WO2019114261A1 - 一种铜基负载型氨氧化催化剂及其制备方法 - Google Patents

一种铜基负载型氨氧化催化剂及其制备方法 Download PDF

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WO2019114261A1
WO2019114261A1 PCT/CN2018/094518 CN2018094518W WO2019114261A1 WO 2019114261 A1 WO2019114261 A1 WO 2019114261A1 CN 2018094518 W CN2018094518 W CN 2018094518W WO 2019114261 A1 WO2019114261 A1 WO 2019114261A1
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copper
ammonia
based supported
cuo
catalyst
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French (fr)
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李俊华
郭晶晶
王驰中
陈建军
彭悦
郝吉明
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清华大学
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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J29/00—Catalysts comprising molecular sieves
    • B01J29/04—Catalysts comprising molecular sieves having base-exchange properties, e.g. crystalline zeolites
    • B01J29/06—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof
    • B01J29/40—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of the pentasil type, e.g. types ZSM-5, ZSM-8 or ZSM-11, as exemplified by patent documents US3702886, GB1334243 and US3709979, respectively
    • B01J29/42—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of the pentasil type, e.g. types ZSM-5, ZSM-8 or ZSM-11, as exemplified by patent documents US3702886, GB1334243 and US3709979, respectively containing iron group metals, noble metals or copper
    • B01J29/46—Iron group metals or copper
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
    • B01D53/86—Catalytic processes
    • B01D53/8621—Removing nitrogen compounds
    • B01D53/8634—Ammonia
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/92—Chemical or biological purification of waste gases of engine exhaust gases
    • B01D53/94—Chemical or biological purification of waste gases of engine exhaust gases by catalytic processes
    • B01D53/9404—Removing only nitrogen compounds
    • B01D53/9436—Ammonia
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J29/00—Catalysts comprising molecular sieves
    • B01J29/04—Catalysts comprising molecular sieves having base-exchange properties, e.g. crystalline zeolites
    • B01J29/06—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof
    • B01J29/70—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of types characterised by their specific structure not provided for in groups B01J29/08 - B01J29/65
    • B01J29/72—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of types characterised by their specific structure not provided for in groups B01J29/08 - B01J29/65 containing iron group metals, noble metals or copper
    • B01J29/76—Iron group metals or copper
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J29/00—Catalysts comprising molecular sieves
    • B01J29/82—Phosphates
    • B01J29/84—Aluminophosphates containing other elements, e.g. metals, boron
    • B01J29/85—Silicoaluminophosphates [SAPO compounds]
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J37/00—Processes, in general, for preparing catalysts; Processes, in general, for activation of catalysts
    • B01J37/08—Heat treatment
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B21/00—Nitrogen; Compounds thereof
    • C01B21/02—Preparation of nitrogen
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2258/00—Sources of waste gases
    • B01D2258/01—Engine exhaust gases
    • B01D2258/012—Diesel engines and lean burn gasoline engines
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2258/00—Sources of waste gases
    • B01D2258/02—Other waste gases
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2258/00—Sources of waste gases
    • B01D2258/02—Other waste gases
    • B01D2258/0283—Flue gases
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
    • Y02A50/00—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE in human health protection, e.g. against extreme weather
    • Y02A50/20—Air quality improvement or preservation, e.g. vehicle emission control or emission reduction by using catalytic converters

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  • the invention belongs to the technical field of ammonia escape control in the field of environmental protection technology, and the target treatment object is ammonia gas which escapes after the SCR system in the exhaust gas of the fixed source flue gas and the motor vehicle (diesel vehicle), and ammonia which is discharged in the agricultural source of the aquaculture factory building.
  • Gas in particular, relates to a copper-based supported ammoxidation catalyst and a preparation method thereof.
