CN108423731B - System and method for crystallizing and drying waste water concentrate fluidization discharged by hot flue gas pressure transformation - Google Patents
System and method for crystallizing and drying waste water concentrate fluidization discharged by hot flue gas pressure transformation Download PDFInfo
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- CN108423731B CN108423731B CN201810234630.3A CN201810234630A CN108423731B CN 108423731 B CN108423731 B CN 108423731B CN 201810234630 A CN201810234630 A CN 201810234630A CN 108423731 B CN108423731 B CN 108423731B
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- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims abstract description 106
- 239000003546 flue gas Substances 0.000 title claims abstract description 96
- 239000002351 wastewater Substances 0.000 title claims abstract description 62
- 238000001035 drying Methods 0.000 title claims abstract description 55
- 238000005243 fluidization Methods 0.000 title claims abstract description 35
- 239000012141 concentrate Substances 0.000 title claims abstract description 33
- 238000000034 method Methods 0.000 title claims abstract description 15
- 230000009466 transformation Effects 0.000 title description 2
- 238000002425 crystallisation Methods 0.000 claims abstract description 56
- 230000008025 crystallization Effects 0.000 claims abstract description 56
- 239000000945 filler Substances 0.000 claims abstract description 33
- 239000012798 spherical particle Substances 0.000 claims abstract description 25
- 238000012546 transfer Methods 0.000 claims abstract description 17
- 150000003839 salts Chemical class 0.000 claims abstract description 14
- 238000007667 floating Methods 0.000 claims abstract description 11
- 239000002245 particle Substances 0.000 claims abstract description 9
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 8
- 239000012159 carrier gas Substances 0.000 claims abstract description 4
- 230000008859 change Effects 0.000 claims abstract description 4
- 238000009826 distribution Methods 0.000 claims description 90
- 239000007789 gas Substances 0.000 claims description 89
- 239000007788 liquid Substances 0.000 claims description 27
- 230000007246 mechanism Effects 0.000 claims description 14
- 238000005507 spraying Methods 0.000 claims description 14
- 230000001174 ascending effect Effects 0.000 claims description 12
- 230000002093 peripheral effect Effects 0.000 claims description 9
- 238000003756 stirring Methods 0.000 claims description 8
- 230000006835 compression Effects 0.000 claims description 6
- 238000007906 compression Methods 0.000 claims description 6
- 238000010438 heat treatment Methods 0.000 claims description 6
- 238000007791 dehumidification Methods 0.000 claims description 4
- 238000009833 condensation Methods 0.000 claims description 3
- 230000005494 condensation Effects 0.000 claims description 3
- 238000007790 scraping Methods 0.000 claims description 3
- 238000006477 desulfuration reaction Methods 0.000 description 25
- 230000023556 desulfurization Effects 0.000 description 24
- 239000000243 solution Substances 0.000 description 24
- 239000008188 pellet Substances 0.000 description 11
- 230000007797 corrosion Effects 0.000 description 6
- 238000005260 corrosion Methods 0.000 description 6
- 239000012717 electrostatic precipitator Substances 0.000 description 6
- 238000001704 evaporation Methods 0.000 description 5
- 230000008569 process Effects 0.000 description 5
- 239000004743 Polypropylene Substances 0.000 description 4
- 238000002347 injection Methods 0.000 description 4
- 239000007924 injection Substances 0.000 description 4
- -1 polytetrafluoroethylene Polymers 0.000 description 4
- VEXZGXHMUGYJMC-UHFFFAOYSA-M Chloride anion Chemical compound [Cl-] VEXZGXHMUGYJMC-UHFFFAOYSA-M 0.000 description 3
- 238000000889 atomisation Methods 0.000 description 3
- 238000010586 diagram Methods 0.000 description 3
- 239000000428 dust Substances 0.000 description 3
- 238000005265 energy consumption Methods 0.000 description 3
- 230000008020 evaporation Effects 0.000 description 3
- 238000012423 maintenance Methods 0.000 description 3
- 239000000463 material Substances 0.000 description 3
- 238000007711 solidification Methods 0.000 description 3
- 230000008023 solidification Effects 0.000 description 3
- 230000003009 desulfurizing effect Effects 0.000 description 2
- 238000007599 discharging Methods 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 239000011152 fibreglass Substances 0.000 description 2
- 239000010881 fly ash Substances 0.000 description 2
- 238000000227 grinding Methods 0.000 description 2
- 239000004033 plastic Substances 0.000 description 2
- 229920003023 plastic Polymers 0.000 description 2
- 229920001155 polypropylene Polymers 0.000 description 2
- 239000004810 polytetrafluoroethylene Substances 0.000 description 2
- 229920001343 polytetrafluoroethylene Polymers 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 238000010998 test method Methods 0.000 description 2
- 229910000975 Carbon steel Inorganic materials 0.000 description 1
- 229910001069 Ti alloy Inorganic materials 0.000 description 1
- 239000010962 carbon steel Substances 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 229920001971 elastomer Polymers 0.000 description 1
- 230000005611 electricity Effects 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000002474 experimental method Methods 0.000 description 1
- 238000002309 gasification Methods 0.000 description 1
- 239000011521 glass Substances 0.000 description 1
- 229910001385 heavy metal Inorganic materials 0.000 description 1
- 230000007774 longterm Effects 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- QSHDDOUJBYECFT-UHFFFAOYSA-N mercury Chemical compound [Hg] QSHDDOUJBYECFT-UHFFFAOYSA-N 0.000 description 1
- 229910052753 mercury Inorganic materials 0.000 description 1
- 229910052751 metal Inorganic materials 0.000 description 1
- 239000002184 metal Substances 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 238000005070 sampling Methods 0.000 description 1
- 239000007921 spray Substances 0.000 description 1
- 239000010935 stainless steel Substances 0.000 description 1
- 229910001220 stainless steel Inorganic materials 0.000 description 1
