CN115970476A - Automatic slurry supply control method for desulfurization island based on DCS control system - Google Patents
Automatic slurry supply control method for desulfurization island based on DCS control system Download PDFInfo
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- CN115970476A CN115970476A CN202310065996.3A CN202310065996A CN115970476A CN 115970476 A CN115970476 A CN 115970476A CN 202310065996 A CN202310065996 A CN 202310065996A CN 115970476 A CN115970476 A CN 115970476A
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- 239000002002 slurry Substances 0.000 title claims abstract description 83
- 238000000034 method Methods 0.000 title claims abstract description 43
- 238000006477 desulfuration reaction Methods 0.000 title claims abstract description 27
- 230000023556 desulfurization Effects 0.000 title claims abstract description 27
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims abstract description 49
- 239000003546 flue gas Substances 0.000 claims abstract description 49
- 239000007789 gas Substances 0.000 claims abstract description 22
- 238000004364 calculation method Methods 0.000 claims abstract description 9
- 238000010521 absorption reaction Methods 0.000 claims description 17
- 238000013461 design Methods 0.000 claims description 12
- 235000019738 Limestone Nutrition 0.000 claims description 11
- 239000006028 limestone Substances 0.000 claims description 11
- 239000011575 calcium Substances 0.000 claims description 7
- 239000007787 solid Substances 0.000 claims description 6
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 claims description 2
- 229910052791 calcium Inorganic materials 0.000 claims description 2
- 238000005457 optimization Methods 0.000 abstract description 8
- 239000000779 smoke Substances 0.000 abstract description 3
- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 description 40
- JGIATAMCQXIDNZ-UHFFFAOYSA-N calcium sulfide Chemical compound [Ca]=S JGIATAMCQXIDNZ-UHFFFAOYSA-N 0.000 description 7
- 230000033228 biological regulation Effects 0.000 description 4
- 230000001276 controlling effect Effects 0.000 description 4
- 238000005507 spraying Methods 0.000 description 4
- 238000011160 research Methods 0.000 description 3
- 238000011217 control strategy Methods 0.000 description 2
- 230000003009 desulfurizing effect Effects 0.000 description 2
- 230000007613 environmental effect Effects 0.000 description 2
- 230000009123 feedback regulation Effects 0.000 description 2
- 239000003517 fume Substances 0.000 description 2
- 239000010440 gypsum Substances 0.000 description 2
- 229910052602 gypsum Inorganic materials 0.000 description 2
- 230000001105 regulatory effect Effects 0.000 description 2
- 206010063385 Intellectualisation Diseases 0.000 description 1
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 1
- 239000002253 acid Substances 0.000 description 1
- 230000003044 adaptive effect Effects 0.000 description 1
- 238000013528 artificial neural network Methods 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 238000004891 communication Methods 0.000 description 1
- 238000002425 crystallisation Methods 0.000 description 1
- 230000008025 crystallization Effects 0.000 description 1
- 125000004122 cyclic group Chemical group 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000004134 energy conservation Methods 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 238000007254 oxidation reaction Methods 0.000 description 1
- 238000004886 process control Methods 0.000 description 1
- 229910052717 sulfur Inorganic materials 0.000 description 1
- 239000011593 sulfur Substances 0.000 description 1
- 230000001502 supplementing effect Effects 0.000 description 1
- 238000012795 verification Methods 0.000 description 1
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- 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
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P90/00—Enabling technologies with a potential contribution to greenhouse gas [GHG] emissions mitigation
- Y02P90/02—Total factory control, e.g. smart factories, flexible manufacturing systems [FMS] or integrated manufacturing systems [IMS]
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Abstract
The invention discloses a DCS control system-based automatic slurry supply control method for a desulfurization island, which comprises the following processes: by using the unit flue gas volume and the unit inlet SO 2 Carrying out feedforward calculation on the concentration and the actual circulation amount of the slurry to obtain the reference slurry supply amount of slurry supply control and the initial target set value of the pH value, and then putting the reference slurry supply amount of slurry supply control and the initial target set value of the pH value into PID control; and during PID control, the pH value is used as a main adjusting parameter, the pulp supply adjusting amount except the reference pulp supply amount is determined according to the difference value of the actual pH value and the target pH value, the actual total pulp supply flow is adjusted by controlling the opening of the pulp supply adjusting valve, and the control of the size of the pulp in the desulfurization island is realized. The invention only passes through the group of DCS systemThe on-line optimization adjustment of the pH value and the slurry supply flow can be realized by establishing the state logic, and the clean smoke gas SO is realized 2 And (4) precisely controlling the concentration.
