WO2011065119A1 - System for controlling operation of desulfurization apparatus - Google Patents

System for controlling operation of desulfurization apparatus Download PDF

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Publication number
WO2011065119A1
WO2011065119A1 PCT/JP2010/066496 JP2010066496W WO2011065119A1 WO 2011065119 A1 WO2011065119 A1 WO 2011065119A1 JP 2010066496 W JP2010066496 W JP 2010066496W WO 2011065119 A1 WO2011065119 A1 WO 2011065119A1
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WIPO (PCT)
Prior art keywords
exhaust gas
desulfurization
absorption liquid
desulfurization facility
limestone
Prior art date
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PCT/JP2010/066496
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French (fr)
Japanese (ja)
Inventor
直行 神山
伊藤　栄基
筒井　誠
立人 長安
紀和 稲葉
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三菱重工業株式会社
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Application filed by 三菱重工業株式会社 filed Critical 三菱重工業株式会社
Publication of WO2011065119A1 publication Critical patent/WO2011065119A1/en

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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
    • B01D53/1456—Removing acid components
    • B01D53/1481—Removing sulfur dioxide or sulfur trioxide
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
    • B01D53/1412—Controlling the absorption process
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2251/00—Reactants
    • B01D2251/40—Alkaline earth metal or magnesium compounds
    • B01D2251/404—Alkaline earth metal or magnesium compounds of calcium
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
    • Y02A50/00—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE in human health protection, e.g. against extreme weather
    • Y02A50/20—Air quality improvement or preservation, e.g. vehicle emission control or emission reduction by using catalytic converters

Definitions

  • the present invention relates to an operation control system for a desulfurization facility that removes SO 2 contained in exhaust gas.
  • Patent Document 1 discloses a control device that controls a plurality of environmental devices installed to remove a predetermined substance with respect to one exhaust gas system in which the concentration of the predetermined substance contained in the exhaust gas is managed.
  • An environmental device control system including a measuring device that detects a concentration of a predetermined substance is disclosed.
  • 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.
  • an efficient environmental device is selected with reference to the efficiency table, and control is performed so that the environmental device performs processing.
  • the apparatus can be efficiently operated, and energy saving or low operation cost can be achieved.
  • This invention solves the subject mentioned above, and aims at providing the operation control system of the desulfurization equipment which can perform the economical operation according to the market price of various things.
  • this operation control system for desulfurization equipment when the revenue market price is high, the SO 2 removal amount is increased, and conversely, when the income market price is low, control is performed so as to reduce the operation cost of the desulfurization equipment. In this way, it becomes possible to optimize the operating conditions of the desulfurization equipment according to the revenue market price.
  • the desulfurization equipment always uses exhaust gas conditions and SO 2 sales that change from moment to moment, and various unit prices (for example, unit price of electric power, unit price of absorbent material, unit price of water supply, unit price of fuel) that change relatively slowly. It is possible to perform an economical operation that minimizes the cost caused by the operation of the vehicle.
  • the revenue market price is higher than the expenditure market price, so it is also possible to record profits by operating the desulfurization facility.
  • the management device has a predictive evaluation index obtained by subtracting the revenue market price from the expenditure market price for the predetermined period in the past in the absorption tower.
  • the amount of the absorbing liquid to be sent and the supply amount of the material constituting the absorbing liquid are set in advance.
  • the SO 2 removal amount is increased, and conversely, when the past revenue market price is low, the desulfurization facility operation cost is reduced.
  • the manager of the facility can make a prior arrangement for materials such as utilities by planning in advance.
  • SO 2 concentration in the flue gas and acquires the SO 2 concentration in the desulfurized flue gas, delivery of the absorbing liquid to the absorption tower, and the absorbing solution SO 2 in the exhaust gas by a control device that controls the supply of the material to be formed, the absorption tower, the absorption liquid delivery section that sends the absorption liquid to the absorption tower, and the material supply section that supplies the material that forms the absorption liquid.
  • the desulfurization equipment which removes is comprised,
  • the said management apparatus is connected to the said control apparatus in the said desulfurization equipment via a network so that communication is possible.
  • the operation control of the desulfurization equipment can be performed remotely via the network.
  • the management device is connected to the control devices in a plurality of the 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.
  • 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 flowchart showing the operation of the operation control system for the desulfurization facility according to Embodiment 1 of the present invention.
  • FIG. 4 is a block diagram of an operation control system for a desulfurization facility according to Embodiment 2 of the present invention.
  • FIG. 5 is a flowchart showing the operation of the operation control system for the desulfurization facility according to Embodiment 2 of the present invention.
  • FIG. 1 is a schematic diagram of an operation control system for a desulfurization facility according to Embodiment 1.
  • a desulfurization facility 1 includes an absorption tower 3 that removes SO 2 (sulfur dioxide) in an exhaust gas 100 a from a boiler (for example, a coal fired boiler) 2 such as a thermal power plant, a control device 5, It has.
  • SO 2 sulfur dioxide
  • the absorption tower 3 of the desulfurization facility 1 applied to such a flue gas treatment system is configured so that an absorption liquid 101 (hereinafter referred to as an absorption liquid) 101 containing limestone is brought into contact with the supplied exhaust gas 100a to thereby adjust the SO in the exhaust gas 100a. 2 (sulfur dioxide) is absorbed by the limestone in the absorbent 101, and the desulfurized exhaust gas 100b from which SO 2 has been removed is discharged.
  • an absorption liquid 101 hereinafter referred to as an absorption liquid
  • 2 sulfur dioxide
  • 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.
  • water 103 is supplied to the bottom of the absorption tower 3 through a water supply pipe 3b. 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.
  • the absorption liquid 101 stored at the bottom in the absorption tower 3 is pumped by the absorption liquid circulation pump 3 c and supplied to the upper part in the absorption tower 3 through the absorption liquid pipe 3 d outside the absorption tower 3. Then, the absorption liquid 101 comes into contact with the exhaust gas 100a rising in the absorption tower 3 in the process of reaching the lower part in the absorption tower 3 while flowing down from the nozzle 3e provided in the upper part in the absorption tower 3. Thereby, SO 2 contained in the exhaust gas 100a reacts with the limestone 102 of the absorbing liquid 101 (see the following formula 1), and SO 2 is removed from the exhaust gas 100a.
  • the desulfurization exhaust gas 100b from which SO 2 has been removed is discharged from the desulfurization facility 1 through the desulfurization exhaust gas pipe 3f 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. SO 2 + 1 / 2O 2 + CaCO 3 + 2H 2 O ⁇ CaSO 4 .2H 2 O + CO 2 Formula 1
  • a part of the absorbing liquid 101 stored at the bottom in the absorption tower 3 is depressurized via an extraction pipe 3g branched from the absorption liquid pipe 3d outside the absorption tower 3 while being pumped by the absorption liquid circulation pump 3c.
  • the dehydrator 3h 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 a byproduct gypsum 104.
  • 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.
  • the bottom of the absorption tower 3 is supplied with the oxidizing air 105 fed by the oxidation blower 3i. 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.
  • the absorption liquid 101 supplied to the upper part of the absorption tower 3 through the absorption liquid pipe 3d is caused to flow down from the nozzle 3e, thereby contacting the exhaust gas 100a rising in the absorption tower 3.
  • the absorbing liquid is supplied to the middle part of the absorption tower via the absorbing liquid pipe, and the absorbing liquid is ejected upward from the nozzle provided in the middle part of the absorption tower.
  • 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 the exhaust gas rising in the absorption tower.
  • the contact between the absorbing liquid 101 and the exhaust gas 100a is not limited to the above-described countercurrent contact. There is a co-current contact that combines.
  • the exhaust gas blower 2b is provided with an exhaust gas blower power consumption detection unit 4a that detects the power consumption (exhaust gas blower power consumption a).
  • the absorption liquid circulation pump 3c is provided with a circulation pump power consumption detection unit 4b for detecting the power consumption (circulation pump power consumption b).
  • the oxidation blower 3i is provided with an oxidation blower power consumption detection unit 4c that detects its power consumption (oxidation blower power consumption c).
  • the exhaust gas pipe 2a is provided with an inlet side SO 2 concentration detector 4d that detects the SO 2 concentration (inlet side SO 2 concentration d) in the exhaust gas 100a reaching the absorption tower 3.
  • the desulfurization exhaust gas pipe 3f is provided with an outlet side SO 2 concentration detector 4e that detects the SO 2 concentration (exit side SO 2 concentration e) in the desulfurization exhaust gas 100b discharged from the absorption tower 3.
  • the absorption liquid pipe 3d is provided with a limestone concentration detection unit 4f that detects the concentration of limestone 102 in the absorption liquid 101 (limestone concentration f).
  • the exhaust gas pipe 2a has an exhaust gas flow rate detection unit 4g for detecting the flow rate (exhaust gas flow rate g) of the exhaust gas 100a reaching the absorption tower 3 together with the inlet side SO 2 concentration detection unit 4d, and the temperature of the exhaust gas 100a reaching the absorption tower 3
  • An exhaust gas temperature detector 4 h that detects (exhaust gas temperature h) and an exhaust gas moisture concentration detector 4 i that detects the moisture concentration (exhaust gas moisture concentration i) of the exhaust gas 100 a reaching the absorption tower 3 are provided.
  • the boiler 2 is provided with a boiler fuel consumption detection unit 4j that detects the amount of fuel consumed (boiler fuel consumption j).
  • the limestone feeder 3a is provided with a limestone supply amount detection unit 4k that detects the supply amount of limestone 102 (limestone supply amount k).
  • the water supply pipe 3b is provided with a supply water flow rate detection unit 4m that detects the supply amount of the water 103 (supply water flow rate m).
  • the absorbing liquid pipe 3d is provided with an absorbing liquid flow rate detection unit 4n that detects the flow rate of the absorbing liquid 101 (absorbing liquid flow rate n).
  • the control device 5 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 5 is constituted by a microcomputer or the like.
  • the control device 5 is provided with a storage unit 5a.
  • the storage unit 5a includes a RAM, a ROM, and the like, and stores programs and data.
  • the controller 5 supplies a voltage to the feeder motor (not shown) to operate the absorbent circulating pump drive unit 5b for applying a voltage when operating the absorbent circulating pump 3c and the limestone feeder 3a.
  • a limestone feeder drive unit 5c is provided for placing.
  • the control device 5 is provided with an input / output unit 5d.
  • the input / output unit 5d includes a keyboard, a mouse, and a monitor.
  • the management apparatus 6 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 6 is composed of a microcomputer or the like. As shown in FIG. 1, the management device 6 is connected to the control device 5 via the network N, and the exhaust gas blower power consumption a, the circulation pump power consumption b, the oxidation blower power consumption c, the inlet side SO 2 concentration d, Control each data of outlet side SO 2 concentration e, limestone concentration f, exhaust gas flow rate g, exhaust gas temperature h, exhaust gas moisture concentration i, boiler fuel consumption j, limestone supply amount k, supply water flow rate m, and absorption liquid flow rate n. Obtained from the device 5.
  • the management device 6 is provided with a storage unit 6a.
  • the storage unit 6a includes a RAM, a ROM, and the like, and stores programs and data.
  • the storage unit 6a has an evaluation index formula database 6aa, an absorption liquid circulation pump supply voltage database 6ab, and a limestone feeder supply voltage database 6ac.
  • the evaluation index formula database 6aa is obtained from the control device 5, the exhaust gas blower power consumption a, the circulation pump power consumption b, the oxidation blower power consumption c, the inlet side SO 2 concentration d, the outlet side SO 2 concentration e, the limestone concentration f, Formula 2 for calculating the evaluation index E based on each data of the exhaust gas flow rate g, the exhaust gas temperature h, the exhaust gas moisture concentration i, the boiler fuel consumption j, the limestone supply amount k, the supply water flow rate m, and the absorption liquid flow rate n ⁇ Expression 5 is stored.
  • E TMG ... Formula 2
  • T (D ⁇ DP) + (L ⁇ LP) + (W ⁇ WP) + (F ⁇ FP) Equation 3
  • M S ⁇ SP Expression 4
  • G H ⁇ HP ... Formula 5
  • the evaluation index E is calculated from the desulfurization facility operating cost T as the expenditure market price of various expenditures generated according to the operation of the desulfurization facility 1, and the SO 2 as the revenue market price of revenues generated according to the operation of the desulfurization facility 1.
  • the sales amount M and the by-product gypsum sales amount (or by-product gypsum processing cost) G are subtracted.
  • D is the power consumption of the desulfurization facility 1 and is obtained by adding the exhaust gas blower power consumption a, the circulation pump power consumption b, and the oxidation blower power consumption c described above.
  • DP is a power unit price.
  • L is a limestone consumption, those obtained by the following equation 6, the obtained SO 2 removal amount S (the amount of SO 2 removed from the flue gas 100a) by the following equation 7, the limestone purity f ', the absorbing liquid It is calculated
  • LP is limestone unit price (absorbing liquid material unit price).
  • W is the amount of water supplied to the desulfurization facility 1 and is determined from the relationship between the exhaust gas flow rate g, the exhaust gas temperature h, and the exhaust gas moisture concentration i described above.
  • WP is the unit price of water supply.
