CN112275121B - Wet desulphurization water balance control system and control method - Google Patents
Wet desulphurization water balance control system and control method Download PDFInfo
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- CN112275121B CN112275121B CN202011119113.5A CN202011119113A CN112275121B CN 112275121 B CN112275121 B CN 112275121B CN 202011119113 A CN202011119113 A CN 202011119113A CN 112275121 B CN112275121 B CN 112275121B
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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
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/77—Liquid phase processes
- B01D53/78—Liquid phase processes with gas-liquid contact
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- B01D45/00—Separating dispersed particles from gases or vapours by gravity, inertia, or centrifugal forces
- B01D45/04—Separating dispersed particles from gases or vapours by gravity, inertia, or centrifugal forces by utilising inertia
- B01D45/06—Separating dispersed particles from gases or vapours by gravity, inertia, or centrifugal forces by utilising inertia by reversal of direction of flow
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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
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/46—Removing components of defined structure
- B01D53/48—Sulfur compounds
- B01D53/50—Sulfur oxides
- B01D53/507—Sulfur oxides by treating the gases with other liquids
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2258/00—Sources of waste gases
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- B01D2258/0283—Flue gases
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Abstract
The invention relates to the technical field of flue gas treatment, and particularly discloses a wet desulphurization water balance control system and a control method. Comprises an absorption tower and a demisting tower which are connected in series; a secondary demisting area is arranged in the demisting tower; the demisting tower, the cyclone feeding pump, the first cyclone, the suspension filter and the demister flushing water tank are sequentially connected through a pipeline, and the pit collects the bottom flow of the first cyclone and returns to the absorption tower through the pit pump; the inlet of a demister washing water pump is connected with a demister washing water tank and a process water tank, and the outlet of the demister washing water pump is connected with a demister washing water pipeline; the demister is independent from the absorption tower in the form of the series connection of the demisting towers, washing water of the demister in the demisting tower is filtered and then recycled, the inner circulation system is independent from the absorption tower, the total process water entering the desulfurization system can be effectively controlled, a larger adjusting range can be reserved for the desulfurization tower, and the working condition of low inlet smoke temperature is adapted.
Description
Technical Field
The invention relates to the technical field of flue gas treatment, in particular to a wet desulphurization water balance control system and a control method.
Background
Limestone-gypsum wet flue gas desulfurization technology is the most widely used method for flue gas desulfurization of coal-fired power plants in the world at present. In the domestic flue gas treatment process, a low-temperature economizer is usually arranged at the front end of a wet electric dust collector, on one hand, the waste heat of the flue gas can be recovered, on the other hand, the fly ash specific resistance of the dust collector is reduced, and the dust collection is facilitated. However, in the actual operation process of the desulfurization system with the low-temperature economizer, the temperature of the flue gas is often lower than 90 ℃. Because the flue gas temperature is too low, the evaporation capacity of water in the absorption tower is reduced, and the actual water consumption of the system is reduced. However, the water consumption of the system cannot be basically changed under certain design conditions, so that the water balance of the desulfurization system cannot be ensured when the water supplement amount of the system far exceeds the water consumption of the system.
In a wet flue gas desulfurization system, water balance data is an important basis for system design and also an important parameter for operation management. The water consumption points of the wet desulphurization system mainly comprise: water carried into the atmosphere by flue gas in gaseous form (i.e. water evaporated in the tower), water carried into the atmosphere by flue gas in liquid form, adhering water and crystal water when gypsum is discharged, and desulfurization waste water discharged from the FGD system.
To maintain proper operation of the system, the same amount of water consumed by the system must be replenished. This mainly realizes through the sparge water of defroster, and remaining thick liquid guarantees the normal operating of defroster when the defroster was not only washed to the defroster sparge water, still plays the effect of adjusting absorption tower liquid level balance. The consumption of the washing water is large and is about 58% -68% of the total water consumption of the whole FGD system, and meanwhile, the washing water of the demister is used as the make-up water of the FGD system and enters the slurry tank of the absorption tower to play a role in adjusting the liquid level balance of the absorption tower. Therefore, when the water consumption of the system is reduced, if clean industrial water is still used as a demister washing water source, the supplementary water amount exceeds the water amount consumed by the FGD system, so that the water balance imbalance is caused, and at the moment, the system flow needs to be optimized, and the water balance of the system needs to be reestablished.
