CN105510532A - Denitration catalytic performance evaluation system and method - Google Patents
Denitration catalytic performance evaluation system and method Download PDFInfo
- Publication number
- CN105510532A CN105510532A CN201510943042.3A CN201510943042A CN105510532A CN 105510532 A CN105510532 A CN 105510532A CN 201510943042 A CN201510943042 A CN 201510943042A CN 105510532 A CN105510532 A CN 105510532A
- Authority
- CN
- China
- Prior art keywords
- reactor
- gas
- air intake
- intake opening
- flue gas
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
Classifications
-
- G—PHYSICS
- G01—MEASURING; TESTING
- G01N—INVESTIGATING OR ANALYSING MATERIALS BY DETERMINING THEIR CHEMICAL OR PHYSICAL PROPERTIES
- G01N33/00—Investigating or analysing materials by specific methods not covered by groups G01N1/00 - G01N31/00
Abstract
The invention relates to a denitration catalytic performance evaluation system and method. The evaluation system comprises a distributed gas metering system, a gas preheating system, an SCR system, a gas-gas heat exchanger (16), a tail gas treatment system and a data collection and control system. Through the system and method, the ammonia-nitrogen molar ratio, denitration efficiency, the ammonia escape rate, activity and the SO2/SO3 conversion rate of reactor catalysts can be obtained. The system has complete functions, is accurate and reliable in operation and can be widely applied to evaluation of catalytic performance on laboratory conditions.
Description
Technical field
The present invention relates to denitrating flue gas field, be specifically related to a kind of denitrating catalyst Performance Appraisal System and evaluation method thereof.
Background technology
Oxynitrides (NOx) is one of main flue gas pollutant of fuel-burning power plant, and its a large amount of discharge not only can cause acid rain and photo-chemical smog, and to health cause also can be larger injury.According to regulation in " thermal power plant's Air Pollutant Emission " (GB13223-2011), coal-burning power plant's NOx concentration will perform 100mg/Nm
3emission limit.According to this requirement, there is the main flow that denitration efficiency is high, the SCR of technology maturation, non-secondary pollution (selectivecatalyticreduction, SCR) technology becomes flue-gas denitration process gradually.
Denitrating catalyst is the core of denitrification apparatus, belongs to " loss " parts.Domestic Catalyst Production producer is many, technology is uneven, and Catalyst Production supervision, operational management is not perfect, and user is to raw catelyst performance index, and to running the performance degradation of catalyzer, life-span, replacement cycle be all in unknown state.At present, the problems such as denitrification apparatus ubiquity the escaping of ammonia exceeds standard, catalyzer accelerates inactivation, catalyzer high temperature sintering, cold operation performance degradation, air preheater blocking dust stratification, the economy of unit operation, reliability and continuity are had a strong impact on, the oepration at full load of even serious operating unit.Therefore, network based on denitrating catalyst and run present situation, needing exploitation a kind of multiple functional, denitrating catalyst device for evaluating performance and method thereof accurately and reliably, for power plant's Selection of Catalyst provides strong foundation.
Summary of the invention
Technical matters to be solved by this invention is to provide a kind of multiple functional, denitrating catalyst Performance Appraisal System and evaluation method thereof accurately and reliably.
The technological means that the present invention adopts is:
A kind of denitrating catalyst Performance Appraisal System, comprises distribution metering system, air preheat system, SCR catalytic reaction system, gas-gas heat exchanger, exhaust treatment system and control system;
Described distribution metering system comprises NH
3air intake opening, SO
2air intake opening, NO air intake opening, the first cushion gas air intake opening, the second cushion gas air intake opening, nitrogen inlet, air inlet, water vapor air intake opening, evener and mixing arrangement, described NH
3air intake opening is connected with described mixing arrangement, described SO
2air intake opening, NO air intake opening, the first cushion gas air intake opening, the second cushion gas air intake opening, nitrogen inlet, air inlet are connected with evener, and described evener is connected with described gas-gas heat exchanger; The import and export pipeline of described gas-gas heat exchanger is equipped with temperature point; Each gas piping is all equipped with mass-flow gas meter, each gas piping is arranged the pitch aperture being used for adjustments of gas mass rate;
Described air preheat system comprises the first preheating furnace and second preheating furnace of two-stage series connection, and the first preheating furnace and the second preheating furnace are vertical; Described first preheating furnace is connected with described gas-gas heat exchanger, and described second preheating furnace is connected with described mixing arrangement;
Described SCR catalytic reaction system is the reactor of two-way in parallel, and a road is single first reactor of the catalyst performance for checking section 150 × 150mm; Another road is 3 reactors of connecting of the catalyst performance for checking 75 × 75mm, and 3 reactors are respectively the second reactor, the 3rd reactor, the 4th reactor; The free length that first reactor, the second reactor, the 3rd reactor, the 4th reactor install catalyzer is respectively not less than 1500mm; First reactor, the second reactor, the 3rd reactor, the 4th reactor import and export place are equipped with pressure-measuring-point and temperature point, and the reactor end distance that pressure-measuring-point is corresponding with it is not less than reactor 2 times of equivalent diameters; All arrange front thief hatch and post-sampling mouth before and after first reactor, the second reactor, the 3rd reactor, the 4th reactor, described front thief hatch and post-sampling mouth are for being connected the flue gas sampling pipe on flue gas analyzer;
Described exhaust treatment system comprises spray column, alkali lye pond and feeding spraying pump, and described spray column and alkali lye pond are by pipeline connection, and feeding spraying pump is connected with spray column; Described spray column is connected with gas-gas heat exchanger, is provided with frequency conversion fan between described spray column and gas-gas heat exchanger, arranges line pressure measuring point and temperature point before described frequency conversion fan;
The pressure signal that the temperature signal that the mass flow rate signal that described mass-flow gas meter records, temperature point record, pressure-measuring-point record, frequency conversion fan are connected with control system.
Further, described NH
3air intake opening, SO
2air intake opening, NO air intake opening, the first cushion gas air intake opening, the second cushion gas air intake opening and be equipped with corresponding gas steel cylinder be connected, described nitrogen inlet is connected with nitrogen preparation facilities, described air inlet is connected with air compressor machine, and described water vapor air intake opening is connected with syringe pump.