- 238000004065 wastewater treatment Methods 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/02—Treatment of water, waste water, or sewage by heating
- C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
- C02F1/043—Details
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D9/00—Crystallisation
- B01D9/0018—Evaporation of components of the mixture to be separated
- B01D9/0027—Evaporation of components of the mixture to be separated by means of conveying fluid, e.g. spray-crystallisation
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D9/00—Crystallisation
- B01D9/0059—General arrangements of crystallisation plant, e.g. flow sheets
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/02—Treatment of water, waste water, or sewage by heating
- C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
- C02F1/042—Prevention of deposits
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/02—Treatment of water, waste water, or sewage by heating
- C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
- C02F1/10—Treatment of water, waste water, or sewage by heating by distillation or evaporation by direct contact with a particulate solid or with a fluid, as a heat transfer medium
- C02F1/12—Spray evaporation
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/02—Treatment of water, waste water, or sewage by heating
- C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
- C02F1/16—Treatment of water, waste water, or sewage by heating by distillation or evaporation using waste heat from other processes
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
- C02F2103/18—Nature of the water, waste water, sewage or sludge to be treated from the purification of gaseous effluents
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- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Water Supply & Treatment (AREA)
- Hydrology & Water Resources (AREA)
- Life Sciences & Earth Sciences (AREA)
- Crystallography & Structural Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Physics & Mathematics (AREA)
- Thermal Sciences (AREA)
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
- Heat Treatment Of Water, Waste Water Or Sewage (AREA)
- Treating Waste Gases (AREA)
Abstract
The invention discloses a waste water concentrate fluidization crystallization drying system and method for pressure-variable discharge of hot flue gas, wherein the system and method take the hot flue gas introduced by a main flue of a power plant as carrier gas to enter from an air inlet of a fluidization crystallization drying tower, and ball particle fillers between an inner cylinder and an outer cylinder of a rotating roller are blown into a micro-floating fluidization state; the preheated wastewater concentrated solution is distributed to an atomizer arranged on an inner barrel of a rotary roller, the atomized wastewater concentrated solution is sprayed to the surface of a spherical particle filler to conduct heat and mass transfer with hot flue gas, moisture is taken away by the hot flue gas to obtain wet saturated flue gas, salt in the concentrated solution is crystallized and dried and hardened on the surface of the fluidized spherical particle filler, along with the rotation of the inner barrel and the flow of the hot flue gas, the salt is ground and collided between the spherical particle fillers and falls off and is deposited to a crystallization collection cone bucket at the bottom of the tower through an outer barrel mesh screen, the wet saturated flue gas is compressed and then subjected to phase change heat exchange through the preheater, condensed water and dehumidified flue gas are formed, and the compressed dehumidified flue gas is discharged in a variable pressure mode through a flue gas expansion unit.
Description
Technical Field
The invention relates to the field of wastewater treatment, relates to end solidification of wastewater, and in particular relates to a system and a method for fluidized crystallization and drying of wastewater concentrate discharged by hot flue gas in a variable pressure manner, wherein the wastewater concentrate can be desulfurization wastewater concentrate.
Background
The desulfurization wastewater zero-emission system generally comprises a pretreatment unit, a concentration decrement unit and a tail end solidification unit.
At present, the terminal curing technology adopted at home and abroad mainly comprises the following steps: evaporating crystallization drying, direct-injection flue crystallization drying, bypass flue crystallization drying and hot air crystallization drying.
Evaporating, crystallizing and drying: the evaporation and crystallization process consumes a large amount of steam and/or electricity, and has large occupied area and building area, high construction and operation cost and serious equipment scaling and corrosion. The investment of evaporation crystallization drying ton water treatment equipment is more than 100 ten thousand; the operation and maintenance cost of ton water treatment is about 100 yuan.
And (5) crystallizing and drying by using a direct-injection flue: the direct-injection high-temperature flue is adopted for crystallization and drying, so that a large amount of high-temperature flue gas heat is consumed, the energy efficiency of the air preheater is directly reduced, the energy consumption is high, and the risks of damaging the dust remover and reducing the dust removal efficiency are simultaneously involved; the direct injection low-temperature flue is adopted for crystallization and drying, and is limited by the flue gas temperature and the dew point temperature of the low-temperature flue, so that the amount of the vaporizable wastewater is limited and cannot be completely vaporized. And has the following problems:
(1) After the desulfurization wastewater is evaporated, the highly corrosive chloride cannot be completely collected by the electrostatic precipitator, so that the highly corrosive chloride is accumulated on a desulfurization tower and subsequent equipment to cause serious corrosion, and the equipment maintenance frequency and the equipment maintenance cost are obviously increased;
(2) Heavy metal and other materials in the desulfurization wastewater are enriched in the fly ash, so that the reutilization of the fly ash and the safety of users are greatly influenced.