Disclosure of Invention
The invention solves the problems that: in the prior art, when the temperature of inlet smoke is low, the water balance in a desulfurizing tower is difficult to control, and a wet desulphurization water balance control system and a control method are provided.
The wet desulphurization water balance control system comprises an absorption tower, a demisting tower, a first cyclone, a suspension filter with back flush, a demister flushing water tank, a demister flushing water pump, a pit, a process water tank and a process water pump;
the flue gas of the absorption tower and the flue gas of the demisting tower enter from bottom to top and are connected in series by a flue; the absorption tower comprises an oxidation area, an absorption area and a primary demisting area; the demisting tower comprises a liquid holding area and a secondary demisting area;
the liquid holding area is connected with an inlet of a cyclone feeding pump through a pipeline, an outlet of the cyclone feeding pump is connected with a first cyclone through a pipeline, an upper outlet of the cyclone is sequentially connected with a suspension filter and a demister flushing water tank in series through a pipeline, a lower outlet of the cyclone is connected to a pit through a pipeline, a pit pump is arranged beside the pit, and the pit, the pit pump and an absorption tower are sequentially connected through a pipeline;
the primary demisting zone and the secondary demisting zone are both provided with demister flushing water pipes, the demister flushing water pipes are connected with a demister flushing water pump, inlet pipes of the demister flushing water pump are respectively connected with a demister flushing water tank and a process water tank in a parallel mode, pipelines are switched by valves, and the process water tank, the process water pump and the absorption tower are sequentially connected through pipelines; the demister is independent from the absorption tower in a mode of connecting the demisting towers in series, washing water of the demister in the demisting tower is filtered and then recycled, an internal circulation system independent from the absorption tower is formed, the situation that the washing water of the demister directly and completely falls into the absorption tower to cause uncontrollable increase of the liquid level of the absorption tower can be avoided, and a proper amount of process water can be supplemented according to the real-time liquid level value of the absorption tower.
The absorption tower, the demisting tower, the demister flushing water tank, the process water tank and the pit are all provided with liquid level meters, so that the water balance can be conveniently adjusted.
Furthermore, the absorption tower is also provided with a gypsum discharge pump and a second cyclone which are sequentially connected in series through a pipeline, the upper outlet of the second cyclone is connected to the feed inlet of the vacuum belt dehydrator through a pipeline, the lower outlet of the second cyclone is connected with the pit through a pipeline, filtrate water of the vacuum belt dehydrator flows into the pit through a pipeline, the outlet pipeline of the pit pump is also provided with a branch pipeline communicated to the pulping pool, the outlet pipeline of the process water pump is provided with a branch pipeline communicated to the pulping pool, the pulping pool is provided with a limestone slurry feeding pump, and the pulping pool, the limestone slurry feeding pump and the absorption tower are sequentially connected through pipelines; the pit is provided with a wastewater feeding pump which is connected with a wastewater system through a pipeline, slurry in the process of a gypsum dewatering system is recycled into the pit, one part of the slurry is used for pulping, and the other part of the slurry is returned into the absorption tower, so that the whole system except wastewater discharge and gypsum carrying water is in large internal circulation, the supplement of extra process water is reduced, and the increase of water balance burden is prevented.
Furthermore, a branch is arranged on an outlet pipeline of the process water pump and used for machine seal cooling water, oxidation fan cooling water and vacuum pump working fluid of each pump, the branch process water is collected to a reuse water tank through a pipeline, the reuse water tank is conveyed to a demister flushing water tank through a reuse water pump, process water supplement in the system is reduced, and water balance adjusting capacity is improved.
Furthermore, a branch pipeline leading to the filter cloth flushing water tank is arranged at the outlet of the reuse water pump and is used for flushing the vacuum belt dehydrator.
