CN211990211U - System for fluidized bed handles industry waste salt - Google Patents
System for fluidized bed handles industry waste salt Download PDFInfo
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- CN211990211U CN211990211U CN202020220038.0U CN202020220038U CN211990211U CN 211990211 U CN211990211 U CN 211990211U CN 202020220038 U CN202020220038 U CN 202020220038U CN 211990211 U CN211990211 U CN 211990211U
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Abstract
The utility model relates to a system for waste salt of fluidized bed processing industry belongs to an industry waste salt processing technology, including waste salt low temperature drying unit, crushing screening and feed unit, fluidized bed middle temperature strip and oxidation treatment unit and flue gas discharge unit, waste salt is after the drum dryer is dry, waste salt particle for suitable particle size through the crushing screening machine breakage, get into fluidized bed suspension layer, through with steam, the fluidization of combustion-supporting gas and air, carry out high torrent and mix, discharge after the dwell certain time, the VOC tail gas that the organic matter of the VOC of strip and dry production get into the second combustion chamber and fully burn, at last through cooling, discharge after purifying, can big batch continuous processing industry waste salt, work efficiency is high, and can practice thrift the cost of enterprise greatly.
Description
Technical Field
The utility model relates to an industry waste salt processing technology, in particular to system for treating industry waste salt by a fluidized bed.
Background
The industrial waste salt is derived from industrial high-salt wastewater (the salinity is more than 2 g/L), and a large amount of industrial salt-containing wastewater which contains complex organic TOC and is difficult to treat is generated in fine chemical industries such as pesticides, dyes, pharmaceutical intermediates and the like, so that great pressure is caused to the ecological environment. The salt-containing wastewater in China accounts for more than 5% of the total wastewater yield, the total amount reaches more than 3 billion cubic meters every year, and the salt-containing wastewater still increases at a certain speed.
The prior mature technologies for treating the high-concentration salt-containing organic wastewater comprise a dilution biochemical method, an evaporation concentration method, an incineration method, a membrane concentration method and a catalytic oxidation method. The dilution biochemical method adopts domesticated salt-tolerant microorganisms, but when the concentration of the total class and the content of organic matters in the waste salt is changed, the metabolism of the salt-tolerant microorganisms is changed, and the capacity of degrading the organic matters is reduced. The dilution biochemical method produces a large amount of wastewater, has high treatment cost and can only be used for treating industrial saline wastewater with the salinity of less than 2 g/L. The membrane concentration method is not used alone, but is generally used only as a pretreatment means for evaporation concentration and incineration.
For industrial salt-containing wastewater with salinity of more than 2g/L, evaporative concentration and crystallization are still the most economical and effective methods. The secondary treatment-evaporative concentration and crystallization of high-salinity wastewater in the whole industry of China produce more than 1000 million tons of waste salt per year, most of the waste salt is not properly treated, and the waste salt is regarded as dangerous solid waste which is difficult to bury and treat in many places. At present, a lot of companies temporarily store a large amount of salt slag, and the phenomenon of expansion of the warehouse is commonly occurred.
Since these industrial waste salts usually adhere to and are enriched with toxic and harmful organic substances, TOC, the thermal treatment of these industrial waste salts to remove, decompose and oxidize these toxic and harmful organic substances, TOC, and convert them into CO2 and H2O completely is the most effective and common method for waste salt treatment.
At present, three methods for thermal treatment of industrial salt mud containing toxic and harmful organic TOC are mainly used, namely high-temperature melting treatment, microwave desorption and cracking or oxidation treatment and graded carbonization cracking treatment.
The Chinese patent CN109579025A is a typical waste salt melting treatment process, industrial waste salt is combusted in a heating chamber at 850-900 ℃, solid waste salt is completely changed into a molten state at the temperature, most organic matters can be decomposed at high temperature, flue gas generated by the heating chamber enters a secondary combustion chamber to be continuously burnt at high temperature, the operation temperature is kept at 1200-1300 ℃, and organic matters such as dioxin and the like possibly carried in the flue gas are completely burnt. After the combustion of the flue gas is finished, preheating combustion air, then feeding the preheated combustion air into the conical furnace top, and reducing the temperature to 400-500 ℃. The biggest problems of the waste salt melting treatment are high energy consumption, and the waste salt in a molten state is carried to downstream condensation and deposition by flue gas, so that downstream equipment is easy to block and corrode.
