CN212632246U - Raw flue gas dechlorination system for desulfurization wastewater zero-discharge process - Google Patents
Raw flue gas dechlorination system for desulfurization wastewater zero-discharge process Download PDFInfo
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- CN212632246U CN212632246U CN202021781666.2U CN202021781666U CN212632246U CN 212632246 U CN212632246 U CN 212632246U CN 202021781666 U CN202021781666 U CN 202021781666U CN 212632246 U CN212632246 U CN 212632246U
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Abstract
The utility model discloses a former flue gas dechlorination system for zero release technology of desulfurization waste water, the electric air blower comprises a blower, the desulfurization absorption tower is connected through former flue to the fan, be provided with HCl absorbing device in the former flue, HCl absorbing device includes packing layer and absorbed layer, the absorbed layer includes the defogging pipe that the level was arranged, the cistern is held in defogging pipe lower part installation, it is provided with circulating water branch pipe to hold the cistern bottom, defogging pipe and hold and be provided with the guiding gutter between the cistern, hold the liquid outlet in cistern and connect first graphite cooler, two medium filter are connected to first graphite cooler, two medium filter connect the high-pressure pump, DTRO membrane device is connected to the high-pressure pump, DTRO membrane device's dense water outlet connection analytic tower, industry hydrochloric acid storage tank is connected at analytic tower top. The dechlorination device develops a new way of limestone-gypsum wet desulphurization wastewater zero discharge engineering, and has the characteristics of low operation cost, resource utilization of industrial hydrochloric acid, no influence on the resource utilization of fly ash, optimized operation of a desulphurization system and the like.
Description
Technical Field
The utility model belongs to the technical field of coal fired power plant's lime stone-gypsum wet flue gas desulfurization waste water zero release, concretely relates to raw flue gas dechlorination system for zero release technology of desulfurization waste water.
Background
The national institute of national affairs 4 months in 2015 promulgates a water pollution prevention action plan (national issue [ 2015 ] 17), takes the industrial pollution prevention and control of strong grasping as an important task, wherein a coal-fired enterprise is taken as an industrial water and water drainage household, takes the aim of saving and protecting water resources with force as a starting point and aims at controlling the total water consumption and improving the water utilization efficiency, the coal-fired enterprise gradually implements the water-saving optimization and transformation of the whole plant, and the principle of 'quality-based recovery and gradient utilization' is followed to realize the non-discharge of wastewater. Along with the increasing speed of the country on the water environment pollution treatment, in recent years, various large-power efficient and power environment-friendly enterprises are put into desulfurization wastewater zero-emission technology exploration and process research and development.
The limestone-gypsum wet desulphurization chemical reaction process determines that the slurry of the absorption tower is in a high-hardness liquid-solid mixture environment for a long time; therefore, the desulfurization wastewater is used as the terminal wastewater of coal-fired enterprises, and the most typical water quality characteristic of the desulfurization wastewater is high Cl-High Ca content2+High Mg content2+High suspended matter, high dissolved salt, high and medium metals, etc. Limestone-gypsum wet desulphurization process design takes into account equipment corrosion and gypsum slurry crystallization factors, and generally requires Cl in the slurry of the absorption tower-The concentration is controlled within 20000 mg/L. Therefore, the discharge amount of the desulfurization waste water is firstly determined by the slurry Cl of the desulfurization absorption tower-Equilibrium concentration of (1), Cl-The lower the equilibrium concentration control is, the larger the wastewater discharge amount is; secondly depending on Cl-Balance of total amounts of in and out of desulfurization System, Cl-Is mainly composed ofThe source is the carrying of coal-fired flue gas and process water, and the Cl carried by the coal-fired flue gas in unit time-The total amount is more than twice of the process water; in addition to the exhaust fumes and the dehydration of gypsum, may carry small amounts of Cl-In addition, Cl is mainly controlled-The equilibrium concentration depends on reasonable desulfurization waste water discharge.
Combining the characteristics of the desulfurized wastewater with Cl-The balance control of the total amount shows that the zero discharge process of the desulfurization wastewater can be started from two major ideas, one is to reduce Cl brought into an absorption tower-The other is to directly dispose the discharged desulfurization waste water. The current common zero-discharge technology of desulfurization waste water is limited to the latter technology, and the technical route mainly comprises three process units of pretreatment softening, chemical or physical concentration, transfer or direct solidification. NaOH and Na are used in the research of Yang building nations and gunn catalpine of Zhejiang university2CO3、NaHCO3Three common basic substances are sprayed into a flue between an air preheater and a dust remover by atomizing basic solution prepared by desulfurization wastewater through a gas-liquid dual-phase flow nozzle, and the process comprises the step of reducing Cl brought into an absorption tower-Total amount of concept. However, the final purpose of the desulfurization wastewater zero-discharge process in the prior art is to produce solid crystalline salt or transfer the crystalline salt to boiler fly ash on the premise of realizing solid-liquid separation.
