CN213506413U - Flue gas SO of thermal power plant3With desulfurization waste water concurrent processing system - Google Patents
Flue gas SO of thermal power plant3With desulfurization waste water concurrent processing system Download PDFInfo
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Abstract
The invention provides a flue gas SO of a thermal power plant3And a desulfurization wastewater co-treatment system, wherein the co-treatment system comprises: the desulfurization waste water magnesium extraction module is used for preparing magnesium hydroxide powder by adding an alkali solution into the desulfurization waste water and collecting the desulfurization waste water after magnesium removal; SO in furnace3A removal module for removing SO from the magnesium hydroxide powder prepared by adding the desulfurization waste water magnesium extraction module into the SCR reactor and/or the air preheater3(ii) a And the bypass flue gas desulfurization wastewater spray drying module is used for extracting high-temperature flue gas from the outlet of the SCR reactor, drying the magnesium-removed desulfurization wastewater, and discharging the treated smoke dust to a dust remover. The system can simultaneously carry out the SO of the flue gas3The method has the characteristics of low initial investment, low comprehensive operation cost, simple process, high production flexibility and the like by the synergistic treatment with the desulfurization wastewater.
Description
[ technical field ] A method for producing a semiconductor device
The invention relates to the technical field of coal-fired boiler wastewater and flue gas treatment, in particular to flue gas SO of a thermal power plant3And a system for co-processing the desulfurization wastewater.
[ background of the invention ]
Along with the increase of environmental protection, SO in the flue gas of the thermal power plant3Gas treatment and desulfurization wastewater treatment are increasingly gaining attention. However, because the physical characteristics and the generation process of the two are completely different, the technical routes of the treatment of the two are different, and the treatment of the two is isolated and split.
Firstly, see SO in the flue gas3And (5) treating the gas. Although SO in the flue gas3The content of gas is little, and only accounts for 1-5% of total sulfur, but the harm is not small, and the gas is a main reason for forming acid rain from a macroscopic view and is also an important component of the atmospheric secondary aerosol (the contribution rate of the secondary aerosol to the PM2.5 of the Chinese atmospheric environment reaches 30-77%). Microcosmically, the smoke-free air preheater is one of main inducers of colored smoke plume of a power plant, and can cause the increase of the acid dew point of smoke, so that low-temperature equipment such as APH (air preheater) is corroded, deposited ash and blocked, the efficiency of a boiler is reduced, and even the safe operation of a unit is endangered.
SO in flue gas3Derived from SO2Oxidation of SO, SO2/SO3The conversion has two sources, namely high-temperature conversion (in a hearth) of about 0.5-2.5%, and catalyst conversion (in SCR) of about 0.5-1.5%, and the specific total amount is different due to the combustion coal. However, the total amount of low-sulfur coal reserves in our country is small, more thermal power plants using high-sulfur coal are needed, and SO is generated at the present stage3The content is higher, and the content is generally 30-80 mg/m of a single unit3。
Removing SO in flue gas at present stage3The method mainly comprises the following three steps: hearth method, out-of-furnace method and tail removal method.
The furnace process typically injects an alkaline sorbent from the top of the furnace. Alkaline absorptionThe absorbent is usually alkali metal absorbent such as sodium and potassium, and alkaline earth metal absorbent such as calcium and magnesium. The hearth method has three main defects, one is that the medicament consumption is large because SO is removed in a high-temperature environment3While removing part of SO2. The consumption of the medicament is large, and the quality of the fly ash is also reduced; secondly, the alkaline absorbent absorbs and removes SO3The later generated sulfate can reduce the ash melting point, so that the hearth is coked; thirdly, only SO in the hearth can be removed3For SO generated in the SCR reactor3Without desorption capacity, the overall efficiency cannot be guaranteed.
The tail method mainly makes articles on a dust remover and a desulfurization island, such as additionally arranging a low-temperature electric dust remover, modifying a wet desulfurization system, additionally arranging a wet electric dust remover, modifying the electric dust remover into an electric dust remover or a bag type dust remover and the like. It is generally seen that this pattern is for SO3The method has obvious removal effect, but has huge investment and high operating cost, and has no effect on improving the problems of ash deposition and blockage of Ammonium Bisulfate (ABS) of APH.
The out-of-furnace method is a newly developed method. Different alkaline absorbents are added at the inlets of an SCR reactor and an APH (air preheater) simultaneously or respectively for desulfurization (SO)3). At present, the absorbent mainly comprises magnesium hydroxide, calcium hydroxide, sodium bicarbonate, sodium carbonate, trona and the like, the removal rate is magnesium hydroxide (75.3%), sodium bicarbonate (69.7%), calcium hydroxide (55.1%) and sodium carbonate (52.8%) in sequence, and the trona effect is close to that of the sodium carbonate. The alkaline absorbents also have some defects, such as high price of magnesium hydroxide, easy coking of sodium bicarbonate and poisoning of an SCR catalyst, change of dust specific resistance by calcium hydroxide and influence on the dust removal efficiency of an electric dust remover at the tail part, and the absorbents can only be in a dry powder form and need to be ground and refined, so that the cost is increased; sodium carbonate is not suitable for desulfurization of APH (air preheater) because it produces part of sodium bisulfate, which has high viscosity like Ammonium Bisulfate (ABS) and is easy to cause APH dust deposition and blockage.
And then treating the desulfurization wastewater.
The waste water produced in the wet desulfurization (limestone/gypsum method) process of boiler flue gas mainly comes from the discharged water of desulfurization absorption tower, the cleaning water of gypsum dehydration process and cleaning system.
