CN105628857A - Industrial pilot test performance testing device and industrial pilot test performance testing method for SCR (selective catalytic reduction) denitration catalyst - Google Patents
Industrial pilot test performance testing device and industrial pilot test performance testing method for SCR (selective catalytic reduction) denitration catalyst Download PDFInfo
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Abstract
The invention relates to an industrial pilot test performance testing device and an industrial pilot test performance testing method for an SCR (selective catalytic reduction) denitration catalyst, aiming to solve the problem that an existing denitration catalyst testing device is incapable of simulating influences of load change on a catalyst during actual running. The industrial pilot test performance testing device comprises a testing device body comprising a gas distribution portion, a reaction portion and a measurement portion, wherein the gas distribution portion is communicated with a gas outlet of a coal economizer, and the reaction portion is communicated with a gas outlet of an air preheater. The testing device body achieves gas distribution and reaction of boiler tail gas through the gas distribution portion and the reaction portion, and the measurement portion is used for collecting and analyzing sample gas. The testing device body is arranged in a boiler tail gas system during actual industrial production, and the boiler tail gas serving as test gas of the testing device body enables flue gas for testing to have physicochemical and process properties of actual flue gas to produce influencing substances, so that reaction between the catalyst in the reaction portion with the flue gas for testing is guaranteed, and accurate and reliable test data are provided for research on running of the existing catalyst under the conditions of different temperatures and flue gas components.
Description
Technical field
The present invention relates to field of thermal power, be specifically related to desulphurization catalyst test.
Background technology
Application along with country's planning implementation of " transferring electricity from the west to the east " engineering and electrical network EHV transmission technology, outer power purchase ratio increases considerably, fired power generating unit rate of load condensate declines, and along with the minimizing of hours of operation, most power plant will be chronically at underload or frequent variable load operation state, additionally, after coal group of motors minimum discharge transformation, it is proposed that most stringent pollutant emission standard, denitrating system can full load put into operation become nitrogen oxides can the key issue of qualified discharge. on the one hand, the SCR(scr reactor of original load design) change of the parameters of flue gas during because of underload causes that denitration efficiency reduces by denitrating system, even cause SCR system out of service owing to SCR work cigarette temperature cannot stably maintain, it is difficult to reach predetermined denitration requirement, on the other hand, the SCR catalyst that original load is designed by variations in temperature and flue gas composition change causes damage, and causes catalyst life dramatic drop-off, thus increasing SCR system operating cost. how to make denitrating system meet operation in full load section and have become as a global problem, so needing existing catalyst running status under different temperatures and flue gas composition situation is studied, and the denitrating catalyst assay device of domestic routine adopts burning natural gas or distribution simulation coal-fired flue-gas to test, and the small size catalyst after cutting can only be carried out lab scale by assay device, the actual working state of full-scale catalyst can not be accurately reflected, the assay device of this structure is adapted under the specific status of criterion, carry out catalyst when dispatching from the factory, operating performance detects, because of impact that catalyst is produced by load variations when cannot simulate actual motion, also actual smoke moisture cannot be simulated, the heavy metal produced in coal burning, alkaline-earth metal, the impact on catalyst physics and chemistry and operational characteristic such as halide ion, make troubles to research.
Summary of the invention
In order to solve the deficiencies in the prior art, the present invention provides a kind of SCR denitration industry test performance testing device, overcome when the limitation of SCR catalyst prior performance test, a kind of SCR denitration pilot scale performance testing device based on actual coal-fired flue-gas and corresponding method thereof are provided, test device draws basis flue gas from coal unit economizer exit, carries out full-scale denitrating catalyst based on operational characteristic detections such as the denitration efficiency under actual flue gas environment, SO2/SO3 conversion ratio, NH3 escapement ratio, activity.
The present invention is accomplished by: a kind of SCR denitration industry test performance testing device, including a test device led to boiler exhaust gas pipeline, described boiler exhaust gas pipeline includes the economizer being sequentially connected in series, scr reactor, air preheater and cleaner unit, described test device includes a distribution portion led to described economizer gas outlet, the measurement portion that one reacting part and led to described air preheater gas outlet is arranged on described reacting part, described test device passes through distribution portion, boiler exhaust gas is realized distribution by reacting part, reaction, and carry out sample gas collection and analysis by described measurement portion. test device is arranged in the boiler exhaust gas system of actual industrial production, utilize boiler exhaust gas as the test gas of test device, test flue gas is made to have the humidity of actual flue gas, heavy metal, alkaline-earth metal, catalyst physics and chemistry and operational characteristic are produced the material of impact by halide ions etc., guarantee the catalyst in reacting part and test smoke reaction, the research that existing catalyst is run under different temperatures and flue gas composition situation provides accurately, reliable test data, the catalyst process characteristic index in life cycle management is assessed under actual flue gas working environment, the all right anti-SO2 of Study of Catalyst, H2O, alkali metal, noxious substance characteristic and the mechanical strengths such as heavy metal, heat stability, in addition, it is succinct that the technical program also has technological process, the features such as construction is little.
As preferably, described distribution portion includes the gas-distribution pipe being sequentially connected in series the first dirt catcher, first order heat exchanger, the second dirt catcher, second level heat exchanger, blender, and the head end of described gas-distribution pipe and described economizer gas outlet are led to, and tail end leads to described reacting part. The feature that basic flue gas has temperature height, dustiness is big introduced from economizer gas outlet, so needing to carry out dedusting, cooling, to meet reacting part catalytic reaction needs. Basis flue gas first the first dirt catcher, can remove the bulky grain dust in the flue gas of basis, it is prevented that block gas-distribution pipe because of dust adhesion; First order heat exchanger, second level heat exchanger all adopt water-cooled structure, and basis flue gas is by realizing cooling with cooling water heat conduction, and concrete cooling extent can need according to test and determine; Described blender plays the effect stirring evenly gas so that the basis each component uniformly dispersing of flue gas, and then guarantees that reaction is fully, and process is truer, reliable. Two-stage heat exchanger is adopted can effectively to control the temperature range of basis flue gas, catalyst testing conversion rate of NOx in relatively low temperature (< 200 DEG C) and wider temperature window.
