CN214345522U

CN214345522U - Simulation and monitoring full-process control flue gas SO3System for controlling a power supply

Info

Publication number: CN214345522U
Application number: CN202022795650.3U
Authority: CN
Inventors: 方攀; 朱翔; 肖婷婷; 谭华玲; 武丹玲; 管肖肖; 熊遥
Original assignee: Wuhan Longking Co ltd
Current assignee: Wuhan Longking Co ltd
Priority date: 2020-11-27
Filing date: 2020-11-27
Publication date: 2021-10-08
Anticipated expiration: 2030-11-27

Abstract

The utility model discloses a collect emulation, monitor full flow control flue gas SO3 system. It comprises an absorbent preparation distribution control system, an absorbent injection section flue effect-extracting device and flue gas SO₃A concentration sampling monitoring system; the absorbent preparation distribution control system is respectively connected with the absorbent injection system and the absorption tower; the absorbent injection system is respectively connected with the absorbent injection section flue effect-raising device and the absorption tower; boiler respectively carries effect device and flue gas SO with absorbent injection section flue₃The concentration sampling monitoring system is connected; flue gas outlet and flue gas SO of absorption tower₃And the concentration sampling monitoring system is connected. The utility model effectively relieves or avoids the problems of catalyst failure, ash deposition, blockage, corrosion and the like of system-associated equipment; has the function of increasing SO₃The removal efficiency is reduced, the consumption of the absorbent is reduced, and the operation cost is reduced.

Description

Simulation and monitoring full-process control flue gas SO3System for controlling a power supply

Technical Field

The utility model relates to a flue gas purification technical field particularly, relates to a collection emulation, monitoring full flow control flue gas SO3 system.

Background

In China, the power source is mainly coal-fired power generation in a certain period of the future. It is known that flue gas generated by coal combustion contains a large amount of gaseous pollutants (NO)_x、SO_xEtc.), which can cause serious harm to the atmospheric environment and human health. With the execution of ultra-low emission standards by the state, the emission of main pollutants is effectively controlled at present, SO that the original low content of SO is caused₃The gas emission specific gravity is in an upward trend.

SO in coal-fired flue gas₃In the discharging process, a series of problems of low-temperature corrosion of a power plant flue and equipment, failure of a catalyst in an SCR (selective catalytic reduction) reactor, blockage of an air preheater, blue smoke plume and the like can be caused; SO discharged into the atmosphere₃Acid rain, etc. may be caused. Thus, for flue gas SO₃The emission control of (2) is imperative.

The existing SO3 removal method mainly comprises the following steps:low-sulfur coal and mixed coal are used for combustion; using low SO₃A conversion SCR catalyst; wet desulphurization; a wet electrostatic precipitator; SO absorption by spray absorbent₃Techniques, and the like. However, when one technique is used alone, the following contradictions exist: the use of low sulfur coal increases the operating costs of the power plant; the cost is high by adopting a catalyst with low conversion rate; wet desulfurization tower pair SO₃Low removal efficiency and difficult removal of SO₃Aerosol; wet-type electric precipitation pair SO₃The removal rate is high, but the problem of dust accumulation, blockage and corrosion of the air preheater can not be solved because the air preheater is generally arranged at the tail end of the flue gas purification device; if the technique of spraying the absorbent adopts alkaline dry powder, SO can be effectively removed₃But the needed absorbent dosage is large and the cost is high; if the calcium-based absorbent is adopted, the specific resistance of fly ash is increased, the load of an electric dust collector is increased, and if the calcium-based absorbent is sprayed after an air preheater, SO cannot be avoided₃Low-temperature corrosion influence is caused to the air preheater.

Thus, for realizing flue gas SO₃The method has the advantages of high removal efficiency, low cost and low damage to associated equipment, and the current perfect technical scheme is lacked.