Furthermore, the one-level defogging area is tubular defroster or baffle formula defroster, has the effect of initial effect defogging, and is difficult for the scale deposit.
Furthermore, the second-stage demisting zone is a tube bundle type demister or a multi-stage baffle type demister or the combination of the two, further catches droplets in the flue gas, and ensures demisting efficiency.
In another aspect of the invention, a wet desulphurization water balance control method is provided, a demisting tower is connected in series behind an absorption tower, most demisting equipment is arranged in a secondary demisting area of the demisting tower, only a primary demisting area with primary demisting is reserved in the absorption tower, a demister flushing water pump is started at regular time, washing the first-stage demisting area and the second-stage demisting area in sequence in a subarea manner, wherein the washing water in the first-stage demisting area falls into the bottom of the absorption tower to be used as water supplement, the washing water in the second-stage demisting area is collected by the demisting tower, the collected flushing water is conveyed to a first cyclone through a cyclone feeding pump for impurity removal, the flushing water with low impurity flows into a suspension filter with back flush, filtered water enters a demister flushing water tank, secondary utilization washing is carried out by a demister flushing water pump, high-impurity flushing water separated by a first cyclone flows into a pit, and the high-impurity flushing water returns to an absorption tower through a pit pump.
Furthermore, the absorption tower, the demisting tower, the demister flushing water tank, the process water tank and the pit are all provided with liquid level meters; the demisting tower and the pit are always kept at low liquid levels; the inlet pipeline of the demister washing water pump is also connected with the process water tank, when the demister is washed, water is preferentially supplied by the demister washing water tank, when the liquid level of the demister washing water tank is low, water is supplied by the process water tank, and when the process water tank supplies water, the secondary demisting zone is preferentially washed; the process water tank is provided with a process water pump, and when the liquid level of the absorption tower is low, the process water pump supplies water to the absorption tower.
And further, collecting machine seal cooling water, oxidation fan cooling water and vacuum pump working solution of each pump to a reuse water tank through pipelines, and conveying the reuse water to a demister flushing water tank or a filter cloth flushing water tank in a vacuum belt dewatering system through a reuse water pump for secondary utilization.
Further, the process slurry flowing out of the gypsum cyclone and the vacuum belt dehydrator equipment for gypsum dehydration is collected into a pit, and the slurry in the pit is returned to the absorption tower and is conveyed to the slurry preparing pool for slurry preparation.
The invention has the beneficial effects that:
1. the demister is independent from the absorption tower in a mode of connecting the demisting towers in series, washing water of the demister in the demisting tower is filtered and then recycled to form an internal circulation system independent from the absorption tower, the situation that the washing water of the demister directly and completely falls into the absorption tower to cause uncontrollable increase of the liquid level of the absorption tower can be avoided, and a proper amount of process water can be supplemented according to the real-time liquid level value of the absorption tower.
2. The invention adjusts the water balance through the liquid level meter; the demisting tower and the pit are always kept at low liquid level through the conveying of each pump; the inlet pipeline of the demister washing water pump is also connected with the process water tank, when the demister is washed, water is preferentially supplied by the demister washing water tank, when the liquid level of the demister washing water tank is low, water is supplied by the process water tank, and when the process water tank supplies water, the secondary demisting zone is preferentially washed; the process water tank is provided with a process water pump, and when the liquid level of the absorption tower is low, the process water pump supplies water to the absorption tower.
3. The invention can make full use of the slurry collected in the pit to prepare the slurry, reduce the total process water supply amount of the desulfurization system and improve the water balance adjustment capability of the system.
4. The invention completely recovers machine seal cooling water, oxidation fan cooling water and vacuum pump working solution, and is used for demister washing water or filter cloth washing water, thereby reducing the supplement of process water, reducing the total process water supplement amount entering a desulfurization system, and improving the water balance regulation capacity of the system.
