purification efficiency are the reaction temperature, the oxygen content in the exhaust gas and the carrier gas velocity.
  • the influence rules are as follows:
  • the oxidation reaction can be carried out at a lower temperature of 50 to 100 ° C in the presence of a catalyst.
  • the increase of the reaction temperature is beneficial to the improvement of the purification efficiency.
  • the reaction temperature is higher than 100 ° C and then the temperature is raised, the improvement of the purification efficiency is not obvious;
  • the oxygen content in the tail gas of the ore-melting electric furnace is 0. 5 ⁇ 3%, and the purification efficiency increases as the oxygen content increases;
  • the carrier gas flow rate is in the range of 300 ⁇ 600m 3 (gas volume) / m 3 (catalyst volume) ⁇ 1 ⁇ , reducing the carrier gas flow rate can improve the purification effect, but the flow rate is reduced to 300m 3 (gas volume) / m 3 ( After the catalyst volume), the purification effect has not been significantly improved.
  • the adsorption capacity of the catalyst to P3 ⁇ 4 is 12 to 28%
  • the adsorption capacity for elemental phosphorus is 24 to 56%
  • the adsorption capacity for hydrogen sulfide is 11 to 25%
  • the adsorption capacity for hydrogen fluoride is 10 to 22 %
  • the content of typical impurities such as hydrogen sulfide, total phosphorus and hydrogen fluoride in the tail gas of the purified hot-melt electric furnace is less than 1mg/m 3 , which meets the requirements for the production of one-carbon chemical products.
  • the invention has the following advantages:
  • the purification efficiency is high, and the purified ore-melting electric furnace exhaust gas reaches the requirement of producing a carbon chemical to the raw material gas;
  • Figure 1 is a process flow diagram of the present invention.
  • the activated alumina was impregnated with a cerium nitrate solution having a mass concentration of 0.25% for 20 hours, aged for another 24 hours, then placed in a muffle furnace at 50 CTC for 6 hours, and finally dried at 11 CTC for 4 hours to obtain a high-efficiency catalyst;
  • the volume of oxygen in the exhaust gas obtained is 0.5%, and the exhaust gas is passed from bottom to top at a rate of 500 m 3 (gas volume) / m 3 (catalyst volume) .h, in the containing step ( 1)
  • the catalytically oxidized fixed bed of the obtained high-efficiency catalyst is subjected to a purification reaction at a reaction temperature of 80 ° C.
  • phosphine is catalytically oxidized, and the oxidized products such as phosphorus pentoxide and phosphorus trioxide are adsorbed on the surface of the catalyst.
  • Purified gas After the body is cooled, a carbon chemical raw material gas is obtained.
  • the content of typical impurities such as phosphorus, sulfur and fluorine in the exhaust gas after purification is less than 1 mg/m 3 .
  • the high-efficiency catalyst after the high-efficiency catalyst fails, it is activated by hot air for 4 hours, so that the adsorbed but not completely oxidized substances, such as elemental phosphorus, phosphine, phosphorus trioxide, hydrogen sulfide, are completely oxidized, then activated by steam for 2h, then washed with water, then It is heated to 110 ° C with steam and finally reconstituted after being activated by hot air drying for 24 hours.
  • the adsorbed but not completely oxidized substances such as elemental phosphorus, phosphine, phosphorus trioxide, hydrogen sulfide
  • the zeolite is impregnated with a ferrous sulfate solution having a mass concentration of 0.3% for 24 hours, aged for another 24 hours, calcined at 55 CTC for 6 hours, and finally dried at 110 ° C for 4 hours to obtain a high-efficiency catalyst;
  • tail gas of the hot-melt electric furnace is washed with an alkali-containing aqueous solution to remove carbon dioxide and some phosphorus, sulfur and fluorine impurities, and the tail gas after alkali washing is preheated to 70 ° C ;
  • the volume of oxygen in the exhaust gas obtained is 0.5%, and the exhaust gas is passed from bottom to top at a rate of 500 m 3 (gas volume) / m 3 (catalyst volume) .h, in the containing step ( 1)
  • the catalytically oxidized fixed bed of the obtained high-efficiency catalyst is subjected to a purification reaction at a reaction temperature of 70 ° C.
  • phosphorus and sulfur impurities are catalytically oxidized, and the oxidized products such as phosphorus pentoxide, phosphorus trioxide, sulfur, etc. are adsorbed.
  • the gas is cooled to obtain a carbon chemical raw material gas.
  • the content of typical impurities such as phosphorus, sulfur and fluorine in the exhaust gas after purification is less than 1 mg/m 3 .
  • the high-efficiency catalyst after the high-efficiency catalyst fails, it is activated by hot air for 6h, so that the adsorbed but not completely oxidized substances, such as elemental phosphorus, phosphine, phosphorus trioxide, hydrogen sulfide, are completely oxidized, then activated by steam for 3h, then washed with water, then It is heated to 100 ° C with steam and finally re-used after being activated by hot air drying for 32 h.
