CN101811013B - Catalysis type hydrogen compounding process method in nuclear power plant - Google Patents
Catalysis type hydrogen compounding process method in nuclear power plant Download PDFInfo
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- CN101811013B CN101811013B CN200910009372XA CN200910009372A CN101811013B CN 101811013 B CN101811013 B CN 101811013B CN 200910009372X A CN200910009372X A CN 200910009372XA CN 200910009372 A CN200910009372 A CN 200910009372A CN 101811013 B CN101811013 B CN 101811013B
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- hydrogen
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- 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
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E30/00—Energy generation of nuclear origin
- Y02E30/30—Nuclear fission reactors
Abstract
The invention belongs to a hydrogen compounding process method, and in particular relates to a catalysis type hydrogen compounding process in a pressurized water reactor nuclear power plant. The catalysis type hydrogen compounding process comprises the following steps of: (1) extracting air possibly containing a large amount of hydrogen; (2) separating the air from water; and (3) compounding the hydrogen with oxygen, comprising the following steps of: (3.1) heating, i.e., heating the air containing the hydrogen extracted in the step (2) to the temperature from 120 DEG C to 140 DEG C; (3.2) depositing, i.e., depositing tiny solid particles in the air; and (3.3) carrying out catalytic reaction, i.e., carrying out reaction on the deposited air by a catalyst, and compounding the hydrogen with the oxygen, wherein the catalyst is metallic oxide catalyst or noble metal catalyst. The invention has the advantages of low heating temperature, short heating time, low electricity consumption and long continuous working time. Moreover, when the concentration of the hydrogen reaches 3%, the hydrogen elimination efficiency is higher than 99%; and reaction can start when the concentration of the hydrogen is 0.5%.
Description
Technical field
The invention belongs to hydrogen compounding process method, be specifically related to a kind of pressurized-water reactor nuclear power plant (PWR) catalysis type hydrogen combination process.
Background technology
Nuclear power station can produce hydrogen in operation, especially behind loss of-coolant accident (LOCA) (LOCA) and major accident (SA), the containment dome has a large amount of hydrogen collection with some plant compartment top.There is the danger of blast in a large amount of hydrogen, and this situation has a strong impact on the normal safety in production of nuclear power station.
What traditional hydrogen complex method adopted is electrical heating method, and it roughly comprises following steps: (1) possibly comprise the gas of a large amount of hydrogen and extract out; (2) the gas heating to extracting out reaches 718 ℃ up to gas temperature, arrive this temperature after hydrogen-oxygen begin reaction; (3) discharge the water that the compound back of hydrogen-oxygen forms, residual gas is carried back in the reactor.
The shortcoming of this method is: (1) heating-up temperature is high because hydrogen-oxygen compound be under 718 ℃ high temperature, to carry out, just can make the reaction beginning so must gas be heated to this temperature; (2) heat time heating time long, need 1～1.5 hour from beginning to be heated to compound completion generally speaking, reaction efficiency is low; (3) power consumption is big, and existing heater nearly all is the electrothermal heater, long-time powerful heating meeting labor electric energy.
Summary of the invention
The present invention is directed to the defective of electrical heating method technology, the nuclear power station catalysis type hydrogen that a kind of heating-up temperature is low, reaction efficiency is high, power consumption is low combination process is provided.
The present invention is achieved in that a kind of nuclear power station catalysis type hydrogen combination process, comprises the steps:
The gas that (1) possibly comprise a large amount of hydrogen is extracted out;
(2) carbonated drink is separated:
Eliminate the iodine of the aerosol state in the gas;
(3) hydrogen-oxygen is compound
This step comprises following steps again
(3.1) heating: the air containing hydrogen gas of extracting out in the step (2) is heated to 120 ℃～140 ℃;
(3.2) sedimentation: with airborne small solid particles sediment;
(3.3) catalytic reaction: make the gas reaction after the sedimentation through catalyst, it is compound to carry out hydrogen-oxygen, and described is metal oxide catalyst or noble metal catalyst.
Aforesaid a kind of nuclear power station catalysis type hydrogen combination process wherein, increases the water that compound back is formed in step (3) back and collects in the dedicated storage jar, and residual gas is carried back the step of containment.
Aforesaid a kind of nuclear power station catalysis type hydrogen combination process, wherein, described catalyst is the stainless steel carrier catalysts of noble metal platinum or the AL of precious metal palladium
2O
3Carried catalyst.
Aforesaid a kind of nuclear power station catalysis type hydrogen combination process, wherein, described noble metal catalyst is an XQ-III G type hydrogen-eliminating catalyst.