Further, carry out denitrating catalyst method of evaluating performance with denitrating catalyst Performance Appraisal System, comprise the steps:
A. according to flue gas flow, the oxygen flow of simulation, control system is utilized to set nitrogen and air mass flow;
B. according to the flue-gas temperature of simulation, utilize control system to set the first preheating furnace, the second preheating furnace, the first reactor, the second reactor, the 3rd reactor, the 4th temperature of reactor, wherein the second preheating furnace temperature should set consistent with the second reactor, the 3rd reactor, the 4th temperature of reactor;
C. after the first preheating furnace, the second preheating furnace, the first reactor, the second reactor, the 3rd reactor, the 4th temperature of reactor reach its setting value, according to the moisture of simulation, control system is utilized to set the metered shot pump supply water yield;
D. according to exhaust gas volumn and the flue gas composition of simulation, control system is utilized to set SO
2, NO, NO
2, CO
2and NH
3flow;
E. utilize control system to set pressure before frequency conversion fan, before realizing blower fan by automatically regulating frequency conversion fan frequency, pressure stability controls;
F. utilize flue gas analyzer to detect the first reactor, the second reactor, the 3rd reactor, the 4th reactor post-sampling mouth Gas Parameters, after stable to be placed into all reactor post-sampling mouth Gas Parameters of catalyzer, can catalyst performance evaluation be carried out;
G. control valve is passed through, make the flue gas flowed out from mixing arrangement by means of only a reactor the first reactor, the second reactor, the 3rd reactor, the 4th reactor, flue gas analyzer is accessed thief hatch and post-sampling mouth before the reactor that flue gas passes through, by test SO
2, NO, NO
2, CO
2, SO
3and NH
3flue gas concentration, the ammonia nitrogen mol ratio of any one reactor catalyst in the first reactor, the second reactor, the 3rd reactor, the 4th reactor, denitration efficiency, the escaping of ammonia rate, activity and SO can be obtained
2/ SO
3conversion ratio.
Further, g step can be replaced by following steps: early gate and the late gate of closing the first reactor, make second reactor, three reactor and four reactor of flue gas by connecting that flow out from mixing arrangement, flue gas analyzer is accessed thief hatch and the 4th reactor post-sampling mouth before the second reactor, by test SO
2, NO, NO
2, CO
2, SO
3and NH
3flue gas concentration, the ammonia nitrogen mol ratio of third-order reaction system catalyst, denitration efficiency, the escaping of ammonia rate and SO can be obtained
2/ SO
3conversion ratio.
Further, g step can be replaced by following steps: pass through control valve, make the flue gas flowed out from mixing arrangement by means of only any two reactors the second reactor, the 3rd reactor, the 4th reactor, flue gas analyzer is connect the front thief hatch of first reactor and the post-sampling mouth of a rear reactor in these two reactors, by test SO
2, NO, NO
2, CO
2, SO
3and NH
3flue gas concentration, the ammonia nitrogen mol ratio of two-stage reaction system catalyst, denitration efficiency, the escaping of ammonia rate and SO can be obtained
2/ SO
3conversion ratio.
Beneficial effect of the present invention:
The present invention accurately and reliably can realize the NH in flue gas
3, SO
2, NO, O
2and the simulation of the component such as water vapour, and cushion gas interface is set, improve the popularity of package unit application; The catalyst performance evaluation of 2 kinds of sizes, maximum 3 number of levels can be realized, pass through valve transfer, any one reactor can carry out single-stage evaluating catalyst, and any two reactors can carry out double-deck progression catalyst performance evaluation, improves the applicability of package unit application; Device is provided with gas-gas heat exchanger, effectively can reduce the heating energy consumption of combination gas, improve the economy of plant running; Device afterbody is provided with exhaust gas processing device, effectively reduces the pollution to surrounding enviroment; Described evaluation method is simple and reliable, can realize the ammonia nitrogen mol ratio of any one stage catalyzing dose, denitration efficiency, the escaping of ammonia rate, activity and SO
2/ SO
3the evaluation of the indexs such as conversion ratio.The present invention is multiple functional, run accurately and reliably, can be widely used in evaluate catalysts performance in laboratory conditions.
Accompanying drawing explanation
Fig. 1 is the schematic diagram of the embodiment of the present invention.
In accompanying drawing, 1-NH
3air intake opening, 2-SO
2air intake opening, 3-NO air intake opening, 4-nitrogen inlet, 5-air inlet, 6-water vapor air intake opening, 7-first cushion gas air intake opening, 8-second cushion gas air intake opening, 9-nitrogen preparation facilities, 10-air compressor machine, 11-steel cylinder, 12-syringe pump, 13-mass flowmeter, 14-pitch aperture, 15-evener, 16-gas-gas heat exchanger, the hot stove of 17-first, 18-second preheating furnace, 19-temperature point, 20-mixing arrangement, 21-1 ~ 21-11-valve, 22 first reactors, 23-1-second reactor, 23-2-the 3rd reactor, 23-3-the 4th reactor, 24-pressure-measuring-point, thief hatch before 25-1-, 25-2-post-sampling mouth, 26-frequency conversion fan, 27-spray column, 28-feeding spraying pump, 29-alkali lye pond.
Embodiment
Embodiment 1
As shown in Figure 1, a kind of denitrating catalyst Performance Appraisal System, comprises distribution metering system, air preheat system, SCR catalytic reaction system, gas-gas heat exchanger, exhaust treatment system and control system.
Described denitrating catalyst Performance Appraisal System is provided with 8 road air intake openings, is respectively NH
3air intake opening 1, SO
2air intake opening 2, NO air intake opening 3, first cushion gas air intake opening 7, second cushion gas air intake opening 8, nitrogen inlet 4, air inlet 5, water vapor air intake opening 6, wherein N
2produced by nitrogen preparation facilities 9, O
2content is introduced air 5 by air compressor machine 10 and is regulated, NH
3, SO
2, NO and the first cushion gas, the second cushion gas use steel cylinder 11 gas, the metered shot pump 12 that water vapour 6 use traffic is adjustable adds water and to produce through heating.
