WO2011065118A1

WO2011065118A1 - System for controlling operation of desulfurization apparatus

Info

Publication number: WO2011065118A1
Application number: PCT/JP2010/066495
Authority: WO
Inventors: 直行神山; 栄基伊藤; 誠筒井; 立人長安; 紀和稲葉
Original assignee: 三菱重工業株式会社
Priority date: 2009-11-24
Filing date: 2010-09-24
Publication date: 2011-06-03
Also published as: JP2011110440A

Abstract

A system for controlling the operation of a desulfurization apparatus, equipped with an electric dust collector for collecting coal ash in an exhaust gas and an absorption column for bringing the dedusted exhaust gas from the electric dust collector into contact with an absorbing liquid so as to allow limestone in the absorbing liquid to absorb SO₂ in the dedusted exhaust gas while discharging the desulfurized exhaust gas from which SO₂ has been removed, wherein the activity constant (K) of the limestone is calculated based on the SO₂ concentration (S1) of the dedusted exhaust gas, the SO₂ concentration (S2) of the desulfurized exhaust gas, the flow rate (S3) of the exhaust gas, the limestone concentration (C) of the absorbing liquid, the tank volume (V) of the absorbing liquid having been brought into contact with the dedusted exhaust gas and pooled in the absorption column, and pH of the absorption liquid, and the activation state of the lime stone is determined by comparing the aforesaid limestone activity constant (K) with a preset lime stone activity constant threshold (X).

Description

Operation control system for desulfurization equipment

The present invention relates to an operation control system for a desulfurization facility that removes SO ₂ contained in exhaust gas.

In a desulfurization facility that desulfurizes SO ₂ in exhaust gas by the lime gypsum method, a cooling tower that removes coal ash and hydrogen fluoride gas is installed in advance before desulfurization, and an absorption tower that removes SO ₂ is installed after that. A so-called dual loop process or a so-called single loop process in which SO ₂ is removed only by an absorption tower without using a cooling tower is used.

However, the dual loop process requires cooling tower installation costs, operation costs, and low pH wastewater treatment equipment discharged from the cooling towers. In addition to increasing the site, construction costs and operation costs increase. Is a big problem.

On the other hand, in the single loop process, there is no problem as in the dual loop process because the cooling tower equipment is not provided, but due to the influence of coal ash and hydrogen fluoride gas, which are unique components contained in the exhaust gas, The problem is that the desulfurization performance and the purity of the gypsum produced as a by-product decrease due to the decrease in the dissolution rate of the limestone, which is the absorbent, and the amount of limestone consumed increases to compensate for this. There is.

As shown in the following formula 1, the deactivation phenomenon is caused by aluminum ions contained in coal ash being dissolved in the absorbing solution and hydrogen fluoride contained in exhaust gas being dissolved in the absorbing solution. It is considered that the fluoroaluminum complex (AlFx) generated by the reaction with fluorine ions is adsorbed on the surface of limestone (CaCO ₃ ) to reduce the dissolution rate.
Al ³⁺ + XF ⁻ → AlFx ^(3-x) [x = 1 to 6] Equation 1

In order to prevent the deactivation phenomenon in the single loop process, the following two methods have been conventionally used.
(1) To reduce the inflow of coal ash, the causative substance, into the absorbent, improve the performance of the electrostatic precipitator placed in the front stage of the absorption tower.
(2) The concentration of limestone, which is an absorption raw material in the absorption liquid, is increased to increase the pH of the absorption liquid to reduce the amount of aluminum dissolved from the coal ash and to decompose the produced AlFx. AlFx decomposes and becomes aluminum hydroxide (Al (OH ₃ )) and calcium fluoride (CaF ₂ ) having low solubility and moves to the solid phase, and the deactivation phenomenon is eliminated.

However, in the method (1), the performance of the electrostatic precipitator is greatly affected by the type of coal and the combustion conditions, and stable coal ash removal performance may not be obtained. Since the aluminum dissolution rate sometimes changes greatly, it has been difficult to stably suppress the deactivation phenomenon.

In the above method (2), although the deactivation phenomenon can be suppressed by increasing the concentration of limestone, which is the raw material for absorption in the absorbent, Reactive limestone remains, and as shown in the following formula 2, the purity of gypsum (CaSO ₄ .2H ₂ O) produced as a by-product is significantly reduced by the reaction of limestone and SO ₂ . There was a problem of increasing consumption. Therefore, the pH cannot be constantly raised. Moreover, since there is a limit to the increase in pH, AlFx cannot be completely decomposed, and complete recovery from deactivation cannot be expected.
SO ₂ + 1 / 2O ₂ + CaCO ₃ + 2H ₂ O → CaSO ₄ .2H ₂ O + CO ₂ Formula 2

In this way, although improving the performance of the electrostatic precipitator or increasing the concentration of limestone to increase the pH of the absorbing solution is effective in eliminating the deactivation phenomenon, it causes new problems as described above. There is a fear. Therefore, in order to prevent the deactivation phenomenon, it is desirable to quickly grasp the situation leading to the deactivation phenomenon and monitor the activity status of the limestone in the absorbent so that the deactivation can be rehabilitated before reaching the deactivation phenomenon. It is rare.

