CN212833139U - Automatic dosing control system of wastewater softening pretreatment system - Google Patents
Automatic dosing control system of wastewater softening pretreatment system Download PDFInfo
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- CN212833139U CN212833139U CN202020646617.1U CN202020646617U CN212833139U CN 212833139 U CN212833139 U CN 212833139U CN 202020646617 U CN202020646617 U CN 202020646617U CN 212833139 U CN212833139 U CN 212833139U
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Abstract
The utility model discloses an automatic dosing control system of a wastewater softening pretreatment system, which comprises a feed-forward water amount compensation module, a first dosing pump flow control module, a second dosing pump flow control module, a hydroxyl alkalinity feedback control module, a pH control module, a carbonate alkalinity feedback control module, a water inlet flow meter arranged at the inlet of a magnesium removal reaction unit, a pH monitor arranged on a pipeline between the magnesium removal reaction unit and a calcium removal reaction unit, an online alkalinity monitor arranged at the outlet of a clarification unit, a first frequency converter used for controlling an alkali liquor dosing pump and a second frequency converter used for controlling a sodium carbonate dosing pump, the system can change the alkalinity of the effluent carbonate and the alkalinity of the hydroxyl in real time and the fluctuation condition of the inflow water, the adding amount of the sodium hydroxide/lime alkali liquor and the sodium carbonate is fed back and adjusted in time so as to stably control the hardness of calcium ions and the hardness of magnesium ions in the softened water.
Description
Technical Field
The utility model belongs to the waste water treatment field relates to a waste water softens pretreatment systems automatic reagent feeding control system.
Background
With the increasingly prominent environmental problems in China and the increasingly strict national environmental emission standards, more and more thermal power plants are required to realize advanced treatment and reuse, even zero discharge, of wastewater, and the treatment of desulfurization wastewater and circulating water sewage is particularly taken as a key point. Because the desulfurization wastewater and the circulating water sewage are generally high in hardness and contain a large amount of calcium and magnesium ions which are easy to scale, in the deep treatment and reuse process, in order to prevent the subsequent membrane concentration system from scaling, lime-sodium carbonate or sodium hydroxide-sodium carbonate is generally adopted for softening pretreatment. The softening process mainly takes place in two core reactions:
Mg2++2OH-→Mg(OH)2↓
Ca2++CO3 2-→CaCO3↓
the quality of the softening effect directly determines the operation stability and reliability of the subsequent membrane concentration system and even the whole advanced treatment system. From the aspects of zero discharge of a large amount of put-into-service desulfurization wastewater and the advanced treatment engineering of circulating water, the softening pretreatment system generally has the problem that the hardness of calcium and magnesium ions in effluent is difficult to stably control due to fluctuation of water quantity and quality, insufficient dosing precision and the like, and the whole system is shut down for a long time even due to poor operation effect of the softening pretreatment system in individual engineering.
In order to ensure that calcium ions and magnesium ions in effluent of a softening pretreatment system are kept as stable as possible, some power plants adopt a method of excessively adding sodium hydroxide and sodium carbonate medicaments, so that not only is the consumption of the medicaments obviously increased, but also a large amount of acid liquor is consumed in subsequent pH adjustment. Therefore, some researchers propose a scheme for realizing stable operation of a softening pretreatment system by measuring calcium and magnesium ions in the inlet water on line and feedforward controlling the dosage of the softening agent, however, the measurement error of the calcium and magnesium ions is large under the condition of high salt and high hardness, and the dosing accuracy and stability are still difficult to guarantee.
In fact, as known from the chemical equilibrium principle, when the precipitate reaches the equilibrium state of dissolution of the precipitate in the solution, the product of the powers of the concentrations of the ion ions participating in the precipitation is a constant, which is called the solubility product constant, and in the case of calcium carbonate precipitation, the concentration product is calculated as:
in the formula, C (Ca)2+) Is the molar concentration of the calcium ions,
is the molar concentration of the carbonate radical,
is the product constant of the ionic concentration of calcium carbonate.
Accordingly, the calcium ion concentration in the solution under certain conditions is:
from this, it is found that the calcium ion concentration in the solution is negatively correlated with the carbonate ion concentration. In different high-salt complex wastewater systems, due to the existence of the homoionic effect and the salt effect,
the difference is large and difficult to measure, but the negative dependence of the calcium ion concentration on the carbonate concentration is always present. Therefore, in actual operation, the carbonate concentration can be determined to be maintained within a certain reasonable excess range through debugging or experiments, so that the calcium ion hardness can be indirectly regulated and controlled to be maintained at a certain lower expected level; similarly, the hardness of the magnesium ions in the effluent can be indirectly regulated by controlling the excessive degree of the hydroxide concentration. The existing engineering practice shows that the control of the hardness of magnesium ions in effluent by simply adjusting pH easily causes excessive addition of alkali liquor and overlarge pH oscillation amplitude.