(3) After atomization of the wastewater, serious corrosion and scaling are caused to a flue, an electrostatic precipitator and downstream equipment, and long-term stable operation of the equipment is affected, such as: the electrostatic precipitator polar plate scale deposit reduces dust removal efficiency, influences electrostatic precipitator normal operating even.
(4) The atomization nozzle and the flue are severely worn, and the equipment is rapidly disabled due to corrosion of high-concentration chloride.
(5) The process mainly relies on an electrostatic precipitator to remove evaporation and crystallization products, and substances which cannot be removed by the electrostatic precipitator return to the desulfurizing tower along with flue gas, so that the process is continuously circulated and enriched, the load of the desulfurizing tower is increased, and PM2.5 emission, mercury emission and the like are easily out of standard.
And (3) crystallizing and drying the bypass flue: the high-temperature flue gas needs to be led in, a large amount of heat of the high-temperature flue gas is consumed, the energy efficiency of the air preheater is directly reduced, the energy consumption is high, the equipment manufacturing cost is high, and the equipment scaling and corrosion are serious. The investment of the bypass flue crystallization drying ton water treatment equipment is about 300 ten thousand, and the atomization equipment is frequently replaced.
And (5) hot air crystallization and drying: a large amount of steam is needed, the energy consumption is high, the product cannot be utilized, and the product is difficult to treat.
Disclosure of Invention
The invention aims to overcome the defects of the prior art and provides a system and a method for crystallizing and drying waste water concentrate in a fluidized mode by using waste water concentrate discharged by hot flue gas in a variable pressure mode, so that tail end solidification of waste water concentrate can be realized, and the waste water concentrate can be desulfurization waste water concentrate.
The above object of the present invention is achieved by the following technical solutions:
a waste water concentrate fluidization crystallization drying system with pressure swing discharge of hot flue gas comprises a flue gas inlet unit, a waste water concentrate inlet unit, a fluidization crystallization drying tower, a waste water concentrate heating unit, a flue gas thermal compression unit and an expansion unit;
the lower part of the fluidization crystallization drying tower is provided with an air inlet, the bottom of the fluidization crystallization drying tower is provided with a crystallization collection cone hopper, and the top of the fluidization crystallization drying tower is provided with a wet flue gas outlet; the inside of the tower body is provided with a rotary roller consisting of an inner cylinder and an outer cylinder, the outer cylinder is of a cylindrical structure, the two ends of the cylindrical structure are fixed on the wall of the tower body, the peripheral wall of the cylindrical structure is in a mesh screen shape, the inner cylinder is rotationally connected on the wall of the tower body through the two shaft ends of the cylindrical structure, and a spherical particle filler with the particle size larger than the mesh screen diameter of the outer cylinder is arranged in a space between the inner cylinder and the outer cylinder; the outer peripheral wall of the inner cylinder is provided with a plurality of liquid spraying pipelines, each liquid spraying pipeline is provided with a plurality of nozzles, the end face of one shaft end of the inner cylinder is provided with a plurality of distribution holes corresponding to the plurality of liquid spraying pipelines, each distribution hole is communicated with the corresponding liquid spraying pipeline, the end face of the shaft end is also provided with a distribution valve fixed on the wall of the tower body, the end face is tightly matched with the distribution valve, the distribution valve is provided with a liquid inlet hole, and each distribution hole of the shaft end is sequentially communicated with the liquid inlet hole along with the rotation of the inner cylinder; the outer peripheral wall of the inner cylinder is also provided with stirring blades for stirring the spherical particle filler during rotation;
the flue gas inlet unit comprises a flue gas pipeline communicated with a main flue of the power plant, and flue gas enters the tower body from the gas inlet of the tower;
the wastewater concentrate inlet unit comprises a wastewater concentrate inlet pipeline, one end of the pipeline is communicated with the liquid inlet hole, and the other end of the pipeline is a wastewater concentrate inlet; the waste water concentrated solution heating unit comprises a preheater arranged on a waste water concentrated solution inlet pipeline, and the waste water concentrated solution is heated by the preheater and enters a rotating roller in the tower body; the preheater is also communicated with a wet flue gas outlet of the fluidized crystallization drying tower through a flue gas thermal compression unit, and compressed wet flue gas is subjected to condensation and dehumidification by the preheater and then is subjected to variable-pressure discharge by a flue gas expansion unit.
