CN113831926A - Anaerobic pyrolysis treatment device and method for printing ink slag - Google Patents
Anaerobic pyrolysis treatment device and method for printing ink slag Download PDFInfo
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- CN113831926A CN113831926A CN202111194982.9A CN202111194982A CN113831926A CN 113831926 A CN113831926 A CN 113831926A CN 202111194982 A CN202111194982 A CN 202111194982A CN 113831926 A CN113831926 A CN 113831926A
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
- C10B53/00—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
- C10B49/00—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated
- C10B49/02—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated with hot gases or vapours, e.g. hot gases obtained by partial combustion of the charge
- C10B49/04—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated with hot gases or vapours, e.g. hot gases obtained by partial combustion of the charge while moving the solid material to be treated
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
- C10B57/00—Other carbonising or coking processes; Features of destructive distillation processes in general
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Abstract
The invention discloses an anaerobic pyrolysis treatment device and method for ink slag, wherein the ink slag to be treated is pretreated by an ink slag pretreatment system to obtain pretreated ink slag; performing pyrolysis treatment on the pretreated printing ink slag by adopting a preset low-pressure high-temperature superheated steam in a countercurrent direct contact mode through an anaerobic pyrolysis system; generating low-pressure saturated steam by a steam generation system, and obtaining low-pressure high-temperature superheated steam for an anaerobic pyrolysis system after the low-pressure saturated steam is superheated by high-temperature flue gas; treating the high-temperature flue gas from the steam generation system through a flue gas treatment system; and discharging the flue gas treated by the flue gas treatment system through a flue gas discharge system. The device can realize the self-sustaining operation of the device without external energy after stable operation, the ink residues originally classified as hazardous waste after being treated by the device can realize good harmlessness, reduction and resource utilization, and the device has the comprehensive advantages of low treatment cost, high treatment degree and less comprehensive energy consumption of the device.
Description
Technical Field
The invention relates to the technical field of PCB (printed circuit board) ink residue treatment, in particular to an anaerobic pyrolysis treatment device and method for ink residue.
Background
A Printed Circuit Board (PCB) is an important electronic component, and is a support for an electronic component and a carrier for electrical connection of the electronic component. The PCB ink is ink used in PCB manufacture, is composed of a plurality of components such as pigment, a coupling agent, an organic solvent, an auxiliary agent and the like, and is an important part in PCB manufacture. The PCB is printed/sprayed with ink, exposed and developed, residual ink is removed by alkali liquor to form alkaline high-content organic/inorganic waste water, and solid components in the alkaline high-content organic/inorganic waste water are separated by centrifugal/filter pressing and other technological operations to form ink residues.
The PCB is irreplaceable in the whole electronic product, and any electronic equipment or product is required to be equipped with the PCB. With the continuous enlargement of the domestic PCB industrial scale, the market demand of the special printing ink for the PCB is rapidly developed, and the amount of the correspondingly generated printing ink slag is increased year by year. Because the ink residues have the characteristics of high toxicity, high pollution and the like, if the ink residues are not treated in time, the continuous accumulation of the ink residues not only occupies a large amount of land, but also causes serious pollution to the surrounding soil, water and air. Meanwhile, the ink residue is dangerous waste (HW12, national hazardous waste list (2021 edition)), and if the hazardous factors are not treated, the sustainable development of enterprises can be greatly influenced. Therefore, no matter from the social ecological environment factors or the sustainability development factors of enterprises, finding an efficient and economic way to treat the ink residues produced by the PCB industry becomes a work which is beneficial to the nation and the people and has practical significance.
At present, the treatment/disposal of the ink slag mainly comprises the following methods:
(1) physical method: drying and crushing the ink residues, and mixing the crushed ink residues with other materials to prepare products such as building templates for recycling;
(2) the chemical method comprises the following steps: carrying out acidification neutralization and then carrying out reduction by means of high-speed centrifugation/filter pressing and the like to prepare dry film slag;
(3) the burning method comprises the following steps: the ink slag is directly reduced and treated harmlessly by high-temperature incineration in an incinerator.
The above treatment methods are comprehensively analyzed, the first treatment method has the advantages of capability of effectively recycling the ink residues, simplicity and convenience in treatment, direct treatment and the like, but reduction and harmlessness cannot be realized, and the reuse of the ink residues as raw materials has the defects of low large scale, low market acceptance, unsmooth finished product sale and the like at present, so that the method is not universally applied; although the second treatment method can realize certain reduction and harmlessness, the influence of the ink residues on the ecological environment can be eliminated only by subsequent treatment, and the harmlessness, the reduction and the like of the ink residues cannot be completely realized, so the second treatment method is mainly used for an intermediate treatment stage of the ink residues; the third treatment mode can realize thorough harmlessness and reduction of the ink residues, and can realize partial energy recycling and other advantages during incineration based on the high calorific value attribute of the ink residues, but high-toxicity substances such as dioxin are easily generated during incineration, and the defects of large primary investment, high treatment cost and the like exist, so that great pressure is generated on the ecological environment and social economy.
Therefore, the existing ink residue treatment method can not realize effective treatment on the ink residue, or has high cost, no good practicability and operability and large influence on comprehensive energy consumption and cracking efficiency.
Disclosure of Invention
The invention mainly aims to provide an anaerobic pyrolysis treatment device and method for ink slag, which can effectively treat the ink slag and have the comprehensive advantages of low treatment cost, high treatment degree and low comprehensive energy consumption of the device.
In order to achieve the purpose, the invention provides an anaerobic pyrolysis treatment device for ink residues, which comprises: printing ink sediment pretreatment systems, anaerobic pyrolysis system, steam generation system, flue gas processing system and flue gas discharge system, wherein:
the ink residue pretreatment system is used for pretreating ink residues to be treated to obtain pretreated ink residues;
the anaerobic pyrolysis system is used for carrying out pyrolysis treatment on the pretreated printing ink slag in a mode of direct countercurrent contact by adopting preset low-pressure high-temperature superheated steam;
the steam generation system is used for generating low-pressure saturated steam, obtaining low-pressure high-temperature superheated steam after the low-pressure saturated steam is superheated by high-temperature flue gas and supplying the low-pressure high-temperature superheated steam to the anaerobic pyrolysis system;
the flue gas treatment system is used for treating the high-temperature flue gas from the steam generation system;
and the flue gas emission system is used for emitting the flue gas treated by the flue gas treatment system.
