CN110805914A - Rotary kiln drying incineration process for PTA activated sludge with additional pre-dryer - Google Patents
Rotary kiln drying incineration process for PTA activated sludge with additional pre-dryer Download PDFInfo
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- CN110805914A CN110805914A CN201911095636.8A CN201911095636A CN110805914A CN 110805914 A CN110805914 A CN 110805914A CN 201911095636 A CN201911095636 A CN 201911095636A CN 110805914 A CN110805914 A CN 110805914A
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- pta
- activated sludge
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
- F23G7/00—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F11/00—Treatment of sludge; Devices therefor
- C02F11/12—Treatment of sludge; Devices therefor by de-watering, drying or thickening
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
- F23G5/00—Incineration of waste; Incinerator constructions; Details, accessories or control therefor
- F23G5/08—Incineration of waste; Incinerator constructions; Details, accessories or control therefor having supplementary heating
- F23G5/14—Incineration of waste; Incinerator constructions; Details, accessories or control therefor having supplementary heating including secondary combustion
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
- F23G5/00—Incineration of waste; Incinerator constructions; Details, accessories or control therefor
- F23G5/44—Details; Accessories
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
- F23G7/00—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals
- F23G7/06—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals of waste gases or noxious gases, e.g. exhaust gases
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- Environmental & Geological Engineering (AREA)
- Mechanical Engineering (AREA)
- General Engineering & Computer Science (AREA)
- Life Sciences & Earth Sciences (AREA)
- Hydrology & Water Resources (AREA)
- Water Supply & Treatment (AREA)
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Treatment Of Sludge (AREA)
- Incineration Of Waste (AREA)
Abstract
The invention provides a rotary kiln drying incineration process for PTA activated sludge, which is additionally provided with a pre-dryer, wherein the pre-dryer is additionally arranged at the front end of a rotary kiln to pre-dry the PTA activated sludge, then the rotary kiln is sent into a rotary kiln to incinerate and remove a large amount of combustible organic matters, so that cobalt manganese oxide is efficiently recovered from the PTA activated sludge, and waste gas generated in the incineration process passes through a secondary combustion chamber, a waste heat boiler, cyclone dust removal, a quench tower and a cloth bag for dust removal, is desulfurized and oxidized, and then is returned to the rotary kiln together with air. The invention has the advantages that the partial waste gas after the temperature reduction treatment of the quenching tower is shunted to dry the PTA activated sludge in the pre-drier, the moisture in the PTA activated sludge is primarily removed greatly, the burning efficiency of the subsequent rotary kiln is improved, in addition, the heat energy of the waste gas is fully utilized, and the recovery and the utilization of the heat energy are realized.
Description
Technical Field
The invention relates to a rotary kiln drying incineration process for PTA activated sludge with an additional pre-dryer, belonging to the field of industrial sludge synergistic treatment.
Background
Terephthalic Acid (PTA) is an important petrochemical product with the yield in the first fifty places of the world, is a main raw material for producing Polyester (PET), and is widely applied to the production fields of fiber terylene, polyester films, packaging bottles, PBT engineering plastics, plastic plasticizers, pesticides, dyes and the like. In the PTA production process, the produced wastewater contains a large amount of organic compounds such as benzoic acid, terephthalic acid, isophthalic acid and the like, and also contains metal compounds such as cobalt, manganese and the like, the metal compounds are derived from a catalyst in the terephthalic acid production process, after the metal compounds are treated by an activated sludge method, cobalt ions and manganese ions enter a sludge phase from a liquid phase, are gradually enriched, are dehydrated and compressed to form a sludge cake, and are conveyed out.
Cobalt and manganese metal ions are difficult to remove in PTA sewage treatment, the content of cobalt and manganese metal ions in discharged waste mud exceeds the standard every year, and the cobalt and manganese can not be separated due to the limitation of the traditional recovery technology, so that resources are wasted and the environment is threatened.
