WO2023212843A1 - 一种选择性脱除co的装置及其使用方法 - Google Patents

一种选择性脱除co的装置及其使用方法 Download PDF

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WO2023212843A1
WO2023212843A1 PCT/CN2022/090871 CN2022090871W WO2023212843A1 WO 2023212843 A1 WO2023212843 A1 WO 2023212843A1 CN 2022090871 W CN2022090871 W CN 2022090871W WO 2023212843 A1 WO2023212843 A1 WO 2023212843A1
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chamber
reaction
hydrogen
catalytic combustion
gas outlet
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English (en)
French (fr)
Inventor
潘立卫
李金晓
宋仁升
张晶
钟和香
陈淑花
靳文尧
于波
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Dalian University
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Dalian University
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    • 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
    • B01D53/02—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 by adsorption, e.g. preparative gas chromatography
    • B01D53/04—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 by adsorption, e.g. preparative gas chromatography with stationary adsorbents
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
    • 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
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G5/00—Incineration of waste; Incinerator constructions; Details, accessories or control therefor
    • F23G5/44—Details; Accessories
    • F23G5/46—Recuperation of heat
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G7/00—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals
    • F23G7/06—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals of waste gases or noxious gases, e.g. exhaust gases
    • F23G7/07—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals of waste gases or noxious gases, e.g. exhaust gases in which combustion takes place in the presence of catalytic material

Definitions

  • the invention belongs to the technical field of energy and environment.
  • the invention relates to a device for selectively removing CO and its use method.
  • Fuel cell is an important technology that efficiently converts the chemical energy of fuel into electrical energy. It does not need to go through the Carnot cycle during use and has a high energy conversion rate. Its raw materials are hydrogen and oxygen, and the product is water. It does not pollute the environment and is an environmentally friendly energy conversion device. Fuel cell technology is considered to be one of the new environmentally friendly and efficient power generation technologies in the 21st century. It has already been applied in transportation power supply, fixed power supply and portable power supply.
  • Proton exchange membrane fuel cell is rapidly developing after alkaline fuel cell (AFC), phosphoric acid fuel cell (PAFC), molten carbonate fuel cell (MCFC), and solid oxide fuel cell (SOFC).
  • AFC alkaline fuel cell
  • PAFC phosphoric acid fuel cell
  • MCFC molten carbonate fuel cell
  • SOFC solid oxide fuel cell
  • the fifth-generation fuel cell which has the lowest temperature, the highest specific energy, the fastest startup, the longest life, and the most wide application, was ranked first among the top ten new technologies in the 21st century in the social survey results of Time Magazine in the United States.
  • Selective oxidation of CO is currently one of the commonly used methods to deal with trace amounts of CO in hydrogen-rich gas.
  • the principle is to introduce oxygen during the reforming process to convert CO into CO 2 .
  • the oxygen-rich environment of this method will cause the loss of some hydrogen, and an external power supply or heat source is required during the process.
  • the process requires the participation of a catalyst to ensure that CO is oxidized prior to hydrogen.
  • some impurities in the hydrogen-rich gas will poison the catalyst, causing the catalyst to become deactivated after a period of use; some precious metal catalysts are too expensive and difficult to reuse; the thermal stability and catalytic activity of non-precious metal catalysts cannot meet the process requirements. need.
  • CO will release a large amount of heat during the oxidation process. If the materials are unevenly distributed during the reaction, it will easily lead to local overheating, which requires relatively high heat resistance of the device and catalyst. And currently, this technology is difficult to remove trace amounts of CO in hydrogen-rich gas to less than 0.2ppm.
  • the present invention provides a device for selectively removing CO and a method of using the device.
  • the device is highly integrated and does not require external power supply, heat source and high-pressure environment.
  • a device for selectively removing CO including two reaction device main bodies.
  • the reaction device main body is a vertical device.
  • An air feed chamber, a catalytic combustion chamber, and a CO reaction chamber are arranged in sequence from the outside to the inside; a catalytic combustion chamber and a CO reaction chamber.
  • the CO reaction chamber is located
  • There is a hydrogen-rich gas inlet at the center of the main body of the reaction device and above the top of the main body of the reaction device.
  • the catalytic combustion chamber and CO reaction chamber of each main body of the reaction device are respectively connected to the hydrogen-rich gas inlet through pipelines; and on the pipelines Correspondingly, there are a hydrogen-rich gas inlet valve of the combustion chamber and a hydrogen-rich gas inlet valve of the CO reaction chamber; a connecting pipeline is provided on the top of the CO reaction chamber and the top of the catalytic combustion chamber, and a CO reaction chamber desorption gas outlet valve is provided on the pipeline; reaction device The side wall of the main body is provided with an air inlet, and the bottom of the catalytic combustion chamber in the main body of the reaction device is connected to the heat exchanger through a pipeline; the bottom of the CO reaction chamber is provided with a product gas outlet pipeline, and a product gas outlet valve is provided on the pipeline.
  • flow meters are respectively provided at the air inlet and the hydrogen-rich gas inlet to effectively control the catalytic combustion reaction rate.
  • air feed chamber catalytic combustion chamber
  • CO reaction chamber are respectively provided with pressure sensors.
  • a CO concentration monitor is installed at the connecting pipeline between the CO reaction chamber and the catalytic combustion chamber to monitor the desorption process of the CO reaction chamber.
  • the CO reaction chamber is equipped with a CO selective adsorbent;
  • the catalytic combustion chamber is filled with a catalytic combustion catalyst;
  • the catalytic combustion catalyst includes but is not limited to Pd-based, Pt-based, Rh-based, Ce-based, Zr-based, and La-based catalysts; when the catalytic combustion catalyst is specifically used, any one of the above catalytic combustion catalysts or more than one kind;
  • the upper part of the catalytic combustion chamber and the air feed chamber is a thin-walled spacer with non-uniformly distributed through holes; the diameter of the through holes is 1-5 mm.
  • the heat exchanger is installed at the tail gas outlet of the main body of the reaction device to fully recover and utilize waste heat.
  • the two reaction device bodies are arranged symmetrically.
  • the main bodies of the two reaction devices are symmetrically distributed.
  • one main body of the reaction device reaches saturation in adsorbing CO, its desorption process is started, and the other main body is started for adsorption at the same time, ensuring that the CO adsorption process can be continued continuously.
  • Another object of the present invention is to request protection for the method of using the above device, which specifically includes the following steps:
  • the hydrogen-rich gas enters the CO reaction chamber of any reaction device body through the hydrogen-rich gas inlet. At this time, the CO contained in the hydrogen-rich gas is efficiently adsorbed by the selective adsorbent in the adsorption chamber, and the product gas flows through the product gas outlet. discharge.
  • the CO reaction chamber undergoes a desorption and adsorption process of CO under heated conditions, and the precipitated CO is introduced into the catalytic combustion chamber to undergo a catalytic combustion reaction with air.
  • the combustion exhaust gas of CO and hydrogen is discharged through the combustion exhaust gas outlet, and the waste heat during the combustion process is recovered through the heat exchanger.
