CN104062393A - Mini-type test evaluation device for integral SCR denitration catalyst reaction performance test and application method thereof - Google Patents
Mini-type test evaluation device for integral SCR denitration catalyst reaction performance test and application method thereof Download PDFInfo
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Abstract
The invention relates to a mini-type test evaluation device for integral SCR denitration catalyst reaction performance test and an application method thereof, and belongs to the technical field of catalysis. A flow control instrument and a temperature control instrument control the temperature of a reaction gas sample introduction control device and a heating furnace of a preheating-reacting device; all component gases and water vapor passing through the reaction gas sample introduction control device are converged into a gas mixing device; simulated flue gas getting out of the gas mixing device enters a gas preheating pipe of the preheating-reacting device, the simulated glue gas getting out of the gas preheating pipe enters a catalyst filling pipe of the preheating-reacting device and passes through a catalyst bed layer; the gas passing through the inlet of the gas preheating pipe of the preheating-reacting device and the gas passing through the outlet of the catalyst filling pipe are led into a flue gas composition analyzing system through a sampler. The operation temperature of the device is high, and the measured activity of the catalyst is relatively low but closer to the real value; the barrier in the heat transmitting process and the thermal loss in the process are reduced, and energy saving is facilitated; the time for achieving balance of the device is shortened.
Description
Technical field
The present invention relates to a kind of catalyst reaction device for evaluating performance, be specifically related to a kind of miniature test evaluation device and using method thereof for overall SCR denitrating catalyst reactivity worth test, belong to catalysis technical field.
Background technology
Oxides of nitrogen (NOx) is the main matter that forms acid rain, photo-chemical smog, haze, and health is had to larger harm.Coal-fired power plant, gas fired-boiler are the main sources of NOx discharge.2011 issue " thermal power plant's air pollution emission standard " (GB13223-2011) in, NOx emission limit is by 450mg/m
3be down to 100mg/m
3, it is imperative that NOx controls.For act.std, adopt selective catalytic reduction (Selective Catalytic Reduction, SCR) be that to remove in boiler exhaust gas the most common while of oxides of nitrogen be also effective method the most, be widely used in each boiler of power plant device.
Denitrating catalyst is the technological core of selective catalytic reduction, and its catalyst reaction performance has very important impact to the usefulness of denitration engineering.Catalyzer is selected unreasonable, not only can cause the indexs such as the denitration rate of device not reach guarantee value, also can cause obstruction and the pressure drop of catalyzer to increase, cause boiler operatiopn fault, so the owner of denitrating catalyst manufacturer, engineering design side, use denitrating catalyst all needs denitrating catalyst catalytic perfomance to carry out experiment test.
Domestic existing SCR denitrating catalyst active testing technology is divided at present: on-line testing technology, off-line test technology.On-line testing technology is that SCR Benitration reactor side arranges small-sized parallel reaction device at the scene, inserts full-scale catalyst block to be measured in reactor, and catalyzer monomer cross section is 150mm × 150mm, and the flue gas that test is used is the boiler smoke under real working condition condition.Although the method for on-line testing can better reflect the activity of the catalyzer under service condition, the method for on-line testing is high for equipment requirement, and test sample demand is large, catalyst change process complexity, and test period is long, so seldom adopt.Off-line test technology is to use simulated flue gas to carry out catalyst activity test, and the composition of simulated flue gas and actual condition flue gas composition may have larger difference, still can carry out data conversion by the method for building database in advance.Because off-line test technology can be controlled test condition (flue gas composition, temperature of reaction) preferably, the method can be reappeared test condition easily, be conducive to test between different mechanism for testing comparison, be conducive to the in-house contrast of carrying out between sample, so off-line test technology is applied more widely.
According to the size of test sample, the proving installation that off-line test technology is used can be divided into: medium-sized reactor catalyst performance testing device, microreactor catalyst performance proving installation.It is test gas that medium-sized reactor catalyst performance testing device uses simulated flue gas, the reactivity worth of the whole catalyzer monomer of non-destructive testing, and catalyzer monomer cross section is 150mm × 150mm, tests the reactivity of the catalyzer monomer of 1～4 series connection according to situation.According to test case, the exhaust gas volumn 100-400 standard cube of medium-sized reactor catalyst performance testing device/hour, test equilibration time is greater than 72 hours, and these cause using the expense of medium-sized reactor catalyst performance testing device detecting catalyst reactivity worth very huge.It is test gas that microreactor catalyst performance proving installation uses simulated flue gas, the cross section of test sample is 10 × 10mm-30 × 30mm, typical length 300mm, due to test sample volume greatly reduce, proving installation to the consumption of simulated flue gas be to the maximum 4 standard cubes/hour.Due to microreactor catalyst performance proving installation moderate dimensions, use sample size is little, simulated flue gas gas consumption is little, so device is controlled comparatively easily, testing expense is relatively cheap, more easily by denitrating catalyst manufacturer, engineering design side are accepted, particularly carry out the occasion (Chinese invention patent " a kind of SCR catalyst for denitrating flue gas performance test methods and proving installation ", CN102072947B) of internal quality control.