Description
Technical Field
The invention belongs to the technical field of energy conservation and environmental protection, and particularly relates to a desulfurization island automatic slurry supply control method based on a DCS (distributed control system).
Background
The wet desulphurization process is used as the most widely applied environmental protection process for flue gas desulphurization. The technological process includes spraying and atomizing slurry with slurry circulating pump inside the absorbing tower to make the slurry flow reversely and contact with fume to absorb SO from fume 2 Desulfurizing agent CaCO in absorption tower 3 Continuously supplementing into the absorption tower by a slurry supply pump, caCO 3 Ca is generated after the Ca is dissolved in the acid environment in the tower 2+ And OH - The pH value of the slurry of the absorption tower can be controlled within a reasonable range by adjusting the size of the slurry supply amount. The whole process is mainly divided into SO 2 Absorption process, caCO 3 Dissolving process, gypsum oxidation process and gypsum crystallization process. Wherein SO is influenced 2 The main link of the removal efficiency is SO 2 Absorption process andCaCO 3 the key parameters of the dissolving process and the process control are liquid-gas ratio and calcium-sulfur ratio. The definition is as follows:
(1) The desulfurization efficiency means sulfur dioxide (SO) removed by a desulfurization apparatus 2 ) The amount of SO contained in the flue gas before removal 2 The percentage of the amount is calculated according to the formula 1-1:
desulfurization efficiency = (c) 1 -c 2 )/C 1 ×100％(1-1)
In the formula: c. C 1 : SO in flue gas before desulfurization 2 Reduced concentration of (i.e. raw flue gas SO) 2 Concentration (standard, dry basis, 6% O) 2 )，mg/m 3 。
c 2 : SO at flue of outlet of desulfurizing device 2 Conversion concentration namely clean flue gas SO 2 Concentration (standard, dry basis, 6% O) 2 )，mg/m 3 。
(2) The Ca/S ratio means that CaCO is consumed by the flue gas desulfurization device 3 Total amount and SO removed 2 Ratio of the total amount, mol/mol.
(3) The liquid-gas ratio (L/G) refers to the ratio of the total circulating amount (liter) of the slurry in the absorption tower to the actual flue gas amount at the outlet of the absorption tower, and L/m 3 。
At present, the traditional Distributed Control System (DCS) is mainly adopted for controlling the wet desulphurization system, and the centralized management and the decentralized control are carried out on the production process. The control of the pH value is realized by setting a target value of the pH value, and after the pH value deviates from the target value, the opening and closing of the limestone slurry supply valve or the opening adjustment are realized by manual operation or a PID program, and the pH value and the calcium-sulfur ratio are in a direct proportion relation in a conventional application range. Under the condition of fixed flue gas quantity, the circulating spraying quantity and the liquid-gas ratio are in a linear relation, the control of the circulating spraying quantity is realized by manually setting the number of the opened circulating pumps, hysteresis exists often, the regulation of the spraying quantity is discrete, and when the working condition of the flue gas fluctuates, the desulfurization efficiency and the SO outlet of a clean flue gas are ensured 2 The discharge index and the pH value can not be stably controlled. In addition, clean flue gas SO under variable working conditions 2 The control precision is difficult to guarantee, and in order to meet the requirement of ultralow emission limit value, the outlet concentration set value of the actual power plant is lower than the emission limit value so as to provide resistance to inlet concentration and negativeSafety margin of charge variation. But the larger the margin, the higher the operating cost. Therefore, it is necessary to develop a research based on advanced control of the desulfurization system to improve the clean flue gas SO at the outlet of the absorption tower 2 And (4) controlling the concentration accurately. Therefore, the traditional DCS is controlled to realize the automatic slurry supply and the stable control of the clean flue gas, which are difficult to realize.