NH
3, SO
2, NO, N
2, air and each gas piping such as the first cushion gas, the second cushion gas are all equipped with mass-flow gas meter 13, each gas flow is regulated by the pitch aperture 14 changing corresponding pipeline.Gas piping flow signal of improving quality feeds back to control system.
SO
2, NO, N
2, air and the first cushion gas, the second cushion gas enter gas-gas heat exchanger 16 and gas pre-heating system successively after evener 15 mixes.
Described air preheat system adopts two-stage series connection first preheating furnace 17, second preheating furnace 18 to form, and is vertical, for heating the water vapour of the mixed gas after gas-gas heat exchanger 16 and syringe pump 12 generation.Water vapour is vaporized after instilling the first preheating furnace 17 by aqueous water by the metered shot pump 12 that flow is adjustable generation, and the liquid water yield is by metered shot pump 12 regulable control.First preheating furnace 17, second preheating furnace 18 is imported and exported and is equipped with temperature point 19, first preheating furnace 17, second preheating furnace 18 temperature regulates and adopts automatic control mode, the wide temperature range that two preheating furnaces realize 80 ~ 450 DEG C regulates, and all temperature signals feed back to control system.
Combination gas goes out after the second preheating furnace 18 and NH
3through mixing arrangement 20, enter SCR catalytic reaction system.Described SCR catalytic reaction system is two-way in parallel, by controlled valve 21-1 ~ valve 21-11, can realize the catalyst performance evaluation of 2 kinds of sizes, maximum 3 number of levels.One tunnel is single first reactor 22, for checking the catalyst performance of section 150 × 150mm; Another road is the reactor of 3 series connection, is respectively the second reactor 23-1 ~ the 4th reactor 23-3, for checking the catalyst performance of 75 × 75mm; The free length that each reactor installs catalyzer is not less than 1500mm.Second reactor 23-1 ~ each reactor of the 4th reactor 23-3 is provided with the pipeline be in parallel respectively with it, the parallel pipeline of the second reactor 23-1 is provided with valve 23-9, the parallel pipeline of the 3rd reactor 23-2 is provided with valve 23-10, the parallel pipeline of the 4th reactor 23-3 is provided with valve 23-11, before and after the first reactor 22, second reactor 23-1, the 3rd reactor 23-2, each reactor of the 4th reactor 23-3, is provided with valve.
Described SCR catalytic reaction system, each reactor import and export place is equipped with pressure-measuring-point 24, and by signal feedback to control system, pressure-measuring-point 24 and its reactor end, place distance are not less than place reactor 2 times of equivalent diameters; In each reactor and pipeline, flue-gas temperature regulates and adopts automatic control mode, and control temperature scope is 80 ~ 450 DEG C; Each reactor upper, middle and lower end is established and is respectively arranged a temperature point 19, and the temperature signal of all reactors feeds back to control system.Described SCR catalytic reaction system, front thief hatch 25-1 is all set with post-sampling mouth 25-2 for being connected the flue gas sampling pipe on flue gas analyzer before and after each reactor, before flue gas analyzer can connect any one, thief hatch 25-1 and post-sampling mouth 25-2 tests, and the signal feedback of flue gas analyzer is to control system.The tail gas of described SCR catalytic reaction system enters the mixed gas after gas-gas heat exchanger 16, then enters exhaust treatment system by frequency conversion fan 26.Arrange line pressure measuring point 24 before frequency conversion fan 26, the import and export pipeline of gas-gas heat exchanger 16 is equipped with temperature point 19, and all temperature signals, frequency conversion fan 26 frequency and pressure feedback are to control system.Pressure realizes stability contorting by automatically regulating frequency conversion fan 26 frequency.
Described exhaust treatment system is made up of spray column 27, alkali lye pond 29 and feeding spraying pump 28.Spray column 27 and alkali lye pond 29, by pipeline connection, maintain liquid level consistent.The pH value in alkali lye pond 29 maintains about 10, after tail gas enters spray column 27, through alkali lye spray-absorption, discharges from top.
When described denitrating catalyst Performance Appraisal System is used for Simulation evaluation coal-burning power plant catalyst monolayers, bilayer or three layers of layout, the resistance under different flue gas condition, denitration efficiency, the escaping of ammonia rate and SO
2/ SO
3the performance index such as conversion ratio.
Evaluation method of the present invention, comprises the steps:
A. according to flue gas flow, the oxygen flow of simulation, control system is utilized to set nitrogen and air mass flow;
B. according to the flue-gas temperature of simulation, utilize control system to set the first preheating furnace 17, second preheating furnace 18, first reactor 22, second reactor 23-1, the 3rd reactor 23-2, the 4th reactor 23-3 temperature, wherein the second preheating furnace 18 temperature should set consistent with the second reactor 23-1, the 3rd reactor 23-2, the 4th reactor 23-3 temperature;
C. after the first preheating furnace 17, second preheating furnace 18, first reactor 22, second reactor 23-1, the 3rd reactor 23-2, the 4th reactor 23-3 temperature reach setting value, according to the moisture of simulation, utilize control system to set metered shot pump 12 and supply the water yield;
D. according to exhaust gas volumn and the flue gas composition of simulation, control system is utilized to set SO
2, NO, NO
2, CO
2and NH
3flow;
E. utilize control system to set pressure before frequency conversion fan 26, before realizing blower fan by automatically regulating frequency conversion fan 26 frequency, pressure stability controls;
F. flue gas analyzer is utilized to detect the first reactor 22, second reactor 23-1, the 3rd reactor 23-2, the 4th reactor 23-3 post-sampling mouth 25-2 Gas Parameters, after stable to be placed into all reactor post-sampling mouth 25-2 Gas Parameters of catalyzer, catalyst performance evaluation can be carried out;
G. by opening valve 21-1 ~ valve 21-2, valve-off 21-3 ~ valve 21-11, make the flue gas flowed out from mixing arrangement 20 by means of only the first reactor 22, flue gas analyzer is accessed thief hatch 25-1 and post-sampling mouth 25-2 before the first reactor 22 that flue gas passes through, by test SO
2, NO, NO
2, CO
2, SO
3and NH
3flue gas concentration, the ammonia nitrogen mol ratio of the first reactor 22 catalyzer, denitration efficiency, the escaping of ammonia rate, activity and SO can be obtained
2/ SO
3conversion ratio.