Chinese patents CN104344407A, CN106801874A, CN110404943A, CN107098363A, CN107892928A and the like disclose microwave desorption, cracking or oxidation methods, wherein CN104344407A discloses a process flow for treating waste salt by microwaves, which comprises the steps of mixing the waste salt, drying and dehydrating by microwaves and cracking, wherein the cracking temperature is 450-500 ℃, and the cracking time is more than 100 min. The main problems of microwave treatment of industrial waste salt are high cost of electricity for drying and dewatering waste salt and TOC cracking. The electric energy is advanced energy, the efficiency of thermal power generation of a power plant is 25-35%, the electric energy is used for heating and wastes a large amount of thermal energy of thermal power generation, and the electricity consumption cost of energy consumption such as drying and cracking with the same power is far more than the cost of common fuel. In addition, the microwave attenuation performance is limited, the single set of equipment for treating the waste salt by microwave has compact structure, is difficult to amplify, cannot treat the waste salt in large batch, and has higher equipment investment.
Chinese patents CN106475398A, CN109882854A and CN110026411A disclose a method for directly pyrolyzing, classifying or not carbonizing waste salt, wherein the adopted pyrolysis carbonization furnaces are a spouted bed, a suspended bed and a circulating fluidized bed, and the carbonization temperature is 500-750 ℃. But the organic carbon particles generated by pyrolysis and carbonization have low activity, are not easy to burn and remove, and deposit in the inner hole or the surface of the waste salt to generate secondary pollution. In addition, the pyrolysis carbonization temperature is high, the heating is uneven, the phenomenon of local waste salt fusion bonding is severe easily caused, the surface of equipment is corroded, and the equipment is damaged in severe cases.
Chinese patent CN109796993A discloses a process method and a device for carbonizing waste salt by superheated steam, wherein the waste salt enriched with organic TOC is treated by a two-stage rake anaerobic carbonization furnace to obtain pure salt, and tail gas after carbonization is incinerated at high temperature. The operation temperature of the first-stage anaerobic carbonization furnace is 490-510 ℃, and the second-stage anaerobic carbonization furnace adopts superheated steam of 700-800 ℃ for stripping and carbonization. The patent is advantageous to inhibiting coking and carbon deposition of organic matters at high temperature by introducing high-temperature steam, and is a main utility model point. However, the following problems still exist in this method: (1) the operating temperature of the primary anaerobic carbonization furnace is 490-510 ℃ which exceeds the carbonization temperature of the organic matter, so that the organic matter is coked and carbonized in the inner hole or on the surface of the waste salt; (2) introducing superheated steam into the secondary anaerobic carbonization furnace at 700-800 ℃, wherein the temperature is far higher than the carbonization temperature of the organic matters; (3) the rake type carbonization furnace has the disadvantages of uneven material mixing and heating, limited filling rate and difficult amplification and large-batch operation.
Chinese patent CN108408744A discloses a system and a method for treating organic matters in industrial waste salt by hot fluid classification gas stripping, wherein the system consists of a hot blast stove, a hot flue gas classification gas stripping pipeline, a cyclone device and a tail gas treatment device. The hot blast stove burns fuel gas to generate primary hot flue gas at 700-1000 ℃, the primary hot flue gas firstly enters a primary gas stripping pipeline and then is subjected to primary cyclone separation to become secondary hot flue gas, the secondary hot flue gas enters a secondary gas stripping pipeline, waste salt firstly enters a secondary gas stripping salt bin and is subjected to secondary hot flue gas stripping to enter secondary cyclone separation, and primary purified salt and tail gas are obtained. The primary clean salt is conveyed to a primary flue gas stripping pipeline and is stripped into final clean salt by primary hot flue gas and secondary gas. The technical scheme has the following problems: (1) the primary gas stripping temperature is 400-800 ℃, and the temperature exceeds the carbonization temperature of waste salt attached to organic matters, so that the organic matters are coked and carbonized, and are more difficult to treat; (2) hot flue gas is used as a gas stripping medium, so that carbonization of organic matters cannot be inhibited, and the hot flue gas is not a proper gas stripping medium; (3) the flue gas pipeline is used as gas stripping equipment, the time of flue gas stripping is only 2-5 s, and the gas stripping effect is influenced.