General minisize reaction performance testing device is that the device of being built according to the drawing of supplier by the catalyzer manufacturing plant introducing technology develops at present, feature is: (1) reactor is made (" laboratory study and exploration ",, 29 volumes in 2010 by stainless steel material, 7 phases, 19 pages); (2) sulphuric dioxide, nitrogen monoxide, nitrogen, oxygen enter stainless steel primary heater after mixing and heat (" China Power " 2010,43 volumes, 11 phases, 64 pages) cryogenic conditions (being generally room temperature) is lower; (3) steam is by being placed in straight shape in heating furnace or serpentine evaporator evaporating liquid water and obtaining (Chinese utility model patent CN 202383117U Fig. 1); (4) simulated flue gas preheating device separates with reactor.
Based on above feature, general microreactor catalyst performance proving installation has following shortcoming at present: (1) is because reactor is stainless steel, visual poor, picks and places comparatively difficulty of test sample in reactor, needs operating personnel to have stronger experience; (2) because reactor and primary heater are stainless steel, stainless steel material can have catalytic action to reaction simulation flue gas under reaction conditions, can not truly reflect the reactivity of catalyzer, and test is active higher; (3) because stainless steel material has comparatively significantly metal atoms migrate phenomenon when temperature is higher than 500 degrees Celsius, at present general minisize reaction performance testing device is after hot conditions test, can there is screw thread bonding phenomenon in the connecting screw of stainless steel reactor, cause reactor to be scrapped; (4) because stainless steel material can react with sulphuric dioxide under high temperature wet condition, cause primary heater and the reactor corrosion of at present general microreactor catalyst performance proving installation serious, so do not pass into sulphuric dioxide when the reactivity worth of common detecting catalyst, this will cause, and catalyst test is active has deviation with actual condition; (5) there are heating furnace inwall-evaporator outer wall, evaporator inwall-evaporative medium two place's heat transfer obstacles in water evaporation device, and in order to obtain the water vapour of rated capacity, the temperature of heating furnace is made as 600 degrees Celsius conventionally, and required energy consumption is larger; (6) smoke pre-heating device separates with reactor, has good heat-insulation layer even if the pipeline between them connects, and still has thermal loss.
Summary of the invention
The object of the invention is to overcome the deficiencies in the prior art part, thereby a kind of miniature test evaluation device and using method thereof for overall SCR denitrating catalyst reactivity worth test is provided.
According to technical scheme provided by the invention, a kind of miniature test evaluation device for overall SCR denitrating catalyst reactivity worth test, the output terminal of reacting gas sample introduction control device utilizes wire to be connected with flow quantity control instrument, the output terminal of steam generator utilizes pipeline to be connected with gas mixer, and the output terminal of reacting gas sample introduction control device utilizes respectively pipeline to be connected with steam generator and gas mixer again; The output terminal of gas mixer utilizes pipeline to be connected with preheating-reactor, and preheating-reactor all utilizes wire to be connected with temperature controller with water vapor generation device; The import and export end of preheating-reactor is connected with reacting gas sampling-analytical equipment; Flow quantity control instrument utilizes respectively wire to be connected with display device with temperature controller.
The furnace temp of flow quantity control instrument and temperature controller control reacting gas sample introduction control device and preheating-reactor; The liquid water that nitrogen carries the plunger type metering pump output of steam generator enters into steam generator; Each composition gas and water vapour through reacting gas sample introduction control device import gas mixer; Enter into the gas economizer bank of preheating-reactor from gas mixer simulated flue gas out, simulated flue gas is heated to and approaches probe temperature; Gas economizer bank simulated flue gas out enters the Catalyst packing pipe of preheating-reactor, passes through beds; By sampler, the exit gas of the inlet gas of the gas economizer bank of preheating-reactor and Catalyst packing pipe is incorporated into flue gas composition analytic system; By control instrument and sensor, temperature, flow, the pressure parameter to test macro monitored and alarm response.
Described reacting gas sample introduction control device comprises N
2volume control device, O
2volume control device, NO volume control device, SO
2volume control device and NH
3volume control device;
Described steam generator comprises volume pump, with the steam generator being connected with volume pump; N
2volume control device is connected with steam generator;
Described O
2volume control device, NO volume control device and SO
2volume control device is all connected with the pipeline being communicated with between steam evaporator and gas mixer;
Described NH
3volume control device directly passes into gas mixer inside by pipeline;
Described reacting gas sampling-analytical equipment comprises flue gas analyzer and sampling selection tee ball valve.