Use effect of the present invention to be: 1. only need gas be heated to 120 ℃～140 ℃ just can realize recombination reaction, and heating-up temperature is low; 2. lack heat time heating time, only need just can reach very short heat time heating time the required temperature of reaction; 3. power consumption is low, and the power consumption of this technology approximately only needs the half the of electrical heating process; 4. stream time is long, and this technology can continuous operation more than 150 hours.5. when density of hydrogen reached 3%, the hydrogen efficiency that disappears just can begin reaction greater than 99% at density of hydrogen at 0.5% o'clock.
Description of drawings
Fig. 1 is the structural principle sketch map of steam-water separator.
Among the figure: 1. steam-water separator, 2. multilayer corrugated filler.
The specific embodiment
Below in conjunction with the accompanying drawing and the specific embodiment catalysis type hydrogen compounding process method in nuclear power plant provided by the invention is further elaborated.
A kind of nuclear power station catalysis type hydrogen combination process comprises the steps:
The gas that (1) will comprise a large amount of hydrogen is extracted out;
The gas that will comprise hydrogen according to the method for prior art is extracted out, and the gas of this hydrogen generally is present in the containment of reactor;
(2) carbonated drink is separated:
Carry out carbonated drink separation through steam-water separator.
It is as shown in Figure 1 in steam-water separator 1, to be provided with multilayer corrugated filler 2, and the material of filler can be provided with as required.Filler in this example mainly is used to eliminate aerosol state iodine, can will effectively separate greater than the drop of 10miu rice.Gas gets into from the inlet of steam-water separator; Through getting rid of from outlet behind the ripple packing; Because the contact-making surface of ripple packing and gas is very big, so the fluid liquid in the gas separates out from ripple packing, and this process can be eliminated the iodine of most aerosol state in the gas.The iodine that removes aerosol state is for fear of in follow-up reaction, making catalyst poisoning.
(3) hydrogen-oxygen is compound
This step comprises following steps again
(3.1) heating: the hydrogen-containing gas of extracting out in the step (2) is heated to 120 ℃～140 ℃, all can selects for for example 120 ℃, 130 ℃, 140 ℃; Heating can be accomplished through electrical heating.Maze-type structure is adopted in the air channel of electric heater, and the air-flow baffling flows through heating element heater, forms small solid particle after the water evaporates of heat, and this small solid particle is suspended in the gas.What described electric heater was selected for use is the electrical heating elements of commercially available " U " type, and the electrical heating elements with some one fixed structures places pressure vessel then, makes pressure vessel airtight.Described air containing hydrogen gas only through in the pressure vessel, can not revealed outside pressure vessel.
(3.2) sedimentation: with the small solid particles sediment in the gas.Sedimentation is used and is adopted the alundum (Al ceramic raschig rings with large surface area and circulation area, and each Raschig ring is of a size of Φ 12 * 1.The main purpose of heating and sedimentation is in order to eliminate NaOH drop and the boric acid drop in the gas; Removing above-mentioned two kinds of materials is for fear of in follow-up reaction, making catalyst poisoning; Avoid two kinds of impurity of NaOH drop and boric acid drop that the physics of catalytic bed is covered simultaneously; Cause the catalytic bed resistance to increase, even stop up.
(3.3) catalytic reaction: through catalyst make after the sedimentation in gas to carry out hydrogen-oxygen compound.
Make gas after the sedimentation through containing the catalytic bed of catalyst, hydrogen after catalyst just can make sedimentation in the process that gas passes through in the gas and oxygen generation recombination reaction.
The initial temperature of catalytic reaction is at least at 120 ℃, because this reaction is exothermic reaction, therefore constantly carries out along with what react, and the temperature of catalytic bed can constantly rise.
Described catalyst can be selected the stainless steel carrier catalysts of noble metal platinum or the AL of precious metal palladium for use
2O
3Carried catalyst.The stainless steel carrier catalysts of wherein said noble metal platinum is meant selects for use stainless steel to do base plate, and the noble metal catalyst of coating is platinum (Pt).The AL of described precious metal palladium
2O
3Carried catalyst is meant with AL
2O
3Do base plate, the noble metal catalyst of coating is palladium (Pd).These two kinds of catalyst all have very high catalytic activity, mithridatism, anti-radiation property and heat endurance.The stainless steel carrier catalysts of noble metal platinum or the AL of precious metal palladium
2O
3Carried catalyst all can customize from market.The AL of preferred precious metal palladium in these two kinds of catalyst
2O
3Carried catalyst.
(4) water that compound back is formed is collected in the dedicated storage jar, and residual gas is carried back containment.