In the method and the equipment for drying and incinerating the PTA activated sludge provided in CN201310261546.8, the rotary kiln is used for incinerating the PTA activated sludge to realize the treatment of the PTA activated sludge, and the heat of the PTA activated sludge incineration waste gas is recycled in the process. However, in the process of recycling the heat of the exhaust gas, after the incineration exhaust gas is subjected to dust removal and harm removal treatment, the exhaust gas is blown into a rotary dryer and a rotary incineration kiln through a high-temperature induced draft fan and a fluidized bed furnace to dry and incinerate the PTA activated sludge, the process is complex and tedious, in addition, the heat loss of the exhaust gas is large in the process, thermocouples need to be arranged at multiple points to increase the temperature of the exhaust gas, and the process cost is increased by the output of electric energy; in addition, the bubbling gas of the fluidized bed combustion boiler involved in the patent is respectively shunted to the rotary dryer and the rotary incinerator, resulting in the same operating temperature of the rotary dryer and the rotary incinerator, which may result in over-drying decomposition of the PTA sludge in the rotary dryer or insufficient incineration in the rotary incinerator.
Disclosure of Invention
Aiming at the existing problems, the invention provides a rotary kiln drying incineration process for PTA activated sludge, which is additionally provided with a pre-dryer, for solving the technical problems.
The invention aims to realize the drying incineration process of the PTA activated sludge rotary kiln with the additional pre-dryer, which is characterized by comprising the following steps:
A. feeding PTA activated sludge into a pre-drier, and drying the PTA activated sludge by using waste gas cooled by a quench tower to preliminarily reduce the water content of the PTA activated sludge;
B. taking crude benzoic acid rectification residues as fuel, supporting combustion by natural gas, sending the crude benzoic acid rectification residues into a combustor for combustion, and providing a heat source for the rotary kiln;
feeding the PTA activated sludge treated by the predrying device in the step A and the high-temperature waste gas after passing through the quenching tower into a rotary kiln, drying and burning in the rotary kiln, removing a large amount of water and organic matters in the PTA activated sludge to obtain burned residues of the PTA activated sludge, and fully enriching valuable metal cobalt and manganese components in the burned residues for preparing a cobalt manganese oxide product;
C. conveying incineration waste gas generated in the incineration process of the PTA activated sludge in the step B into a secondary chamber for combustion;
D. after the heat in the high-temperature waste gas combusted in the secondary combustion chamber is recovered by a waste heat boiler, cobalt manganese oxide particles contained in the waste gas are recovered by cyclone dust removal, a quench tower and a cloth bag dust removal in sequence, and then partial tail gas is returned to the rotary kiln together with air after desulfurization and oxidation;
and (3) shunting part of high-temperature gas from the tail gas of the quenching tower, and blowing the high-temperature gas into a predrying device to dry the PTA activated sludge.
In the step A, the predrying device is arranged at the front end of the rotary kiln, and partial tail gas cooled by the quench tower is blown into the predrying device by using a flow dividing valve, wherein PTA activated sludge and high-temperature waste gas are dried by adopting downstream contact.
In the step A, the temperature of the flue gas entering the pre-drier is 150-200 ℃, and the retention time of PTA activated sludge in the pre-drier is 30 min.
In the step B, the burning temperature of the rotary kiln is about 850 ℃, the inclination of the rotary kiln is 4%, the rotating speed of the rotary kiln is 2.5rpm, the retention time of PTA activated sludge is 45min, and the feeding direction of the PTA activated sludge is opposite to the air flow direction.
And step C, blowing the dried gas entering the rotary kiln and incineration waste gas generated in the incineration process into a secondary combustion chamber for combustion.
In the step C, the working temperature in the secondary combustion chamber is more than or equal to 1100 ℃, and the retention time of the flue gas is more than or equal to 2 s.
The water content of the PTA activated sludge is 80%.
Temperature control programs are arranged at the feed end of the predrying device, the feed end and the discharge end of the rotary kiln, the secondary combustion chamber, the exhaust-heat boiler air outlet, the cyclone dust removal air inlet, the quench tower air outlet and the cloth bag dust removal air inlet.
Has the advantages that: the method comprises the steps of adding a pre-dryer at the front end of the rotary kiln to pre-dry PTA activated sludge, then sending the pre-dried PTA activated sludge into the rotary kiln to burn and remove a large amount of water and combustible organic matters, further realizing the efficient recovery of cobalt manganese oxide from the PTA activated sludge, removing dust from waste gas generated in the burning process through a secondary combustion chamber, a waste heat boiler, cyclone dust removal, a quench tower and a cloth bag, and returning the waste gas and air into the rotary kiln after desulfurization and oxidation.