As preferably, described distribution portion includes the modified assembly of gas and the modified assembly of steam, the modified assembly of described gas includes a header, respectively through the modified unit of nitric oxide that check valve and described header lead to, the modified unit of sulfur dioxide, the modified unit of oxygen and the modified unit of nitrogen, connect end outside described header to lead to described blender air inlet after described first order heat exchanger, the modified assembly of described steam includes a water tank and one and the tank connected steam evaporator of described water storage, the gas outlet of described steam evaporator and described blender air inlet lead to. including the modified unit of nitric oxide, the modified unit of sulfur dioxide, the modified assembly of gas of the modified unit of oxygen and the modified unit of nitrogen can basis flue gas is added various gases according to test needs, the modified assembly of steam can regulate the humidity of basis flue gas, basis flue gas is formed in distribution portion both there is heavy metal, alkaline-earth metal, the various material such as halide ion, can also need to regulate the humidity of basis flue gas according to experiment, component etc., by providing the modified gas having complicated flue gas composition and difference basis smoke components proportioning concurrently to obtain full and accurate test data for reacting part. owing to the gas in the modified unit of nitric oxide, the modified unit of sulfur dioxide, the modified unit of oxygen and the modified unit of nitrogen is room temperature state, various gases flow through first order heat exchanger by header after forming mixture gas by preset ratio, mixture gas is played the effect of heat temperature raising, it is simple to mixture gas mixes with the basic flue gas with certain heat energy, owing to steam evaporator is by obtaining steam to the mode adding hot water, so steam has had certain heat, then without being heated by first order heat exchanger, can being introduced directly into the air inlet of blender, blender is by basis flue gas, mixture gas and steam mix homogeneously and forms modified gas.
As preferably, described reacting part include an ammonia generating assembly, in set reaction cabin and an exhaust structure of containing cavity, described gas-distribution pipe is led to by a reaction tube group and described containing cavity, described containing cavity is led to by described exhaust structure and described air preheater gas outlet, described ammonia generating assembly and described reaction tube group are led to, and place denitrating catalyst in described containing cavity. Utilize ammonia reduce basis flue gas in NOx, be effectively improved conversion rate of NOx, described modified gas mix with ammonia after formation reacting gas.
As preferably, described containing cavity include some head and the tail lead to and with the accommodating section of full-scale catalyst outline, described reaction tube group includes a reaction supervisor led to described distribution portion and the reaction arm led to each accommodating section head end, described reaction arm leads to described reaction supervisor each through corresponding adjustment valve, described exhaust structure includes a stage casing and sets the aerofluxus supervisor of air-introduced machine and be responsible for, with described aerofluxus, the exhaust branch pipe led to by flow valve, the tail end of the inlet end of described exhaust branch pipe section accommodating with described in latter end is corresponding to be led to, the outlet side of described aerofluxus supervisor is led to described air preheater gas outlet. accommodating section can lay full-scale catalyst, is prevented effectively from the inaccurate situation of data causing using small size catalyst test to obtain because catalyst each portion characteristic is inconsistent, actually used situation of more fitting, multiple catalyst are arranged in single containing cavity, reacting gas is delivered to the head end of each catalyst by reaction supervisor by each reaction arm, make reacting part can individually test the full-scale catalyst of arbitrary accommodating section as required or test some full-scale catalyst adjacent successively, by change the catalyst combination of test obtain comprehensive, test data reliably. reacting gas forms reaction end gas by catalyst action reaction, and described reaction end gas sends into air preheater gas outlet by exhaust structure, and air-introduced machine provides driving force for reaction end gas circulation, and flow valve plays the effect controlling containing cavity reaction gases flow, the tail end of exhaust branch pipe section accommodating with described in latter end is corresponding to be led to so that the reaction gas physical ability of entrance containing cavity is discharged after acting on successively with tactic catalyst, it is ensured that reacting gas and catalyst are fully contacted. the outlet side of described aerofluxus supervisor is led to described air preheater gas outlet so that have the reaction end gas efficiency of heating surface without influence on air preheater of lower temperature, improves heat transfer efficiency. described reaction arm leads to described reaction supervisor each through corresponding adjustment valve, make operator can lead to state by what switch that each adjustment valve controls each reaction arm, and then controlling the position of reacting gas inflow containing cavity, it is achieved selectivity uses any catalyst monomer or combination.
As preferably, two strip containing cavities it are provided with in described reaction cabin, three accommodating sections it are provided with in described containing cavity, described reaction arm is the six roots of sensation, described exhaust branch pipe is two, is provided with gap between adjacent catalyst, and the head end of first section of described accommodating section is provided with acoustic wave ash ejector, described ammonia generating assembly includes an ammonia generator and a heater, and described ammonia generator is contacted successively by pipeline and led to described reaction supervisor after a check valve and described heater. Containing cavity is two, places three accommodating sections in every containing cavity, and six roots of sensation arm leads to each catalyst head end respectively, and exhaust branch pipe connects with containing cavity respectively, is used for discharging reaction end gas; Acoustic wave ash ejector can effectively prevent dust from gathering on a catalyst, it is ensured that the contact area between catalyst and reacting gas, and then ensures catalytic efficiency; The ammonia that ammonia generating assembly produces is being sent in containing cavity after heating, it is prevented that reduce modified gas temperature because low temperature ammonia enters containing cavity, it is ensured that reaction carries out at preset temperature, tests data reliably to obtain.