Reactor 22 is utilized to detect size 150 × 150 × 920mm (long × wide × high) catalyzer (the geometric proportion surface area 499.1m2/m3) performance under following operating mode:
Testing procedure is as follows:
A. catalyst sample is put into reactor 22, Open valve 21-1,21-2; Off-response device 23-1 ~ 23-3 terminal valve.
B. according to air speed and catalyst size, simulated flue gas amount is 82.8Nm
3/ h; The inlet gas component data simulated as required, nitrogen flow is adjusted to 1209g/min; Artificial atmosphere is 425g/min.
C. one-level preheating furnace temperature 250 DEG C is set, secondary preheating furnace and reactor 22 temperature 350 DEG C.After preheating furnace and temperature of reactor reach setting value, setting metered shot pump supply water yield 67g/min.
D. NO flow 370mg/min is set; SO
2flow 1577mg/min; NH
3flow 168mg/min.Pressure-100Pa before setting frequency conversion fan, realizes pressure stability before blower fan by automatically controlling frequency conversion fan frequency.
E. utilize flue gas analyzer test access Gas Parameters, concentration is as follows: NO202ppm, SO
2397ppm, O
24.98%; NH
3161ppm; SO
30ppm; After exiting flue gas parameter stability, utilize flue gas analyzer test outlet Gas Parameters as follows: NO42ppm, SO
2393ppm, O
24.98%; NH
30.51ppm; SO
33.02ppm.By above data, can obtain 350 DEG C, under ammonia nitrogen mol ratio is 0.80 condition, the denitration efficiency of catalyzer is 79.21%, and the escaping of ammonia is 0.51ppm, SO2/SO3 conversion ratio is 0.76%, and activity is 24.80.
Denitration efficiency computing formula:
The denitration efficiency of η-catalyzer, %;
C
nO-in-reactor inlet NO concentration (excess air coefficient 1.4), ppm;
C
nO-out-reactor outlet NO concentration (excess air coefficient 1.4), ppm;
Ammonia nitrogen mol ratio computing formula:
MR-ammonia nitrogen mol ratio;
-reactor inlet NH
3concentration (excess air coefficient 1.4), ppm;
SO
2/ SO
3conversion ratio computing formula:
X-SO
2/ SO
3conversion ratio;
-reactor outlet SO
3concentration (excess air coefficient 1.4), ppm;
-reactor inlet SO
3concentration (excess air coefficient 1.4), ppm;
C
sO2-in-Reactor inlet SO
2concentration (excess air coefficient 1.4), ppm;
Catalyst activity computing formula is as follows:
V-reactor inlet exhaust gas volumn, Nm
3/ h;
A
p-catalyzer geometric proportion surface area, m
2/ m
3;
V
c-catalyst volume, m
3;
Embodiment 2
Other step is identical with embodiment 1, g step can be replaced by following steps: valve-off 21-1, valve 21-2, valve 21-5 ~ valve 21-8, open valve 21-9 ~ valve 21-11, valve 21-3, valve 21-4, the flue gas that flows out from mixing arrangement 20 is made flue gas analyzer to be accessed thief hatch 25-1 and post-sampling mouth 25-2 before the second reactor 23-1, by test SO by the second reactor 23-1
2, NO, NO
2, CO
2, SO
3and NH
3flue gas concentration, the ammonia nitrogen mol ratio of the second reactor 23-1 catalyzer, denitration efficiency, the escaping of ammonia rate and SO can be obtained
2/ SO
3conversion ratio.
Embodiment 3
Other step is identical with embodiment 1, g step can be replaced by following steps: close the valve 21-1 of the first reactor, valve 21-2, valve 21-9 ~ valve 21-11, open valve 21-3 ~ valve 21-8, the flue gas flowed out from mixing arrangement 20 is made to pass through the second reactor 23-1, the 3rd reactor 23-2 and the 4th reactor 23-3 of series connection, flue gas analyzer is accessed thief hatch 25-1 and the 4th reactor 23-3 post-sampling mouth 25-2 before the second reactor 23-1, by test SO
2, NO, NO
2, CO
2, SO
3and NH
3flue gas concentration, the ammonia nitrogen mol ratio of third-order reaction system catalyst, denitration efficiency, the escaping of ammonia rate and SO can be obtained
2/ SO
3conversion ratio.
Embodiment 4
Other step is identical with embodiment 1, g step can be replaced by following steps: by valve-off 21-1,21-2, valve 21-7 ~ valve 21-10, Open valve 21-3 ~ 21-6,21-11, make the flue gas flowed out from mixing arrangement 20 by means of only the second reactor 23-1, the 3rd reactor 23-2 two reactors, flue gas analyzer is met the post-sampling mouth 25-2 of thief hatch 25-1 and the 3rd reactor 23-2 reactor before this second reactor 23-1, by test SO
2, NO, NO
2, CO
2, SO
3and NH
3flue gas concentration, the ammonia nitrogen mol ratio of two-stage reaction system catalyst, denitration efficiency, the escaping of ammonia rate and SO can be obtained
2/ SO
3conversion ratio.
Reactor 23-1,23-2 is utilized to detect size 75 × 75 × 920mm (long × wide × high) catalyzer (geometric proportion surface area 499.1m
2/ m
3) performance under following operating mode:
| Project | Unit | Numerical value |
| Air speed | h -1 | 5000 |
| Ammonia nitrogen mol ratio | \ | 0.9 |
| Entrance SO 2 | ppm | 400 |
| Entrance NO | ppm | 200 |
| Entrance water capacity | ％ | 6 |
| Entrance oxygen level | ％ | 5 |
| Temperature of reaction | ℃ | 320 |
Testing procedure is as follows:
F. catalyst sample is put into reactor 23-1,23-2, Open valve 21-3 ~ 21-6,21-11; Close other valve.
G. according to air speed and catalyst size, simulated flue gas amount is 51.75Nm
3/ h; The inlet gas component data simulated as required, nitrogen flow is adjusted to 756g/min; Artificial atmosphere is 266g/min.