  • stop flowing gas into the air feed chamber and catalytic combustion chamber close the combustion exhaust gas outlet, and wait for the main body of the reaction device to cool down.
  • the hydrogen-rich gas is passed into the CO reaction chamber of another reaction device body. At this time, the CO removal of the hydrogen-rich gas is carried out in the device body, and the product gas is discharged from the product gas outlet.
  • the above-mentioned selective adsorbents include but are not limited to copper-based adsorbents, molecular sieve adsorbents, zeolite adsorbents, activated nickel, and porous carbon; when the selective adsorbents are specifically used, the above-mentioned selective adsorbents are used. any one or more than one;
  • physical adsorption is used to remove trace amounts of CO from hydrogen-rich gas, thereby avoiding the loss of a part of the hydrogen during the selective catalytic combustion process.
  • the absorption of CO can be carried out at normal temperature and pressure without additional heating or pressurization conditions.
  • Two sets of symmetrical device bodies are set up. When one set of devices is saturated with adsorption, the desorption program is started and the other set of devices is selected for further adsorption, which improves the treatment efficiency.
  • the desorption energy of CO is provided by the catalytic combustion process of part of the hydrogen-rich gas to be treated and air (oxygen), and no additional heat source is required.
  • the desorbed CO undergoes a catalytic combustion reaction in the catalytic combustion chamber, and the released energy further provides energy for desorption.
  • the product is CO 2 , which will not cause pollution to the environment.
  • the air feed chamber, catalytic combustion chamber, and CO reaction chamber are alternately arranged and compact in structure, while ensuring a more complete exchange of gas and heat.
  • the air feed chamber and half of the catalytic combustion chamber are separated by a thin wall, and the upper half of the thin wall has non-uniformly distributed 1 to 5 mm through holes. This design can not only ensure the full contact reaction between hydrogen and air, improve the utilization rate of materials, but also ensure the uniform mixing of materials and avoid the sintering and deactivation of the catalyst caused by local overheating of the reaction device.
  • the catalytic combustion process of air and hydrogen can be carried out at normal temperature and pressure, and no other conditions are required.
  • a heat exchanger is installed at the combustion exhaust gas outlet connected to the catalytic combustion chamber, which can fully recover the waste heat in the exhaust gas and maximize energy utilization.
  • the reaction device of the present invention can remove the carbon monoxide concentration from 0.1-2.0% to less than 1-0.2 ppm in the raw gas containing hydrogen with a volume concentration of 50-75%.
  • Figure 1 is a schematic diagram of a device for selectively removing CO according to the present invention
  • Figure 2 is a top view of the main body a of the reaction device of the present invention.
  • Figure 3 is a schematic structural diagram of the wall between the air feed chamber and the catalytic combustion chamber of the present invention.
  • the combustion chamber hydrogen-rich gas inlet valve a, the CO reaction chamber hydrogen-rich gas inlet valve a, the CO reaction chamber desorption gas outlet valve a, the product gas outlet valve a, and the heat exchanger a are connected to the PLC system.
  • combustion chamber hydrogen-rich gas inlet valve b CO reaction chamber desorption gas outlet valve b, CO reaction chamber hydrogen-rich gas inlet valve b, heat exchanger b, product gas outlet valve b, flow meter, pressure sensor, CO concentration monitor
  • combustion chamber hydrogen-rich gas inlet valve b CO reaction chamber desorption gas outlet valve b
  • CO reaction chamber hydrogen-rich gas inlet valve b heat exchanger b
  • product gas outlet valve b flow meter
  • pressure sensor CO concentration monitor
  • a device for selectively removing CO includes two reaction device main bodies: reaction device main body a 22, reaction device main body b 23, both reaction device main bodies are vertical devices,
  • the main body a 22 of the reaction device includes an air feed chamber a 4, a catalytic combustion chamber a 5, and a CO reaction chamber a 6 arranged in sequence from the outside to the inside; there is a 0.5-3mm thin wall between the catalytic combustion chamber a 5 and the CO reaction chamber a 6 Phase separation; the lower part between the catalytic combustion chamber a 5 and the air feed chamber a 4 is a thin-walled partition, and the upper part is a thin-walled partition with non-uniformly distributed through holes; the CO reaction chamber a 6 is located in the main body of the reaction device At the center of a 22, a hydrogen-rich gas inlet 8 is provided above the top of the reaction device body a 22.
  • the catalytic combustion chamber a 5 and the CO reaction chamber a 6 are respectively connected to the hydrogen-rich gas inlet 8 through pipelines; and the pipes On the road, there are corresponding hydrogen-rich gas inlet valves a 1 of the combustion chamber and hydrogen-rich gas inlet valve a 2 of the CO reaction chamber; there are connecting pipelines on the top of the CO reaction chamber a 6 and the top of the catalytic combustion chamber a 5, and there is a CO on the pipeline.
  • Reaction chamber desorption gas outlet valve a 3 the side wall of the reaction device main body a 22 is provided with an air inlet a 12, and the bottom of the catalytic combustion chamber a 5 in the reaction device main body a 22 is connected to the heat exchanger a 10 through a pipeline; CO reaction A product gas outlet pipeline is provided at the bottom of cavity a 6 and a product gas outlet valve a 7 is provided on the pipeline;
  • the main body b 23 of the reaction device includes an air feed chamber b 16, a catalytic combustion chamber b 17, and a CO reaction chamber b 18 arranged in sequence from the outside to the inside; a 0.5-3mm thin wall is provided between the catalytic combustion chamber b 17 and the CO reaction chamber b 18. Phase separation; the lower part between the catalytic combustion chamber b 17 and the air feed chamber b 16 is a thin-walled partition, and the upper part is a thin-walled partition with non-uniformly distributed through holes; the CO reaction chamber b 18 is located in the main body of the reaction device At the center of b 23, there is a hydrogen-rich gas inlet 8 above the top of the reaction device body b 23.
  • the catalytic combustion chamber b 17 and the CO reaction chamber b 18 are respectively connected to the hydrogen-rich gas inlet 8 through pipelines; and the pipes On the road, there are corresponding hydrogen-rich gas inlet valves b 11 of the combustion chamber and hydrogen-rich gas inlet valve b 14 of the CO reaction chamber; there are connecting pipelines on the top of the CO reaction chamber b 18 and the top of the catalytic combustion chamber b 17, and there is a CO on the pipeline.
  • reaction chamber desorption gas outlet valve b 13 The reaction chamber desorption gas outlet valve b 13; the side wall of the reaction device main body b 23 is provided with an air inlet b 21, and the bottom of the catalytic combustion chamber b 17 in the reaction device main body b 23 is connected to the heat exchanger b 15 through a pipeline; CO reaction The bottom of cavity b 18 is provided with a product gas outlet pipeline and the pipeline is provided with a product gas outlet valve b 19;
  • air inlet a 12 air inlet b 21, and hydrogen-rich gas inlet 8 are respectively equipped with flow meters to effectively control the catalytic combustion reaction rate.
  • the air feed chamber a 4 the catalytic combustion chamber a 5, the CO reaction chamber a 6, the air feed chamber b 16, the catalytic combustion chamber b 17, and the CO reaction chamber b 18 are respectively provided with pressure sensors.