The method is mainly characterized by comprising the following steps:
(1) the wastewater is weak in acidity, and the pH value is 5-7. The suspended matter is very high (mainly gypsum particles) and can reach tens of thousands of mg/L;
(2) the total dissolved solid has high TDS content (about 20000-90000mg/L), high contents of calcium ions, magnesium ions, sodium ions, chloride ions, sulfate ions, sulfite ions and the like, and standard exceeding indexes of heavy metals, fluorides, ammonia nitrogen, COD and the like, so that the recovery of salt in the wastewater is difficult. Influenced by solubility, wherein the content of calcium ions is below 1000mg/L, while the content of magnesium ions is higher and is above 4000mg/L at least;
(3) the discharge amount is small. According to the technical manual of wet flue gas desulfurization of thermal power plants, Cl in the slurry is maintained when the chlorine content of the fire coal is 0.05 percent-The concentration is not more than 20000mg/L, and the design values of the single desulfurization waste water amount of 300MW, 600MW and 1000MW units under the working condition are respectively 4m3/h、7m3H and 12m3H is used as the reference value. According to field measurement, the actual emission of most power plants is about 70% higher on average, namely 7m3/h、12m3H and 20m3/h。
With the improvement of national and local environmental protection standards, the requirement of near zero emission of the desulfurization wastewater is increasing day by day, and the development of related technologies is rapid. From the property of finished products, the near zero emission technology of the desulfurization wastewater can be divided into a salt separation technology and a salt mixing technology. Both technical routes can be simplified into three modules: pretreatment → concentration reduction → solidification crystallization.
The salt separation process was analyzed. The salt separation process is to perform conditioning (pH) and full softening treatment on the wastewater to remove calcium and magnesium ions which may influence the normal operation of the concentration and decrement module; then the wastewater enters a concentration and decrement module for further treatment, and the module can be used for membrane concentration or thermal concentration; finally, the concentrated tail liquid enters a crystallizer for crystallization and salt separation treatment. The clean water and the condensed water generated in the whole process are recycled, and part of concentrated water and mother liquor possibly need to be discharged or concentrated by a thermal method for drying and mixed salt treatment.
In summary, a large amount of basic agents are required to be added in the salt separation process, a large amount of salt-containing sludge is generated, the salt separation process has a long chain and a large and complex system, and more importantly, the finished product of inorganic salt has low added value and cannot form large-scale production. Therefore, the application of the salt separation process is greatly limited due to the characteristics of large investment and high operation and maintenance cost.
Accordingly, the use of mixed salt processes is more common. The mixed salt process is to extract high-temperature flue gas at the SCR outlet, dry the waste water or the concentrated and reduced waste water by using the high-temperature flue gas, and directly feed the formed mixed salt ash slag into a dust remover along with the flue gas to be mixed with the fly ash. However, in order to prevent ash deposition and blockage of APH, the extraction amount of high-temperature flue gas is generally not more than 3%.
Taking a certain 2X 350MW thermoelectric unit as an example, the amount of the flue gas at the SCR outlet of a single unit under the BMCR working condition is about 1408666kg/h, the temperature of the flue gas is 360 ℃, and if 3 percent of the amount of the flue gas is extracted, about 4.2 ten thousand kg/h, about 2.6m of the flue gas can be dried3H, wastewater. According to the current waste water production, 3 percent of the smoke amount obviously cannot satisfy the requirement of directly drying all waste water. Therefore, the existing industrial routes of mixed salt all need to concentrate and reduce the amount of wastewater, and then carry out thermal solidification and crystallization. The concentration and decrement treatment has the same technical route as the salt separation process. Therefore, the salt mixing process has the characteristics of large investment and high operation and maintenance cost.
To sum up, the flue gas SO at the present stage3The treatment and zero-emission treatment system of the desulfurization wastewater is isolated and split, and deviates from the development principle of comprehensive utilization of energy advocated by the state. On the one hand, flue gas SO3In the treatment process, a large amount of alkaline absorbent is consumed. Although the magnesium hydroxide has the best effect, sodium carbonate or calcium hydroxide with obvious side effect is mostly used as an absorbent due to the cost; on the other hand, in the treatment process of the waste water, a large amount of alkaline medicament is used for removing magnesium ions, and the cost is high. And a large amount of magnesium ions are discarded, and secondary pollution is caused.
The two are isolated and split, so that two sets of treatment systems are required to be built, the construction is repeated, the investment is increased, the repeated dosing is serious, the production cost is increased, the process is complex, and the operation and maintenance cost is increased.
Therefore, it is necessary to research the SO of the flue gas3The deficiencies of the prior art are addressed in a system and method for co-processing desulfurized wastewater to solve or mitigate one or more of the problems set forth above.
[ summary of the invention ]
In view of the above, the invention provides a flue gas SO3With desulfurization waste water concurrent processing system, this system can use in industrial and mining enterprises that contain coal fired boiler such as thermal power plant, paper mill, can carry out flue gas SO simultaneously3The method has the characteristics of low initial investment, low comprehensive operation cost, simple process, high production flexibility and the like by the synergistic treatment with the desulfurization wastewater.
In one aspect, the invention provides a co-processing system for flue gas SO3 and desulfurization wastewater, comprising:
desulfurization waste water magnesium extraction module and SO in furnace3The system comprises a removing module and a bypass flue gas desulfurization wastewater spray drying module, wherein the desulfurization wastewater magnesium extracting module is connected with SO in a furnace3A desorption module, SO in the furnace3The removal module is arranged at an inlet of the SCR reactor and/or the APH, one end of the bypass flue gas desulfurization wastewater spray drying module is connected with an outlet of the SCR reactor and/or the APH, and the other end of the bypass flue gas desulfurization wastewater spray drying module is connected with the desulfurization wastewater magnesium extraction module.
The above-described aspects and any possible implementations further provide an implementation in which the desulfurization waste water magnesium extraction module includes: one-level buffer pool, first magnesium unit, the second of carrying are carried magnesium unit and filter-pressing drying unit, the filter-pressing drying unit is connected the one-level buffer pool simultaneously, is first to carry magnesium unit and second and carries the magnesium unit, desulfurization waste water inlet tube is connected to one-level buffer pool one end, and the other end connects gradually first magnesium unit and the second of carrying and carries the magnesium unit, the second is carried the magnesium unit and is connected bypass flue gas desulfurization waste water spray drying module.
The aspect and any possible implementation mode described above further provide an implementation mode, a first-level buffer tank dosing device is arranged above the first-level buffer tank, a flocculating agent is arranged in the first-level buffer tank dosing device, and the bottom end of the first-level buffer tank is connected with a desulfurization wastewater sludge discharge pipe.