According to water quality analytical chemistry, the alkalinity of a general solution generally consists of three parts of hydroxide, carbonate and bicarbonate, and the alkalinity can be measured by a titration method or an on-line potentiometric titration method, and the measurement process is simpler, more reliable and more stable than the measurement of the hardness of calcium and magnesium ions. In engineering applications, the carbonate concentration in the wastewater may be approximately considered equal to the carbonate alkalinity, and the hydroxide concentration may be approximately considered equal to the hydroxide alkalinity. Therefore, the hardness of the calcium and magnesium ions in the effluent is indirectly regulated and controlled by monitoring and regulating the alkalinity of the effluent of the softening pretreatment system, the reliability and the stability of the softening pretreatment system are greatly improved, and the softening pretreatment system has the advantage of simple and convenient operation.
SUMMERY OF THE UTILITY MODEL
An object of the utility model is to overcome above-mentioned prior art's shortcoming, a wastewater softening pretreatment system automatic reagent feeding control system is provided, this system can be according to the real-time change of play water carbonate basicity and hydroxyl basicity and the undulant condition of the flow of intaking, and the dosage of timely feedback adjustment sodium hydroxide lime alkali lye and sodium carbonate to stable control softens out water calcium ion hardness and magnesium ion hardness, avoids the medicament to throw and throws excessive waste or throw the water quality of water that influences inadequately.
In order to achieve the purpose, the automatic dosing control device of the wastewater softening pretreatment system comprises a magnesium removal reaction unit, a calcium removal reaction unit and a clarification unit which are sequentially communicated, wherein a dosing port of the magnesium removal reaction unit is communicated with an alkali liquor dosing pump, a dosing port of the calcium removal reaction unit is communicated with a sodium carbonate dosing pump, an inlet of the alkali liquor dosing pump is communicated with an alkali liquor storage box, and an inlet of the sodium carbonate dosing pump is communicated with a sodium carbonate solution box;
the control device comprises a feed-forward water amount compensation module, a first dosing pump flow control module, a second dosing pump flow control module, a hydroxyl alkalinity feedback control module, a pH control module, a carbonate alkalinity feedback control module, a water inlet flow meter arranged at an inlet of a magnesium removal reaction unit, a pH monitor arranged on a pipeline between the magnesium removal reaction unit and a calcium removal reaction unit, an online alkalinity monitor arranged at an outlet of a clarification unit, a first frequency converter for controlling an alkali liquor dosing pump and a second frequency converter for controlling a sodium carbonate dosing pump;
the output end of the water inlet flow meter is connected with the input end of the feed-forward water amount compensation module, and the output end of the feed-forward water amount compensation module is connected with the input end of the first dosing pump flow control module and the input end of the second dosing pump flow control module;
the input end of the hydroxyl alkalinity feedback control module is connected with one output end of the on-line alkalinity monitor, the output end of the hydroxyl alkalinity feedback control module is connected with the input end of the first dosing pump flow control module, the output end of the pH monitor is connected with the input end of the pH control module, the output end of the pH control module is connected with the input end of the first dosing pump flow control module, and the output end of the first dosing pump flow control module is connected with the control end of the first frequency converter;
the input end of the carbonate alkalinity feedback control module is connected with the other output end of the on-line alkalinity monitor, the output end of the carbonate alkalinity feedback control module is connected with the input end of the second dosing pump flow control module, and the output end of the second dosing pump flow control module is connected with the control end of the second frequency converter.
The utility model discloses following beneficial effect has:
the utility model discloses an automatic dosing control system of a wastewater softening pretreatment system, which controls the dosing flow of an alkali liquor dosing pump according to the hydroxide radical alkalinity of effluent of a clarification unit, the inflow detected by an inflow flowmeter and the current pH value of effluent of a magnesium removal reaction unit during specific operation; according to the current value OP of carbonate alkalinity of effluent of the clarification unitCalcium carbonate(t) controlling the dosing flow of a sodium carbonate dosing pump by using the water inlet flow acquired by a water inlet flow meter so as to realize timely feedback adjustment of the dosing amounts of the sodium hydroxide/lime alkali liquor and the sodium carbonate according to the real-time change of the carbonate alkalinity and the hydroxyl alkalinity of the effluent and the fluctuation condition of the water inlet flow, thereby achieving the purpose of stably controlling the hardness of softened calcium ions and magnesium ions in the effluent and avoiding the waste caused by excessive dosing or the influence on the effluent quality caused by insufficient dosing of the medicament.