Further, the fluidization crystallization drying system also comprises an air inlet modulation mechanism arranged at the air inlet of the tower body and an exhaust modulation mechanism arranged at the wet flue gas outlet of the tower body;
the inlet gas distribution modulator comprises an inlet gas distribution modulator and a plurality of inlet guide plates, wherein the inlet guide plates are arranged below the inlet gas distribution modulator and used for guiding horizontal gas flow into vertical gas flow; the exhaust modulation mechanism comprises an outlet gas distribution modulator and a plurality of outlet guide plates which are arranged above the outlet gas distribution modulator and used for guiding vertical gas flow into horizontal gas flow;
the inlet gas distribution modulator and the outlet gas distribution modulator respectively comprise a middle modulation shaft body and modulation blades arranged on the periphery of the modulation shaft body; the middle of the modulation shaft body of the inlet gas distribution modulator is a cylinder, and the two ends of the modulation shaft body are hemispheres or cones; the modulation shaft body of the outlet gas distribution modulator is a cylinder with a lower end of a semicircle sphere or cone; the modulation blades are arranged at the lower end of the cylinder and comprise a plurality of blades which are obliquely arranged in the circumferential direction of the cylinder and are used for modulating vertical ascending airflow into rotary ascending airflow;
the outlet gas distribution modulator is located vertically above the inlet gas distribution modulator.
Further, the inlet guide plate or the outlet guide plate is respectively composed of a horizontal section and a vertical section, and the horizontal section and the vertical section are connected and transited by an arc section.
Further, the modulation blades are circumferentially fixed at equal intervals through the inner stirrups and the outer stirrups and sleeved at the lower end of the cylinder of the gas distribution modulator.
Further, the modulation shaft body is of a hollow structure.
Further, a plurality of scrapers are arranged at the bottom of the inner wall of the outer cylinder.
A method for fluidized crystallization and drying of wastewater concentrate by adopting the system comprises the following steps: hot flue gas introduced by a main flue of a power plant is taken as carrier gas to enter from an air inlet of a fluidization crystallization drying tower, and ball particle fillers between an inner cylinder and an outer cylinder of a rotating roller are blown to form a micro-floating fluidization state; the preheated wastewater concentrated solution is distributed to an atomizer arranged on an inner barrel of a rotary roller, the atomized wastewater concentrated solution is sprayed to the surface of a spherical particle filler to conduct heat and mass transfer with hot flue gas, moisture is taken away by the hot flue gas to obtain wet saturated flue gas, salt in the concentrated solution is crystallized and dried and hardened on the surface of the fluidized spherical particle filler, along with the rotation of the inner barrel and the flow of the hot flue gas, the salt is ground and collided between the spherical particle fillers and falls off and is deposited to a crystallization collection cone bucket at the bottom of the tower through an outer barrel mesh screen, the wet saturated flue gas is compressed and then subjected to phase change heat exchange through the preheater, condensed water and dehumidified flue gas are formed, and the compressed dehumidified flue gas is discharged in a variable pressure mode through a flue gas expansion unit.
The basic principle of the invention (taking desulfurization waste water concentrate as an example): hot flue gas enters from the air inlet at the bottom of the tower, is modulated into cyclone flow state by a gas modulating mechanism, and is filled with an inert pellet filler layer between the inner cylinder and the outer cylinder of the rotating roller to be blown into micro-floating fluidization state. The desulfurization waste water concentrated solution is distributed to an atomizer arranged on an inner barrel of the rotating roller through a liquid distribution device in the rotating roller, atomized and sprayed to the surfaces of the spherical particles and hot flue gas to conduct heat and mass transfer, water and gasification are discharged out of a tower body along with the gas, salt is crystallized and dried and hardened on the surfaces of the fluidized inert spherical particles, the salt is rotated along with the rotating roller and flows of the hot flue gas modulated into cyclone flow state, the fluidized inert spherical particles are ground and collided to fall off, the salt is deposited to the bottom of the tower through an outer barrel screen to be collected and discharged. The evaporated moisture is discharged from the top of the tower along with the hot flue gas, and the high-temperature wet flue gas discharged from the fluidization crystallization drying tower is subjected to heat recovery by a preheater to obtain dehumidification flue gas pressure-variable discharge.