The above aspects and any possible implementation manners further provide an implementation manner, where the first magnesium extraction unit includes a first magnesium extraction dosing device, a first basic group reagent storage device, a magnesium extraction dosing box drain pipe, and a magnesium hydroxide solid phase main drain pipe, the first basic group reagent storage device is disposed above the first magnesium extraction dosing device, a bottom end of the first magnesium extraction dosing device is connected to the filter-pressing drying unit through the magnesium hydroxide solid phase main drain pipe, the first magnesium extraction dosing device is connected to the magnesium extraction dosing box drain pipe, and an alkali solution and a flocculant are disposed in the first basic group reagent storage device.
The first magnesium extraction unit further comprises a secondary sedimentation tank for extracting magnesium from the desulfurization wastewater, a drainage pump for the magnesium-removed wastewater, a drainage pipe for the magnesium-removed wastewater, and an auxiliary solid-phase magnesium hydroxide discharge pipe, wherein the bottom end of the secondary sedimentation tank for extracting magnesium from the desulfurization wastewater is connected with a filter-press drying unit through the auxiliary solid-phase magnesium hydroxide discharge pipe, one side of the secondary sedimentation tank for extracting magnesium from the desulfurization wastewater is connected with a first magnesium extraction dosing device, the other side of the secondary sedimentation tank for extracting magnesium from the desulfurization wastewater is connected with the drainage pipe for the magnesium-removed wastewater through the drainage pump for the magnesium-removed wastewater, and the drainage pipe for the magnesium-removed wastewater is connected with a second.
The above-mentioned aspect and any possible implementation manner further provide an implementation manner, where the second magnesium extracting unit includes a secondary desulfurization wastewater buffer pool and a second base agent storage device, where an alkali solution and a flocculant are disposed in the second base agent storage device, the second base agent storage device is disposed above the secondary desulfurization wastewater buffer pool, the secondary desulfurization wastewater buffer pool is connected to a magnesium removal wastewater drain pipe, a high efficiency filter and a backwashing device are further disposed in the secondary desulfurization wastewater buffer pool, and a filtration standard of the high efficiency filter is as follows: SS is less than 200 mg/L.
Aspects and any possible implementation as described aboveFurther provided is a realization mode, the SO in the furnace3The removal module comprises: first SO3Removal unit and second SO3A removal unit, the first SO3The removal unit is positioned at the flue gas inlet of the SCR reactor, and the second SO3The removal unit is positioned at a flue gas inlet of the APH, wherein the flue gas inlet of the APH is connected with a flue gas outlet of the SCR reactor, and an inlet of the SCR reactor is connected with a boiler furnace.
The above aspect and any possible implementation manner further provide a further implementation manner, where the bypass flue gas desulfurization wastewater spray drying module includes a spray drying tower, and a top end of the spray drying tower is connected to the desulfurization wastewater secondary buffer tank and a flue gas outlet of the SCR reactor at the same time.
The above aspects and any possible implementation manners further provide an implementation manner, wherein the co-processing system further comprises a dust remover and an FGD, one end of the dust remover is connected to the bottom end of the spray drying tower and the flue gas outlet of the APH, and the other end of the dust remover is communicated with an external chimney through the FGD.
The above aspects and any possible implementation manners further provide an implementation manner, the filter-press drying unit comprises a sludge filter press, a fluidized bed dryer and a magnesium hydroxide powder bin, one end of the sludge filter press is connected with the magnesium hydroxide solid-phase main discharge pipe, the magnesium hydroxide solid-phase auxiliary discharge pipe and the desulfurization wastewater sludge discharge pipe at the same time, the other end of the sludge filter press is connected with the magnesium hydroxide powder bin through the fluidized bed dryer, and the magnesium hydroxide powder bin is connected with the SO in the furnace3And a removal module.
Compared with the prior art, the invention can obtain the following technical effects:
(1) the wastewater does not need to be precisely pretreated, so that the pretreatment difficulty is greatly reduced;
(2) method for removing SO in flue gas by using magnesium ions in wastewater3The added value of magnesium ions in the wastewater is increased;
(3) magnesium hydroxide is the optimum desulfurization (SO)3) The absorbent, compared with other absorbents, has optimal desulfurization efficiency and no side effect.
Of course, it is not necessary for any one product in which the invention is practiced to achieve all of the above-described technical effects simultaneously.
[ description of the drawings ]
In order to more clearly illustrate the technical solutions of the embodiments of the present invention, the drawings needed to be used in the embodiments will be briefly described below, and it is obvious that the drawings in the following description are only some embodiments of the present invention, and it is obvious for those skilled in the art to obtain other drawings based on these drawings without creative efforts.
Fig. 1 is a block diagram of a cooperative processing system according to an embodiment of the present invention.
Wherein, in the figure:
1-a first-level buffer pool; 2-a dosing box for extracting magnesium from the desulfurization waste water; 3-extracting magnesium from the desulfurization waste water in a secondary sedimentation tank; 4-sludge filter press; 5-fluidized bed dryer; 6-magnesium hydroxide powder bin; 7-SCR (denitration reactor); 8-APH (air preheater); 9-SDE (spray drying tower); 10-a secondary buffer tank for desulfurization wastewater; 11-a desulfurization wastewater inlet pipe; 12-a desulfurization wastewater drain pipe 13-a desulfurization wastewater sludge discharge pipe; 21-basic group medicament storage tank 22-magnesium extraction dosing tank drain pipe; 23-a magnesium hydroxide solid phase main discharge pipe; 31-a magnesium removal wastewater drainage pump; 32-a magnesium-removing wastewater drain pipe; 33-magnesium hydroxide solid phase auxiliary discharge pipe; 34-a sludge pump 41-a sludge discharge pipe; 42-desliming wastewater drainage pump; 43-desliming wastewater drain pipe; 51-dry powder discharge pipe; 61-dry powder main regulating valve; 62-dust-containing hot air pipe; 63-dry powder blower; 64-dry powder delivery pipe; 65-SCR bin nozzles; 66-APH bin regulating valve; 67-APH cabin nozzle; 71-SCR outlet flue gas main flue; 72-bypass stack discharge duct.
[ detailed description ] embodiments
For better understanding of the technical solutions of the present invention, the following detailed descriptions of the embodiments of the present invention are provided with reference to the accompanying drawings.
It should be understood that the described embodiments are only some embodiments of the invention, and not all 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.