Disclosure of Invention

The utility model aims at providing a collect emulation, monitor full flow control flue gas SO₃System for raising SO₃The method has the advantages of reducing absorbent consumption, reducing operation cost, effectively relieving or avoiding the problems of catalyst failure, ash deposition, blockage, corrosion and the like of system associated equipment while achieving removal efficiency.

In order to realize the purpose, the technical scheme of the utility model is that: simulation and monitoring full-process control flue gas SO₃A system, characterized by: comprises an absorbent preparation distribution control system, an absorbent injection section flue effect-extracting device and flue gas SO₃A concentration sampling monitoring system;

the absorbent preparation distribution control system is respectively connected with the absorbent injection system and the absorption tower;

the absorbent injection system is respectively connected with the absorbent injection section flue effect-raising device and the absorption tower;

boiler efficiency improving device and method with absorbent injection section flue respectivelyFlue gas SO₃The concentration sampling monitoring system is connected;

flue gas outlet and flue gas SO of absorption tower₃And the concentration sampling monitoring system is connected.

In the technical scheme, a flue gas inlet is formed in the side wall of the absorption tower;

the interior of the absorption tower is provided with a gas uniform distributor and NaHSO from bottom to top₃A spray layer and a demister; the gas uniform distributor is arranged above the flue gas inlet;

an outlet flue is arranged at the upper end of the absorption tower, and an inlet flue is arranged at the side of the lower part of the absorption tower;

wherein, the outlet flue and SO₃The concentration sampling monitoring system is connected;

one end of the inlet flue is connected with the economizer, and the other end of the inlet flue is connected with the flue gas inlet;

the inlet flue is sequentially provided with an SCR catalytic reactor, an air preheater and a dust remover, wherein the SCR catalytic reactor is positioned at the outlet end of the economizer, and the dust remover is positioned at the inlet end of the flue gas inlet.

In the technical scheme, the absorbent injection section flue effect lifting device is arranged in the inlet flue and behind the injection point of the nozzle;

the flue effect-improving device of the absorbent injection section comprises an annular inclined baffle plate, a grid and a support on the inner wall of the flue gas pipeline;

the annular inclined baffle plate on the inner wall of the flue gas pipeline is arranged on the inner wall of the inlet flue;

the support is arranged on the inner wall of the annular inclined baffle plate on the inner wall of the flue gas pipeline; the supports are uniformly arranged along the inner wall of the inlet flue; 4-6 supports are arranged;

the grating is respectively connected with the annular inclined baffle and the support.

In the above technical solution, the absorbent injection system comprises NaHSO₃Solution delivery pumps and nozzles;

the compressed air buffer tank is connected with the nozzle;

the number of the nozzles is multiple; the plurality of nozzles are respectively arranged on the front side and the rear side of the SCR catalytic reactor.

In the above technical solution, the nozzle is a two-fluid nozzle.

In the above technical scheme, the absorbent preparation distribution control system comprises NaHSO₃Solution storage tank, NaHSO₃The device comprises a delivery pump, a valve group control unit and a metering unit;

NaHSO₃solution storage tank and NaHSO₃The delivery pump, the valve group control unit and the metering unit are sequentially connected; wherein, NaHSO₃Solution storage tank and NaHSO₃The preparation system is connected with the metering unit and the nozzle and the NaHSO respectively₃The spraying layers are connected.

In the above technical scheme, the flue gas SO₃The concentration sampling monitoring system is respectively connected between the economizer and the SCR catalytic reactor, on an inlet flue between the air preheater and the dust remover and on an outlet flue of the absorption tower;

valve bank control unit and flue gas SO₃The concentration sampling monitoring system is connected;

in the above technical scheme, the flue gas SO₃The concentration sampling monitoring system comprises an SO₃Analyzer and Signal processing System, SO₃The analyzer is connected with the signal processing system.