According to the technical scheme, hot flue gas enters the tower body from the air inlet, inert pellet filler is blown into a micro-floating fluidization state by rotating ascending airflow in the tower, concentrated solution which is atomized and sprayed to the surface of the pellet is dried, wet saturated flue gas carrying moisture is discharged from the wet flue gas outlet, and salt is crystallized, dried and hardened on the surface of the fluidized inert pellet, and then drops to a crystallization collection cone bucket at the bottom of the tower along with grinding and collision falling of the pellet through an outer cylinder mesh screen. The preheater is used for collecting heat of wet flue gas to primarily preheat the desulfurization wastewater concentrated solution on one hand, and condensing and dehumidifying the wet flue gas on the other hand, and discharging the dehumidified flue gas in a variable pressure mode. In order to reduce the tower height, reduce equipment investment and occupied space, the flue gas fluidization drying efficiency needs to be improved, and an air inlet modulation mechanism and an air exhaust modulation mechanism can exert the effect. The inlet gas distribution modulator and the outlet gas distribution modulator respectively comprise a middle modulation shaft body and modulation blades arranged on the periphery of the modulation shaft body. The outlet gas distribution modulator is positioned vertically above the inlet gas distribution modulator and is positioned on the central line of the tower body; the inlet guide plate is positioned below the inlet gas distribution modulator in the vertical direction, and is opposite to the air inlet pipeline in the horizontal direction; the outlet guide plate is positioned above the outlet gas distribution modulator in the vertical direction, and faces the exhaust pipeline in the horizontal direction; the flue gas enters from the air inlet pipeline and is blown to the inlet guide plate and is guided to be in a vertical flow state by the horizontal flow state, then is blown to the inlet gas distribution modulator and is modulated to be in a rotary ascending flow state by the vertical ascending flow state, and is sequentially blown to the outlet gas distribution modulator and the outlet guide plate to be discharged after being subjected to mass transfer with the spherical particle filler of the sprayed concentrated solution. The modulation shaft body of the outlet gas distribution modulator and the modulation shaft body of the inlet gas distribution modulator are like a pair of virtual bearings, the inlet gas distribution modulator and the outlet gas distribution modulator jointly modulate the air flow into cyclone flow state, so that efficient mass and heat transfer is realized, the air inlet and outlet are more uniform, the space utilization rate in the tower is greatly improved, and the height of the tower is effectively reduced. The middle of the modulation shaft body of the inlet gas distribution modulator is a cylinder, the two ends of the modulation shaft body are hemispheres or cones, the rotation modulation intensity of the modulation blades on gas can be enhanced, and the lower end of the modulation shaft body of the outlet gas distribution modulator has the same function.
The invention has the advantages that:
1. high heat and mass transfer efficiency: the ball-in rate of the rotating roller is high, the inert ball particle filler is in a micro-floating state in the tower, and direct heat exchange is adopted, so that the heat and mass transfer area is greatly increased, and the heat and mass transfer efficiency is high; 2. the scale resistance is extremely strong: the heat and mass transfer main body, the inert pellet filler, is in a micro-floating state in the tower and moves along with the rotating roller, so that the scale resistance is extremely strong; 3. simple process equipment, low investment and small occupied area; 4. the operation is stable and reliable; 5. the operation cost is low: the hot flue gas is used as fluidization drying gas, and almost no operation cost exists.
Drawings
FIG. 1 is a schematic diagram of a desulfurization wastewater concentrate fluidized crystallization drying system;
FIG. 2 is a schematic diagram of an inlet gas distribution modulator;
FIG. 3 is a schematic view of the structure of a modulating vane of an inlet gas distribution modulator;
FIG. 4 is a schematic view of the inlet gas distribution modulator and inlet baffle structure;
FIG. 5 is a schematic diagram of the structure of the outlet gas distribution modulator and the outlet baffle;
FIG. 6 is a schematic view of a structure of a rotating roller;
FIG. 7 is a schematic view of the end face of the dispensing orifice of the inner barrel and a schematic view of the dispensing valve structure;
FIG. 8 is a schematic structural view of the end face of the inner barrel opposite the dispensing orifice;
FIG. 9 is a schematic view of the configuration of the inner cartridge and spray conduit, and dispensing valve;
the device comprises a 21-inlet guide plate, a 22-outlet guide plate, a 23-modulation shaft body, 24-blades, 25-inner stirrups, 26-outer stirrups, 31-inner cylinders, 32-outer cylinders, 33-spherical particle fillers, 34-liquid spraying pipelines, 35-atomizers, 36-distribution holes, 37-distribution valves, 38-liquid inlet holes, 39-stirring blades, 40-scraping plates, 41-pipelines for communicating the liquid spraying pipelines with the distribution holes, 42-desulfurization wastewater concentrate inlets and 43-stirring blades.
Detailed Description
The following describes the essential aspects of the present invention in detail with reference to examples, but is not intended to limit the scope of the present invention. The test procedures not described in detail in the experiments are conventional test procedures well known to those skilled in the art.
This example takes desulfurization wastewater concentrate as an example.
The desulfurization waste water concentrate fluidization crystallization drying system with the pressure-variable discharge of hot flue gas as shown in fig. 1 comprises a flue gas inlet unit, a desulfurization waste water concentrate liquid inlet unit, a fluidization crystallization drying tower, a desulfurization waste water concentrate liquid heating unit, a flue gas thermal compression unit and an expansion unit;
the lower part of the fluidization crystallization drying tower is provided with an air inlet, the bottom of the fluidization crystallization drying tower is provided with a crystallization collection cone hopper, and the top of the fluidization crystallization drying tower is provided with a wet flue gas outlet; the inside of the tower body is provided with a rotary roller consisting of an inner cylinder and an outer cylinder, the outer cylinder is of a cylindrical structure, the two ends of the cylindrical structure are fixed on the wall of the tower body, the peripheral wall of the cylindrical structure is in a mesh screen shape, the inner cylinder is rotationally connected on the wall of the tower body through the two shaft ends of the cylindrical structure, and a spherical particle filler with the particle size larger than the mesh screen diameter of the outer cylinder is arranged in a space between the inner cylinder and the outer cylinder; the outer peripheral wall of the inner cylinder is provided with a plurality of liquid spraying pipelines, each liquid spraying pipeline is provided with a plurality of nozzles, the end face of one shaft end of the inner cylinder is provided with a plurality of distribution holes corresponding to the plurality of liquid spraying pipelines, each distribution hole is communicated with the corresponding liquid spraying pipeline, the end face of the shaft end is also provided with a distribution valve fixed on the wall of the tower body, the end face is tightly matched with the distribution valve, the distribution valve is provided with a liquid inlet hole, and each distribution hole of the shaft end is sequentially communicated with the liquid inlet hole along with the rotation of the inner cylinder; the outer peripheral wall of the inner cylinder is also provided with stirring blades (shown in figures 6-9) for stirring the spherical particle filler during rotation;
the flue gas inlet unit comprises a flue gas pipeline communicated with a main flue of the power plant, and flue gas enters the tower body from the gas inlet of the tower;
the desulfurization waste water concentrated solution inlet unit comprises a desulfurization waste water concentrated solution inlet pipeline, one end of the pipeline is communicated with the liquid inlet hole, and the other end of the pipeline is provided with a desulfurization waste water concentrated solution inlet; the desulfurization waste water concentrated solution heating unit comprises a preheater arranged on a desulfurization waste water concentrated solution inlet pipeline, and desulfurization waste water concentrated solution is heated by the preheater and enters a rotary roller in the tower body; the preheater is also communicated with a wet flue gas outlet of the fluidized crystallization drying tower through a flue gas thermal compression unit, and compressed wet flue gas is subjected to condensation and dehumidification by the preheater and then is subjected to variable-pressure discharge by a flue gas expansion unit.