Conventionally, Patent Document 1 discloses an exhaust gas treatment provided with an electrostatic precipitator and a wet desulfurization device that is installed downstream of the electrostatic precipitator in the exhaust gas flow direction and performs desulfurization treatment of exhaust gas and generation of gypsum. An apparatus is disclosed. This exhaust gas treatment device includes a soot concentration detection means for detecting the soot concentration in the exhaust gas on the outlet side of the electrostatic precipitator, an exhaust gas flow rate detection means for detecting the flow rate of the exhaust gas to be processed, and the inlet SO ₂ concentration of the desulfurization device. a desulfurization apparatus inlet SO ₂ concentration detection means for detecting a desulfurizer outlet SO ₂ concentration detection means for detecting the outlet SO ₂ concentration in the desulfurization apparatus, absorbents for detecting a supply flow rate of the absorbent slurry to the absorption part of the desulfurizer The slurry flow rate detecting means, the dust amount calculating means for calculating the dust amount based on the detection signals from the dust concentration detecting means and the exhaust gas flow rate detecting means, and the detection signal in the absorbent based on the detection signal from the absorbent slurry flow rate detecting means. The amount of impurities in the absorbent for calculating the amount of impurities, the amount of soot calculated by the means for calculating the amount of dust, and the amount of impurities in the absorbent calculated by the means for calculating the amount of impurities in the absorbent Gypsum purity prediction calculation means for predicting the purity of the gypsum to be generated based on, and electric dust collector control means for adjusting the operating conditions of the electric dust collector based on the predicted value from the gypsum purity prediction calculation means ing.

Conventionally, Patent Document 2 discloses a control device that controls a plurality of environmental devices installed to remove a predetermined substance in one exhaust gas system in which the concentration of the predetermined substance contained in the exhaust gas is managed. And an environmental device control system including a measuring device for detecting the concentration of a predetermined substance. In this environmental device control system, the control device stores an efficiency table including efficiency information of a predetermined element with respect to a predetermined substance removal capability for each of a plurality of environmental devices, and the measurement unit calculates the detected concentration of the predetermined substance. The control device determines the amount of change for changing the concentration of the substance from the concentration of the predetermined substance received from the measurement unit and the target value of the concentration of the predetermined substance. Then, an efficient environmental device is selected with reference to the efficiency table, and control is performed so that the environmental device performs processing.

Japanese Patent No. 2510583 JP 2004-37056 A

The present invention solves the above-mentioned problems, and provides an operation control system for a desulfurization facility that can monitor the activity status of limestone while grasping whether or not the activity of limestone in the absorption liquid is a deactivation sign. The purpose is to provide.

In order to achieve the above-described object, in the operation control system of the desulfurization facility of the present invention, an electrostatic precipitator that collects coal ash in the exhaust gas, and an absorbing liquid is brought into contact with the dedusted exhaust gas that has passed through the electric dust collector. in desulfurization of operation control system comprising an absorption tower for discharging the desulfurized flue gas while the SO ₂ is absorbed in the limestone in the absorbing liquid SO ₂ has been removed in the dust removal in the exhaust gas by causing the dedusting flue gas and SO ₂ concentration in the a SO ₂ concentration of the desulfurization in the exhaust gas, and the exhaust gas flow rate of the exhaust gas, and limestone concentration of the absorbent liquid, the absorbent liquid stored in contact with the dedusting flue gas in said absorption tower Management device that calculates the limestone activity constant based on the amount of the absorption liquid tank held in and the pH of the absorption liquid, and compares the limestone activation constant with a preset limestone activation constant threshold to determine the activity status of the limestone The It is characterized by having.

According to the operation control system of this desulfurization facility, the activity status of limestone can be monitored while grasping whether or not the activity of limestone in the absorption liquid is a deactivation sign.

Further, in the operation control system of the desulfurization facility of the present invention, the management device, when the activity status of limestone is a deactivation sign, the relationship between the limestone concentration and the limestone activity constant, and the pH and the limestone activity constant Based on the relationship, the cause of deactivation is determined.

運転 According to the operation control system of this desulfurization facility, the cause of deactivation can be grasped.

Further, in the operation control system for the desulfurization facility of the present invention, the management device regenerates the deactivation sign based on the cause leading to deactivation, and the dust collection force of the electric dust collector and / or the absorption. The supply amount of limestone to the liquid is set.

According to the operation control system of this desulfurization facility, the electrostatic precipitator and / or the limestone feeder is driven according to the deactivation sign, so that the deactivation sign can be rehabilitated to prevent the deactivation phenomenon. In addition, since the electrostatic precipitator and / or limestone feeder is driven according to the deactivation sign, it is possible to prevent excessive consumption of electric power and limestone, and to prevent deterioration of the quality of the gypsum produced as a by-product.

Further, in the operation control system of the desulfurization facility of the present invention, the SO ₂ concentration in the dedusted exhaust gas, the SO ₂ concentration in the desulfurized exhaust gas, the exhaust gas flow rate, the limestone concentration, the amount of the absorbent tank held, and the pH And collecting the coal ash in the exhaust gas by the electric dust collector and the control device for controlling the supply of limestone to the absorption liquid, the electric dust collector, and the absorption tower, and desulfurization equipment for removing sO ₂ is formed, the management device is characterized in that through the upper network is communicatively connected with the control device in the desulfurization.

運転 According to the operation control system of this desulfurization facility, the operation control of the desulfurization facility can be performed at a remote place.

The operation control system of the desulfurization facility of the present invention further includes a strong alkaline liquid supply unit that supplies a strong alkaline liquid to the absorption liquid of the absorption tower, and the management device has the limestone activation constant threshold value that is the limestone activation constant threshold value. If less, the supply amount of the strong alkali solution by the strong alkali solution supply unit is set.

This desulfurization equipment operation control system can avoid deactivation. In addition, since the strong alkaline solution is supplied as necessary, it is possible to prevent the excessive consumption of the strong alkaline solution.