As preferably, gas-distribution pipe between described first order heat exchanger and second level heat exchanger is connected the second dirt catcher, one it is provided with the 6th jumper pipe controlling valve between the described gas outlet of the second dirt catcher and the air inlet of blender, described exhaust structure includes a cooling assembly, described cooling assembly includes being located at described aerofluxus and is responsible for the first control valve of first section, lead to the described first cooling pipe controlling valve air inlet and described second level heat exchanger air inlet and lead to the described first return duct controlling valve air gate and heat exchanger gas outlet, the described second level, described cooling pipe and return duct are respectively equipped with the second control valve and the 3rd and control valve, it is positioned between the second dirt catcher and second level heat exchanger, gas-distribution pipe between second level heat exchanger and blender is respectively equipped with the 4th control valve and the 5th and controls valve. reduce the dustiness in the flue gas of basis further by setting up the second dirt catcher, effectively prevent dust from gathering adhesion in pipeline, and then cause pipeline blockage, owing to air-introduced machine has normal working temperature scope, when the temperature of reaction end gas is more than air-introduced machine normal working temperature scope, reaction end gas utilizes cooling assembly realize cooling and meet the normal working temperature requirement of air-introduced machine, when using cooling assembly, form low-temp reaction tail gas by realizing pyroreaction tail gas with the use of each control valve by the second heat exchanger cooling, will arrange outside low-temp reaction tail gas again through air-introduced machine.
As preferably, described measurement portion include flue gas preprocessor, flue gas analyzer, be sequentially connected in series described flue gas preprocessor, flue gas analyzer measure supervisor and the measurement arm that leads to respectively with described reaction arm, exhaust branch pipe, described measurement arm leads to described measurement supervisor each through corresponding adjustment valve, and the sample gas of described measurement arm collection flows through described flue gas preprocessor successively by measurement supervisor and flue gas analyzer realizes response data collection. Measure arm to lead to each reaction arm, exhaust branch pipe respectively, measuring supervisor and can gather, by the valve that regulates controlling on each measurement arm, the sample gas being positioned at catalyst two ends, flue gas analyzer obtains every technic index parameter of corresponding catalyst by analyzing above-mentioned sample gas.
As preferably, described reaction arm leads to described measurement arm by being positioned at its pipeline regulated between valve and reaction cabin, described exhaust branch pipe leads to described measurement arm by the pipeline being positioned between its flow valve and reaction cabin, when the flow valve regulated on valve or exhaust branch pipe reacting arm cuts out, also ensure that corresponding measurement arm can collect relevant sample gas, it is ensured that test is normally carried out.
A kind of SCR denitration industry test performance test methods, comprises the following steps:
1, basis flue gas is introduced from economizer gas outlet;
2, basis flue gas is by forming modified gas after the modified assembly of gas and the processing of steam modified assembly;
3, in modified gas, add the reducing gas through preheating, form reacting gas;
4, reacting gas is passed in the containing cavity of reaction cabin, after reacting gas and full-scale catalyst reaction, form reaction end gas;
5, gather reacting gas and reaction end gas, and obtain flue gas data by flue gas analyzer analysis;
6, reaction end gas enters the gas outlet of air preheater by air-introduced machine.
The present invention introduces basis flue gas from coal unit economizer exit, and arrange that two-stage heat exchanger is to regulate reaction temperature, flue gas quality regulating system is set simultaneously to adjust reaction operating mode, can in-site modeling denitrating catalyst running status, carry out full-scale denitrating catalyst based on operational characteristic detections such as the denitration efficiency under actual flue gas environment, SO2/SO3 conversion ratio, NH3 escapement ratio, activity, provide technological guidance for the SCR denitration standardized management of specification coal-burning power plant.
The prominent beneficial effect of the present invention: 1, technological process is clear, and construction is little, can assess the catalyst process characteristic index in life cycle management under actual coal-fired flue-gas working environment; 2, SCR denitration can be studied for a long time under actual coal-fired flue-gas working environment, noxious substance characteristic and mechanical strength, the heat stability such as anti-SO2, H2O, alkali metal, heavy metal; 3, liquefied ammonia can be analyzed and spray into mixing uniformity, research outlet the escaping of ammonia control strategy; 4, can according to actual needs, Adjustment Tests works, the activity and selectivity of checking catalyst, and whether catalyst testing has higher conversion rate of NOx in relatively low temperature (< 200 DEG C) and wider temperature window.
Accompanying drawing explanation
Fig. 1 is that the present invention uses status architecture schematic diagram;
Fig. 2 is reaction cabin, reaction tube group, exhaust stack and measures pipe group attachment structure schematic diagram;
In figure: 1, economizer, 2, scr reactor, 3, air preheater, 4, cleaner unit, 5, first dirt catcher, 6, first order heat exchanger, 7, second level heat exchanger, 8, blender, 9, gas-distribution pipe, 10, header, 11, the modified unit of nitric oxide, 12, the modified unit of sulfur dioxide, 13, the modified unit of oxygen, 14, the modified unit of nitrogen, 15, water tank, 16, steam evaporator, 17, reaction cabin, 18, catalyst, 19, accommodating section, 20, reaction supervisor, 21, reaction arm, 22, air-introduced machine, 23, aerofluxus is responsible for, and 24, exhaust branch pipe, 25, acoustic wave ash ejector, 26, ammonia generator, 27, heater, 28, second dirt catcher, 29, 6th controls valve, and 30, jumper pipe, 31, first controls valve, and 32, second controls valve, and 33, 3rd controls valve, and 34, 4th controls valve, and 35, 5th controls valve, and 36, cooling pipe, 37, return duct, 38, flue gas preprocessor, 39, flue gas analyzer, 40, measure supervisor, 41, measure arm.