H. one-level preheating furnace temperature 250 DEG C is set, secondary preheating furnace and reactor 23-1,23-2 temperature 320 DEG C.After preheating furnace and temperature of reactor reach setting value, setting metered shot pump supply water yield 42g/min.
I. NO flow 231mg/min is set; SO
2flow 986mg/min; NH
3flow 118mg/min.Pressure-100Pa before setting frequency conversion fan, realizes pressure stability before blower fan by automatically controlling frequency conversion fan frequency.
Utilize flue gas analyzer test access Gas Parameters, concentration is as follows: NO203ppm, SO
2398ppm, O
24.97%; NH
3183ppm; SO
30ppm; After question response device 23-2 exiting flue gas parameter stability, utilize flue gas analyzer test 23-2 exiting flue gas parameter as follows: NO22ppm, SO
2394ppm, O
24.97%; NH
31.64ppm; SO
32.75ppm.By above data, two-stage catalyzer 320 DEG C, under ammonia nitrogen mol ratio is 0.90 condition, the denitration efficiency of catalyzer is 89.16%, and the escaping of ammonia is 1.64ppm, SO
2/ SO
3conversion ratio is 0.69%, and activity is 34.54.Test 23-1 exiting flue gas Gas Parameters is as follows: NO38ppm, SO
2396ppm, O
24.97%; NH
317.85ppm; SO
31.41ppm.First order catalyzer 320 DEG C, under ammonia nitrogen mol ratio is 0.90 condition, the denitration efficiency of catalyzer is 81.28%, and the escaping of ammonia is 17.85ppm, SO
2/ SO
3conversion ratio is 0.35%, and activity is 40.17.
To the above-mentioned explanation of the disclosed embodiments, professional and technical personnel in the field are realized or uses the present invention.To be apparent for those skilled in the art to the multiple amendment of these embodiments, General Principle as defined herein can without departing from the spirit or scope of the present invention, realize in other embodiments.Therefore, the present invention can not be restricted to these embodiments shown in this article, but will meet the widest scope consistent with principle disclosed herein and features of novelty.
Claims (5)
1. a denitrating catalyst Performance Appraisal System, is characterized in that, comprises distribution metering system, air preheat system, SCR catalytic reaction system, gas-gas heat exchanger (16), exhaust treatment system and control system;
Described distribution metering system comprises NH
3air intake opening (1), SO
2air intake opening (2), NO air intake opening (3), the first cushion gas air intake opening (7), the second cushion gas air intake opening (8), nitrogen inlet (4), air inlet (5), water vapor air intake opening (6), evener (15) and mixing arrangement (20), described NH
3air intake opening (1) is connected with described mixing arrangement (20), described SO
2air intake opening (2), NO air intake opening (3), the first cushion gas air intake opening (7), the second cushion gas air intake opening (8), nitrogen inlet (4), air inlet (5) are connected with evener (15), and described evener (15) is connected with described gas-gas heat exchanger (16); The import and export pipeline of described gas-gas heat exchanger (16) is equipped with temperature point (19); Each gas piping is all equipped with mass-flow gas meter (13), each gas piping is arranged the pitch aperture (14) being used for adjustments of gas mass rate;
Described air preheat system comprises the first hot stove (17) and second preheating furnace (18) of two-stage series connection, and the first preheating furnace (17) and the second preheating furnace (18) are vertical; Described first preheating furnace (17) is connected with described gas-gas heat exchanger (16), and described second preheating furnace (18) is connected with described mixing arrangement (20);
Described SCR catalytic reaction system is the reactor of two-way in parallel, and a road is single first reactor (22) of the catalyst performance for checking section 150 × 150mm; Another road is 3 tandem reactors of the catalyst performance for checking 75 × 75mm, is respectively the second reactor (23-1), the 3rd reactor (23-2), the 4th reactor (23-3); The free length of the first reactor (22), the second reactor (23-1), the 3rd reactor (23-2), the 4th reactor (23-3) each reactor installation catalyzer is not less than 1500mm; First reactor (22), the second reactor (23-1), the 3rd reactor (23-2), the 4th reactor (23-3) import and export place are equipped with pressure-measuring-point (24) and temperature point (19), and pressure-measuring-point (24) and its reactor end, place distance are not less than place reactor 2 times of equivalent diameters; All arrange front thief hatch (25-1) and post-sampling mouth (25-2) before and after first reactor (22), the second reactor (23-1), the 3rd reactor (23-2), the 4th reactor (23-3), described front thief hatch (25-1) and post-sampling mouth (25-2) are for being connected the flue gas sampling pipe on flue gas analyzer;
Described exhaust treatment system comprises spray column (27), alkali lye pond (29) and feeding spraying pump (28), and described spray column (27) and alkali lye pond (29) are by pipeline connection, and feeding spraying pump (28) is connected with spray column (27); Described spray column (27) is connected with gas-gas heat exchanger (16), is provided with frequency conversion fan (26) between described spray column (27) and gas-gas heat exchanger (16), and described frequency conversion fan (26) is front arranges line pressure measuring point (24) and temperature point (19);
The pressure signal that the temperature signal that the mass flow rate signal that described mass-flow gas meter (13) records, temperature point (19) record, pressure-measuring-point (24) record, frequency conversion fan (26) are connected with control system.
2. denitrating catalyst Performance Appraisal System according to claim 1, is characterized in that, described NH
3air intake opening (1), SO
2air intake opening (2), NO air intake opening (3), the first cushion gas air intake opening (7), the second cushion gas air intake opening (8) and be equipped with corresponding gas steel cylinder (11) be connected, described nitrogen inlet (4) is connected with nitrogen preparation facilities (9), described air inlet (5) is connected with air compressor machine (10), and described water vapor air intake opening (6) is connected with syringe pump (12).