  • the adsorbed but not completely oxidized substances such as elemental phosphorus, phosphine, phosphorus trioxide, hydrogen sulfide
  • the activated carbon was immersed in a potassium hydroxide solution with a concentration of 0.5% for 18 hours, aged for another 24 hours, calcined at 350 ° C for 12 hours, and finally dried at 110 ° C for 6 hours to obtain a high-efficiency catalyst;
  • the oxygen content in the exhaust gas obtained is 0.5%, and the exhaust gas is introduced from the bottom to the bottom at a rate of 600 m 3 (gas volume) / m 3 (catalyst volume) .h, in the containing step ( 1)
  • the catalytically oxidized fixed bed of the obtained high-efficiency catalyst is subjected to a purification reaction at a reaction temperature of 100 ° C.
  • phosphorus and sulfur impurities are catalytically oxidized, and the oxidized products such as phosphorus pentoxide, phosphorus trioxide, sulfur, etc. are adsorbed on On the surface of the catalyst, after purification, the gas is cooled to obtain a carbon chemical raw material gas.
  • the content of typical impurities such as phosphorus, sulfur and fluorine in the exhaust gas after purification is less than 1 mg/m 3 .
  • the high-efficiency catalyst fails, it is activated by hot air for 8 hours, so that the adsorbed but not completely oxidized substances, such as elemental phosphorus, phosphine, phosphorus trioxide, hydrogen sulfide, are completely oxidized, then activated by steam for 4h, then washed with water, then It is heated to 110 ° C with steam and finally reconstituted after drying with hot air for 48 h.
  • the diatomaceous earth was immersed in an aluminum nitrate solution with a mass concentration of 0.4% for 20 hours, aged for another 18 hours, calcined at 65 CTC for 8 hours, and finally dried at 110 ° C for 2 hours to obtain a high-efficiency catalyst;
  • the volume of oxygen in the exhaust gas obtained is 0.5%, and the exhaust gas is passed from bottom to top at a rate of 400 m 3 (gas volume) / m 3 (catalyst volume) .h, in the containing step ( 1)
  • the catalytic oxidation of the obtained high-efficiency catalyst is carried out in a fixed bed for purification reaction at a reaction temperature of 50 ° C.
  • phosphorus and sulfur impurities are catalytically oxidized, and the oxidized products such as phosphorus pentoxide, phosphorus trioxide, sulfur, etc. are adsorbed in
  • the gas is cooled to obtain a carbon chemical raw material gas.
  • the content of typical impurities such as phosphorus, sulfur and fluorine in the exhaust gas after purification is less than 1 mg/m 3 .
  • the high-efficiency catalyst after the high-efficiency catalyst fails, it is activated by hot air for 5 hours, and the adsorbed but not completely oxidized substances such as elemental phosphorus, phosphine, phosphorus trioxide and hydrogen sulfide are completely oxidized, and then activated by steam for 3.5 hours, and then washed with water. It is then heated to 95 ° C with steam and finally reconstituted with hot air for 40 h.
  • the activated carbon was immersed in a sodium carbonate solution with a mass concentration of 7% for 10 h, and then aged for 20 h, calcined at 450 ° C for 10 h, and finally dried at 11 CTC for 8 h to obtain a high-efficiency catalyst;
  • the oxygen content in the exhaust gas is 0.8%, and the exhaust gas is passed at a rate of 300 m 3 (gas volume) / m 3 (catalyst volume) ⁇ 1 ⁇ , which is highly efficient in the step (1).
  • the catalyst is catalytically oxidized in a fixed bed for purification reaction, the reaction temperature is 100 ° C, and the purified gas is cooled to obtain a carbon chemical raw material gas.
  • the content of typical impurities such as phosphorus, sulfur and fluorine in the exhaust gas after purification is less than 1 mg/m 3 .
  • the high-efficiency catalyst after the high-efficiency catalyst fails, it is activated by hot air for 5 hours, and the adsorbed but not completely oxidized substances, such as elemental phosphorus, phosphine, phosphorus trioxide and hydrogen sulfide, are completely oxidized, then activated by steam for 3 hours, then washed with water, then It is heated to 100 ° C with steam and finally activated by drying with hot air for 30 h.
  • the adsorbed but not completely oxidized substances such as elemental phosphorus, phosphine, phosphorus trioxide and hydrogen sulfide
  • Example 6 The activated alumina was immersed for 14 h with a cerium nitrate solution having a mass concentration of 0.35%, aged for another 24 hours, calcined at 350 ° C for llh, and finally dried at 110 ° C for 8 h to obtain a high-efficiency catalyst;
  • the oxygen content in the exhaust gas obtained is 3%, and the exhaust gas is introduced at a rate of 400 m 3 (gas volume) / m 3 (catalyst volume), in the high-efficiency catalyst containing the step (1).
  • the catalytic oxidation fixed bed is subjected to a purification reaction, the reaction temperature is 90 ° C, and the purified gas is cooled to obtain a carbon chemical raw material gas.
  • the content of typical impurities such as phosphorus, sulfur and fluorine in the exhaust gas after purification is less than 1 mg/m 3 .
  • the zeolite was impregnated with a ferrous sulfate solution having a mass concentration of 0.4% for 16 hours, aged for another 18 hours, calcined at 65 CTC for 6 hours, and finally dried at 110 ° C for 3 hours to obtain a high-efficiency catalyst;
  • the oxygen content in the exhaust gas obtained is 1%, and the exhaust gas is introduced at a rate of 500 m 3 (gas volume) / m 3 (catalyst volume) in the high-efficiency catalyst containing the step (1).