Detailed description of the invention
Below in conjunction with specification drawings and specific embodiments, the substantive distinguishing features of the present invention is further described.
A kind of SCR denitration industry test performance testing device as shown in Figure 1, the test device led to by one and boiler exhaust gas pipeline forms, described boiler exhaust gas pipeline includes the economizer 1 being sequentially connected in series, scr reactor 2, air preheater 3 and cleaner unit 4, it is characterized in that described test device includes a distribution portion led to described economizer 1 gas outlet, the measurement portion that one reacting part and led to described air preheater 3 gas outlet is arranged on described reacting part, described test device passes through distribution portion, boiler exhaust gas is realized distribution by reacting part, reaction, and carry out sample gas collection and analysis by described measurement portion.
In use, by the method for testing that this test device is formed, comprise the following steps:
1, introducing basis flue gas from economizer 1 gas outlet, described base gas enters gas-distribution pipe 9 and passes sequentially through the first dirt catcher 5, first order heat exchanger the 6, second dirt catcher 28 and second level heat exchanger 7;
2, each unit gas in the modified assembly of gas is mixed to form mixture gas, and the modified assembly of steam forms steam, steam and the mixture gas after utilizing first order heat exchanger 6 heating and is mixed to form modified gas in blender 8 with basis flue gas;
3, ammonia generating assembly produces high temperature ammonia, and high temperature ammonia and modified gas are mixed to form reacting gas;
4, reacting gas is passed in the containing cavity of reaction cabin 17, after reacting gas and the reaction of full-scale catalyst 18, form reaction end gas;
5, gather reacting gas and reaction end gas, and analyze acquisition flue gas data by flue gas analyzer 39;
6, reaction end gas enters the gas outlet of air preheater 3 by air-introduced machine 22.
The purpose of the technical program is to overcome when the limitation of SCR catalyst prior 18 performance test, it is provided that a kind of SCR denitration 18 pilot scale performance testing device based on actual coal-fired flue-gas and corresponding method thereof. The present invention draws flue gas from coal unit economizer 1 outlet, arrange that two-stage heat exchanger is to regulate reaction temperature, flue gas quality regulating system is set simultaneously to adjust reaction operating mode, can in-site modeling denitrating catalyst 18 running status, carry out full-scale denitrating catalyst 18 based on operational characteristic detections such as the denitration efficiency under actual flue gas environment, SO2/SO3 conversion ratio, NH3 escapement ratio, activity, provide technological guidance for SCR denitration 18 standardized management of specification coal-burning power plant. Hereinto on examination platform, it is possible not only under actual flue gas working environment and assesses the catalyst 18 operational characteristic index in life cycle management, it is also possible to noxious substance characteristic and mechanical strength, the heat stability such as the anti-SO2 of Study of Catalyst 18, H2O, alkali metal, heavy metal; And liquefied ammonia can be analyzed and spray into mixing uniformity, research outlet the escaping of ammonia control strategy; Can also verifying the activity and selectivity of catalyst 18, whether catalyst testing 18 has higher conversion rate of NOx in relatively low temperature (< 200 DEG C) and wider temperature window.
In practical operation, described distribution portion includes the gas-distribution pipe 9 being sequentially connected in series the first dirt catcher 5, first order heat exchanger the 6, second dirt catcher 28, second level heat exchanger 7, blender 8, the head end of described gas-distribution pipe 9 and described economizer 1 gas outlet are led to, and tail end leads to described reacting part. the filter screen mesh of described first dirt catcher 5 and the second dirt catcher 28, because requiring according to basis flue gas situation and reacting part catalytic reaction and adjust, is regarded as specific embodiments of the invention. in practical operation, described first order heat exchanger 6 and second level heat exchanger 7 all adopt gas-liquid two-phase cooling structure, utilize gas piping mutually isolated in heat exchanger and cooling water pipeline interlacing contact to carry out heat exchange, and then optimized integration flue gas cool-down, temperature when generally basis flue gas introduces from economizer 1 gas outlet is more than 300 degree, after first order heat exchanger 6, the temperature of basis flue gas is minimum is down to 250 degree, after the second heat exchanger, the temperature of basis flue gas is minimum can be down to 150 degree, it is provided with jumper pipe 30 between the described gas outlet of the second dirt catcher 28 and the air inlet of blender 8, the gas temperature entering reacting part can be adjusted as required by, such as basis flue gas saves second level heat exchanger 7 by after first order heat exchanger 6 either directly through jumper pipe 30, the basic flue gas entering reacting part is made to have higher temperature, needs with satisfied test different basis flue gas operating mode. filter screen in described first dirt catcher 5 and the second dirt catcher 28 is to filtering bulky grain dust so that flows out and has more little particle dust in the basic flue gas in distribution portion, the boiler exhaust gas that simulation is actual.
In practical operation, described distribution portion includes the modified assembly of gas and the modified assembly of steam, the modified assembly of described gas includes a header 10, the modified unit of nitric oxide 11, the modified unit of sulfur dioxide 12, the modified unit of oxygen 13 and the modified unit 14 of nitrogen that lead to respectively through check valve and described header 10, the gaseous species that the modified assembly of described gas comprises can adjust according to test needs, in order to realize the test device test to catalyst 18 work efficiency in complicated composition situation, it is regarded as specific embodiments of the invention. The various gases that the modified assembly of gas and the modified assembly of steam are provided that should need proportioning to add according to test, there is no the requirement that must add, with the needs of satisfied test device to test different component gas.