In conclusion, no effective method for continuously treating the industrial waste salt containing toxic and harmful organic TOC in large batch exists at present, the utility model aims to solve the problem and provide a technical scheme for treating the industrial waste salt in energy-saving, large-batch and non-coking modes.
SUMMERY OF THE UTILITY MODEL
The technical scheme for realizing the purpose is as follows:
the utility model provides a system for treating industrial waste salt by a fluidized bed, which comprises a waste salt low-temperature drying unit, a crushing, screening and feeding unit, a fluidized bed medium-temperature steam stripping and oxidation treatment unit and a flue gas discharge unit;
the waste salt low-temperature drying unit is provided with a low-temperature drying dehydrator for removing surface water of the waste salt and part of volatile organic matters, namely VOC tail gas;
the crushing, screening and feeding unit is provided with a lifter, a crushing and screening machine and a screw feeder, the lifter is positioned at the downstream of a chute of the low-temperature drying and dewatering machine and can be lifted to a feeding hopper of the crushing and screening machine, waste salt is dried and dewatered, then falls to the lifter by gravity, is lifted by the lifter and is conveyed to the feeding hopper of the crushing and screening machine for crushing and screening, waste salt particles meeting the standard are screened out, a discharge port of the crushing and screening machine is communicated with the screw feeder, and qualified waste salt particles are quantitatively conveyed to a distribution plate of a suspension fluidized bed through the screw feeder;
the medium temperature steam-lifting oxidation treatment unit of the fluidized bed is provided with a suspension fluidized bed, a dilute phase section and a dense phase section are arranged in the fluidized bed from top to bottom, a distribution plate is arranged at the bottom of the dense phase section, the distribution plate is provided with a plurality of nozzles and sieve pores which are communicated with the dense phase section, the nozzles are communicated with combustion-supporting gas, the sieve pores are communicated with primary air and steam, the fluidized bed is provided with an overflow port or a bottom ascending pipe and a waste salt inlet communicated with the spiral feeder, the bottom ascending pipe is communicated with the outside of the fluidized bed, purified salt is discharged through the overflow port or the bottom ascending pipe, the waste salt inlet is close to the upper part of the distribution plate, waste salt sent from the spiral feeder is received through the distribution plate, the pipe orifice of the overflow port or the bottom ascending pipe is higher than the waste salt inlet, so that the waste salt can stay for a certain time, toxic and harmful organic TCO on the surface and the inner hole of the waste salt shell can be desorbed and volatilized fully, the dilute phase section is provided with a high-temperature combustion secondary combustion chamber, the secondary combustion chamber is communicated with combustion-supporting gas, secondary air and steam, and the dilute phase section is set as the secondary combustion chamber, so that the space of the dilute phase section of the fluidized bed can be fully utilized, and the equipment arrangement is simplified;
the flue gas emission unit is equipped with exhaust-heat boiler, air heater, cooling device, purifier, draught fan and the chimney that communicates in proper order, exhaust-heat boiler communicates the top of fluidized bed, high temperature flue gas at first produces saturated or superheated steam through exhaust-heat boiler to preheat the air, then through cooling device's cooling, most flying dust of purifier's purification desorption leads the chimney discharge through the draught fan.
Further, the low-temperature drying dehydrator is a roller dryer.