Optionally, the ink residue pretreatment system comprises: printing ink sediment breaker, screw conveyer, drying-machine, belt weigher that connect gradually, wherein:
the exit linkage of printing ink sediment breaker to screw conveyer's feed inlet, screw conveyer's discharge gate with the material import of drying-machine is connected, the material export of drying-machine with the entry of belt weigher is connected, the export of belt weigher with anaerobic pyrolysis system is connected.
Optionally, a steam inlet and a waste steam outlet of the dryer are respectively connected with the steam generation system.
Optionally, the anaerobic pyrolysis system comprises: the spiral feeder, the preheater, the pyrolysis reactor and the cyclone separator are connected in sequence; wherein:
the inlet of the spiral feeder is connected with the outlet of the belt weigher, the outlet of the spiral feeder is communicated with the material inlet of the preheater, the material outlet of the preheater is communicated with the material inlet of the pyrolysis reactor, the gas phase outlet of the preheater is connected with the inlet of the cyclone separator, and the gas phase outlet of the cyclone separator is connected with the steam generation system; and the gas-phase inlet of the pyrolysis reactor is communicated with the steam generation system.
Optionally, a screw is arranged in the center of the preheater and the pyrolysis reactor; the connection pipe of the material outlet of the preheater and the material inlet of the pyrolysis reactor serves as a gas phase outlet pipe of the pyrolysis reactor.
Optionally, the steam generation system comprises: direct combustion chamber, over heater, steam boiler, wherein:
a gas phase inlet of the direct combustion chamber is connected with a gas phase outlet of the cyclone separator, and a dead steam outlet of the dryer is connected with the other gas phase inlet of the direct combustion chamber; the flue gas outlet of the direct combustion chamber is connected with the flue gas inlet of the superheater, and the flue gas outlet of the superheater is connected with the flue gas inlet of the steam boiler; the smoke outlet of the steam boiler is connected with the smoke treatment system; the combustion system to which the direct combustion chamber belongs comprises a fuel feeding system, combustion air and a combustion air system; a boiler water inlet of the steam boiler is connected with a boiler water preparation system; one path of a steam outlet of the steam boiler is connected with a steam inlet of the superheater, and the other path of the steam outlet of the steam boiler is communicated with a steam inlet of the dryer; and a steam outlet of the superheater is connected with a gas-phase inlet of the pyrolysis reactor.
Optionally, the flue gas treatment system comprises: flue gas reheater, half-dry deacidification tower, bag collector, venturi cooler and scrubbing tower that connect gradually, wherein:
a flue gas inlet at one side of the flue gas reheater is connected with a flue gas outlet of the steam boiler, a flue gas outlet at one side of the flue gas reheater is connected with a flue gas inlet of the semi-dry type deacidification tower, and a flue gas outlet of the semi-dry type deacidification tower is connected with a flue gas inlet of the bag type dust collector; the flue gas outlet of the bag type dust collector is connected with the flue gas inlet of the Venturi cooler, and the bottom outlet of the Venturi cooler is connected with the lower inlet of the washing tower; and a top flue gas outlet of the washing tower is connected with a flue gas inlet at the other side of the flue gas reheater, and a flue gas outlet at the other side of the flue gas reheater is connected with the flue gas discharge system.
Optionally, the flue gas emission system comprises: a flue gas induced draft fan and a chimney; the inlet of the flue gas induced draft fan is connected with the flue gas outlet at the other side of the flue gas reheater, and the outlet of the flue gas induced draft fan is connected with the inlet of the chimney.
Optionally, the dryer performs drying by using an indirect heating mode; the rotating speed of a built-in screw part of the pyrolysis reactor is 5-50 rpm, the material filling coefficient is 0.1-0.45, and the reaction retention time is less than or equal to 30 min; and/or the presence of a gas in the gas,
the temperature of a dead steam outlet of the dryer is controlled to be 90-100 ℃; the temperature of a high-temperature superheated steam inlet of the pyrolysis reactor is controlled to be between 400 and 800 ℃, and the temperature of a pyrolysis gas outlet of the preheater is controlled to be between 200 and 400 ℃; and/or the presence of a gas in the gas,
the operation pressure of the preheater and the pyrolysis reactor is micro-negative pressure operation, and the outlet temperature of waste residue of the pyrolysis reactor is 400-600 ℃; and/or the presence of a gas in the gas,
the operation temperature of the direct combustion chamber is 850-1200 ℃, and the temperature of the smoke outlet of the steam boiler is 300-500 ℃.
In addition, the embodiment of the invention also provides an anaerobic pyrolysis treatment method for the ink slag, which comprises the following steps:
pretreating the ink slag to be treated by an ink slag pretreatment system to obtain pretreated ink slag;
performing pyrolysis treatment on the pretreated printing ink slag by adopting a preset low-pressure high-temperature superheated steam in a countercurrent direct contact mode through an anaerobic pyrolysis system;
generating low-pressure saturated steam by a steam generation system, and obtaining low-pressure high-temperature superheated steam for the anaerobic pyrolysis system after the low-pressure saturated steam is superheated by high-temperature flue gas;
treating the high-temperature flue gas from the steam generation system through a flue gas treatment system;
and discharging the flue gas treated by the flue gas treatment system through a flue gas discharge system.
According to the device and the method for the anaerobic pyrolysis treatment of the ink slag, the ink slag to be treated is pretreated through an ink slag pretreatment system to obtain pretreated ink slag; performing pyrolysis treatment on the pretreated printing ink slag by adopting a preset low-pressure high-temperature superheated steam in a countercurrent direct contact mode through an anaerobic pyrolysis system; generating low-pressure saturated steam by a steam generation system, and obtaining low-pressure high-temperature superheated steam for the anaerobic pyrolysis system after the low-pressure saturated steam is superheated by high-temperature flue gas; treating the high-temperature flue gas from the steam generation system through a flue gas treatment system; and discharging the flue gas treated by the flue gas treatment system through a flue gas discharge system. The device can realize the self-sustaining operation of the device without external energy after running stably, the ink residues which are originally classified as hazardous wastes after being treated by the process device can realize good harmlessness, reduction and resource utilization, and the device has the comprehensive advantages of low treatment cost, high treatment degree and less comprehensive energy consumption of the device.