The method has the advantages that the partial waste gas after the temperature reduction treatment of the quenching tower is shunted dries the PTA activated sludge in the predrying device, the moisture in the PTA activated sludge is removed greatly preliminarily, and the moisture content in the PTA sludge is reduced, so that the retention time of the PTA sludge in the rotary kiln can be shortened, the heat energy requirement in the rotary kiln is reduced, and the burning efficiency of the rotary kiln is further improved; in addition, the heat energy of the waste gas is fully utilized, and the recovery and utilization of the heat energy are realized; the process is simple, the recovery rate of cobalt and manganese oxide is up to 99%, and the purity of cobalt and manganese oxide can also be up to about 93%.
Drawings
FIG. 1 is a process flow diagram used in the present invention.
Detailed Description
The technical solutions in the examples of the present invention will be described in detail below with reference to the accompanying drawings in the examples of the present invention.
The invention relates to a rotary kiln drying incineration process of PTA activated sludge with an additional pre-dryer, which comprises the following steps:
A. feeding PTA activated sludge into a pre-drier, drying the PTA activated sludge by using waste gas cooled by a quench tower to reduce the moisture content of the PTA activated sludge preliminarily, and then feeding the sludge subjected to preliminary drying and high-temperature flue gas into a rotary kiln for further treatment;
B. crude benzoic acid rectification residues are used as fuel, and are conveyed into a combustor for combustion through natural gas combustion supporting, so that a heat source is provided for the rotary kiln. Drying and burning the PTA activated sludge treated by the predrying device in a rotary kiln to remove a large amount of water and organic matters, and fully enriching valuable metal cobalt and manganese components in the burned residues for preparing cobalt manganese oxide products;
C. conveying incineration waste gas generated in the process of burning PTA activated sludge into a secondary chamber for combustion;
D. after the heat in the high-temperature waste gas combusted in the secondary combustion chamber is recovered by a waste heat boiler, the high-temperature waste gas sequentially passes through cyclone dust removal, a quench tower and a cloth bag dust removal to recover cobalt manganese oxide particles mixed in the waste gas, and then part of tail gas is shunted after desulfurization and oxidation and is returned to the rotary kiln together with air;
E. in addition, a part of high-temperature gas is branched from the tail gas of the quenching tower and sent to a predrying device for drying the PTA activated sludge.
Further, in the step A, a predrying device is arranged at the front end of the rotary kiln, and a part of tail gas cooled by the quenching tower is blown into the predrying device by utilizing a flow dividing valve.
In the step A, the temperature of the flue gas entering the pre-drier is 150-200 ℃, and the retention time of PTA sludge in the pre-drier is 30 min.
In the step A, the burning temperature of the rotary kiln is about 850 ℃, the inclination of the rotary kiln is 4%, the rotating speed of the rotary kiln is 2.5rpm, the retention time of PTA activated sludge is 45min, and the feeding direction of the PTA activated sludge is opposite to the air flow direction.
In the step B, the drying gas entering the rotary kiln and the incineration waste gas generated in the incineration process are collected at the top of the rotary kiln and are blown into a secondary combustion chamber for combustion.
The working temperature in the secondary combustion chamber is more than or equal to 1100 ℃, and the smoke retention time is more than or equal to 2 s.
Temperature control programs are arranged at the feed end of the predrying device, the feed/discharge end of the rotary kiln, the secondary combustion chamber, the exhaust-heat boiler air outlet, the cyclone dust removal air inlet, the quench tower air outlet and the cloth bag dust removal air inlet.
In addition, the water content of the PTA activated sludge is about 80%.
As shown in fig. 1, the distillation residue generated in the benzoic acid production process is sent into a burner to support combustion with natural gas and provide heat energy for the rotary kiln, air is blown in from an air inlet near the burner end of the rotary kiln, and PTA sludge is input from the other end of the rotary kiln to be subjected to high-temperature incineration, wherein the transmission directions of the PTA sludge and the air are opposite in the high-temperature incineration process; and (3) removing a large amount of organic matters in the PTA sludge subjected to high-temperature incineration, and collecting the obtained cobalt manganese oxide residues flowing out from the bottom of the rotary kiln close to the burner end. Waste gas generated in the sludge incineration process is sent into a secondary combustion chamber for incineration, the incineration waste gas is subjected to heat recovery by a waste heat boiler, then is subjected to cyclone dust removal and cooling by a quench tower in sequence, cobalt manganese oxide particles in the incineration waste gas are recovered by cloth bag dust removal, and the tail gas after dust removal is subjected to desulfurization, oxidation and purification and then is returned to the rotary kiln together with air. In addition, a part of high-temperature gas is branched from the tail gas of the quenching tower and is blown into a predrying device to carry out drying treatment on the PTA activated sludge, wherein the sludge and the high-temperature waste gas are dried by adopting concurrent contact. In the process, the treatment process can be regulated and controlled in real time through temperature control programs of a feed end of a pre-drier, a feed/discharge end of a rotary kiln, a secondary combustion chamber, a gas outlet of a waste heat boiler, a gas inlet of cyclone dust removal, a gas outlet of a quench tower and a gas inlet of cloth bag dust removal.