  • CO concentration monitors are respectively provided at the connecting pipelines between the CO reaction chamber a 6 and the catalytic combustion chamber a 5, and at the connecting pipelines between the CO reaction chamber b 18 and the catalytic combustion chamber b 17 to monitor the CO reaction chamber. The desorption process is monitored.
  • the CO reaction chamber a 6 and the CO reaction chamber b 18 are equipped with CO selective adsorbents; the catalytic combustion chamber a 5 and the catalytic combustion chamber b 17 are filled with Pd-based catalysts for catalytic combustion;
  • the heat exchanger a 10 is arranged at the tail gas outlet of the reaction device main body a 22; the heat exchanger b 15 is set at the tail gas outlet of the reaction device main body b 23; to fully realize waste heat recovery and utilization.
  • the end of the heat exchanger a 10 is provided with a combustion exhaust gas outlet a 9; the end of the heat exchanger b 15 is provided with a combustion exhaust gas outlet b 20.
  • Combustion chamber hydrogen-rich gas inlet valve a 1, CO reaction chamber hydrogen-rich gas inlet valve a 2, CO reaction chamber desorption gas outlet valve a 3, product gas outlet valve a 7, heat exchanger a 10, combustion chamber hydrogen-rich gas inlet Valve b 11, CO reaction chamber desorption gas outlet valve b 13, CO reaction chamber hydrogen-rich gas inlet valve b 14, heat exchanger b 15, product gas outlet valve b 19, flow meter, pressure sensor, CO concentration monitor and PLC system is connected.
  • the main body of the reaction device is two sets of vertical devices, arranged symmetrically. Each device has three different functional chambers from the outside to the inside, including an air feed chamber, a catalytic combustion chamber and a CO reaction chamber.
  • a hydrogen-rich gas inlet 8 is provided on the top of the main body of the reaction device.
  • the gas input into the catalytic combustion chamber in the CO desorption stage is controlled through the hydrogen-rich gas inlet valve of the combustion chamber.
  • the hydrogen-rich gas inlet valve in the CO reaction chamber controls the gas input into the CO adsorption stage.
  • the input of hydrogen gas controls the emission of CO gas to the catalytic combustion chamber during the CO desorption stage through the CO reaction chamber desorption gas outlet valve.
  • An air inlet is provided on one side of the main body of the reaction device.
  • a combustion exhaust gas outlet and a heat exchanger are provided at the bottom of the reaction device to fully utilize the waste heat of the combustion exhaust gas.
  • a product gas outlet valve is provided to fully control the discharge of product gas.
  • the CO reaction chamber is filled with CO selective adsorbent.
  • the CO reaction chamber and the catalytic combustion chamber are separated by a thin wall.
  • the lower half of the catalytic combustion chamber and the air feed chamber are separated by a thin wall.
  • the upper half of the thin wall has non-uniformly distributed through holes to ensure hydrogen. Fully reacts with air to improve material utilization. At the same time, it can ensure that the materials are mixed evenly and avoid local overheating of the main body of the reaction device causing sintering and deactivation of the catalyst.
  • the air tightness of the entire device must first be checked.
  • the specific operation is: close the combustion exhaust gas outlet a 9, the combustion exhaust gas outlet b 20, the product gas outlet valve a 7, the product gas outlet valve b 19, the hydrogen-rich gas inlet 8, the combustion chamber hydrogen-rich gas inlet valve a 1, CO Reaction chamber hydrogen-rich gas inlet valve a 2, CO reaction chamber desorption gas outlet valve a 3, combustion chamber hydrogen-rich gas inlet valve b 11, CO reaction chamber desorption gas outlet valve b 13, CO reaction chamber hydrogen-rich gas inlet valve b 14 .
  • Air is introduced from the air inlet a 12 and the air inlet b 21 to the reaction device main body a 22 and the reaction device main body b 23.
  • the pressure in the air feed chamber or the catalytic combustion chamber reaches 0.2MPa
  • the air is stopped. Air, when the pressure remains constant, the airtightness of this part is good.
  • the air inlet 8 supplies air to the reaction device main body a 22 and the reaction device main body b 23.
  • the pressure in the CO reaction chamber reaches 0.2MPa
  • the air will diffuse into the catalytic combustion chamber a 5 through the small holes between the walls of the catalytic combustion chamber a 5 and the air feed chamber a 4.
  • the hydrogen-rich gas and air undergo a hydrogen-oxygen catalytic combustion reaction through the action of the catalytic combustion catalyst filled in the catalytic combustion chamber a 5 , and heat is transferred through the wall between the catalytic combustion chamber a 5 and the CO reaction chamber a 6 .
  • the CO selective adsorbent in the CO reaction chamber a 6 undergoes a desorption and adsorption process of CO under heated conditions.
  • the precipitated CO flows from the CO reaction chamber desorption gas outlet valve a 3 into the catalytic combustion chamber a 5 to undergo a catalytic combustion reaction with air.
  • the combustion exhaust gas (main components are CO 2 and H 2 O) in the catalytic combustion chamber a 5 is discharged through the combustion exhaust gas outlet a 9, and the waste heat during the combustion process is recovered through the heat exchanger a 10.
  • the CO reaction chamber desorption gas outlet valve a 3 is provided with a CO concentration detection device. When the end of the desorption process is detected, the flow of air to the air inlet a 12 is stopped, and the hydrogen-rich gas inlet valve a 1 of the combustion chamber is closed. CO reaction chamber desorption gas outlet valve a 3 and combustion exhaust gas outlet a 9, wait for the reaction device to cool down. At the same time, start the adsorption process of the main body b 23 of the other reaction device.
  • the specific operations are as follows: open the hydrogen-rich gas inlet valve b 14 and the product gas outlet valve b 19 of the CO reaction chamber, and keep the hydrogen-rich gas inlet valve b 11 and The CO reaction chamber desorption gas outlet valve b 13 is closed. At this time, the hydrogen-rich gas that needs to be processed flows into the CO reaction chamber b 18, in which trace amounts of CO are fully adsorbed by the CO selective adsorbent filled in the CO reaction chamber b 18, and the gas that reaches the standard is discharged through the product gas outlet valve b 19.
  • the air will diffuse into the catalytic combustion chamber b 17 through the small holes between the walls of the catalytic combustion chamber b 17 and the air feed chamber b 16.
  • the hydrogen-rich gas and air undergo a hydrogen-oxygen catalytic combustion reaction through the action of the catalytic combustion catalyst filled in the catalytic combustion chamber b 17, and heat is transferred through the wall between the catalytic combustion chamber b 17 and the CO reaction chamber b 18.
  • the CO selective adsorbent in the CO reaction chamber b 18 undergoes a desorption and adsorption process of CO under heated conditions, and the precipitated CO flows from the CO reaction chamber desorption gas outlet valve b 13 into the catalytic combustion chamber b 17 to undergo a catalytic combustion reaction with air.
  • the combustion exhaust gas in the catalytic combustion chamber b 17 is discharged through the combustion exhaust gas outlet b 20, and the waste heat during the combustion process is recovered through the heat exchanger b 15.