Described N
2volume control device, O
2volume control device, NO volume control device, SO
2volume control device and NH
3the structure of volume control device is identical, with N
2volume control device is example, comprises the first tee ball valve, and a passage in the first tee ball valve is public air intake opening, and one, two other passage is connected with gas mass flow controller, and another is connected with aciculiform variable valve; Gas mass flow controller is connected with two passages of the second tee ball valve with aciculiform variable valve, and another passage of described the second tee ball valve is common pipe gas outlet;
Described steam generator comprises generator body and be positioned at the intrinsic heating rod of generator, and generator body exterior is enclosed with heat-insulation layer; Generator bodies top arranges nitrogen inlet and liquid water entrance, and bottom is provided with steam (vapor) outlet;
Described gas mixer is a pipeline, is provided with several concave point cross sections on pipeline, and each concave point all arranges several concave points on cross section, and on adjacent concave point cross section, the location interval of concave point is identical.
Described preheating-reactor comprises preheating furnace and reacting furnace, and preheating furnace and reacting furnace form an entirety; Preheating furnace inside arranges gas economizer bank, and reacting furnace inside arranges catalyst filling pipe; The caliber of gas economizer bank is greater than the caliber of catalyst filling pipe, and both form a complete tapered pipeline; Described catalyst filling pipe inside is provided with catalyzer, and catalyzer is fixed in catalyst filling pipe by several back-up blocks; The openend of gas economizer bank carries out shutoff by lid.
Between the gas economizer bank of described gas mixer and preheating-reactor, connect by a connecting pipe with arm.
Described connecting pipe, gas mixer, gas economizer bank and catalyst filling pipe are quartz glass tube, pass through spherical ground joint sealing between quartz glass tube; Described steam generator body and heating rod shell are 2520 alloy materials or 316L stainless steel.
Be cut into 100-400mm for test long, the catalytic perfomance of the integral honeycomb shape catalyzer that sectional dimension is 10 × 10mm-30 × 30mm, board-like catalyzer or corrugated plate dst catalyzer.
The method of testing of the described miniature test evaluation device for overall SCR denitrating catalyst reactivity worth test, step is:
By each corresponding volume control device, heating furnace in some position in flow quantity control instrument and temperature controller control device; Nitrogen monoxide, ammonia, sulphuric dioxide, oxygen, nitrogen utilize pipeline to connect with volume control device corresponding in reacting gas sample introduction control device respectively, and nitrogen is through N
2after volume control device, utilize pipeline to flow into the nitrogen inlet of steam generator; Liquid water is pumped into the liquid water entrance of steam generator by plunger type metering pump; Nitrogen is blown into liquid water in steam generator, and directly and heating rod Surface Contact and fast vaporizing, the temperature of steam (vapor) outlet is 300-500 DEG C to liquid water; Nitrogen monoxide, ammonia, sulphuric dioxide, oxygen that water vapour and the metering of reacting gas sample introduction control device are flowed out converge at gas mixer leading portion, are greater than 200 DEG C by the temperature of the simulated flue gas after gas mixer;
Simulated flue gas enters the gas economizer bank of preheating-reactor through connecting pipe, and the gas economizer bank of preheating-reactor is preheating section, and by controlling the preheating furnace heating-up temperature of its surrounded, to make preheating section gas temperature be 250-510 DEG C; The Catalyst packing pipe of preheating-reactor is catalyzer space of living in, makes reaction bed temperature remain on 200-500 DEG C by the reacting furnace heating-up temperature of controlling its surrounded;
Reacting gas sampling-analytical equipment selects tee ball valve selectivity that the exit gas of the Catalyst packing pipe of the inlet gas of the gas economizer bank of preheating-reactor, preheating-reactor is taken out from arm, the catalyst filling pipe tail end of connecting pipe respectively by a sampling, then the gas of taking-up is delivered to flue gas analyzer analysis.