Aiming at the characteristics of multivariable input, nonlinearity and large time delay of a wet desulphurization system, the current external research mainly focuses on PID optimization and the introduction of an advanced control algorithm. For example, fuzzy adaptive PID control strategies of external PLC or algorithm server, PID control strategies based on neural network, model prediction algorithms, etc., however, the present cases of converting control theory research into practical application mainly focus on parameter optimization of PID control, and there are few cases of introducing advanced control algorithms and successfully implementing engineering application verification, and meanwhile, introducing algorithms often requires external PLC, etc., and there are usually problems of high hardware cost, insufficient data communication security, etc.
Disclosure of Invention
The invention aims to solve the technical problem of providing a desulfurization island automatic slurry supply control method based on a DCS (distributed control system) aiming at the defects of the traditional DCS control system slurry supply control method 2 And (4) precisely controlling the concentration.
The invention adopts the following technical scheme:
a kind of automatic slurry supply control method of desulfurization island based on DCS control system, the desulfurization island has return line and main line electric control valve, including the following process:
by using the unit flue gas volume and the unit inlet SO 2 Carrying out feedforward calculation on the concentration and the actual circulation amount of the slurry to obtain the reference slurry supply amount of slurry supply control and the initial target set value of the pH value, and then putting the reference slurry supply amount of slurry supply control and the initial target set value of the pH value into PID control;
and during PID control, the pH value is used as a main adjusting parameter, the pulp supply adjusting amount except the reference pulp supply amount is determined according to the difference value of the actual pH value and the target pH value, and the actual total pulp supply flow is adjusted by controlling the opening of the pulp supply adjusting valve, so that the control of the pulp amount of the desulfurization island is realized.
Preferably, the reference stock supply amount q 0 The following:
wherein q is 0 For the reference stock supply, m 3 /h；c 1 Is standard, dry basis, 6% O 2 Raw flue gas SO at inlet of absorption tower under condition 2 Concentration; c. C 2 Is standard, dry basis, 6% 2 Clean flue gas SO at outlet of absorption tower under condition 2 Concentration, mg/m 3 (ii) a G is standard, dry basis, 6% O 2 Flue gas volume of unit m under the condition 3 H; rho is the density of limestone slurry and has the unit of kg/m 3 (ii) a Omega is the solid content of the limestone slurry, and the unit is percent.
Preferably, the limestone slurry density ρ is calculated by the following formula:
ρ＝k×ω+C
wherein C and k are constants, and C and k are obtained by field calibration fitting of limestone slurry density and solid content linear curves.
Preferably, the initial target set value of the pH value is obtained by determining according to the liquid-gas ratio, the actual flue gas amount and the design parameters.
Preferably, the process of determining the initial target setting value of the pH value according to the liquid-gas ratio, the actual flue gas amount and the design parameters is as follows:
if it is
The initial target set value of the pH value is 5.4;
if it is
The initial target set value of the pH value is 6;
wherein, (L/G) Practice of For actual liquid-gas ratio, (L/G) Design of To design the liquid-gas ratio, c max Is c max Is standard, dry basis, 6% O 2 Design SO of raw flue gas at inlet of absorption tower under condition 2 The highest concentration.
Preferably, the actual total flow rate q of the stock supply is calculated by the following formula:
wherein,
is the calcium-sulfur ratio, q 1 Adjusting the amount for pulp supply, q 2 Is a PID adjustment amount.