In practical operation, connect end outside described header 10 to lead to described blender 8 air inlet after described first order heat exchanger 6, the modified assembly of described steam includes water tank 15 and the steam evaporator 16 being connected with described water tank 15, and the gas outlet of described steam evaporator 16 and described blender 8 air inlet lead to. Mixture gas, steam and basis flue gas mix at the air inlet place of blender 8, owing to basis flue gas has experienced dedusting and cooling process, both effectively prevented the dust in the flue gas of basis from hardening in blender 8 because meeting steam, moreover it is possible to guarantee that three's temperature difference is less, be beneficial to and all should mix. In first order heat exchanger 6, including sealing off the gas-distribution pipe 9 of setting, header 10 and cooling water pipe each other, exist only in heat transfer process between three, do not lead to each other.
In practical operation, described reacting part include an ammonia generating assembly, in set reaction cabin 17 and an exhaust structure of containing cavity, described gas-distribution pipe 9 is led to by a reaction tube group and described containing cavity, described containing cavity is led to by described exhaust structure and described air preheater 3 gas outlet, described ammonia generating assembly and described reaction tube group are led to, and place denitrating catalyst 18 in described containing cavity. Ammonia generating assembly provides reducing gas for reaction, and basis flue gas and reducing gas are sent in containing cavity by reaction tube group, and reducing gas reacts with the NOx in modified gas under catalyst 18 acts on, and improves the transformation efficiency of NOx with this. Reducing gas and the mixing in reaction supervisor 20 of modified gas, and utilize reaction arm 21 to be delivered to the position specifying containing cavity.
In practical operation, described containing cavity include some head and the tail lead to and with the accommodating section 19 of full-scale catalyst 18 outline, described reaction tube group includes a reaction supervisor 20 led to described distribution portion and the reaction arm 21 led to each accommodating section 19 head end, described reaction arm 21 leads to described reaction supervisor 20 each through corresponding adjustment valve, described exhaust structure includes the aerofluxus supervisor 23 that a stage casing sets air-introduced machine 22 and the exhaust branch pipe 24 led to by flow valve with described aerofluxus supervisor 23, the tail end of the inlet end of described exhaust branch pipe 24 section 19 accommodating with described in latter end is corresponding to be led to, the outlet side of described aerofluxus supervisor 23 is led to described air preheater 3 gas outlet. the quantity of described containing cavity and the quantity of accommodating section 19 can increase and decrease adjustment according to test needs, with satisfied test needs, are regarded as specific embodiments of the invention.
In practical operation, being provided with two strip containing cavities in described reaction cabin 17, be provided with three accommodating sections 19 in described containing cavity, described reaction arm 21 is the six roots of sensation, and described exhaust branch pipe 24 is two (as shown in Figure 2). Set: described containing cavity includes left chamber and right chamber; Left intracavity be provided be arranged in order the first from left catalyst 18, the second from left catalyst 18, left three catalyst 18; Right intracavity is provided with the right side one catalyst 18 being arranged in order, right two catalyst 18, right three catalyst 18; Described reaction arm 21 includes the right side three reaction tube that the first from left reaction tube corresponding with the first from left catalyst 18 head end the second from left reaction tube corresponding with a second from left catalyst 18 head end left side three reaction tube corresponding with the left three catalyst 18 head ends right side one reaction tube corresponding with right catalyst 18 head end right side two reaction tube corresponding with right two catalyst 18 head ends is corresponding with right three catalyst 18 head ends; Described exhaust branch pipe 24 includes left bank trachea, right exhaustor; Described measurement arm 41 is eight, measures pipe including the first from left led to the first from left reaction tube and pipe is measured on pipe is measured on pipe is measured on pipe is measured on pipe is measured on pipe is measured on the second from left that the second from left reaction tube leads to measures pipe and left three reaction tubes lead to a left side three and left bank trachea leads to a left side four and a right reaction tube leads to the right side one and right two reaction tubes lead to the right side two and right three reaction tubes lead to the right side three and right exhaustor leads to the right side four. Before testing, distribution portion has been mixed to form the modified gas meeting test request, ammonia formation component is also ready for enough reduction ammonias and forms reacting gas with modified gas, each reaction arm 21 and the correspondence measured on arm 41 regulate valve and are closed mode, control valve on described exhaust branch pipe 24 is opening, when test, realized reaction and the measurement of different catalysts 18 operating mode by following mode of operation:
1. the test data under the catalyst 18 cooperation state of three, left chamber of test: during reaction, open the adjustment valve on the first from left reaction tube, reacting gas is made to flow to the head end of the first from left catalyst 18 by the first from left reaction tube, know from experience due to reaction gas and flow successively through the first from left catalyst 18, the second from left catalyst 18 and left three catalyst 18, reacting gas reaction under each catalyst 18 acts on forms reaction end gas, and by row outside left bank trachea; Course of reaction carries out parameter measurement, open the first from left and measure the adjustment valve on pipe, for collecting reacting gas sample gas, open the left four adjustment valves measuring on pipe, for collecting the sample gas of reaction end gas, analyze two groups of sample gas by flue gas analyzer 39 and obtain reduced parameter, and then obtain catalyst 18 efficiency data.
In practical operation, when testing right three catalyst 18 in chamber, also should adopt aforesaid operations mode, to obtain three, right chamber catalyst 18 duty test data simultaneously.