The fluidized crystallization drying system also comprises an air inlet modulation mechanism arranged at the air inlet of the tower body and an air exhaust modulation mechanism arranged at the wet flue gas outlet of the tower body (as shown in figures 2-5);
the inlet gas distribution modulator comprises an inlet gas distribution modulator and a plurality of inlet guide plates, wherein the inlet guide plates are arranged below the inlet gas distribution modulator and used for guiding horizontal gas flow into vertical gas flow; the exhaust modulation mechanism comprises an outlet gas distribution modulator and a plurality of outlet guide plates which are arranged above the outlet gas distribution modulator and used for guiding vertical gas flow into horizontal gas flow;
the inlet gas distribution modulator and the outlet gas distribution modulator respectively comprise a middle modulation shaft body and modulation blades arranged on the periphery of the modulation shaft body; the middle of the modulation shaft body of the inlet gas distribution modulator is a cylinder, and the two ends of the modulation shaft body are hemispheres or cones; the modulation shaft body of the outlet gas distribution modulator is a cylinder with a lower end of a semicircle sphere or cone; the modulation blades are arranged at the lower end of the cylinder and comprise a plurality of blades which are obliquely arranged in the circumferential direction of the cylinder and are used for modulating vertical ascending airflow into rotary ascending airflow;
the outlet gas distribution modulator is located vertically above the inlet gas distribution modulator.
The inlet guide plate or the outlet guide plate consists of a horizontal section and a vertical section respectively, and the horizontal section and the vertical section are connected and transited by an arc section; the modulation blades are circumferentially fixed at equal intervals through the inner stirrups and the outer stirrups and sleeved at the lower end of the cylinder of the gas distribution modulator; the modulation shaft body is of a hollow structure; the bottom of the inner wall of the outer cylinder is provided with a plurality of scraping plates so as to improve the efficiency of separating salt hardened from the spherical particle filler.
A fluidized crystallization drying method for desulfurization wastewater concentrate by adopting the system comprises the following steps: hot flue gas introduced by a main flue of a power plant is taken as carrier gas to enter from an air inlet of a fluidization crystallization drying tower, and ball particle fillers between an inner cylinder and an outer cylinder of a rotating roller are blown to form a micro-floating fluidization state; the preheated desulfurization waste water concentrated solution is distributed to an atomizer arranged on an inner barrel of a rotary roller, the atomized solution is sprayed to the surface of a spherical particle filler to conduct heat and mass transfer with hot flue gas, moisture is taken away by the hot flue gas to obtain wet saturated flue gas, salt in the concentrated solution is crystallized and dried and hardened on the surface of the fluidized spherical particle filler, along with the rotation of the inner barrel and the flow of the hot flue gas, the salt is ground and collided between the spherical particle fillers and falls off and is deposited to a crystallization collection cone bucket at the bottom of the tower through an outer barrel mesh screen, the wet saturated flue gas is compressed and then subjected to phase change heat exchange through the preheater, condensed to form condensed water and dehumidified flue gas, and the compressed dehumidified flue gas is discharged in a variable pressure mode through a flue gas expansion unit.
In addition, the sampling port, the observation port and the overhaul port are designed for different working sections, so that the internal components can be conveniently observed, sampled, observed and overhauled in an opening manner at any time; different working sections are provided with pressure gauges and thermometers. And the tower body is manufactured in a sectional way and is connected with a flange. The materials of the different components should be selected according to the composition and concentration of the contact medium. The corrosion resistant material can be rubber or plastic with the carbon steel lining temperature resistance of more than or equal to 100 ℃ according to the components and the concentration of the contact medium [ for example: polytetrafluoroethylene, glass fiber reinforced plastic, PP polypropylene, glass flake, etc.), or metal [ e.g.: stainless steel, titanium alloy, C276, 1.4529, etc.), or plastics with a temperature resistance of not less than 100 [ e.g.: polytetrafluoroethylene, glass fiber reinforced plastic, PP polypropylene, etc.).