Preferably, the PID adjustment amount q 2 The adjustment range of (2) is: -20% q 0 ≤q 2 ≤20％q 0 。
Preferably, the flue gas SO is purified according to the outlet of the absorption tower 2 Concentration c 2 To the adjustment amount q of slurry supply 1 And assigning, comprising the following processes:
when the pH value is more than 5.6, if 30mg/m 3 ＞c 2 ≥15mg/m 3 Then q is 1 ＝10％q 0 ；
When the pH is less than or equal to 5.6, if 30mg/m 3 ＞c 2 ≥15mg/m 3 Then q is 1 ＝5％q 0 ；
If c is 2 ≥30mg/m 3 Adjusting the pH target value, and increasing the current pH absolute value to 0.2 to serve as a new pH target value;
if c is 2 <15/m 3 And adjusting the pH target value, and reducing the current pH absolute value by 0.2 to be used as a new pH target value.
Preferably, the amount of pulp supply adjustment q 1 The initial assignment is 0.
Compared with the prior art, the invention has at least the following beneficial effects:
the traditional PID control still adopts a mode of manually setting a pH target value as a main regulation parameter, and the change of the original flue gas parameter cannot realize the outlet SO 2 Stable control of clean flue gas, originallyThe invention is to determine the flue gas volume and the inlet SO of the unit 2 On the basis of the relation between the concentration and the slurry circulation volume, the relation is used as an input volume of feedforward calculation, a reference slurry supply volume of slurry supply control and an initial target set value of a pH value are provided, PID control is put into operation, the pH value is used as a main adjusting parameter in the PID control, a slurry supply adjusting volume except the reference slurry supply volume is output according to the difference value between the actual pH value and the pH target value, and a control model adjusts the actual total slurry supply flow through the opening of a slurry supply adjusting valve to realize the automatic control of the slurry volume. Therefore, the slurry supply control method has more guiding significance for the automatic operation of the wet desulphurization device.
Drawings
FIG. 1 is the main logic of the desulfurization island automatic slurry supply control method based on DCS control system;
FIG. 2 is a logic diagram of PID feedback regulation in an embodiment of the invention.
Detailed Description
The technical solution of the present invention is further described in detail by the accompanying drawings and embodiments.
The core of the invention is to establish a rapid optimization model of the slurry supply flow and to clean the flue gas SO through the outlet 2 Concentration feedback, rapid adjustment of the amount of pulp supply adjustment q 1 And PID adjustment amount q 2 To obtain a more accurate supply flow q. Calculating actual liquid-gas ratio (L/G) of parameters by feedforward in the process of flue gas parameter change or switching operation equipment Practice of With raw flue gas SO 2 The concentration is judged according to the liquid-gas ratio, a reasonable pH initial target value and a reference slurry supply quantity are quickly obtained, and the PID adjustment quantity q is adjusted 2 Limiting to reduce pH perturbation and ensure clean flue gas SO 2 The stability of concentration control realizes the automatic control of the pulp supply system.
The invention relates to a DCS control system-based automatic slurry supply control method for a desulfurization island, which specifically comprises the following steps:
firstly, confirming that the quality state and the equipment state of slurry are good, and proposing to set a hardware configuration mode of 'a return pipeline + a main pipeline electric regulating valve' for realizing the linear regulation of slurry supply flow;
secondly, establishing a main body control logic:
according to the measuring point parameters: unit flue gas volume (or unit load), inlet SO 2 Carrying out feedforward calculation on the concentration and the actual circulation volume of the slurry, providing a reference slurry supply volume of slurry supply control and an initial target set value of a pH value, and then putting into PID control, wherein the PID control takes the pH value as a main regulation parameter and outputs the opening of a slurry supply regulating valve to regulate the slurry supply flow;
specifically, the detailed steps of the feedforward calculation include:
step 1) reading parameters of field measuring points: the raw smoke gas amount G; raw flue gas SO 2 Concentration c 1 ；
Step 2), equipment fixing parameters: rated flow of the slurry circulating pump: p is a radical of formula 1 、p 2 、p i 、p n Unit is m 3 H, wherein n is the total number of the slurry circulating pumps, and i is the serial number of the slurry circulating pumps; design maximum flue gas volume G max ；
Design total slurry circulation
Total amount of slurry circulation in real time L 0 Is the sum of the rated flow rates of the operating devices;
step 3) feedforward calculation is based on raw flue gas quantity G and raw flue gas SO 2 Concentration c 1 To obtain a reference stock supply q 0 The calculation formula of the reference pulp supply amount is as follows:
q 0 for the reference stock supply, m 3 /h
c 1 Is raw flue gas SO at the inlet of an absorption tower 2 Concentration, mg/m 3 (standard, dry basis, 6% by weight) 2 )
c 2 To absorbClean flue gas SO at tower outlet 2 Concentration, mg/m 3 (standard, dry basis, 6% 2 )
G is the unit smoke gas volume m 3 H, (standard, dry basis, 6% O 2 )
Rho is the density of limestone slurry (unit: kg/m) 3 ) The corresponding solid content is calculated as ω (unit: %)
Step 4), calibrating and fitting a limestone slurry density and solid content linear curve on site, and determining formula constants C and k:
ρ＝k×ω+C
step 5) calculating actual liquid-gas ratio (L/G) of parameters according to feedforward Practice of With raw flue gas SO 2 Concentration c 1 And judging the liquid-gas ratio to obtain an initial pH target value, so as to determine a reasonable calcium-sulfur ratio interval according to the number of the slurry circulating pumps.