Firstly, the zero discharge engineering of desulfurization waste water generally has the practical problems of complex process route, high investment cost, short engineering construction site, high operation and maintenance cost and the like. Secondly, although the method for producing the solid mixed salt is not influenced by the guidance of the later policy, the resource utilization is a serious problem at present, and the method finally involves the solidification and landfill direction. Yield of Na2SO4And the NaCl salt separation mode is more suitable for areas with developed economy, concentrated chemical enterprises and rich snow resources, but the long-term resource utilization can not be ensured. The mode of solidifying in the fly ash does not belong to resource utilization, and only avoids the problem of disposing the solid waste of the terminal while the existing policy standard is executed. This approach is currently accepted by most coal burning businesses. Once policy standard is refined, the definition of desulfurization waste water terminal solid waste is upgraded or the resource utilization of fly ash is improvedThe downstream industry standard, this mode will face the situation of upgrading and transforming again.
SUMMERY OF THE UTILITY MODEL
The utility model aims at providing a former flue gas dechlorination system for zero release technology of desulfurization waste water to water is as the circulation absorbent, and the HCl gas in the direct high-efficient entrapment flue gas reduces and brings into the Cl of absorption tower-Total amount of the components.
The utility model adopts the technical proposal that the raw flue gas dechlorination system for the desulfurization waste water zero discharge process comprises a fan, the fan is connected with the inlet of a desulfurization absorption tower through an L-shaped raw flue, an HCl absorption device is horizontally arranged in the vertical flue section of the raw flue, the HCl absorption device comprises a packing layer and an absorption layer which are arranged up and down, the absorption layer comprises demisting pipes which are horizontally arranged in sequence, a V-shaped liquid holding groove is correspondingly arranged at the lower part of each demisting pipe, a circulating water branch pipe is arranged at the bottom of each liquid holding groove, an inverted V-shaped diversion trench is arranged between each demisting pipe and each liquid holding groove, wherein, outside the flue at the other end of the liquid holding groove, a first graphite cooler is connected through a pipeline after absorption liquid converges, the first graphite cooler is connected with a double-medium filter, the double-medium filter is connected with a high-pressure pump, the high-pressure pump is connected with a DTRO membrane device, the concentrated water outlet of the DTRO membrane device, the top of the resolution tower is connected with an industrial hydrochloric acid storage tank.
The utility model is also characterized in that,
the fresh water outlet of the DTRO membrane device is connected with a circulating water tank, the circulating water tank is connected with a circulating water pump, and the circulating water pump is connected with a water inlet of a circulating water branch pipe positioned outside the flue.
And a precipitation liquid outlet of the desorption tower is connected with a second graphite cooler, and the second graphite cooler is connected with a circulating water tank.
The circulating water branch pipes are all porous dripping pipes.
The diversion trench and the liquid holding trench are distributed in a staggered manner.
The utility model has the advantages that:
the washed acid solution is subjected to membrane concentration, thermal desorption and other processes to finally produce 30% industrial hydrochloric acid. The acid liquor discharged by the dechlorination device is characterized by high chlorine, low hardness and low suspended matters. The softening link in the conventional desulfurization wastewater zero-discharge process is avoided, and the operation stability of the membrane concentration process is improved, so that a large amount of operation reagent cost is saved. Before and after the membrane concentration device, the acid liquor can also be directly generated into chloride salt by adding an alkaline neutralizing agent (such as sodium carbonate, sodium hydroxide and the like), and then the thermal method concentration and solidification process is utilized to realize zero discharge of wastewater, so that the risks of scaling, blockage and the like of equipment can be obviously reduced.
Drawings
FIG. 1 is a schematic structural diagram of a raw flue gas dechlorination system for a desulfurization wastewater zero-discharge process of the present invention;
FIG. 2 is a schematic structural diagram of an HCl absorption device in a raw flue gas dechlorination system for a desulfurization wastewater zero-discharge process of the present invention;
in the figure, 1, a fan, 2, an original flue, 3, a desulfurization absorption tower, 4, a liquid holding tank, 5, a diversion trench, 6, a demisting pipe, 7, a packing layer, 8, an absorption layer, 9, a first graphite cooler, 10, a double-medium filter, 11, a high-pressure pump, 12, a DTRO membrane device, 13, a circulating water tank, 14, a circulating water pump, 15, a desorption tower, 16, a second graphite cooler, 17, an industrial hydrochloric acid storage tank and 18, a circulating water branch pipe are arranged.