  • F is a fuel consumption amount in the boiler 2 and corresponds to the above-described boiler fuel consumption amount j.
  • FP is the fuel unit price of the boiler 2.
  • S (inlet side SO 2 concentration d ⁇ outlet side SO 2 concentration e) ⁇ exhaust gas flow rate g / 22.4 ⁇ 10 6
  • the limestone concentration f is the concentration of excess limestone in the absorption liquid 101.
  • H is the amount of byproduct gypsum produced, and is determined from the relationship between the SO 2 removal amount S, the limestone purity f ′, and the limestone concentration f in the absorbing liquid 101.
  • HP is the by-product gypsum sales unit price (or by-product gypsum processing unit price (in the case of by-product gypsum processing unit price, it is a negative value)).
  • the absorption liquid circulation pump supply voltage database 6ab is such that the evaluation index E described above is minimized, that is, the desulfurization facility operating cost T, which is the expenditure market price of various expenditures generated according to the operation of the desulfurization facility 1, is minimized.
  • the absorption liquid circulation pump information for applying a voltage to the absorption liquid circulation pump 3c is stored.
  • the relationship between the absorption liquid delivery amount (absorption liquid flow rate n) by the absorption liquid circulation pump 3c and the power consumption D and SO 2 removal amount S of the desulfurization facility 1 is theoretical or experimental. It is the one requested by
  • the limestone feeder supply voltage database 6ac has the absorption index so that the evaluation index E described above is minimized, that is, the desulfurization facility operating cost T, which is the expenditure market price of various expenditures generated according to the operation of the desulfurization facility 1, is minimized.
  • the desulfurization facility operating cost T which is the expenditure market price of various expenditures generated according to the operation of the desulfurization facility 1, is minimized.
  • feeder voltage information for applying a voltage to a feeder motor (not shown) of the limestone feeder 3a is stored.
  • this feeder voltage information the relationship between the limestone supply amount k and the SO 2 removal amount S by the limestone feeder 3a is obtained in advance by a theoretical formula or an experimental formula.
  • the management device 6 is provided with an expenditure market price information input unit 6b.
  • a power unit price DP, a limestone unit price LP, a supply water unit price WP, and a fuel unit price FP for obtaining the desulfurization facility operating cost T as the expenditure market price are input.
  • the electric power unit price DP, the limestone unit price LP, and the supply water unit price WP are obtained by being automatically input from the Internet or manually by an operator.
  • the management device 6 is provided with a processing unit 6d.
  • the processing unit 6d includes a desulfurization facility operating cost calculation unit 6da, an SO 2 sales calculation unit 6db, a by-product gypsum sales calculation unit (or by-product gypsum processing cost calculation unit) 6dc, an evaluation index calculation unit 6dd, and an absorption liquid delivery amount setting unit. 6de and a limestone supply amount setting unit 6df.
  • the desulfurization facility operating cost calculation unit 6da calculates the desulfurization facility operating cost T from the above equation 3 stored in the evaluation index formula database 6aa of the storage unit 6a. That is, exhaust Gasuburoa power a, circulating pump power consumption b, and obtains the power consumption D of desulfurization 1 by adding the oxidizing blower power consumption c, the exhaust gas subtracts the outlet SO 2 concentration e from the inlet side SO 2 concentration d
  • the limestone consumption L is determined from the SO 2 removal amount S multiplied by the flow rate g, the limestone purity f ′, and the limestone concentration f, and the supply water amount W is determined from the relationship between the exhaust gas flow rate g, the exhaust gas temperature h, and the exhaust gas moisture concentration i.
  • the fuel consumption F is obtained from the boiler fuel consumption j, and the desulfurization facility operating cost T is calculated from the power unit price DP, the limestone unit price LP, the supply water unit price WP, and the fuel unit price FP acquired from the expenditure market price information input unit 6b. .
  • the SO 2 sales amount calculation unit 6db calculates the SO 2 sales amount M from the above formula 4 stored in the evaluation index formula database 6aa of the storage unit 6a. That is, by subtracting the outlet side SO 2 concentration e from the inlet side SO 2 concentration d and multiplying by the exhaust gas flow rate g, the SO 2 removal amount S is obtained, and the SO 2 transaction unit price SP acquired from the revenue market price information input unit 6c 2 Calculate sales M.
  • Byproduct gypsum sales amount calculation unit (or byproduct gypsum processing cost calculation unit) 6dc calculates byproduct gypsum sales amount (byproduct gypsum processing cost) G from the above equation 5 stored in the evaluation index formula database 6aa of the storage unit 6a. To do. That is, the amount of byproduct gypsum produced H is obtained from the SO 2 removal amount S obtained by subtracting the outlet side SO 2 concentration e from the inlet side SO 2 concentration d and multiplied by the exhaust gas flow rate g, the limestone purity f ′, and the limestone concentration f, and further the revenue market.
  • By-product gypsum sales (by-product gypsum processing cost) G is calculated from the by-product gypsum sales unit price (or by-product gypsum processing unit price) HP acquired from the price information input unit 6c.
  • the evaluation index calculation unit 6dd calculates the evaluation index E from the above formula 2 stored in the evaluation index formula database 6aa of the storage unit 6a. That is, the desulfurization equipment operation cost T calculated by desulfurization equipment operation cost calculation unit 6da, SO 2 sales calculator SO 2 sales calculated in 6db M, and by-product gypsum sales calculator (or by-product gypsum processing cost calculation unit)
  • the evaluation index E is calculated from the amount of by-product gypsum sales (cost of by-product gypsum treatment) G calculated at 6 dc.
  • the absorption liquid delivery amount setting unit 6de uses the absorption liquid circulation pump information stored in the absorption liquid circulation pump supply voltage database 6ab of the storage unit 6a to minimize the evaluation index E calculated by the evaluation index calculation unit 6dd.
  • the amount of the absorption liquid 101 to be sent to the absorption tower 3, that is, the voltage applied to the absorption liquid circulation pump 3c is set.
  • the limestone supply amount setting unit 6df absorbs the absorbent 101 so that the evaluation index E calculated by the evaluation index calculation unit 6dd is minimized based on the feeder voltage information stored in the limestone feeder supply voltage database 6ac of the storage unit 6a.
  • the supply amount of the limestone 102 which is the material forming the above, that is, the voltage applied to the feeder motor (not shown) of the limestone feeder 3a is set.
  • the management device 6 is provided with an input / output unit 6e.
  • the input / output unit 6e includes a keyboard, a mouse, and a monitor.
  • the management device 6 is provided with an information communication unit 6f.
  • the information communication unit 6 f is for performing information communication with the information communication unit 5 e of the control device 5. Based on the information input from the control device 5, the management device 6 controls the control device 5 in an integrated manner with respect to the absorbent circulating pump 3c and the limestone feeder 3a in accordance with programs and data stored in advance in the storage unit 6a. To output information.
  • the exhaust gas blower power consumption a As shown in FIG. 3, first, in the control device 5, the exhaust gas blower power consumption a, the circulation pump power consumption b, the oxidation blower power consumption c, the inlet side SO 2 concentration d, the outlet side SO 2 concentration e, the limestone concentration f,
  • Each data of the limestone purity f ′, the exhaust gas flow rate g, the exhaust gas temperature h, the exhaust gas moisture concentration i, the boiler fuel consumption j, the limestone supply amount k, the supply water flow rate m, and the absorption liquid flow rate n is output to the management device 6 ( Step ST1).
  • the management device 6 inputs each of the above data from the control device 5 (step ST2), the desulfurization facility operation cost calculation unit 6da calculates the desulfurization facility operation cost T, and the SO 2 sales calculation unit 6db
  • the SO 2 sales amount M is calculated, the by-product gypsum sales calculating unit (or by-product gypsum processing cost calculating unit) 6dc calculates the by-product gypsum sales amount (by-product gypsum processing cost) G, and the evaluation index calculating unit 6dd evaluates it.
  • An index E is calculated (step ST3).
  • the management device 6 sets the amount of the absorption liquid 101 to be sent to the absorption tower 3 (that is, the voltage applied to the absorption liquid circulation pump 3c) so that the evaluation index E is minimized in the absorption liquid delivery amount setting unit 6de.
  • the limestone supply amount setting unit 6df the supply amount of limestone 102 which is a material constituting the absorbing liquid 101 (that is, a feeder motor (not shown) of the limestone feeder 3a) is added so that the evaluation index E is minimized. Voltage) is set (step ST4).
  • control device 5 while the SO 2 removal amount S within a predetermined range, the set voltage of the absorbent circulating pump 3c in the management apparatus 6, and the voltage of the feeder motor limestone feeder 3a (not shown) Accordingly, the absorption liquid circulation pump 3c and the limestone feeder 3a are driven (step ST5).
  • the amount of the absorbing liquid 101 sent to the absorption tower 3 and the amount of the material (limestone 102) constituting the absorbing liquid 101 are set.
  • the operation control system of this desulfurization facility when the revenue market price (SO 2 sales M, by-product gypsum sales G) is high, the SO 2 removal amount S is increased, and conversely, the revenue market price (SO 2 When the sales amount M and the by-product gypsum sales amount G) are low, the desulfurization equipment operating cost T is controlled to be reduced.
  • the operating conditions of the desulfurization facility 1 can be optimized according to the revenue market price (SO 2 sales M, by-product gypsum sales (by-product gypsum processing cost) G).
  • the management device 6 is connected to the control device 5 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.
  • the management device 6 is communicably connected to the control devices 5 in the plurality of desulfurization facilities 1 via the network N.
  • FIG. 2 shows a form in which the control device 5 and the management device 6 in one desulfurization facility 1 are connected in a one-to-one relationship. However, the control device 5 and the management device 6 in the plurality of desulfurization facilities 1 are connected to each other.
  • the management device 6 When connected in a many-to-one relationship, in the management device 6, corresponding to each control device 5, a storage unit 6a, an expenditure market price information input unit 6b, an income market price information input unit 6c, a processing unit 6d, The input / output unit 6e and the information communication unit 6f function. As a result, the operation control of the plurality of desulfurization facilities 1 can be performed in a remote place.
  • the control device 5 and the management device 6 in the desulfurization facility 1 are connected in a one-to-one relationship, the control device 5 and the management device 6 are not connected via the network N, and the management device 6 is desulfurized. It may be included in the control device 5 of the facility 1.
  • the absorption liquid to absorb SO 2 it has been described desulfurization 1 lime gypsum method of applying the absorption liquid 101 containing limestone 102, not limited thereto.
  • the embodiments described above can be applied to other wet desulfurization facilities such as a water mug method and a caustic soda method.
  • the limestone unit price LP is changed to a magnesium hydroxide unit price or a caustic soda unit price.
  • FIG. 4 is a block diagram of an operation control system for a desulfurization facility according to Embodiment 2 of the present invention.
  • 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. 4 further includes a spending market price information database 6ad and an income market price information database 6ae in the storage unit 6a in the management device 6 as compared with the first embodiment described above.
  • the expenditure market price information database 6ad is a unit price of electricity DP, a unit price of limestone LP, a unit price of supply water WP, and a unit price of fuel FP as the expenditure market price input to the expenditure market price information input unit 6b.
  • the revenue market price information database 6ae stores the SO 2 transaction unit price SP for obtaining the SO 2 sales amount M as the revenue market price input to the revenue market price information input unit 6c, and by-product gypsum sales (or by-product gypsum processing costs). ) Store by-product gypsum sales unit price (or by-product gypsum processing unit price) HP for obtaining G.
  • the management device 6 calculates the predicted evaluation index Ea by subtracting the income market price from the acquired expenditure market price in the evaluation index calculation unit 6dd (step ST12).
  • the calculation of the predicted evaluation index Ea is the same as the evaluation index E of the first embodiment described above.
  • the management device 6 sends the absorption liquid 101 sent to the absorption tower 3 (that is, the voltage applied to the absorption liquid circulation pump 3c) so that the predicted evaluation index Ea is minimized in the absorption liquid delivery quantity setting unit 6de.
  • the limestone supply amount setting unit 6df the supply amount of limestone 102 that is the material constituting the absorbent 101 (that is, a feeder motor (not shown) of the limestone feeder 3a) so that the predicted evaluation index Ea is minimized. Is set (step ST13).
  • control device 5 while the SO 2 removal amount S within a predetermined range, the set voltage of the absorbent circulating pump 3c in the management apparatus 6, and the voltage of the feeder motor limestone feeder 3a (not shown) Accordingly, the absorption liquid circulation pump 3c and the limestone feeder 3a are driven (step ST14).
  • the revenue market price (SO 2 sales M, by-product gypsum sales (The amount of absorption liquid 101 sent to the absorption tower 3 and the supply amount of the material (limestone 102) constituting the absorption liquid 101 are set in such a manner that the predicted evaluation index Ea obtained by subtracting the byproduct gypsum processing cost G) is minimized. .
  • the SO 2 removal amount S is increased, and conversely the past revenue market.
  • the desulfurization equipment operating cost T is set to be low.
  • the manager of the facility can make a prior arrangement for materials such as utilities (for example, limestone 102) by planning in advance.
  • the predicted evaluation index Ea can be corrected by the evaluation index E of the first embodiment described above.
  • the management device 6 is connected to the control device 5 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.
  • the operation control of the plurality of desulfurization facilities 1 can be performed in a remote place.