3. carry out denitrating catalyst method of evaluating performance with denitrating catalyst Performance Appraisal System according to claim 2, it is characterized in that, comprise the steps:
A. according to flue gas flow, the oxygen flow of simulation, control system is utilized to set nitrogen and air mass flow;
B. according to the flue-gas temperature of simulation, utilize control system to set the first preheating furnace (17), the second preheating furnace (18), the first reactor (22), the second reactor (23-1), the 3rd reactor (23-2), the 4th reactor (23-3) temperature, wherein the second preheating furnace (18) temperature should set consistent with the second reactor (23-1), the 3rd reactor (23-2), the 4th reactor (23-3) temperature;
C. after the first preheating furnace (17), the second preheating furnace (18), the first reactor (22), the second reactor (23-1), the 3rd reactor (23-2), the 4th reactor (23-3) temperature reach setting value, according to the moisture of simulation, control system is utilized to set metered shot pump (12) the supply water yield;
D. according to exhaust gas volumn and the flue gas composition of simulation, control system is utilized to set SO
2, NO, NO
2, CO
2and NH
3flow;
E. utilize control system to set frequency conversion fan (26) front pressure, before realizing blower fan by automatically regulating frequency conversion fan (26) frequency, pressure stability controls;
F. flue gas analyzer is utilized to detect the first reactor (22), the second reactor (23-1), the 3rd reactor (23-2), the 4th reactor (23-3) post-sampling mouth (25-2) Gas Parameters, after stable to be placed into all reactor post-sampling mouth (25-2) Gas Parameters of catalyzer, catalyst performance evaluation can be carried out;
G. by control valve (21-1) ~ valve (21-11), make the flue gas flowed out from mixing arrangement (20) by means of only a reactor the first reactor (22), the second reactor (23-1), the 3rd reactor (23-2), the 4th reactor (23-3), flue gas analyzer is accessed thief hatch (25-1) and post-sampling mouth (25-2) before the reactor that flue gas passes through, by test SO
2, NO, NO
2, CO
2, SO
3and NH
3flue gas concentration, the ammonia nitrogen mol ratio of any one reactor catalyst in the first reactor (22), the second reactor (23-1), the 3rd reactor (23-2), the 4th reactor (23-3), denitration efficiency, the escaping of ammonia rate, activity and SO can be obtained
2/ SO
3conversion ratio.
4. denitrating catalyst method of evaluating performance according to claim 3, it is characterized in that, g step can be replaced by following steps: early gate (21-1) and the late gate (21-2) of closing the first reactor, make second reactor (23-1), three reactor (23-2) and four reactor (23-3) of flue gas by connecting that flow out from mixing arrangement (20), flue gas analyzer is accessed the second reactor (23-1) front thief hatch (25-1) and the 4th reactor (23-3) post-sampling mouth (25-2), by test SO
2, NO, NO
2, CO
2, SO
3and NH
3flue gas concentration, the ammonia nitrogen mol ratio of third-order reaction system catalyst, denitration efficiency, the escaping of ammonia rate and SO can be obtained
2/ SO
3conversion ratio.
5. denitrating catalyst method of evaluating performance according to claim 3, it is characterized in that, g step can be replaced by following steps: by control valve (21-1) ~ valve (21-11), make the flue gas flowed out from mixing arrangement (20) by means of only any two reactors the second reactor (23-1), the 3rd reactor (23-2), the 4th reactor (23-3), flue gas analyzer is connect the post-sampling mouth (25-2) of first front thief hatch of reactor (25-1) and a rear reactor in these two reactors, by test SO
2, NO, NO
2, CO
2, SO
3and NH
3flue gas concentration, the ammonia nitrogen mol ratio of two-stage reaction system catalyst, denitration efficiency, the escaping of ammonia rate and SO can be obtained
2/ SO
3conversion ratio.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201510943042.3A CN105510532A (en) | 2015-12-16 | 2015-12-16 | Denitration catalytic performance evaluation system and method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201510943042.3A CN105510532A (en) | 2015-12-16 | 2015-12-16 | Denitration catalytic performance evaluation system and method |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN105510532A true CN105510532A (en) | 2016-04-20 |
Family
ID=55718660
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201510943042.3A Pending CN105510532A (en) | 2015-12-16 | 2015-12-16 | Denitration catalytic performance evaluation system and method |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN105510532A (en) |
Cited By (11)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105866322A (en) * | 2016-05-03 | 2016-08-17 | 浙江三龙催化剂有限公司 | Mobile flue gas denitrification catalyst performance testing device |
| CN106248865A (en) * | 2016-09-12 | 2016-12-21 | 南京电力设备质量性能检验中心 | A kind of full-scale catalyst for denitrating flue gas operational characteristic experimental provision |
| CN106404984A (en) * | 2016-08-27 | 2017-02-15 | 华电电力科学研究院 | Equal-length middle-sized flue gas denitrification catalyst performance detection device and detection method |
| CN106932526A (en) * | 2017-04-12 | 2017-07-07 | 华能国际电力股份有限公司 | One kind is used for denitrating catalyst cryogenic property characterization processes and device |
| CN107202857A (en) * | 2017-04-28 | 2017-09-26 | 国网天津市电力公司 | A kind of laboratory's denitrating catalyst denitration efficiency computational methods |
| CN109387606A (en) * | 2018-11-27 | 2019-02-26 | 清华大学盐城环境工程技术研发中心 | A kind of SCR denitration full-scale performance evaluation system |
| CN109682923A (en) * | 2018-12-17 | 2019-04-26 | 中国科学院过程工程研究所 | A kind of full-scale SCR denitration evaluation system and method |