Detailed Description
The present invention will be described in detail with reference to the accompanying drawings and specific embodiments.
The utility model relates to a former flue gas dechlorination system for zero release technology of desulfurization waste water, as shown in figure 1, including fan 1, fan 1 connects the entry of desulfurization absorption tower 3 through former flue 2, former flue 2 is L type flue, the perpendicular flue section of former flue 2 and fan 2 exit linkage, and level in the perpendicular flue section of former flue 2 is provided with HCl absorbing device, HCl absorbing device includes packing layer 7 and absorbed layer 8 that are set up from top to bottom, absorbed layer 8 includes defogging pipe 6 that arranges horizontally in proper order, the inner wall at former flue 2 is fixed at the both ends of each defogging pipe 6, the cross section of defogging pipe 6 is egg type structure, the one side that meets the flue gas has four bellied liquid drop barrier strips, the surface of one side of back flue gas is smooth; the lower part of each demisting pipe 6 is correspondingly provided with a V-shaped liquid holding groove 4, the liquid holding groove 4 is fixed on the inner wall of the original flue 2, the bottom of each liquid holding groove 4 is provided with a circulating water branch pipe 18, the circulating water branch pipe 18 is fixed on the inner wall of the original flue 2, the circulating water branch pipe 18 is a porous dripping pipe, an inverted V-shaped diversion groove 5 is arranged between each demisting pipe 6 and each liquid holding groove 4, the diversion groove 5 is fixed on the inner wall of the original flue 2, the diversion groove 5 and the liquid holding groove 4 are distributed in a staggered manner, and flue gas washing is enhanced by changing the flow direction of flue gas;
a confluence liquid outlet is arranged on the outer side of the flue at the other end of the liquid holding tank 4, the liquid outlet is connected with a first graphite cooler 9 through a pipeline, the first graphite cooler 9 is connected with a double-medium filter 10, the double-medium filter 10 is connected with a high-pressure pump 11, the high-pressure pump 11 is connected with a DTRO (digital rights object) membrane device 12, a fresh water outlet of the DTRO membrane device 12 is connected with a circulating water tank 13, the circulating water tank 13 is connected with a circulating water pump 14, a liquid inlet of the circulating water pump 14 is connected with a liquid inlet of a circulating water branch pipe 18 on the outer side of the flue, and a liquid inlet of;
the concentrated water outlet of the DTRO membrane device 12 is connected with an analytical tower 15, the top of the analytical tower 15 is connected with an industrial hydrochloric acid storage tank 17, the output of the analyzed liquid of the analytical tower 15 is connected with a second graphite cooler 16, and the second graphite cooler 16 is connected with a circulating water tank 13 or is discharged to a desulfurization process water tank. The water coming from the desulfurization industrial water can be directly supplemented to the circulating water tank.
The DTRO membrane device 12 is a hydrochloric acid selective concentration device. The first graphite cooler 9 and the second graphite cooler 16 are tubular heat exchange devices, circulating water is fed on a tube side, and cooling water is fed on a shell side.
The desorption tower 15 is a non-contact heat exchange packed tower, high-temperature steam is fed on a tube side, and concentrated acid liquid is fed on a shell side.
The packing layer 7 is a particle body with a certain geometric shape and size, generally piled in a tower in a random mode, also called as random packing or particle packing, the bulk packing is divided into an annular packing layer, a ring saddle-shaped packing layer, a spherical packing layer and the like according to different structural characteristics, the particle material can be selected from high-temperature-resistant and corrosion-resistant light ceramics, the main purpose is to intercept smoke carrying liquid drops after passing through an absorption device, and the packing layer 7 can be selectively configured;
the utility model relates to a raw flue gas dechlorination system for zero release technology of desulfurization waste water, its concrete theory of operation is:
absorbing liquid of a circulating water tank 13 is pumped into a circulating water branch pipe 18 in an HCl absorbing device through a circulating water pump 14, a certain liquid level in a liquid holding tank 4 is maintained through flow regulation of the circulating water pump 14, flue gas is in efficient contact with the absorbing liquid in the liquid holding tank 4 in a controllable flue gas temperature process in the process of changing the flow direction of the flue gas, washed flue gas enters a desulfurization absorbing tower 3 after liquid drops are intercepted by a packing layer, the washed absorbing liquid is converged at the other end of the liquid holding tank 4 and then is conveyed into a first graphite cooler 9 through a pipeline, the temperature of the absorbing liquid is reduced to be within the range of 30-40 ℃, the condensed absorbing liquid is further subjected to suspended matter removal through a double-medium filter 10 and then is conveyed to a DTRO membrane device 12 through a high-pressure pump 11 for acid liquid concentration treatment, the produced fresh water returns to the circulating water tank 13, the discharged fresh water enters an analyzing tower 15, and concentrated water in the analyzing tower 15 volatilizes HCl gas after heat exchange through high-, and then the industrial hydrochloric acid with the concentration of 30 percent is prepared by adsorption. The temperature of the educt discharged from the desorption tower 15 is reduced to be within the range of 30-40 ℃ after passing through the second graphite cooler 16, and the educt can be returned to the circulating water tank 13 or can be periodically discharged to a desulfurization process water tank.