The terminology used in the embodiments of the invention is for the purpose of describing particular embodiments only and is not intended to be limiting of the invention. As used in the examples of the present invention and the appended claims, the singular forms "a," "an," and "the" are intended to include the plural forms as well, unless the context clearly indicates otherwise.
Flue gas SO of thermal power plant3With desulfurization waste water concurrent processing system, the concurrent processing system includes: desulfurization waste water magnesium extraction module and SO in furnace3The system comprises a removing module and a bypass flue gas desulfurization wastewater spray drying module, wherein the desulfurization wastewater magnesium extracting module is connected with SO in a furnace3A desorption module, SO in the furnace3The removal module is arranged at an inlet of the SCR reactor and/or the APH, one end of the bypass flue gas desulfurization wastewater spray drying module is connected with an outlet of the SCR reactor and/or the APH, and the other end of the bypass flue gas desulfurization wastewater spray drying module is connected with the desulfurization wastewater magnesium extraction module. The desulfurization waste water magnesium extraction module comprises: one-level buffer pool, first magnesium unit, the second of carrying are carried magnesium unit and filter-pressing drying unit, the filter-pressing drying unit is connected the one-level buffer pool simultaneously, is first to carry magnesium unit and second and carries the magnesium unit, desulfurization waste water inlet tube is connected to one-level buffer pool one end, and the other end connects gradually first magnesium unit and the second of carrying and carries the magnesium unit, the second is carried the magnesium unit and is connected bypass flue gas desulfurization waste water spray drying module. The device is characterized in that a primary buffer tank dosing device is arranged above the primary buffer tank, a flocculating agent is arranged in the primary buffer tank dosing device, and a desulfurization wastewater sludge discharge pipe is connected to the bottom end of the primary buffer tank. The first magnesium extraction unit comprises a first magnesium extraction dosing device, a first basic group medicament storage device, a magnesium extraction dosing box drain pipe and a magnesium hydroxide solid phase main discharge pipe, the first basic group medicament storage device is arranged above the first magnesium extraction dosing device, the bottom end of the first magnesium extraction dosing device is connected with the filter-pressing drying unit through the magnesium hydroxide solid phase main discharge pipe, the first magnesium extraction dosing device is connected with the magnesium extraction dosing box drain pipe, and an alkali solution and a flocculating agent are arranged in the first basic group medicament storage device. The first magnesium extraction unit also comprises a second magnesium extraction stage of desulfurization waste waterThe device comprises a sedimentation tank, a demagging wastewater draining pump, a demagging wastewater draining pipe and a magnesium hydroxide solid-phase auxiliary draining pipe, wherein the bottom end of a secondary sedimentation tank for extracting magnesium from desulfurization wastewater is connected with a filter-pressing drying unit through the magnesium hydroxide solid-phase auxiliary draining pipe, one side of the secondary sedimentation tank for extracting magnesium from desulfurization wastewater is connected with a first magnesium extracting and dosing device, the other side of the secondary sedimentation tank for extracting magnesium from desulfurization wastewater is connected with the demagging wastewater draining pipe through the demagging wastewater draining pump, and the magnesium removing wastewater draining. The second magnesium extraction unit comprises a desulfurization wastewater secondary buffer pool and a second base agent storage device, wherein an alkali solution and a flocculating agent are arranged in the second base agent storage device, the second base agent storage device is arranged above the desulfurization wastewater secondary buffer pool, the desulfurization wastewater secondary buffer pool is connected with a magnesium removal wastewater drainage pipe, a high-efficiency filter and a back washing device are further arranged in the desulfurization wastewater secondary buffer pool, and the filtering standard of the high-efficiency filter is as follows: SS is less than 200 mg/L. SO in the furnace3The removal module comprises: first SO3Removal unit and second SO3A removal unit, the first SO3The removal unit is positioned at the flue gas inlet of the SCR reactor, and the second SO3The removal unit is positioned at a flue gas inlet of the APH, wherein the flue gas inlet of the APH is connected with a flue gas outlet of the SCR reactor, and an inlet of the SCR reactor is connected with a boiler furnace. The bypass flue gas desulfurization waste water spray drying module comprises a spray drying tower, wherein the top end of the spray drying tower is simultaneously connected with a secondary desulfurization waste water buffer tank and a flue gas outlet of the SCR reactor. The coprocessing system still includes dust remover and FGD, spray drying tower bottom and APH's exhanst gas outlet are connected simultaneously to dust remover one end, and the other end passes through FGD intercommunication outside chimney, the filter-pressing drying unit includes sludge press filter, fluidized bed desiccator and magnesium hydrate powder storehouse, magnesium hydrate solid phase main discharge tube, magnesium hydrate solid phase auxiliary discharge pipe and desulfurization waste water sludge discharge pipe are connected simultaneously to sludge press filter one end, and the other end passes through fluidized bed desiccator and connects magnesium hydrate powder storehouse, SO powder storehouse connection stove in the magnesium hydrate powder storehouse3And a removal module.
The magnesium extraction module for the desulfurization wastewater prepares magnesium hydroxide powder by adding an alkali solution into the desulfurization wastewater, and simultaneously collects the magnesium-removed desulfurization wastewater;
SO in the furnace3A removal module for removing SO from the magnesium hydroxide powder prepared by adding the desulfurization waste water magnesium extraction module into the SCR reactor and/or the air preheater3；
The bypass flue gas desulfurization wastewater spray drying module extracts high-temperature flue gas from an outlet of an SCR (selective catalytic reduction) reactor, dries the magnesium-removed desulfurization wastewater, discharges treated smoke dust to a dust remover, and generally does not exceed 3 percent in the prior art, SO as to prevent deposition and blockage of APH (air preheater), and the extracted amount of the high-temperature flue gas at the outlet of the SCR is in a state of passing through SO in a furnace3The removal module can extract 8% of high-temperature flue gas after desulfurization, has no influence on the boiler, and does not generate dust accumulation and blockage in the APH (air preheater).