  • the catalytic oxidation fixed bed is subjected to a purification reaction, the reaction temperature is 100 ° C, and the purified gas is cooled to obtain a carbon chemical raw material gas.
  • the content of typical impurities such as phosphorus, sulfur and fluorine in the exhaust gas after purification is less than 1 mg/m 3 .
  • the high-efficiency catalyst after the high-efficiency catalyst fails, it is activated by hot air for 5 hours, and the adsorbed but not completely oxidized substances such as elemental phosphorus, phosphine, phosphorus trioxide and hydrogen sulfide are completely oxidized, then activated by steam for 4 hours, then washed with water, then It is heated to 110 ° C with steam and finally re-used after drying with hot air for 28 h.
  • the activated carbon is immersed in a sodium hydroxide solution with a concentration of 0.5% for 22 hours, aged for another 20 hours, calcined at 450 ° C for 10 hours, and finally dried at 110 ° C for 5 hours to obtain a high-efficiency catalyst;
  • the volume of oxygen in the exhaust gas obtained is 2%, and the exhaust gas is introduced at a rate of 400 m 3 (gas volume) / m 3 (catalyst volume) in the high-efficiency catalyst containing the step (1).
  • the catalytic oxidation fixed bed is subjected to a purification reaction, the reaction temperature is 90 ° C, and the purified gas is cooled to obtain a carbon chemical raw material gas.
  • the content of typical impurities such as phosphorus, sulfur and fluorine in the exhaust gas after purification is less than 1 mg/m 3 .
  • the high-efficiency catalyst after the high-efficiency catalyst fails, it is activated by hot air for 8 hours to make adsorbed but not completely oxidized substances.
  • elemental phosphorus, phosphine, phosphorus trioxide and hydrogen sulfide are completely oxidized, and then activated by steam for 4 hours, then washed with water, then heated to 110 ° C with steam, and finally activated by drying with hot air for 48 hours.
  • the activated carbon is immersed in a copper acetate solution with a mass concentration of 0.2% for 21 hours, aged for another 24 hours, calcined at 650 ° C for 12 hours, and finally dried at 110 ° C for 7 hours to obtain a high-efficiency catalyst;
  • the oxygen content in the exhaust gas obtained is 1.2%, and the exhaust gas is introduced at a rate of 600 m 3 (gas volume) / m 3 (catalyst volume) ⁇ 1 ⁇ , which is highly efficient in the step (1).
  • the catalyst is catalytically oxidized in a fixed bed for purification reaction, the reaction temperature is 100 ° C, and the purified gas is cooled to obtain a carbon chemical raw material gas.
  • the content of typical impurities such as phosphorus, sulfur and fluorine in the exhaust gas after purification is less than 1 mg/m 3 .
  • the diatomaceous earth was immersed in an aluminum nitrate solution with a mass concentration of 0.55% for 6 hours, then immersed in a lead chloride solution having a mass concentration of 0.25% for 10 hours, aged for another 24 hours, and then calcined at 350 ° C for 12 hours. Finally, drying at 11CTC for 4h to obtain a high-efficiency catalyst;
  • the oxygen content in the exhaust gas obtained is 2.5%, and the exhaust gas is introduced at a rate of 600 m 3 (gas volume) / m 3 (catalyst volume) ⁇ 1 ⁇ , which is highly efficient in the step (1).
  • the catalyst is catalytically oxidized in a fixed bed for purification reaction, the reaction temperature is 100 ° C, and the purified gas is cooled to obtain a carbon chemical raw material gas.
  • the content of typical impurities such as phosphorus, sulfur and fluorine in the exhaust gas after purification is less than 1 mg/m 3 .
  • the high-efficiency catalyst after the high-efficiency catalyst fails, it is activated by hot air for 4 hours, so that the adsorbed but not completely oxidized substances, such as elemental phosphorus, phosphine, phosphorus trioxide, hydrogen sulfide, are completely oxidized, then activated by steam for 4h, then washed with water, then It is heated to 95 ° C with steam and finally reconstituted after drying with hot air for 48 h.