Further, in the operation control system of the desulfurization facility of the present invention, the SO ₂ concentration in the dedusted exhaust gas, the SO ₂ concentration in the desulfurized exhaust gas, the exhaust gas flow rate, the limestone concentration, the amount of the absorbent tank held, and the pH A controller for controlling the electrostatic precipitator, the supply of limestone to the absorbing liquid, and the strong alkaline liquid supply unit, the electrostatic precipitator, the absorption tower, and the strong alkaline liquid The supply unit constitutes a desulfurization facility that collects coal ash in the exhaust gas and removes SO ₂ , and the management device is communicably connected to the control device in the desulfurization facility via a network. It is characterized by.

According to this desulfurization equipment operation control system, the operation control of the desulfurization equipment can be performed remotely via the network.

In the operation control system for a desulfurization facility according to the present invention, the management device is connected to the control devices in a plurality of desulfurization facilities via a network so as to be communicable.

This operation control system for a desulfurization facility makes it possible to control operation of a plurality of desulfurization facilities from a remote location through a network.

According to the present invention, it is possible to monitor the activity status of limestone while grasping whether or not the activity of limestone in the absorption liquid is a deactivation sign.

FIG. 1 is a schematic diagram of an operation control system for a desulfurization facility according to Embodiment 1 of the present invention. FIG. 2 is a block diagram of the operation control system for the desulfurization facility according to Embodiment 1 of the present invention. FIG. 3 is a graph of the relationship between the limestone concentration of the absorbent and the limestone activity constant. FIG. 4 is a graph of the relationship between the pH of the absorbent and the limestone activity constant. FIG. 5 is a flowchart showing the operation of the operation control system for the desulfurization facility according to Embodiment 1 of the present invention. FIG. 6 is a schematic diagram of an operation control system for a desulfurization facility according to Embodiment 2 of the present invention. FIG. 7 is a block diagram of an operation control system for a desulfurization facility according to Embodiment 2 of the present invention. FIG. 8 is a flowchart showing the operation of the operation control system for the desulfurization facility according to Embodiment 2 of the present invention.

Hereinafter, embodiments of the present invention will be described in detail with reference to the drawings. Note that the present invention is not limited to the embodiments. In addition, constituent elements in the following embodiments include those that can be easily replaced by those skilled in the art or those that are substantially the same.

[Embodiment 1]
The present embodiment will be described with reference to the drawings. 1 is a schematic diagram of an operation control system for a desulfurization facility according to Embodiment 1. FIG. As shown in FIG. 1, a desulfurization facility 1 includes an electric dust collector 2 that collects coal ash in an exhaust gas 100 a from a coal fired boiler (not shown) such as a thermal power plant, and an electric dust collector 2. and SO 2 absorption tower 3 to remove _(sulfur dioxide) in the dedusting exhaust gas 100b having passed through, and a control unit 9.

The electrostatic precipitator 2 charges the dust such as coal ash by corona discharge to the exhaust gas 100a supplied in the casing, and attaches the dust to the positively and negatively charged attachment portions by an electric suction force. The electric dust collector 2 is provided with a power supply device 2a and is driven by voltage supply from the power supply device 2a. The dust-removed exhaust gas 100b removed by the electric dust collector 2 is supplied into the absorption tower 3 through the dust-removed exhaust gas pipe 2b.

The absorption tower 3 absorbs SO ₂ (sulfur dioxide) in the dedusted exhaust gas 100b by contacting the dedusted exhaust gas 100b passed through the electrostatic precipitator 2 with an absorbent 101 containing limestone (hereinafter referred to as an absorbent). The desulfurization exhaust gas 100c from which the limestone in the liquid 101 is absorbed and thereby SO ₂ is removed is discharged.

Absorption liquid 101 is stored in the bottom of absorption tower 3. A limestone feeder 3 a is provided outside the absorption tower 3, and the limestone 102 is measured by the limestone feeder 3 a and supplied to the bottom of the absorption tower 3. Further, water 103 is supplied to the bottom of the absorption tower 3. That is, the absorption liquid 101 is generated by the limestone 102 and the water 103 supplied to the bottom of the absorption tower 3.

Absorption liquid 101 stored in a tank provided at the bottom of absorption tower 3 is pumped by absorption liquid circulation pump 3b and supplied to the upper part of absorption tower 3 via absorption liquid header 3c outside absorption tower 3. . Then, the absorption liquid 101 comes into contact with the dedusted exhaust gas 100b rising in the absorption tower 3 in the process of flowing down from the nozzle 3d provided in the upper part in the absorption tower 3 and reaching the lower part in the absorption tower 3. Thereby, SO ₂ contained in the dedusted exhaust gas 100b reacts with the limestone 102 in the absorbing liquid 101 (see the above formula 2), and SO ₂ is removed from the dedusted exhaust gas 100b. Then, the desulfurization exhaust gas 100c from which SO ₂ has been removed is discharged from the desulfurization facility 1 via the desulfurization exhaust gas pipe 3e connected to the top of the absorption tower 3. Further, the absorbing liquid 101 used for the removal of SO ₂ is stored at the bottom in the absorption tower 3.

Further, a part of the absorption liquid 101 stored at the bottom in the absorption tower 3 is dehydrated through an extraction pipe 3f branched from the absorption liquid header 3c outside the absorption tower 3 while being pumped by the absorption liquid circulation pump 3b. Sent to 3g. The dehydrator 3g is constituted by, for example, a belt filter, dehydrates the absorbent 101 in the process of being conveyed by the belt filter, and is discharged out of the system as gypsum 104. Moreover, the filtrate which dehydrated the absorption liquid 101 is utilized as the water 103 supplied to the bottom part of the absorption tower 3 in this Embodiment.