The primary buffer tank is used for settling the desulfurization wastewater discharged by the desulfurization island;
the first magnesium extraction unit is used for collecting supernatant discharged by the first-stage buffer tank, adding an alkali solution and a flocculating agent, and settling magnesium hydroxide for the first time, wherein the alkali solution is a sodium hydroxide solution or other waste alkali solutions;
the second magnesium extraction unit is used for collecting the supernatant discharged by the first magnesium extraction unit, adding an alkali solution and a flocculating agent, and settling magnesium hydroxide for the second time;
and the filter pressing and drying unit is used for collecting the sediments of the primary buffer tank, the first magnesium extraction unit and the second magnesium extraction unit, and carrying out filter pressing and drying to prepare the magnesium hydroxide powder.
The first base agent storage device is used for storing an alkali solution and a flocculating agent;
the first magnesium extraction dosing device is used for collecting supernatant discharged from the primary buffer tank, and adding alkali solution and a flocculating agent in the first base agent storage device into the supernatant discharged from the primary buffer tank.
The second base medicament storage device is used for storing an alkali solution and a flocculating agent;
the second magnesium extraction dosing device is used for collecting the supernatant discharged by the first magnesium extraction unit, and adding the alkali solution and the flocculating agent in the second alkali-based agent storage device into the supernatant discharged by the first magnesium extraction dosing device;
high efficiency filter and back flush unit all set up in the second carries magnesium charge device, and the filter effect is: SS is less than 200 mg/L.
The first SO3A removing unit which is positioned at a flue gas inlet of the SCR reactor and carries out the first SO by adding the magnesium hydroxide powder generated by the filter pressing drying unit3Removing;
the second SO3A removing unit which is positioned at the flue gas inlet of the APH and carries out the second SO by adding the magnesium hydroxide powder generated by the filter pressing drying unit3The desorption, twice desulfurization process can separately carry out also can go on in step, and the desulfurization is also going on for the second time in first desulfurization promptly, and the system can remain stable simultaneously, or carries out first desulfurization earlier, and first desulfurization is accomplished the back, and the flue gas gets into APH, carries out the desulfurization for the second time.
The SDE provides a space for the bypass flue gas discharged by the SCR reactor to enter;
and the secondary buffer tank is used for collecting the supernatant discharged by the second magnesium extraction unit, and the supernatant enters the SDE in a spraying mode and is dried.
In addition, the SCR reactor and the APH in this application are common devices in existing coal fired boilers, wherein:
the SCR reactor (denitration reactor) is used for receiving flue gas SO generated by a boiler hearth3；
An APH (air preheater, commonly referred to as an air preheater) is used to receive the high temperature flue gas from the SCR reactor.
The cooperative processing system carries out cooperative processing by the following method, and comprises the following steps:
s1: preparing magnesium hydroxide powder by a desulfurization waste water magnesium extraction module, replacing magnesium ions with magnesium hydroxide by adding an alkali solution which is a sodium hydroxide solution or other alkali solutions, wherein the magnesium hydroxide is an insoluble solid, and drying by using waste heat or waste heat after extraction to remove SO3The absorbent of (4);
s2: the bypass flue gas desulfurization wastewater spray drying module extracts high-temperature flue gas from an SCR outlet, dries the wastewater which is not subjected to concentration and reduction treatment, and discharges the treated smoke dust to a dust remover to finish zero emission of the desulfurization wastewater;
s3: SO in furnace3The removal module removes SO from the magnesium hydroxide dry powder prepared by adding3First, SO generated in the furnace is removed3And then removing SO generated by SCR3To complete SO in the high-temperature flue gas3And (4) removing.
The S1 specifically includes:
s11: settling the desulfurization wastewater discharged from the desulfurization island in a primary buffer tank;
s12: collecting supernatant discharged from a first-stage buffer tank in a first magnesium extraction unit, adding an alkali solution and a flocculating agent, and settling magnesium hydroxide for the first time;
s13: collecting the supernatant discharged by the first magnesium extraction unit in the second magnesium extraction unit, adding an alkali solution and a flocculating agent, and settling magnesium hydroxide for the second time;
s14: and collecting and gathering sediments of the primary buffer tank, the first magnesium extraction unit and the second magnesium extraction unit, and performing filter pressing and drying to prepare the magnesium hydroxide powder.
The S3 specifically includes:
s31: the SCR reactor receives SO-containing gas generated by a boiler furnace3The flue gas of (2);
s32: first SO3The removal unit is arranged at a flue gas inlet of the SCR reactor, and magnesium hydroxide powder generated by the filter-pressing drying unit is added for carrying out first SO3Removing;
s33: the flue gas discharged by the SCR reactor enters APH;
s34: second SO3The removing unit is arranged at an APH inlet, and magnesium hydroxide powder generated by the filter pressing drying unit is added for carrying out the second SO3Removing SO in the flue gas3And (4) removing.
The S2 specifically includes:
s21, enabling the bypass flue gas discharged by the SCR reactor to enter the SDE;
s22, collecting supernatant discharged by the second magnesium extraction unit in a secondary buffer pool, and feeding the supernatant into the SDE in a spraying mode;
and S23, drying to finish zero emission of the desulfurization wastewater.
As shown in figure 1, the system provided by the invention comprises a desulfurization waste water magnesium extracting module, a bypass flue gas desulfurization waste water spray drying module and a furnace SO3The removal module comprises:
(1) the magnesium extraction module is used for preparing magnesium hydroxide powder. Magnesium ions are replaced by magnesium hydroxide by adding high-concentration sodium hydroxide solution or other alkali liquor. The magnesium hydroxide is insoluble solid, and is dried by using waste heat or waste heat after extraction to remove SO3The absorbent of (1).
(2) The bypass flue gas desulfurization waste water spray drying module extracts high-temperature flue gas from an SCR outlet, dries waste water which is not subjected to concentration and decrement treatment, and discharges treated smoke dust to a dust remover. The module comprises a wastewater buffer tank, a spray pump, a pipeline, a spray drying tower (comprising a tower body, a flue gas distributor and a nozzle), a flue gas baffle door, an adjusting valve, a bypass flue and the like;
(3) SO in furnace3The removal module removes SO by adding medicament dosage (magnesium hydroxide dry powder)3. The system comprises an absorbent bin, a spray gun, a booster fan and a pipeline, wherein the module is divided into two independent subsystems, and the subsystem is arranged at the inlet of an SCR (selective catalytic reduction) and mainly used for removing SO (sulfur oxide) generated in a hearth3Subsystem II is arranged at the APH inlet and mainly used for removing SO generated by SCR3. The two systems can be flexibly combined according to the situation, can be combined and can be installed singly.