  • the adsorbed but not completely oxidized substances such as elemental phosphorus, phosphine, phosphorus trioxide, hydrogen sulfide

Abstract

一种矿热熔融电炉尾气催化氧化净化的方法，先用浸渍液对催化剂载体进行浸渍，再陈化后，焙烧，最后干燥制得高效催化剂；然后将矿热熔融电炉尾气用含碱的水溶液洗涤，碱洗后的尾气升温预热；调节尾气中氧体积含量，将尾气以一定速度通入，在含有高效催化剂的催化氧化固定床进行净化反应，净化后气体经冷却，即得到一碳化工原料气。

Description

一种矿热熔融电炉尾气催化氧化净化的方法 技术领域
本发明涉及一种矿热熔融电炉尾气催化氧化净化的方法。
背景技术
碳一化产品是重要的有机化工原料。 随着石油资源的减少和价格的不断上 涨，碳一化产品替代石化产品应用范围和数量不断扩大， 碳一化工在各国经济中 的地位愈来愈显重要。 目前， 碳一化工已成为世界许多国家研究和开发的热点。 新产品、 新工艺、 新触媒层出不穷， 一氧化碳几乎变成与石油化工中乙烯、 丙烯 等基本化工原料等量齐观的化工原料。随着一碳化工技术发展， 尤其在一氧化碳 羰基合成技术方面所获得的成果， 一氧化碳羰基合成制造甲酸甲酯、二甲醚、醋 酸、 甲醇、 碳酸二甲酯等各种极有经济价值的有机化合物成为可能。
工业废气中一氧化碳丰富，矿热熔融电炉中 CO更是值得加以利用。矿热熔融 电炉化工利用时， 首先应做好净化提纯。 如能利用含一氧化碳 30〜90%的还原性 矿热熔融电炉尾气作为制取一碳化工产品的原料， 必须首先获得高纯度的 CO气。 显然，矿热熔融电炉尾气中杂质的存在大大限制了该气体的有效利用， 为了保证 产品质量和后续综合利用工艺的顺利进行， 必须对其进行净化预处理。 以矿热熔 融电炉尾气作为原料气制取一碳化工产品还可改变目前矿热熔融电炉生产因成 本过高， 在市场上竞争无力的状况， 实现节能减排， 节能降耗， 清洁化生产。 但 像矿热熔融电炉尾气这样富含一氧化碳的宝贵资源，至今其应用仅局限于烘干原 料， 大部分矿热熔融电炉尾气都直接燃烧放空， 其限制因素就在于矿热熔融电炉 尾气含有影响其羰基合成的杂质， 即矿热熔融电炉尾气净化问题没有得到解决， 尤其是矿热熔融电炉尾气中磷的去除，直接对一氧化碳羰基化合催化剂有严重影 响。
由于矿热熔融电炉还原矿石时反应是在高温下发生的还原反应，所以矿热熔 融电炉尾气中的杂质主要以还原态存在。 例如： 磷主要是单质磷 (P4)和磷化氢 (PH3)， 硫主要是硫化氢 (H2S)和有机硫， 氟主要是氟化氢 (HF)、 氟化硅 (SiF4)等。 针对还原性工业废气中杂质的存在形式， 目前工业上主要采用水洗和碱洗两种方 法进行净化： 1、 水洗： 对还原性废气进行降温、 除尘， 同时可除去氟化物和一部分单质 磷、 磷化氢、 氟化氢和硫化氢。 由于磷的蒸汽压随温度的降低而迅速降低， 所以 水洗降温后尾气中一些磷因冷凝除去， 而硫化氢因溶解在水中可除去一部分。
2、 碱洗： 用 0. 8〜10%的氢氧化钠 （NaOH) 溶液通过化学反应除去大量的二 氧化碳 （co2)、 硫化氢、 氟化氢等酸性气体。
上述方法存在的主要问题是： 对单质的去除效率较低， 脱除不完全， 对使用 各种触媒的场合会造成触媒毒害， 无法满足一碳化工对原料气的要求。
发明内容
本发明克服了现有技术的不足， 旨在解决矿热融电炉尾气的净化预处理难 题，提供一种矿热熔融电炉尾气催化氧化净化的方法，使净化矿热融电炉尾气后， 其中硫、磷、氟等典型杂质浓度均小于 lmg/m3， 使之达到制取高附加值的一碳化 工产品原料气的要求。
矿热熔融电炉尾气属还原性工业废气， 主要成份为： CO 85〜95% (V/V)， C02 3〜7% (V/V)， H2 1〜8% (V/V)， N2 2〜5% (V/V)， 02 0. 2〜1% (V/V)， 总磷 1000— 5000mg/m3, H2S 1000〜5000mg/m3， HF 300〜4000mg/m3。
碱洗能除去矿热熔融电炉尾气中的呈单质状态存在的典型污染物，并将单质 状态典型污染物由气溶胶单质状态转化为气体状态，有利于采用催化氧化净化方 法除去； 碱洗后的转化气体经升温后进入催化氧化固定床， 气体状态的典型杂质 利用矿热熔融电炉尾气中微量氧气在催化剂表面被氧化后除去。
矿热熔融电炉尾气用含碱的水溶液洗涤除去尾气中氟化硅、二氧化碳和部分 单质磷等杂质， 反应过程如下：
P4 + 3Na0H + 3H20 → 3Na¾P04 + PH3
3SiF4 + 4¾0 → 2H2SiF6+ Si02 · H20