Furthermore, the low-temperature drying dehydrator is provided with a tail gas conveying pipeline communicated with the secondary combustion chamber and used for conveying VOC tail gas to the secondary combustion chamber for high-temperature combustion so as to thoroughly oxidize and decompose organic matters in the VOC tail gas into harmless flue gas.
Furthermore, the crushing and screening machine is also communicated with the hoister and is used for returning oversize materials to the feeding hopper for crushing and screening again, so that the waste salt is fully treated.
Further, the nozzles are uniformly distributed in the center of the distribution plate and on the annular circumference surrounding the center, the diameter of each nozzle is 10-200mm, the fluid spraying speed of each nozzle is 30-100m/s, waste salt particles in a bed layer are highly turbulent and well mixed, heat transfer thermal mass is promoted, and the diameter of each nozzle in actual operation depends on the steam amount, combustion-supporting gas amount and air amount required by material and heat balance in a suspended fluidized bed.
Further, the operating temperature of the dense-phase section is 200-600 ℃, preferably 300-400 ℃;
the operation temperature of the secondary combustion chamber is 1100-1200 ℃, and the flow rate of flue gas is 0.5-1.0 m/s.
Furthermore, the diameter of the secondary combustion chamber is larger than that of the dense phase section, which is beneficial to reducing the flue gas speed, ensuring that the retention time of VOC tail gas and VOC organic matters stripped by a suspension layer in the secondary combustion chamber reaches more than 2s, simultaneously reducing the flue gas speed, and also being beneficial to enabling a small amount of waste salt powder possibly carried by VOC to fall back to the dense phase section of the suspension fluidized bed by gravity after the VOC is melted in the secondary combustion chamber, and being re-cooled into solid particles by rising tail gas in the falling process and then being discharged by an overflow port or a bottom riser.
Further, the secondary combustion chamber is communicated with the waste heat boiler and the air preheater and is used for providing secondary air and steam for the secondary combustion chamber;
the sieve holes are communicated with the waste heat boiler and the air preheater and used for providing primary air and steam for the dense-phase section, so that heat and steam contained in tail gas are fully utilized, energy consumption is reduced, and enterprise cost is saved.
The utility model also provides a method of fluidized bed processing industry waste salt, including following step:
s1, heating and drying the waste salt, controlling the temperature at 150 ℃ and 300 ℃ to remove the outer surface water of the waste salt and desorb part of volatile organic matters, namely VOC tail gas, as far as possible;
s2, crushing and screening the waste salt, wherein the particle size of the crushed waste salt is 0.5-1.5 mm;
s3, fluidizing the waste salt particles in the dense phase section of the suspension fluidized bed by steam, combustion-supporting gas and air to make the waste salt particles highly turbulent and mixed, wherein the operation temperature is 200-;
s4, controlling the retention time of the waste salt in the suspension layer of the fluidized bed to be 60-120min, preferably 80-100min, discharging the clean salt, ensuring the sufficient turbulent mixing in the fluidized bed and ensuring the sufficient time for organic matter desorption and volatilization;
s5, burning the VOC organic matter stripped from the suspension layer in the dilute phase section of the fluidized bed at the operation temperature of 1100-1200 ℃, and taking the dilute phase section as a combustion chamber to fully utilize the space of the fluidized bed and simplify the equipment arrangement;
and S6, discharging the high-temperature flue gas, cooling and discharging.
Further, the VOC tail gas formed after the waste salt is heated in step S1 is introduced into step S5 to be burned so as to completely decompose the VOC tail gas generated in the drying and dehydrating process of the waste salt.