  • Ammonia that escapes into the air can cause many degrees of harm to human health. For example, ammonia can irritate human skin tissue and respiratory tract, causing a decline in human immunity. In addition, the emission of ammonia gas will also seriously pollute the environment and cause harm to the ecological environment. Therefore, while the denitration effect basically meets the emission requirements, in order to ensure the quality of the atmospheric environment, it is necessary to further develop new environmental protection technologies, improve the ammonia conversion efficiency, and reduce the escape amount of ammonia.
  • selective catalytic oxidation (SCO) is one technology used widely, it makes the conversion of NH 3 O 2 in the reaction with catalyst N 2, thereby reducing ammonia slip and equipment The negative impact of the environment. The method is simple in operation, high in NH 3 removal rate and rapid in reaction, and is a promising method for controlling ammonia escape phenomenon. At its core is the development of catalysts.
  • the NH 3 -SCO catalyst can be classified into a noble metal catalyst, a transition metal oxide catalyst, and a metal molecular sieve catalyst depending on the active component.
  • noble metal catalysts have outstanding low-temperature activity, they have the disadvantages of high cost and poor selectivity.
  • transition metal oxide catalysts are low in cost and good in selectivity, their low-temperature activity is relatively poor; metal molecular sieve catalysts have been in NH in recent years.
  • the 3- SCO field has received extensive attention and research. The reported molecular sieve catalysts have a higher N 2 selectivity, but the temperature window is higher. These catalysts are not effective in controlling ammonia slip, and thus for an improved catalyst NH 3 -SCO demand still exists.
  • the invention also provides a preparation method of the copper-based supported ammonia oxidation catalyst, comprising the following steps:
  • the support is an oxide or molecular sieve comprising one of SiO 2 , Al 2 O 3 , TiO 2 , ZSM-5, SAPO-34 and SSZ-13.
  • the mass ratio of the CuO to the carrier is 0.1.
  • the rotary evaporator has a rotation speed of 500 r/min in step (4), a water bath temperature of 70 ° C, and an evaporation time of 2 h.
  • the drying temperature in the step (5) is 100 ° C
  • the drying time is 12 h
  • the baking temperature in the step (6) is 400 ° C
  • the baking time is 6 h.
  • the copper-based supported ammonia oxidation catalyst of the invention is used for the elimination of the ammonia escape phenomenon of the fixed source flue gas and the automobile exhaust gas, and is also suitable for the treatment of the ammonia gas discharge in the agricultural source of the aquaculture factory building. Includes the following steps:
  • the prepared copper-based supported ammonia oxidation catalyst is taken from a 40-60 mesh powder and charged into a micro fixed bed reactor at a reaction temperature of 150 to 400 ° C;
  • Ammonia gas is used as a reducing agent, nitrogen is used as a balance gas, the total flow rate of the control gas is 500 mL/min, and the space velocity is controlled to be 1.5 ⁇ 10 5 mL ⁇ g -1 ⁇ h -1 .
  • the invention Compared with the prior art, the invention has the advantages of no toxicity, high activity and high selectivity, wherein the active component CuO achieves good NH 3 conversion rate, and the carrier SSZ-13 ensures low by-product formation and improves. N 2 selectivity.
  • the CuO 0.1 /SSZ-13 ammoxidation catalyst of the present invention can achieve nearly 95% NH 3 conversion and more than 90% N 2 selectivity in the temperature range of 225-400 °C.
  • Figure 1 is a graph showing the relationship between the conversion of NH 3 and the reaction temperature of a prepared copper-based supported ammoxidation catalyst.
  • Figure 2 is a graph showing the relationship between the selectivity of the prepared copper-based supported ammoxidation catalyst N 2 and the reaction temperature.
  • the catalyst was used in the reaction condition of 400 ppm NH 3 , 10% O 2 and the equilibrium gas was N 2 , the amount of the catalyst was 0.2 g, and the reaction space velocity was 1.5 ⁇ 10 5 mL ⁇ g -1 ⁇ h -1 .