  • the control device 5 and the management device 6 in the desulfurization facility 1 are connected in a one-to-one relationship, the control device 5 and the management device 6 are not connected via the network N, and the management device 6 is desulfurized. It may be included in the control device 5 of the facility 1.
  • the operation control system for a desulfurization facility according to the present invention is suitable for performing economical operation in accordance with various market prices.

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Abstract

A system for controlling the operation of a desulfurization apparatus equipped with an absorption column for bringing an exhaust gas into contact with an absorbing liquid so as to allow the absorbing liquid to absorb SO2 in the exhaust gas while discharging the desulfurized exhaust gas from which SO2 has been removed, which is further provided with a management unit for, while regulating the amount of SO2 removed from the exhaust gas within a definite range, setting the feeding rate of the absorbing liquid to the absorption column and the feeding rate of a material constituting the absorbing liquid in such a manner that an evaluation index (E), which is calculated by subtracting the income market price of income items arising from the operation of the desulfurization apparatus from the expenditure market price of expenditure items arising from the operation of the desulfurization apparatus, is minimized.

Description

脱硫設備の運転制御システムOperation control system for desulfurization equipment
　本発明は、排ガスに含まれるＳＯ２を除去する脱硫設備の運転制御システムに関する。 The present invention relates to an operation control system for a desulfurization facility that removes SO 2 contained in exhaust gas.
　従来、特許文献１には、排ガスに含まれる所定の物質の濃度が管理されている一の排ガス系統に対し、所定の物質を除去するために設置される複数の環境装置を制御する制御装置と、所定の物質の濃度を検出する測定器とを備えた環境装置制御システムが開示されている。この環境装置制御システムでは、制御装置は、複数の環境装置ごとに所定の物質の除去能力に対する所定の要素の効率情報を含む効率テーブルを記憶し、測定部は、検出した所定の物質の濃度を含む情報を制御装置に送信し、さらに制御装置は、測定部から受信した所定の物質の濃度と、所定の物質の濃度の目標値とから、物質の濃度を変更するための変更量を決定し、効率テーブルを参照して効率のよい環境装置を選択し、当該環境装置で処理するように制御する。この制御システムによれば、装置を効率よく運転し、省エネルギー、または低運転コストを図ることができる。 Conventionally, Patent Document 1 discloses a control device that controls a plurality of environmental devices installed to remove a predetermined substance with respect to one exhaust gas system in which the concentration of the predetermined substance contained in the exhaust gas is managed. An environmental device control system including a measuring device that detects a concentration of a predetermined substance is disclosed. 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. According to this control system, the apparatus can be efficiently operated, and energy saving or low operation cost can be achieved.
特開２００４－３７０５６号公報JP 2004-37056 A
　ところで、近年では、ＳＯ２排出権の取引市場が活発化している。このため、単にＳＯ２排出規制値を達成する運転のみではなく、ＳＯ２排出権の変動に応じた経済的運転が望まれている。例えば、ＳＯ２排出権の市場価格が下がった場合には排出規制値より余剰にＳＯ２を除去することで余剰分を市場で販売し、逆にＳＯ２排出権の市場価格が上がった場合には排出規制値を超える運転を行い、不足分を購入することが考えられる。さらに、ＳＯ２排出権の他、例えば、ＳＯ２を吸収する吸収液や、ポンプなどを稼動するための電力料も市場価格が経時変化することから、経済的運転の最適条件は常に変動する。 By the way, in recent years, the trading market for SO 2 emission rights has become active. For this reason, not only an operation that achieves the SO 2 emission regulation value but also an economical operation that responds to fluctuations in the SO 2 emission right is desired. For example, when the market price of SO 2 emission rights falls, the excess is sold in the market by removing SO 2 more than the emission regulation value, and conversely when the market price of SO 2 emission rights rises Can operate above the emission limit and purchase the shortage. Furthermore, in addition to the SO 2 emission rights, for example, the absorbing liquid that absorbs SO 2 , and the power charges for operating the pump, etc., change the market price over time, so the optimal conditions for economic operation always fluctuate.
　本発明は上述した課題を解決するものであり、諸事の市場価格に応じた経済的運転を行うことのできる脱硫設備の運転制御システムを提供することを目的とする。 This invention solves the subject mentioned above, and aims at providing the operation control system of the desulfurization equipment which can perform the economical operation according to the market price of various things.
　上述の目的を達成するために、本発明の脱硫設備の運転制御システムでは、排ガスに吸収液を接触させることで前記排ガス中のＳＯ２を前記吸収液に吸収させつつＳＯ２が除去された脱硫排ガスを排出する吸収塔を備える脱硫設備の運転制御システムにおいて、前記排ガスからＳＯ２を除去したＳＯ２除去量を所定範囲内としつつ、脱硫設備の運転に応じて生じる支出諸事の支出市場価格から脱硫設備の運転に応じて生じる収入諸事の収入市場価格を差し引いた評価指数が最小となる態様で、前記吸収塔に送る吸収液の送出量、および前記吸収液を成す材料の供給量を設定する管理装置を備えたことを特徴とする。 To achieve the above object, in desulfurization operation control system of the present invention, while absorbing the SO 2 in the flue gas by contacting the absorption liquid to the exhaust gas in the absorption liquid SO 2 has been removed desulfurized In the operation control system of a desulfurization facility provided with an absorption tower for discharging exhaust gas, from the expenditure market price of various expenditures generated in accordance with the operation of the desulfurization facility while the SO 2 removal amount obtained by removing SO 2 from the exhaust gas is within a predetermined range In a mode in which the evaluation index obtained by subtracting the revenue market price of revenues generated in accordance with the operation of the desulfurization facility is minimized, the amount of the absorption liquid sent to the absorption tower and the supply amount of the material constituting the absorption liquid are set. A management device is provided.
　この脱硫設備の運転制御システムによれば、収入市場価格が高い場合は、ＳＯ２除去量を増加させ、逆に、収入市場価格が低い場合は、脱硫設備運転費を少なくするように制御する。このように、収入市場価格に応じて脱硫設備の運転条件を最適化することが可能になる。この結果、刻々と変化する排ガス条件やＳＯ２販売高、および比較的緩やかに変動する各種単価（例えば、電力単価、吸収液材料単価、供給水単価、燃料単価）の各データにより、常に脱硫設備の運転に応じて生じる費用が最小となる経済的運転を行うことが可能になる。しかも、条件によっては、収入市場価格が支出市場価格よりも多くなるので、脱硫設備の運転により利益計上を図ることも可能である。 According to this operation control system for desulfurization equipment, when the revenue market price is high, the SO 2 removal amount is increased, and conversely, when the income market price is low, control is performed so as to reduce the operation cost of the desulfurization equipment. In this way, it becomes possible to optimize the operating conditions of the desulfurization equipment according to the revenue market price. As a result, the desulfurization equipment always uses exhaust gas conditions and SO 2 sales that change from moment to moment, and various unit prices (for example, unit price of electric power, unit price of absorbent material, unit price of water supply, unit price of fuel) that change relatively slowly. It is possible to perform an economical operation that minimizes the cost caused by the operation of the vehicle. In addition, depending on the conditions, the revenue market price is higher than the expenditure market price, so it is also possible to record profits by operating the desulfurization facility.
　また、本発明の脱硫設備の運転制御システムでは、前記管理装置は、過去の所定期間について、前記支出市場価格から前記収入市場価格を差し引いた予測評価指数が最小となる態様で、前記吸収塔に送る吸収液の送出量、および前記吸収液を成す材料の供給量を予め設定することを特徴とする。 Further, in the operation control system for a desulfurization facility of the present invention, the management device has a predictive evaluation index obtained by subtracting the revenue market price from the expenditure market price for the predetermined period in the past in the absorption tower. The amount of the absorbing liquid to be sent and the supply amount of the material constituting the absorbing liquid are set in advance.
　この脱硫設備の運転制御システムによれば、過去の収入市場価格が高い場合は、ＳＯ２除去量を増加させ、逆に、過去の収入市場価格が低い場合は、脱硫設備運転費を少なくするように設定する。このように、過去の収入市場価格に応じて最適な脱硫設備の運転条件を予測することが可能になる。この結果、設備の管理者は、予め計画してユーティリティーなどの材料の先行手配を行うことが可能になる。 According to the operation control system of the desulfurization facility, when the past revenue market price is high, the SO 2 removal amount is increased, and conversely, when the past revenue market price is low, the desulfurization facility operation cost is reduced. Set to. In this way, it is possible to predict the optimum operating conditions of the desulfurization facility according to the past revenue market price. As a result, the manager of the facility can make a prior arrangement for materials such as utilities by planning in advance.
　また、本発明の脱硫設備の運転制御システムでは、前記排ガス中のＳＯ２濃度、および前記脱硫排ガス中のＳＯ２濃度を取得すると共に、前記吸収塔への吸収液の送出、および前記吸収液を成す材料の供給を制御する制御装置と、前記吸収塔と、前記吸収塔に吸収液を送る吸収液送出部と、前記吸収液を成す材料を供給する材料供給部とにより、排ガス中のＳＯ２を除去する脱硫設備が構成され、前記管理装置は、ネットワーク上を介して前記脱硫設備における前記制御装置と通信可能に接続されていることを特徴とする。 Further, in desulfurization operation control system of the present invention, SO 2 concentration in the flue gas, and acquires the SO 2 concentration in the desulfurized flue gas, delivery of the absorbing liquid to the absorption tower, and the absorbing solution SO 2 in the exhaust gas by a control device that controls the supply of the material to be formed, the absorption tower, the absorption liquid delivery section that sends the absorption liquid to the absorption tower, and the material supply section that supplies the material that forms the absorption liquid. The desulfurization equipment which removes is comprised, The said management apparatus is connected to the said control apparatus in the said desulfurization equipment via a network so that communication is possible.
　この脱硫設備の運転制御システムによれば、ネットワーク上を介して脱硫設備の運転制御を遠隔地にて行える。 According to this desulfurization equipment operation control system, the operation control of the desulfurization equipment can be performed remotely via the network.
　また、本発明の脱硫設備の運転制御システムでは、前記管理装置は、ネットワーク上を介して複数の前記脱硫設備における前記制御装置と通信可能に接続されていることを特徴とする。 In the operation control system for a desulfurization facility of the present invention, the management device is connected to the control devices in a plurality of the desulfurization facilities via a network so as to be communicable.
　この脱硫設備の運転制御システムによれば、ネットワーク上を介して複数の脱硫設備の運転制御を遠隔地にて統括して行うことが可能になる。 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.
　本発明によれば、諸事の市場価格に応じた経済的運転を行うことができる。 According to the present invention, economical operation according to the market price of various things can be performed.
図１は、本発明の実施の形態１に係る脱硫設備の運転制御システムの概略図である。FIG. 1 is a schematic diagram of an operation control system for a desulfurization facility according to Embodiment 1 of the present invention. 図２は、本発明の実施の形態１に係る脱硫設備の運転制御システムのブロック図である。FIG. 2 is a block diagram of the operation control system for the desulfurization facility according to Embodiment 1 of the present invention. 図３は、本発明の実施の形態１に係る脱硫設備の運転制御システムの動作を示すフローチャートである。FIG. 3 is a flowchart showing the operation of the operation control system for the desulfurization facility according to Embodiment 1 of the present invention. 図４は、本発明の実施の形態２に係る脱硫設備の運転制御システムのブロック図である。FIG. 4 is a block diagram of an operation control system for a desulfurization facility according to Embodiment 2 of the present invention. 図５は、本発明の実施の形態２に係る脱硫設備の運転制御システムの動作を示すフローチャートである。FIG. 5 is a flowchart showing the operation of the operation control system for the desulfurization facility according to Embodiment 2 of the present invention.
　以下に、本発明に係る実施の形態を図面に基づいて詳細に説明する。なお、この実施の形態によりこの発明が限定されるものではない。また、下記実施の形態における構成要素には、当業者が置換可能かつ容易なもの、あるいは実質的に同一のものが含まれる。 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.
［実施の形態１］
　本実施の形態について、図面を参照して説明する。図１は、実施の形態１に係る脱硫設備の運転制御システムの概略図である。図１に示すように、脱硫設備１は、火力発電所などのボイラ（例えば、石炭焚ボイラ）２からの排ガス１００ａ中のＳＯ２（二酸化硫黄）を除去する吸収塔３と、制御装置５とを備えている。 [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 absorption tower 3 that removes SO 2 (sulfur dioxide) in an exhaust gas 100 a from a boiler (for example, a coal fired boiler) 2 such as a thermal power plant, a control device 5, It has.