In order to solve the shortcoming of the universal miniature reactivity worth proving installation existence of mentioning in background technology, the present invention improves as follows: (1) gas mixer, gas economizer bank-, and between link adopting quartz glass manufacture, the catalytic action of restraining device wall to test simulation flue gas facilitates tester to fill the reactivity worth of catalyzer under sample and test hot conditions simultaneously; (2) adopt spherical ground, frosted flat-face flange structure to solve the impermeability problem under silica glass material hot conditions; (3) steam generator is the corrosion-resistant thermo-insulating pipe line that inside has heating rod, and nitrogen carries liquid water and after this pipeline, obtains high-temperature steam potpourri; (4) internal mixer has outstanding structure, high temperature mixed vapour, nitrogen monoxide, ammonia, sulphuric dioxide, oxygen enter gas mixer front end together, when they flow through mixer, mixed device inside is given prominence to structure flow-disturbing and is formed cyclone vortex, makes to mix completely; (5) adopt special-shaped reaction tube, realize gas warm-up block and reaction tube module and merge, simplify the attemperator of warm-up block and reaction tube intermodule in original device; (6) by RS485 or RS232 communications protocol, directly use man-machine interface (HMI, Human Machine Interface) flow, temperature control instrument that device is related to manage concentratedly and data acquisition, simplify and in current device, use microcomputer to control and the mode of data acquisition, improved the reliability of system control; (7), when the temperature of temperature control point exceedes alarming value, control instrument cuts off the supply of heating furnace power supply by warning output port trigger relay, and opens corresponding alarm; (8), when reactor pressure exceedes alarming value, pressure transducer trigger relay cuts off heating furnace power supply, cuts out gas flow controller, and opens corresponding alarm; (9), when system gas flow is lower than alarming value, control instrument cuts off the supply of heating furnace power supply by warning output port trigger relay, and opens corresponding alarm.
Beneficial effect of the present invention: (1) device is can operating temperature high; (2) due to the chemical inertness of quartz glass to simulated flue gas, the catalyst activity of measuring is relatively on the low side, but more approaches actual value; (3) due to the inside of heating rod in steam raising plant, reduce the obstacle in heat transfer process, the working temperature of steam raising plant is reduced, be conducive to energy-conservation; (4) due to preheating section and a catalyst reaction Duan Weiyi coherent structure, reduced the thermal loss in process, be conducive to energy-conservation; (5) device reaches the time shorten of balance, is conducive to energy-conservation.
Brief description of the drawings
Fig. 1 is structural representation of the present invention.
Fig. 2 is volume control device schematic diagram.
Fig. 3 is steam generator structural representation.
Fig. 4 is gas mixer structural representation.
Fig. 4-A is gas mixer A-A schematic cross-section.
Fig. 4-B is gas mixer B-B schematic cross-section.
Fig. 5 is the structural representation of gas economizer bank-Catalyst packing pipe.
Fig. 6 is the connecting pipe structure schematic diagram with arm.
Embodiment
Embodiment 1
As shown in Fig. 1-6, a kind of miniature test evaluation device for overall SCR denitrating catalyst reactivity worth test, the output terminal of reacting gas sample introduction control device 1 utilizes wire to be connected with flow quantity control instrument 6, the output terminal of steam generator 2 utilizes pipeline to be connected with gas mixer 3, and the output terminal of reacting gas sample introduction control device 1 utilizes respectively pipeline to be connected with steam generator 2 and gas mixer 3 again; The output terminal of gas mixer 3 utilizes pipeline to be connected with preheating-reactor 4, and preheating-reactor 4 all utilizes wire to be connected with temperature controller 8 with water vapor generation device 2; The import and export end of preheating-reactor 4 is connected with reacting gas sampling-analytical equipment 5; Flow quantity control instrument 6 utilizes respectively wire to be connected with display device 7 with temperature controller 8.
Described reacting gas sample introduction control device 1 comprises N
2volume control device 11, O
2volume control device 12, NO volume control device 13, SO
2volume control device 14 and NH
3volume control device 15;
Described steam generator 2 comprises volume pump 21, with the steam generator 22 being connected with volume pump 21; N
2volume control device 11 is connected with steam generator 22;
Described O
2volume control device 12, NO volume control device 13 and SO
2volume control device 14 is all connected with the pipeline being communicated with between steam evaporator 22 and gas mixer 3;
Described NH
3volume control device 15 directly utilizes pipeline to be connected with gas mixer 3;
Described reacting gas sampling-analytical equipment 5 comprises flue gas analyzer 51 and sampling selection tee ball valve 52.
Described N
2volume control device 11, O
2volume control device 12, NO volume control device 13, SO
2volume control device 14 and NH
3the structure of volume control device 15 is identical, include the first tee ball valve 101, a passage in described the first tee ball valve 101 is public air intake opening, in two other passage, one is connected with gas mass flow controller 102, and another is connected with aciculiform variable valve 103; Gas mass flow controller 102 is connected with two passages of the second tee ball valve 104 with aciculiform variable valve 103, and another passage of described the second tee ball valve 104 is public gas outlet;
Described steam generator 22 comprises generator body 221 and the heating rod 222 that is positioned at generator body 221, and generator body 221 outer wrap have heat-insulation layer 223; Generator body 221 tops arrange nitrogen inlet 224 and liquid water entrance 225, and bottom is provided with steam (vapor) outlet 226;
Described gas mixer 3 is a pipeline, is provided with several concave point cross sections on pipeline, and each concave point all arranges several concave points on cross section, and on adjacent concave point cross section, the location interval of concave point is identical.Be specially the tube shown in Fig. 4, its inside alternately has the structure to inner process shown in Fig. 4-A, Fig. 4-B, makes air-flow form cyclone vortex, strengthening mixed process.