C02 + 2Na0H → N¾C03 + H20
HF + NaOH → NaF + H20
含 N¾C03的洗涤液经苛化处理回收 NaOH， 返回***循环使用。 经上述碱洗 处理后尾气仍不能达到制取化工产品对原料气的要求。为了进一步除去磷、硫化 物等杂质，在以上碱洗的基础上， 本发明采用了矿热熔融电炉尾气催化氧化高效 净化技术。 碱洗后的尾气通过预热器预热， 并自下而上经过反应器， 反应器内填充了高 效催化剂，单质磷、磷化氢、氟化氢杂质被催化氧化。其中硫被催化氧化反应式：
2H2S + 02 催化剂 > 2S + 2¾0 单质磷被催化氧化反应式：
P4 + 302 催化剂 > 2P203
磷化氢具有较强的还原性， 尾气中低价态的 P与高价金属离子 （Me3+) 发生 氧化还原反应， P 被氧化转化为磷酸， 金属离子 （Me3+) 被还原， 被还原的金属 离子又被气体中的 02氧化， 实现催化剂的循环使用， 主要反应方程如下：
PH3 (g) + 8Me3+ (s) + 4H20 (1) → 8Me2+ (aq) + H3P04 (aq) + 8H+ (aq)
02 (g) + 4Me2+ (aq) + 2H20 (1) → 4Me3+ (s) + 40H" (aq) 总反应为：
PH3 (g) + 202 (g) 催侧 ) H3P04 (aq) 氟被催化氧化反应式：
MenOm + HF→ MeFm + H20
式中 MenOm 催化剂中添加的金属氧化物。
从反应器中排出的净化尾气经冷却塔冷却至 30°C后， 即得到合格的一碳化 工原料气。
该方法的具体步骤如下：
( 1 )用浸渍液对催化剂载体进行浸渍 10〜24h，再陈化 18〜24h后，在 350〜 650°C焙烧 6〜12h， 最后在 110°C下干燥 2〜8h制得高效催化剂；
( 2 ) 矿热熔融电炉尾气用含碱的水溶液洗涤， 碱洗后的尾气升温预热到 70〜110°C ;
( 3 ) 调节步骤 （2 ) 所得的尾气中氧体积含量为 0. 5〜3%， 将尾气以 300〜 600m3 (气体体积) /m3 (催化剂体积) .h的速度自下而上通入， 在含有步骤（1 )所得 高效催化剂的催化氧化固定床进行净化反应， 反应温度为 50〜100°C， 净化后气 体经冷却， 即得到一碳化工原料气。
所述步骤 （1 ) 的催化剂载体是活性氧化铝、 沸石、 活性炭或硅藻土。
所述步骤 （1 ) 的浸渍液为质量浓度为 0. 25〜7%的氢氧化钠、 氢氧化钾、 硫 酸亚铁、 氯化铅、 硝酸铝、 碳酸钠、 醋酸铜或硝酸镧溶液。
所述催化剂载体是活性氧化铝时用质量浓度为 0. 35%的硝酸镧溶液浸渍。 所述催化剂载体是沸石时用质量浓度为 0. 4%的硫酸亚铁溶液浸渍。
所述催化剂载体是活性炭时用质量浓度为 0. 5%的氢氧化钾溶液浸渍。 所述催化剂载体是活性炭时用质量浓度为 0. 5%的氢氧化钠溶液浸渍。 所述催化剂载体是活性炭时用质量浓度为 0. 2%的醋酸铜溶液浸渍。
所述催化剂载体是活性炭时用质量浓度为 7%的碳酸钠溶液浸渍。
所述催化剂载体是硅藻土时先用质量浓度为 0. 55%的硝酸铝溶液浸渍后， 再 用质量浓度为 0. 25%的氯化铅溶液浸渍。
所述步骤 （3 ) 的高效催化剂失效后用热空气活化 4〜8h， 使被吸附但未完 全氧化的物质， 如单质磷、 磷化氢、 三氧化二磷、 硫化氢彻底氧化， 再用水蒸汽 活化 2〜4h， 然后水洗， 接着用蒸汽加热至 95〜110°C， 最后用热空气干燥活化 24〜48h后即可循环使用。
本发明中催化氧化净化可以采用两固定床并联***，其中一个固定床失效后 转入催化剂再生， 另一固定床继续净化， 催化剂再生时间为矿热熔融电炉尾气催 化氧化净化时间的 1/2〜1/3， 可保证整个***连续运行。
本发明是先将矿热熔融电炉尾气经碱洗除去矿热熔融电炉尾气中的呈单质 状态存在的典型污染物，并将单质状态典型污染物由气溶胶单质状态转化为气体 状态，碱洗后的转化气体经升温后进入催化氧化固定床， 气体状态的典型杂质利 用矿热熔融电炉尾气中微量氧气在催化剂表面被氧化后除去， 经上述方法净化 后，矿热熔融电炉尾气中典型杂质含量均小于 lmg/m3。本发明中采用的催化剂能 大幅提高矿热熔融电炉尾气的净化效率， 催化剂易再生， 利用率高， 工艺流程简 单， 净化成本低。
影响净化效率的主要因素是反应温度，尾气中氧含量及载气速度， 其影响规 律如下：
( 1 ) 在催化剂存在下， 氧化反应可在较低温度 50〜100°C下进行。 反应温 度升高有利于净化效率的提高， 当反应温度大于 100°C， 再升高温度， 净化效率 的提高已不明显；