　ボイラ２から排出される排ガス１００ａは、排ガス管２ａに介装された排ガスブロア２ｂにより圧送されつつ吸収塔３に供給される。なお、本実施の形態における脱硫設備１を含む排煙処理システムでは、図には明示しないが、ボイラ２から排出される排ガス１００ａは、吸収塔３に至る前に、脱硝設備によりＮＯｘ（窒素酸化物）を除去され、さらに集塵器（例えば電気集塵器）により燃焼灰を除去される。さらに、本実施の形態における脱硫設備１によりＳＯ２を除去された脱硫排ガス１００ｂは、ＣＯ２（二酸化炭素）回収設備によりＣＯ２を除去される。 The exhaust gas 100a discharged from the boiler 2 is supplied to the absorption tower 3 while being pumped by the exhaust gas blower 2b interposed in the exhaust gas pipe 2a. In the exhaust gas treatment system including the desulfurization facility 1 according to the present embodiment, the exhaust gas 100a discharged from the boiler 2 is treated with NOx (nitrogen oxidation) by the denitration facility before reaching the absorption tower 3, although not clearly shown in the figure. The combustion ash is removed by a dust collector (for example, an electrostatic dust collector). Further, desulfurized flue gas 100b of the FGD 1 of the present embodiment is removed SO 2 is removed CO 2 by CO 2 (carbon dioxide) recovery equipment.
　このような排煙処理システムに適用される脱硫設備１の吸収塔３は、供給された排ガス１００ａに、石灰石を含む吸収液（以下、吸収液という）１０１を接触させることで排ガス１００ａ中のＳＯ２（二酸化硫黄）を吸収液１０１中の石灰石に吸収させ、これによりＳＯ２が除去された脱硫排ガス１００ｂを排出する。 The absorption tower 3 of the desulfurization facility 1 applied to such a flue gas treatment system is configured so that an absorption liquid 101 (hereinafter referred to as an absorption liquid) 101 containing limestone is brought into contact with the supplied exhaust gas 100a to thereby adjust the SO in the exhaust gas 100a. 2 (sulfur dioxide) is absorbed by the limestone in the absorbent 101, and the desulfurized exhaust gas 100b from which SO 2 has been removed is discharged.
　吸収塔３は、その底部に吸収液１０１が貯留されている。吸収塔３の外部には、石灰石フィーダ３ａが設けられ、この石灰石フィーダ３ａにより石灰石１０２が計量されつつ吸収塔３内の底部に供給される。また、吸収塔３内の底部には、給水管３ｂを介して水１０３が供給される。すなわち、吸収塔３内の底部に供給された石灰石１０２と水１０３とで吸収液１０１が生成される。 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 through a water supply pipe 3b. 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.
　吸収塔３内の底部に貯留された吸収液１０１は、吸収液循環ポンプ３ｃにより圧送され吸収塔３の外部の吸収液管３ｄを経て吸収塔３内の上部に供給される。そして、吸収液１０１は、吸収塔３内の上部に設けられたノズル３ｅから流下されつつ、吸収塔３内の下部に至る過程で、吸収塔３内を上昇する排ガス１００ａと接触する。これにより、排ガス１００ａに含まれるＳＯ２が吸収液１０１の石灰石１０２と反応し（下記式１参照）、排ガス１００ａからＳＯ２が除去されることになる。そして、ＳＯ２が除去された脱硫排ガス１００ｂは、吸収塔３の頂部に接続された脱硫排ガス管３ｆを介して脱硫設備１から排出される。また、ＳＯ２の除去に用いられた吸収液１０１は、吸収塔３内の底部に貯留される。
　ＳＯ２＋１／２Ｏ２＋ＣａＣＯ３＋２Ｈ２Ｏ→ＣａＳＯ４・２Ｈ２Ｏ＋ＣＯ２・・・式１ The absorption liquid 101 stored at the bottom in the absorption tower 3 is pumped by the absorption liquid circulation pump 3 c and supplied to the upper part in the absorption tower 3 through the absorption liquid pipe 3 d outside the absorption tower 3. Then, the absorption liquid 101 comes into contact with the exhaust gas 100a rising in the absorption tower 3 in the process of reaching the lower part in the absorption tower 3 while flowing down from the nozzle 3e provided in the upper part in the absorption tower 3. Thereby, SO 2 contained in the exhaust gas 100a reacts with the limestone 102 of the absorbing liquid 101 (see the following formula 1), and SO 2 is removed from the exhaust gas 100a. Then, the desulfurization exhaust gas 100b from which SO 2 has been removed is discharged from the desulfurization facility 1 through the desulfurization exhaust gas pipe 3f 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.
SO 2 + 1 / 2O 2 + CaCO 3 + 2H 2 O → CaSO 4 .2H 2 O + CO 2 Formula 1
　また、吸収塔３内の底部に貯留された吸収液１０１の一部は、吸収液循環ポンプ３ｃにより圧送されつつ吸収塔３の外部の吸収液管３ｄから分岐した抜出管３ｇを経て脱水器３ｈに送られる。脱水器３ｈは、例えば、ベルトフィルタで構成され、当該ベルトフィルタで搬送される過程で吸収液１０１を脱水処理し、副生石膏１０４として系外に排出される。また、吸収液１０１を脱水したろ過液は、本実施の形態では吸収塔３の底部に供給される水１０３として利用される。 Further, a part of the absorbing liquid 101 stored at the bottom in the absorption tower 3 is depressurized via an extraction pipe 3g branched from the absorption liquid pipe 3d outside the absorption tower 3 while being pumped by the absorption liquid circulation pump 3c. Sent to 3h. The dehydrator 3h 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 a byproduct 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.
　吸収塔３内の底部には、酸化ブロア３ｉにより圧送された酸化用空気１０５が供給される。このため、吸収液１０１に酸化用空気１０５が含まれることで吸収液１０１の酸化が促進されるので、ＳＯ２の除去効率を向上できる。 The bottom of the absorption tower 3 is supplied with the oxidizing air 105 fed by the oxidation blower 3i. 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.
　なお、上述した吸収塔３では、吸収液管３ｄを経て吸収塔３内の上部に供給された吸収液１０１を、ノズル３ｅから流下させることで、吸収塔３内を上昇する排ガス１００ａと接触させているが、この限りではない。例えば、図には明示しないが、吸収液管を経て吸収塔内の中部に吸収液を供給し、吸収塔内の中部に設けられたノズルから吸収液を吸収塔内の上方に噴出させる。これにより、吸収液は、吸収塔内の上部で分散しつつ微細な液滴となって吸収塔内を降下し、吸収塔内を上昇する排ガスと接触する。この結果、より大きな気液接触面積を確保して気液接触効率を向上するので、ＳＯ２の除去効率を向上できる。なお、吸収液１０１と排ガス１００ａとの接触には、上述した向流接触の他、流下する吸収液１０１に対して排ガス１００ａが並行して流される並流接触や、並流接触と向流接触とを組み合わせた並向流接触がある。 In the absorption tower 3 described above, the absorption liquid 101 supplied to the upper part of the absorption tower 3 through the absorption liquid pipe 3d is caused to flow down from the nozzle 3e, thereby contacting the exhaust gas 100a rising in the absorption tower 3. This is not the case. For example, although not shown in the figure, the absorbing liquid is supplied to the middle part of the absorption tower via the absorbing liquid pipe, and the absorbing 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 the 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. In addition to the countercurrent contact described above, the contact between the absorbing liquid 101 and the exhaust gas 100a is not limited to the above-described countercurrent contact. There is a co-current contact that combines.
　上述した脱硫設備１において、図１に示すように、排ガスブロア２ｂには、その消費電力（排ガスブロア消費電力ａ）を検出する排ガスブロア消費電力検出部４ａが設けられている。また、吸収液循環ポンプ３ｃには、その消費電力（循環ポンプ消費電力ｂ）を検出する循環ポンプ消費電力検出部４ｂが設けられている。また、酸化ブロア３ｉには、その消費電力（酸化ブロア消費電力ｃ）を検出する酸化ブロア消費電力検出部４ｃが設けられている。また、排ガス管２ａには、吸収塔３に至る排ガス１００ａ中のＳＯ２濃度（入口側ＳＯ２濃度ｄ）を検出する入口側ＳＯ２濃度検出部４ｄが設けられている。また、脱硫排ガス管３ｆには、吸収塔３から排出される脱硫排ガス１００ｂ中のＳＯ２濃度（出口側ＳＯ２濃度ｅ）を検出する出口側ＳＯ２濃度検出部４ｅが設けられている。また、吸収液管３ｄには、吸収液１０１中の石灰石１０２の濃度（石灰石濃度ｆ）を検出する石灰石濃度検出部４ｆが設けられている。また、排ガス管２ａには、入口側ＳＯ２濃度検出部４ｄと共に、吸収塔３に至る排ガス１００ａの流量（排ガス流量ｇ）を検出する排ガス流量検出部４ｇ、吸収塔３に至る排ガス１００ａの温度（排ガス温度ｈ）を検出する排ガス温度検出部４ｈ、および吸収塔３に至る排ガス１００ａの水分濃度（排ガス水分濃度ｉ）を検出する排ガス水分濃度検出部４ｉが設けられている。また、ボイラ２には、その消費する燃料の量（ボイラ燃料消費量ｊ）を検出するボイラ燃料消費量検出部４ｊが設けられている。また、石灰石フィーダ３ａには、石灰石１０２の供給量（石灰石供給量ｋ）を検出する石灰石供給量検出部４ｋが設けられている。また、給水管３ｂには、水１０３の供給量（供給水流量ｍ）を検出する供給水流量検出部４ｍが設けられている。また、吸収液管３ｄには、吸収液１０１の流量（吸収液流量ｎ）を検出する吸収液流量検出部４ｎが設けられている。 In the desulfurization facility 1 described above, as shown in FIG. 1, the exhaust gas blower 2b is provided with an exhaust gas blower power consumption detection unit 4a that detects the power consumption (exhaust gas blower power consumption a). Further, the absorption liquid circulation pump 3c is provided with a circulation pump power consumption detection unit 4b for detecting the power consumption (circulation pump power consumption b). The oxidation blower 3i is provided with an oxidation blower power consumption detection unit 4c that detects its power consumption (oxidation blower power consumption c). Further, the exhaust gas pipe 2a is provided with an inlet side SO 2 concentration detector 4d that detects the SO 2 concentration (inlet side SO 2 concentration d) in the exhaust gas 100a reaching the absorption tower 3. The desulfurization exhaust gas pipe 3f is provided with an outlet side SO 2 concentration detector 4e that detects the SO 2 concentration (exit side SO 2 concentration e) in the desulfurization exhaust gas 100b discharged from the absorption tower 3. The absorption liquid pipe 3d is provided with a limestone concentration detection unit 4f that detects the concentration of limestone 102 in the absorption liquid 101 (limestone concentration f). In addition, the exhaust gas pipe 2a has an exhaust gas flow rate detection unit 4g for detecting the flow rate (exhaust gas flow rate g) of the exhaust gas 100a reaching the absorption tower 3 together with the inlet side SO 2 concentration detection unit 4d, and the temperature of the exhaust gas 100a reaching the absorption tower 3 An exhaust gas temperature detector 4 h that detects (exhaust gas temperature h) and an exhaust gas moisture concentration detector 4 i that detects the moisture concentration (exhaust gas moisture concentration i) of the exhaust gas 100 a reaching the absorption tower 3 are provided. Further, the boiler 2 is provided with a boiler fuel consumption detection unit 4j that detects the amount of fuel consumed (boiler fuel consumption j). The limestone feeder 3a is provided with a limestone supply amount detection unit 4k that detects the supply amount of limestone 102 (limestone supply amount k). The water supply pipe 3b is provided with a supply water flow rate detection unit 4m that detects the supply amount of the water 103 (supply water flow rate m). Further, the absorbing liquid pipe 3d is provided with an absorbing liquid flow rate detection unit 4n that detects the flow rate of the absorbing liquid 101 (absorbing liquid flow rate n).
　そして、これら排ガスブロア消費電力ａ、循環ポンプ消費電力ｂ、酸化ブロア消費電力ｃ、入口側ＳＯ２濃度ｄ、出口側ＳＯ２濃度ｅ、石灰石濃度ｆ、排ガス流量ｇ、排ガス温度ｈ、排ガス水分濃度ｉ、ボイラ燃料消費量ｊ、石灰石供給量ｋ、供給水流量ｍ、および吸収液流量ｎの各データは、制御装置５に入力される。 And these exhaust gas blower power consumption a, circulation pump power consumption b, oxidation blower power consumption c, inlet side SO 2 concentration d, outlet side SO 2 concentration e, limestone concentration f, exhaust gas flow rate g, exhaust gas temperature h, exhaust gas moisture concentration Each data of i, boiler fuel consumption j, limestone supply amount k, supply water flow rate m, and absorption liquid flow rate n is input to the control device 5.