According to the technical scheme, hot flue gas enters the tower body from the air inlet, inert pellet filler is blown into a micro-floating fluidization state by rotating ascending airflow in the tower, concentrated solution which is atomized and sprayed to the surface of the pellet is dried, wet saturated flue gas carrying moisture is discharged from the wet flue gas outlet, and salt is crystallized, dried and hardened on the surface of the fluidized inert pellet, and then drops to a crystallization collection cone bucket at the bottom of the tower along with grinding and collision falling of the pellet through an outer cylinder mesh screen. The preheater is used for collecting heat of wet flue gas to primarily preheat the desulfurization wastewater concentrated solution on one hand, and condensing and dehumidifying the wet flue gas on the other hand, and discharging the dehumidified flue gas in a variable pressure mode. In order to reduce the tower height, reduce equipment investment and occupied space, the flue gas fluidization drying efficiency needs to be improved, and an air inlet modulation mechanism and an air exhaust modulation mechanism can exert the effect. The inlet gas distribution modulator and the outlet gas distribution modulator respectively comprise a middle modulation shaft body and modulation blades arranged on the periphery of the modulation shaft body. The outlet gas distribution modulator is positioned vertically above the inlet gas distribution modulator and is positioned on the central line of the tower body; the inlet guide plate is positioned below the inlet gas distribution modulator in the vertical direction, and is opposite to the air inlet pipeline in the horizontal direction; the outlet guide plate is positioned above the outlet gas distribution modulator in the vertical direction, and faces the exhaust pipeline in the horizontal direction; the flue gas enters from the air inlet pipeline and is blown to the inlet guide plate and is guided to be in a vertical flow state by the horizontal flow state, then is blown to the inlet gas distribution modulator and is modulated to be in a rotary ascending flow state by the vertical ascending flow state, and is sequentially blown to the outlet gas distribution modulator and the outlet guide plate to be discharged after being subjected to mass transfer with the spherical particle filler of the sprayed concentrated solution. The modulation shaft body of the outlet gas distribution modulator and the modulation shaft body of the inlet gas distribution modulator are like a pair of virtual bearings, the inlet gas distribution modulator and the outlet gas distribution modulator jointly modulate the air flow into cyclone flow state, so that efficient mass and heat transfer is realized, the air inlet and outlet are more uniform, the space utilization rate in the tower is greatly improved, and the height of the tower is effectively reduced. The middle of the modulation shaft body of the inlet gas distribution modulator is a cylinder, the two ends of the modulation shaft body are hemispheres or cones, the rotation modulation intensity of the modulation blades on gas can be enhanced, and the lower end of the modulation shaft body of the outlet gas distribution modulator has the same function.
The system and the method provided by the invention can effectively dry the desulfurization wastewater concentrated solution, and compared with the prior art, the system and the method have the following advantages:
1. high heat and mass transfer efficiency: the ball-in rate of the rotating roller is high, the inert ball particle filler is in a micro-floating state in the tower, and direct heat exchange is adopted, so that the heat and mass transfer area is greatly increased, and the heat and mass transfer efficiency is high; 2. the scale resistance is extremely strong: the heat and mass transfer main body, the inert pellet filler, is in a micro-floating state in the tower and moves along with the rotating roller, so that the scale resistance is extremely strong; 3. simple process equipment, low investment and small occupied area; 4. the operation is stable and reliable; 5. the operation cost is low: the hot flue gas is used as fluidization drying gas, and almost no operation cost exists.
The above-described embodiments serve to describe the substance of the present invention in detail, but those skilled in the art should understand that the scope of the present invention should not be limited to this specific embodiment.
Claims (7)
1. A waste water concentrate fluidization crystallization drying system that hot flue gas vary voltage was discharged, its characterized in that: the device comprises a flue gas inlet unit, a wastewater concentrate inlet unit, a fluidization crystallization drying tower, a wastewater concentrate heating unit, a flue gas thermal compression unit and an expansion unit;
the lower part of the fluidization crystallization drying tower is provided with an air inlet, the bottom of the fluidization crystallization drying tower is provided with a crystallization collection cone hopper, and the top of the fluidization crystallization drying tower is provided with a wet flue gas outlet; the inside of the tower body is provided with a rotary roller consisting of an inner cylinder and an outer cylinder, the outer cylinder is of a cylindrical structure, the two ends of the cylindrical structure are fixed on the wall of the tower body, the peripheral wall of the cylindrical structure is in a mesh screen shape, the inner cylinder is rotationally connected on the wall of the tower body through the two shaft ends of the cylindrical structure, and a spherical particle filler with the particle size larger than the mesh screen diameter of the outer cylinder is arranged in a space between the inner cylinder and the outer cylinder; the outer peripheral wall of the inner cylinder is provided with a plurality of liquid spraying pipelines, each liquid spraying pipeline is provided with a plurality of nozzles, the end face of one shaft end of the inner cylinder is provided with a plurality of distribution holes corresponding to the plurality of liquid spraying pipelines, each distribution hole is communicated with the corresponding liquid spraying pipeline, the end face of the shaft end is also provided with a distribution valve fixed on the wall of the tower body, the end face is tightly matched with the distribution valve, the distribution valve is provided with a liquid inlet hole, and each distribution hole of the shaft end is sequentially communicated with the liquid inlet hole along with the rotation of the inner cylinder; the outer peripheral wall of the inner cylinder is also provided with stirring blades for stirring the spherical particle filler during rotation;
the flue gas inlet unit comprises a flue gas pipeline communicated with a main flue of the power plant, and flue gas enters the tower body from the gas inlet of the tower;
the wastewater concentrate inlet unit comprises a wastewater concentrate inlet pipeline, one end of the pipeline is communicated with the liquid inlet hole, and the other end of the pipeline is a wastewater concentrate inlet; the waste water concentrated solution heating unit comprises a preheater arranged on a waste water concentrated solution inlet pipeline, and the waste water concentrated solution is heated by the preheater and enters a rotating roller in the tower body; the preheater is also communicated with a wet flue gas outlet of the fluidized crystallization drying tower through a flue gas thermal compression unit, and compressed wet flue gas is subjected to condensation and dehumidification by the preheater and then is subjected to variable-pressure discharge by a flue gas expansion unit.