  • the sampling temperature points are: 150, 200 , 225, 250, 275, 300 , 325, 350, 400 ° C, the catalyst NH 3 conversion is shown in Figure 1, and the N 2 selectivity is shown in Figure 2. It can be seen that the ammoxidation activity of 300-400 ° C is more than 95%, and the N 2 selectivity is excellent, and the entire temperature range is above 95%.
  • the catalyst was used in the reaction condition of 400 ppm NH 3 , 10% O 2 and the equilibrium gas was N 2 , the amount of the catalyst was 0.2 g, and the reaction space velocity was 1.5 ⁇ 10 5 mL ⁇ g -1 ⁇ h -1 .
  • the sampling temperature points are: 150, 200 , 225, 250, 275, 300 , 325, 350, 400 ° C, the catalyst NH 3 conversion is shown in Figure 1, and the N 2 selectivity is shown in Figure 2. It can be seen that the ammoxidation activity of 300-400 ° C is more than 90%, and the N 2 selectivity is excellent, and the temperature range is over 90%.
  • the catalyst was used in the reaction condition of 400 ppm NH 3 , 10% O 2 and the equilibrium gas was N 2 , the amount of the catalyst was 0.2 g, and the reaction space velocity was 1.5 ⁇ 10 5 mL ⁇ g -1 ⁇ h -1 .
  • the sampling temperature points are: 150, 200 , 225, 250, 275, 300 , 325, 350, 400 ° C, the catalyst NH 3 conversion is shown in Figure 1, and the N 2 selectivity is shown in Figure 2. It can be seen that the ammoxidation activity at 225-400 °C is over 95%, and the N 2 selectivity is excellent, and the temperature range is over 90%.
  • the copper-based supported ammoxidation catalyst with molecular sieve as the carrier has excellent intermediate-low temperature NH 3 conversion, especially the CuO 0.1 /SSZ-13 catalyst, and its NH 3 conversion rate is nearly 95% at 225 ° C.
  • the N 2 selectivity is above 90% over the entire temperature range, and has the advantages of no toxicity, high activity, high selectivity and the like.