Has the advantages that: compared with the prior art, the utility model discloses a difference lies in, the utility model provides a system for fluidized bed treatment industry waste salt is provided with waste salt low temperature drying unit, crushing screening and feed unit, the middle temperature strip of fluidized bed and oxidation treatment unit and flue gas discharge unit for:
1. the waste salt particles are fully turbulent and mixed in the suspended fluidized bed, so that the problems of local overheating and coking are avoided, the steam stripping and oxidation temperature is controlled below the carbonization temperature of organic matters, and the coking and carbonization of the organic matters on the surface of the waste salt are avoided;
2. the height of the pipe orifice of the salt discharge overflow port or the bottom riser is controlled, so that the retention time of waste salt particles in the suspended fluidized bed is controlled, and the TOC attached to the surface or the inner hole of the waste salt can be removed completely under the conditions of sufficient turbulence, mixing, heat transfer and mass transfer of the waste salt in the fluidized bed, so that the standard of resource recycling or ocean dumping is met;
3. the treatment of the utility model is carried out under the condition of medium temperature, which is far lower than the melting point of the waste salt, the waste salt can not generate any melting ring formation phenomenon, and the obtained pure salt has better quality;
4. the fluidized bed reactor is used for treating the industrial waste salt, so that the problem that equipment such as microwave treatment and the like is difficult to amplify is solved, industrial application is easy to amplify, the industrial waste salt can be continuously treated in a large batch, the working efficiency is greatly improved, and the enterprise cost is saved.
Drawings
FIG. 1 is a schematic diagram of the operation of the system for treating industrial waste salt by a fluidized bed.
FIG. 2 is a schematic diagram of the operation of the moderate temperature stripping and oxidation treatment unit in the fluidized bed of the present application.
Fig. 3 is a top view of a distribution plate of the present application.
Wherein, the device comprises a 10-dilute phase section, a 20-dense phase section, a 21-distribution plate, a 1-nozzle, a 2-sieve hole, a 3-overflow port and a 4-bottom riser.
Detailed Description
The invention will be further explained with reference to the drawings and the specific embodiments.
Referring to fig. 1 and 2, the utility model provides a system for treating industrial waste salt by a fluidized bed, which comprises a waste salt low-temperature drying unit, a crushing, screening and feeding unit, a fluidized bed medium-temperature stripping and oxidation treatment unit and a flue gas discharge unit;
the waste salt low-temperature drying unit is provided with a low-temperature drying dehydrator for removing surface water of the waste salt and part of volatile organic matters, namely VOC tail gas;
the low-temperature drying dehydrator can be indirectly heated or directly heated, preferably indirectly heated, is a drum dryer, a heating medium is saturated steam supplied from the outside of the system, and can also preferably be saturated steam which is a byproduct recovered from the waste heat of high-temperature flue gas at the downstream, so that the energy is saved, the cost is reduced, the temperature of the low-temperature drying dehydration of the waste salt is controlled to be 300 ℃ at 150 ℃, and the external surface water of the waste salt and the volatile organic matters of a desorption part are removed as far as possible. The secondary steam containing the organic VOC is completely conveyed to a downstream secondary combustion chamber through a tail gas conveying pipeline for high-temperature combustion so as to completely oxidize and decompose organic matters in the secondary steam into harmless flue gas.
The crushing, screening and feeding unit is provided with a lifter, a crushing and screening machine and a screw feeder, the lifter is positioned at the downstream of a chute of the low-temperature drying and dewatering machine and can be lifted to a feeding hopper of the crushing and screening machine, waste salt is dried and dewatered, then falls to the lifter by gravity, is lifted by the lifter and is conveyed to the feeding hopper of the crushing and screening machine for crushing and screening, waste salt particles meeting the standard are screened out, a discharge port of the crushing and screening machine is communicated with the screw feeder, and qualified waste salt particles are quantitatively conveyed to a distribution plate of a suspension fluidized bed through the screw feeder;
preferably, the crushing and screening machine is further communicated with the elevator, after the waste salt is crushed, part of the waste salt falls down through the screening function of the crushing and screening machine by gravity to be called as undersize, part of the waste salt with larger particle diameter stays in the crushing and screening machine to be called as oversize, the oversize is returned to the feeding hopper through the elevator to be crushed and screened again, and the waste salt is circularly and repeatedly treated, and the waste salt is completely crushed to be the size of the required diameter.