( 2 ) 控制矿热熔融电炉尾气中氧含量为 0. 5〜3%， 随着氧含量的增加净化 效率提高； (3)载气流速在 300〜600m3 (气体体积) /m3(催化剂体积） ·1ι范围内， 降低载 气流速可提高净化效果， 但流速降至 300m3 (气体体积) /m3(催化剂体积) .h后， 净 化效果无已显著提高。
在本发明提出的工艺条件下， 催化剂对 P¾吸附容量为 12〜28%， 对单质磷 吸附容量为 24〜56%， 对硫化氢吸附容量为 11〜25%， 对氟化氢吸附容量为 10〜 22%, 净化后矿热熔融电炉尾气中硫化氢、 总磷、 氟化氢等典型杂质含量均小于 lmg/m3, 达到生产一碳化工产品对原料气的要求。
本发明与现有技术相比具有以下的优点：
(1) 净化效率高、 经净化后的矿热熔融电炉尾气达到生产一碳化工对原料 气的要求；
(2) 工艺流程简单， 催化剂价廉、 易得；
(3) 中毒或失效后的催化剂易于再生， 催化剂经多次再生后催化性能基本 不变， 利用率高， 降低了净化成本；
(4) 通过额外补氧增加尾气中氧含量以及提高尾气温度的措施大大提高了 净化效率；
(5) 整个***在正压下操作， 可保证操作的安全性。
附图说明
图 1是本发明的工艺流程图。
具体实施方式
下面将结合实施例进一步阐明本发明的内容，但这些实例并不限制本发明的 保护范围。
实施例 1
(1)用质量浓度为 0.25%的硝酸镧溶液对活性氧化铝进行浸渍 20h， 再陈化 24h后，在 50CTC下放入马弗炉焙烧 6h，最后在 11CTC下干燥 4h制得高效催化剂；
(2)矿热熔融电炉尾气用质量浓度为 0.8〜10%的 NaOH水溶液洗涤除去磷， 碱洗后的尾气升温预热到 80°C;
(3) 调节步骤 （2) 所得的尾气中氧体积含量为 0.5%， 将尾气以 500m3 (气 体体积 )/m3(催化剂体积) .h 的速度自下而上通入， 在含有步骤 （1) 所得高效催 化剂的催化氧化固定床进行净化反应， 反应温度为 80°C， 此时， 磷化氢被催化 氧化， 氧化后的产物五氧化二磷、三氧化二磷等被吸附在催化剂表面， 净化后气 体经冷却， 即得到一碳化工原料气。 净化后尾气中磷、 硫、 氟等典型杂质含量均 小于 lmg/m3。
其中， 高效催化剂失效后用热空气活化 4h， 使被吸附但未完全氧化的物质， 如单质磷、 磷化氢、 三氧化二磷、 硫化氢彻底氧化， 再用水蒸汽活化 2h， 然后 水洗， 接着用蒸汽加热至 110°C， 最后用热空气干燥活化 24h后即可循环使用。
实施例 2
(1) 用质量浓度为 0.3%的硫酸亚铁溶液对沸石进行浸渍 24h， 再陈化 24h 后， 在 55CTC焙烧 6h， 最后在 110°C下干燥 4h制得高效催化剂；
(2) 矿热熔融电炉尾气用含碱的水溶液洗涤除去二氧化碳和部分磷、 硫、 氟杂质， 碱洗后的尾气升温预热到 70°C;
(3) 调节步骤 （2) 所得的尾气中氧体积含量为 0.5%， 将尾气以 500m3 (气 体体积 )/m3(催化剂体积) .h 的速度自下而上通入， 在含有步骤 （1) 所得高效催 化剂的催化氧化固定床进行净化反应， 反应温度为 70°C， 此时磷、 硫杂质被催 化氧化， 氧化后的产物五氧化二磷、 三氧化二磷、 硫等被吸附在催化剂表面， 净 化后气体经冷却， 即得到一碳化工原料气。 净化后尾气中磷、 硫、 氟等典型杂质 含量均小于 lmg/m3。
其中， 高效催化剂失效后用热空气活化 6h， 使被吸附但未完全氧化的物质， 如单质磷、 磷化氢、 三氧化二磷、 硫化氢彻底氧化， 再用水蒸汽活化 3h， 然后 水洗， 接着用蒸汽加热至 100°C， 最后用热空气干燥活化 32h后即可循环使用。
实施例 3
(1)用质量浓度为 0.5%的氢氧化钾溶液对活性炭进行浸渍 18h，再陈化 24h 后， 在 350°C焙烧 12h， 最后在 110°C下干燥 6h制得高效催化剂；
(2) 矿热熔融电炉尾气用含碱的水溶液洗涤除去二氧化碳和部分磷、 硫、 氟杂质， 碱洗后的尾气升温预热到 110°C;
(3) 调节步骤 （2) 所得的尾气中氧体积含量为 0.5%， 将尾气以 600m3 (气 体体积 )/m3(催化剂体积) .h 的速度自下而上通入， 在含有步骤 （1) 所得高效催 化剂的催化氧化固定床进行净化反应， 反应温度为 100°C， 此时磷、 硫杂质被催 化氧化， 氧化后的产物五氧化二磷、 三氧化二磷、 硫等被吸附在催化剂表面， 净 化后气体经冷却， 即得到一碳化工原料气。 净化后尾气中磷、 硫、 氟等典型杂质 含量均小于 lmg/m3。 其中， 高效催化剂失效后用热空气活化 8h， 使被吸附但未完全氧化的物质， 如单质磷、 磷化氢、 三氧化二磷、 硫化氢彻底氧化， 再用水蒸汽活化 4h， 然后 水洗， 接着用蒸汽加热至 110°C， 最后用热空气干燥活化 48h后即可循环使用。