Described preheating-reactor 4 comprises preheating furnace 41 and reacting furnace 42, and preheating furnace 41 and reacting furnace 42 form an entirety; Preheating furnace 41 inside arrange gas economizer bank 43, and reacting furnace 42 inside arrange catalyst filling pipe 44; The caliber of gas economizer bank 43 is greater than the caliber of catalyst filling pipe 44, and both form a complete tapered pipeline; Described catalyst filling pipe 44 inside are provided with catalyzer 45 in use, and catalyzer 45 utilizes several back-up blocks 46 to be fixed in catalyst filling pipe 44; The openend of gas economizer bank 43 is by utilizing lid 47 to carry out shutoff.
Between described gas mixer 3 and the gas economizer bank 43 of preheating-reactor 4, connect by a connecting pipe 9 with arm.
Described connecting pipe 9, gas mixer 3, gas economizer bank 43 and catalyst filling pipe 44 are quartz glass tube, pass through spherical ground joint sealing between quartzy pipe fitting; Described generator body 221, heating rod 222 shells are 2520 alloys or 316L stainless steel material.
Embodiment 2
Choose 086 batch of honeycombed catalyst product that applicant manufactures, be cut to 300 millimeters of length, sectional dimension is the laboratory sample of 25 × 25 millimeters.Sample axial component is wound around appropriate inertia insulation material and then puts into the Catalyst packing pipe inside shown in Fig. 5, and sample upper end is apart from 400 millimeters of gas economizer bank upper ends.Sample interior is inserted temperature thermocouple, by gas economizer bank openend quartz glass cap covers, realizes sealing by frosted flat-face flange.
As shown in Figure 1, coupled reaction gas sampling control device 1, steam generator 2, gas mixer 3, preheating-reactor 4 and reacting gas sampling-analytical equipment 5.By HIM(man-machine interface) use each corresponding temperature, flow instrument for automatic control in some position in RS485 communication modes centralized control system, make each gas flow and furnace temp reach the requirement of experiment condition.Nitrogen monoxide, ammonia, sulphuric dioxide, oxygen, nitrogen connect with the entrance of the corresponding control device in reacting gas sample introduction control device 1 respectively with pipeline, and the concrete connection of control device as shown in Figure 2.
Shown in Fig. 1, nitrogen flow into the nitrogen inlet 224 of the steam generator 2 shown in Fig. 3 after answering the Nitrogen Control Units in gas sampling control section by pipeline.Liquid water is pumped into the liquid water entrance 225 of the steam generator 2 shown in Fig. 3 according to setting flow by plunger type metering pump 21.Nitrogen is blown into liquid water in the generator body of steam generator 2 in 221 fast, equably, and directly and heating rod Surface Contact and fast vaporizing, outlet temperature is 400 DEG C to liquid water.Nitrogen monoxide, ammonia, sulphuric dioxide, oxygen that water vapour and 1 metering of reacting gas sample introduction control device are flowed out converge at gas mixer 3 leading portions, are 200 DEG C by the temperature of the simulated flue gas after gas mixer 3.
Simulated flue gas enters in the gas economizer bank of the preheating-reactor 4 shown in Fig. 5 through the quartzy interface unit shown in Fig. 6, and the connection sealing between quartz is existing by the cause for gossip of GB 28# pot mill.The gas economizer bank 43 of preheating-reactor 4 is preheating section, and by controlling the reacting furnace heating-up temperature of its surrounded, to make preheating section gas temperature be 390 DEG C.The Catalyst packing pipe 44 of preheating-reactor 4 is catalyzer space of living in, makes reaction bed temperature remain on 380 DEG C by controlling the reacting furnace heating-up temperature of its surrounded.
Reacting gas sampling-analytical equipment 5 as shown in Figure 1, by tee ball valve 52 selectivity, the exit gas of the Catalyst packing pipe (44) of the inlet gas of the gas economizer bank (43) of preheating-reactor (4), preheating-reactor (4) is taken out from Catalyst packing pipe (44) tail end shown in the arm shown in Fig. 6, Fig. 5 respectively, then the gas of taking-up is delivered to flue gas analyzer 51 and analyze.