2. test the first from left catalyst 18 test data: during reaction, open the adjustment valve on the first from left reaction tube, reacting gas is made to flow to the head end of the first from left catalyst 18 by the first from left reaction tube, know from experience due to reaction gas and flow successively through the first from left catalyst 18, the second from left catalyst 18 and left three catalyst 18, reacting gas reaction under each catalyst 18 acts on forms reaction end gas, and by row outside left bank trachea; Course of reaction carries out parameter measurement, open the first from left and measure the adjustment valve on pipe, for collecting reacting gas sample gas, open the second from left and measure the adjustment valve on pipe, for collecting the sample gas of reaction end gas, two groups of sample gas represent the gas componant before by the first from left catalyst 18 and respectively by the gas componant after the first from left catalyst 18, analyze two groups of sample gas by flue gas analyzer 39 and obtain reduced parameter, and then obtain catalyst 18 efficiency data.
In practical operation, when testing a right catalyst 18, also should adopt aforesaid operations mode, to obtain a right catalyst 18 duty test data.
3, test the second from left catalyst 18 test data: during reaction, open the adjustment valve on the second from left reaction tube, reacting gas is made to flow to the head end of the second from left catalyst 18 by the second from left reaction tube, know from experience due to reaction gas and flow successively through the second from left catalyst 18 and left three catalyst 18, reacting gas reaction under each catalyst 18 acts on forms reaction end gas, and by row outside left bank trachea; Course of reaction carries out parameter measurement, open the second from left and measure the adjustment valve on pipe, for collecting reacting gas sample gas, open the left three adjustment valves measuring on pipe, for collecting the sample gas of reaction end gas, two groups of sample gas represent the gas componant before by the second from left catalyst 18 and respectively by the gas componant after the second from left catalyst 18, analyze two groups of sample gas by flue gas analyzer 39 and obtain reduced parameter, and then obtain catalyst 18 efficiency data.
In practical operation, when testing right two catalyst 18, also should adopt aforesaid operations mode, aforesaid operations mode also should be adopted to obtain corresponding test data.
4. test left three catalyst 18 test datas: during reaction, open the adjustment valve on left three reaction tubes, reacting gas is made to flow to the head end of left three catalyst 18 by left three reaction tubes, know from experience due to reaction gas and flow through left three catalyst 18, reacting gas reaction under catalyst 18 acts on forms reaction end gas, and by row outside left bank trachea; Course of reaction carries out parameter measurement, open the left three adjustment valves measuring on pipe, for collecting reacting gas sample gas, open the left four adjustment valves measuring on pipe, for collecting the sample gas of reaction end gas, two groups of sample gas represent the gas componant before by left three catalyst 18 and respectively by the gas componant after left three catalyst 18, analyze two groups of sample gas by flue gas analyzer 39 and obtain reduced parameter, and then obtain catalyst 18 efficiency data.
In practical operation, when testing right three catalyst 18, also should adopt aforesaid operations mode, aforesaid operations mode also should be adopted to obtain corresponding test data.
5. test the test data under the first from left catalyst 18 and the second from left catalyst 18 cooperation state: during reaction, open the adjustment valve on the first from left reaction tube, reacting gas is made to flow to the head end of the first from left catalyst 18 by the first from left reaction tube, know from experience due to reaction gas and flow successively through the first from left catalyst 18, the second from left catalyst 18 and left three catalyst 18, reacting gas reaction under each catalyst 18 acts on forms reaction end gas, and by row outside left bank trachea; Course of reaction carries out parameter measurement, open the first from left and measure the adjustment valve on pipe, for collecting reacting gas sample gas, open the left three adjustment valves measuring on pipe, for collecting the sample gas of reaction end gas, two groups of sample gas represent the gas componant before by default testing catalytic agent 18 and respectively by the gas componant after default testing catalytic agent 18, analyze two groups of sample gas by flue gas analyzer 39 and obtain reduced parameter, and then obtain catalyst 18 efficiency data.
In practical operation, when testing a right catalyst 18 and right two catalyst 18 cooperation, aforesaid operations mode also should be adopted to obtain corresponding test data.
6. test the test data under the second from left catalyst 18 and left three catalyst 18 cooperation states: during reaction, open the adjustment valve on the second from left reaction tube, reacting gas is made to flow to the head end of the second from left catalyst 18 by the second from left reaction tube, know from experience due to reaction gas and flow successively through the second from left catalyst 18, left three catalyst 18, reacting gas reaction under each catalyst 18 acts on forms reaction end gas, and by row outside left bank trachea; Course of reaction carries out parameter measurement, open the second from left and measure the adjustment valve on pipe, for collecting reacting gas sample gas, open the left four adjustment valves measuring on pipe, for collecting the sample gas of reaction end gas, two groups of sample gas represent the gas componant before by default testing catalytic agent 18 and respectively by the gas componant after default testing catalytic agent 18, analyze two groups of sample gas by flue gas analyzer 39 and obtain reduced parameter, and then obtain catalyst 18 efficiency data.
In practical operation, when testing right two catalyst 18 and right three catalyst 18 cooperation, aforesaid operations mode also should be adopted to obtain corresponding test data.
The mode of test measurement device difference operating mode catalyst 18 combination is not limited to above-described embodiment, it is also possible to left chamber and right chamber are measured simultaneously, to obtain the parameter of real use state of more fitting, also should be regarded as specific embodiments of the invention.
In practical operation, when left chamber and right chamber work simultaneously, control valve by the correspondence being separately positioned on left bank trachea and right exhaustor and realize flow-control, so that the reacting gas flowing through left chamber and right chamber is balanced.