实施例 4
(1) 用质量浓度为 0.4%的硝酸铝溶液对硅藻土进行浸渍 20h， 再陈化 18h 后， 在 65CTC焙烧 8h， 最后在 110°C下干燥 2h制得高效催化剂；
(2) 矿热熔融电炉尾气用含碱的水溶液洗涤除去二氧化碳和部分磷、 硫、 氟杂质， 碱洗后的尾气升温预热到 10CTC;
(3) 调节步骤 （2) 所得的尾气中氧体积含量为 0.5%， 将尾气以 400m3 (气 体体积 )/m3(催化剂体积) .h 的速度自下而上通入， 在含有步骤 （1) 所得高效催 化剂的催化氧化固定床进行净化反应， 反应温度为 50°C， 此时磷、 硫杂质被催 化氧化， 氧化后的产物五氧化二磷、 三氧化二磷、 硫等被吸附在催化剂表面， 净 化后气体经冷却， 即得到一碳化工原料气。 净化后尾气中磷、 硫、 氟等典型杂质 含量均小于 lmg/m3。
其中， 高效催化剂失效后用热空气活化 5h， 使被吸附但未完全氧化的物质， 如单质磷、 磷化氢、 三氧化二磷、 硫化氢彻底氧化， 再用水蒸汽活化 3.5h， 然 后水洗， 接着用蒸汽加热至 95°C， 最后用热空气干燥活化 40h后即可循环使用。
实施例 5
(1)用质量浓度为 7%的碳酸钠溶液对活性炭进行浸渍 10h， 再陈化 20h后， 在 450°C焙烧 10h， 最后在 11CTC下干燥 8h制得高效催化剂；
(2) 矿热熔融电炉尾气用含碱的水溶液洗涤， 碱洗后的尾气升温预热到
90 °C;
(3) 调节步骤 （2) 所得的尾气中氧体积含量为 0.8%， 将尾气以 300m3 (气 体体积 )/m3(催化剂体积) ·1ι 的速度通入， 在含有步骤 （1) 所得高效催化剂的催 化氧化固定床进行净化反应， 反应温度为 100°C， 净化后气体经冷却， 即得到一 碳化工原料气。 净化后尾气中磷、 硫、 氟等典型杂质含量均小于 lmg/m3。
其中， 高效催化剂失效后用热空气活化 5h， 使被吸附但未完全氧化的物质， 如单质磷、 磷化氢、 三氧化二磷、 硫化氢彻底氧化， 再用水蒸汽活化 3h， 然后 水洗， 接着用蒸汽加热至 100°C， 最后用热空气干燥活化 30h后即可循环使用。
实施例 6 (1)用质量浓度为 0.35%的硝酸镧溶液对活性氧化铝进行浸渍 14h， 再陈化 24h后， 在 350°C焙烧 llh， 最后在 110°C下干燥 8h制得高效催化剂；
(2) 矿热熔融电炉尾气用含碱的水溶液洗涤， 碱洗后的尾气升温预热到
70 °C;
(3) 调节步骤 （2) 所得的尾气中氧体积含量为 3%， 将尾气以 400m3 (气体 体积) /m3(催化剂体积) 的速度通入， 在含有步骤 （1) 所得高效催化剂的催化 氧化固定床进行净化反应， 反应温度为 90°C， 净化后气体经冷却， 即得到一碳 化工原料气。 净化后尾气中磷、 硫、 氟等典型杂质含量均小于 lmg/m3。
实施例 7
(1) 用质量浓度为 0.4%的硫酸亚铁溶液对沸石进行浸渍 16h， 再陈化 18h 后， 在 65CTC焙烧 6h， 最后在 110°C下干燥 3h制得高效催化剂；
(2) 矿热熔融电炉尾气用含碱的水溶液洗涤， 碱洗后的尾气升温预热到 110°C;
(3) 调节步骤 （2) 所得的尾气中氧体积含量为 1%， 将尾气以 500m3 (气体 体积) /m3(催化剂体积) 的速度通入， 在含有步骤 （1) 所得高效催化剂的催化 氧化固定床进行净化反应， 反应温度为 100°C， 净化后气体经冷却， 即得到一碳 化工原料气。 净化后尾气中磷、 硫、 氟等典型杂质含量均小于 lmg/m3。
其中， 高效催化剂失效后用热空气活化 5h， 使被吸附但未完全氧化的物质， 如单质磷、 磷化氢、 三氧化二磷、 硫化氢彻底氧化， 再用水蒸汽活化 4h， 然后 水洗， 接着用蒸汽加热至 110°C， 最后用热空气干燥活化 28h后即可循环使用。
实施例 8
(1)用质量浓度为 0.5%的氢氧化钠溶液对活性炭进行浸渍 22h，再陈化 20h 后， 在 450°C焙烧 10h， 最后在 110°C下干燥 5h制得高效催化剂；
(2) 矿热熔融电炉尾气用含碱的水溶液洗涤， 碱洗后的尾气升温预热到 110°C;
(3) 调节步骤 （2) 所得的尾气中氧体积含量为 2%， 将尾气以 400m3 (气体 体积) /m3(催化剂体积) 的速度通入， 在含有步骤 （1) 所得高效催化剂的催化 氧化固定床进行净化反应， 反应温度为 90°C， 净化后气体经冷却， 即得到一碳 化工原料气。 净化后尾气中磷、 硫、 氟等典型杂质含量均小于 lmg/m3。
其中， 高效催化剂失效后用热空气活化 8h， 使被吸附但未完全氧化的物质， 如单质磷、 磷化氢、 三氧化二磷、 硫化氢彻底氧化， 再用水蒸汽活化 4h， 然后 水洗， 接着用蒸汽加热至 110°C， 最后用热空气干燥活化 48h后即可循环使用。