  • the CO reaction chamber desorption gas outlet valve b 13 is provided with a CO concentration detection device. When the end of the desorption process is detected, the flow of air to the air inlet b 21 is stopped, and the hydrogen-rich gas inlet valve b 11 of the combustion chamber is closed. CO reaction chamber desorption gas outlet valve b 13 and combustion exhaust gas outlet b 20, wait for the reaction device to cool down. At this time, the other reaction device body a 22 has completed the desorption of CO and has cooled down. The adsorption process of the reaction device body a 22 is started. The specific operation is the same as step S2.
  • the reaction device main body a 22 and the reaction device main body b 23 can respectively perform the adsorption and desorption processes of CO to ensure the continuity of the entire CO removal process.

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Abstract

本发明属于能源环境技术领域，公开了一种选择性脱除CO的装置及其使用方法。设置了对称的两套装置主体，当其中一套装置吸附饱和时，启动脱附程序，选用另一套装置进行进一步吸附，提高了处理效率。CO的脱附能量由一部分的待处理富氢气体和空气的催化燃烧过程提供，不需要额外热源。脱附出的CO在催化燃烧腔中发生催化燃烧反应，放出的能量进一步为脱附提供能量，其产物为CO 2，不会对环境造成污染。空气进料腔、催化燃烧腔、CO反应腔交互排列、结构紧凑，同时又能保证气体、热量的交换更加充分。与催化燃烧腔连接的燃烧尾气出口处设置换热器，可充分回收尾气中的余热，最大程度的提高了能量利用率。

Description

一种选择性脱除CO的装置及其使用方法 技术领域
本发明属于能源环境技术领域，本发明涉及一种选择性脱除CO的装置及其使用方法。
背景技术
燃料电池是将燃料的化学能高效转化为电能的重要技术，它在使用过程中不需要经过卡诺循环，能量转化率高。其原料为氢气和氧气，产物为水，对环境不会产生污染，是一种环境友好的能量转换装置。燃料电池技术被认为是21世纪新型环保高效的发电技术之一，目前已经在交通动力电源、固定电源及便携式电源等方面开始应用。
质子交换膜燃料电池(PEMFC)是继碱性燃料电池(AFC)、磷酸型燃料电池(PAFC)、熔融碳酸盐燃料电池(MCFC)、固体氧化物燃料电池(SOFC)之后正在迅速发展起来工作温度最低、比能最高、启动最快、寿命最长、应用最广的第五代燃料电池，在美国《时代周刊》的社会调查结果中被列为21世纪十大科技新技术之首。
然而，CO对PEMFC的电极具有毒化作用，即使原料气中具有极其微量的CO，也会对PEMFC的电极造成致命的影响。虽然纯氢是PEMFC最理想的原料气，但其制备成本、储运成本较高且安全性差，不利于其规模化使用。现场制氢直接与PEMFC联用是更为经济、可行的选择，但是产物氢气在进入燃料电池前需要将富氢气体中的CO进行深度脱除。
CO选择性氧化是目前处理富氢气体中微量CO的常用方法之一。其原理是在重整过程中通入氧气，使CO转化为CO 2。但是该方法的富氧环境会造成一些氢气的损失，过程中还需要外加电源或者热源。此外，过程需要催化剂的参与以保证CO优先于氢气氧化。然而，富氢气体中的一些杂质成分会对催化剂有毒化作用，导致催化剂使用一段时间后失活；一些贵金属催化剂成本过高，难以重复使用；非贵金属催化剂热稳定性、催化活性等不能满足工艺需求。CO在氧化过程中会放出大量的热，如果反应过程中物料分布不均，容易导致局部过热，对装置和催化剂的耐热性要求都比较高。而且目前来说，该技术对富氢气体中微量CO很难脱除到0.2ppm以下。
发明内容
为了克服现有技术的不足，本发明提供一种选择性脱除CO的装置及其使用方法，该装置集成度高，不需要外加电源、热源且不需要高压环境。
本发明的上述目的是通过以下技术方案实现的：
一种选择性脱除CO的装置，包括两个反应装置主体，反应装置主体为立式装置，由外向内依次设置空气进料腔、催化燃烧腔、CO反应腔；催化燃烧腔与CO反应腔之间设有0.5-3mm薄壁相间隔；催化燃烧腔和空气进料腔之间下半部分为薄壁间隔，上半部分为带有非均布通孔的薄壁间隔；CO反应腔位于反应装置主体的中心位置，反应装置主体顶部上方设有富氢气体进气口，每个反应装置主体的催化燃烧腔、CO反应腔分别通过管路与富氢气体进气口连接；且管路上对应分别设有燃烧腔富氢气体进口阀、CO反应腔富氢气体进口阀；CO反应腔顶部与催化燃烧腔顶部设有连接管路且管路上设有CO反应腔脱附气体出口阀；反应装置主体侧壁设有空气进气口，反应装置主体中催化燃烧腔的底部通过管路连接换热器；CO反应腔底部设有产品气出气管路且管路上设有产品气出口阀。
进一步的，空气进气口、富氢气体进气口处分别设有流量计；以对催化燃烧反应速率进行有效控制。
进一步的，空气进料腔、催化燃烧腔、CO反应腔处分别设有压力传感器。
进一步的，在CO反应腔与催化燃烧腔的连接管路处设置CO浓度监测器，以对CO反应腔的脱附过程进行监测。
进一步的，CO反应腔内部装有CO选择性吸附剂；催化燃烧腔中装填有催化燃烧催化剂；
进一步的，所述催化燃烧催化剂包括但不限于Pd基、Pt基、Rh基、Ce基、Zr基、La基催化剂；所述催化燃烧催化剂具体使用时采用上述催化燃烧催化剂中的任一种或一种以上；