The waste salt is dehydrated by a low-temperature drying dehydrator, crushed and sieved by a crushing and sieving machine, and is fed to a waste salt inlet by metering. The particle size of the waste salt is 0.5-1.0 mm, the original total water Mt of the waste salt is 40%, and the waste salt is dried to 5% -10%. The properties of the dry-based waste salt are given in the table below.
The steam-lift oxidation treatment unit in the fluidized bed is provided with a suspension fluidized bed, a dilute phase section 10 and a dense phase section 20 are arranged in the fluidized bed from top to bottom, a distribution plate 21 is arranged at the bottom of the dense phase section 20, the distribution plate 21 is provided with five nozzles 1 and sieve holes 2, the nozzles 1 are communicated with combustion-supporting gas, the sieve holes 2 are communicated with a downstream waste heat boiler and an air preheater to provide steam and primary air for the dense phase section 20, the air preheating temperature is 200 ℃, the steam is 0.5MPag superheated steam, the operating temperature of the dense phase section 20 is preferably 300-400 ℃, the temperature for steam stripping desorption and VOC partial oxidation is ensured to be lower than the carbonization temperature of organic matters, and organic carbon difficult to oxidize and burn is avoided; the fluidized bed is provided with an overflow port 3 or a bottom riser 4 and a waste salt inlet communicated with the screw feeder, the bottom riser 4 is vertically and downwardly communicated with the outside of the fluidized bed, purified salt is discharged through the overflow port 3 or the bottom riser 4, the waste salt inlet is close to the upper part of the distribution plate 21, waste salt sent by the screw feeder is received through the distribution plate 21, the pipe orifice of the overflow port 3 or the bottom riser 4 is higher than the waste salt inlet, the height of the pipe orifice is set to be 1500mm, the residence time of the waste salt in the fluidized bed for steam stripping and oxidation reaction is 100min, which is greatly different from the flue gas classification and air stripping time of CN108408744A of only 2-5 s, so that harmful organic TCO (transparent conductive oxygen) on the surface of a waste salt shell and an inner hole can be fully desorbed and volatilized, the dilute phase section 10 is provided with a high-temperature combustion secondary combustion chamber which is communicated with combustion-supporting gas, steam and secondary air provided by a downstream waste heat boiler and an air preheater, the dilute phase section 10 is set as a secondary combustion chamber, so that the space of the dilute phase section of the fluidized bed can be fully utilized, and the equipment arrangement is simplified;
the secondary combustion chamber may be provided as a straight section within the fluidized bed, i.e., extending vertically upward along the diameter of the primary dense-phase section 20, or more preferably as an expanded section, the diameter of the secondary combustion chamber is set to be larger than the diameter of the dense phase section 20, which is favorable for reducing the flue gas speed, the operating temperature is controlled within the range of 1100-1200 ℃, the flue gas flow rate is controlled to be 0.5-1.0m/s, the retention time of VOC tail gas and VOC organic matters in the secondary combustion chamber is ensured to reach more than 2s, any chlorinated aromatic hydrocarbon in the organic VOC stripped by steam is ensured to be completely combusted, no dioxin is generated, meanwhile, the flue gas velocity is reduced, which is beneficial to the gravity fall of a small amount of waste salt powder possibly carried by VOC to the dense phase section of the suspension fluidized bed after the VOC is melted in the secondary combustion chamber, and is cooled again into solid particles by the ascending tail gas in the falling process, and then is discharged from an overflow port or a bottom ascending pipe;
preferably, referring to fig. 3, the distribution plate 21 is provided with one nozzle 1 at the center, four nozzles 1 are further arranged around the center, the nozzles 1 are distributed around the center in a uniform circumference, the diameter of each nozzle 1 is 10-200mm, the fluid spraying speed of each nozzle 1 is 30-100m/s, waste salt particles in a bed layer are highly turbulent and are well mixed, and heat transfer thermal mass is promoted, and the diameter of each nozzle 1 in actual operation depends on the steam quantity and the combustion-supporting gas and air quantity required by material and heat balance in a suspended fluidized bed.