　制御装置５について、図２の実施の形態１に係る脱硫設備の運転制御システムのブロック図を参照して説明する。制御装置５は、マイコンなどで構成されている。制御装置５には、記憶部５ａが設けられている。記憶部５ａは、ＲＡＭやＲＯＭなどから構成され、プログラムやデータが格納されている。また、制御装置５には、吸収液循環ポンプ３ｃを稼動するうえで電圧をかけるための吸収液循環ポンプ駆動部５ｂや、石灰石フィーダ３ａを稼動するうえでフィーダモータ（図示せず）に電圧をかけるための石灰石フィーダ駆動部５ｃが設けられている。また、制御装置５には、入出力部５ｄが設けられている。入出力部５ｄは、キーボードやマウスやモニターで構成されている。また、制御装置５には、情報通信部５ｅが設けられている。情報通信部５ｅは、管理装置６の情報通信部６ｆとの間で情報通信を行うためのものである。この制御装置５は、管理装置６から入力された情報に基づき、記憶部５ａに予め格納されたプログラムやデータに従って、吸収液循環ポンプ３ｃおよび石灰石フィーダ３ａを統括的に制御する。 The control device 5 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 5 is constituted by a microcomputer or the like. The control device 5 is provided with a storage unit 5a. The storage unit 5a includes a RAM, a ROM, and the like, and stores programs and data. In addition, the controller 5 supplies a voltage to the feeder motor (not shown) to operate the absorbent circulating pump drive unit 5b for applying a voltage when operating the absorbent circulating pump 3c and the limestone feeder 3a. A limestone feeder drive unit 5c is provided for placing. The control device 5 is provided with an input / output unit 5d. The input / output unit 5d includes a keyboard, a mouse, and a monitor. The control device 5 is provided with an information communication unit 5e. The information communication unit 5 e is for performing information communication with the information communication unit 6 f of the management device 6. The control device 5 comprehensively controls the absorption liquid circulation pump 3c and the limestone feeder 3a according to programs and data stored in advance in the storage unit 5a based on information input from the management device 6.
　管理装置６について、図２の実施の形態１に係る脱硫設備の運転制御システムのブロック図を参照して説明する。管理装置６は、マイコンなどで構成されている。管理装置６は、図１に示すように、制御装置５とネットワークＮ上を介して接続され、排ガスブロア消費電力ａ、循環ポンプ消費電力ｂ、酸化ブロア消費電力ｃ、入口側ＳＯ２濃度ｄ、出口側ＳＯ２濃度ｅ、石灰石濃度ｆ、排ガス流量ｇ、排ガス温度ｈ、排ガス水分濃度ｉ、ボイラ燃料消費量ｊ、石灰石供給量ｋ、供給水流量ｍ、および吸収液流量ｎの各データを制御装置５から取得する。 The management apparatus 6 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 6 is composed of a microcomputer or the like. As shown in FIG. 1, the management device 6 is connected to the control device 5 via the network N, and the exhaust gas blower power consumption a, the circulation pump power consumption b, the oxidation blower power consumption c, the inlet side SO 2 concentration d, Control each data of outlet side SO 2 concentration e, limestone concentration f, exhaust gas flow rate g, exhaust gas temperature h, exhaust gas moisture concentration i, boiler fuel consumption j, limestone supply amount k, supply water flow rate m, and absorption liquid flow rate n. Obtained from the device 5.
　管理装置６には、記憶部６ａが設けられている。記憶部６ａは、ＲＡＭやＲＯＭなどから構成され、プログラムやデータが格納されている。記憶部６ａは、評価指数式データベース６ａａ、吸収液循環ポンプ供給電圧データベース６ａｂ、および石灰石フィーダ供給電圧データベース６ａｃを有している。 The management device 6 is provided with a storage unit 6a. The storage unit 6a includes a RAM, a ROM, and the like, and stores programs and data. The storage unit 6a has an evaluation index formula database 6aa, an absorption liquid circulation pump supply voltage database 6ab, and a limestone feeder supply voltage database 6ac.
　評価指数式データベース６ａａは、制御装置５から取得した、排ガスブロア消費電力ａ、循環ポンプ消費電力ｂ、酸化ブロア消費電力ｃ、入口側ＳＯ２濃度ｄ、出口側ＳＯ２濃度ｅ、石灰石濃度ｆ、排ガス流量ｇ、排ガス温度ｈ、排ガス水分濃度ｉ、ボイラ燃料消費量ｊ、石灰石供給量ｋ、供給水流量ｍ、および吸収液流量ｎの各データに基づき評価指数Ｅを算出するための下記式２～式５が格納されている。
　Ｅ＝Ｔ－Ｍ－Ｇ・・・式２
　Ｔ＝（Ｄ×ＤＰ）＋（Ｌ×ＬＰ）＋（Ｗ×ＷＰ）＋（Ｆ×ＦＰ）・・・式３
　Ｍ＝Ｓ×ＳＰ・・・式４
　Ｇ＝Ｈ×ＨＰ・・・式５ The evaluation index formula database 6aa is obtained from the control device 5, the exhaust gas blower power consumption a, the circulation pump power consumption b, the oxidation blower power consumption c, the inlet side SO 2 concentration d, the outlet side SO 2 concentration e, the limestone concentration f, Formula 2 for calculating the evaluation index E based on each data of the exhaust gas flow rate g, the exhaust gas temperature h, the exhaust gas moisture concentration i, the boiler fuel consumption j, the limestone supply amount k, the supply water flow rate m, and the absorption liquid flow rate n ~ Expression 5 is stored.
E = TMG ... Formula 2
T = (D × DP) + (L × LP) + (W × WP) + (F × FP) Equation 3
M = S × SP Expression 4
G = H × HP ... Formula 5
　上記式２において、Ｔは、脱硫設備１の運転に応じて生じる支出諸事の支出市場価格としての脱硫設備運転費であり、上記式３により求められる。また、上記式２において、Ｍは、脱硫設備１の運転に応じて生じる収入諸事の収入市場価格としてのＳＯ２販売高（ＳＯ２排出権）であり、上記式４により求められる。また、上記式２において、Ｇは、脱硫設備１の運転に応じて生じる収入諸事の収入市場価格としての副生石膏販売高または副生石膏処理費用（なお、副生石膏処理費用の場合はマイナス数値とする）であり、上記式５により求められる。すなわち、評価指数Ｅは、脱硫設備１の運転に応じて生じる支出諸事の支出市場価格としての脱硫設備運転費Ｔから、脱硫設備１の運転に応じて生じる収入諸事の収入市場価格としてのＳＯ２販売高Ｍ、および副生石膏販売高（または副生石膏処理費用）Ｇを差し引いたものである。 In the above equation 2, T is a desulfurization facility operating cost as an expenditure market price of various expenditures generated in accordance with the operation of the desulfurization facility 1, and is obtained by the above equation 3. Further, in the above formula 2, M is the SO 2 sales amount (SO 2 emission right) as the revenue market price of revenues generated in accordance with the operation of the desulfurization facility 1, and is obtained by the above formula 4. In the above formula 2, G is a by-product gypsum sales amount or a by-product gypsum processing cost as a revenue market price of revenues generated according to the operation of the desulfurization facility 1 (in the case of a by-product gypsum processing cost, it is a negative value) ) And is obtained by the above equation 5. That is, the evaluation index E is calculated from the desulfurization facility operating cost T as the expenditure market price of various expenditures generated according to the operation of the desulfurization facility 1, and the SO 2 as the revenue market price of revenues generated according to the operation of the desulfurization facility 1. The sales amount M and the by-product gypsum sales amount (or by-product gypsum processing cost) G are subtracted.
　上記式３において、Ｄは、脱硫設備１の電力消費量であり、上述した排ガスブロア消費電力ａ、循環ポンプ消費電力ｂ、および酸化ブロア消費電力ｃを加えることで求められる。ＤＰは、電力単価である。Ｌは、石灰石消費量であり、下記式６により求められるもので、下記式７により求められるＳＯ２除去量Ｓ（排ガス１００ａから除去したＳＯ２の量）と、石灰石純度ｆ’と、吸収液１０１中の石灰石濃度ｆとの関係から求められる。ＬＰは、石灰石単価（吸収液材料単価）である。Ｗは、脱硫設備１への供給水量であり、上述した排ガス流量ｇ、排ガス温度ｈ、および排ガス水分濃度ｉの関係から求められる。ＷＰは、供給水単価である。Ｆは、ボイラ２における燃料消費量であり、上述したボイラ燃料消費量ｊに相当する。ＦＰは、ボイラ２の燃料単価である。
　Ｌ＝Ｓ×１００／石灰石純度ｆ’　［１００＝ＣａＣＯ３分子量］・・・式６
　Ｓ＝（入口側ＳＯ２濃度ｄ－出口側ＳＯ２濃度ｅ）×排ガス流量ｇ／２２．４×１０６・・・式７
　なお、石灰石濃度ｆは、吸収液１０１中で余剰となった石灰石の濃度であり、これが一定であれば、石灰石消費量ＬはＳＯ２除去量Ｓに応じてのみ変化することになる。ただし、石灰石濃度ｆにより脱硫性能が変わるので、脱硫性能の要求が変わった場合は、一時的に石灰石消費量Ｌに余剰の石灰石を足す必要がある。 In the above formula 3, D is the power consumption of the desulfurization facility 1 and is obtained by adding the exhaust gas blower power consumption a, the circulation pump power consumption b, and the oxidation blower power consumption c described above. DP is a power unit price. L is a limestone consumption, those obtained by the following equation 6, the obtained SO 2 removal amount S (the amount of SO 2 removed from the flue gas 100a) by the following equation 7, the limestone purity f ', the absorbing liquid It is calculated | required from the relationship with the limestone density | concentration f in 101. LP is limestone unit price (absorbing liquid material unit price). W is the amount of water supplied to the desulfurization facility 1 and is determined from the relationship between the exhaust gas flow rate g, the exhaust gas temperature h, and the exhaust gas moisture concentration i described above. WP is the unit price of water supply. F is a fuel consumption amount in the boiler 2 and corresponds to the above-described boiler fuel consumption amount j. FP is the fuel unit price of the boiler 2.
L = S × 100 / limestone purity f ′ [100 = CaCO 3 molecular weight] Formula 6
S = (inlet side SO 2 concentration d−outlet side SO 2 concentration e) × exhaust gas flow rate g / 22.4 × 10 6 Formula 7
The limestone concentration f is the concentration of excess limestone in the absorption liquid 101. If this is constant, the limestone consumption L changes only in accordance with the SO 2 removal amount S. However, since the desulfurization performance changes depending on the limestone concentration f, when the demand for the desulfurization performance changes, it is necessary to temporarily add excess limestone to the limestone consumption L.
　また、上記式４において、Ｓは、上述したＳＯ２除去量である。ＳＰは、ＳＯ２取引単価である。 In the above formula 4, S is the SO 2 removal amount described above. SP is the SO 2 transaction unit price.
　また、上記式５において、Ｈは、副生石膏製造量であり、上述したＳＯ２除去量Ｓと、石灰石純度ｆ’と、吸収液１０１中の石灰石濃度ｆとの関係から求められる。ＨＰは、副生石膏販売単価（または副生石膏処理単価（副生石膏処理単価の場合はマイナス数値とする）である。 In Formula 5, H is the amount of byproduct gypsum produced, and is determined from the relationship between the SO 2 removal amount S, the limestone purity f ′, and the limestone concentration f in the absorbing liquid 101. HP is the by-product gypsum sales unit price (or by-product gypsum processing unit price (in the case of by-product gypsum processing unit price, it is a negative value)).
　吸収液循環ポンプ供給電圧データベース６ａｂは、上述した評価指数Ｅが最小となる、すなわち脱硫設備１の運転に応じて生じる支出諸事の支出市場価格である脱硫設備運転費Ｔが最も少なくなるように、吸収塔３に送る吸収液１０１の送出量を設定するため、吸収液循環ポンプ３ｃに電圧を加える吸収液循環ポンプ情報が格納されている。この吸収液循環ポンプ情報は、吸収液循環ポンプ３ｃによる吸収液送出量（吸収液流量ｎ）と、脱硫設備１の電力消費量ＤおよびＳＯ２除去量Ｓとの関係が予め理論式や実験式により求められたものである。 The absorption liquid circulation pump supply voltage database 6ab is such that the evaluation index E described above is minimized, that is, the desulfurization facility operating cost T, which is the expenditure market price of various expenditures generated according to the operation of the desulfurization facility 1, is minimized. In order to set the delivery amount of the absorption liquid 101 to be sent to the absorption tower 3, the absorption liquid circulation pump information for applying a voltage to the absorption liquid circulation pump 3c is stored. In this absorption liquid circulation pump information, the relationship between the absorption liquid delivery amount (absorption liquid flow rate n) by the absorption liquid circulation pump 3c and the power consumption D and SO 2 removal amount S of the desulfurization facility 1 is theoretical or experimental. It is the one requested by
　石灰石フィーダ供給電圧データベース６ａｃは、上述した評価指数Ｅが最小となる、すなわち脱硫設備１の運転に応じて生じる支出諸事の支出市場価格である脱硫設備運転費Ｔが最も少なくなるように、吸収塔３に供給する吸収液１０１の供給量を設定するため、石灰石フィーダ３ａのフィーダモータ（図示せず）に電圧を加えるフィーダ電圧情報が格納されている。このフィーダ電圧情報は、石灰石フィーダ３ａによる石灰石供給量ｋとＳＯ２除去量Ｓとの関係が予め理論式や実験式により求められたものである。 The limestone feeder supply voltage database 6ac has the absorption index so that the evaluation index E described above is minimized, that is, the desulfurization facility operating cost T, which is the expenditure market price of various expenditures generated according to the operation of the desulfurization facility 1, is minimized. In order to set the supply amount of the absorbent 101 supplied to the feeder 3, feeder voltage information for applying a voltage to a feeder motor (not shown) of the limestone feeder 3a is stored. In this feeder voltage information, the relationship between the limestone supply amount k and the SO 2 removal amount S by the limestone feeder 3a is obtained in advance by a theoretical formula or an experimental formula.