Oxidizing air 105 is supplied to the bottom of the absorption tower 3. For this reason, since the oxidizing liquid 105 is contained in the absorbing liquid 101, the oxidizing of the absorbing liquid 101 is promoted, so that the SO ₂ removal efficiency can be improved.

In the absorption tower 3 described above, the desorbed exhaust gas 100b rising in the absorption tower 3 by flowing the absorption liquid 101 supplied to the upper part of the absorption tower 3 through the absorption liquid header 3c from the nozzle 3d, and It is not limited to this. For example, although not clearly shown in the figure, the absorption liquid is supplied to the middle part of the absorption tower via the absorption liquid header, and the absorption liquid is ejected upward from the nozzle provided in the middle part of the absorption tower. As a result, the absorbing liquid becomes fine droplets while being dispersed in the upper part of the absorption tower, descends in the absorption tower, and comes into contact with dedusted exhaust gas rising in the absorption tower. As a result, a larger gas-liquid contact area is secured and the gas-liquid contact efficiency is improved, so that the SO ₂ removal efficiency can be improved. For the contact between the absorbing liquid 101 and the dedusted exhaust gas 100b, in addition to the countercurrent contact described above, a cocurrent contact or a cocurrent contact in which the dedusted exhaust gas 100b flows in parallel with the absorbing liquid 101 that flows down is used. And co-current contact combined with counter-current contact.

In the desulfurization facility 1 described above, the dust removal exhaust pipe 2b is provided with an inlet side SO ₂ concentration detection unit 4 that detects the SO ₂ concentration S1 in the dust removal exhaust gas 100b that passes through the electrostatic precipitator 2 and reaches the absorption tower 3. It has been. The desulfurization exhaust gas pipe 3e is provided with an outlet-side SO ₂ concentration detection unit 5 that detects the SO ₂ concentration S2 in the desulfurization exhaust gas 100c discharged from the absorption tower 3. Moreover, the limestone density | concentration detection part 6 which detects the limestone density | concentration C of the absorption liquid 101 is provided in the absorption liquid header 3c. Further, in the absorption tower 3, the absorption tank holding amount for detecting the holding amount (hereinafter referred to as absorption tank holding amount) V of the absorption liquid 101 stored in contact with the dedusted exhaust gas 100 b in the absorption tower 3. A detection unit 7 is provided. Further, the absorbent header 3c is provided with a pH detector 8 that detects the pH of the absorbent 101. An exhaust gas flow rate detection unit 4a that detects the exhaust gas flow rate S3 of the dedusted exhaust gas 100b (exhaust gas 100a) is also provided at the position where the inlet side SO ₂ concentration detection unit 4 is provided.

The SO ₂ concentration S1 in the dedusted exhaust gas 100b detected by the inlet side SO ₂ concentration detector 4, the SO ₂ concentration S2 in the desulfurized exhaust gas 100c detected by the outlet side SO ₂ concentration detector 5, and the exhaust gas flow rate The exhaust gas flow rate S3 detected by the detection unit 4a, the limestone concentration C of the absorption liquid 101 detected by the limestone concentration detection unit 6, the absorption liquid tank holding amount V detected by the absorption liquid tank holding amount detection unit 7, and the pH detection Each data of the pH of the absorbent 101 detected by the unit 8 is input to the control device 9.

The control device 9 will be described with reference to the block diagram of the operation control system for the desulfurization facility according to Embodiment 1 in FIG. The control device 9 is configured by a microcomputer or the like. The control device 9 is provided with a storage unit 9a. The storage unit 9a includes a RAM, a ROM, and the like, and stores programs and data. The control device 9 also includes a feeder motor (not shown) for operating the electrostatic precipitator drive unit 9b for applying a voltage to the power supply device 2a when operating the electrostatic precipitator 2 and the limestone feeder 3a. ) Is provided with a limestone feeder driver 9c. Further, the control device 9 is provided with an input / output unit 9d. The input / output unit 9d includes a keyboard, a mouse, and a monitor. The control device 9 is provided with an information communication unit 9e. The information communication unit 9e is for performing information communication with the information communication unit 10d of the management apparatus 10. Based on information input from the management device 10, the control device 9 controls the electrostatic precipitator 2 and the limestone feeder 3a in accordance with programs and data stored in advance in the storage unit 9a.

The management apparatus 10 is demonstrated with reference to the block diagram of the operation control system of the desulfurization equipment which concerns on Embodiment 1 of FIG. The management device 10 is configured by a microcomputer or the like. Management device 10, as shown in FIG. 1, the control unit 9 and is connected through the upper network N, SO ₂ concentration S1 in dedusting exhaust gas 100b, SO ₂ concentration S2 of in desulfurized flue gas 100c, exhaust gas flow rate S3, Each data of the limestone concentration C of the absorbing liquid 101, the absorbing tank holding amount V, and the pH of the absorbing liquid 101 is acquired from the control device 9.

The management device 10 is provided with a storage unit 10a. The storage unit 10a includes a RAM, a ROM, and the like, and stores programs and data. The storage unit 10a includes an activity constant expression database 10aa, a limestone activation constant threshold database 10ab, a limestone concentration / limestone activation constant database 10ac, a pH / limestone activation constant database 10ad, a power supply supply voltage database 10ae, and a limestone feeder supply voltage database 10af. Have.