进一步的，催化燃烧腔和空气进料腔上半部分为带有非均布通孔的薄壁间隔；其通孔孔径为1-5mm。
进一步的，所述换热器设置在反应装置主体尾气出口处；以充分进行余热回收利用。换热器末端设有燃烧尾气出口；
进一步的，两个反应装置主体对称布置。两个反应装置主体为对称分布，当一个反应装置主体吸附CO达到饱和时，启动其脱附流程，同时启动另一主体进行吸附，保证CO吸附过程可连续进行。
本发明另一个目的是请求保护上述装置的使用方法，具体包括以下步骤：
S1.检查装置气密性，启动反应装置；
S2.富氢气体由富氢气体进气口进入任一反应装置主体的CO反应腔，此时富氢气体中含有的CO被吸附腔内的选择性吸附剂高效吸附，产品气由产品气出口排出。
S3.当该反应装置主体CO吸附饱和时，停止向该反应装置主体的CO反应腔进行进气。 同时，将富氢气体通入该反应装置主体的催化燃烧腔，将空气通入该反应装置主体的空气进料腔。空气通过催化燃烧腔与空气进料腔间的通孔向催化燃烧腔扩散，此时在催化剂的作用下催化燃烧腔内发生氢氧催化燃烧反应，为CO反应腔供热。CO反应腔在加热的条件下发生CO的解析附过程，析出的CO通入催化燃烧腔中与空气进行催化燃烧反应。CO与氢气的燃烧尾气通过燃烧尾气出口排出，燃烧过程中的余热通过换热器回收。当脱附过程结束后，停止向空气进料腔和催化燃烧腔通入气体，关闭燃烧尾气出口，等待反应装置主体降温。与该过程同步的，将富氢气体通入另一反应装置主体的CO反应腔，此时富氢气体的CO脱除在该应装置主体中进行，产品气由产品气出口排出。
S4.当另一反应装置主体的CO吸附饱和时，进行该反应装置主体的脱吸附过程并启动上一反应装置主体的吸附过程。
进一步的，上述选择性吸附剂包括但不限于铜基吸附剂、分子筛类吸附剂、沸石类吸附剂、活性镍、多孔炭；所述选择性吸附剂具体使用时采用上述选择性吸附剂中的任一种或一种以上；
本发明的提供的装置中，富氢气体中微量CO的脱除选择了物理吸附的手段，避免了选择性催化燃烧过程一部分氢气的损失。CO的吸收在常温常压下即可进行，不需要额外加热或加压条件。设置了对称的两套装置主体，当其中一套装置吸附饱和时，启动脱附程序，选用另一套装置进行进一步吸附，提高了处理效率。CO的脱附能量由一部分的待处理富氢气体和空气(氧气)的催化燃烧过程提供，不需要额外热源。脱附出的CO在催化燃烧腔中发生催化燃烧反应，放出的能量进一步为脱附提供能量，其产物为CO 2，不会对环境造成污染。空气进料腔、催化燃烧腔、CO反应腔交互排列、结构紧凑，同时又能保证气体、热量的交换更加充分。空气进料腔和催化燃烧腔半部分通过薄壁相间隔，上半部分的薄壁带有非均布的1～5mm通孔。该设计既可保证氢气与空气充分接触反应，提高物料的利用率，又可以保证物料混合均匀，避免反应装置局部过热造成催化剂烧结失活。空气与氢气的催化燃烧过程在常温常压下即可进行，不需要附加其他条件。与催化燃烧腔连接的燃烧尾气出口处设置换热器，可充分回收尾气中的余热，最大程度的提高了能量利用率。
本发明与现有技术相比的有益效果是：
(1)将空气进料腔、催化燃烧腔、CO反应腔高度集成，使得反应装置结构紧凑，解决了一般反应装置集成度较差、占地面积大等问题；
(2)对催化燃烧腔和CO反应腔两个相邻腔之间热量交换进行合理匹配，充分利用原料 气体的能量，供给CO的脱附过程，同时在催化燃烧尾气的出口处设置换热器，将尾气余热充分回收，极大提高了整个装置的能量效率；
(3)通过合理设置空气进料腔和催化燃烧腔之间的通孔分布改进反应装置有限空间内的物料混合不充分的问题，避免局部过热的发生，提高原料利用效率。采用本发明的反应装置可以将含有氢气体积浓度为50-75％原料气中的一氧化碳浓度由0.1-2.0％脱除到1～0.2ppm以下。
附图说明
图1为本发明一种选择性脱除CO的装置的示意图；
图2为本发明反应装置主体a的俯视图；
图3为本发明空气进料腔和催化燃烧腔之间壁面的结构示意图；
图中：1、燃烧腔富氢气体进口阀a，2、CO反应腔富氢气体进口阀a，3、CO反应腔脱附气体出口阀a，4、空气进料腔a，5、催化燃烧腔a，6、CO反应腔a，7、产品气出口阀a，8、富氢气体进气口，9、燃烧尾气出口a，10、换热器a，11、燃烧腔富氢气体进口阀b，12、空气进气口a，13、CO反应腔脱附气体出口阀b，14、CO反应腔富氢气体进口阀b，15、换热器b，16、空气进料腔b，17、催化燃烧腔b，18、CO反应腔b，19、产品气出口阀b，20、燃烧尾气出口b，21、空气进气口b，22、反应装置主体a，23、反应装置主体b。
具体实施方式
下面结合附图和具体实施例对本发明作进一步说明，下述具体实施方式仅仅是示意性的而不是限定性的，其他人员在本发明的启示下，在不违背本发明宗旨及权利要求下，可以做出多种类似的表示，这样的变换均落入本发明的保护范围之内。实施例中涉及的与PLC系统相连接的燃烧腔富氢气体进口阀a、CO反应腔富氢气体进口阀a、CO反应腔脱附气体出口阀a、、产品气出口阀a、换热器a、燃烧腔富氢气体进口阀b、CO反应腔脱附气体出口阀b、CO反应腔富氢气体进口阀b、换热器b、产品气出口阀b、流量计、压力传感器、CO浓度监测器均不限定某一具体型号，实现其工作功能即可。
实施例1
一种选择性脱除CO的装置，如图1-图3所示，包括两个反应装置主体：反应装置主体a 22、反应装置主体b 23，两个反应装置主体均为立式装置，
反应装置主体a 22包括由外向内依次设置空气进料腔a 4、催化燃烧腔a 5、CO反应腔a 6；催化燃烧腔a 5与CO反应腔a 6之间设有0.5-3mm薄壁相间隔；催化燃烧腔a 5和空气 进料腔a 4之间下半部分为薄壁间隔，上半部分为带有非均布通孔的薄壁间隔；CO反应腔a 6位于反应装置主体a 22的中心位置，反应装置主体a 22顶部上方设有富氢气体进气口8，催化燃烧腔a 5、CO反应腔a 6分别通过管路与富氢气体进气口8连接；且管路上对应分别设有燃烧腔富氢气体进口阀a 1、CO反应腔富氢气体进口阀a 2；CO反应腔a 6顶部与催化燃烧腔a 5顶部设有连接管路且管路上设有CO反应腔脱附气体出口阀a 3；反应装置主体a 22侧壁设有空气进气口a 12，反应装置主体a 22中催化燃烧腔a 5的底部通过管路连接换热器a 10；CO反应腔a 6底部设有产品气出气管路且管路上设有产品气出口阀a 7；