In practical operation, between adjacent catalyst 18, it is provided with gap, it is simple to form the cavity that gas is detained, it is simple to measure arm 41 and gather sample gas; The head end of first section of described accommodating section 19 is provided with acoustic wave ash ejector 25, described ammonia generating assembly includes ammonia generator 26 and a heater 27, and described ammonia generator 26 is contacted successively by pipeline and led to described reaction supervisor 20 after a check valve and described heater 27.
In practical operation, one it is provided with the 6th jumper pipe 30 controlling valve 29 between the described gas outlet of the second dirt catcher 28 and the air inlet of blender 8, described exhaust structure includes a cooling assembly, described cooling assembly includes being located at described aerofluxus and is responsible for the first control valve 31 of 23 first sections, lead to the described first cooling pipe 36 controlling valve 31 air inlet and described second level heat exchanger 7 air inlet and lead to the described first return duct 37 controlling valve 31 gas outlet and heat exchanger 7 gas outlet, the described second level, described cooling pipe 36 and return duct 37 are respectively equipped with the second control valve 32 and the 3rd and control valve 33, it is positioned between the second dirt catcher 28 and second level heat exchanger 7, gas-distribution pipe 9 between second level heat exchanger 7 and blender 8 is respectively equipped with the 4th control valve 34 and the 5th and controls valve 35. owing to needing to provide the reacting gas of each temperature section for reacting part so that the temperature of reaction end gas there will be the temperature range exceeding air-introduced machine 22 normal operation, so needing the reaction end gas to temperature is higher to carry out cooling process. in actual motion, when reacting part needs the reacting gas of lower temperature, open the 4th control valve the 34, the 5th control valve 35 and close the 6th control valve 29, basis flue gas is made to reduce temperature by flowing through first order heat exchanger 6 and second level heat exchanger 7 successively, close the second control valve the 32, the 3rd control valve 33 and open the first control valve 31 so that the low-temp reaction tail gas that reacting part is formed can be discharged either directly through air-introduced machine 22, when reacting part needs the reacting gas of higher temperature, close the 4th control valve 34, 5th controls valve 35 and opens the 6th control valve 29, make basis flue gas by forming high temperature basis flue gas after striding across second level heat exchanger 7 after first order heat exchanger 6, close the first control valve 31 and open the second control valve 32, 3rd controls valve 33, the pyroreaction tail gas that reacting part is formed first passes through cooling pipe 36 and flows through second level heat exchanger 7 and lower the temperature and arrange again through the return duct 37 connect with air-introduced machine 22 is outer, pyroreaction tail gas is by meeting the operating temperature range of air-introduced machine 22 after second level heat exchanger 7 cooling.
In practical operation, described measurement portion include flue gas preprocessor 38, flue gas analyzer 39, be sequentially connected in series described flue gas preprocessor 38, flue gas analyzer 39 measure supervisor 40 and the measurement arm 41 that leads to respectively with described reaction arm 21, exhaust branch pipe 24, described measurement arm 41 is measured supervisor 40 each through corresponding adjustment valve lead to described, and the sample gas that described measurement arm 41 gathers is by measuring supervisor 40 and flow through described flue gas preprocessor 38 successively and flue gas analyzer 39 realizing response data collection.
Described reaction arm 21 leads to described measurement arm 41 by the pipeline being positioned between its adjustment valve and reaction cabin 17, and described exhaust branch pipe 24 leads to described measurement arm 41 by the pipeline being positioned between its flow valve and reaction cabin 17.
In practical operation, the gas outlet of described gas-distribution pipe 9 head end and economizer 1 is led to, also should include the scheme that the pipeline connecting economizer 1 gas outlet leads to gas-distribution pipe 9, pipeline between the access point of gas-distribution pipe 9 and economizer 1 gas outlet does not have valve etc. to hinder structure, also the boiler exhaust gas that can realize discharging from economizer 1 gas outlet is freely accessible to the purpose of gas-distribution pipe 9, in aforesaid way other structure suitable in the technical program, such as leading between aerofluxus supervisor 23 and air preheater 3 gas outlet, cooling pipe 36 controls valve 31 air inlet with first respectively, leading between second level heat exchanger 7 air inlet, return duct 37 controls valve 31 gas outlet with first respectively, leading between second level heat exchanger 7 gas outlet, it is regarded as specific embodiments of the invention. otherwise, described measurement arm is connected on reaction arm or the exhaust branch pipe of correspondence, also should include measuring arm directly to lead to containing cavity, the connection of described measurement arm position on containing cavity and connection being positioned adjacent on containing cavity of corresponding reaction arm or exhaust branch pipe, also should be regarded as specific embodiments of the invention.
Claims (10)
1. a SCR denitration industry test performance testing device, including a test device led to boiler exhaust gas pipeline, described boiler exhaust gas pipeline includes the economizer (1) being sequentially connected in series, scr reactor (2), air preheater (3) and cleaner unit (4), it is characterized in that described test device includes a distribution portion led to described economizer (1) gas outlet, the measurement portion that one reacting part and led to described air preheater (3) gas outlet is arranged on described reacting part, described test device passes through distribution portion, boiler exhaust gas is realized distribution by reacting part, reaction, and carry out sample gas collection and analysis by described measurement portion.
2. a kind of SCR denitration industry test performance testing device according to claim 1, it is characterized in that described distribution portion includes being sequentially connected in series the gas-distribution pipe (9) of the first dirt catcher (5), first order heat exchanger (6), second level dirt catcher (28), second level heat exchanger (7), blender (8), the head end of described gas-distribution pipe (9) and described economizer (1) gas outlet are led to, and tail end leads to described reacting part.