Taking the process flow of the invention to dry and incinerate 1 ton of PTA activated sludge as an example, the related benefits are considered. Wherein, the water content of the PTA sludge is 83.71 percent, and the content of cobalt and manganese elements is 6.42 percent. Wherein the temperature of the pre-drier is 150 ℃, the retention time of sludge in the pre-drier is 30min, the burning temperature of the rotary kiln is 850 ℃, the retention time of sludge in the rotary kiln is 45min, the temperature of the secondary combustion chamber is 1100 ℃, the retention time of flue gas is 2s, 70 percent of high-temperature gas is shunted from tail gas of the quench tower, and the high-temperature gas is blown into the pre-drier.
Through engineering tests and engineering calculation, 1 ton of PTA activated sludge is processed, about 1.5 hours is saved, the flow of the used combustion-supporting natural gas is 140m for carrying out heavy planting/h, and the natural gas is saved by 1.5 x 140 x 4.5=945 yuan according to 4.5 yuan/cubic meter. In the pre-drying process of PTA sludge, if the drying is carried out by electric energy heating, about 600 degrees of electricity is expected to be consumed by drying 1 ton of PTA sludge with the water content of 80%, and the total cost is 600 yuan if the industrial electricity is 1 yuan/meter. Therefore, the PTA sludge is subjected to pre-dehydration treatment by adding the pre-drier, and the waste gas subjected to cooling treatment by the quenching tower is used as a drying heat source, so that the incineration efficiency of the rotary kiln can be obviously improved, meanwhile, the heat energy of the waste gas is fully utilized, and the process production cost is reduced.
After the treatment by the process, the collectable rotary kiln manganese cobalt oxide residue reaches 63.52kg, the PTA sludge has obvious weight-reducing and volume-reducing effects, the purity of the collected manganese cobalt oxide can reach 92.70%, and the purity of the manganese cobalt oxide collected by cyclone dust collection and cloth bag dust collection can reach 99.97%.
In conclusion, the rotary kiln drying incineration process for PTA activated sludge, which is additionally provided with the pre-dryer, can obviously improve the incineration efficiency of the rotary kiln; meanwhile, the recycling and utilization of heat energy can be realized, the production cost of the process is reduced, and the method has obvious environmental and economic benefits.
Claims (8)
1. A rotary kiln drying incineration process for PTA activated sludge with an additional pre-dryer is characterized by comprising the following steps:
A. feeding PTA activated sludge into a pre-drier, and drying the PTA activated sludge by using waste gas cooled by a quench tower to preliminarily reduce the water content of the PTA activated sludge;
B. taking crude benzoic acid rectification residues as fuel, supporting combustion by natural gas, sending the crude benzoic acid rectification residues into a combustor for combustion, and providing a heat source for the rotary kiln;
feeding the PTA activated sludge treated by the predrying device in the step A and the high-temperature waste gas after passing through the quenching tower into a rotary kiln, drying and burning in the rotary kiln, removing a large amount of water and organic matters in the PTA activated sludge to obtain burned residues of the PTA activated sludge, and fully enriching valuable metal cobalt and manganese components in the burned residues for preparing a cobalt manganese oxide product;
C. conveying incineration waste gas generated in the incineration process of the PTA activated sludge in the step B into a secondary chamber for combustion;
D. after the heat in the high-temperature waste gas combusted in the secondary combustion chamber is recovered by a waste heat boiler, cobalt manganese oxide particles contained in the waste gas are recovered by cyclone dust removal, a quench tower and a cloth bag dust removal in sequence, and then partial waste gas is shunted after desulfurization and oxidation and is returned to the rotary kiln together with air;
and (3) shunting part of high-temperature gas from the waste gas of the quenching tower, and blowing the high-temperature gas into a predrying device to dry the PTA activated sludge.