Specifically, compared with the existing ink residue treatment technology, the method can achieve the following beneficial effects: toxic factors such as organic matters in the ink residues are removed through high-temperature pyrolysis by utilizing the high-temperature pyrolyzability of the ink residues; compared with the traditional high-temperature flue gas pyrolysis mode, the mode of direct contact of high-temperature superheated steam is adopted for pyrolysis, on one hand, the higher enthalpy change of the high-temperature superheated steam can be utilized to realize the relatively fast pyrolysis of the ink slag, the pyrolysis reaction time is reduced, and on the other hand, the anaerobic operation of the direct contact pyrolysis process can be ensured; furthermore, a built-in high-temperature resistant screw is used for pushing and raising materials, so that sufficient pyrolysis of the materials is guaranteed, the retention time is shortened, and the equipment investment cost is reduced; the mode of direct contact pyrolysis under micro negative pressure and relatively low temperature is adopted, on one hand, the complete pyrolysis of the ink residues can be ensured at relatively low temperature, and the secondary pollution caused by the leakage of harmful gas can be prevented, on the other hand, the manufacturing cost of equipment can be reduced, and the total investment cost of the device can be reduced; by adopting the mode of directly burning the pyrolysis gas, on one hand, the series of problems caused by the follow-up treatment of the tar generated by low-temperature pyrolysis are thoroughly solved, and on the other hand, the combustion heat of the pyrolysis gas and the tar can be fully utilized to generate steam, so that the self-sustaining operation of the device can be realized; through multi-stage deacidification, dust removal and flue gas reheating treatment, the standard emission of the flue gas can be ensured, and the problems of white flue gas and the like during emission are avoided; the invention can completely remove toxic and harmful organic substances, thereby reducing, harmlessly and resourcefully treating resources; the invention makes full use of the fuel resource generated by the device system, thereby not only eliminating the possibility of secondary pollution, but also effectively reducing the operation cost of enterprises, and having good environmental benefit, social benefit and economic benefit.
Drawings
In order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the drawings used in the description of the embodiments or the prior art will be briefly described below, it is obvious that the drawings in the following description are only some embodiments of the present invention, and for those skilled in the art, other drawings can be obtained according to the structures shown in the drawings without creative efforts.
FIG. 1 is a schematic structural diagram of a schematic diagram of an embodiment of an anaerobic pyrolysis treatment device for ink slag.
The reference numbers illustrate:
| reference numerals | Name (R) | Reference numerals | Name (R) |
| 1 | Crushing |
2 | Screw conveyer |
| 3 | Drying machine | 4 | |
| 5 | |
6 | Preheater |
| 7 | Pyrolysis reactor | 8 | Cyclone separator |
| 9 | |
10 | Superheater |
| 11 | |
12 | |
| 13 | Semi-dry |
14 | Bag type dust collector |
| 15 | Venturi |
16 | Washing tower |
| 17 | |
18 | Chimney |
The implementation, functional features and advantages of the objects of the present invention will be further explained with reference to the accompanying drawings.
Detailed Description
The technical solutions in the embodiments of the present invention will be clearly and completely described below with reference to the drawings in the embodiments of the present invention, and it is obvious that the described embodiments are only a part of the embodiments of the present invention, and not all of the embodiments. All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the protection scope of the present invention.
It should be noted that, if directional indications (such as up, down, left, right, front, and back … …) are involved in the embodiment of the present invention, the directional indications are only used to explain the relative positional relationship between the components, the movement situation, and the like in a specific posture (as shown in the drawing), and if the specific posture is changed, the directional indications are changed accordingly.
In addition, if there is a description of "first", "second", etc. in an embodiment of the present invention, the description of "first", "second", etc. is for descriptive purposes only and is not to be construed as indicating or implying relative importance or implicitly indicating the number of technical features indicated. Thus, a feature defined as "first" or "second" may explicitly or implicitly include at least one such feature. In addition, technical solutions between various embodiments may be combined with each other, but must be realized by a person skilled in the art, and when the technical solutions are contradictory or cannot be realized, such a combination should not be considered to exist, and is not within the protection scope of the present invention.
The embodiment of the invention considers that the existing ink slag treatment method can not realize effective treatment of the ink slag, or has high cost, no better practicability and operability and great influence on comprehensive energy consumption and cracking efficiency.
For example, the prior art discloses a vacuum thermal cracking harmless treatment technology of waste oil ink residue of printed circuit boards, which comprises a drying module, a pyrolysis module and a separation module. The invention can realize the anaerobic pyrolysis of the waste oil ink residue, but a large amount of non-condensable gas can be generated after the pyrolysis, higher energy is consumed if the system is required to keep vacuum, and the danger is easily caused if air leaks into the system under high vacuum, and the generated tar belongs to dangerous chemicals, so that a series of problems can be still caused by the subsequent treatment. The invention adopts an intermittent mode to carry out anaerobic thermal cracking, so that the whole device system obviously has no better practicability and operability in industrialization.
Also, as the prior art discloses a device for carbonizing and cracking by utilizing normal-pressure superheated steam, which comprises a carbonization reactor, a steam generator, a heat exchanger, a reheated steam electromagnetic coil, a catalytic cracking device, a spray purifier, an activated carbon absorber and the like. The invention can effectively pyrolyze biomass and effectively utilize energy generated by combustion of pyrolysis gas, but has the defects of unsmooth discharge of a carbonization reactor, low efficiency of a catalytic cracking device, easy poisoning of a catalyst and the like.