　また、管理装置６には、支出市場価格情報入力部６ｂが設けられている。この支出市場価格情報入力部６ｂには、支出市場価格としての脱硫設備運転費Ｔを求めるための電力単価ＤＰ、石灰石単価ＬＰ、供給水単価ＷＰ、および燃料単価ＦＰが入力される。かかる電力単価ＤＰ、石灰石単価ＬＰ、および供給水単価ＷＰは、インターネットなどから自動で入力されたり、オペレータにより手動で入力されたりすることで得られる。 Further, the management device 6 is provided with an expenditure market price information input unit 6b. In this expenditure market price information input unit 6b, a power unit price DP, a limestone unit price LP, a supply water unit price WP, and a fuel unit price FP for obtaining the desulfurization facility operating cost T as the expenditure market price are input. The electric power unit price DP, the limestone unit price LP, and the supply water unit price WP are obtained by being automatically input from the Internet or manually by an operator.
　また、管理装置６には、収入市場価格情報入力部６ｃが設けられている。この収入市場価格情報入力部６ｃには、収入市場価格としてのＳＯ２販売高Ｍを求めるためのＳＯ２取引単価ＳＰ、および収入市場価格としての副生石膏販売高（または副生石膏処理費用）Ｇを求めるための副生石膏販売単価（または副生石膏処理単価）ＨＰが入力される。かかるＳＯ２取引単価ＳＰ、および副生石膏販売単価（または副生石膏処理単価）ＨＰは、インターネットなどから自動で入力されたり、オペレータにより手動で入力されたりすることで得られる。 The management device 6 is provided with an income market price information input unit 6c. In the revenue market price information input unit 6c, an SO 2 transaction unit price SP for obtaining the SO 2 sales amount M as the revenue market price and a by-product gypsum sales amount (or by-product gypsum processing cost) G as the revenue market price are stored. The by-product gypsum sales unit price (or by-product gypsum processing unit price) HP for obtaining is input. Such SO 2 transaction unit price SP and by-product gypsum sales unit price (or by-product gypsum processing unit price) HP are obtained by being automatically input from the Internet or manually by an operator.
　また、管理装置６には、処理部６ｄが設けられている。処理部６ｄは、脱硫設備運転費算出部６ｄａ、ＳＯ２販売高算出部６ｄｂ、副生石膏販売高算出部（または副生石膏処理費用算出部）６ｄｃ、評価指数算出部６ｄｄ、吸収液送出量設定部６ｄｅ、および石灰石供給量設定部６ｄｆを有している。 Further, the management device 6 is provided with a processing unit 6d. The processing unit 6d includes a desulfurization facility operating cost calculation unit 6da, an SO 2 sales calculation unit 6db, a by-product gypsum sales calculation unit (or by-product gypsum processing cost calculation unit) 6dc, an evaluation index calculation unit 6dd, and an absorption liquid delivery amount setting unit. 6de and a limestone supply amount setting unit 6df.
　脱硫設備運転費算出部６ｄａは、上述した記憶部６ａの評価指数式データベース６ａａに格納された上記式３から脱硫設備運転費Ｔを算出する。すなわち、排ガスブロア消費電力ａ、循環ポンプ消費電力ｂ、および酸化ブロア消費電力ｃを足して脱硫設備１の電力消費量Ｄを求め、入口側ＳＯ２濃度ｄから出口側ＳＯ２濃度ｅを差し引き排ガス流量ｇを乗じたＳＯ２除去量Ｓ、石灰石純度ｆ’、および石灰石濃度ｆから石灰石消費量Ｌを求め、排ガス流量ｇ、排ガス温度ｈ、および排ガス水分濃度ｉの関係から供給水量Ｗを求め、さらにボイラ燃料消費量ｊから燃料消費量Ｆを求め、支出市場価格情報入力部６ｂから取得した電力単価ＤＰ、石灰石単価ＬＰ、供給水単価ＷＰ、および燃料単価ＦＰにより脱硫設備運転費Ｔを算出する。 The desulfurization facility operating cost calculation unit 6da calculates the desulfurization facility operating cost T from the above equation 3 stored in the evaluation index formula database 6aa of the storage unit 6a. That is, exhaust Gasuburoa power a, circulating pump power consumption b, and obtains the power consumption D of desulfurization 1 by adding the oxidizing blower power consumption c, the exhaust gas subtracts the outlet SO 2 concentration e from the inlet side SO 2 concentration d The limestone consumption L is determined from the SO 2 removal amount S multiplied by the flow rate g, the limestone purity f ′, and the limestone concentration f, and the supply water amount W is determined from the relationship between the exhaust gas flow rate g, the exhaust gas temperature h, and the exhaust gas moisture concentration i. Further, the fuel consumption F is obtained from the boiler fuel consumption j, and the desulfurization facility operating cost T is calculated from the power unit price DP, the limestone unit price LP, the supply water unit price WP, and the fuel unit price FP acquired from the expenditure market price information input unit 6b. .
　ＳＯ２販売高算出部６ｄｂは、上述した記憶部６ａの評価指数式データベース６ａａに格納された上記式４からＳＯ２販売高Ｍを算出する。すなわち、入口側ＳＯ２濃度ｄから出口側ＳＯ２濃度ｅを差し引き排ガス流量ｇを乗じてＳＯ２除去量Ｓを求め、さらに収入市場価格情報入力部６ｃから取得したＳＯ２取引単価ＳＰにより、ＳＯ２販売高Ｍを算出する。 The SO 2 sales amount calculation unit 6db calculates the SO 2 sales amount M from the above formula 4 stored in the evaluation index formula database 6aa of the storage unit 6a. That is, by subtracting the outlet side SO 2 concentration e from the inlet side SO 2 concentration d and multiplying by the exhaust gas flow rate g, the SO 2 removal amount S is obtained, and the SO 2 transaction unit price SP acquired from the revenue market price information input unit 6c 2 Calculate sales M.
　副生石膏販売高算出部（または副生石膏処理費用算出部）６ｄｃは、上述した記憶部６ａの評価指数式データベース６ａａに格納された上記式５から副生石膏販売高（副生石膏処理費用）Ｇを算出する。すなわち、入口側ＳＯ２濃度ｄから出口側ＳＯ２濃度ｅを差し引き排ガス流量ｇを乗じたＳＯ２除去量Ｓ、石灰石純度ｆ’、および石灰石濃度ｆから副生石膏製造量Ｈを求め、さらに収入市場価格情報入力部６ｃから取得した副生石膏販売単価（または副生石膏処理単価）ＨＰにより、副生石膏販売高（副生石膏処理費用）Ｇを算出する。 Byproduct gypsum sales amount calculation unit (or byproduct gypsum processing cost calculation unit) 6dc calculates byproduct gypsum sales amount (byproduct gypsum processing cost) G from the above equation 5 stored in the evaluation index formula database 6aa of the storage unit 6a. To do. That is, the amount of byproduct gypsum produced H is obtained from the SO 2 removal amount S obtained by subtracting the outlet side SO 2 concentration e from the inlet side SO 2 concentration d and multiplied by the exhaust gas flow rate g, the limestone purity f ′, and the limestone concentration f, and further the revenue market. By-product gypsum sales (by-product gypsum processing cost) G is calculated from the by-product gypsum sales unit price (or by-product gypsum processing unit price) HP acquired from the price information input unit 6c.
　評価指数算出部６ｄｄは、上述した記憶部６ａの評価指数式データベース６ａａに格納された上記式２から評価指数Ｅを算出する。すなわち、脱硫設備運転費算出部６ｄａで算出した脱硫設備運転費Ｔ、ＳＯ２販売高算出部６ｄｂで算出したＳＯ２販売高Ｍ、および副生石膏販売高算出部（または副生石膏処理費用算出部）６ｄｃで算出した副生石膏販売高（副生石膏処理費用）Ｇにより、評価指数Ｅを算出する。 The evaluation index calculation unit 6dd calculates the evaluation index E from the above formula 2 stored in the evaluation index formula database 6aa of the storage unit 6a. That is, the desulfurization equipment operation cost T calculated by desulfurization equipment operation cost calculation unit 6da, SO 2 sales calculator SO 2 sales calculated in 6db M, and by-product gypsum sales calculator (or by-product gypsum processing cost calculation unit) The evaluation index E is calculated from the amount of by-product gypsum sales (cost of by-product gypsum treatment) G calculated at 6 dc.
　吸収液送出量設定部６ｄｅは、上述した記憶部６ａの吸収液循環ポンプ供給電圧データベース６ａｂに格納された吸収液循環ポンプ情報により、評価指数算出部６ｄｄで算出した評価指数Ｅが最小となるように、吸収塔３に送る吸収液１０１の送出量、すなわち吸収液循環ポンプ３ｃに加える電圧を設定する。 The absorption liquid delivery amount setting unit 6de uses the absorption liquid circulation pump information stored in the absorption liquid circulation pump supply voltage database 6ab of the storage unit 6a to minimize the evaluation index E calculated by the evaluation index calculation unit 6dd. In addition, the amount of the absorption liquid 101 to be sent to the absorption tower 3, that is, the voltage applied to the absorption liquid circulation pump 3c is set.
　石灰石供給量設定部６ｄｆは、上述した記憶部６ａの石灰石フィーダ供給電圧データベース６ａｃに格納されたフィーダ電圧情報により、評価指数算出部６ｄｄで算出した評価指数Ｅが最小となるように、吸収液１０１を成す材料である石灰石１０２の供給量、すなわち石灰石フィーダ３ａのフィーダモータ（図示せず）に加える電圧を設定する。 The limestone supply amount setting unit 6df absorbs the absorbent 101 so that the evaluation index E calculated by the evaluation index calculation unit 6dd is minimized based on the feeder voltage information stored in the limestone feeder supply voltage database 6ac of the storage unit 6a. The supply amount of the limestone 102 which is the material forming the above, that is, the voltage applied to the feeder motor (not shown) of the limestone feeder 3a is set.
　また、管理装置６には、入出力部６ｅが設けられている。入出力部６ｅは、キーボードやマウスやモニターで構成されている。また、管理装置６には、情報通信部６ｆが設けられている。情報通信部６ｆは、制御装置５の情報通信部５ｅとの間で情報通信を行うためのものである。この管理装置６は、制御装置５から入力された情報に基づき、記憶部６ａに予め格納されたプログラムやデータに従って、制御装置５に対し、吸収液循環ポンプ３ｃおよび石灰石フィーダ３ａを統括的に制御するための情報を出力する。 Further, the management device 6 is provided with an input / output unit 6e. The input / output unit 6e includes a keyboard, a mouse, and a monitor. In addition, the management device 6 is provided with an information communication unit 6f. The information communication unit 6 f is for performing information communication with the information communication unit 5 e of the control device 5. Based on the information input from the control device 5, the management device 6 controls the control device 5 in an integrated manner with respect to the absorbent circulating pump 3c and the limestone feeder 3a in accordance with programs and data stored in advance in the storage unit 6a. To output information.
　上述した制御装置５および管理装置６による脱硫設備の運転制御について、図３の実施の形態１に係る脱硫設備の運転制御システムの動作を示すフローチャートを参照して説明する。 The operation control of the desulfurization facility by the control device 5 and the management device 6 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 of FIG.
　図３に示すように、まず、制御装置５では、排ガスブロア消費電力ａ、循環ポンプ消費電力ｂ、酸化ブロア消費電力ｃ、入口側ＳＯ２濃度ｄ、出口側ＳＯ２濃度ｅ、石灰石濃度ｆ、石灰石純度ｆ’、排ガス流量ｇ、排ガス温度ｈ、排ガス水分濃度ｉ、ボイラ燃料消費量ｊ、石灰石供給量ｋ、供給水流量ｍ、および吸収液流量ｎの各データを管理装置６に出力する（ステップＳＴ１）。 As shown in FIG. 3, first, in the control device 5, the exhaust gas blower power consumption a, the circulation pump power consumption b, the oxidation blower power consumption c, the inlet side SO 2 concentration d, the outlet side SO 2 concentration e, the limestone concentration f, Each data of the limestone purity f ′, the exhaust gas flow rate g, the exhaust gas temperature h, the exhaust gas moisture concentration i, the boiler fuel consumption j, the limestone supply amount k, the supply water flow rate m, and the absorption liquid flow rate n is output to the management device 6 ( Step ST1).
　次に、管理装置６は、制御装置５から上記各データを入力し（ステップＳＴ２）、脱硫設備運転費算出部６ｄａにおいて、脱硫設備運転費Ｔを算出し、ＳＯ２販売高算出部６ｄｂにおいて、ＳＯ２販売高Ｍを算出し、副生石膏販売高算出部（または副生石膏処理費用算出部）６ｄｃにおいて、副生石膏販売高（副生石膏処理費用）Ｇを算出し、評価指数算出部６ｄｄにおいて、評価指数Ｅを算出する（ステップＳＴ３）。 Next, the management device 6 inputs each of the above data from the control device 5 (step ST2), the desulfurization facility operation cost calculation unit 6da calculates the desulfurization facility operation cost T, and the SO 2 sales calculation unit 6db The SO 2 sales amount M is calculated, the by-product gypsum sales calculating unit (or by-product gypsum processing cost calculating unit) 6dc calculates the by-product gypsum sales amount (by-product gypsum processing cost) G, and the evaluation index calculating unit 6dd evaluates it. An index E is calculated (step ST3).