Drawings
FIG. 1 is a block diagram of the present invention;
1 is the magnesium removal reaction unit, 2 is the calcium removal reaction unit, 3 is the clarification unit, 4 is the alkali lye storage tank, 5 is the alkali lye dosing pump, 6 is the sodium carbonate dosing pump, 7 is the sodium carbonate solution case, 81 is the inflow flowmeter, 82 is the pH monitor, 83 is online basicity monitor, 9 is first converter, 10 is the second converter, 111 is first dosing pump flow control module, 112 is the pH control module, 113 is the second dosing pump flow control module, 114 is hydroxyl basicity feedback control module, 115 is carbonate basicity feedback control module, 116 is feed forward water compensation module.
Detailed Description
The present invention will be described in further detail with reference to the accompanying drawings:
referring to fig. 1, the automatic dosing control device of the wastewater softening pretreatment system of the utility model comprises a magnesium removal reaction unit 1, a calcium removal reaction unit 2 and a clarification unit 3 which are sequentially communicated, wherein a dosing port of the magnesium removal reaction unit 1 is communicated with an alkali liquor dosing pump 5, a dosing port of the calcium removal reaction unit 2 is communicated with a sodium carbonate dosing pump 6, an inlet of the alkali liquor dosing pump 5 is communicated with an alkali liquor storage tank 4, and an inlet of the sodium carbonate dosing pump 6 is communicated with a sodium carbonate solution tank 7; the control device comprises a feed-forward water amount compensation module 116, a first dosing pump flow control module 111, a second dosing pump flow control module 113, a hydroxyl alkalinity feedback control module 114, a first dosing pump flow control module 111, a pH control module 112, a carbonate alkalinity feedback control module 115, a water inlet flow meter 81 arranged at the inlet of the magnesium removal reaction unit 1, a pH monitor 82 arranged on a pipeline between the magnesium removal reaction unit 1 and the calcium removal reaction unit 2, an online alkalinity monitor 83 arranged at the outlet of the clarification unit 3, a first frequency converter 9 used for controlling an alkali liquor dosing pump 5 and a second frequency converter 10 used for controlling a sodium carbonate dosing pump 6;
the output end of the water inlet flow meter 81 is connected with the input end of the feed-forward water amount compensation module 116, and the output end of the feed-forward water amount compensation module 116 is connected with the input end of the first dosing pump flow control module 111 and the input end of the second dosing pump flow control module 113; the input end of the hydroxyl alkalinity feedback control module 114 is connected with one output end of the online alkalinity monitor 83, the output end of the hydroxyl alkalinity feedback control module 114 is connected with the input end of the first dosing pump flow control module 111, the output end of the pH monitor 82 is connected with the input end of the pH control module 112, the output end of the pH control module 112 is connected with the input end of the first dosing pump flow control module 111, and the output end of the first dosing pump flow control module 111 is connected with the control end of the first frequency converter 9; the input end of the carbonate alkalinity feedback control module 115 is connected with the other output end of the online alkalinity monitor 83, the output end of the carbonate alkalinity feedback control module 115 is connected with the input end of the second dosing pump flow control module 113, and the output end of the second dosing pump flow control module 113 is connected with the control end of the second frequency converter 10.