Drawings
FIG. 1 is a process flow diagram of a wet desulfurization water balance control system according to the present invention (example one);
FIG. 2 is a process flow diagram of a wet desulfurization water balance control system according to the present invention (example II);
in the figure:
1, an absorption tower; 1-1 primary demisting area; 2, a demisting tower; 2-1 of a secondary demisting area; 3, a feeding pump of a swirler; 4 a first swirler; 5, suspending the filter; 6 a demister flushing water tank; 7 a demister flushing water pump; 8, a pit; 9, a process water tank; 10, a process water pump; 11 pit pump; 12 a gypsum discharge pump; 13 a second cyclone; 14, a vacuum belt dehydrator; 15 a pulping tank; 16 limestone slurry feed pumps; 17 a wastewater feed pump; 18 a waste water system; 19 recycling the water tank; 20 recycling the water pump; 21 filter cloth flush tank.
Detailed Description
The technical solutions in the embodiments of the present invention will be clearly and completely described below with reference to the drawings in the embodiments of the present invention, and it is obvious that the described embodiments are only a part of the embodiments of the present invention, and not all of the embodiments. All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the protection scope of the present invention.
In the first embodiment, as shown in fig. 1, a wet desulfurization water balance control system includes an absorption tower 1, a demister tower 2, a first cyclone 4, a suspension filter 5 with a back flush, a demister flushing water tank 6, a demister flushing water pump 7, a pit 8, a process water tank 9, and a process water pump 10;
the flue gas of the absorption tower 1 and the flue gas of the demisting tower 2 both enter from bottom to top and are connected in series by a flue; the absorption tower 1 comprises an oxidation area, an absorption area and a primary demisting area 1-1; the demisting tower 2 comprises a liquid holding area and a secondary demisting area 2-1;
the liquid holding area is connected with an inlet of a cyclone feeding pump 3 through a pipeline, an outlet of the cyclone feeding pump 3 is connected with a first cyclone 4 through a pipeline, an upper outlet of the cyclone is sequentially connected with a suspension filter 5 and a demister flushing water tank 6 in series through a pipeline, a lower outlet of the cyclone is connected to a pit 8 through a pipeline, a pit pump 11 is arranged beside the pit 8, and the pit 8, the pit pump 11 and the absorption tower 1 are sequentially connected through pipelines;
the primary demisting zone 1-1 and the secondary demisting zone 2-1 are both provided with demister flushing water pipes, the demister flushing water pipes are connected with a demister flushing water pump 7, inlet pipes of the demister flushing water pump 7 are respectively connected with a demister flushing water tank 6 and a process water tank 9 in a parallel mode, pipelines are switched by valves, and the process water tank 9, the process water pump 10 and the absorption tower 1 are sequentially connected through pipes; the demister is independent from the absorption tower 1 in the form of series connection of the demisting towers 2, washing water of the demister in the demisting tower 2 is filtered and then recycled to form an internal circulation system independent from the absorption tower 1, the situation that the washing water of the demister directly and completely falls into the absorption tower to cause uncontrollable increase of the liquid level of the absorption tower can be avoided, and a proper amount of process water can be supplemented according to the real-time liquid level value of the absorption tower.
The absorption tower 1, the demisting tower 2, the demister flushing water tank 6, the process water tank 9 and the pit 8 are all provided with liquid level meters, so that the water balance can be conveniently adjusted.
The second embodiment, as shown in fig. 2, is different from the first embodiment in that: the absorption tower 1 is further provided with a gypsum discharge pump 12 and a second cyclone 13 which are sequentially connected in series through a pipeline, the upper outlet of the second cyclone 13 is connected to the feed inlet of a vacuum belt dehydrator 14 through a pipeline, the lower outlet of the second cyclone 13 is connected with a pit 8 through a pipeline, filtrate water of the vacuum belt dehydrator 14 flows into the pit 8 through a pipeline, the outlet pipeline of the pit pump 11 is further provided with a branch pipeline communicated to a pulping pool 15, the outlet pipeline of the process water pump 10 is provided with a branch pipeline communicated to the pulping pool 15, the pulping pool 15 is provided with a limestone slurry feed pump 16, and the pulping pool 15, the limestone slurry feed pump 16 and the absorption tower 1 are sequentially connected through pipelines; the pit 8 is provided with a wastewater feeding pump 17 which is connected with a wastewater system 18 through a pipeline, slurry in the process of a gypsum dewatering system is recycled into the pit 8, one part of the slurry is used for pulping, and the other part of the slurry is returned into the absorption tower 1, so that the whole system except wastewater discharge and gypsum carrying water is in large internal circulation, the supplement of extra process water is reduced, and the increase of water balance burden is prevented.