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Abstract

一种铜基负载型氨氧化催化剂，该催化剂以CuO为活性组分，催化剂表示为CuOx/M(M表示为载体)，其中负载比例x为m(CuO)/m(M)＝0.05～0.2；同时提供了铜基负载型氨氧化催化剂的制备方法；制备完成的铜基负载型氨氧化催化剂适用于固定源和移动源的氨气净化，可应用在SCR系统下游，消除氨逃逸现象，同时也适用于养殖业厂房农业源中产生排放氨气的处理。

Description

一种铜基负载型氨氧化催化剂及其制备方法 技术领域
本发明属于环保技术领域中氨逃逸控制技术领域，设计目标处理物为固定源烟气和机动车(柴油车)尾气中SCR系统后逃逸的氨气，以及养殖业厂房农业源中产生排放的氨气，具体涉及一种铜基负载型氨氧化催化剂及其制备方法。
背景技术
氨气(NH 3)是大气污染物之一。大气中氨气的排放主要来源于工业、农业、移动源等多方面。例如我们熟知的脱硝技术--氨选择性催化还原反应(NH 3-SCR)中即以氨气为还原剂还原NO x，往往因不完全反应而产生氨逃逸现象，使未反应的氨直接排放到大气中；同时随着SCR脱硝催化剂中毒、老化，进一步使得NH 3使用率降低，增大逃逸量。此外，养殖业厂房等农业源中同样也会产生排放氨气。逃逸到空气中的氨气会对人体的健康造成诸多不同程度的危害，例如：氨气会刺激腐蚀人体皮肤组织和呼吸道，造成人免疫力下降。此外，氨气的排放还会严重污染环境，对生态环境造成危害。因此，在脱硝效果基本达到排放要求的同时，为了保障大气环境质量，还需要进一步发展新的环保技术，提高氨转化效率，削减氨的逃逸量。在氨逃逸控制技术中，选择性催化氧化技术(SCO)是应用比较广泛的技术之一，它使NH 3在催化剂作用下与O 2反应转化成N 2，由此来降低氨逃逸对设备与环境所带来的负面影响。该方法操作简便、NH 3去除率高且反应迅速，是治理氨逃逸现象非常有前景的一种方法。其核心是催化剂的研发。
NH 3-SCO催化剂根据活性组分的不同，可以分为贵金属催化剂、过渡金属氧化物催化剂和金属分子筛催化剂。贵金属催化剂虽然具有突出的低温活性，但存在成本较贵、选择性差等缺陷；过渡金属氧化物催化剂虽成本低廉，选择性较好，但其低温活性相对较差；金属分子筛催化剂近些年来在NH 3-SCO领域受到广泛的关注与研究，已报道的金属分子筛催化剂虽然N 2选择性较好，但温度窗口偏高。这些催化剂在氨逃逸控制中并不是高效的，因此对于改进NH 3-SCO催化剂仍然存在着市场需求。
发明内容
为了克服现有NH 3-SCO领域催化剂的缺陷，本发明的目的在于提出一种铜基负载型氨氧化催化剂及其制备方法，该催化剂可用于消除固定源和机动车尾气SCR系统产生的氨逃逸现象，处理养殖业厂房农业源所产生排放的氨气，具有无毒性、高活性及高选择性等优点，能很好满足实际应用要求。
为了实现上述目的，本发明采用的技术方案是：
一种铜基负载型氨氧化催化剂，以CuO为活性组分，催化剂可表示为CuO x/M(M表示为载体)，其中x＝m(CuO)/m(M)＝0.05～0.2。
本发明同时提供了所述铜基负载型氨氧化催化剂的制备方法，包括如下步骤：
(1)按照CuO/M(M表示为载体)质量比0.05～0.2的比例称取一定量的铜盐和载体粉末备用；
(2)将称取好的铜盐溶解于去离子水中；
(3)在铜盐完全溶解后，在其中加入称取好的载体粉末，并在室温下搅拌5min；
(4)停止搅拌后，将所得溶液转移至旋蒸瓶，利用旋转蒸发仪以300～500r/min的转速及60～80℃水浴温度蒸发2～4h，使溶剂蒸发；
(5)将蒸发后所得物质放入100～120℃的烘箱内干燥10～14h，得到半成品；
(6)将所得到的半成品放入马弗炉，以10℃·min -1的速率升温至400～600℃条件下保温焙烧6～8h，最后炉内自然冷却，制得铜基负载型氨氧化催化剂。
优选地，所述铜盐为硝酸铜或硝酸铜。
优选地，所述载体为氧化物或分子筛，包括SiO 2、Al 2O 3、TiO 2、ZSM-5、SAPO-34和SSZ-13中的一种。