When the utility model works, the hardness control of magnesium ions and the hardness control of calcium ions are included;
the specific process of controlling the hardness of the magnesium ions is as follows:
presetting the optimal value OP of the hydroxide alkalinity required when the hardness of the magnesium ions in the effluent of the clarifying unit 3 is maintained within the preset magnesium ion hardness rangest, magnesiumAnd a tolerable upper limit value OP of the hydroxide alkalinityMagnesium, upper limitAnd a lower limit value of hydroxyl alkalinity OPLower limit of magnesium；
The hydroxyl alkalinity feedback control module 114 detects the current value OP of the hydroxyl alkalinity of the effluent of the clarification unit 3 according to the online alkalinity monitor 83Magnesium alloy(t) and a set value OPst, magnesiumThe difference value between the alkali liquor dosing pump 5 and the current control period is the dosing flow Q of the alkali liquor dosing pump 51(t) is:
Q1(t)＝Q1,t-1+ΔQ11(t) (1)
wherein Q is1,t-1The dosage flow, delta Q, of the alkali liquor dosage pump 5 in the last control period11(t) is the dosage increment of the alkali liquor dosage pump 5 in the current control period, wherein, delta Q11The expression of (t) is:
ΔQ11(t)＝-k1[OPmagnesium alloy(t)-OPst, magnesium] (2)
Wherein k is1Adding the chemical coefficient to the alkali liquor;
when OPMagnesium alloy(t)>OPMagnesium, upper limit，ΔQ11The expression of (t) is:
ΔQ11(t)＝-k1[OPmagnesium, upper limit-OPLower limit of magnesium] (3)
When OPMagnesium alloy(t)<OPLower limit of magnesium，ΔQ11The expression of (t) is:
ΔQ11(t)＝-k1[OPlower limit of magnesium-OPMagnesium, upper limit] (4)
Meanwhile, the feed-forward water amount compensation module 116 detects the inflow water amount through the inflow water flowmeter 81, and when the variation amplitude of the inflow water amount exceeds the preset value FstWhen it is, thenCalculating feed-forward water quantity compensation delta Q12(t), then the first frequency converter 9 is controlled by the first dosing pump flow control module 111, so that the dosing flow increment of the alkali liquor dosing pump 5 is delta Q12(t)+ΔQ11(t) when the variation range of the water inlet quantity does not exceed the preset value FstMeanwhile, the first chemical feeding pump flow control module 111 controls the first frequency converter 9, so that the chemical feeding flow increment of the alkali liquor chemical feeding pump 5 is delta Q11(t) wherein the feed forward water amount compensation Δ Q12The expression of (t) is:
wherein q istIs the arithmetic mean value of the water inlet flow in the current control period, qt-1The average value of the water inlet flow in the previous control period is obtained;
meanwhile, the protective lower limit value pH of the effluent pH of the magnesium removal reaction unit 1 is presetstThe pH control module 112 detects the current pH value and pH value of the effluent of the magnesium removal reaction unit 1 through the pH monitor 821When pH is higher1＜pHstThen calculate the pH enhanced feedback compensation Δ Q13(t), the first frequency converter 9 is controlled by the first dosing pump flow control module 111, and the dosing flow increment of the alkali liquor dosing pump 5 is increased to delta Q12(t)+ΔQ11(t)+ΔQ13(t)，ΔQ13The expression of (t) is:
ΔQ13(t)＝-k1[OPlower limit of magnesium-OPMagnesium, upper limit] (6)
The specific process of controlling the calcium ion hardness is as follows:
presetting an optimal carbonate alkalinity value OP required when the calcium ion hardness of the effluent of the clarification unit 3 is maintained within a preset calcium ion hardness rangest, calciumAnd an upper limit value OP of the tolerable carbonate alkalinityCalcium, upper limitAnd a lower limit of carbonate alkalinity OPCalcium, lower limitThe carbonate alkalinity feedback control module 115 detects the current carbonate alkalinity value OP of the effluent of the clarification unit 3 according to the online alkalinity monitor 83Calcium carbonate(t) and OPst, calciumDifference between themCalculating the medicine adding flow Q of the sodium carbonate medicine adding pump 6 in the current control period2(t)：
Q2(t)＝Q2,t-1+ΔQ21(t) (7)
Wherein Q is2,t-1The adding flow rate, delta Q, of the sodium carbonate adding pump 6 for the last control period21(t) is the dosage increment of the sodium carbonate dosage pump 6 in the current control period, delta Q21The expression of (t) is:
ΔQ21(t)＝-k2[OPcalcium carbonate(t)-OPst, calcium] (8)
Wherein k is2Adding the chemical coefficient to sodium carbonate;
when OPCalcium carbonate(t)>OPCalcium, upper limit，ΔQ21The expression of (t) is:
ΔQ21(t)＝-k2[OPcalcium, upper limit-OPCalcium, lower limit] (9)
When OPCalcium carbonate(t)<OPCalcium, lower limit，ΔQ21The expression of (t) is:
ΔQ21(t)＝-k2[OPcalcium, lower limit-OPCalcium, upper limit] (10)
Meanwhile, the feed-forward water amount compensation module 116 collects the inflow water amount through the inflow water flowmeter 81, and when the variation amplitude of the inflow water amount in the control period exceeds the preset value FstThen, calculating feed-forward compensation delta Q of water inlet flow22(t), the second frequency converter 10 is controlled by the second dosing pump flow control module 113, so that the dosing flow increment of the sodium carbonate dosing pump 6 is delta Q21(t)+ΔQ22(t) when the variation amplitude of the inflow water flow in the control period does not exceed the preset value FstIn the meantime, the second frequency converter 10 is controlled by the second dosing pump flow control module 113, so that the dosing flow increment of the sodium carbonate dosing pump 6 is delta Q21(t) wherein the feed-forward compensation of the inflow Δ Q22The expression of (t) is:
it should be noted that the utility model mainly uses the main feedback control of hydroxyl alkalinity and carbonate alkalinity, realizes the automatic regulation and control of the softening agent addition of the softening pretreatment system, and has the characteristics of strong water quality impact load resistance, simple and flexible monitoring and the like compared with the method of directly monitoring the hardness of calcium and magnesium ions in the effluent to feed back the dosage; and simultaneously, the utility model discloses the situation of change according to the play water basicity is provided with two kinds of control methods of weak feedback and strong feedback in fact, can adapt to the fluctuation by a wide margin of quality of water sooner.