The utility model has the advantages of as follows:

(1) the utility model adopts NaHSO₃The solution, atomizing the alkali liquor into mist-like droplets with fine particle size through a nozzle, has the following advantages: i, due to NaHSO₃Strong alkalinity of solution, and SO₃The reaction rate is high, and the reaction does not react with SO₂Reaction of the gas with SO₃Has stronger pertinence to ensure high SO₃Removal rate, low NaHSO₃Consumption of the solution; the utility model adopts NaHSO₃The solution is atomized into fog-like liquid drops with fine particle size by a nozzle, so that less fly ash is generated, and the influence on the subsequent dust removal efficiency is further avoided; II, compared with the dry method absorbent spraying adopted by other processes, the utility model discloses a slight NaHSO that the nozzle produced₃In the drying process of the liquid drop, ions in the liquid drop are diffused quickly, the mass transfer efficiency is far higher than that of the gas-solid absorption process of the dry method, absorbent powder obtained by drying the liquid drop has larger specific surface area than that of the powder obtained by grinding the dry powder, and SO is further improved₃The absorption efficiency of (a);

(2) the utility model discloses add baffle grid integral structure's advantage as follows in spraying some back flues: i, the wall attachment phenomenon of the flue gas near the inner wall of the flue due to the influence of self inertia force and viscous force, if NaHSO₃The alkali liquor injection can not completely cover the cross section of the flue, SO that SO in the flue gas attached to the wall can be caused₃Escape, the baffle structure is helpful to guide the wall-attached flue gas to the middle area of the flue so that the flue gas is positioned in the NaHSO₃The effective coverage area of alkali liquor spraying is beneficial to SO₃Removing; II, in special cases, if NaHSO₃The alkali liquor is sprayed too much, the effective coverage area is far larger than the cross section of the flue, and part of NaHSO₃Alkali liquor can be collected on the inner wall of the flue, scaling of the inner wall is easily caused, and the baffle structure is beneficial to the surplus NaHSO₃Dropping and evaporating unreacted NaHSO₃The powder, product particles generated by the reaction and the like are blown to the middle area of the flue again under the driving action of the flue gas; III, SO in flue gas₃The distribution is not uniform, plus spraying NaHSO₃The disturbance of alkali liquor to the flow field causes the SO in the NaHSO3 fog drops and the flue gas₃Uneven mixing of the components causes SO₃The removal efficiency is reduced, and the grid structure is additionally arranged, so that the NaHSO can be effectively enhanced₃Fog drops and SO₃Mixing to uniform degree, increasing SO₃The removal efficiency; IV, the baffle and the grid are integrally designed, so that the installation space is saved, and the installation and construction are facilitated;

(3) the utility model discloses a CFD simulation technique carries out the advantage that designs to baffle grid integral structure as follows: i, can be according to flue gas parameter, NaHSO of mounted position department₃Carrying out personalized design on specific conditions such as injection parameters and the like; II, continuously adjusting and optimizing according to a simulation result, finally determining a structural form with a uniform flow field and small pressure loss, and effectively shortening the design period and reducing the design cost by utilizing the CFD simulation auxiliary baffle plate and grid integrated structural design; III, CFD simulation can also be performed on NaHSO₃SO in flue gas before and after injection₃The concentration is calculated, and the simulation calculation result can be compared with SO on the one hand₃The measurement results of the analyzer are compared, and on the other hand, the comparison can be achieved according to the requirements after each injection point is removedTo SO₃Concentration, reverse calculation of NaHSO₃The injection quantity is used as a basis for selecting engineering design parameters;

(4) the utility model discloses set up a plurality of SO₃Detection point, multiple NaHSO₃The purpose of the solution injection point is to monitor the SO according to each section₃Concentration, targeted adjustment of the amount of NaHSO3 solution at each injection point, on the one hand, ensuring SO₃On the other hand, the influence of excessive fly ash on subsequent denitration, dust removal and other efficiency is avoided, and finally higher SO can be achieved₃Removal rate, low NaHSO₃Solution consumption;

(5) the utility model discloses can reduce 90 ~ 95% SO₃Can greatly reduce NaHSO₃The solution consumption is reduced, and meanwhile, the corrosion of relevant equipment and a flue behind an injection point to sulfuric acid is effectively avoided; solves the problem of the existing flue gas SO₃In the removal technology, the problems of high operation cost, low removal efficiency, failure of SCR catalyst, blockage and corrosion of system-associated equipment and the like exist.