2. The fluidized crystallization drying system according to claim 1, wherein: the device also comprises an air inlet modulation mechanism arranged at the air inlet of the tower body and an exhaust modulation mechanism arranged at the wet flue gas outlet of the tower body;
the inlet gas distribution modulator comprises an inlet gas distribution modulator and a plurality of inlet guide plates, wherein the inlet guide plates are arranged below the inlet gas distribution modulator and used for guiding horizontal gas flow into vertical gas flow; the exhaust modulation mechanism comprises an outlet gas distribution modulator and a plurality of outlet guide plates which are arranged above the outlet gas distribution modulator and used for guiding vertical gas flow into horizontal gas flow;
the inlet gas distribution modulator and the outlet gas distribution modulator respectively comprise a middle modulation shaft body and modulation blades arranged on the periphery of the modulation shaft body; the middle of the modulation shaft body of the inlet gas distribution modulator is a cylinder, and the two ends of the modulation shaft body are hemispheres or cones; the modulation shaft body of the outlet gas distribution modulator is a cylinder with a lower end of a semicircle sphere or cone; the modulation blades are arranged at the lower end of the cylinder and comprise a plurality of blades which are obliquely arranged in the circumferential direction of the cylinder and are used for modulating vertical ascending airflow into rotary ascending airflow;
the outlet gas distribution modulator is located vertically above the inlet gas distribution modulator.
3. The fluidized crystallization drying system according to claim 2, wherein: the inlet guide plate or the outlet guide plate is respectively composed of a horizontal section and a vertical section, and an arc section for connecting and transitional the horizontal section and the vertical section.
4. The fluidized crystallization drying system according to claim 2, wherein: the modulation blades are circumferentially fixed at equal intervals through the inner stirrups and the outer stirrups and sleeved at the lower end of the cylinder of the gas distribution modulator.
5. The fluidized crystallization drying system according to claim 2, wherein: the modulation shaft body is of a hollow structure.
6. The fluidized crystallization drying system according to claim 1, wherein: the bottom of the inner wall of the outer cylinder is provided with a plurality of scraping plates.
7. A method of fluidized crystallization drying of wastewater concentrate using the system of any one of claims 1-6, characterized by: hot flue gas introduced by a main flue of a power plant is taken as carrier gas to enter from an air inlet of a fluidization crystallization drying tower, and ball particle fillers between an inner cylinder and an outer cylinder of a rotating roller are blown to form a micro-floating fluidization state; the preheated wastewater concentrated solution is distributed to an atomizer arranged on an inner barrel of a rotary roller, the atomized wastewater concentrated solution is sprayed to the surface of a spherical particle filler to conduct heat and mass transfer with hot flue gas, moisture is taken away by the hot flue gas to obtain wet saturated flue gas, salt in the concentrated solution is crystallized and dried and hardened on the surface of the fluidized spherical particle filler, along with the rotation of the inner barrel and the flow of the hot flue gas, the salt is ground and collided between the spherical particle fillers and falls off and is deposited to a crystallization collection cone bucket at the bottom of the tower through an outer barrel mesh screen, the wet saturated flue gas is compressed and then subjected to phase change heat exchange through the preheater, condensed water and dehumidified flue gas are formed, and the compressed dehumidified flue gas is discharged in a variable pressure mode through a flue gas expansion unit.
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| CN112479293A (en) * | 2020-11-10 | 2021-03-12 | 西安西热水务环保有限公司 | Wastewater and flue gas waste heat drying system and method based on semi-dry desulfurization tower |
| CN114560519B (en) * | 2022-03-02 | 2022-11-29 | 北京节度科技有限公司 | Coal fired power plant flue gas desulfurization waste water evaporation tower |
| CN117466516A (en) * | 2023-11-24 | 2024-01-30 | 河北长润环保科技有限公司 | Sludge drying coupling combustion system and process thereof |
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