In addition, the fluctuation change of the water inflow amount is quickly responded through the feed-forward water amount compensation module 116, so that the stability of the quality of the outlet water of the softening pretreatment system is stably ensured.
Finally, the utility model discloses need not to survey high concentration calcium, the magnesium ion content that is difficult to accurate detection in coming the aquatic, overcome feed forward control alkali lye and sodium carbonate solution and thrown the shortcoming that the precision is difficult to the accurate guarantee. Simultaneously, still can set up out water calcium ion hardness, magnesium ion hardness and pH monitoring instrument as required, but its data only regard as its operation reference data, do not participate in the control to can regard as the verification or the contrast foundation that judge detection automatic reagent feeding control system running state, the operating personnel of being convenient for in time discover, overhaul relevant trouble instrument, in addition, the utility model provides an operation is all realized through adder, subtracter, multiplier, divider and comparator.
Claims (1)
1. An automatic dosing control system of a wastewater softening pretreatment system is characterized in that the wastewater softening pretreatment system comprises a magnesium removal reaction unit (1), a calcium removal reaction unit (2) and a clarification unit (3) which are sequentially communicated, wherein a dosing port of the magnesium removal reaction unit (1) is communicated with an alkali liquor dosing pump (5), a dosing port of the calcium removal reaction unit (2) is communicated with a sodium carbonate dosing pump (6), an inlet of the alkali liquor dosing pump (5) is communicated with an alkali liquor storage tank (4), and an inlet of the sodium carbonate dosing pump (6) is communicated with a sodium carbonate solution tank (7);
the control device comprises a feed-forward water quantity compensation module (116), a first dosing pump flow control module (111), a second dosing pump flow control module (113), a hydroxyl alkalinity feedback control module (114), a pH control module (112), a carbonate alkalinity feedback control module (115), a water inlet flow meter (81) arranged at the inlet of the magnesium removal reaction unit (1), a pH monitor (82) arranged on a pipeline between the magnesium removal reaction unit (1) and the calcium removal reaction unit (2), an online alkalinity monitor (83) arranged at the outlet of the clarification unit (3), a first frequency converter (9) used for controlling the alkali liquor dosing pump (5) and a second frequency converter (10) used for controlling the sodium carbonate dosing pump (6);
the output end of the water inlet flow meter (81) is connected with the input end of a feed-forward water quantity compensation module (116), and the output end of the feed-forward water quantity compensation module (116) is connected with the input end of a first dosing pump flow control module (111) and the input end of a second dosing pump flow control module (113);
the input end of the hydroxyl alkalinity feedback control module (114) is connected with one output end of an online alkalinity monitor (83), the output end of the hydroxyl alkalinity feedback control module (114) is connected with the input end of a first dosing pump flow control module (111), the output end of the pH monitor (82) is connected with the input end of a pH control module (112), the output end of the pH control module (112) is connected with the input end of the first dosing pump flow control module (111), and the output end of the first dosing pump flow control module (111) is connected with the control end of a first frequency converter (9);
the input end of the carbonate alkalinity feedback control module (115) is connected with the other output end of the online alkalinity monitor (83), the output end of the carbonate alkalinity feedback control module (115) is connected with the input end of the second dosing pump flow control module (113), and the output end of the second dosing pump flow control module (113) is connected with the control end of the second frequency converter (10).
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