Claims (2)
1. a nuclear power station catalysis type hydrogen combination process comprises the steps:
The gas that (1) will comprise a large amount of hydrogen is extracted out:
The gas that comprises hydrogen that will be present in the containment of reactor is extracted out;
It is characterized in that: also comprise the steps
(2) carbonated drink is separated:
Eliminate the iodine of the aerosol state in the gas;
(3) hydrogen-oxygen is compound
This step comprises following steps again
(3.1) heating: the hydrogen-containing gas of finishing dealing with in the step (2) is heated to 120 ℃～140 ℃;
(3.2) sedimentation: with the small solid particles sediment in the hydrogen;
(3.3) catalytic reaction: it is compound to make gas after the sedimentation carry out hydrogen-oxygen through catalyst
Described catalyst is the stainless steel carrier catalysts of noble metal platinum or the Al of precious metal palladium
2O
3Carried catalyst.
2. a kind of nuclear power station catalysis type hydrogen combination process as claimed in claim 1 is characterized in that: increase the water that compound back is formed in step (3) back and collect in the holding vessel, residual gas is carried back the step of containment.
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| CN200910009372XA CN101811013B (en) | 2009-02-20 | 2009-02-20 | Catalysis type hydrogen compounding process method in nuclear power plant |
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| CN200910009372XA CN101811013B (en) | 2009-02-20 | 2009-02-20 | Catalysis type hydrogen compounding process method in nuclear power plant |
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| CN101811013A CN101811013A (en) | 2010-08-25 |
| CN101811013B true CN101811013B (en) | 2012-01-25 |
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Families Citing this family (6)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN105895183B (en) * | 2016-04-21 | 2018-01-05 | 中广核研究院有限公司 | Carbon containing 14 waste gas processing method and system |
| CN108364698B (en) * | 2018-01-03 | 2020-05-22 | 中广核研究院有限公司 | Hydrogen elimination method and system for small space of nuclear power station |
| CN109545417A (en) * | 2018-11-19 | 2019-03-29 | 中广核工程有限公司 | The system of nuclear power station removal radioactive emission hydrogen component |
| CN113380431A (en) * | 2021-06-03 | 2021-09-10 | 哈尔滨工程大学 | Hydrogen recombiner catalytic unit |
| CN113908776B (en) * | 2021-11-12 | 2023-10-20 | 西北核技术研究所 | Method and device for efficiently converting high-concentration hydrogen into water |
| CN113941295B (en) * | 2021-11-12 | 2023-10-20 | 西北核技术研究所 | Method and device for efficiently converting hydrogen into water |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1125888A (en) * | 1994-12-28 | 1996-07-03 | 中国科学院兰州化学物理研究所 | Catalytic hydrogen-eliminating technological process for nuclear energy system |
| US6054108A (en) * | 1996-09-09 | 2000-04-25 | Siemens Aktiengesellschaft | Catalyst system and recombination device for recombining hydrogen and oxygen, in particular for a nuclear power station and method for operating a catalyst system |
| CN1345451A (en) * | 1999-03-31 | 2002-04-17 | 费罗马托姆Anp有限责任公司 | Recombination device and method for catalytically recombining hydrogen and/or carbon monoxide with oxygen in gaseous mixture |
| US20020086796A1 (en) * | 1999-03-31 | 2002-07-04 | Bernd Eckardt | Catalytic element with restrictor layer |
| CN1923360A (en) * | 2005-08-31 | 2007-03-07 | 中国科学院大连化学物理研究所 | Preparation process and application of axial non-uniformness integral catalyst |
-
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Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1125888A (en) * | 1994-12-28 | 1996-07-03 | 中国科学院兰州化学物理研究所 | Catalytic hydrogen-eliminating technological process for nuclear energy system |
| US6054108A (en) * | 1996-09-09 | 2000-04-25 | Siemens Aktiengesellschaft | Catalyst system and recombination device for recombining hydrogen and oxygen, in particular for a nuclear power station and method for operating a catalyst system |
| CN1345451A (en) * | 1999-03-31 | 2002-04-17 | 费罗马托姆Anp有限责任公司 | Recombination device and method for catalytically recombining hydrogen and/or carbon monoxide with oxygen in gaseous mixture |
| US20020086796A1 (en) * | 1999-03-31 | 2002-07-04 | Bernd Eckardt | Catalytic element with restrictor layer |
| CN1923360A (en) * | 2005-08-31 | 2007-03-07 | 中国科学院大连化学物理研究所 | Preparation process and application of axial non-uniformness integral catalyst |
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