As the prior art, a cracking device and a cracking method for solid organic waste are also disclosed, and the main equipment of the cracking device is a cracking furnace. After the solid organic waste is introduced into the cracking furnace, the rotating shaft is used for driving the shoveling plate to rotate, so that the materials are pushed, stirred and crushed, and then the pyrolysis reaction is carried out in a jacket indirect heating mode. The invention can realize the cracking reaction of the solid organic waste, and can discharge the cracked oil gas in time by arranging a plurality of cracked oil gas outlets along the axial direction of the shell, thereby realizing the improvement of the yield and the quality of the tar. However, although the device improves the yield and quality of the oil tar, a large amount of heat can be taken away by high-temperature oil gas discharged in a segmented mode, and meanwhile, the defects of low heat transfer efficiency, insufficient treatment capacity and the like are caused by the adoption of an indirect heating mode, so that the comprehensive energy consumption and the cracking efficiency are inevitably influenced greatly.
Referring to fig. 1, the embodiment of the invention provides an anaerobic pyrolysis treatment device for ink slag, which can effectively treat the ink slag and has the comprehensive advantages of low treatment cost, high treatment degree, low comprehensive energy consumption of the device and the like.
The anaerobic pyrolysis treatment device for the ink slag can comprise: printing ink sediment pretreatment systems, anaerobic pyrolysis system, steam generation system, flue gas processing system and flue gas discharge system, wherein:
the ink residue pretreatment system is used for pretreating ink residues to be treated to obtain pretreated ink residues;
the anaerobic pyrolysis system is used for carrying out pyrolysis treatment on the pretreated printing ink slag in a mode of direct countercurrent contact by adopting preset low-pressure high-temperature superheated steam;
the steam generation system is used for generating low-pressure saturated steam, obtaining low-pressure high-temperature superheated steam after the low-pressure saturated steam is superheated by high-temperature flue gas and supplying the low-pressure high-temperature superheated steam to the anaerobic pyrolysis system;
the flue gas treatment system is used for treating the high-temperature flue gas from the steam generation system;
and the flue gas emission system is used for emitting the flue gas treated by the flue gas treatment system.
Compared with the prior art, the anaerobic pyrolysis treatment device for the ink residues utilizes the high-temperature pyrolyzability of the ink residues to remove toxic factors such as organic matters in the ink residues through high-temperature pyrolysis; in traditional high temperature flue gas pyrolysis mode, the mode that adopts high temperature superheated steam direct contact carries out the pyrolysis, thereby can utilize the higher enthalpy change of high temperature superheated steam to be favorable to the pyrolysis of printing ink sediment mutually on the one hand, on the other hand can guarantee the anaerobic operation of direct contact pyrolysis process again, what after this device was handled originally is categorized into danger waste printing ink sediment and can realize good innoxiousness, minimizing and resource utilization, and have the treatment cost low, the treatment degree is high, the comprehensive advantage that the device comprehensive energy consumption is few, and this device does not need the self-sustaining operation that the external energy can realize the device after the steady operation.
Specifically, the ink residue pretreatment system includes: printing ink sediment breaker 1, screw conveyer 2, drying-machine 3, belt weigher 4 that connect gradually, wherein:
the exit linkage of printing ink sediment breaker 1 to screw conveyer 2's feed inlet, screw conveyer 2's discharge gate with drying-machine 3's material import is connected, drying-machine 3's material export with belt weigher 4's entry is connected, belt weigher 4's export with anaerobic pyrolysis system is connected.
And a steam inlet and a waste steam outlet of the dryer 3 are respectively connected with the steam generation system, and the waste steam outlet of the dryer 3 is connected with one inlet of the direct combustion chamber 9 of the steam generation system.
The anaerobic pyrolysis system comprises: the device comprises a spiral feeder 5, a preheater 6, a pyrolysis reactor 7 and a cyclone separator 8 which are connected in sequence; wherein:
an inlet of the spiral feeder 5 is connected with an outlet of the belt scale 4, an outlet of the spiral feeder 5 is communicated with a material inlet of the preheater 6, a material outlet of the preheater 6 is communicated with a material inlet of the pyrolysis reactor 7, a gas phase outlet of the preheater 6 is connected with an inlet of the cyclone separator 8, and a gas phase outlet of the cyclone separator 8 is connected with the steam generation system; the gas phase inlet of the pyrolysis reactor 7 is communicated with the steam generation system.
The connection duct of the material outlet of the preheater 6 to the material inlet of the pyrolysis reactor 7 also serves as a connection duct of the gas phase outlet of the pyrolysis reactor 7 to the gas phase inlet of the preheater 6.
Furthermore, a through type high temperature resistant stainless steel continuous screw is arranged in the centers of the preheater 6 and the pyrolysis reactor 7; the spiral part is controlled by a variable frequency motor, so that the rotating speed and the material retention time can be adjusted according to the feeding property, and the energy consumption is saved under the condition that the material is completely pyrolyzed; simultaneously, through the rotatory propelling movement and the material of raising of spiral piece, thereby guarantee on the one hand to treat that the pyrolysis material can move forward in order and prevent that the material from gathering in the device, and then take place the melting of ash content and the coking on the wall, thereby on the other hand makes the material can fully contact with high temperature superheated steam and shortens the pyrolysis time, reduces equipment volume, reduces equipment investment cost.
Further, the steam generation system includes: the direct combustion chamber 9, the superheater 10, the steam boiler 11, also include fuel feed system, combustion air and combustion air system, boiler water preparation system, wherein:
a gas phase inlet of the direct combustion chamber 9 is connected with a gas phase outlet of the cyclone separator 8, and a dead steam outlet of the dryer 3 is connected with another gas phase inlet of the direct combustion chamber 9; the flue gas outlet of the direct combustion chamber 9 is connected with the flue gas inlet of the superheater 10, and the flue gas outlet of the superheater 10 is connected with the flue gas inlet of the steam boiler 11; the flue gas outlet of the steam boiler 11 is connected with the flue gas treatment system; the combustion system to which the direct combustion chamber 9 belongs comprises a fuel feeding system, combustion air and a combustion air system; in particular, the fuel feeding system, the combustion air and combustion air system outlets are connected with the burner inlet of the direct combustion chamber 9, and the boiler water inlet of the steam boiler 11 is connected with the boiler water preparation system; one path of a steam outlet of the steam boiler 11 is connected with a steam inlet of the superheater 10, and the other path of the steam outlet is communicated with a steam inlet of the dryer 3; the steam outlet of the superheater 10 is connected to the gas phase inlet of the pyrolysis reactor 7.