The specific judgment formula is as follows:
if it is
The initial pH value is 5.4;
if it is
The initial pH value is 6;
step 6) calcium-sulfur ratio assignment
According to the pH value, the Ca/S ratio parameter is assigned and substituted into a formula, the pulp supply quantity q and the pulp supply adjustment quantity q are calculated 1 The initial assignment is 0.
The table of the assignment of pH value to calcium-sulfur ratio is shown in Table 1:
TABLE 1
| pH | 6 | 5.8 | 5.6 | 5.4 | 5.2 | 5.0 | 4.8 |
| Ca/S ratio of calcium to sulfur | 1.4 | 1.3 | 1.2 | 1.07 | 1.05 | 1.03 | 1.01 |
Step 7) PID adjustment amount limitation
q 2 Q is PID adjustment amount, and q is used for avoiding too large pH value disturbance caused by PID adjustment 2 The adjustment range of (c) is a recommended limit: -20% q 0 ≤q 2 ≤20％q 0 。
Step 8) outlet flue gas SO 2 Concentration c 2 Determining and adjusting the amount q of pulp supply 1 And (4) assignment is carried out:
if 30mg/m 3 ＞c 2 ≥15mg/m 3 Then q is 1 ＝10％q 0 (pH > 5.6);
if 30mg/m 3 ＞c 2 ≥15mg/m 3 Then q is 1 ＝5％q 0 (ii) a (when the pH value is less than or equal to 5.6);
if c is 2 ≥30mg/m 3 Adjusting the pH target value, and increasing the current pH absolute value to 0.2 to serve as a new pH target value;
if c is 2 <15/m 3 Adjusting the pH target value, and reducing the current pH absolute value by 0.2 to be used as a new pH target value;
step 9) performing circulation judgment according to the outlet SO 2 The output value of the concentration is used as a PID feedback adjustment parameter, PID feedback adjustment logic is shown in figure 2, and if the pH target value is less than 4.8, a liquid-gas ratio adjustment suggestion is output: "reduce or adjust the number of running circulation pumps"; if the pH target value is more than 6, outputting a liquid-gas ratio adjustment suggestion: the number of the circulating pumps put into operation is increased in time, and the discharge value is prevented from exceeding the standard.
The information for triggering PID feedback regulation of the invention is clean flue gas SO 2 Concentration c 2 The upper and lower limit values of (2) can realize automatic optimization and adjustment of pH value, and avoid unreasonable manual setting of pH value and clean flue gas SO 2 The invention realizes the automatic control of the pH value of the slurry, can obtain a reasonable pH target value through repeated cyclic judgment, and avoids the continuous intervention of manual adjustment under the condition of frequent fluctuation of the working condition of the flue gas. The whole process time is short, extra work of operators is not needed, and the method is simple, convenient and quick. The invention defines the intellectualization of the control process, realizes the gradient optimization strategy of the pH value and finally achieves the aim of automatically optimizing the slurry supply control of the DCS control system. In the pH value online optimization process, the pH value triggers the upper limit value and the lower limit value to indicate that the liquid-gas ratio is matched with the calcium-sulfur ratio to have further optimization space, and liquid-gas ratio adjustment suggestion, namely the suggestion for starting and stopping the slurry circulating pump, can be given. The invention defines the outlet SO 2 The accurate control range of the concentration can realize SO 2 The fluctuation of the concentration is not higher than +/-5 mg/m under the steady-state working condition 3 (ii) a Fluctuation of not higher than +/-8 mg/m under unsteady state working condition 3 Compared with the traditional DCS pulp supply control method, the control precision can be improved by at least 50%.