优选地，所述CuO和载体的质量比为0.1。
优选地，步骤(4)所述旋转蒸发仪转速为500r/min，水浴温度为70℃，蒸发时间为2h。
优选地，步骤(5)所述干燥温度为100℃，干燥时间为12h；步骤(6)所述焙烧温度为400℃，焙烧时间为6h。
本发明所述铜基负载型氨氧化催化剂用于固定源烟气和汽车尾气氨逃逸现象的消除，同时也适用于养殖业厂房农业源中氨气排放的处理。包括以下步骤：
(1)制备好的铜基负载型氨氧化催化剂取40～60目粉末，装入微型固定床反应器中，反应温度控制在150～400℃；
(2)以氨气为还原剂，氮气为平衡气，控制气体的总流量为500mL/min，并控制空速为1.5×10 5mL·g -1·h -1。
与现有技术相比，本发明具有无毒性、高活性及高选择性等优点，其中活性组分CuO实现良好的NH 3转化率，载体SSZ-13等则保证低副产物生成量，提高了N 2选择性。本发明的CuO 0.1/SSZ-13氨氧化催化剂在225-400℃温度区间内可达到近95％NH 3转化率和90％以上的N 2选择性。
附图说明
图1为制备的铜基负载型氨氧化催化剂NH 3转化率与反应温度的关系图。
图2为制备的铜基负载型氨氧化催化剂N 2选择性与反应温度的关系图。
具体实施方式
下面结合附图和实施例详细说明本发明的实施方式。
实施例1
CuO 0.1/ZSM-5样品的制备
(1)称取0.9075g三水硝酸铜和3g ZSM-5粉末备用；
(2)将称好的三水硝酸铜溶解于少量去离子水中；
(3)在三水硝酸铜完全溶解后，在其中加入称取好的ZSM-5粉末，并在室温下搅拌5min；
(4)停止搅拌后，将所得溶液转移至旋蒸瓶，利用旋转蒸发仪以500r/min的转速及 70℃水浴温度蒸发2h，使溶剂蒸发；
(5)将蒸发后所得物质放入100℃的烘箱内干燥12h，得到半成品；
(6)将所得到的半成品放入马弗炉，以10℃·min -1的速率升温至400℃条件下保温焙烧6h，最后炉内自然冷却，制得铜基负载型氨氧化催化剂。
该催化剂在400ppm NH 3，10％O 2，平衡气体为N 2的反应条件下，催化剂的用量为0.2g，反应空速为1.5×10 5mL·g -1·h -1。采样温度点分别为：150、200、225、250、275、300、325、350、400℃，催化剂NH 3转化率见图1，N 2选择性见图2。可以看出300～400℃氨氧化活性达到95％以上，而N 2选择性较为优异，整个温度区间内都在95％以上。
实施例2
CuO 0.1/SAPO-34样品的制备
(1)称取0.9075g三水硝酸铜和3g H-SAPO-34粉末备用；
(2)将称好的三水硝酸铜溶解于少量去离子水中；
(3)在三水硝酸铜完全溶解后，在其中加入称取好的H-SAPO-34粉末，并在室温下搅拌5min；
(4)停止搅拌后，将所得溶液转移至旋蒸瓶，利用旋转蒸发仪以400r/min的转速及60℃水浴温度蒸发2h，使溶剂蒸发；
(5)将蒸发后所得物质放入100℃的烘箱内干燥14h，得到半成品；
(6)将所得到的半成品放入马弗炉，以10℃·min -1的速率升温至500℃条件下保温焙烧6h，最后炉内自然冷却，制得铜基负载型氨氧化催化剂。
该催化剂在400ppm NH 3，10％O 2，平衡气体为N 2的反应条件下，催化剂的用量为0.2g，反应空速为1.5×10 5mL·g -1·h -1。采样温度点分别为：150、200、225、250、275、300、325、350、400℃，催化剂NH 3转化率见图1，N 2选择性见图2。可以看出300～400℃氨氧化活性达到90％以上，且N 2选择性较为优异，整个温度区间内都在90％以上。
实施例3
CuO 0.1/SSZ-13样品的制备
(1)称取0.7500g三水醋酸铜和3g H-SSZ-13粉末备用；
(2)将称好的三水醋酸铜溶解于少量去离子水中；
(3)在三水醋酸铜完全溶解后，在其加入称取好的H-SSZ-13粉末，并在室温下搅拌5min；
(4)停止搅拌后，将所得溶液转移至旋蒸瓶，利用旋转蒸发仪以500r/min的转速及60℃水浴温度蒸发4h，使溶剂蒸发；
(5)将蒸发后所得物质放入100℃的烘箱内干燥12h，得到半成品；