Beds alarm temperature is set to 400 DEG C, heightens preheating furnace 41 heating-up temperatures, and reaction bed temperature is higher than 400 DEG C time, trigger temperature alarming, control instrument is by warning output port trigger relay, and system is cut off heating power supply, cut off source of the gas, alarm is opened.Other temperature control points also can have identical alarm mechanism.Reaction system alarm pressure is set to 0.05MPa, in the present embodiment, normal force value is 0.04MPa, nitrogen flow is tuned up, system pressure exceedes 0.05MPa, trigger pressure alarm, control instrument is by warning output port trigger relay, and system is cut off heating power supply, cut off source of the gas, alarm is opened.In the present embodiment, normal nitrogen flow value is 52 liters/min, and by nitrogen inlet valve closing, nitrogen flow value is less than 40 liters/min of warning flows, triggering flow is reported to the police, and control instrument is by warning output port trigger relay, and system is cut off heating power supply, cut off source of the gas, alarm is opened.In the present embodiment, normal nitrogen flow value is 52 liters/min, and nitrogen inlet pressure is raise, and nitrogen flow value is greater than 60 liters/min of warning flows, triggering flow is reported to the police, and control instrument is by warning output port trigger relay, and system is cut off heating power supply, cut off source of the gas, alarm is opened.Nitrogen monoxide, ammonia, sulphuric dioxide, oxygen flux control point also can have flow super large or alarm mechanism less than normal.By gas mass flow controller dump corresponding nitrogen monoxide gas circuit, analog gas mass flow controller distress condition, two tee ball valves that identify in Fig. 2 are rotated to " manually " position from " automatically " position simultaneously, regulate the aciculiform variable valve identifying in Fig. 2 to the position of demarcating in advance, other gases also have identical control mode conversion.
In the present embodiment, steam exit temperature is 450 DEG C, 390 DEG C of gas preheating section temperature, and 380 DEG C of reaction bed temperatures, device reaches equilibrium state and takes 90 minutes.In the present embodiment, reactor inlet place nitric oxide concentration is 180ppm, ammonia 180ppm, oxygen 2.00%, sulphuric dioxide 100ppm; Reactor exit nitric oxide concentration is 95ppm, ammonia 89ppm, oxygen 1.97%, sulphuric dioxide 97ppm, nitrogen monoxide conversion ratio 47.2%.
Embodiment 3
Install most of state and parameter setting is identical with embodiment 2, difference is in order to make reaction bed temperature reach 500 DEG C, reacting furnace heating-up temperature by preheating-reactor 4 upper end surrounded is 530 DEG C, making gas preheating section gas temperature is 510 DEG C, be 510 DEG C by the reacting furnace heating-up temperature of controlling reactor lower end surrounded, make reaction bed temperature remain on 500 DEG C.Reactor no damage occurred phenomenon.
In the present embodiment, steam exit temperature is 500 DEG C, 510 DEG C of gas preheating section temperature, 500 DEG C of reaction bed temperatures.Reactor inlet place nitric oxide concentration is 179ppm, ammonia 180ppm, oxygen 2.01%, sulphuric dioxide 100ppm; Reactor exit nitric oxide concentration is 15ppm, ammonia 0ppm, oxygen 1.70%, sulphuric dioxide 59ppm, nitrogen monoxide conversion ratio 91.6%.
Embodiment 4
The corrugated plate dst catalyzer of choosing certain power plant's censorship, is cut to length 400mm, the laboratory sample that sectional dimension is 20 × 20mm.Unit state parameter arranges identical with embodiment 2, and simulated flue gas flow is adjusted according to the area parameters of sample.
In the present embodiment, steam exit temperature is 400 DEG C, 250 DEG C of gas preheating section temperature, 200 DEG C of reaction bed temperatures.Reactor inlet place nitric oxide concentration is 180ppm, ammonia 179ppm, oxygen 1.99%, sulphuric dioxide 99ppm; Reactor exit nitric oxide concentration is 100ppm, ammonia 95ppm, oxygen 1.97%, sulphuric dioxide 99ppm, nitrogen monoxide conversion ratio 44.4%.
Embodiment 5
Choose the board-like catalyzer of so-and-so power plant's censorship, be cut to 4 length 400mm, wide 30mm bar, puts into quartz glass support, assembling growth 400mm, the laboratory sample that sectional dimension is 30 × 30mm.Unit state parameter arranges identical with embodiment 2, and simulated flue gas flow is adjusted according to the area parameters of sample.
In the present embodiment, steam exit temperature is 450 DEG C, 410 DEG C of gas preheating section temperature, 380 DEG C of reaction bed temperatures.Reactor inlet place nitric oxide concentration is 181ppm, ammonia 180ppm, oxygen 2.00%, sulphuric dioxide 101ppm; Reactor exit nitric oxide concentration is 105ppm, ammonia 100ppm, oxygen 1.99%, sulphuric dioxide 100ppm, nitrogen monoxide conversion ratio 41.98%.
Embodiment 6
Choose aperture honeycombed catalyst product, be cut to length 100mm, the laboratory sample that sectional dimension is 10 × 10mm.Unit state parameter arranges identical with embodiment 2, and simulated flue gas flow is adjusted according to the area parameters of sample.