The flue gas emission unit is equipped with exhaust-heat boiler, air heater, cooling device, purifier, draught fan and the chimney that communicates in proper order, exhaust-heat boiler communicates the top of fluidized bed, high temperature flue gas at first produces saturated or superheated steam through exhaust-heat boiler to preheat the air through air heater, cool down to 500 ℃, then through cooling device rapid cooling to 200 ℃, avoid the dioxin to generate, purifier purifies desorption most flying dust, causes the chimney discharge through the draught fan at last.
The cooling device can be selected as a quenching tower (NaOH solution) for quenching and a semi-dry tower (baking soda and activated carbon) for capturing possible fly ash, and the purification device can be selected as a bag-type dust remover.
Specifically, waste salt is heated and dried by a low-temperature drying dehydrator, the temperature is controlled at 150 ℃ to 300 ℃, so that the surface water of the waste salt and the desorption part of volatile organic matters, namely VOC tail gas, are removed as far as possible;
then, crushing, screening and drying the dehydrated waste salt by a crushing and screening machine, wherein the particle size of the crushed waste salt is 0.5-1.5 mm;
then, the waste salt with qualified particle size enters the suspension fluidized bed through a waste salt inlet, and the waste salt particles are highly turbulent and mixed through fluidization of steam, combustion-supporting gas and air at the dense-phase section of the suspension fluidized bed, wherein the operation temperature is 200-600 ℃, and is preferably 300-400 ℃;
then, by setting the height of an overflow port or the pipe orifice of a bottom ascending pipe, controlling the retention time of the waste salt in the suspension layer of the fluidized bed to be 60-120min, preferably 80-100min, discharging the clean salt, ensuring the sufficient turbulent mixing in the fluidized bed and ensuring the sufficient time for desorbing and volatilizing the organic matters, wherein when the height is 1500mm, the retention time is 100 min;
then, burning the VOC organic matter stripped from the suspension layer in the dilute phase section of the fluidized bed at the operation temperature of 1100-1200 ℃, ensuring that all the organic matter is completely oxidized and decomposed, and under the condition that the TOC attached to the waste salt does not contain chlorinated organic matter and aromatic hydrocarbon, reducing the operation temperature of a secondary combustion chamber to 600-800 ℃, and taking the dilute phase section as a combustion chamber, so that the space of the fluidized bed can be fully utilized, and the equipment arrangement is simplified;
and finally, discharging the high-temperature flue gas through a waste heat boiler, an air preheater, a quench tower, a semi-dry tower, a bag-type dust collector, an EV heat exchanger and a draught fan and finally through a chimney.
When the low-temperature drying dehydrator is used for drying waste salt, part of VOC tail gas can be generated, and preferably, the part of VOC tail gas is sent to a secondary combustion chamber formed by a dilute phase section to be combusted together.
The above embodiments are merely preferred embodiments of the present disclosure, which are not intended to limit the present disclosure, and any modifications, equivalents, improvements and the like, which are within the spirit and principle of the present disclosure, should be included in the scope of the present disclosure.
Claims (8)
1. A system for treating industrial waste salt by a fluidized bed is characterized by comprising a waste salt low-temperature drying unit, a crushing, screening and feeding unit, a fluidized bed medium-temperature steam stripping and oxidation treatment unit and a flue gas discharge unit;
the waste salt low-temperature drying unit is provided with a low-temperature drying dehydrator;
the crushing, screening and feeding unit is provided with a lifter, a crushing and screening machine and a screw feeder, the lifter is positioned at the downstream of a chute of the low-temperature drying and dewatering machine and can be lifted to a feeding hopper of the crushing and screening machine, and a discharge port of the crushing and screening machine is communicated with the screw feeder;
the fluidized bed is provided with an overflow port or a bottom ascending pipe and a waste salt inlet communicated with the spiral feeder, the bottom ascending pipe is communicated with the outside of the fluidized bed, the waste salt inlet is close to the upper part of the distribution plate, the pipe orifice of the overflow port or the bottom ascending pipe is higher than the waste salt inlet, the dilute phase section is provided with a high-temperature combustion secondary combustion chamber, and the secondary combustion chamber is communicated with combustion-supporting gas, secondary air and steam;
the flue gas emission unit is equipped with exhaust-heat boiler, air heater, cooling device, purifier, draught fan and the chimney that communicates in proper order, exhaust-heat boiler communicates the top of fluidized bed.