　次に、管理装置６は、吸収液送出量設定部６ｄｅにおいて、評価指数Ｅが最小となるように、吸収塔３に送る吸収液１０１の送出量（すなわち吸収液循環ポンプ３ｃに加える電圧）を設定すると共に、石灰石供給量設定部６ｄｆにおいて、評価指数Ｅが最小となるように、吸収液１０１を成す材料である石灰石１０２の供給量（すなわち石灰石フィーダ３ａのフィーダモータ（図示せず）に加える電圧）を設定する（ステップＳＴ４）。 Next, the management device 6 sets the amount of the absorption liquid 101 to be sent to the absorption tower 3 (that is, the voltage applied to the absorption liquid circulation pump 3c) so that the evaluation index E is minimized in the absorption liquid delivery amount setting unit 6de. At the same time, in the limestone supply amount setting unit 6df, the supply amount of limestone 102 which is a material constituting the absorbing liquid 101 (that is, a feeder motor (not shown) of the limestone feeder 3a) is added so that the evaluation index E is minimized. Voltage) is set (step ST4).
　最後に、制御装置５では、ＳＯ２除去量Ｓを所定の範囲内としつつ、管理装置６で設定された吸収液循環ポンプ３ｃの電圧、および石灰石フィーダ３ａのフィーダモータ（図示せず）の電圧に応じ、吸収液循環ポンプ３ｃおよび石灰石フィーダ３ａを駆動する（ステップＳＴ５）。 Finally, the control device 5, while the SO 2 removal amount S within a predetermined range, the set voltage of the absorbent circulating pump 3c in the management apparatus 6, and the voltage of the feeder motor limestone feeder 3a (not shown) Accordingly, the absorption liquid circulation pump 3c and the limestone feeder 3a are driven (step ST5).
　このように、実施の形態１に係る脱硫設備の運転制御システムでは、排ガス１００ａからＳＯ２を除去したＳＯ２除去量Ｓを所定範囲内としつつ、脱硫設備１の運転に応じて生じる支出諸事の支出市場価格（脱硫設備運転費Ｔ）から、脱硫設備１の運転に応じて生じる収入諸事の収入市場価格（ＳＯ２販売高Ｍ、副生石膏販売高（副生石膏処理費用）Ｇ）を差し引いた評価指数Ｅが最小となる態様で、吸収塔３に送る吸収液１０１の送出量、および吸収液１０１を成す材料（石灰石１０２）の供給量を設定する。 As described above, in the operation control system for the desulfurization facility according to the first embodiment, the expenditures generated in accordance with the operation of the desulfurization facility 1 while keeping the SO 2 removal amount S obtained by removing SO 2 from the exhaust gas 100a within a predetermined range. Evaluation by subtracting the revenue market price (SO 2 sales M, by-product gypsum sales (by-product gypsum treatment cost) G) from the expenditure market price (desulfurization facility operating cost T) and the revenue generated by the operation of the desulfurization facility 1 In a mode in which the index E is minimized, the amount of the absorbing liquid 101 sent to the absorption tower 3 and the amount of the material (limestone 102) constituting the absorbing liquid 101 are set.
　この脱硫設備の運転制御システムによれば、収入市場価格（ＳＯ２販売高Ｍ、副生石膏販売高Ｇ）が高い場合は、ＳＯ２除去量Ｓを増加させ、逆に、収入市場価格（ＳＯ２販売高Ｍ、副生石膏販売高Ｇ）が低い場合は、脱硫設備運転費Ｔを少なくするように制御する。このように、収入市場価格（ＳＯ２販売高Ｍ、副生石膏販売高（副生石膏処理費用）Ｇ）に応じて脱硫設備１の運転条件を最適化することが可能になる。この結果、刻々と変化する排ガス１００ａ条件（入口側ＳＯ２濃度ｄ、出口側ＳＯ２濃度ｅ、石灰石濃度ｆ、排ガス流量ｇ、排ガス温度ｈ）やＳＯ２販売高Ｍ、および比較的緩やかに変動する各種単価（電力単価ＤＰ、石灰石単価ＬＰ、供給水単価ＷＰ、燃料単価ＦＰ）の各データにより、常に脱硫設備１の運転に応じて生じる費用が最小となる経済的運転を行うことが可能になる。 According to the operation control system of this desulfurization facility, when the revenue market price (SO 2 sales M, by-product gypsum sales G) is high, the SO 2 removal amount S is increased, and conversely, the revenue market price (SO 2 When the sales amount M and the by-product gypsum sales amount G) are low, the desulfurization equipment operating cost T is controlled to be reduced. Thus, the operating conditions of the desulfurization facility 1 can be optimized according to the revenue market price (SO 2 sales M, by-product gypsum sales (by-product gypsum processing cost) G). As a result, the exhaust gas 100a conditions (inlet side SO 2 concentration d, outlet side SO 2 concentration e, limestone concentration f, exhaust gas flow rate g, exhaust gas temperature h), SO 2 sales M, and relatively slowly fluctuate. Each unit price (power unit price DP, limestone unit price LP, supply water unit price WP, fuel unit price FP) can be used to perform economical operation that always minimizes the cost caused by the operation of the desulfurization facility 1. Become.
　しかも、条件によっては、上記式２（Ｅ＝Ｔ－Ｍ－Ｇ）において、収入市場価格（Ｍ，Ｇ）が支出市場価格（Ｔ）よりも多くなれば、評価指数Ｅがマイナスとなり、脱硫設備１の運転により利益計上を図ることも可能である。 Moreover, depending on the conditions, in the above formula 2 (E = TMG), if the revenue market price (M, G) is greater than the expenditure market price (T), the evaluation index E becomes negative, and the desulfurization equipment It is also possible to record profits by driving 1.
　また、実施の形態１に係る脱硫設備の運転制御システムでは、管理装置６は、ネットワークＮ上を介して脱硫設備１における制御装置５と通信可能に接続されている。この結果、脱硫設備１の運転制御を遠隔地にて行うことが可能になる。 Further, in the operation control system for the desulfurization facility according to the first embodiment, the management device 6 is connected to the control device 5 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.
　なお、実施の形態１に係る脱硫設備の運転制御システムでは、図１に示すように、管理装置６がネットワークＮ上を介して複数の脱硫設備１における制御装置５と通信可能に接続されている。図２では、１つの脱硫設備１における制御装置５と管理装置６とが一対一の関係で接続されている形態を示しているが、複数の脱硫設備１における制御装置５と管理装置６とが多対一の関係で接続されている場合は、管理装置６において、各制御装置５に対応して記憶部６ａ、支出市場価格情報入力部６ｂ、収入市場価格情報入力部６ｃ、処理部６ｄ、入出力部６ｅ、および情報通信部６ｆが機能する。この結果、複数の脱硫設備１の運転制御を遠隔地にて統括して行うことが可能になる。なお、脱硫設備１における制御装置５と管理装置６とが一対一の関係で接続される場合は、制御装置５と管理装置６とがネットワークＮ上を介して接続されず、管理装置６が脱硫設備１の制御装置５に含まれて構成されていてもよい。 In the operation control system for the desulfurization facility according to the first embodiment, as shown in FIG. 1, the management device 6 is communicably connected to the control devices 5 in the plurality of desulfurization facilities 1 via the network N. . FIG. 2 shows a form in which the control device 5 and the management device 6 in one desulfurization facility 1 are connected in a one-to-one relationship. However, the control device 5 and the management device 6 in the plurality of desulfurization facilities 1 are connected to each other. When connected in a many-to-one relationship, in the management device 6, corresponding to each control device 5, a storage unit 6a, an expenditure market price information input unit 6b, an income market price information input unit 6c, a processing unit 6d, The input / output unit 6e and the information communication unit 6f function. As a result, the operation control of the plurality of desulfurization facilities 1 can be performed in a remote place. When the control device 5 and the management device 6 in the desulfurization facility 1 are connected in a one-to-one relationship, the control device 5 and the management device 6 are not connected via the network N, and the management device 6 is desulfurized. It may be included in the control device 5 of the facility 1.
　なお、ＳＯ２を吸収する吸収液として、石灰石１０２を含む吸収液１０１を適用した石灰石膏法の脱硫設備１について説明したが、この限りではない。例えば、水マグ法や苛性ソーダ法など、他の湿式脱硫設備でも、上述した実施の形態が適用可能である。その場合、石灰石単価ＬＰを水酸化マグネシウム単価や苛性ソーダ単価に変更する。 As the absorption liquid to absorb SO 2, it has been described desulfurization 1 lime gypsum method of applying the absorption liquid 101 containing limestone 102, not limited thereto. For example, the embodiments described above can be applied to other wet desulfurization facilities such as a water mug method and a caustic soda method. In that case, the limestone unit price LP is changed to a magnesium hydroxide unit price or a caustic soda unit price.
［実施の形態２］
　本実施の形態について、図面を参照して説明する。図４は、本発明の実施の形態２に係る脱硫設備の運転制御システムのブロック図である。なお、以下に説明する実施の形態２において、上述した実施の形態１と同等の構成には同一の符号を付してその説明を省略する。 [Embodiment 2]
The present embodiment will be described with reference to the drawings. FIG. 4 is a block 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.
　図４に示す脱硫設備１は、上述した実施の形態１に対し、管理装置６において、記憶部６ａに支出市場価格情報データベース６ａｄ、および収入市場価格情報データベース６ａｅをさらに備えている。 The desulfurization facility 1 shown in FIG. 4 further includes a spending market price information database 6ad and an income market price information database 6ae in the storage unit 6a in the management device 6 as compared with the first embodiment described above.
　支出市場価格情報データベース６ａｄは、支出市場価格情報入力部６ｂに入力された支出市場価格として、脱硫設備運転費Ｔを求めるための電力単価ＤＰ、石灰石単価ＬＰ、供給水単価ＷＰ、および燃料単価ＦＰを記憶する。 The expenditure market price information database 6ad is a unit price of electricity DP, a unit price of limestone LP, a unit price of supply water WP, and a unit price of fuel FP as the expenditure market price input to the expenditure market price information input unit 6b. Remember.
　収入市場価格情報データベース６ａｅは、収入市場価格情報入力部６ｃに入力された収入市場価格として、ＳＯ２販売高Ｍを求めるためのＳＯ２取引単価ＳＰ、および副生石膏販売高（または副生石膏処理費用）Ｇを求めるための副生石膏販売単価（または副生石膏処理単価）ＨＰを記憶する。 The revenue market price information database 6ae stores the SO 2 transaction unit price SP for obtaining the SO 2 sales amount M as the revenue market price input to the revenue market price information input unit 6c, and by-product gypsum sales (or by-product gypsum processing costs). ) Store by-product gypsum sales unit price (or by-product gypsum processing unit price) HP for obtaining G.
　制御装置５および管理装置６による脱硫設備の運転制御について、図５の実施の形態２に係る脱硫設備の運転制御システムの動作を示すフローチャートを参照して説明する。 The operation control of the desulfurization facility by the control device 5 and the management device 6 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 of FIG.
　図５に示すように、まず、管理装置６では、過去の所定期間について、支出市場価格情報データベース６ａｄに記憶された支出市場価格、および収入市場価格情報データベース６ａｅに記憶された収入市場価格を取得する（ステップＳＴ１１）。 As shown in FIG. 5, first, the management device 6 acquires the expenditure market price stored in the expenditure market price information database 6ad and the income market price stored in the income market price information database 6ae for a predetermined period in the past. (Step ST11).
　次に、管理装置６は、評価指数算出部６ｄｄにおいて、取得した支出市場価格から収入市場価格を差し引いて、予測評価指数Ｅａを算出する（ステップＳＴ１２）。予測評価指数Ｅａの算出は、上述した実施の形態１の評価指数Ｅと同じである。 Next, the management device 6 calculates the predicted evaluation index Ea by subtracting the income market price from the acquired expenditure market price in the evaluation index calculation unit 6dd (step ST12). The calculation of the predicted evaluation index Ea is the same as the evaluation index E of the first embodiment described above.
　次に、管理装置６は、吸収液送出量設定部６ｄｅにおいて、予測評価指数Ｅａが最小となるように、吸収塔３に送る吸収液１０１の送出量（すなわち吸収液循環ポンプ３ｃに加える電圧）を設定すると共に、石灰石供給量設定部６ｄｆにおいて、予測評価指数Ｅａが最小となるように、吸収液１０１を成す材料である石灰石１０２の供給量（すなわち石灰石フィーダ３ａのフィーダモータ（図示せず）に加える電圧）を設定する（ステップＳＴ１３）。 Next, the management device 6 sends the absorption liquid 101 sent to the absorption tower 3 (that is, the voltage applied to the absorption liquid circulation pump 3c) so that the predicted evaluation index Ea is minimized in the absorption liquid delivery quantity setting unit 6de. In addition, in the limestone supply amount setting unit 6df, the supply amount of limestone 102 that is the material constituting the absorbent 101 (that is, a feeder motor (not shown) of the limestone feeder 3a) so that the predicted evaluation index Ea is minimized. Is set (step ST13).