Furthermore, steam is generated through high-temperature combustion of the direct combustion chamber 9 and is used for supplying a heat source to the whole device, so that combustion heat of pyrolysis gas and pyrolysis tar can be fully utilized, and stable self-sustaining operation of the device can be guaranteed.
The flue gas treatment system comprises: flue gas reheater 12, half dry deacidification tower 13, bag collector 14, venturi cooler 15 and scrubbing tower 16 that connect gradually, wherein:
a flue gas inlet at one side of the flue gas reheater 12 is connected with a flue gas outlet of the steam boiler 11, a flue gas outlet at one side of the flue gas reheater 12 is connected with a flue gas inlet of the semi-dry type deacidification tower 13, and a flue gas outlet of the semi-dry type deacidification tower 13 is connected with a flue gas inlet of the bag type dust collector 14; a flue gas outlet of the bag type dust collector 14 is connected with a flue gas inlet of the venturi cooler 15, and a bottom outlet of the venturi cooler 15 is connected with a lower inlet of the washing tower 16; and a top flue gas outlet of the washing tower 16 is connected with a flue gas inlet at the other side of the flue gas reheater 12, and a flue gas outlet at the other side of the flue gas reheater 12 is connected with the flue gas discharge system.
Further, through multistage deacidification, dust removal and flue gas reheating, the finally discharged flue gas can be ensured to be discharged up to the standard, and the problems of whitening and the like existing in the flue gas discharge process are avoided.
The flue gas discharge system comprises: a flue gas induced draft fan 17 and a chimney 18; the inlet of the flue gas induced draft fan 17 is connected with the flue gas outlet at the other side of the flue gas reheater 12, and the outlet of the flue gas induced draft fan 17 is connected with the inlet of the chimney 18.
Further, the dryer 3 adopts an indirect heating mode to dry; the rotating speed of a built-in screw part of the pyrolysis reactor 7 is 5-50 rpm, the material filling coefficient is 0.1-0.45, and the reaction retention time is less than or equal to 30 min; and/or the presence of a gas in the gas,
the temperature of a dead steam outlet of the dryer 3 is controlled to be 90-100 ℃; the temperature of a high-temperature superheated steam inlet of the pyrolysis reactor 7 is controlled to be between 400 and 800 ℃, and the temperature of a pyrolysis gas outlet of the preheater 6 is controlled to be between 200 and 400 ℃; and/or the presence of a gas in the gas,
the operation pressure of the preheater 6 and the pyrolysis reactor 7 is micro-negative pressure operation, and the outlet temperature of the waste residue of the pyrolysis reactor 7 is 400-600 ℃; and/or the presence of a gas in the gas,
the operation temperature of the direct combustion chamber 9 is 850-1200 ℃, and the temperature of the flue gas outlet of the steam boiler 11 is 300-500 ℃.
The principle of the anaerobic pyrolysis treatment device for the ink residue of the embodiment of the invention is explained in detail as follows:
the embodiment of the invention provides an anaerobic pyrolysis treatment device for ink residues, which can effectively treat the ink residues generated in PCB production.
The raw materials input to the treatment of the embodiment of the invention are ink residues generated in the PCB industry: raw oil ink residue enters a crusher 1, is crushed and then is conveyed into a dryer 3 by a screw conveyor 2, and then is dried by low-pressure saturated steam from a steam generation system in an indirect heating mode, so that the amount of materials to be treated is reduced, and the volume of a pyrolysis reactor 7 is reduced.
The dried materials are fed into an ink slag pyrolysis system for pyrolysis after being measured by a belt weigher 4, exhaust steam dried by a dryer 3 enters a direct combustion chamber 9 for combustion to remove harmful substances, so that the exhaust steam is convenient to discharge up to the standard, and steam condensate water condensed by the dryer 3 can be returned to a boiler water supply position for recycling.
The dried ink residues from the ink residue pretreatment system are firstly sent to the preheater 6 by the spiral feeder 5, further dehydrated and preheated under the action of the built-in spiral, and then are subjected to countercurrent high-temperature direct contact pyrolysis with high-temperature superheated steam from the steam generation system in the pyrolysis reactor 7, and the waste residues obtained after pyrolysis are discharged out of the pyrolysis reactor 7 after being blended.
Pyrolysis gas obtained after pyrolysis enters a preheater 6, most of dust is removed through a cyclone dust collector after the pyrolysis gas is in direct contact with a preheated feeding raw material in a countercurrent manner, so that the phenomenon that the service life of equipment is influenced due to the fact that excessive ash is molten and coked on the wall of the direct combustion chamber 9 during high-temperature combustion is avoided.
The dedusted pyrolysis gas from the cyclone separator 8 directly enters the direct combustion chamber 9 for combustion, and the combusted high-temperature hot flue gas firstly heats one path of saturated steam from the steam boiler 11 to generate high-temperature superheated steam and then enters the steam boiler 11 to generate low-pressure saturated steam; one path of the generated saturated steam enters the superheater 10 to generate high-temperature superheated steam, and the other path of the generated saturated steam enters the dryer 3 to provide drying heat.
The hot flue gas from the steam boiler 11 heats the low-temperature flue gas from the washing tower 16, then enters the semi-dry deacidification tower 13 for cooling and deacidification treatment, and then enters the bag type dust collector 14 for dust removal; the hot flue gas after dust removal is firstly cooled by a venturi cooler 15 in a spray water mode, and then is finally deacidified and dedusted by a washing tower 16 in an alkali washing mode, and washing water discharged from the bottom of the washing tower 16 is recycled and then is discharged for treatment; the washed and purified low-temperature flue gas is reheated by hot flue gas from the steam boiler 11 and then is guided to a chimney 18 by a flue gas induced draft fan 17 for high-altitude emission.
Compared with the prior art, the anaerobic pyrolysis treatment device for the ink slag has the advantages of good treatment effect, low energy consumption, no secondary pollution, high comprehensive efficiency and the like.