In the present embodiment, steam exit temperature is 300 DEG C, 400 DEG C of gas preheating section temperature, 350 DEG C of reaction bed temperatures.Reactor inlet place nitric oxide concentration is 180ppm, ammonia 180ppm, oxygen 2.00%, sulphuric dioxide 100ppm; Reactor exit nitric oxide concentration is 85ppm, ammonia 80ppm, oxygen 1.99%, sulphuric dioxide 95ppm, nitrogen monoxide conversion ratio 52.8%.
Comparative example 1
Catalyst activity system safety testing device is built according to imported technology data.Nitrogen, oxygen, nitrogen monoxide, sulphuric dioxide enter stainless steel multi-chamber mixer through gas flow control section, after mixing in mixer, enter the stainless-steel tube of a 500mm length, internal diameter 40mm, the liquid water of the metering of ammonia and volume pump output also enters in this stainless-steel tube.Nitrogen, oxygen, nitrogen monoxide, sulphuric dioxide, water, ammonia are vaporized in this stainless-steel tube, preheating.Above-mentioned simulated flue gas enters stainless steel reactor through stainless-steel tube.
Choose 086 batch of honeycombed catalyst product that embodiment 1 uses, be cut to length 300mm, the laboratory sample that sectional dimension is 25 × 25mm.Sample axial component is wound around appropriate inertia insulation material and then puts into stainless steel reactor.Under experiment condition, 400 DEG C of the stainless-steel tube outlet temperatures of aforementioned 500mm length, internal diameter 40mm, peripheral heating furnace is set to 650 DEG C.The peripheral heating furnace of stainless steel reactor is set to 390 degrees Celsius, 380 DEG C of reaction bed temperatures.
In the present embodiment, vaporization-primary heater control temperature is 650 DEG C, 390 DEG C of catalyst section control temperature, and 380 DEG C of reaction bed temperatures, device reaches equilibrium state and takes 120 minutes.
In the present embodiment, reactor inlet place nitric oxide concentration is 181ppm, ammonia 180ppm, oxygen 1.99%, sulphuric dioxide 100ppm; Reactor exit nitric oxide concentration is 90ppm, ammonia 87ppm, oxygen 1.97%, sulphuric dioxide 30ppm, nitrogen monoxide conversion ratio 50.3%.After experiment finishes, reactor finds that there is corrosion condition.
Comparative example 2
Install most of state and parameter setting is identical with comparative example 1, difference is in order to make reaction bed temperature reach 500 DEG C, vaporization-primary heater control temperature is 670 DEG C, 600 DEG C of catalyst section control temperature, 510 DEG C of reaction bed temperatures, device reaches equilibrium state and takes 240 minutes, after experiment finishes, and stainless steel reactor connecting screw dismounting difficulty.
Claims (10)
1. the miniature test evaluation device for overall SCR denitrating catalyst reactivity worth test, it is characterized in that: the output terminal of reacting gas sample introduction control device (1) utilizes wire to be connected with flow quantity control instrument (6), the output terminal of steam generator (2) utilizes pipeline to be connected with gas mixer (3), and the output terminal of reacting gas sample introduction control device (1) utilizes respectively pipeline to be connected with steam generator (2) and gas mixer (3) again; The output terminal of gas mixer (3) utilizes pipeline to be connected with preheating-reactor (4), and preheating-reactor (4) all utilizes wire to be connected with temperature controller (8) with water vapor generation device (2); The import and export end of preheating-reactor (4) is connected with reacting gas sampling-analytical equipment (5); Flow quantity control instrument (6) utilizes respectively wire to be connected with display device (7) with temperature controller (8).
2. as claimed in claim 1 for the miniature test evaluation device of overall SCR denitrating catalyst reactivity worth test, it is characterized in that:
Described reacting gas sample introduction control device (1) comprises N
2volume control device (11), O
2volume control device (12), NO volume control device (13), SO
2volume control device (14) and NH
3volume control device (15);
Described steam generator (2) comprises volume pump (21), with the steam generator (22) being connected with volume pump (21); Described N
2volume control device (11) is connected with steam generator (22);
Described O
2volume control device (12), NO volume control device (13) and SO
2volume control device (14) is all connected with the pipeline being communicated with between steam generator (22) and gas mixer (3);
NH
3volume control device (15) directly utilizes pipeline to be connected with gas mixer (3);
Described reacting gas sampling-analytical equipment (5) comprises flue gas analyzer (51) and sampling selection tee ball valve (52).
3. as claimed in claim 2 for the miniature test evaluation device of overall SCR denitrating catalyst reactivity worth test, it is characterized in that:
N
2volume control device (11), O
2volume control device (12), NO volume control device (13), SO
2volume control device (14) and NH
3the structure of volume control device (15) is identical, include the first tee ball valve (101), a passage in described the first tee ball valve (101) is public air intake opening, in two other passage, one is connected with gas mass flow controller (102), and another is connected with aciculiform variable valve (103); Gas mass flow controller (102) is connected with two passages of the second tee ball valve (104) with aciculiform variable valve (103), and another passage of described the second tee ball valve (104) is public gas outlet.