2. The rotary kiln drying and incinerating process for PTA activated sludge with the added predryer as claimed in claim 1, wherein in step A, the predryer is arranged at the front end of the rotary kiln, and a part of the waste gas cooled by the quench tower is blown into the predryer by a diverter valve, wherein the PTA activated sludge and the high-temperature waste gas are dried by concurrent contact.
3. The rotary kiln drying incineration process of PTA activated sludge with an additional predryer as claimed in claim 1, wherein in the step A, the temperature of the flue gas entering the predryer is 150-200 ℃, and the retention time of the PTA activated sludge in the predryer is 30 min.
4. The rotary kiln drying incineration process of PTA activated sludge with an additional pre-dryer as claimed in claim 1, wherein in step B, the rotary kiln incineration temperature is about 850 ℃, the rotary kiln inclination is 4%, the rotary kiln rotation speed is 2.5rpm, the PTA activated sludge retention time is 45min, and the feeding direction is opposite to the air flow direction.
5. The rotary kiln drying incineration process of PTA activated sludge with the added pre-dryer as claimed in claim 1, wherein in step C, the drying gas entering the rotary kiln and the incineration exhaust gas generated in the incineration process are blown into a secondary combustion chamber for combustion.
6. The rotary kiln drying incineration process of PTA activated sludge with an additional pre-dryer as claimed in claim 1, wherein in step C, the working temperature in the secondary chamber is not less than 1100 ℃, and the smoke retention time is not less than 2 s.
7. The rotary kiln drying incineration process of PTA activated sludge with an additional pre-dryer as claimed in claim 1, wherein the moisture content of the PTA activated sludge is 80%.
8. The rotary kiln drying and incinerating process for PTA activated sludge with an additional predryer as claimed in claim 1, wherein a temperature control program is arranged at the feed end of the predryer, the feed and discharge ends of the rotary kiln, the secondary combustion chamber, the exhaust-heat boiler gas outlet, the gas inlet of cyclone dust collection, the gas outlet of the quench tower and the gas inlet of the bag dust collection.
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| CN201911095636.8A CN110805914A (en) | 2019-11-11 | 2019-11-11 | Rotary kiln drying incineration process for PTA activated sludge with additional pre-dryer |
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| CN201911095636.8A CN110805914A (en) | 2019-11-11 | 2019-11-11 | Rotary kiln drying incineration process for PTA activated sludge with additional pre-dryer |
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Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20060046217A1 (en) * | 2004-09-02 | 2006-03-02 | Parker Joseph L | Waste treatment system for PTA and PET manufacturing plants |
| CN204756949U (en) * | 2015-04-30 | 2015-11-11 | 江苏华旭再生资源利用有限公司 | Device of preparation cobalt oxide manganese among follow PTA activated sludge |
| CN106111667A (en) * | 2016-06-29 | 2016-11-16 | 福建正仁环保有限公司 | Biomass are prepared RDF 4 smokeless and are burned steam-electric power technique |
| CN108358407A (en) * | 2018-02-12 | 2018-08-03 | 常州德诚环境科技有限公司 | PTA oxidation residuas and comprehensive utilization of mud system and method |
| CN110220203A (en) * | 2019-06-11 | 2019-09-10 | 宜昌桑德环保科技有限公司 | A kind of dangerous waste incinerator returns cigarette control system |
-
2019
- 2019-11-11 CN CN201911095636.8A patent/CN110805914A/en active Pending
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20060046217A1 (en) * | 2004-09-02 | 2006-03-02 | Parker Joseph L | Waste treatment system for PTA and PET manufacturing plants |
| CN204756949U (en) * | 2015-04-30 | 2015-11-11 | 江苏华旭再生资源利用有限公司 | Device of preparation cobalt oxide manganese among follow PTA activated sludge |
| CN106111667A (en) * | 2016-06-29 | 2016-11-16 | 福建正仁环保有限公司 | Biomass are prepared RDF 4 smokeless and are burned steam-electric power technique |
| CN108358407A (en) * | 2018-02-12 | 2018-08-03 | 常州德诚环境科技有限公司 | PTA oxidation residuas and comprehensive utilization of mud system and method |
| CN110220203A (en) * | 2019-06-11 | 2019-09-10 | 宜昌桑德环保科技有限公司 | A kind of dangerous waste incinerator returns cigarette control system |
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Application publication date: 20200218 |
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