3. a kind of SCR denitration industry test performance testing device according to claim 2, it is characterized in that described distribution portion includes the modified assembly of gas and the modified assembly of steam, the modified assembly of described gas includes a header (10), respectively through the modified unit of the nitric oxide (11) that check valve and described header (10) lead to, the modified unit of sulfur dioxide (12), the modified unit of oxygen (13) and the modified unit of nitrogen (14), connect end outside described header (10) to lead to described blender (8) air inlet afterwards through described first order heat exchanger (6), the modified assembly of described steam includes a water tank (15) and a steam evaporator (16) being connected with described water tank (15), the gas outlet of described steam evaporator (16) and described blender (8) air inlet lead to.
4. according to the arbitrary described a kind of SCR denitration industry test performance testing device of claim 2-3, it is characterized in that described reacting part include an ammonia generating assembly, in set reaction cabin (17) and an exhaust structure of containing cavity, described gas-distribution pipe (9) is led to by a reaction tube group and described containing cavity, described containing cavity is led to by described exhaust structure and described air preheater (3) gas outlet, described ammonia generating assembly and described reaction tube group are led to, and place denitrating catalyst (18) in described containing cavity.
5. a kind of SCR denitration industry test performance testing device according to claim 4, it is characterized in that described containing cavity include some head and the tail lead to and with the accommodating section (19) of full-scale catalyst (18) outline, described reaction tube group includes reaction supervisor (20) led to described distribution portion and the reaction arm (21) led to each accommodating section (19) head end, described reaction arm (21) is led to described reaction supervisor (20) each through corresponding adjustment valve, described exhaust structure includes aerofluxus supervisor (23) that a stage casing sets air-introduced machine (22) and the exhaust branch pipe (24) led to by flow valve with described aerofluxus supervisor (23), the tail end of the inlet end of described exhaust branch pipe (24) section (19) accommodating with described in latter end is corresponding to be led to, the outlet side of described aerofluxus supervisor (23) and described air preheater (3) gas outlet are led to.
6. a kind of SCR denitration industry test performance testing device according to claim 5, it is characterized in that being provided with in described reaction cabin (17) two strip containing cavities, three accommodating sections (19) it are provided with in described containing cavity, described reaction arm (21) is the six roots of sensation, described exhaust branch pipe (24) is two, adjacent catalyst is provided with gap between (18), the head end of first section of described accommodating section (19) is provided with acoustic wave ash ejector (25), described ammonia generating assembly includes an ammonia generator (26) and a heater (27), contacted successively by a pipeline check valve and described heater (27) of described ammonia generator (26) is led to described reaction supervisor (20) afterwards.
7. a kind of SCR denitration industry test performance testing device according to claim 6, it is characterized in that being provided with one between the air inlet of the gas outlet of described second dirt catcher (28) and blender (8) with the 6th jumper pipe (30) controlling valve (29), described exhaust structure includes a cooling assembly, described cooling assembly includes the first control valve (31) being located at first section of described aerofluxus supervisor (23), lead to described first and control valve (31) air inlet and the cooling pipe (36) of described second level heat exchanger (7) air inlet and the return duct (37) leading to described first control valve (31) gas outlet and heat exchanger (7) gas outlet, the described second level, described cooling pipe (36) and return duct (37) are respectively equipped with the second control valve (32) and the 3rd and control valve (33), it is positioned between the second dirt catcher (28) and second level heat exchanger (7), gas-distribution pipe (9) between second level heat exchanger (7) and blender (8) is respectively equipped with the 4th control valve (34) and the 5th and controls valve (35).
8. a kind of SCR denitration industry test performance testing device according to claim 6, it is characterized in that described measurement portion includes flue gas preprocessor (38), flue gas analyzer (39), it is sequentially connected in series described flue gas preprocessor (38), flue gas analyzer (39) measurement supervisor (40) and respectively with described reaction arm (21), the measurement arm (41) that exhaust branch pipe (24) leads to, described measurement arm (41) is led to described measurement supervisor (40) each through corresponding adjustment valve, the sample gas that described measurement arm (41) gathers flows through described flue gas preprocessor (38) successively by measurement supervisor (40) and flue gas analyzer (39) realizes response data collection.
9. a kind of SCR denitration industry test performance testing device according to claim 8, it is characterized in that described reaction arm (21) leads to described measurement arm (41) by being positioned at its pipeline regulated between valve and reaction cabin (17), described exhaust branch pipe (24) leads to described measurement arm (41) by the pipeline being positioned between its flow valve and reaction cabin (17).
10. a SCR denitration industry test performance test methods, comprises the following steps: 1, introduce basis flue gas from economizer (1) gas outlet; 2, basis flue gas is by forming modified gas after the modified assembly of gas and the processing of steam modified assembly; 3, in modified gas, add the reducing gas through preheating, form reacting gas; 4, being passed into by reacting gas in the containing cavity of reaction cabin (17), reacting gas forms reaction end gas after reacting with full-scale catalyst (18); 5, gather reacting gas and reaction end gas, and analyze acquisition flue gas data by flue gas analyzer (39); 6, reaction end gas enters the gas outlet of air preheater (3) by air-introduced machine (22).
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Address after: 311121 Zhejiang Hangzhou Yuhang city Yuhang road 2159-1 Yuhang Zeng energy business building Applicant after: Zhejiang Co., Ltd of Zhe Neng Institute for Research and Technology Address before: 310003, 15 building, Guoxin property building, 108 Feng Lu, Hangzhou, Zhejiang Applicant before: Zhejiang Co., Ltd of Zhe Neng Institute for Research and Technology |