　最後に、制御装置５では、ＳＯ２除去量Ｓを所定の範囲内としつつ、管理装置６で設定された吸収液循環ポンプ３ｃの電圧、および石灰石フィーダ３ａのフィーダモータ（図示せず）の電圧に応じ、吸収液循環ポンプ３ｃおよび石灰石フィーダ３ａを駆動する（ステップＳＴ１４）。 Finally, the control device 5, while the SO 2 removal amount S within a predetermined range, the set voltage of the absorbent circulating pump 3c in the management apparatus 6, and the voltage of the feeder motor limestone feeder 3a (not shown) Accordingly, the absorption liquid circulation pump 3c and the limestone feeder 3a are driven (step ST14).
　このように、実施の形態２に係る脱硫設備の運転制御システムでは、過去の所定期間について、支出市場価格（脱硫設備運転費Ｔ）から収入市場価格（ＳＯ２販売高Ｍ、副生石膏販売高（副生石膏処理費用）Ｇ）を差し引いた予測評価指数Ｅａが最小となる態様で、吸収塔３に送る吸収液１０１の送出量、および吸収液１０１を成す材料（石灰石１０２）の供給量を設定する。 As described above, in the operation control system for the desulfurization facility according to the second embodiment, the revenue market price (SO 2 sales M, by-product gypsum sales ( The amount of absorption liquid 101 sent to the absorption tower 3 and the supply amount of the material (limestone 102) constituting the absorption liquid 101 are set in such a manner that the predicted evaluation index Ea obtained by subtracting the byproduct gypsum processing cost G) is minimized. .
　この脱硫設備の運転制御システムによれば、過去の収入市場価格（ＳＯ２販売高Ｍ、副生石膏販売高Ｇ）が高い場合は、ＳＯ２除去量Ｓを増加させ、逆に、過去の収入市場価格（ＳＯ２販売高Ｍ、副生石膏販売高Ｇ）が低い場合は、脱硫設備運転費Ｔを少なくするように設定する。このように、過去の収入市場価格（ＳＯ２販売高Ｍ、副生石膏販売高（副生石膏処理費用）Ｇ）に応じて最適な脱硫設備１の運転条件を予測することが可能になる。この結果、設備の管理者は、予め計画してユーティリティーなどの材料（例えば、石灰石１０２）の先行手配を行うことが可能になる。なお、予測評価指数Ｅａは、上述した実施の形態１の評価指数Ｅにより補正することが可能である。 According to the operation control system of this desulfurization facility, when the past revenue market price (SO 2 sales M, by-product gypsum sales G) is high, the SO 2 removal amount S is increased, and conversely the past revenue market. When the price (SO 2 sales M, by-product gypsum sales G) is low, the desulfurization equipment operating cost T is set to be low. Thus, it becomes possible to predict the optimal operating conditions of the desulfurization facility 1 according to the past revenue market price (SO 2 sales amount M, by-product gypsum sales amount (by-product gypsum treatment cost) G). As a result, the manager of the facility can make a prior arrangement for materials such as utilities (for example, limestone 102) by planning in advance. The predicted evaluation index Ea can be corrected by the evaluation index E of the first embodiment described above.
　また、実施の形態２に係る脱硫設備の運転制御システムでは、管理装置６は、ネットワークＮ上を介して脱硫設備１における制御装置５と通信可能に接続されている。この結果、脱硫設備１の運転制御を遠隔地にて行うことが可能になる。 In the operation control system for the desulfurization facility according to the second embodiment, the management device 6 is connected to the control device 5 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.
　なお、実施の形態２に係る脱硫設備の運転制御システムでは、図１に示すように、管理装置６がネットワークＮ上を介して複数の脱硫設備１における制御装置５と通信可能に接続されている。図４では、１つの脱硫設備１における制御装置５と管理装置６とが一対一の関係で接続されている形態を示しているが、複数の脱硫設備１における制御装置５と管理装置６とが多対一の関係で接続されている場合は、管理装置６において、各制御装置５に対応して記憶部６ａ、支出市場価格情報入力部６ｂ、収入市場価格情報入力部６ｃ、処理部６ｄ、入出力部６ｅ、および情報通信部６ｆが機能する。この結果、複数の脱硫設備１の運転制御を遠隔地にて統括して行うことが可能になる。なお、脱硫設備１における制御装置５と管理装置６とが一対一の関係で接続される場合は、制御装置５と管理装置６とがネットワークＮ上を介して接続されず、管理装置６が脱硫設備１の制御装置５に含まれて構成されていてもよい。 In the operation control system for the desulfurization facility according to the second embodiment, as shown in FIG. 1, the management device 6 is communicably connected to the control devices 5 in the plurality of desulfurization facilities 1 via the network N. . In FIG. 4, the control device 5 and the management device 6 in one desulfurization facility 1 are connected in a one-to-one relationship, but the control device 5 and the management device 6 in the plurality of desulfurization facilities 1 are connected. When connected in a many-to-one relationship, in the management device 6, corresponding to each control device 5, a storage unit 6a, an expenditure market price information input unit 6b, an income market price information input unit 6c, a processing unit 6d, The input / output unit 6e and the information communication unit 6f function. As a result, the operation control of the plurality of desulfurization facilities 1 can be performed in a remote place. When the control device 5 and the management device 6 in the desulfurization facility 1 are connected in a one-to-one relationship, the control device 5 and the management device 6 are not connected via the network N, and the management device 6 is desulfurized. It may be included in the control device 5 of the facility 1.
　以上のように、本発明に係る脱硫設備の運転制御システムは、諸事の市場価格に応じた経済的運転を行うことに適している。 As described above, the operation control system for a desulfurization facility according to the present invention is suitable for performing economical operation in accordance with various market prices.
　１　脱硫設備
　２　ボイラ
　２ａ　排ガス管
　２ｂ　排ガスブロア
　３　吸収塔
　３ａ　石灰石フィーダ
　３ｂ　給水管
　３ｃ　吸収液循環ポンプ
　３ｄ　吸収液管
　３ｅ　ノズル
　３ｆ　脱硫排ガス管
　３ｇ　抜出管
　３ｈ　脱水器
　３ｉ　酸化ブロア
　４ａ　排ガスブロア消費電力検出部
　４ｂ　循環ポンプ消費電力検出部
　４ｃ　酸化ブロア消費電力検出部
　４ｄ　入口側ＳＯ２濃度検出部
　４ｅ　出口側ＳＯ２濃度検出部
　４ｆ　石灰石濃度検出部
　４ｇ　排ガス流量検出部
　４ｈ　排ガス温度検出部
　４ｉ　排ガス水分濃度検出部
　４ｊ　ボイラ燃料消費量検出部
　４ｋ　石灰石供給量検出部
　４ｍ　供給水流量検出部
　４ｎ　吸収液流量検出部
　５　制御装置
　５ａ　記憶部
　５ｂ　吸収液循環ポンプ駆動部
　５ｃ　石灰石フィーダ駆動部
　５ｄ　入出力部
　５ｅ　情報通信部
　６　管理装置
　６ａ　記憶部
　６ｂ　支出市場価格情報入力部
　６ｃ　収入市場価格情報入力部
　６ｄ　処理部
　６ｅ　入出力部
　６ｆ　情報通信部
　１００ａ　排ガス
　１００ｂ　脱硫排ガス
　１０１　吸収液
　１０２　石灰石
　１０３　水
　１０４　副生石膏
　１０５　酸化用空気
　Ｎ　ネットワーク
　Ｅ　評価指数
　Ｅａ　予測評価指数
　Ｔ　脱硫設備運転費
　Ｍ　ＳＯ２販売高
　Ｇ　副生石膏販売高
　Ｓ　ＳＯ２除去量 DESCRIPTION OF SYMBOLS 1 Desulfurization equipment 2 Boiler 2a Exhaust pipe 2b Exhaust blower 3 Absorption tower 3a Limestone feeder 3b Water supply pipe 3c Absorption liquid circulation pump 3d Absorption liquid pipe 3e Nozzle 3f Desulfurization exhaust pipe 3g Extraction pipe 3h Dehydrator 3i Oxidation blower 4a Exhaust blower power consumption Detection unit 4b Circulating pump power consumption detection unit 4c Oxidation blower power consumption detection unit 4d Inlet side SO 2 concentration detection unit 4e Outlet side SO 2 concentration detection unit 4f Limestone concentration detection unit 4g Exhaust gas flow rate detection unit 4h Exhaust gas temperature detection unit 4i Exhaust gas moisture Concentration detection unit 4j Boiler fuel consumption detection unit 4k Limestone supply amount detection unit 4m Supply water flow rate detection unit 4n Absorbed liquid flow rate detection unit 5 Controller 5a Storage unit 5b Absorption liquid circulation pump drive unit 5c Limestone feeder drive unit 5d Input / output unit 5e Information communication unit 6 Management device 6a Storage unit 6b Expenditure market price information Information input part 6c Revenue market price information input part 6d Processing part 6e Input / output part 6f Information communication part 100a Exhaust gas 100b Desulfurization exhaust gas 101 Absorbent liquid 102 Limestone 103 Water 104 Byproduct gypsum 105 Air for oxidation N Network E Evaluation index Ea Predictive evaluation index T Operating cost of desulfurization equipment M SO 2 sales G By-product gypsum sales S SO 2 removal

Claims (4)

  1. 　排ガスに吸収液を接触させることで前記排ガス中のＳＯ２を前記吸収液に吸収させつつＳＯ２が除去された脱硫排ガスを排出する吸収塔を備える脱硫設備の運転制御システムにおいて、
    　前記排ガスからＳＯ２を除去したＳＯ２除去量を所定範囲内としつつ、脱硫設備の運転に応じて生じる支出諸事の支出市場価格から脱硫設備の運転に応じて生じる収入諸事の収入市場価格を差し引いた評価指数が最小となる態様で、前記吸収塔に送る吸収液の送出量、および前記吸収液を成す材料の供給量を設定する管理装置を備えたことを特徴とする脱硫設備の運転制御システム。     In operation control system of desulfurization comprising an absorption tower for discharging the desulfurized flue gas SO 2 is removed SO 2 while absorbed into the absorbing solution in the exhaust gas by contacting the absorption liquid to the exhaust gas,
    The amount of SO 2 removed by removing SO 2 from the exhaust gas is within a predetermined range, and the revenue market price of revenues generated according to the operation of the desulfurization facility is subtracted from the expenditure market price of the expenditures generated according to the operation of the desulfurization facility. An operation control system for a desulfurization facility, comprising a management device for setting a delivery amount of an absorption liquid to be sent to the absorption tower and a supply amount of a material constituting the absorption liquid in such a manner that the evaluation index is minimized. .
  2. 　前記管理装置は、過去の所定期間について、前記支出市場価格から前記収入市場価格を差し引いた予測評価指数が最小となる態様で、前記吸収塔に送る吸収液の送出量、および前記吸収液を成す材料の供給量を予め設定することを特徴とする請求項１に記載の脱硫設備の運転制御システム。 The management device is configured such that, for a predetermined period in the past, a predicted evaluation index obtained by subtracting the revenue market price from the expenditure market price is minimized, and the amount of the absorption liquid sent to the absorption tower and the absorption liquid are formed. 2. The operation control system for a desulfurization facility according to claim 1, wherein a supply amount of the material is set in advance.
  3. 　前記排ガス中のＳＯ２濃度、および前記脱硫排ガス中のＳＯ２濃度を取得すると共に、前記吸収塔への吸収液の送出、および前記吸収液を成す材料の供給を制御する制御装置と、前記吸収塔と、前記吸収塔に吸収液を送る吸収液送出部と、前記吸収液を成す材料を供給する材料供給部とにより、排ガス中のＳＯ２を除去する脱硫設備が構成され、
    　前記管理装置は、ネットワーク上を介して前記脱硫設備における前記制御装置と通信可能に接続されていることを特徴とする請求項１または２に記載の脱硫設備の運転制御システム。     SO 2 concentration in the exhaust gas, and acquires the SO 2 concentration in the desulfurized flue gas, and a control device for controlling the supply of material forming delivery, and the absorption liquid in the absorption liquid to the absorption tower, the absorbing A desulfurization facility for removing SO 2 in the exhaust gas is constituted by a tower, an absorption liquid sending section that sends an absorption liquid to the absorption tower, and a material supply section that supplies a material that forms the absorption liquid.
    The operation control system for a desulfurization facility according to claim 1 or 2, wherein the management device is connected to the control device in the desulfurization facility via a network so as to be communicable.
  4. 　前記管理装置は、ネットワーク上を介して複数の前記脱硫設備における前記制御装置と通信可能に接続されていることを特徴とする請求項３に記載の脱硫設備の運転制御システム。 The operation control system for a desulfurization facility according to claim 3, wherein the management device is connected to the control devices in a plurality of the desulfurization facilities via a network.
PCT/JP2010/066496 2009-11-24 2010-09-24 System for controlling operation of desulfurization apparatus WO2011065119A1 (en)

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CN112288296A (en) * 2020-11-03 2021-01-29 北京国电龙源环保工程有限公司 Real-time evaluation system and application method for operation performance and economy of desulfurization device
CN113313325A (en) * 2021-06-21 2021-08-27 西安热工研究院有限公司 Desulfurization system operation optimization method, system, equipment and storage medium
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