Activity constant expression database 10aa was acquired from the control unit 9, SO ₂ concentration S1 in dedusting exhaust gas 100b, SO ₂ concentration S2 of in desulfurized flue gas 100c, limestone concentration of the absorbent 101 C, the absorption liquid tank stockpile V, And the following formula 3 for calculating the limestone activity constant K based on each data of the pH of the absorbent 101 is stored.
K = f (ΔS, C, V, pH) Equation 3
Here, ΔS is the SO ₂ removal amount obtained by removing SO ₂ from the exhaust gas 100a by the limestone 102 in the absorbing liquid 101, and the SO ₂ concentration S2 in the desulfurized exhaust gas 100c is changed from the SO ₂ concentration S1 in the dedusted exhaust gas 100b. Subtract and multiply by the exhaust gas flow rate S3.
In Equation 3, the larger the SO ₂ removal amount ΔS, the better the activity of the limestone 102 to absorb SO ₂ and the higher the limestone activity constant K. Furthermore, as the pH of the absorption liquid 101 is high in activity may limestone activity constant K limestone 102 absorbs SO ₂ is high. On the other hand, the higher the limestone concentration C, the worse the activity of the limestone 102 to absorb SO _2, and the lower the limestone activity constant K. Moreover, the more the absorbent liquid tank holding amount V is, the less active the limestone 102 absorbs SO ₂ and the lower the limestone activity constant K.

The limestone activity constant threshold value database 10ab stores a limestone activity constant threshold value X that is a reference for determining the activity status of the limestone 102.

The limestone concentration / limestone activity constant database 10ac stores the relationship between the limestone concentration C and the limestone activity constant K. As described above, the relationship between the limestone concentration C and the limestone activity constant K is such that the higher the limestone concentration C, the lower the activity of the limestone 102 to absorb SO ₂ and the lower the limestone activity constant K. Specifically, FIG. It shows in the graph of the relationship between the limestone density | concentration of an absorption liquid, and a limestone activity constant.

The pH / limestone activity constant database 10ad stores the relationship between the pH of the absorbent 101 and the limestone activity constant K. As described above, the relationship between the pH of the absorption liquid 101 and the limestone activity constant K is such that the higher the pH of the absorption liquid 101, the better the limestone 102 absorbs SO ₂ and the higher the limestone activation constant K. Fig. 4 is a graph showing the relationship between the pH of the absorbing solution and the limestone activity constant in Fig. 4.

The power supply voltage database 10ae stores power supply voltage information for applying a voltage to the power supply 2a of the electrostatic precipitator 2 corresponding to the limestone activation constant K described above.

The limestone feeder supply voltage database 10af stores feeder voltage information for applying a voltage to a feeder motor (not shown) of the limestone feeder 3a corresponding to the limestone activation constant K described above.

Further, the management device 10 is provided with a processing unit 10b. The processing unit 10b includes an activity constant calculation unit 10ba, an activity status determination unit 10bb, and a deactivation cause determination unit 10bc.

The activity constant calculation unit 10ba adds the SO ₂ removal amount ΔS, the limestone concentration C, the absorption liquid tank holding amount V, and the pH of the absorption liquid 101 to the above equation 3 stored in the activation constant expression database 10aa of the storage unit 10a. To calculate the limestone activity constant K.

The activity status determination unit 10bb compares the limestone activity constant K calculated by the activity constant calculation unit 10ba with the limestone activity constant threshold value X stored in the limestone activity constant threshold value database 10ab, and determines the activity status of the limestone 102. Specifically, the limestone activity constant threshold value X is the lowest value at which the activity of the limestone 102 is good. And if the limestone activity constant K is more than the limestone activity constant threshold value X, it can be determined that the activity of the limestone 102 is good. That is, if the limestone activity constant K exceeds the limestone activity constant threshold value X, the activity of the limestone 102 is better, and the activity of the limestone 102 becomes worse as the limestone activity constant K approaches the limestone activity constant threshold value X, that is, lost. It can be determined that there is a vital sign. On the other hand, when the limestone activation constant K is less than the limestone activation constant threshold X, it can be determined that the activity of the limestone 102 is poor, that is, it is in a deactivation phenomenon.

The deactivation cause determination unit 10bc determines the limestone concentration C stored in the limestone concentration / limestone activation constant database 10ac when the activation status determination unit 10bb is in a deactivation sign where the limestone activation constant K approaches the limestone activation constant threshold value X. And the limestone activity constant K, and the relationship between the pH of the absorbent 101 and the limestone activity constant K stored in the pH / limestone activity constant database 10ad, the cause of deactivation is determined.

Also, the management device 10 is provided with an input / output unit 10c. The input / output unit 10c includes a keyboard, a mouse, and a monitor. In addition, the management device 10 is provided with an information communication unit 10d. The information communication unit 10 d is for performing information communication with the information communication unit 9 e of the control device 9. This management device 10 controls the electrostatic precipitator 2 and the limestone feeder 3a in an integrated manner with respect to the control device 9 in accordance with programs and data stored in advance in the storage unit 10a based on information input from the control device 9. To output information.

The operation control of the desulfurization facility by the control device 9 and the management device 10 described above will be described with reference to the flowchart showing the operation of the operation control system of the desulfurization facility according to the first embodiment in FIG.

As shown in FIG. 5, first, in the control device 9, the desulfurization detected by the SO ₂ concentration S 1 in the dedusted exhaust gas 100 b detected by the inlet side SO ₂ concentration detection unit 4 and the outlet side SO ₂ concentration detection unit 5. The SO ₂ concentration S2 in the exhaust gas 100c, the exhaust gas flow rate S3 detected by the exhaust gas flow rate detection unit 4a, the limestone concentration C of the absorption liquid 101 detected by the limestone concentration detection unit 6, and the absorption liquid tank holding amount detection unit 7 are detected. Each data of the absorption tank holding amount V and the pH of the absorption liquid 101 detected by the pH detector 8 is output to the management device 10 (step ST1). Then, the management device 10 inputs the above data (step ST2).