反应装置主体b 23包括由外向内依次设置空气进料腔b 16、催化燃烧腔b 17、CO反应腔b 18；催化燃烧腔b 17与CO反应腔b 18之间设有0.5-3mm薄壁相间隔；催化燃烧腔b 17和空气进料腔b 16之间下半部分为薄壁间隔，上半部分为带有非均布通孔的薄壁间隔；CO反应腔b 18位于反应装置主体b 23的中心位置，反应装置主体b 23顶部上方设有富氢气体进气口8，催化燃烧腔b 17、CO反应腔b 18分别通过管路与富氢气体进气口8连接；且管路上对应分别设有燃烧腔富氢气体进口阀b 11、CO反应腔富氢气体进口阀b 14；CO反应腔b 18顶部与催化燃烧腔b 17顶部设有连接管路且管路上设有CO反应腔脱附气体出口阀b 13；反应装置主体b 23侧壁设有空气进气口b 21，反应装置主体b 23中催化燃烧腔b 17的底部通过管路连接换热器b 15；CO反应腔b 18底部设有产品气出气管路且管路上设有产品气出口阀b 19；
进一步的，空气进气口a 12、空气进气口b 21、富氢气体进气8处分别设有流量计；以对催化燃烧反应速率进行有效控制。
进一步的，空气进料腔a 4、催化燃烧腔a 5、CO反应腔a 6、空气进料腔b 16、催化燃烧腔b 17、CO反应腔b 18处分别设有压力传感器。
进一步的，在CO反应腔a 6与催化燃烧腔a 5的连接管路处、CO反应腔b 18与催化燃烧腔b 17的连接管路处分别设置CO浓度监测器，以对CO反应腔的脱附过程进行监测。
进一步的，CO反应腔a 6、CO反应腔b 18内部均装有CO选择性吸附剂；催化燃烧腔a 5、催化燃烧腔b 17中均装填有催化燃烧的Pd基催化剂；
进一步的，所述换热器a 10设置在反应装置主体a 22尾气出口处；所述换热器b 15设置在反应装置主体b 23尾气出口处；以充分进行余热回收利用。换热器a 10末端设有燃烧尾气出口a 9；换热器b 15末端设有燃烧尾气出口b 20。
燃烧腔富氢气体进口阀a 1、CO反应腔富氢气体进口阀a 2、CO反应腔脱附气体出口阀 a 3、产品气出口阀a 7、换热器a 10、燃烧腔富氢气体进口阀b 11、CO反应腔脱附气体出口阀b 13、CO反应腔富氢气体进口阀b 14、换热器b 15、产品气出口阀b 19、流量计、压力传感器、CO浓度监测器分别与PLC系统相连接。
反应装置主体为两套立式装置，呈对称布置。每套装置有外向内共三层不同的功能腔，依次设置空气进料腔、催化燃烧腔和CO反应腔。在反应装置主体顶部设有富氢气体进气口8，并通过燃烧腔富氢气体进口阀控制CO脱附阶段催化燃烧腔的气体输入，通过CO反应腔富氢气体进口阀控制CO吸附阶段富氢气体的输入，通过CO反应腔脱附气体出口阀控制在CO脱附阶段CO气体向催化燃烧腔的排放。反应装置主体一侧设有空气进气口。在反应装置底部设有燃烧尾气出口及换热器以充分利用燃烧尾气的余热，同时设置产品气出口阀以充分控制产品气的排出。所述CO反应腔内装填有CO选择性吸附剂。CO反应腔与催化燃烧腔之间通过薄壁间隔，催化燃烧腔与空气进料腔之间下半部分通过薄壁相间隔，上半部分的薄壁带有非均布的通孔以保证氢气与空气充分接触反应，提高物料的利用率。同时可以保证物料混合均匀，避免反应装置主体局部过热造成催化剂烧结失活。
上述一种富氢气体中微量CO脱除装置的使用方法，具体为：
S1.启动反应装置前，由于整个装置的实验流程涉及一氧化碳和氢气等有毒或易燃易爆气体，所以首先要检查整个装置的气密性。具体操作是：关闭燃烧尾气出口a 9、燃烧尾气出口b 20、产品气出口阀a 7、产品气出口阀b 19、富氢气体进气口8、燃烧腔富氢气体进口阀a 1、CO反应腔富氢气体进口阀a 2、CO反应腔脱附气体出口阀a 3、燃烧腔富氢气体进口阀b 11、CO反应腔脱附气体出口阀b 13、CO反应腔富氢气体进口阀b 14。由空气进气口a 12、空气进气口b 21向反应装置主体a 22、反应装置主体b 23通入空气，当空气进料腔或催化燃烧腔内的压力达到0.2MPa后，停止通入空气，当压力保持不变，则该部分气密性良好。关闭空气进气口a 12、空气进气口b 21，打开富氢气体进气口8、CO反应腔富氢气体进口阀a 2、CO反应腔富氢气体进口阀b 14，由富氢气体进气口8向反应装置主体a 22、反应装置主体b 23通入空气，当CO反应腔内的压力达到0.2MPa后，停止通入空气，当压力保持不变，则气密性良好，启动装置。
S2.打开富氢气体进气口8、CO反应腔富氢气体进口阀a 2、产品气出口阀a 7，保持其他进气口、出口及阀门关闭。向富氢气体进气口8通入需要处理的富氢气体，使富氢气体内的微量CO充分被CO反应腔a 6中填充的CO选择性吸附剂吸附，达标的气体通过产品气出口阀a 7排出。
S3.当反应装置主体a 22达到CO吸附饱和时，关闭CO反应腔富氢气体进口阀a 2和产品气出口阀a 7，停止向该反应装置主体a 22的CO吸附腔a 6的进气，同时启动该反应装置的CO脱附程序，具体操作如下：打开燃烧腔富氢气体进口阀a 1，空气进气口a 12，CO反应腔脱附气体出口阀a 3以及燃烧尾气出口a 9。向空气进料腔a 4通入空气，此时空气将通过催化燃烧腔a 5和空气进料腔a 4壁面间的小孔向催化燃烧腔a 5内扩散。富氢气体和空气通过催化燃烧腔a 5内填充的催化燃烧催化剂的作用发生氢氧催化燃烧反应，通过催化燃烧腔a 5和CO反应腔a 6间的壁面传热。CO反应腔a 6内的CO选择性吸附剂在受热条件下发生CO的解析附过程，析出的CO由CO反应腔脱附气体出口阀a 3处流入催化燃烧腔a 5与空气进行催化燃烧反应。催化燃烧腔a 5的燃烧尾气(主要成分为CO 2和H 2O)通过燃烧尾气出口a 9排出，燃烧过程中的余热通过换热器a 10回收。在CO反应腔脱附气体出口阀a 3设有CO浓度检测装置，当探测到脱附过程结束后，停止向空气进气口a 12通入空气，并关闭燃烧腔富氢气体进口阀a 1、CO反应腔脱附气体出口阀a 3和燃烧尾气出口a 9，等待反应装置降温。与此同时，开启另一反应装置主体b 23的吸附流程，具体操作如下：打开CO反应腔富氢气体进口阀b 14和产品气出口阀b 19，保持燃烧腔富氢气体进口阀b 11及CO反应腔脱附气体出口阀b 13关闭。此时需要处理的富氢气体通入CO反应腔b 18，其中微量CO充分被CO反应腔b 18中填充的CO选择性吸附剂吸附，达标的气体通过产品气出口阀b 19排出。