During normal operation, the circulating absorption liquid is insufficient in water amount, and the desulfurization industrial water can be directly supplemented to the circulating water tank 13. The amount of the supplementary industrial water is determined by the evaporation amount of the circulating absorption liquid in the gas-liquid contact process. The process has no wastewater discharge per se, and is only used for maintaining reasonable SO4 2-And SO3 2-The concentration range of (2) is required to periodically discharge the precipitation liquid of the desorption tower 15 to a desulfurization process water tank, and the precipitation liquid is secondarily used for a desulfurization system, such as washing of a demister of an absorption tower or washing operation of a desulfurization pipeline.
Hydrogen chloride is colorless gas, has pungent odor, has specific gravity 1.268 times of air, is easily soluble in water, has melting point of-114.6 deg.C, boiling point of-84.1 deg.C, heat generation of-92.340 kJ/mol, and high negative value of heat generation, and shows that HCl gas is relatively stable and only decomposes at 1000 deg.C by 0.014%. The solubility of hydrogen chloride in water is quite large, 1 volume of water can dissolve 450 volumes of hydrogen chloride, and the exothermic amount of hydrogen chloride absorbed by water is 75.339kJ/mol (HCl gas). The temperature of the hydrochloric acid will therefore increase during absorption, and the partial pressure of hydrogen chloride above the aqueous hydrochloric acid solution increases with increasing temperature.
In combination with the chemical properties of hydrogen chloride, water is the most effective and inexpensive absorbent for removing HCl pollutants from flue gases. When water is used for absorbing hydrogen chloride in flue gas, not only is solution heat generated, but also heat is transferred in the gas-liquid contact process, so that cooling of the circulating absorption liquid is particularly important, and the lower the cooling temperature is, the absorption efficiency of HCl gas is favorably improved.
The key technology of the utility model lies in that the temperature of the original flue gas of the control desulfurization is not lower than 90 ℃, if the flue gas temperature drops greatly, it is big to cause at first the circulation absorption liquid evaporation capacity, needs to supply a larger amount of industrial water to maintain the water balance of circulation absorption liquid. And secondly, the water balance of the desulfurization system body cannot be controlled, the water consumption of a normal water user of the desulfurization system cannot be met, and the running stability of the desulfurization system is influenced. The HCl absorption device can be fully contacted with the flue gas through a limited amount of circulating absorption liquid, and the temperature of the original flue gas is controlled to be reduced within the range of 10-20 ℃ during operation. In addition, on the premise of not adding an alkaline medicament, the pH value of the circulating absorption liquid is controlled to be 2-4, and the DTRO membrane device is a key device for controlling the pH value of the circulating absorption liquid. The normal supplemented industrial water is neutral, and the circulating absorption liquid absorbs HCl and SO simultaneously in the contact process with the raw flue gas2、SO3And HF, which is not considered separately because of the relatively low concentration. Highest concentration of SO2H is generated after contacting with the circulating absorption liquid2SO3Due to H2SO3Dissolving in water to perform reversible reaction, SO that the circulating absorption liquid can inhibit SO when being maintained in an acidic state2Inevitably, there will be a very small amount of H2SO3Will be naturally oxidized into H2SO4Or direct absorption of SO3To generate H2SO4. Therefore, the circulating absorption liquid must be in an acidic state, i.e., the circulating absorption liquid can selectively absorb the HCl gas efficiently.