Next, in the management device 10, the activity constant calculation unit 10ba calculates the limestone activation constant K based on the above equation 3 stored in the activity constant equation database 10aa (step ST3).

Next, in the management apparatus 10, the activity status determination unit 10bb compares the limestone activation constant K calculated by the activation constant calculation unit 10ba with the limestone activation constant threshold X stored in the limestone activation constant threshold database 10ab, and the limestone The active status of 102 is determined (step ST4).

Thereby, it can be grasped from the activity state of the limestone 102 in the desulfurization facility 1 whether or not the activity of the limestone 102 is an inactivation sign.

And in the determination in step ST4, when the activity of the limestone 102 is in a deactivation sign (step ST5: Yes), in the management apparatus 10, the deactivation cause determination part 10bc determines the cause leading to deactivation (step ST6). ).

Thereby, when the activity of the limestone 102 is in the inactivation sign, the cause leading to the inactivation can be grasped.

In addition, in the determination in step ST4, when the activity of the limestone 102 is not a deactivation sign (step ST5: No), the management device 10 returns to steps ST1 and ST2 and inputs the above data output from the control device 9 To do.

Next, in the management apparatus 10, based on the cause leading to the deactivation determined in step ST6, the dust collection force of the electric dust collector 2 is set and / or limestone so as to regenerate the deactivation sign. The supply amount of 102 is set (step ST7). For setting the dust collecting power of the electrostatic precipitator 2, the power supply device voltage information for the power supply device 2 a corresponding to the limestone activation constant K is acquired from the power supply device supply voltage database 10 ae. Moreover, the supply amount of the limestone 102 acquires the feeder voltage information to the limestone feeder 3a corresponding to the limestone activation constant K from the limestone feeder supply voltage database 10af. The management device 10 outputs both or one of the voltage information to the control device 9. And the control apparatus 9 drives the electrostatic precipitator 2 and / or the limestone feeder 3a based on the input voltage information (step ST8).

This causes the deactivation sign to be rehabilitated by driving the electrostatic precipitator 2 and / or the limestone feeder 3a based on the cause of deactivation.

As described above, in the desulfurization operation control system according to the first embodiment, the exhaust gas of the SO ₂ concentration S1 in dedusting exhaust gas 100b, SO ₂ concentration S2 of in desulfurized flue gas 100c, dedusting exhaust 100b (gas 100a) The limestone activation constant K is calculated from the flow rate S3, the limestone concentration C of the absorption liquid 101, the absorption liquid tank holding amount V, and the pH of the absorption liquid 101, and the limestone activation constant K is set as a preset limestone activity. Compared with the constant threshold value X, the activity status of the limestone 102 is determined. As a result, it is possible to monitor the activity status of the limestone 102 while grasping whether the activity of the limestone 102 is a deactivation sign.

Moreover, in the operation control system of the desulfurization facility according to Embodiment 1, when the activity status of the limestone 102 is in the deactivation sign, the relationship between the limestone concentration C and the limestone activation constant K, and the pH and the limestone activation constant K Based on the relationship, determine the cause of deactivation. As a result, the cause leading to inactivation can be grasped.

Further, in the operation control system for the desulfurization facility according to the first embodiment, the dust collecting power of the electric dust collector 2 (power supplied to the power supply device 2a) is rehabilitated based on the cause of deactivation. ) And / or the supply amount of limestone 102 to the absorption liquid 101 (power supplied to the limestone feeder 3a) is set. As a result, since the electrostatic precipitator 2 and / or the limestone feeder 3a are driven according to the deactivation sign, it is possible to regenerate the deactivation sign and prevent the deactivation phenomenon. In addition, since the electrostatic precipitator 2 and / or the limestone feeder 3a are driven according to the deactivation signs, it is possible to prevent an excessive consumption of power and limestone 102 and to reduce the quality of the gypsum 104 that is by-produced. It becomes possible to prevent.

In the operation control system for the desulfurization facility according to the first embodiment, the management device 10 is connected to the control device 9 in the desulfurization facility 1 via the network N so as to be communicable. As a result, operation control of the desulfurization facility 1 can be performed at a remote location.

In the operation control system for the desulfurization facility according to the first embodiment, as shown in FIG. 1, the management device 10 is communicably connected to the control devices 9 in the plurality of desulfurization facilities 1 via the network N. . In FIG. 2, the control device 9 and the management device 10 in one desulfurization facility 1 are connected in a one-to-one relationship, but the control device 9 and the management device 10 in the plurality of desulfurization facilities 1 are connected. When connected in a many-to-one relationship, in the management device 10, the storage unit 10a, the processing unit 10b, the input / output unit 10c, and the information communication unit 10d function corresponding to each control device 9. As a result, the operation control of the plurality of desulfurization facilities 1 can be performed in a remote place. When the control device 9 and the management device 10 in the desulfurization facility 1 are connected in a one-to-one relationship, the control device 9 and the management device 10 are not connected via the network N, and the management device 10 is desulfurized. It may be configured to be included in the control device 9 of the facility 1.