Drawings

Fig. 1 is a schematic structural diagram of the present invention.

Fig. 2 is an enlarged view of fig. 1 at a.

Fig. 3 is a schematic view of a three-dimensional structure of the flue effect-improving device of the absorbent injection section of the present invention.

FIG. 1-absorbent preparation distribution control System, 1-NaHSO₃Solution storage tank, 1, 2-NaHSO₃A delivery pump, 1.3-a valve group control unit, 1.4-a metering unit, 2-an absorbent injection system, 2.1-a nozzle, 3-an absorbent injection section flue effect-improving device, 3.1-a flue gas pipeline inner wall annular inclined baffle, 3.2-a grid, 3.3-a support and 4-flue gas SO₃A concentration sampling monitoring system, 5-an absorption tower, 5.1-a flue gas inlet, 5.2-a gas uniform distributor and 5.3-NaHSO₃Spraying layer, 5.4-demister, 5.5-outlet flue, 5.6-inlet flue, 6-compressed air buffer tank, 7-boiler, 8-economizer and 9-NaHSO₃The preparation system comprises a 10-SCR catalytic reactor, an 11-air preheater and a 12-dust remover.

Detailed Description

The following detailed description of the embodiments of the present invention will be made with reference to the accompanying drawings, which are not intended to limit the present invention, but are merely exemplary. While the advantages of the invention will be clear and readily appreciated by the description.

The utility model provides a pass through emulation optimization reaction flow field in the design phase, implement SO in stronger multiple spot monitoring of pertinence, hierarchical desorption flue gas according to monitoring signal in the operation phase₃Can ensure high SO₃And the alkali liquor consumption is reduced while the removal is carried out, and the low-cost operation is realized.

With reference to the accompanying drawings: simulation and monitoring full-process control flue gas SO₃The system comprises an absorbent preparation distribution control system 1, an absorbent injection system 2, an absorbent injection section flue effect-improving device 3 and flue gas SO₃A concentration sampling monitoring system 4;

the absorbent preparation distribution control system 1 is respectively connected with the absorbent injection system 2 and the absorption tower 5;

the absorbent injection system 2 is respectively connected with the absorbent injection section flue effect-raising device 3 and the absorption tower 5;

the boiler 7 respectively carries the effect device 3 and the flue gas SO with the flue of the absorbent injection section₃The concentration sampling monitoring system 4 is connected;

flue gas outlet and flue gas SO of absorption tower 5₃The concentration sampling monitoring system 4 is connected; the SO3 removal efficiency is improved, and meanwhile, the absorbent consumption and the operation cost are reduced.

Further, a flue gas inlet 5.1 is arranged on the side wall of the absorption tower 5;

the interior of the absorption tower 5 is provided with a gas uniform distributor 5.2 and NaHSO from bottom to top₃A spray layer 5.3 and a demister 5.4; the gas uniform distributor 5.2 is arranged above the flue gas inlet 5.1;

an outlet flue 5.5 is arranged at the upper end of the absorption tower 5, and an inlet flue 5.6 is arranged at the side of the lower part of the absorption tower;

wherein, the outlet flue 5.5 and SO₃The concentration sampling monitoring system 4 is connected;

one end of the inlet flue 5.6 is connected with the coal economizer 8, and the other end is connected with the flue gas inlet 5.1;

the inlet flue 5.6 is sequentially provided with an SCR catalytic reactor 10, an air preheater 11 and a dust remover 12, wherein the SCR catalytic reactor 10 is positioned at the outlet end of the economizer 8, and the dust remover 12 is positioned at the inlet end of the flue gas inlet 5.1; to be deprived of SO₃The flue gas enters a cylinder body of an absorption tower 5 from a flue gas inlet 5.1; the gas uniform distributor 5.2 is used for uniformly dispersing gas; NaHSO3 spray layer 5.3 for spraying NaHSO₃Solution, removal of SO₃(ii) a The demister 5.4 is used for removing mist in the gas; removal of SO₃The clean flue gas is discharged through an outlet flue 5.5.