Referring to fig. 1, the present invention includes the following: the system comprises an ink slag pretreatment system, an ink slag anaerobic pyrolysis system, a steam generation system, a flue gas treatment system and a flue gas discharge system.
The printing ink sediment pretreatment systems includes: the printing ink sediment breaker 1, screw conveyer 2, drying-machine 3 and belt weigher 4 that connect gradually. Wherein, the outlet of the crusher 1 is connected with the material inlet of the screw conveyor 2, and the outlet of the screw conveyor 2 is directly connected with the material inlet of the dryer 3; the material outlet of the dryer 3 is communicated with the inlet of the belt weigher, the steam inlet of the dryer is connected with the saturated steam pipeline of the steam generation system, and the exhaust steam outlet of the dryer is directly connected with one of the gas phase inlets of the direct combustion chamber 9.
Printing ink sediment anaerobic pyrolysis system includes: the device comprises a spiral feeder 5, a preheater 6 and a pyrolysis reactor 7 which are connected in sequence, and further comprises a cyclone separator 8. Wherein, the material inlet of the spiral feeder 5 is connected with the outlet of the belt weigher 4, the material outlet thereof is connected with the material inlet of the preheater 6, and the gas phase outlet thereof is communicated with the inlet of the cyclone separator 8; a material inlet of the pyrolysis reactor 7 is connected with a material outlet of the preheater 6, and a high-temperature superheated steam inlet of the pyrolysis reactor is communicated with a high-temperature superheated steam pipeline of the steam generation system; the gas phase outlet of the cyclone separator 8 is connected with one of the gas phase inlets of the direct combustion chamber 9 of the steam generation system, and the generated fly ash is collected and then concentrated; in particular, the blanking pipe connecting the material outlet of the preheater 6 with the material inlet of the pyrolysis reactor 7 also serves as a connecting pipe for the gas phase outlet of the pyrolysis reactor 7 with the gas phase inlet of the preheater 6.
The steam generation system includes: a direct combustion chamber 9, a superheater 10 and a steam boiler 11, and further comprises a fuel feeding system, a combustion air and combustion air system and a boiler water preparation system. Wherein, the gas phase inlet of the direct combustion chamber 9 is respectively connected with the exhaust steam outlet of the dryer 3 and the gas phase outlet of the cyclone separator 8, the flue gas outlet thereof is connected with the flue gas inlet of the superheater 10, the burner thereof is connected with the fuel feeding system, the combustion air and the combustion air system, and the generated fly ash is collected and then treated in a centralized way; a flue gas inlet of the superheater 10 is connected with a flue gas outlet of the direct combustion chamber 9, a flue gas outlet of the superheater is connected with a flue gas inlet 11 of the steam boiler, a steam inlet of the superheater is connected with one path of saturated steam from the steam boiler, and a high-temperature superheated steam outlet of the superheater is connected with a high-temperature superheated steam inlet of the pyrolysis reactor 7; the smoke outlet of the steam boiler 11 is connected with the inlet pipeline of the smoke processing system, the water pipeline inlet of the boiler is connected with the pipeline outlet of the boiler water preparation system, the steam outlet of the steam boiler is divided into two paths and is respectively connected with the steam inlet of the dryer 3 and the steam inlet of the superheater 10, and the generated fly ash is collected and then treated in a centralized manner.
The flue gas treatment system comprises: a flue gas reheater 12, a semi-dry deacidification tower 13 and a belt type dust remover 14 which are connected in sequence; a venturi desuperheater 15 and a scrubber 16 are also included. Wherein, a flue gas inlet at one side of the flue gas reheater 12 is connected with a flue gas outlet pipeline of the steam boiler 11, a flue gas outlet pipeline at one side thereof is connected with a flue gas inlet pipeline of the semi-dry deacidification tower 13, a flue gas inlet pipeline at the other side thereof is communicated with a gas phase outlet at the top of the washing tower, and a flue gas outlet pipeline at the other side thereof is communicated with a flue gas discharge system; the flue gas outlet of the semi-dry deacidification tower 13 is connected with the flue gas inlet of the bag type dust collector 14, the inlet of the deacidification cooling pipeline is externally connected with a lime water feeding pipeline, and the generated fly ash is collected and then is treated in a centralized way; a flue gas inlet of the bag type dust collector 14 is connected with a flue gas outlet of the semi-dry type deacidification tower 13, a flue gas outlet of the bag type dust collector is connected with a flue gas inlet of the Venturi cooler 15, and generated fly ash is collected and then is treated in a centralized manner; the flue gas inlet of the Venturi cooler 15 is connected with the flue gas outlet of the bag type dust collector 14, the inlet of a liquid phase spraying pipeline of the Venturi cooler is communicated with a spraying water pipeline, and the discharge hole at the bottom of the Venturi cooler is communicated with the material inlet at the lower part of the washing tower 16; a flue gas outlet at the top of the washing tower 16 is connected with a flue gas inlet at the other side of the flue gas reheater 12, a liquid phase inlet pipeline at the upper part of the washing tower is communicated with an alkaline water system pipeline, and waste water at the bottom of the washing tower is discharged after being recycled; in particular, the liquid-phase spray water of the venturi cooler 15 can also be used as the waste water from the bottom of the washing tower 16.
The flue gas discharge system comprises: a flue gas induced draft fan 17 and a chimney 18. Wherein, a flue gas pipeline from a flue gas outlet at the other side of the flue gas reheater 12 is connected with a chimney 18 through a flue gas induced draft fan 17.
Specifically, after ink residues with the water content of 50% -80% from the outside are crushed by a crusher 1, the ink residues are conveyed to a dryer 3 by a screw conveyor 2, low-pressure saturated steam with the temperature of about 120 ℃ from a steam generation system is subjected to indirect contact drying at the temperature of-100 ℃, dried exhaust steam directly enters a direct combustion chamber 9 to be incinerated to remove harmful components, and steam condensate water from the dryer 3 can be returned to a boiler water preparation system for reuse; the dried ink residue with the water content lower than 20 percent is fed into an anaerobic pyrolysis system after being measured by a belt scale 4.