Thus, in the operation control system of the desulfurization facility according to Embodiment 1, when the exhaust gas 100a from a thermal power plant or the like is processed by the desulfurization facility 1 by the lime gypsum method of a single loop process, limestone 102 as an absorbent is used. It is possible to prevent performance degradation due to deactivation of the battery and to improve operational stability. As a result, it is possible to ensure the quality of the byproduct gypsum 104 and prevent an increase in running cost.

[Embodiment 2]
The present embodiment will be described with reference to the drawings. FIG. 6 is a schematic diagram of an operation control system for a desulfurization facility according to Embodiment 2 of the present invention. In the second embodiment described below, the same reference numerals are given to the same components as those in the first embodiment described above, and the description thereof is omitted.

The desulfurization facility 1 shown in FIG. 6 is further provided with a strong alkaline solution supply unit 11 as compared with the first embodiment described above. The strong alkaline liquid supply unit 11 supplies the strong alkaline liquid 106 to the absorbing liquid 101 stored in the absorption tower 3, and absorbs the strong alkaline liquid tank 11a containing the strong alkaline liquid 106 and the strong alkaline liquid tank 11a. A strong alkaline liquid pipe 11b connected to the tower 3 and a strong alkaline liquid pump 11c interposed in the strong alkaline liquid pipe 11b are provided. That is, the strong alkaline liquid supply unit 11 pumps the strong alkaline liquid 106 stored in the strong alkaline liquid tank 11a to the absorption tower 3 via the strong alkaline liquid pipe 11b by the strong alkaline liquid pump 11c.

Further, as shown in the block diagram of the operation control system for the desulfurization facility according to the second embodiment of FIG. 7, the controller 9 operates the strong alkaline liquid supply unit 11 in comparison with the first embodiment described above. A strong alkaline liquid pump drive unit 9f for applying a voltage to the strong alkaline liquid pump 11c is further provided.

Further, as shown in FIG. 7, the storage unit 10a of the management apparatus 10 further includes a strong alkaline liquid pump supply voltage database 10ag as compared with the first embodiment described above.

The strong alkaline liquid pump supply voltage database 10ag stores pump voltage information for applying a voltage to the strong alkaline liquid pump 11c of the strong alkaline liquid supply unit 11 corresponding to the limestone activation constant K described above.

The operation control of the desulfurization facility by the control device 9 and the management device 10 described above will be described with reference to the flowchart showing the operation of the operation control system of the desulfurization facility according to the second embodiment in FIG.

As shown in FIG. 8, first, in the control device 9, the desulfurization detected by the SO ₂ concentration S 1 in the dedusted exhaust gas 100 b detected by the inlet side SO ₂ concentration detection unit 4 and the outlet side SO ₂ concentration detection unit 5. The SO ₂ concentration S2 in the exhaust gas 100c, the exhaust gas flow rate S3 detected by the exhaust gas flow rate detection unit 4a, the limestone concentration C of the absorption liquid 101 detected by the limestone concentration detection unit 6, and the absorption liquid tank holding amount detection unit 7 are detected. Each data of the absorption tank holding amount V and the pH of the absorption liquid 101 detected by the pH detector 8 is output to the management device 10 (step ST1). Then, the management device 10 inputs the above data (step ST2).

In step ST4, when the activity of the limestone 102 is not a deactivation sign (step ST5: No), the management device 10 returns to steps ST1 and ST2 and inputs the above-described data output from the control device 9.

Next, the activity status determination unit 10bb compares the limestone activation constant K calculated by the activation constant calculation unit 10ba with the limestone activation constant threshold X stored in the limestone activation constant threshold database 10ab, and the limestone activation constant K is calculated as limestone. When the activity constant is less than the threshold value X, that is, when the activity of the limestone 102 is in the deactivation phenomenon (step ST9: Yes), the management apparatus 10 is strong so as to recover the activity of the limestone 102 and avoid the deactivation phenomenon. The supply amount of the strong alkaline solution 106 in the alkaline solution supply unit 11 is set (step ST10). As for the supply amount of the strong alkaline liquid 106, the pump voltage information to the strong alkaline liquid pump 11c corresponding to the limestone activation constant K is acquired from the strong alkaline liquid pump supply voltage database 10ag. The management device 10 outputs this pump voltage information to the control device 9. And the control apparatus 9 drives the strong alkaline liquid pump 11c based on the input pump voltage information (step ST11).

In step ST9, when the activity of the limestone 102 is not a deactivation phenomenon (step ST9: No), the management device 10 returns to steps ST1 and ST2 and inputs each of the data output from the control device 9.

As described above, in the operation control system for the desulfurization facility according to the second embodiment, in addition to the first embodiment described above, when the limestone activation constant K is less than the limestone activation constant threshold value X, the strong alkaline liquid supply unit 11 performs strong. The supply amount of the alkaline liquid 106 is set. When a disturbance factor that causes inactivation, for example, a sudden change in the type of combustion coal, may result in complete inactivation (a state in which the dissolution rate of limestone is significantly reduced). As an early recovery method in this case, in the second embodiment, the strong alkaline liquid 106 is supplied to the absorption tower 3 to decompose AlFx as a deactivation cause substance. As a result, the deactivation phenomenon can be avoided. Moreover, since the strong alkaline solution 106 is supplied as necessary, it is possible to prevent a situation in which the strong alkaline solution 106 is excessively consumed.

In the operation control system for the desulfurization facility according to the second embodiment, the management device 10 is connected to the control device 9 in the desulfurization facility 1 via the network N so as to be communicable. As a result, operation control of the desulfurization facility 1 can be performed at a remote location.