Further, the absorbent injection section flue effect lifting device 3 is arranged on the inlet flue 5.6 behind the two absorbent injection points;

the flue effect-improving device 3 of the absorbent injection section comprises an annular inclined baffle 3.1 on the inner wall of the flue gas pipeline, a grid 3.2 and a support 3.3;

the inner wall of the flue gas pipeline is provided with an annular inclined baffle 3.1 on the inner wall of the inlet flue 5.6; the support 3.3 is arranged on the annular inclined baffle 3.1 on the inner wall of the flue gas pipeline and the inner wall of the flue gas pipeline; the supports 3.3 are uniformly arranged along the flue in an annular shape, 4-6 supports are preferably arranged on the supports 3.3, and the number of the supports 3.3 is adjusted according to the size of the flue; the grating 3.2 is integrated with the annular inclined baffle 3.1 and the support 3.3; NaHSO for avoiding spraying flue gas₃The solution generates a wall attachment phenomenon on the inner wall of the flue, and an annular inclined baffle structure is additionally arranged behind the injection points of the first path and the second path; NaHSO for enhanced jetting₃The mixing uniformity of the solution and the flue gas promotes mass transfer reaction, thereby improving SO₃The grid structure is additionally arranged in the flue behind the annular inclined baffle;

considering the spatial property and the convenient installation, the annular inclined baffle plate and the grid structure are combined into a whole and fixedly installed with the flue by the support; the structures of the annular inclined baffle and the grating are designed by adopting CFD (Computational Fluid Dynamics) simulation, so that the uniform flow field and small pressure drop are ensured;

the SCR catalytic reactor 10 is sequentially connected with an air preheater 11 and a dust remover 12; wherein, the SCR catalytic reactor 10 is connected with the coal economizer 8, and the dust remover 12 is connected with the flue gas inlet 5.1; the air preheater 11 is used for heating the gas entering the absorption tower 5; the dust collector 12 is used to remove impurities such as dust from the gas entering the absorption tower 5.

Further, the absorbent injection system 2 includes NaHSO₃A solution delivery pump 1.2 and a nozzle 2.1;

the compressed air buffer tank 6 is connected with the nozzle 2.1; the nozzle 2.1 is connected with an inlet flue 5.6;

two nozzles 2.1 are provided; the two nozzles 2.1 are connected in parallel and are respectively arranged in front of the SCR catalytic reactor 10 and the air preheater 11; NaHSO₃Passing the solution through NaHSO₃The delivery pump 1.2 delivers to the nozzle 2.1, and the nozzle 2.1 sprays according to the valve group control unit 1.3 signal branch three ways: the first path is sprayed to a flue in front of an SCR (selective catalytic reduction) catalytic reactor behind an economizer, the second path is sprayed to a flue in front of an air preheater behind the SCR catalytic reactor, and the third path is sprayed to an absorption tower below a demister; wherein, the first path and the second path adopt high-pressure air and a double-fluid nozzle for spraying and continuously operate; the third path adopts a spiral hollow cone nozzle for spraying and can continuously/discontinuously operate.

Further, the nozzle 2.1 is a two-fluid nozzle.