2. The system for fluidized bed treatment of industrial waste salt according to claim 1, wherein:
the low-temperature drying dehydrator is a roller dryer.
3. The system for fluidized bed treatment of industrial waste salt according to claim 1 or 2, wherein:
the low-temperature drying dehydrator is provided with a tail gas conveying pipeline communicated with the secondary combustion chamber and used for conveying VOC tail gas to the secondary combustion chamber.
4. The system for fluidized bed treatment of industrial waste salt according to claim 1, wherein:
the crushing and screening machine is also communicated with the elevator and is used for returning oversize materials to the feeding hopper for secondary crushing and screening.
5. The system for fluidized bed treatment of industrial waste salt according to claim 1, wherein:
the nozzles are uniformly distributed in the center of the distribution plate and on the annular circumference surrounding the center, the diameter of each nozzle is 10-200mm, and the fluid spraying speed of each nozzle is 30-100 m/s.
6. The system for fluidized bed treatment of industrial waste salt according to claim 1, wherein:
the operating temperature of the dense-phase section is 200-600 ℃, and preferably 300-400 ℃;
the operation temperature of the secondary combustion chamber is 1100-1200 ℃, and the flow rate of flue gas is 0.5-1.0 m/s.
7. The system for fluidized bed treatment of industrial waste salt according to claim 1, wherein:
the diameter of the secondary combustion chamber is larger than that of the dense-phase section.
8. The system for fluidized bed treatment of industrial waste salt according to claim 1 or 7, wherein:
the secondary combustion chamber is communicated with the waste heat boiler and the air preheater and is used for providing secondary air and steam for the secondary combustion chamber;
the sieve holes are communicated with the waste heat boiler and the air preheater and are used for providing primary air and steam for the dense-phase section.
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111167841A (en) * | 2020-02-27 | 2020-05-19 | 亚德（上海）环保系统有限公司 | System and method for treating industrial waste salt by fluidized bed |
| CN112879922A (en) * | 2021-01-06 | 2021-06-01 | 浙江工业大学 | Method and device for treating industrial waste salt by plasma torch |
| CN113877937A (en) * | 2021-10-18 | 2022-01-04 | 亚德（上海）环保系统有限公司 | Method and system for treating waste salt through microwave thermal desorption and oxidation of rotary kiln |
| CN114249336A (en) * | 2021-12-30 | 2022-03-29 | 盐城市国投环境技术股份有限公司 | Process for preparing industrial sodium carbonate by using chemical tail gas waste salt |
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2020
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| CN111167841A (en) * | 2020-02-27 | 2020-05-19 | 亚德（上海）环保系统有限公司 | System and method for treating industrial waste salt by fluidized bed |
| CN112879922A (en) * | 2021-01-06 | 2021-06-01 | 浙江工业大学 | Method and device for treating industrial waste salt by plasma torch |
| CN113877937A (en) * | 2021-10-18 | 2022-01-04 | 亚德（上海）环保系统有限公司 | Method and system for treating waste salt through microwave thermal desorption and oxidation of rotary kiln |
| CN113877937B (en) * | 2021-10-18 | 2023-12-26 | 亚德（上海）环保系统有限公司 | Method and system for thermal desorption and oxidation treatment of waste salt through rotary kiln microwaves |
| CN114249336A (en) * | 2021-12-30 | 2022-03-29 | 盐城市国投环境技术股份有限公司 | Process for preparing industrial sodium carbonate by using chemical tail gas waste salt |
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