| CN111579708A (en) * | 2020-05-19 | 2020-08-25 | 福州大学 | Device and method for evaluating activity of desulfurization catalyst |
| CN113533023A (en) * | 2021-07-14 | 2021-10-22 | 华电电力科学研究院有限公司 | Flow-adjustable denitration catalyst abrasion strength testing device and testing method |
| WO2023015888A1 (en) * | 2021-08-13 | 2023-02-16 | 交通运输部天津水运工程科学研究所 | Scr catalyst performance evaluation system for marine engine |
| CN115754146A (en) * | 2022-11-17 | 2023-03-07 | 南方电网电力科技股份有限公司 | Evaluation test bench of active carbon adsorption degradation |
Citations (17)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH11183462A (en) * | 1997-12-22 | 1999-07-09 | Tokyo Gas Co Ltd | Method and apparatus for measuring catalyst activity |
| US20050255605A1 (en) * | 2004-05-14 | 2005-11-17 | Fossil Energy Research Corp. | In-line localized monitoring of catalyst activity in selective catalytic NOx reduction systems |
| CN101274252A (en) * | 2006-12-29 | 2008-10-01 | 亚申科技研发中心（上海）有限公司 | Catalytic process exploitation apparatus and method |
| CN101327417A (en) * | 2008-03-20 | 2008-12-24 | 武汉理工大学 | Reaction system for quickly evaluating Claus unit tail gas hydrodesulphurization catalyst |
| CN201841007U (en) * | 2010-11-01 | 2011-05-25 | 内江天科化工有限责任公司 | Reaction device for preparing cyclohexane by using pure benzene through solid-phase catalytic hydrogenation |
| CN102103047A (en) * | 2009-12-21 | 2011-06-22 | 中国科学院城市环境研究所 | Method and device for detecting fume denitration catalyst activity |
| CN202383117U (en) * | 2011-12-07 | 2012-08-15 | 广东电网公司电力科学研究院 | Device for evaluating activity of SCR (Selective Catalytic Reduction) denitration catalyst in coal-fired power plant |
| CN202453333U (en) * | 2011-12-01 | 2012-09-26 | 广州市威格林环保科技有限公司 | Multi-channel device for evaluating catalysts |
| CN202533420U (en) * | 2012-02-28 | 2012-11-14 | 广东电网公司电力科学研究院 | Evaluation system for testing performance of selective catalytic reduction (SCR) denitration catalyst |
| CN103182312A (en) * | 2011-12-31 | 2013-07-03 | 上海钒铖环保科技有限公司 | Low temperature NH3-SCR denitration catalyst for flue gas with low water vapor content, and preparation method thereof |
| CN203405452U (en) * | 2013-07-31 | 2014-01-22 | 广东电网公司电力科学研究院 | Catalyst activity detecting device of SCR (Selective Catalytic Reduction) de-nitration system |
| CN103638991A (en) * | 2013-11-18 | 2014-03-19 | 广东电网公司电力科学研究院 | Composite apparatus for generating SCR denitrification catalyst and testing activity of catalyst before and after regeneration |
| CN104062393A (en) * | 2014-07-04 | 2014-09-24 | 江苏龙源催化剂有限公司 | Mini-type test evaluation device for integral SCR denitration catalyst reaction performance test and application method thereof |
| CN203941143U (en) * | 2014-07-04 | 2014-11-12 | 江苏龙源催化剂有限公司 | A kind of miniature test evaluation device for whole SCR denitrating catalyst reactivity worth test |
| CN204008584U (en) * | 2014-05-30 | 2014-12-10 | 北京市劳动保护科学研究所 | Denitrating catalyst demercuration performance testing device |
| CN204648286U (en) * | 2015-03-27 | 2015-09-16 | 天津市澍丰农业科技有限公司 | A kind of steam generator system of high-efficiency environment friendly energy-conservation |
| CN104965050A (en) * | 2015-06-25 | 2015-10-07 | 苏州西热节能环保技术有限公司 | Full-size flue gas denitrification catalytic performance detecting device and method |
-
2015
- 2015-12-16 CN CN201510943042.3A patent/CN105510532A/en active Pending
Patent Citations (17)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH11183462A (en) * | 1997-12-22 | 1999-07-09 | Tokyo Gas Co Ltd | Method and apparatus for measuring catalyst activity |
| US20050255605A1 (en) * | 2004-05-14 | 2005-11-17 | Fossil Energy Research Corp. | In-line localized monitoring of catalyst activity in selective catalytic NOx reduction systems |
| CN101274252A (en) * | 2006-12-29 | 2008-10-01 | 亚申科技研发中心（上海）有限公司 | Catalytic process exploitation apparatus and method |
| CN101327417A (en) * | 2008-03-20 | 2008-12-24 | 武汉理工大学 | Reaction system for quickly evaluating Claus unit tail gas hydrodesulphurization catalyst |
| CN102103047A (en) * | 2009-12-21 | 2011-06-22 | 中国科学院城市环境研究所 | Method and device for detecting fume denitration catalyst activity |
| CN201841007U (en) * | 2010-11-01 | 2011-05-25 | 内江天科化工有限责任公司 | Reaction device for preparing cyclohexane by using pure benzene through solid-phase catalytic hydrogenation |
| CN202453333U (en) * | 2011-12-01 | 2012-09-26 | 广州市威格林环保科技有限公司 | Multi-channel device for evaluating catalysts |
| CN202383117U (en) * | 2011-12-07 | 2012-08-15 | 广东电网公司电力科学研究院 | Device for evaluating activity of SCR (Selective Catalytic Reduction) denitration catalyst in coal-fired power plant |
| CN103182312A (en) * | 2011-12-31 | 2013-07-03 | 上海钒铖环保科技有限公司 | Low temperature NH3-SCR denitration catalyst for flue gas with low water vapor content, and preparation method thereof |
| CN202533420U (en) * | 2012-02-28 | 2012-11-14 | 广东电网公司电力科学研究院 | Evaluation system for testing performance of selective catalytic reduction (SCR) denitration catalyst |
| CN203405452U (en) * | 2013-07-31 | 2014-01-22 | 广东电网公司电力科学研究院 | Catalyst activity detecting device of SCR (Selective Catalytic Reduction) de-nitration system |
| CN103638991A (en) * | 2013-11-18 | 2014-03-19 | 广东电网公司电力科学研究院 | Composite apparatus for generating SCR denitrification catalyst and testing activity of catalyst before and after regeneration |
| CN204008584U (en) * | 2014-05-30 | 2014-12-10 | 北京市劳动保护科学研究所 | Denitrating catalyst demercuration performance testing device |
| CN104062393A (en) * | 2014-07-04 | 2014-09-24 | 江苏龙源催化剂有限公司 | Mini-type test evaluation device for integral SCR denitration catalyst reaction performance test and application method thereof |