In practical application, the outlet pipeline of the process water pump 10 is provided with a branch for machine seal cooling water, oxidation fan cooling water and vacuum pump working fluid of each pump, the branch process water is collected to the reuse water tank 19 through a pipeline, the reuse water tank 19 is conveyed to the demister flushing water tank 6 through the reuse water pump 20, process water supplement in the system is reduced, and the water balance regulation capacity is improved.
In practical applications, the outlet of the reuse water pump 20 is provided with a branch pipe leading to the filter cloth flushing water tank 21 for flushing the vacuum belt dehydrator 14.
In practical application, the first-stage demisting zone 1-1 is a tubular demister or baffle type demister, has an effect of primary demisting, and is not easy to scale.
In practical application, the second-stage demisting zone 2-1 is a tube bundle type demister or a multi-stage baffle type demister or a combination of the two, further captures fog drops in flue gas, and ensures demisting efficiency.
In another aspect of the invention, a wet desulphurization water balance control method is provided: a defogging tower 2 is connected in series behind an absorption tower 1, most defogging equipment is arranged in a secondary defogging area 2-1 of the defogging tower 2, only a primary defogging area 1-1 with primary defogging is reserved in the absorption tower 1, a defogging flushing water pump 7 is started at regular time to flush the primary defogging area 1-1 and the secondary defogging area 2-1 in a sequential partitioning manner, flushing water of the primary defogging area 1-1 falls into the bottom of the absorption tower 1 to be used as water supplement, flushing water of the secondary defogging area 2-1 is collected by the defogging tower 2, the collected flushing water is conveyed to a first swirler 4 through a swirler feed pump 3 to remove impurities, flushing water with low impurities flows into a suspension filter 5 with backwashing, filtered water enters a defogging flushing water tank 6 and is subjected to secondary utilization flushing through the defogging flushing water pump 7, high-impurity flushing water separated by the first swirler 4 flows into a pit 8, returned to the absorption tower 1 by a pit pump 11.
In practical application, the absorption tower 1, the demisting tower 2, the demister flushing water tank 6, the process water tank 9 and the pit 8 are all provided with liquid level meters; the demisting tower 2 and the pit 8 are always kept at low liquid levels; the inlet pipeline of the demister flushing water pump 7 is also connected with the process water tank 9, when the demister is flushed, water is preferentially supplied by the demister flushing water tank 6, when the liquid level of the demister flushing water tank 6 is low, water is supplied by the process water tank 9, and when the process water tank 9 supplies water, the secondary demisting zone 2-1 is preferentially flushed; the process water tank 9 is provided with a process water pump 10, when the liquid level of the absorption tower 1 is low, the process water pump 10 supplies water to the absorption tower 1, and elastic supply is performed according to the liquid level, so that the process water tank is more flexible.
In practical application, machine seal cooling water, oxidation fan cooling water and vacuum pump working solution of each pump are collected to a reuse water tank 19 through pipelines, reuse water is conveyed to a demister flushing water tank 6 or a filter cloth flushing water tank 21 in a vacuum belt dewatering system through a reuse water pump 20 for secondary utilization, the consumption of process water in the whole desulfurization system is reduced, and a larger adjusting range can be reserved for an absorption tower.
In practical application, slurry in the process of flowing out of the gypsum cyclone for gypsum dehydration and the vacuum belt dehydrator 14 is collected into the pit 8, the slurry in the pit 8 is returned to the absorption tower 1 and is conveyed into the slurry making pool 15 for slurry preparation, and compared with direct slurry making by using process water, the total consumption of the process water in the system is reduced, and a larger adjusting range can be reserved for the absorption tower.