S4.当反应装置主体b 23达到CO吸附饱和时，关闭CO反应腔富氢气体进口阀b 14和产品气出口阀b 19，停止向该反应装置主体b 23的CO吸附腔b 18的进气，同时启动该反应装置的CO脱附程序，具体操作如下：打开燃烧腔富氢气体进口阀b 11，空气进气口b 21，CO反应腔脱附气体出口阀b 13以及燃烧尾气出口b 20。向空气进料腔b 16通入空气，此时空气将通过催化燃烧腔b 17和空气进料腔b 16壁面间的小孔向催化燃烧腔b 17内扩散。富氢气体和空气通过催化燃烧腔b 17内填充的催化燃烧催化剂的作用发生氢氧催化燃烧反应，通过催化燃烧腔b 17和CO反应腔b 18间的壁面传热。CO反应腔b 18内的CO选择性吸附剂在受热条件下发生CO的解析附过程，析出的CO由CO反应腔脱附气体出口阀b 13处流入催化燃烧腔b 17与空气进行催化燃烧反应。催化燃烧腔b 17的燃烧尾气通过燃烧尾气出口b 20排出，燃烧过程中的余热通过换热器b 15回收。在CO反应腔脱附气体出口阀b 13设有CO浓度检测装置，当探测到脱附过程结束后，停止向空气进气口b 21通入空气，并关闭燃烧腔富氢气体进口阀b 11、CO反应腔脱附气体出口阀b 13和燃烧尾气出口b 20，等待反应装置 降温。此时，另一反应装置主体a 22已完成CO的脱附并已降温完毕，开启该反应装置主体a 22的吸附流程，具体操作同步骤S2。
反应装置主体a 22与反应装置主体b 23可分别进行CO的吸附和脱吸附过程，保证整个CO脱除过程的连续性。
反应稳定后，还需在产品气出口处定期抽样检测产品气体的组成，以判断本发明的反应装置是否运行正常。
以上所述，仅为本发明创造较佳的具体实施方式，但本发明创造的保护范围并不局限于此，任何熟悉本技术领域的技术人员在本发明创造披露的技术范围内，根据本发明创造的技术方案及其发明构思加以等同替换或改变，都应涵盖在本发明创造的保护范围之内。

Claims (8)

  1. 一种选择性脱除CO的装置，其特征是，包括两个反应装置主体，反应装置主体为立式装置，由外向内依次设置空气进料腔、催化燃烧腔、CO反应腔；催化燃烧腔与CO反应腔之间设有0.5-3mm薄壁相间隔；催化燃烧腔和空气进料腔之间下半部分为薄壁间隔，上半部分为带有非均布通孔的薄壁间隔；CO反应腔位于反应装置主体的中心位置，反应装置主体顶部上方设有富氢气体进气口(8)，每个反应装置主体的催化燃烧腔、CO反应腔分别通过管路与富氢气体进气口(8)连接；且管路上对应分别设有燃烧腔富氢气体进口阀、CO反应腔富氢气体进口阀；CO反应腔顶部与催化燃烧腔顶部设有连接管路且管路上设有CO反应腔脱附气体出口阀；反应装置主体侧壁设有空气进气口，反应装置主体中催化燃烧腔的底部通过管路连接换热器；CO反应腔底部设有产品气出气管路且管路上设有产品气出口阀。
  2. 如权利要求1所述的一种选择性脱除CO的装置，其特征是，空气进气口、富氢气体进气口(8)处分别设有流量计；空气进料腔、催化燃烧腔、CO反应腔处分别设有压力传感器。
  3. 如权利要求2所述的一种选择性脱除CO的装置，其特征是，在CO反应腔与催化燃烧腔的连接管路处设置CO浓度监测器。
  4. 如权利要求3所述的一种选择性脱除CO的装置，其特征是，CO反应腔内部装有CO选择性吸附剂；催化燃烧腔中装填有催化燃烧催化剂。
  5. 如权利要求4所述的一种选择性脱除CO的装置，其特征是，所述换热器设置在反应装置主体尾气出口处；换热器末端设有燃烧尾气出口。
  6. 如权利要求1所述的一种选择性脱除CO的装置，其特征是，包括两个反应装置主体：反应装置主体a(22)、反应装置主体b(23)，两个反应装置主体均为立式装置，
    反应装置主体a(22)包括由外向内依次设置空气进料腔a(4)、催化燃烧腔a(5)、CO反应腔a(6)；催化燃烧腔a(5)与CO反应腔a(6)之间设有0.5-3mm薄壁相间隔；催化燃烧腔a(5)和空气进料腔a(4)之间下半部分为薄壁间隔，上半部分为带有非均布通孔的薄壁间隔；CO反应腔a(6)位于反应装置主体a(22)的中心位置，反应装置主体a(22)顶部上方设有富氢气体进气口(8)，催化燃烧腔a(5)、CO反应腔a(6)分别通过管路与富氢气体进气口(8)连接；且管路上对应分别设有燃烧腔富氢气体进口阀a(1)、CO反应腔富氢气体进口阀a(2)；CO反应腔a(6)顶部与催化燃烧腔a(5)顶部设有连接管路且管路上设有CO反应腔脱附气体出口阀a(3)；反应装置主体a(22)侧壁设有空气进气口a(12)，反应装置主体a(22)中催化燃烧腔a(5)的底部通过管路连接换热器a(10)；CO反应腔a(6)底部设有产品气出气管路且管路上设有产品气出口阀a(7)；
    反应装置主体b(23)包括由外向内依次设置空气进料腔b(16)、催化燃烧腔b(17)、CO反应腔b(18)；催化燃烧腔b(17)与CO反应腔b(18)之间设有0.5-3mm薄壁相间隔；催化燃烧腔b(17)和空气进料腔b(16)之间下半部分为薄壁间隔，上半部分为带有非均布通孔的薄壁间隔；CO反应腔b(18)位于反应装置主体b(23)的中心位置，反应装置主体b(23)顶部上方设有富氢气体进气口(8)，催化燃烧腔b(17)、CO反应腔b(18)分别通过管路与富氢气体进气口(8)连接；且管路上对应分别设有燃烧腔富氢气体进口阀b(11)、CO反应腔富氢气体进口阀b(14)；CO反应腔b(18)顶部与催化燃烧腔b(17)顶部设有连接管路且管路上设有CO反应腔脱附气体出口阀b(13)；反应装置主体b(23)侧壁设有空气进气口b(21)，反应装置主体b(23)中催化燃烧腔b(17)的底部通过管路连接换热器b(15)；CO反应腔b(18)底部设有产品气出气管路且管路上设有产品气出口阀b(19)；空气进气口a(12)、空气进气口b(21)、富氢气体进气口(8)处分别设有流量计；
    空气进料腔a(4)、催化燃烧腔a(5)、CO反应腔a(6)、空气进料腔b(16)、催化燃烧腔b(17)、CO反应腔b(18)处分别设有压力传感器；
    在CO反应腔a(6)与催化燃烧腔a(5)的连接管路处、CO反应腔b(18)与催化燃烧腔b(17)的连接管路处分别设置CO浓度监测器；
    CO反应腔a(6)、CO反应腔b(18)内部均装有CO选择性吸附剂；催化燃烧腔a(5)、催化燃烧腔b(17)中均装填有催化燃烧催化剂；
    所述换热器a(10)设置在反应装置主体a(22)尾气出口处；所述换热器b(15)设置在反应装置主体b(23)尾气出口处；
    换热器a(10)末端设有燃烧尾气出口a(9)；换热器b(15)末端设有燃烧尾气出口b(20)。