Claims (9)
1. A desulfurization island automatic slurry supply control method based on a DCS control system is characterized in that a desulfurization island is provided with a return pipeline and a main pipeline electric control valve, and the method comprises the following steps:
by using the unit flue gas volume and the unit inlet SO 2 Carrying out feedforward calculation on the concentration and the actual circulation quantity of the slurry to obtain a reference slurry supply quantity of slurry supply control and an initial target set value of a pH value, and then putting the reference slurry supply quantity of slurry supply control and the initial target set value of the pH value into PID control;
and during PID control, the pH value is used as a main adjusting parameter, the pulp supply adjusting amount except the reference pulp supply amount is determined according to the difference value of the actual pH value and the target pH value, the actual total pulp supply flow is adjusted by controlling the opening of the pulp supply adjusting valve, and the control of the size of the pulp in the desulfurization island is realized.
2. The DCS control system-based automatic slurry supply control method for the desulfurization island according to claim 1, wherein the reference slurry supply amount q is 0 The following:
wherein q is 0 For the reference stock supply, m 3 /h；c 1 Is standard, dry basis, 6% O 2 Raw flue gas SO at inlet of absorption tower under condition 2 Concentration; c. C 2 Is standard, dry basis, 6% O 2 Clean flue gas SO at outlet of absorption tower under condition 2 Concentration, mg/m 3 (ii) a G is standard, dry basis, 6% O 2 Flue gas volume of unit under the condition m 3 H; rho is the density of limestone slurry and has the unit of kg/m 3 (ii) a Omega is the solid content of the limestone slurry, and the unit is percent.
3. The method for controlling the automatic slurry supply of the desulfurization island based on the DCS control system according to claim 2, wherein the calculation formula of the density p of the limestone slurry is as follows:
ρ＝k×ω+C
wherein C and k are constants, and C and k are obtained by field calibration fitting of limestone slurry density and solid content linear curves.
4. The method of claim 2, wherein the initial target set value of the pH value is determined according to a liquid-gas ratio, an actual flue gas amount and design parameters.
5. The method for controlling the automatic slurry supply of the desulfurization island based on the DCS control system according to claim 4, wherein the process of determining the initial target set value of the pH value according to the liquid-gas ratio, the actual flue gas volume and the design parameters is as follows:
if it is
The initial target set value of the pH value is 5.4;
if it is
The initial target set value of the pH value is 6;
wherein, (L/G) Practice of For actual liquid-gas ratio (L/G) Design of To design the liquid-gas ratio, c max Is standard, dry basis, 6% O 2 Design SO of raw flue gas at inlet of absorption tower under condition 2 The highest concentration.
6. The method of claim 2, wherein the actual total flow q of the supplied slurry is calculated by the following formula:
wherein,
is calcium sulfurRatio, q 1 Adjustment of the amount for pulp supply, q 2 Is a PID adjustment amount.