In the operation control system for the desulfurization facility according to the second embodiment, as shown in FIG. 6, the management device 10 is communicably connected to the control devices 9 in the plurality of desulfurization facilities 1 via the network N. . In FIG. 7, the control device 9 and the management device 10 in one desulfurization facility 1 are connected in a one-to-one relationship, but the control device 9 and the management device 10 in the plurality of desulfurization facilities 1 are connected. When connected in a many-to-one relationship, in the management device 10, the storage unit 10a, the processing unit 10b, the input / output unit 10c, and the information communication unit 10d function corresponding to each control device 9. As a result, the operation control of the plurality of desulfurization facilities 1 can be performed in a remote place. When the control device 9 and the management device 10 in the desulfurization facility 1 are connected in a one-to-one relationship, the control device 9 and the management device 10 are not connected via the network N, and the management device 10 is desulfurized. It may be configured to be included in the control device 9 of the facility 1.

As described above, the operation control system for a desulfurization facility according to the present invention is suitable for monitoring the activity status of limestone.

1 desulfurization 2 dust collector 2a power supply 3 absorption column 3a limestone feeder 4 inlet side SO ₂ concentration detection unit 5 outlet SO ₂ concentration detector 6 limestone concentration detection unit 7 absorption liquid tank holding amount detecting section 8 pH detector DESCRIPTION OF SYMBOLS 9 Control apparatus 9a Memory | storage part 9b Electric dust collector drive part 9c Limestone feeder drive part 9d Input / output part 9e Information communication part 9f Strong alkaline liquid pump drive part 10 Management apparatus 10a Memory | storage part 10aa Active constant type | formula database 10ab Limestone active constant threshold value database 10ac Limestone concentration / limestone activation constant database 10ad pH / limestone activation constant database 10ae Power supply supply voltage database 10af Limestone feeder supply voltage database 10ag Strong alkaline liquid pump supply voltage database 10b Processing section 10ba Activity constant calculation section 10bb Sexual state determination unit 10bc Deactivation cause determination unit 10c Input / output unit 10d Information communication unit 11 Strong alkaline liquid supply unit 11a Strong alkaline liquid tank 11b Strong alkaline liquid pipe 11c Strong alkaline liquid pump 100a Exhaust gas 100b Dedusted exhaust gas 100c Desulfurized exhaust gas 101 Absorption SO ₂ concentration S3 flue gas flow rate C limestone concentration V absorbing liquid tank stockpile K limestone activity constant of the liquid 102 limestone 103 water 104 gypsum 105 SO ₂ concentration S2 desulfurized flue gas of oxidizing air 106 strongly alkaline solution N-network system S1 dedusting flue gas X Limestone activity constant threshold

Claims

A dust collector for dust collection of the coal ash in the exhaust gas, absorbing the SO 2 in the dedusted flue gas by contacting the absorption liquid in the dedusting flue gas having passed through the electrostatic precipitator to the limestone in the absorbing liquid In an operation control system of a desulfurization facility comprising an absorption tower for discharging desulfurization exhaust gas from which SO 2 has been removed,
The SO 2 concentration in the dedusted exhaust gas, the SO 2 concentration in the desulfurized exhaust gas, the exhaust gas flow rate of the exhaust gas, the limestone concentration of the absorption liquid, and the desorbed exhaust gas in contact with the desorbed exhaust gas are stored. Based on the amount of the absorbent tank held in the absorbent and the pH of the absorbent, the limestone activity constant is calculated, and the limestone activity constant is compared with a preset limestone activity constant threshold. An operation control system for a desulfurization facility, comprising a management device for judging.
The management device determines the cause of deactivation based on the relationship between the limestone concentration and the limestone activity constant and the relationship between the pH and the limestone activity constant when the activity status of limestone is in the inactivation sign The operation control system for a desulfurization facility according to claim 1.
The management device sets the dust collection power of the electric dust collector and / or the supply amount of limestone to the absorption liquid in a mode of rehabilitating the deactivation sign based on the cause leading to deactivation. An operation control system for a desulfurization facility according to claim 2.
Obtaining the SO 2 concentration in the dedusted exhaust gas, the SO 2 concentration in the desulfurized exhaust gas, the exhaust gas flow rate, the limestone concentration, the absorption tank holding amount, and the pH, the electric dust collector, and the A desulfurization facility that collects coal ash in the exhaust gas and removes SO 2 is configured by the control device that controls the supply of limestone to the absorption liquid, the electric dust collector, and the absorption tower.
The desulfurization facility operation control system according to any one of claims 1 to 3, wherein the management device is communicably connected to the control device in the desulfurization facility via a network.
A strong alkaline solution supply unit for supplying a strong alkaline solution to the absorbing solution of the absorption tower;
4. The management device according to claim 1, wherein when the limestone activity constant is less than the limestone activity constant threshold, a supply amount of strong alkaline liquid by the strong alkali liquid supply unit is set. Operation control system for the desulfurization facility described in 1.
The SO 2 concentration in the dedusted exhaust gas, the SO 2 concentration in the desulfurized exhaust gas, the exhaust gas flow rate, the limestone concentration, the absorption liquid tank holding amount, and the pH are obtained, and the electric dust collector, the absorption Limestone is supplied to the liquid, and the controller for controlling the strong alkaline liquid supply unit, the electric dust collector, the absorption tower, and the strong alkaline liquid supply unit collect coal ash in the exhaust gas. And a desulfurization facility for removing SO 2 is configured,
6. The operation control system for a desulfurization facility according to claim 5, wherein the management device is communicably connected to the control device in the desulfurization facility via a network.
The operation control system for a desulfurization facility according to claim 4 or 6, wherein the management device is communicably connected to the control device in a plurality of the desulfurization facilities via a network.