And after the desulfurization wastewater is discharged from the desulfurization island, performing gravity settling treatment in a primary buffer tank, wherein the precipitate is equal sludge mainly containing calcium sulfate and is discharged to a special filter press through a sludge pipeline. The supernatant enters a magnesium extraction dosing box, the magnesium removing agent is alkali liquor such as sodium hydroxide, and a flocculating agent is added to accelerate the sedimentation of the magnesium hydroxide. Most of the magnesium hydroxide is settled in the tank and discharged to a special filter press through a sludge pipeline. The supernatant enters the next-stage sedimentation tank. The pool is provided with a high-efficiency filter, and residual magnesium hydroxide is collected and discharged to a special filter press through a sludge pipeline. The supernatant flows into a secondary buffer pool.
The magnesium hydroxide filter press can be a centrifugal type or a plate and frame type, and the like, comprises magnesium hydroxide particles and waste water sludge, the water content of a filter cake is controlled below 70%, and the filter cake is sent to a sludge dryer, and the dryer can be a belt type dryer, a fluidized bed type dryer, and the like, preferably a fluidized bed type dryer. And (4) further dehydrating the filter cake on a dryer to obtain dry powder with the content of below 20%, and then feeding the dry powder into a storage bin. The drying heat source can be hot water of a low-temperature economizer, boiler steam or other heat sources with the temperature not lower than 75 ℃, and preferably waste heat sources such as the low-temperature economizer. The engineering feeding bin can be only used as a spare, and the powder can be directly pressurized by a blower and then respectively fed into SCR for pre-desulfurization (SO)3) System and APH Pre-desulfurization (SO)3) And the system carries out desulfurization. The two systems can be combined into a whole or can be respectively and independently installed. The desulfurization system is composed of a blower, an air pipe, a regulating valve and an ejector. The alkali (magnesium) sulfur ratio is a key control point and is not higher than 2.5. The desulfurization efficiency is not lower than 80%. The adding amount of the alkali (magnesium) powder is mainly determined by the pressure difference of APH and the temperature difference of an inlet and an outlet. The overflowing material is a normal-temperature wear-resistant material, and preferably a ceramic material.
And (4) pumping the wastewater in the secondary buffer tank into a bypass flue gas spray drying tower (SDE) through a spray pump, wherein the bypass flue gas is taken from an SCR outlet. The waste water is quickly dried by the high-temperature flue gas in the tower, and the generated crystal salt is uniformly mixed with the fly ash before entering the inlet of the dust remover along with the bypass flue gas, so that zero discharge treatment of the waste water is realized. The extracted flue gas amount is determined by the wastewater treatment amount and the flue gas inlet temperature, 8% of flue gas can be extracted at most without influencing APH and other tail flues, and the general requirements of most projects can be met.
The specific working process is as follows:
the wastewater discharged from the desulfurization island FGD enters a primary buffer tank 1 along a wastewater inlet pipe 11, and the buffer tank also has the function of a regulating tank. The total suspended matter TSS of the wastewater is high, and most TSS is settled after conventional medicaments such as flocculating agent and the like are added. Wherein the supernatant liquid flows into the magnesium extracting dosing tank 2 along a drain pipe 12, and the settled sludge is discharged to the filter press 4 along a sludge discharge pipe 13. The material of overflowing is 316L, and the buffer pool is lined with carbon steel rubber or glass flakes.
The supernatant liquid in the magnesium-extracting dosing tank 2 reacts with the alkali liquor dosed in the basic group medicament storage tank 21 to generate magnesium hydroxide. The alkali solution is solution of sodium hydroxide, calcium hydroxide, etc., preferably sodium hydroxide. The pH value of the dosing tank 2 is not less than 10. The medicament reservoir may also include conventional medicaments such as flocculants. The supernatant is discharged to a secondary sedimentation tank for removing magnesium along with a drain pipe 22. Since the supernatant still contains a large amount of magnesium hydroxide particles, to recover Mg as much as possible2+Secondary sedimentation is required. The sedimentary sludge mainly containing magnesium hydroxide particles is discharged to the filter press 4 along with the main magnesium hydroxide solid-phase discharge pipe 23. The material of overflowing is carbon steel lining rubber or lining plastic.
The magnesium extraction secondary sedimentation tank 3 contains a high-efficiency filter and is provided with a back washing device. The filtering effect is adjustable, and the recommended SS is less than 200mg/L to reduce the backwashing frequency. The filtered clear liquid is pressurized by a magnesium removal waste water discharge pump 31 and then pumped into a secondary buffer tank 10 along a magnesium removal waste water discharge pipe 32. The deposited magnesium hydroxide particles are discharged to the filter press 4 along with the solid-phase auxiliary discharge pipe 33 of magnesium hydroxide. The sludge pump 34 is a common apparatus. The overflowing material of the pump valve is 316L, and the rest is carbon steel lining rubber or lining plastic.
The sludge and magnesium hydroxide particles in the primary buffer tank 1, the magnesium extracting and dosing tank 2 and the magnesium extracting and secondary sedimentation tank 3 are gathered in a filter press 4. The filter press may be of the centrifugal type or of the plate and frame type, etc., preferably of the plate and frame type. The water content of the filter cake is not higher than 70 percent, and the filter cake is sent to a drier 5 through a sludge discharge pipe 41 for thermal drying. The filtrate is pressurized by the drainage pump 42 and then drained back to the primary buffer tank 1 along the drainage pipe 43. The overflowing material of the pump valve is 316L, and the rest is carbon steel lining rubber or lining plastic.
The dryer 5 is a thermal dryer, which may be a fluidized bed, belt, or other means, preferably a fluidized bed dryer. The dried magnesium hydroxide particles are powdery, the water content is lower than 20%, and the hot air and the dry powder are discharged to the magnesium hydroxide powder bin 6 along the discharge pipe 51 without installing a dust remover. The heat source is hot water, steam or hot air with the temperature of not lower than 75 ℃, and preferably hot water of a low-temperature economizer. If no low-temperature economizer is arranged, a gas-water heat exchanger is preferably arranged after APH.