Further, the absorbent preparation distribution control system 1 comprises a NaHSO3 solution storage tank 1.1 and NaHSO₃The device comprises a delivery pump 1.2, a valve bank control unit 1.3 and a metering unit 1.4;

NaHSO₃solution storage tank 1.1 and NaHSO₃The delivery pump 1.2, the valve group control unit 1.3 and the metering unit 1.4 are connected in sequence; wherein, NaHSO₃Solution storage tank 1.1 and NaHSO₃The preparation system is connected with a metering unit 1.4 and a nozzle 2.1 and NaHSO respectively₃The spraying layers are connected by 5.3; SO (SO)₃The absorbent is industrial bagged sodium bisulfite, and is prepared into dilute NaHSO3 solution with low concentration (10-15%) by adding desalted water, stirring, diluting, etc., and the solution is conveyed to NaHSO₃A solution storage tank 1.1;

the valve group control unit 1.3 receives signals from the SO₃The signal of the gas sampling monitoring system respectively controls the first path, the second path and the third path of injection (wherein, the first path of injection is injected into SCR (selective catalytic reduction) behind the economizerReduction technology) flue in front of SCR catalytic reactor, the second path is sprayed to flue in front of air preheater behind SCRSCR catalytic reactor, and the third path is sprayed to absorption tower below demister) opening and closing of pipeline valve, metering unit is used for metering optimal alkali liquor and SO₃Automatic adjustment of the stoichiometry of NaHSO to be assigned to each injection point₃Amount of solution to ensure NaHSO₃Maximum utilization of solution and reduction of NaHSO₃Consumption.

Further, flue gas SO₃The concentration sampling monitoring system 4 is connected on an inlet flue 5.6 between the economizer 8 and the SCR catalytic reactor 10, between the air preheater 11 and the dust remover 12 and on an outlet flue 5.5 of the absorption tower 5;

valve group control unit 1.3 and flue gas SO₃The concentration sampling monitoring system 4 is connected;

further, flue gas SO₃The concentration sampling monitoring system 4 comprises SO₃Analyzer and Signal processing System, SO₃The analyzer is connected with the signal processing system; for comprehensively controlling SO in the flue between the rear part of the economizer 8 and the outlet of the absorption tower 5₃Concentration, and then adjusting each path of NaHSO₃Amount of injection, and thus to SO₃The precise removal is carried out to achieve the purpose of reducing NaHSO₃The purpose of solution consumption; the utility model discloses set up three sampling point: the first sampling point is arranged behind the economizer and the first path of NaHSO₃A flue between the injection points and a second sampling point are arranged on a second path of NaHSO₃A flue between the air preheater and the dust remover after the injection point, and a third sampling point arranged in a third path NaHSO₃An absorption tower outlet flue behind the injection point;

the utility model provides a flue gas sampling and SO in flue gas₃Measurement with PENTOL SO₃An analyzer; the SO3 analyzer inputs the measurement results to a signal processing system.

The NaHSO₃The delivery pump 1.2, the valve group control unit 1.3, the metering unit 1.4, the SCR catalytic reactor 3.1, the air preheater 3.2, the dust remover 3.3, the two-fluid nozzle, the boiler 7 and the dryer 8 are all the prior art.

The SO₃The analyzer and the signal processing system are both prior art; wherein the content of the first and second substances,the analyzer adopts German PENTOL SO₃And the analyzer is used for acquiring a result and transmitting the acquired result into the signal processing system in a signal form.

Collection emulation, monitoring full flow control flue gas SO₃The working process of the system is as follows:

1) according to the parameters of the flue gas, NaHSO₃Spraying parameters and the like, and designing a set of flue baffle grid integrated structure with good mixed flow effect and small pressure loss by adopting a CFD simulation technology;

2) using PENTOL SO₃The analyzer samples the flue gas and measures SO in the flue gas₃Concentration measurement, three sampling points are set: the first sampling point is arranged behind the economizer and the first path of NaHSO₃A flue between the injection points and a second sampling point are arranged on a second path of NaHSO₃A flue between the air preheater and the dust remover after the injection point, and a third sampling point arranged in a third path NaHSO₃An absorption tower outlet flue behind the injection point; the SO3 analyzer inputs the measured data into the SO₃A gas sampling monitoring system signal processing module;