7. The DCS control system based automatic slurry supply control method for desulfurization island according to claim 6, wherein the PID adjustment quantity q is 2 The adjustment range of (2) is: -20% q 0 ≤q 2 ≤20％q 0 。
8. The DCS control system based automatic slurry supply control method for desulfurization island according to claim 6, characterized in that the method is based on SO of clean flue gas at the outlet of the absorption tower 2 Concentration c 2 To the adjustment amount q of slurry supply 1 And assigning, comprising the following processes:
when the pH value is more than 5.6, if 30mg/m 3 ＞c 2 ≥15mg/m 3 Then q is 1 ＝10％q 0 ；
When the pH is less than or equal to 5.6, if 30mg/m 3 ＞c 2 ≥15mg/m 3 Then q is 1 ＝5％q 0 ；
If c is 2 ≥30mg/m 3 Adjusting the pH target value, and increasing the current pH absolute value to 0.2 to serve as a new pH target value;
if c is 2 <15/m 3 And adjusting the pH target value, and reducing the current pH absolute value by 0.2 to be used as a new pH target value.
9. The method of claim 8, wherein the slurry supply adjustment q is a value obtained by adding a predetermined amount of slurry to the desulfurization island 1 The initial value is 0.
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Citations (20)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS62204829A (en) * | 1986-03-04 | 1987-09-09 | Babcock Hitachi Kk | Method for desulfurizing wet off-gas |
| JP2001017825A (en) * | 1999-07-07 | 2001-01-23 | Babcock Hitachi Kk | Flue gas desulfurization method and apparatus |
| CN1785483A (en) * | 2005-11-11 | 2006-06-14 | 南京科远控制工程有限公司 | Control method wet method smoke desulfur for elecric power plant |
| CN102553424A (en) * | 2011-11-28 | 2012-07-11 | 中国神华能源股份有限公司 | Method for adjusting pH value of absorption column |
| CN103955751A (en) * | 2014-04-11 | 2014-07-30 | 国家电网公司 | Method for predicting multi-element nonlinear limestone-gypsum wet desulphurization efficiency |
| CN106582284A (en) * | 2016-12-14 | 2017-04-26 | 河南华润电力古城有限公司 | Automatic control method and system of thermal-power-unit SCR denitration ammonia spraying |
| CN107247994A (en) * | 2017-06-22 | 2017-10-13 | 东南大学 | A kind of fuzzy Modeling Method of pallet absorber desulfurization device desulfuration efficiency |
| CN109634315A (en) * | 2018-12-29 | 2019-04-16 | 福建龙净环保股份有限公司 | A kind of method and device controlling plasm PH value |
| CN111229010A (en) * | 2020-01-19 | 2020-06-05 | 福建龙净环保股份有限公司 | Opening control system and opening control method of slurry supply regulating valve |
| CN111450694A (en) * | 2020-04-10 | 2020-07-28 | 大唐环境产业集团股份有限公司 | Desulfurization system industrial controller based on multi-objective optimization and control method |
| CN112206645A (en) * | 2019-07-10 | 2021-01-12 | 内蒙古电力(集团)有限责任公司内蒙古电力科学研究院分公司 | Thermal power plant desulfurization efficiency control method and system |
| CN112569760A (en) * | 2020-11-19 | 2021-03-30 | 西安热工研究院有限公司 | Wet desulphurization adjustment slurry supply method |
| CN112619389A (en) * | 2020-11-19 | 2021-04-09 | 内蒙古蒙达发电有限责任公司 | Method and system for optimizing control of slurry supply of limestone-wet desulphurization system |
| CN113058417A (en) * | 2021-04-15 | 2021-07-02 | 大唐环境产业集团股份有限公司 | Control device suitable for restraining pH fluctuation of carbide slag flue gas desulfurization slurry |
| CN113457402A (en) * | 2021-06-30 | 2021-10-01 | 华能左权煤电有限责任公司 | Efficient composite slurry supply method for desulfurizing tower |
| CN113648800A (en) * | 2021-08-16 | 2021-11-16 | 浙江浩普智能科技有限公司 | Wet desulphurization pH value prediction control method and system |