In conclusion, the wet desulphurization water balance control system can effectively control the total process water amount entering the desulphurization system, can reserve a larger adjusting range for the desulphurization tower, and is suitable for the working condition of low inlet smoke temperature.
The foregoing illustrates and describes the principles, general features, and advantages of the present invention. It should be understood by those skilled in the art that the foregoing embodiments are merely illustrative of the technical spirit and features of the present invention, and the present invention is not limited thereto but may be implemented by those skilled in the art.
Claims (6)
1. A wet desulphurization water balance control method is characterized in that: the control system adopted by the method comprises: the system comprises an absorption tower (1), a demisting tower (2), a first cyclone (4), a suspension filter (5) with back washing, a demister flushing water tank (6), a demister flushing water pump (7), a pit (8), a process water tank (9) and a process water pump (10); the flue gas of the absorption tower (1) and the flue gas of the demisting tower (2) both enter from bottom to top and are connected in series by a flue; the absorption tower (1) comprises an oxidation area, an absorption area and a primary demisting area (1-1); the demisting tower (2) comprises a liquid holding area and a secondary demisting area (2-1); the liquid holding area is connected with an inlet of a cyclone feeding pump (3) through a pipeline, an outlet of the cyclone feeding pump (3) is connected with a first cyclone (4) through a pipeline, an upper outlet of the cyclone is sequentially connected with a suspension filter (5) and a demister flushing water tank (6) in series through a pipeline, a lower outlet of the cyclone is connected to a pit (8) through a pipeline, a pit pump (11) is arranged beside the pit (8), and the pit (8), the pit pump (11) and the absorption tower (1) are sequentially connected through pipelines; the primary demisting zone (1-1) and the secondary demisting zone (2-1) are respectively provided with a demister flushing water pipeline, the demister flushing water pipeline is connected with a demister flushing water pump (7), an inlet pipeline of the demister flushing water pump (7) is respectively connected with the demister flushing water tank (6) and the process water tank (9) in a parallel mode, pipelines are switched by valves, and the process water tank (9), the process water pump (10) and the absorption tower (1) are sequentially connected through pipelines; the absorption tower (1), the demisting tower (2), the demister flushing water tank (6), the process water tank (9) and the pit (8) are all provided with liquid level meters;
the method comprises the steps of serially connecting a defogging tower (2) behind an absorption tower (1), installing most defogging equipment in a secondary defogging area (2-1) of the defogging tower (2), only reserving a primary defogging area (1-1) with primary defogging in the absorption tower (1), starting a defogger flushing water pump (7) at regular time, flushing the primary defogging area (1-1) and the secondary defogging area (2-1) in a sequential subarea manner, enabling flushing water of the primary defogging area (1-1) to fall into the bottom of the absorption tower (1) as water supplement, collecting flushing water of the secondary defogging area (2-1) by the defogging tower (2), conveying the collected flushing water to a first cyclone (4) through a cyclone feeding pump (3) for impurity removal, enabling low-impurity flushing water to flow into a suspension filter (5) with backwashing water, and enabling the filtered water to enter a flushing demister water tank (6), the secondary utilization washing is carried out by a demister washing water pump (7), and the high impurity washing water separated by the first cyclone (4) flows into a pit (8) and returns to the absorption tower (1) by a pit pump (11);
the demisting tower (2) and the pit (8) are always kept at low liquid levels; an inlet pipeline of a demister flushing water pump (7) is also connected with a process water tank (9), when the demister is flushed, water is preferentially supplied by the demister flushing water tank (6), when the liquid level of the demister flushing water tank (6) is low, water is supplied by the process water tank (9), and when the process water tank (9) supplies water, the secondary demisting zone (2-1) is preferentially flushed; the process water tank (9) is provided with a process water pump (10), and when the liquid level of the absorption tower (1) is low, the process water pump (10) is used for supplementing water to the absorption tower (1).