实施例 9
(1) 用质量浓度为 0.2%的醋酸铜溶液对活性炭进行浸渍 21h， 再陈化 24h 后， 在 650°C焙烧 12h， 最后在 110°C下干燥 7h制得高效催化剂；
(2) 矿热熔融电炉尾气用含碱的水溶液洗涤， 碱洗后的尾气升温预热到 110°C;
(3) 调节步骤 （2) 所得的尾气中氧体积含量为 1.2%， 将尾气以 600m3 (气 体体积 )/m3(催化剂体积) ·1ι 的速度通入， 在含有步骤 （1) 所得高效催化剂的催 化氧化固定床进行净化反应， 反应温度为 100°C， 净化后气体经冷却， 即得到一 碳化工原料气。 净化后尾气中磷、 硫、 氟等典型杂质含量均小于 lmg/m3。
实施例 10
(1)用质量浓度为 0.55%的硝酸铝溶液对硅藻土进行浸渍 6h后， 再用质量 浓度为 0.25%的氯化铅溶液浸渍 10h， 再陈化 24h后， 在 350°C焙烧 12h， 最后在 11CTC下干燥 4h制得高效催化剂；
(2) 矿热熔融电炉尾气用含碱的水溶液洗涤， 碱洗后的尾气升温预热到
70 °C;
(3) 调节步骤 （2) 所得的尾气中氧体积含量为 2.5%， 将尾气以 600m3 (气 体体积 )/m3(催化剂体积) ·1ι 的速度通入， 在含有步骤 （1) 所得高效催化剂的催 化氧化固定床进行净化反应， 反应温度为 100°C， 净化后气体经冷却， 即得到一 碳化工原料气。 净化后尾气中磷、 硫、 氟等典型杂质含量均小于 lmg/m3。
其中， 高效催化剂失效后用热空气活化 4h， 使被吸附但未完全氧化的物质， 如单质磷、 磷化氢、 三氧化二磷、 硫化氢彻底氧化， 再用水蒸汽活化 4h， 然后 水洗， 接着用蒸汽加热至 95°C， 最后用热空气干燥活化 48h后即可循环使用。

Claims

权利 要求书
1、 一种矿热熔融电炉尾气催化氧化净化的方法， 其特征在于经过下列各步 骤：
( 1 )用浸渍液对催化剂载体进行浸渍 10〜24h，再陈化 18〜24h后，在 350〜 650°C焙烧 6〜12h， 最后在 110°C下干燥 2〜8h制得高效催化剂；
( 2 ) 矿热熔融电炉尾气用含碱的水溶液洗涤， 碱洗后的尾气升温预热到 70〜110°C ;
( 3 ) 调节步骤 （2 ) 所得的尾气中氧体积含量为 0. 5〜3%， 将尾气以 300〜 600m3 (气体体积) /m3 (催化剂体积) .h的速度自下而上通入， 在含有步骤（1 )所得 高效催化剂的催化氧化固定床进行净化反应， 反应温度为 50〜100°C， 净化后气 体经冷却， 即得到一碳化工原料气。
2、 根据权利要求 1所述的矿热熔融电炉尾气催化氧化净化的方法， 其特征 在于： 所述步骤 （1 ) 的催化剂载体是活性氧化铝、 沸石、 活性炭或硅藻土。
3、 根据权利要求 1所述的矿热熔融电炉尾气催化氧化净化的方法， 其特征 在于： 所述步骤 （1 ) 的浸渍液为质量浓度为 0. 25〜7%的氢氧化钠、 氢氧化钾、 硫酸亚铁、 氯化铅、 硝酸铝、 碳酸钠、 醋酸铜或硝酸镧溶液。
4、 根据权利要求 2所述的矿热熔融电炉尾气催化氧化净化的方法， 其特征 在于： 所述催化剂载体是活性氧化铝时用质量浓度为 0. 35%的硝酸镧溶液浸渍。
5、 根据权利要求 2所述的矿热熔融电炉尾气催化氧化净化的方法， 其特征 在于： 所述催化剂载体是沸石时用质量浓度为 0. 4%的硫酸亚铁溶液浸渍。
6、 根据权利要求 2所述的矿热熔融电炉尾气催化氧化净化的方法， 其特征 在于： 所述催化剂载体是活性炭时用质量浓度为 0. 5%的氢氧化钠或氢氧化钾溶 液浸渍。
7、 根据权利要求 2所述的矿热熔融电炉尾气催化氧化净化的方法， 其特征 在于： 所述催化剂载体是活性炭时用质量浓度为 0. 2%的醋酸铜溶液浸渍。
8、 根据权利要求 2所述的矿热熔融电炉尾气催化氧化净化的方法， 其特征 在于： 所述催化剂载体是活性炭时用质量浓度为 7%的碳酸钠溶液浸渍。
9、 根据权利要求 2所述的矿热熔融电炉尾气催化氧化净化的方法， 其特征 在于： 所述催化剂载体是硅藻土时先用质量浓度为 0. 55%的硝酸铝溶液浸渍后， 再用质量浓度为 0. 25%的氯化铅溶液浸渍。
10、根据权利要求 1所述的矿热熔融电炉尾气催化氧化净化的方法， 其特征 在于： 所述步骤 （3 ) 的高效催化剂失效后用热空气活化 4〜8h， 再用水蒸汽活 化 2〜4h，然后水洗，接着用蒸汽加热至 95〜110°C，最后用热空气干燥活化 24〜 48h后即可循环使用。
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