3) from NaHSO₃The low-concentration NaHSO3 solution of the preparation system 9 enters NaHSO₃Solution storage tank 1.1, passing through NaHSO₃The delivery pump 1.2 is delivered to a NaHSO3 injection point in three paths through a valve group control unit 1.3 and a metering unit 1.4: the first path is sprayed to a flue in front of an SCRSCR catalytic reactor behind an economizer, the second path is sprayed to a flue in front of an air preheater behind the SCRSCR catalytic reactor, and the third path is sprayed to an absorption tower below a demister;

4) the valve group control unit 1.3 respectively controls the first path NaHSO, the second path NaHSO and the third path NaHSO according to the signals fed back by the signal processing module₃Opening and closing the solution pipeline valve, wherein the first pipeline valve and the second pipeline valve are normally opened, and the third pipeline valve is normally closed under the normal condition;

5) the metering unit 1.4 respectively controls the supply amounts of the first, second and third paths of NaHSO3 solutions according to the signals fed back by the signal processing module:

the specific regulation and control process is as follows: the first sampling point is mainly measured as SO in the boiler flue gas₃Concentration, adjusting the first NaHSO according to the measurement signal₃Solution sprayingThe liquid drops of the first path of injection point are gradually dried by the waste heat of the flue gas, and the SO in the flue gas from an economizer 8 of a boiler 7 is mixed in the drying process₃The reaction generates fine sodium sulfate powder, and most of SO in the flue gas is removed₃(ii) a First path NaHSO₃SO not removed after solution spraying₃Gas and SO from SCR reactor₂Generated SO₃Gas from the second path of NaHSO₃Removing SO by spraying solution₃The concentration is measured by the second sampling point, and the second path NaHSO is adjusted according to the measurement signal₃The spraying amount of the solution, the liquid drop of the second spraying point and SO₃Fine sodium sulfate powder is generated by the reaction and is removed by a subsequent dust remover 12 after passing through an air preheater 11; the third measuring point is mainly used for measuring whether the concentration of SO3 in the clean flue gas exhausted into the atmosphere meets the emission standard or not, and if SO, the third path of NaHSO3 is detected₃Closing the valve of the solution pipeline, and if the valve of the solution pipeline is not satisfied, opening the third path of NaHSO according to the measurement signal₃And (4) carrying out jet removal on a solution pipeline valve.

The utility model adopts CFD simulation to individually design the flue efficiency-improving device after the alkali liquor injection point, and has simple structure, small pressure loss, short design period and low cost; the flue is used for improving the efficiency to ensure that alkali liquor and SO are sprayed₃Fully mixed and reacted, and can effectively promote SO₃The removal efficiency of (2).

The utility model discloses utilize segmentation multiple spot monitoring, multistage accurate desorption method, guaranteeing high SO₃On the premise of removing efficiency, the method is helpful for greatly reducing the consumption of alkali liquor, has obvious economic advantages and is convenient for wide popularization.

Other parts not described belong to the prior art.

Claims

1. Simulation and monitoring full-process control flue gas SO₃A system, characterized by: comprises an absorbent preparation distribution control system (1), an absorbent injection system (2), an absorbent injection section flue effect-improving device (3) and flue gas SO₃A concentration sampling monitoring system (4);

the absorbent preparation distribution control system (1) is respectively connected with the absorbent injection system (2) and the absorption tower (5);

the absorbent injection system (2) is respectively connected with the absorbent injection section flue effect-raising device (3) and the absorption tower (5);

the boiler (7) is respectively connected with the flue of the absorbent injection section to improve the effect of the device (3) and the flue gas SO₃The concentration sampling monitoring system (4) is connected;

the flue gas outlet of the absorption tower (5) and the flue gas SO₃The concentration sampling monitoring system (4) is connected.