2. The wet desulfurization water balance control method according to claim 1, characterized in that: the process water pump (10) outlet pipeline is provided with a branch for machine seal cooling water, oxidation fan cooling water and vacuum pump working liquid of each pump, the branch process water is collected to a reuse water tank (19) through a pipeline, the reuse water tank (19) is conveyed to a demister flushing water tank (6) through a reuse water pump (20), the outlet of the reuse water pump (20) is provided with a branch pipeline leading to a filter cloth flushing water tank (21) for washing of a vacuum belt dehydrator (14), the machine seal cooling water, the oxidation fan cooling water and the vacuum pump working liquid of each pump are collected to the reuse water tank (19) through pipelines, and the reuse water is conveyed to the demister flushing water tank (6) or the filter cloth flushing water tank (21) in a vacuum belt dehydration system through the reuse water pump (20).
3. The wet desulfurization water balance control method according to claim 1, characterized in that: the process slurry flowing out of the gypsum cyclone and vacuum belt dehydrator (14) equipment for dehydrating the gypsum is collected into a pit (8), and the slurry in the pit (8) is returned to the absorption tower (1) and is also conveyed into a slurry making pool (15) for preparing the slurry.
4. The wet desulfurization water balance control method according to claim 1, characterized in that: the absorption tower (1) is further provided with a gypsum discharge pump (12) and a second cyclone (13) which are sequentially connected in series through a pipeline, the upper outlet of the second cyclone (13) is connected to the feed inlet of a vacuum belt dehydrator (14) through a pipeline, the lower outlet of the second cyclone (13) is connected with a pit (8) through a pipeline, filtrate water of the vacuum belt dehydrator (14) flows into the pit (8) through a pipeline, the outlet pipeline of the pit pump (11) is further provided with a branch pipeline communicated to a pulping pool (15), the outlet pipeline of a process water pump (10) is provided with a branch pipeline communicated to the pulping pool (15), the pulping pool (15) is provided with a limestone slurry feeding pump (16), and the pulping pool (15), the limestone slurry feeding pump (16) and the absorption tower (1) are sequentially connected through pipelines; the pit (8) is provided with a wastewater feeding pump (17) which is connected with a wastewater system (18) through a pipeline.
5. The wet desulfurization water balance control method according to claim 1, characterized in that: the first-stage demisting zone (1-1) is a tubular demister or a baffle type demister.
6. The wet desulfurization water balance control method according to claim 1, characterized in that: the second-stage demisting zone (2-1) is a tube bundle type demister or a multi-stage baffle type demister or a combination of the two demisting zones.
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| CN107224865A (en) * | 2017-07-21 | 2017-10-03 | 上海龙净环保科技工程有限公司 | A kind of wet desulphurization water balance control water-saving system and method |
| CN110052121A (en) * | 2019-05-14 | 2019-07-26 | 北京国电龙源环保工程有限公司 | A kind of desulphurization system water balance regulator control system and its process |
| CN110723858A (en) * | 2019-11-22 | 2020-01-24 | 北京龙源环保工程有限公司 | Desulfurization wastewater zero-discharge treatment system and treatment process |
| CN111229012A (en) * | 2020-03-26 | 2020-06-05 | 中煤能源研究院有限责任公司 | Low-load absorption tower water balance adjustment process system |
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| CN101816888A (en) * | 2010-05-14 | 2010-09-01 | 孙厚杰 | Wet flue gas desulfurization absorption tower for power plant |
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| CN101670225A (en) * | 2009-10-19 | 2010-03-17 | 浙江赞宇科技股份有限公司 | Sulfonated tail gas cycle-absorption method and cycle-absorption system |
| CN107224865A (en) * | 2017-07-21 | 2017-10-03 | 上海龙净环保科技工程有限公司 | A kind of wet desulphurization water balance control water-saving system and method |
| CN110052121A (en) * | 2019-05-14 | 2019-07-26 | 北京国电龙源环保工程有限公司 | A kind of desulphurization system water balance regulator control system and its process |
| CN110723858A (en) * | 2019-11-22 | 2020-01-24 | 北京龙源环保工程有限公司 | Desulfurization wastewater zero-discharge treatment system and treatment process |
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