  7. 如权利要求5所述的一种选择性脱除CO的装置的使用方法，其特征是，
    S1.检查装置气密性，启动反应装置；
    S2.富氢气体由富氢气体进气口(8)进入任一反应装置主体的CO反应腔，此时富氢气体中含有的CO被吸附腔内的选择性吸附剂高效吸附，产品气由产品气出口排出；
    S3.当该反应装置主体CO吸附饱和时，停止向该反应装置主体的CO反应腔进行进气；同时，将富氢气体通入该反应装置主体的催化燃烧腔，将空气通入该反应装置主体的空气进料腔；空气通过催化燃烧腔与空气进料腔间的通孔向催化燃烧腔扩散，此时在催化剂的作用下催化燃烧腔内发生氢氧催化燃烧反应，为CO反应腔供热；CO反应腔在加热的条件下发生CO的解析附过程，析出的CO通入催化燃烧腔中与空气进行催化燃烧反应；CO与氢气的燃 烧尾气通过燃烧尾气出口排出，燃烧过程中的余热通过换热器回收；当脱附过程结束后，停止向空气进料腔和催化燃烧腔通入气体，关闭燃烧尾气出口，等待反应装置主体降温；与该过程同步的，将富氢气体通入另一反应装置主体的CO反应腔，此时富氢气体的CO脱除在该应装置主体中进行，产品气由产品气出口排出；
    S4.当另一反应装置主体的CO吸附饱和时，进行该反应装置主体的脱吸附过程并启动上一反应装置主体的吸附过程。
  8. 如权利要求6所述的一种选择性脱除CO的装置的使用方法，其特征是，具体步骤如下所示：
    S1.启动反应装置前，由于整个装置的实验流程涉及一氧化碳和氢气等有毒或易燃易爆气体，所以首先要检查整个装置的气密性；具体操作是：关闭燃烧尾气出口a(9)、燃烧尾气出口b(20)、产品气出口阀a(7)、产品气出口阀b(19)、富氢气体进气口(8)、燃烧腔富氢气体进口阀a(1)、CO反应腔富氢气体进口阀a(2)、CO反应腔脱附气体出口阀a(3)、燃烧腔富氢气体进口阀b(11)、CO反应腔脱附气体出口阀b(13)、CO反应腔富氢气体进口阀b(14)；由空气进气口a(12)、空气进气口b(21)向反应装置主体a(22)、反应装置主体b(23)通入空气，当空气进料腔或催化燃烧腔内的压力达到0.2MPa后，停止通入空气，当压力保持不变，则该部分气密性良好；关闭空气进气口a(12)、空气进气口b(21)，打开富氢气体进气口(8)、CO反应腔富氢气体进口阀a(2)、CO反应腔富氢气体进口阀b(14)，由富氢气体进气口(8)向反应装置主体a(22)、反应装置主体b(23)通入空气，当CO反应腔内的压力达到0.2MPa后，停止通入空气，当压力保持不变，则气密性良好，启动装置；
    S2.打开富氢气体进气口(8)、CO反应腔富氢气体进口阀a(2)、产品气出口阀a(7)，保持其他进气口、出口及阀门关闭；向富氢气体进气口(8)通入需要处理的富氢气体，使富氢气体内的微量CO充分被CO反应腔a(6)中填充的CO选择性吸附剂吸附，达标的气体通过产品气出口阀a(7)排出；
    S3.当反应装置主体a(22)达到CO吸附饱和时，关闭CO反应腔富氢气体进口阀a(2)和产品气出口阀a(7)，停止向该反应装置主体a(22)的CO吸附腔a(6)的进气，同时启动该反应装置的CO脱附程序，具体操作如下：打开燃烧腔富氢气体进口阀a(1)，空气进气口a(12)，CO反应腔脱附气体出口阀a(3)以及燃烧尾气出口a(9)；向空气进料腔a(4)通入空气，此时空气将通过催化燃烧腔a(5)和空气进料腔a(4)壁面间的小孔向催化燃烧腔a(5)内扩散；富氢气体和空气通过催化燃烧腔a(5)内填充的催化燃烧催化剂的作用发 生氢氧催化燃烧反应，通过催化燃烧腔a(5)和CO反应腔a(6)间的壁面传热；CO反应腔a(6)内的CO选择性吸附剂在受热条件下发生CO的解析附过程，析出的CO由CO反应腔脱附气体出口阀a(3)处流入催化燃烧腔a(5)与空气进行催化燃烧反应；催化燃烧腔a(5)的燃烧尾气通过燃烧尾气出口a(9)排出，燃烧过程中的余热通过换热器a(10)回收；在CO反应腔脱附气体出口阀a(3)设有CO浓度检测装置，当探测到脱附过程结束后，停止向空气进气口a(12)通入空气，并关闭燃烧腔富氢气体进口阀a(1)、CO反应腔脱附气体出口阀a(3)和燃烧尾气出口a(9)，等待反应装置降温；与此同时，开启另一反应装置主体b(23)的吸附流程，具体操作如下：打开CO反应腔富氢气体进口阀b(14)和产品气出口阀b(19)，保持燃烧腔富氢气体进口阀b(11)及CO反应腔脱附气体出口阀b(13)关闭；此时需要处理的富氢气体通入CO反应腔b(18)，其中微量CO充分被CO反应腔b(18)中填充的CO选择性吸附剂吸附，达标的气体通过产品气出口阀b(19)排出；
    S4.当反应装置主体b(23)达到CO吸附饱和时，关闭CO反应腔富氢气体进口阀b(14)和产品气出口阀b(19)，停止向该反应装置主体b(23)的CO吸附腔b(18)的进气，同时启动该反应装置的CO脱附程序，具体操作如下：打开燃烧腔富氢气体进口阀b(11)，空气进气口b(21)，CO反应腔脱附气体出口阀b(13)以及燃烧尾气出口b(20)；向空气进料腔b(16)通入空气，此时空气将通过催化燃烧腔b(17)和空气进料腔b(16)壁面间的小孔向催化燃烧腔b(17)内扩散；富氢气体和空气通过催化燃烧腔b(17)内填充的催化燃烧催化剂的作用发生氢氧催化燃烧反应，通过催化燃烧腔b(17)和CO反应腔b(18)间的壁面传热；CO反应腔b(18)内的CO选择性吸附剂在受热条件下发生CO的解析附过程，析出的CO由CO反应腔脱附气体出口阀b(13)处流入催化燃烧腔b(17)与空气进行催化燃烧反应；催化燃烧腔b(17)的燃烧尾气通过燃烧尾气出口b(20)排出，燃烧过程中的余热通过换热器b(15)回收；在CO反应腔脱附气体出口阀b(13)设有CO浓度检测装置，当探测到脱附过程结束后，停止向空气进气口b(21)通入空气，并关闭燃烧腔富氢气体进口阀b(11)、CO反应腔脱附气体出口阀b(13)和燃烧尾气出口b(20)，等待反应装置降温；此时，另一反应装置主体a(22)已完成CO的脱附并已降温完毕，开启该反应装置主体a(22)的吸附流程，具体操作同步骤S2；
    反应装置主体a(22)与反应装置主体b(23)可分别进行CO的吸附和脱吸附过程，保证整个CO脱除过程的连续性。
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