2. The integrated simulation and monitoring full-process control flue gas SO as claimed in claim 1₃A system, characterized by: a flue gas inlet (5.1) is arranged on the side wall of the absorption tower (5);

the interior of the absorption tower (5) is provided with a gas uniform distributor (5.2) and NaHSO from bottom to top₃A spraying layer (5.3) and a demister (5.4); the gas uniform distributor (5.2) is arranged above the flue gas inlet (5.1);

an outlet flue (5.5) is arranged at the upper end of the absorption tower (5), and an inlet flue (5.6) is arranged at the side of the lower part of the absorption tower;

wherein, the outlet flue (5.5) and SO₃The concentration sampling monitoring system (4) is connected;

one end of the inlet flue (5.6) is connected with the economizer (8), and the other end is connected with the flue gas inlet (5.1);

the inlet flue (5.6) is sequentially provided with an SCR catalytic reactor (10), an air preheater (11) and a dust remover (12), wherein the SCR catalytic reactor (10) is positioned at the outlet end of the economizer (8), and the dust remover (12) is positioned at the inlet end of the flue gas inlet (5.1).

3. The integrated simulation and monitoring full-process control flue gas SO as claimed in claim 2₃A system, characterized by: the absorbent injection section flue effect-lifting device (3) is arranged in the inlet flue (5.6) and is arranged behind the injection point of the nozzle (2.1);

the flue effect-improving device (3) of the absorbent injection section comprises an annular inclined baffle (3.1) on the inner wall of the flue gas pipeline, a grid (3.2) and a support (3.3);

the inner wall of the flue gas pipeline is provided with an annular inclined baffle (3.1) on the inner wall of the inlet flue (5.6);

the support (3.3) is arranged on the inner wall of the annular inclined baffle (3.1) on the inner wall of the flue gas pipeline; the supports (3.3) are uniformly arranged along the inner wall of the inlet flue (5.6); 4-6 supports (3.3);

the grating (3.2) is respectively connected with the annular inclined baffle (3.1) and the support (3.3).

4. The set of simulation and monitoring full-process control flue gas SO of claim 3₃A system, characterized by: the absorbent injection system (2) comprises NaHSO₃A solution delivery pump (1.2) and a nozzle (2.1);

the compressed air buffer tank (6) is connected with the nozzle (2.1);

the nozzle (2.1) is connected to the inlet flue (5.6); a plurality of nozzles (2.1) are arranged; the nozzles (2.1) are respectively arranged on the front side and the rear side of the SCR catalytic reactor (10).

5. The set of simulation and monitoring full-process control flue gas SO of claim 4₃A system, characterized by: the nozzle (2.1) is a two-fluid nozzle.

6. The set of simulation and monitoring full-process control flue gas SO of claim 5₃A system, characterized by: the absorbent preparation distribution control system (1) comprises NaHSO₃Solution storage tank (1.1) and NaHSO₃The device comprises a delivery pump (1.2), a valve bank control unit (1.3) and a metering unit (1.4);

NaHSO₃solution storage tank (1.1) and NaHSO₃The delivery pump (1.2), the valve group control unit (1.3) and the metering unit (1.4) are connected in sequence; wherein, NaHSO₃Solution storage tank (1.1) and NaHSO₃The preparation system (9) is connected, and the metering unit (1.4) is respectively connected with the nozzle (2.1) and the NaHSO₃The spraying layers (5.3) are connected.

7. The set of simulation and monitoring full-process control flue gas SO of claim 6₃A system, characterized by: flue gas SO₃The concentration sampling monitoring system (4) is respectively connected on the inlet flue (5.6) between the economizer (8) and the SCR catalytic reactor (10) and between the air preheater (11) and the dust remover (12)And an outlet flue (5.5) of the absorption tower (5);

valve group control unit (1.3) and flue gas SO₃The concentration sampling monitoring system (4) is connected.

8. The set of simulation and monitoring full-process control flue gas SO of claim 7₃A system, characterized by: flue gas SO₃The concentration sampling monitoring system (4) comprises SO₃Analyzer and Signal processing System, SO₃The analyzer is connected with the signal processing system.