The magnesium hydroxide powder bin 6 is provided with a cyclone separator and a storage tankAnd (7) a tank. The storage tank is provided with a thermostat to prevent the dry powder from water absorption and hardening. The heat source is from the heat source outlet of the dryer 5. The powder bin storage tank is provided with a main regulating valve 61 for controlling the feeding amount of the dry powder. The hot air from the dryer 5 is discharged from the cyclone, and then introduced into the dry powder duct 64 along the hot air pipe 62, and then is supplied to the desulfurization (SO)3) In the system, the blowing wind pressure is provided by a blower 63. In order to ensure the desulfurization rate, a dry powder injector before SCR and a dry powder injector before APH are respectively arranged. The two ejectors can be installed in a combined mode, or can be installed independently, and preferably are installed independently. Desulfurization (SO)3) The system consists of blower 63, conduit 64, regulator valves 65 and 67, and dry powder injectors 66 and 68, where injector 66 is installed at the SCR inlet and injector 68 is installed at the APH inlet. The total desulfurization efficiency is not lower than 80%, and the alkali (magnesium) sulfur ratio is a key control point and is not higher than 2.5. The adding amount of the alkali (magnesium) powder is mainly determined by the pressure difference of APH and the temperature difference of an inlet and an outlet. The overflowing material is a normal-temperature wear-resistant material, the ejector needs to resist the high temperature of 500 ℃, and a ceramic material is preferred.
SO3The flue gas with the content reduced by about 50 percent is divided into two paths of flue gas at the outlet of the SCR reactor 7, wherein the main flue gas flows to an APH (air preheater) 8 along a main flue 71. Flue gas for drying wastewater enters an SDE (spray drying tower) 9 along a bypass flue 72, and the amount of the flue gas is controlled by a bypass flue gas regulating valve 73. The extracted flue gas amount is determined by the wastewater treatment amount and the flue gas inlet temperature, and 8% of flue gas can be extracted at most without influencing APH and other tail flues.
The amount of flue gas entering APH (air preheater) 8 is reduced, but because of SO3When the desorption system works, the acid dew point temperature is reduced to be below 100 ℃, the deposited ash is mainly common deposited ash, the ABS deposited ash strength is inhibited, and the heat exchange efficiency is maintained. The smoke temperature of the main smoke discharge pipe 81 can be reduced to 110 ℃ at the lowest. The heat storage element of the APH (air preheater) 8 may be a DU plate or an NF plate, preferably a DU plate.
The wastewater of the secondary buffer tank 10 for desulfurization wastewater, the supernatant from the magnesium extraction settling tank 3, has a pH of about 10. Therefore, the secondary buffer tank has the function of conditioning, and the pH value can be adjusted to be neutral by adding acid. The conditioned wastewater is pressurized by a spray water supply pump 101, pumped into an SDE (spray drying tower) 9 along a spray pipe 102, and dried. The flow material is 316L or higher.
And (3) allowing the bypass flue gas from the SCR to enter an SDE (spray drying tower) 9, and drying the desulfurization wastewater from the secondary buffer tank 10. The SDE consists of a tower body, a nozzle and a smoke distributor. The nozzles may be pressure, air or centrifugal nozzles, preferably 2205 lined with a wear resistant and corrosion resistant material such as silicon carbide or other ceramics. The tower body and the flue gas distributor are both made of common carbon steel. The flue gas is dispersed by a flue gas distributor in the tower body and is fully mixed with the waste water atomized by the nozzle, and the waste water is thoroughly evaporated and dried in the tower body. The temperature of the dried flue gas is reduced to more than 120 ℃, the dried flue gas is discharged to a flue gas discharge main pipeline 81 through a flue gas discharge pipe 91, is mixed with the flue gas at an APH outlet, and is finally discharged to a dust remover, so that zero discharge of waste water is realized.
The key point of the invention is that the magnesium ions in the wastewater are recovered by using the alkali liquor to produce the magnesium hydroxide, and no secondary pollution is caused. Magnesium hydroxide is used for flue gas desulfurization (SO)3) One of the most preferred absorbents. The additional value of the magnesium salt is improved; meanwhile, the waste heat of the flue gas is utilized to produce the magnesium hydroxide dry powder, the doped sludge is dried together, and the production process has no secondary pollution; in addition, SO in the furnace flue gas is removed by using magnesium ions in the wastewater3The denitration efficiency of the SCR is improved, the SCR can still work normally under low load, and the service life of the catalyst is prolonged; finally, removing SO in SCR flue gas by using magnesium ions in wastewater3The method can reduce the acid dew point temperature of the flue gas, inhibit the ABS dust deposition strength, improve the heat exchange efficiency by about 5-10% under the condition that the heat exchange area of an APH (air preheater) is kept in a conventional design, and the newly added heat is used for zero emission treatment of the desulfurization wastewater. Therefore, the concentration and decrement treatment of the wastewater is not needed, and the investment and operation and maintenance cost of zero discharge of the wastewater are greatly reduced.
Flue gas SO of thermal power plant provided by the embodiment of the application3The system is described in detail in conjunction with a desulfurization wastewater treatment system. The above description of the embodiments is only for the purpose of helping to understand the method of the present application and its core ideas; meanwhile, for the ordinary skilled in the art, according to the idea of the present application, inThe present disclosure should not be considered limited to the particular examples and applications described above.
As used in the specification and claims, certain terms are used to refer to particular components. As one skilled in the art will appreciate, manufacturers may refer to a component by different names. This specification and claims do not intend to distinguish between components that differ in name but not function. In the following description and in the claims, the terms "include" and "comprise" are used in an open-ended fashion, and thus should be interpreted to mean "include, but not limited to. "substantially" means within an acceptable error range, and a person skilled in the art can solve the technical problem within a certain error range to substantially achieve the technical effect. The description which follows is a preferred embodiment of the present application, but is made for the purpose of illustrating the general principles of the application and not for the purpose of limiting the scope of the application. The protection scope of the present application shall be subject to the definitions of the appended claims.