| CN203941143U (en) * | 2014-07-04 | 2014-11-12 | 江苏龙源催化剂有限公司 | A kind of miniature test evaluation device for whole SCR denitrating catalyst reactivity worth test |
| CN204648286U (en) * | 2015-03-27 | 2015-09-16 | 天津市澍丰农业科技有限公司 | A kind of steam generator system of high-efficiency environment friendly energy-conservation |
| CN104965050A (en) * | 2015-06-25 | 2015-10-07 | 苏州西热节能环保技术有限公司 | Full-size flue gas denitrification catalytic performance detecting device and method |
Cited By (15)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105866322A (en) * | 2016-05-03 | 2016-08-17 | 浙江三龙催化剂有限公司 | Mobile flue gas denitrification catalyst performance testing device |
| CN106404984A (en) * | 2016-08-27 | 2017-02-15 | 华电电力科学研究院 | Equal-length middle-sized flue gas denitrification catalyst performance detection device and detection method |
| CN106404984B (en) * | 2016-08-27 | 2018-09-11 | 华电电力科学研究院 | The isometric medium-sized catalyst for denitrating flue gas device for detecting performance of one kind and detection method |
| CN106248865A (en) * | 2016-09-12 | 2016-12-21 | 南京电力设备质量性能检验中心 | A kind of full-scale catalyst for denitrating flue gas operational characteristic experimental provision |
| CN106932526A (en) * | 2017-04-12 | 2017-07-07 | 华能国际电力股份有限公司 | One kind is used for denitrating catalyst cryogenic property characterization processes and device |
| CN107202857A (en) * | 2017-04-28 | 2017-09-26 | 国网天津市电力公司 | A kind of laboratory's denitrating catalyst denitration efficiency computational methods |
| CN109387606A (en) * | 2018-11-27 | 2019-02-26 | 清华大学盐城环境工程技术研发中心 | A kind of SCR denitration full-scale performance evaluation system |
| CN109682923A (en) * | 2018-12-17 | 2019-04-26 | 中国科学院过程工程研究所 | A kind of full-scale SCR denitration evaluation system and method |
| CN109682923B (en) * | 2018-12-17 | 2021-03-12 | 中国科学院过程工程研究所 | Full-size SCR denitration catalyst evaluation system and method |
| CN111579708A (en) * | 2020-05-19 | 2020-08-25 | 福州大学 | Device and method for evaluating activity of desulfurization catalyst |
| CN111579708B (en) * | 2020-05-19 | 2021-12-24 | 福州大学 | Device and method for evaluating activity of desulfurization catalyst |
| CN113533023A (en) * | 2021-07-14 | 2021-10-22 | 华电电力科学研究院有限公司 | Flow-adjustable denitration catalyst abrasion strength testing device and testing method |
| CN113533023B (en) * | 2021-07-14 | 2023-06-27 | 华电电力科学研究院有限公司 | Flow-adjustable denitration catalyst abrasion strength testing device and testing method |
| WO2023015888A1 (en) * | 2021-08-13 | 2023-02-16 | 交通运输部天津水运工程科学研究所 | Scr catalyst performance evaluation system for marine engine |
| CN115754146A (en) * | 2022-11-17 | 2023-03-07 | 南方电网电力科技股份有限公司 | Evaluation test bench of active carbon adsorption degradation |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN105510532A (en) | Denitration catalytic performance evaluation system and method | |
| CN104722203B (en) | A kind of SCR denitration control system of flue gas of heating furnace and method | |
| CN105043967B (en) | Flue gas-coal ash collaboration corrosion testing apparatus | |
| CN104965050A (en) | Full-size flue gas denitrification catalytic performance detecting device and method | |
| CN204044136U (en) | A kind of experimental provision evaluated for SCR denitrating flue gas honeybee shape catalyst activity | |
| CN203479784U (en) | Catalyst activity detection experimental device of SCR (selective catalytic reduction) denitration system | |
| CN104965021A (en) | Performance evaluation device and performance evaluation method of coal-fired flue gas denitration catalyst | |
| CN106404984B (en) | The isometric medium-sized catalyst for denitrating flue gas device for detecting performance of one kind and detection method | |
| CN105572291A (en) | Catalyst activity detection method for boiler denitrification system | |
| CN106984187A (en) | A kind of long lab scale catalyst for denitrating flue gas device for detecting performance and detection method | |
| CN203405452U (en) | Catalyst activity detecting device of SCR (Selective Catalytic Reduction) de-nitration system | |
| CN111398512A (en) | Catalyst performance detection system and detection method based on-site flue gas denitration device | |
| CN103529161A (en) | Detection device and method for activity of catalyst of selective catalytic reduction method denitration system | |
| CN106295166A (en) | A kind of SCR denitration device amount of ammonia slip measuring method and application thereof | |
| CN215610573U (en) | Flue gas denitration subregion spouts ammonia system based on pyrolysis is directly spouted to urea | |
| CN210090396U (en) | SCR denitration catalyst performance detection device | |
| CN109932472A (en) | A kind of SCR denitration device for detecting performance and detection method | |
| CN109387606A (en) | A kind of SCR denitration full-scale performance evaluation system | |
| CN219646952U (en) | Adiabatic cyclone dust collector and flue gas treatment facility | |
| CN203705415U (en) | Evaluation device for denitration catalyst | |
| CN107402278B (en) | Performance pilot-scale device of SCR denitration catalyst | |
| CN208588711U (en) | SCR denitration demercuration integration catalyst integrated experiment device | |
| CN204855328U (en) | Flue gas - coal ash is corrosion test device in coordination | |
| CN209490673U (en) | A kind of sintering device flue gas denitrating system | |
| CN207689445U (en) | A kind of SCR denitration full-scale performance detection evaluating apparatus |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| RJ01 | Rejection of invention patent application after publication | ||
| RJ01 | Rejection of invention patent application after publication |
Application publication date: 20160420 |