The method comprises the following steps that ink slag from an ink slag pretreatment system is fed into a preheater 6 through a spiral feeder 5, pyrolysis gas from a pyrolysis reactor 7 is directly contacted and preheated at the temperature of 200-400 ℃, then enters the pyrolysis reactor 7 for anaerobic direct contact pyrolysis at the rotating speed of 5-50 rpm at the temperature of 400-600 ℃, and pyrolysis energy is provided by high-temperature superheated steam at the temperature of 400-800 ℃ from a steam generation system; pyrolysis gas is preheated by a preheater 6 and then enters a cyclone separator 8 for dust removal, and then enters a steam generation system for treatment, and waste residue after pyrolysis is discharged after temperature reduction and collected and treated in a unified way.
Pyrolysis gas from the oxygen-free pyrolysis system of the ink slag enters the direct combustion chamber 9 and is combusted together with exhaust steam from the dryer 3, combustion air and combustion-supporting air are required to be continuously supplemented during combustion to ensure complete combustion of the pyrolysis gas, additional fuel is not required to be supplemented during normal operation of the direct combustion chamber 9, and the additional fuel is only used for supplementing the insufficient energy part of the system during driving/parking; high-temperature flue gas at 850-1200 ℃ from the direct combustion chamber 9 enters a superheater 10, and one path of saturated steam from a steam boiler 11 is superheated to 400-800 ℃ and then enters the steam boiler 11 to generate low-pressure saturated steam; one path of low-pressure saturated steam generated by a steam boiler 11 enters a superheater 11, is heated and then enters a pyrolysis reactor 7, and the other path of the low-pressure saturated steam enters a dryer 3; the boiler water required by the steam boiler 11 is provided by a boiler water preparation system.
300-500 flue gas from a steam generation system enters a flue gas reheater 12, the flue gas from a washing tower 16 is preheated, then enters a semi-dry deacidification tower 13, deacidified by lime water atomization and cooled to below 200 ℃; the flue gas after deacidification and temperature reduction is subjected to particulate matter removal by a bag type dust collector 14, then is cooled to below 60 ℃ by a venturi cooler 15 through spray water, and then enters a washing tower 16 to be washed by alkaline water; the washed flue gas enters a flue gas reheater 12, the temperature is raised to 130-150 ℃, and then the flue gas is guided to a chimney 18 by a flue gas induced draft fan 17 to be discharged at high altitude.
Particularly, the fly ash generated by the device is collected and then is treated uniformly, and the generated waste water is discharged for treatment after being recycled.
Compared with the prior art, the embodiment of the invention has the following technical effects:
(1) toxic factors such as organic matters in the ink residues are removed through high-temperature pyrolysis by utilizing the high-temperature pyrolyzability of the ink residues; (2) compared with the traditional high-temperature flue gas pyrolysis mode, the mode of direct contact of high-temperature superheated steam is adopted for pyrolysis, on one hand, the higher enthalpy change of the high-temperature superheated steam can be utilized to facilitate the rapid pyrolysis of the ink slag, the pyrolysis reaction time is reduced, and on the other hand, the anaerobic operation of the direct contact pyrolysis process can be ensured; (3) the material pushing and lifting are carried out by adopting the built-in high-temperature resistant spiral, so that the sufficient pyrolysis of the material is ensured, the retention time is shortened, and the equipment investment cost is reduced; (4) the mode of direct contact pyrolysis under micro negative pressure and relatively low temperature is adopted, on one hand, the complete pyrolysis of the ink residues can be ensured at relatively low temperature, and the secondary pollution caused by the leakage of harmful gas can be prevented, on the other hand, the manufacturing cost of equipment can be reduced, and the total investment cost of the device can be reduced; (5) by adopting the mode of directly burning the pyrolysis gas, on one hand, the series of problems caused by the follow-up treatment of the tar generated by low-temperature pyrolysis are thoroughly solved, and on the other hand, the combustion heat of the pyrolysis gas and the tar can be fully utilized to generate steam, so that the self-sustaining operation of the device can be realized; (6) through multi-stage deacidification, dust removal and flue gas reheating treatment, the standard emission of the flue gas can be ensured, and the problems of white flue gas and the like during emission are avoided; (7) the invention can completely remove toxic and harmful organic substances, thereby reducing, harmlessly and resourcefully treating resources; (8) the invention makes full use of the fuel resource generated by the device system, thereby not only eliminating the possibility of secondary pollution, but also effectively reducing the operation cost of enterprises, and having good environmental benefit, social benefit and economic benefit.
In addition, the invention also provides an anaerobic pyrolysis treatment method for the ink slag, which comprises the following steps:
step S1, preprocessing the ink slag to be processed through an ink slag preprocessing system to obtain preprocessed ink slag;
step S2, performing pyrolysis treatment on the pretreated ink slag by adopting preset low-pressure high-temperature superheated steam in a countercurrent direct contact mode through an anaerobic pyrolysis system;
step S3, generating low-pressure saturated steam through a steam generation system, and obtaining low-pressure high-temperature superheated steam to be supplied to the anaerobic pyrolysis system after the low-pressure saturated steam is superheated by high-temperature flue gas;
step S4, processing the high-temperature flue gas from the steam generation system through a flue gas processing system;
and step S5, discharging the flue gas treated by the flue gas treatment system through a flue gas discharge system.
The principle of the anaerobic pyrolysis treatment of the ink slag is realized in the embodiment of the invention, please refer to the above embodiment, and details are not repeated herein.
The above description is only a preferred embodiment of the present invention, and is not intended to limit the scope of the present invention, and all modifications and equivalents of the present invention, which are made by the contents of the present specification and the accompanying drawings, or directly/indirectly applied to other related technical fields, are included in the scope of the present invention.
Claims (10)
1. An ink sediment anaerobic pyrolysis processing device, its characterized in that, the device includes: printing ink sediment pretreatment systems, anaerobic pyrolysis system, steam generation system, flue gas processing system and flue gas discharge system, wherein:
the ink residue pretreatment system is used for pretreating ink residues to be treated to obtain pretreated ink residues;
the anaerobic pyrolysis system is used for carrying out pyrolysis treatment on the pretreated printing ink slag in a mode of direct countercurrent contact by adopting preset low-pressure high-temperature superheated steam;
the steam generation system is used for generating low-pressure saturated steam, obtaining low-pressure high-temperature superheated steam after the low-pressure saturated steam is superheated by high-temperature flue gas and supplying the low-pressure high-temperature superheated steam to the anaerobic pyrolysis system;
the flue gas treatment system is used for treating the high-temperature flue gas from the steam generation system;
and the flue gas emission system is used for emitting the flue gas treated by the flue gas treatment system.