It is also noted that the terms "comprises," "comprising," or any other variation thereof, are intended to cover a non-exclusive inclusion, such that a good or system that comprises a list of elements does not include only those elements but may include other elements not expressly listed or inherent to such good or system. Without further limitation, an element defined by the phrase "comprising an … …" does not exclude the presence of other like elements in a commodity or system that includes the element.
It should be understood that the term "and/or" as used herein is merely one type of association that describes an associated object, meaning that three relationships may exist, e.g., a and/or B may mean: a exists alone, A and B exist simultaneously, and B exists alone. In addition, the character "/" herein generally indicates that the former and latter related objects are in an "or" relationship.
The foregoing description shows and describes several preferred embodiments of the present application, but as aforementioned, it is to be understood that the application is not limited to the forms disclosed herein, but is not to be construed as excluding other embodiments and is capable of use in various other combinations, modifications, and environments and is capable of changes within the scope of the application as described herein, commensurate with the above teachings, or the skill or knowledge of the relevant art. And that modifications and variations may be effected by those skilled in the art without departing from the spirit and scope of the application, which is to be protected by the claims appended hereto.
Claims (10)
1. Flue gas SO of thermal power plant3With desulfurization waste water concurrent processing system, characterized in that, the concurrent processing system includes:
desulfurization waste water magnesium extraction module and SO in furnace3The system comprises a removing module and a bypass flue gas desulfurization wastewater spray drying module, wherein the desulfurization wastewater magnesium extracting module is connected with SO in a furnace3A desorption module, SO in the furnace3The removal module is arranged at an inlet of the SCR reactor and/or the APH, one end of the bypass flue gas desulfurization wastewater spray drying module is connected with an outlet of the SCR reactor and/or the APH, and the other end of the bypass flue gas desulfurization wastewater spray drying module is connected with the desulfurization wastewater magnesium extraction module.
2. The co-processing system according to claim 1, wherein the desulfurization waste water magnesium extraction module comprises: one-level buffer pool, first magnesium unit, the second of carrying are carried magnesium unit and filter-pressing drying unit, the filter-pressing drying unit is connected the one-level buffer pool simultaneously, is first to carry magnesium unit and second and carries the magnesium unit, desulfurization waste water inlet tube is connected to one-level buffer pool one end, and the other end connects gradually first magnesium unit and the second of carrying and carries the magnesium unit, the second is carried the magnesium unit and is connected bypass flue gas desulfurization waste water spray drying module.
3. The system of claim 2, wherein a first-stage buffer tank dosing device is arranged above the first-stage buffer tank, a flocculating agent is arranged in the first-stage buffer tank dosing device, and a desulfurization wastewater sludge discharge pipe is connected to the bottom end of the first-stage buffer tank.
4. The cooperative processing system according to claim 3, wherein the first magnesium extraction unit comprises a first magnesium extraction dosing device, a first basic group agent storage device, a magnesium extraction dosing tank drain pipe and a magnesium hydroxide solid phase main drain pipe, the first basic group agent storage device is arranged above the first magnesium extraction dosing device, the bottom end of the first magnesium extraction dosing device is connected with the filter-pressing drying unit through the magnesium hydroxide solid phase main drain pipe, the first magnesium extraction dosing device is connected with the magnesium extraction dosing tank drain pipe, and an alkali solution and a flocculant are arranged in the first basic group agent storage device.
5. The cooperative treatment system according to claim 4, wherein the first magnesium extraction unit further comprises a secondary sedimentation tank for extracting magnesium from the desulfurization wastewater, a drainage pump for the magnesium-removed wastewater, a drainage pipe for the magnesium-removed wastewater, and an auxiliary drainage pipe for solid magnesium hydroxide, wherein the bottom end of the secondary sedimentation tank for extracting magnesium from the desulfurization wastewater is connected with the filter-press drying unit through the auxiliary drainage pipe for solid magnesium hydroxide, one side of the secondary sedimentation tank for extracting magnesium from the desulfurization wastewater is connected with the first magnesium extraction dosing device, the other side of the secondary sedimentation tank for extracting magnesium from the desulfurization wastewater is connected with the drainage pipe for the magnesium-removed wastewater through the drainage pump for wastewater, and the drainage pipe for the.
6. The cooperative processing system according to claim 5, wherein the second magnesium extraction unit comprises a secondary desulfurization wastewater buffer pool and a second alkaline agent storage device, the second alkaline agent storage device is provided with an alkaline solution and a flocculating agent therein, the second alkaline agent storage device is arranged above the secondary desulfurization wastewater buffer pool, the secondary desulfurization wastewater buffer pool is connected with a magnesium removal wastewater drain pipe, the secondary desulfurization wastewater buffer pool is further provided with a high efficiency filter and a backwashing device therein, and the filtration standard of the high efficiency filter is as follows: SS is less than 200 mg/L.
7. The co-processing system according to claim 6, wherein the in-furnace SO3The removal module comprises: first SO3Removal unit and second SO3Removal unitSaid first SO3The removal unit is positioned at the flue gas inlet of the SCR reactor, and the second SO3The removal unit is positioned at a flue gas inlet of the APH, wherein the flue gas inlet of the APH is connected with a flue gas outlet of the SCR reactor, and an inlet of the SCR reactor is connected with a boiler furnace.
8. The co-processing system according to claim 7, wherein the bypass flue gas desulfurization wastewater spray drying module comprises a spray drying tower, and the top end of the spray drying tower is connected with the desulfurization wastewater secondary buffer tank and the flue gas outlet of the SCR reactor at the same time.
9. The co-processing system according to claim 8, further comprising a dust collector and a FGD, wherein one end of the dust collector is connected to both the bottom end of the spray drying tower and the flue gas outlet of the APH, and the other end is connected to an external chimney through the FGD.
10. The system of claim 8, wherein the filter-press drying unit comprises a sludge filter press, a fluidized bed dryer and a magnesium hydroxide powder bin, one end of the sludge filter press is connected with the main solid-phase magnesium hydroxide discharge pipe, the auxiliary solid-phase magnesium hydroxide discharge pipe and the desulfurization wastewater sludge discharge pipe at the same time, the other end of the sludge filter press is connected with the magnesium hydroxide powder bin through the fluidized bed dryer, and the magnesium hydroxide powder bin is connected with SO in the furnace3And a removal module.
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