(6)将所得到的半成品放入马弗炉，以10℃·min -1的速率升温至400℃条件下保温焙烧8h，最后炉内自然冷却，制得铜基负载型氨氧化催化剂。
该催化剂在400ppm NH 3，10％O 2，平衡气体为N 2的反应条件下，催化剂的用量为0.2g，反应空速为1.5×10 5mL·g -1·h -1。采样温度点分别为：150、200、225、250、275、300、325、350、400℃，催化剂NH 3转化率见图1，N 2选择性见图2。可以看出225～400℃氨氧化活性达到95％以上，且N 2选择性较为优异，整个温度区间内都在90％以上。
综上所述，以分子筛为载体的铜基负载型氨氧化催化剂的中低温NH 3转化率较为 优异，尤其是CuO 0.1/SSZ-13催化剂，其NH 3转化率在225℃就将近95％，且N 2选择性在整个温度区间内都在90％以上，具有无毒性，高活性，高选择性等优点。
申请人声明，本发明通过上述实施例来说明本发明的详细方法，但本发明并不局限于上述详细方法，即不意味着本发明必须依赖上述详细方法才能实施。所属技术领域的技术人员应该明了，对本发明的任何改进，对本发明产品各原料的等效替换及辅助成分的添加、具体方式的选择等，均落在本发明的保护范围和公开范围之内。

Claims (10)

  1. 一种铜基负载型氨氧化催化剂，其特征在于，能够用于消除固定源和移动源产生的氨逃逸污染，处理养殖业厂房农业源中排放的氨气，将氨选择性催化氧化为无害的氮气；以CuO为活性组分，催化剂表示为CuO x/M，M表示为载体，其中x＝m(CuO)/m(M)＝0.05～0.2。
  2. 一种制备权利要求1所述铜基负载型氨氧化催化剂的方法，其特征在于，包括如下步骤：
    (1)按照CuO/M质量比0.05～0.2的比例称取一定量的铜盐和载体粉末备用，其中M表示为载体；
    (2)将称取好的铜盐溶解于去离子水中；
    (3)在铜盐完全溶解后，在其中加入称取好的载体粉末，并在室温下搅拌5min；
    (4)停止搅拌后，将所得溶液转移至旋蒸瓶，利用旋转蒸发仪以300～500r/min的转速及60～80℃水浴温度蒸发2～4h，使溶剂蒸发；
    (5)将蒸发后所得物质放入100～120℃的烘箱内干燥10～14h，得到半成品；
    (6)将所得到的半成品放入马弗炉，以10℃·min -1的速率升温至400～600℃条件下保温焙烧6～8h，最后炉内自然冷却，制得铜基负载型氨氧化催化剂。
  3. 根据权利要求2所述铜基负载型氨氧化催化剂的制备方法，其特征在于，所述铜盐为硝酸铜或醋酸铜。
  4. 根据权利要求2所述铜基负载型氨氧化催化剂的制备方法，其特征在于，所述载体为氧化物或分子筛，包括SiO 2、Al 2O 3、TiO 2、ZSM-5、SAPO-34和SSZ-13中的一种。
  5. 根据权利要求2所述铜基负载型氨氧化催化剂的制备方法，其特征在于，所述CuO和载体的质量比为0.1。
  6. 根据权利要求2所述铜基负载型氨氧化催化剂的制备方法，其特征在于，步骤(4)所述旋转蒸发仪转速为500r/min，水浴温度为70℃，蒸发时间为2h，以保证活性组分在载体表面均匀负载。
  7. 根据权利要求2所述铜基负载型氨氧化催化剂的制备方法，其特征在于，步骤(5)所述干燥温度为100℃，干燥时间为12h。
  8. 根据权利要求2所述铜基负载型氨氧化催化剂的制备方法，其特征在于，步骤(6)所述焙烧温度为400℃，焙烧时间为6h。
  9. 权利要求1所述铜基负载型氨氧化催化剂，应用于固定源和移动源的SCR系统下游，实现前级SCR系统泄漏出的氨气的净化，消除氨逃逸现象；同时也适用于养殖业厂房农业源中氨气排放的处理。
  10. 根据权利要求9所述用途，其特征在于，包括以下步骤：
    (1)制备好的铜基负载型氨氧化催化剂取40～60目粉末，装入微型固定床反应器中，反应温度控制在150～400℃；
    (2)以氨气为还原剂，氮气为平衡气，控制气体的总流量为500mL/min，并控制空速为1.5×10 5mL·g -1·h -1。
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