4. the miniature test evaluation device of testing for overall SCR denitrating catalyst reactivity worth as claimed in claim 2, it is characterized in that: described steam generator (22) comprises generator body (221) and be positioned at the heating rod (222) of generator body (221), generator body (221) outer wrap has heat-insulation layer (223); Generator body (221) top arranges nitrogen inlet (224) and liquid water entrance (225), and bottom is provided with steam (vapor) outlet (226).
5. the miniature test evaluation device of testing for overall SCR denitrating catalyst reactivity worth as claimed in claim 2, it is characterized in that: described preheating-reactor (4) comprises preheating furnace (41) and reacting furnace (42), preheating furnace (41) and reacting furnace (42) form an entirety; Preheating furnace (41) inside arranges gas economizer bank (43), and reacting furnace (42) inside arranges catalyst filling pipe (44); The caliber of gas economizer bank (43) is greater than the caliber of catalyst filling pipe (44), and both form a complete tapered pipeline; Described catalyst filling pipe (44) inside is provided with catalyzer to be tested (45) in use, and catalyzer (45) utilizes several back-up blocks (46) to be fixed in catalyst filling pipe (44); The openend of gas economizer bank (43) utilizes lid (47) to carry out shutoff.
6. the miniature test evaluation device of testing for overall SCR denitrating catalyst reactivity worth as claimed in claim 5, it is characterized in that: described gas economizer bank (43) and catalyst filling pipe (44) are quartz glass tube, between stone quartz glass tube, pass through spherical ground joint sealing.
7. as claimed in claim 1 for the miniature test evaluation device of overall SCR denitrating catalyst reactivity worth test, it is characterized in that: between described gas mixer (3) and preheating-reactor (4), connect by a connecting pipe with arm (9).
8. the miniature test evaluation device of testing for overall SCR denitrating catalyst reactivity worth as claimed in claim 7, it is characterized in that: described connecting pipe (9) is quartz glass tube with gas mixer (3), between stone quartz glass tube, pass through spherical ground joint sealing.
9. as claimed in claim 4 for the miniature test evaluation device of overall SCR denitrating catalyst reactivity worth test, it is characterized in that: described generator body (221), heating rod (222) shell are 2520 alloy materials or 316L stainless steel.
10. the using method of the miniature test evaluation device of testing for overall SCR denitrating catalyst reactivity worth described in claim 1, is characterized in that step is:
By each corresponding volume control device and heating furnace in some position in flow quantity control instrument (6) and temperature controller (8) control device; Nitrogen monoxide, ammonia, sulphuric dioxide, oxygen, nitrogen connect with volume control device corresponding in reacting gas sample introduction control device (1) respectively with pipeline, and nitrogen is through N
2after volume control device (11), flow into the nitrogen inlet (224) of steam generator (2) by pipeline; Liquid water is pumped into liquid water entrance (225) by plunger type metering pump (21); Nitrogen is blown into liquid water in steam generator (2), and directly and heating rod (222) Surface Contact and fast vaporizing, the temperature of steam (vapor) outlet (226) is 300-500 DEG C to liquid water; Nitrogen monoxide, ammonia, sulphuric dioxide, oxygen that water vapour and reacting gas sample introduction control device (1) metering are flowed out converge at gas mixer (3) leading portion, are greater than 200 DEG C by the temperature of the simulated flue gas after gas mixer (3);
Simulated flue gas enters the gas economizer bank (43) of preheating-reactor (4) through connecting pipe (9), and by controlling preheating furnace (41) heating-up temperature of its surrounded, to make preheating section gas temperature be 250-510 DEG C; The Catalyst packing pipe (44) of preheating-reactor (4) is catalyzer space of living in, makes reaction bed temperature remain on 200-500 DEG C by reacting furnace (42) heating-up temperature of controlling its surrounded;
Reacting gas sampling-analytical equipment (5) selects tee ball valve (52) selectivity that the exit gas of the inlet gas of the gas economizer bank (43) of preheating-reactor (4) and Catalyst packing pipe (44) is taken out from the arm of connecting pipe (9) and the tail end of catalyst filling pipe (44) respectively by sampling, then the gas of taking-up is delivered to flue gas analyzer (51) and is analyzed.
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Address after: No.6 Yongsheng Road, Yixing Economic Development Zone, Wuxi City, Jiangsu Province Patentee after: Guoneng Longyuan catalyst Jiangsu Co.,Ltd. Address before: 214151 No. 78, qianluo Road, Qianqiao Town, Huishan District, Wuxi City, Jiangsu Province Patentee before: JIANGSU LONGYUAN CATALYST Co.,Ltd. |