| US20220040633A1 (en) * | 2020-08-05 | 2022-02-10 | Shang'an Power Plant Of Huaneng Power International Inc. | Automatic control system for emission indexes of desulfurization device of thermal power unit and method thereof |
| CN114307571A (en) * | 2021-11-26 | 2022-04-12 | 华能沁北发电有限责任公司 | Novel carbide slag slurry supply system and method |
| CN114740713A (en) * | 2021-12-31 | 2022-07-12 | 北京工业大学 | Multi-objective optimization control method for wet flue gas desulfurization process |
| CN115400571A (en) * | 2022-08-31 | 2022-11-29 | 华能湖南岳阳发电有限责任公司 | Automatic slurry supply method and device for desulfurization absorption tower |
-
2023
- 2023-01-16 CN CN202310065996.3A patent/CN115970476B/en active Active
Patent Citations (20)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS62204829A (en) * | 1986-03-04 | 1987-09-09 | Babcock Hitachi Kk | Method for desulfurizing wet off-gas |
| JP2001017825A (en) * | 1999-07-07 | 2001-01-23 | Babcock Hitachi Kk | Flue gas desulfurization method and apparatus |
| CN1785483A (en) * | 2005-11-11 | 2006-06-14 | 南京科远控制工程有限公司 | Control method wet method smoke desulfur for elecric power plant |
| CN102553424A (en) * | 2011-11-28 | 2012-07-11 | 中国神华能源股份有限公司 | Method for adjusting pH value of absorption column |
| CN103955751A (en) * | 2014-04-11 | 2014-07-30 | 国家电网公司 | Method for predicting multi-element nonlinear limestone-gypsum wet desulphurization efficiency |
| CN106582284A (en) * | 2016-12-14 | 2017-04-26 | 河南华润电力古城有限公司 | Automatic control method and system of thermal-power-unit SCR denitration ammonia spraying |
| CN107247994A (en) * | 2017-06-22 | 2017-10-13 | 东南大学 | A kind of fuzzy Modeling Method of pallet absorber desulfurization device desulfuration efficiency |
| CN109634315A (en) * | 2018-12-29 | 2019-04-16 | 福建龙净环保股份有限公司 | A kind of method and device controlling plasm PH value |
| CN112206645A (en) * | 2019-07-10 | 2021-01-12 | 内蒙古电力(集团)有限责任公司内蒙古电力科学研究院分公司 | Thermal power plant desulfurization efficiency control method and system |
| CN111229010A (en) * | 2020-01-19 | 2020-06-05 | 福建龙净环保股份有限公司 | Opening control system and opening control method of slurry supply regulating valve |
| CN111450694A (en) * | 2020-04-10 | 2020-07-28 | 大唐环境产业集团股份有限公司 | Desulfurization system industrial controller based on multi-objective optimization and control method |
| US20220040633A1 (en) * | 2020-08-05 | 2022-02-10 | Shang'an Power Plant Of Huaneng Power International Inc. | Automatic control system for emission indexes of desulfurization device of thermal power unit and method thereof |
| CN112569760A (en) * | 2020-11-19 | 2021-03-30 | 西安热工研究院有限公司 | Wet desulphurization adjustment slurry supply method |
| CN112619389A (en) * | 2020-11-19 | 2021-04-09 | 内蒙古蒙达发电有限责任公司 | Method and system for optimizing control of slurry supply of limestone-wet desulphurization system |
| CN113058417A (en) * | 2021-04-15 | 2021-07-02 | 大唐环境产业集团股份有限公司 | Control device suitable for restraining pH fluctuation of carbide slag flue gas desulfurization slurry |
| CN113457402A (en) * | 2021-06-30 | 2021-10-01 | 华能左权煤电有限责任公司 | Efficient composite slurry supply method for desulfurizing tower |
| CN113648800A (en) * | 2021-08-16 | 2021-11-16 | 浙江浩普智能科技有限公司 | Wet desulphurization pH value prediction control method and system |
| CN114307571A (en) * | 2021-11-26 | 2022-04-12 | 华能沁北发电有限责任公司 | Novel carbide slag slurry supply system and method |
| CN114740713A (en) * | 2021-12-31 | 2022-07-12 | 北京工业大学 | Multi-objective optimization control method for wet flue gas desulfurization process |
| CN115400571A (en) * | 2022-08-31 | 2022-11-29 | 华能湖南岳阳发电有限责任公司 | Automatic slurry supply method and device for desulfurization absorption tower |
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