2. The ink slag anaerobic pyrolysis treatment device of claim 1, wherein the ink slag pretreatment system comprises: printing ink sediment breaker, screw conveyer, drying-machine, belt weigher that connect gradually, wherein:
the exit linkage of printing ink sediment breaker to screw conveyer's feed inlet, screw conveyer's discharge gate with the material import of drying-machine is connected, the material export of drying-machine with the entry of belt weigher is connected, the export of belt weigher with anaerobic pyrolysis system is connected.
3. The apparatus of claim 2, wherein the steam inlet and the exhaust steam outlet of the dryer are respectively connected to the steam generation system.
4. The ink slag anaerobic pyrolysis treatment device of claim 3, wherein the anaerobic pyrolysis system comprises: the spiral feeder, the preheater, the pyrolysis reactor and the cyclone separator are connected in sequence; wherein:
the inlet of the spiral feeder is connected with the outlet of the belt weigher, the outlet of the spiral feeder is communicated with the material inlet of the preheater, the material outlet of the preheater is communicated with the material inlet of the pyrolysis reactor, the gas phase outlet of the preheater is connected with the inlet of the cyclone separator, and the gas phase outlet of the cyclone separator is connected with the steam generation system; and the gas-phase inlet of the pyrolysis reactor is communicated with the steam generation system.
5. The apparatus for anaerobic pyrolysis treatment of ink slag according to claim 4, wherein a screw is arranged in the center of the preheater and the pyrolysis reactor; the connection pipe of the material outlet of the preheater and the material inlet of the pyrolysis reactor serves as a gas phase outlet pipe of the pyrolysis reactor.
6. The ink slag anaerobic pyrolysis treatment device of claim 5, wherein the steam generation system comprises: direct combustion chamber, over heater, steam boiler, wherein:
a gas phase inlet of the direct combustion chamber is connected with a gas phase outlet of the cyclone separator, and a dead steam outlet of the dryer is connected with the other gas phase inlet of the direct combustion chamber; the flue gas outlet of the direct combustion chamber is connected with the flue gas inlet of the superheater, and the flue gas outlet of the superheater is connected with the flue gas inlet of the steam boiler; the smoke outlet of the steam boiler is connected with the smoke treatment system; the combustion system to which the direct combustion chamber belongs comprises a fuel feeding system, combustion air and a combustion air system; a boiler water inlet of the steam boiler is connected with a boiler water preparation system; one path of a steam outlet of the steam boiler is connected with a steam inlet of the superheater, and the other path of the steam outlet of the steam boiler is communicated with a steam inlet of the dryer; and a steam outlet of the superheater is connected with a gas-phase inlet of the pyrolysis reactor.
7. The ink slag anaerobic pyrolysis treatment device of claim 6, wherein the flue gas treatment system comprises: flue gas reheater, half-dry deacidification tower, bag collector, venturi cooler and scrubbing tower that connect gradually, wherein:
a flue gas inlet at one side of the flue gas reheater is connected with a flue gas outlet of the steam boiler, a flue gas outlet at one side of the flue gas reheater is connected with a flue gas inlet of the semi-dry type deacidification tower, and a flue gas outlet of the semi-dry type deacidification tower is connected with a flue gas inlet of the bag type dust collector; the flue gas outlet of the bag type dust collector is connected with the flue gas inlet of the Venturi cooler, and the bottom outlet of the Venturi cooler is connected with the lower inlet of the washing tower; and a top flue gas outlet of the washing tower is connected with a flue gas inlet at the other side of the flue gas reheater, and a flue gas outlet at the other side of the flue gas reheater is connected with the flue gas discharge system.
8. The apparatus of claim 7, wherein the flue gas exhaust system comprises: a flue gas induced draft fan and a chimney; the inlet of the flue gas induced draft fan is connected with the flue gas outlet at the other side of the flue gas reheater, and the outlet of the flue gas induced draft fan is connected with the inlet of the chimney.
9. The anaerobic pyrolysis treatment device for the ink slag according to claim 8, wherein the dryer is used for drying by means of indirect heating; the rotating speed of a built-in screw part of the pyrolysis reactor is 5-50 rpm, the material filling coefficient is 0.1-0.45, and the reaction retention time is less than or equal to 30 min; and/or the presence of a gas in the gas,
the temperature of a dead steam outlet of the dryer is controlled to be 90-100 ℃; the temperature of a high-temperature superheated steam inlet of the pyrolysis reactor is controlled to be between 400 and 800 ℃, and the temperature of a pyrolysis gas outlet of the preheater is controlled to be between 200 and 400 ℃; and/or the presence of a gas in the gas,
the operation pressure of the preheater and the pyrolysis reactor is micro-negative pressure operation, and the outlet temperature of waste residue of the pyrolysis reactor is 400-600 ℃; and/or the presence of a gas in the gas,
the operation temperature of the direct combustion chamber is 850-1200 ℃, and the temperature of the smoke outlet of the steam boiler is 300-500 ℃.
10. An anaerobic pyrolysis treatment method for ink slag is characterized by comprising the following steps:
pretreating the ink slag to be treated by an ink slag pretreatment system to obtain pretreated ink slag;
performing pyrolysis treatment on the pretreated printing ink slag by adopting a preset low-pressure high-temperature superheated steam in a countercurrent direct contact mode through an anaerobic pyrolysis system;
generating low-pressure saturated steam by a steam generation system, and obtaining low-pressure high-temperature superheated steam for the anaerobic pyrolysis system after the low-pressure saturated steam is superheated by high-temperature flue gas;
treating the high-temperature flue gas from the steam generation system through a flue gas treatment system;
and discharging the flue gas treated by the flue gas treatment system through a flue gas discharge system.
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