Use the utility modelThe novel device controls the HCl concentration in the washed flue gas within a lower range, and maintains the Cl of the same level of the slurry of the desulfurization absorption tower-The concentration can obviously reduce the discharge amount of the desulfurization waste water, and even can realize the discharge without the desulfurization waste water. After the coal-fired power plant generally implements water-saving reconstruction, the flue gas of the unit carries Cl in unit time-The total amount is about twice of the process water, if the unit burns high-chlorine coal, the proportion is still improved to a certain extent, and if the concentration of chloride ions in the process water of the desulfurization system is controlled at a lower level, the proportion is still improved to a certain extent. In combination, carry Cl in accordance with the flue gas-The amount accounts for 70% of the total amount entering the desulfurization system, and accordingly the emission amount of the desulfurization wastewater can be reduced by 70% at most, wherein about 15% of the amount of the chloride ions can be carried and discharged out of the desulfurization system through the gypsum and the flue gas, and the amount of the desulfurization wastewater normally discharged accounts for about 25% of the amount before the project is implemented in consideration of the removal efficiency of the process on HCl in the flue gas. Under the condition that the water quantity of the proportion is normal, the water is simply treated by the existing triple-header wastewater treatment process and then is used for a boiler slag conveyor or the dry slag is mixed with wet slag to be completely consumed. If the unit burns high-sulfur coal, the amount of the gypsum produced correspondingly increases, the amount of the desulfurization waste water discharged normally can be further reduced, and even the desulfurization system does not need to discharge the waste water.
Relate to the utility model discloses a gas-liquid contact process, the key is the type of avoiding using the nozzle to spray the contact, does not have under the condition in volume pond, can guarantee the high-efficient circulation of absorption liquid. If HCl absorption device with similar liquid-holding effect exists, all belong to the protection scope of this patent.
Claims (5)
1. The utility model provides a raw flue gas dechlorination system for zero release technology of desulfurization waste water, its characterized in that includes fan (1), fan (1) passes through the entry of the raw flue (2) of L type connection desulfurization absorption tower (3), the level is provided with HCl absorbing device in the perpendicular flue section of raw flue (2), HCl absorbing device is including packing layer (7) and absorbed layer (8) that are setting up from top to bottom, absorbed layer (8) are including defogging pipe (6) of arranging horizontally in proper order, every the lower part of defogging pipe (6) corresponds installation V type holds cistern (4), every the bottom of holding cistern (4) is provided with circulating water branch pipe (18), every be provided with between defogging pipe (6) and every liquid holding cistern (4) diversion trench (5) of type of falling V, diversion trench (5) all are the dislocation formula and are distributed with holding cistern (4), wherein the liquid outlet of holding cistern (4) passes through first graphite cooler (9) of pipe connection, two medium filter (10) are connected in first graphite cooler (9), high-pressure pump (11) are connected in two medium filter (10), DTRO membrane device (12) is connected in high-pressure pump (11), dense water outlet connection analytic tower (15) of DTRO membrane device (12), industry hydrochloric acid storage tank (17) are connected at analytic tower (15) top, the fresh water outlet connection circulating water tank (13) of DTRO membrane device (12), circulating water pump (14) are connected in circulating water tank (13), the water inlet of circulating water branch pipe (18) that are located the flue outside is connected to the inlet of circulating water pump (14).
2. The raw flue gas dechlorination system for the desulfurization waste water zero discharge process according to claim 1, wherein the effluent outlet of the desorption tower (15) is connected with a second graphite cooler (16), and the second graphite cooler (16) is connected with the circulating water tank (13).
3. The raw flue gas dechlorination system for the desulfurization waste water zero discharge process according to claim 1, wherein the circulating water branch pipes (18) are all porous dripping pipes.
4. The raw flue gas dechlorination system for the desulfurization waste water zero discharge process according to claim 1, wherein the cross section of the demisting pipe (6) is egg-shaped.
5. The raw flue gas dechlorination system for the desulfurization wastewater zero-discharge process according to claim 1, wherein the demisting pipe (6), the diversion trench (5), the liquid holding tank (4) and the circulating water branch pipe (18) are fixed on the inner wall of the raw flue (2).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202021781666.2U CN212632246U (en) | 2020-08-24 | 2020-08-24 | Raw flue gas dechlorination system for desulfurization wastewater zero-discharge process |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202021781666.2U CN212632246U (en) | 2020-08-24 | 2020-08-24 | Raw flue gas dechlorination system for desulfurization wastewater zero-discharge process |
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| Publication Number | Publication Date |
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| CN212632246U true CN212632246U (en) | 2021-03-02 |
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| CN202021781666.2U Expired - Fee Related CN212632246U (en) | 2020-08-24 | 2020-08-24 | Raw flue gas dechlorination system for desulfurization wastewater zero-discharge process |
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