CN110713182A - Method and system for co-processing coking wastewater sludge and tar residue - Google Patents
Method and system for co-processing coking wastewater sludge and tar residue Download PDFInfo
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- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 description 1
- QAOWNCQODCNURD-UHFFFAOYSA-L Sulfate Chemical compound [O-]S([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-L 0.000 description 1
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B32/00—Carbon; Compounds thereof
- C01B32/30—Active carbon
- C01B32/312—Preparation
- C01B32/318—Preparation characterised by the starting materials
- C01B32/324—Preparation characterised by the starting materials from waste materials, e.g. tyres or spent sulfite pulp liquor
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B32/00—Carbon; Compounds thereof
- C01B32/30—Active carbon
- C01B32/312—Preparation
- C01B32/342—Preparation characterised by non-gaseous activating agents
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B32/00—Carbon; Compounds thereof
- C01B32/30—Active carbon
- C01B32/39—Apparatus for the preparation thereof
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- Chemical & Material Sciences (AREA)
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- Inorganic Chemistry (AREA)
- Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Materials Engineering (AREA)
- Treatment Of Sludge (AREA)
Abstract
The invention relates to a method and a system for the co-treatment of coking wastewater sludge and tar residue, wherein the method comprises the following steps: the water content of the coking wastewater sludge and the water content of the tar residue are respectively reduced to 30 to 50 percent and 70 to 93 percent through a pretreatment method; the dewatered sludge and the dewatered tar residue are mixed and formed, and the formed mixture is used as a raw material to prepare the active carbon. The system comprises a waste mixing unit, a forming unit, a carbonization furnace and an activation reaction tower which are sequentially connected through a material transfer unit; the device also comprises a sludge pretreatment unit and a tar residue pretreatment unit which are respectively used for reducing the water content of the sludge and the tar residue, and the two pretreatment units are respectively connected with the material inlet of the waste material mixing unit through a screw conveyer. The dehydrated coking wastewater sludge and the tar residue are mixed to prepare the activated carbon, the dehydrated sludge can be used as a carbon-based framework structure of the tar residue, the porosity and the specific surface area of the activated carbon are increased, the synergistic treatment of the coking wastewater sludge and the tar residue is realized, and the coking wastewater sludge and the tar residue can be changed into valuable things.
Description
Technical Field
The invention belongs to the technical field of solid waste treatment, and particularly relates to a coking wastewater sludge and tar residue co-processing method and a coking wastewater sludge and tar residue co-processing system.
Background
In the process of preparing coal gas, coke, coal tar and the like by coking, a large amount of industrial solid waste is generated; wherein, in the coking production process, 0.1 percent of tar residues can be generated in the process unit, and about 0.2 percent of biochemical sludge can be generated in the coking wastewater treatment unit. Most enterprises fail to reasonably recover and utilize the sludge and tar residues produced in large quantities.
In the current resource utilization technology in the coking field, coking wastewater sludge is a complex rheological semi-dry solid waste because of complex components, contains inorganic substances, toxic and harmful substances (such as microorganisms and organic substances) and oil sludge, and is generally subjected to a physical and chemical method, and a plate frame is simply dehydrated under pressure and then placed on a coal piling site to be piled as a coal blending additive or sent to a solid waste landfill site for landfill; the tar residues are from three types, namely, the tar residues are from a mechanized tar ammonia water clarifying tank, and due to the large relative density, the coal tar residues are deposited at the bottom of the clarifying tank and are continuously discharged in a semisolid state through a scraper, so that the tar residues are the main source of the coal tar residues in a coking plant; secondly, in order to remove finer fine residues in the naturally settled tar, the tar is further separated by a super centrifuge, and the separated tar is semi-liquid coal tar residues with higher residue content; the rest is the clean coal tar residue after the natural sedimentation of the tar storage tank, the consistency is between that of the mechanical clean coal tar residue and that of the super centrifuge, and the tar residue from the three sources is directly mixed with the molded coal to be used as a coal blending adhesive or used as fuel for combustion.
The above-described processing method has the following problems:
(1) coking wastewater sludge contains a large amount of inorganic components (such as sulfate, aluminum-containing polymer and the like), and the coking wastewater sludge can obviously influence the quality of coke due to uneven mixing when being added into coking coal;
(2) the viscosity of the tar residue and the fluctuation of the components can cause the tar residue to be bonded on a belt conveyor and a belt carrier roller, so that the coal blending process of the coal material is not uniform, the blending is difficult to be accurate due to the fluctuation of the tar residue components, the coke quality is unstable, and the heat load of the coke oven is increased.
(3) Because a large amount of polycyclic aromatic hydrocarbons (such as polycyclic aromatic hydrocarbons and benzene) exist in the coking wastewater sludge and the tar residues, a large amount of toxic and harmful gases can be generated in the incomplete combustion of the coking wastewater sludge and the tar residues as fuels or coal blending additives, so that the standard-reaching emission of the atmosphere of a coking plant is caused, and the treatment difficulty and the treatment cost are increased.
At present, the two solid waste treatment modes cannot achieve environment-friendly, green and sustainable resource utilization, the pollution of final treatment cannot be effectively guaranteed, and the requirements of production and environmental protection cannot be met.
Disclosure of Invention
The invention relates to a method for co-processing coking wastewater sludge and tar residue and a system for co-processing coking wastewater sludge and tar residue, which can at least solve part of the defects in the prior art.
The invention relates to a method for co-processing coking wastewater sludge and tar residue, which comprises the following steps:
s1, pretreating coking wastewater sludge and tar residues to reduce the water content of the coking wastewater sludge to 30% -50% and the water content of the tar residues to 70% -93%;
s2, mixing and molding the dewatered sludge and the dewatered tar residues to obtain a molded mixture;
s3, taking the formed mixture as a raw material to prepare the activated carbon.
As one example, in S1, a method for pretreating a coking wastewater sludge includes:
s111, adding an acid-base regulator, an ionic flocculant, an inorganic salt pretreating agent and a demulsifier into the coking wastewater sludge, and carrying out pre-shrinking treatment on the coking wastewater sludge;
s112, adding a flocculating agent into the coking wastewater sludge subjected to the pre-shrinking treatment, and then feeding the coking wastewater sludge into a spiral stacking machine for moving annular spiral dewatering and filter pressing to reduce the water content of the sludge to 75-88%;
s113, contacting the coking wastewater sludge treated in the step S102 with hot air, and drying to reduce the water content of the coking wastewater sludge to 30-50% to obtain the dewatered sludge.
As one example, in S1, the method for pretreating tar residue includes:
s121, heating and stirring the tar residue, adjusting the fluidity of the tar residue to be in a homogeneous state, and adding a demulsifier into the tar residue in the stirring process;
s122, contacting the flowing tar residue with hot air, and drying to reduce the water content of the tar residue to 70% -93%, thereby obtaining the dehydrated tar residue.
As one example, in S3, the method for preparing activated carbon using the molding mixture as a raw material includes:
s301, feeding the formed mixture into a carbonization furnace for high-temperature carbonization to obtain an intermediate carbide, wherein the temperature in the carbonization furnace is controlled to be 600-850 ℃, and the residence time of the formed mixture in the carbonization furnace is controlled to be 4-7 hours;
s302, impregnating the intermediate carbide with an activating agent, and then performing activation treatment to obtain an activated substance;
s303, carrying out acid washing and water washing on the activated substance, and drying to obtain the activated carbon.
In one embodiment, in S302, the activation temperature is 650-700 ℃ and the activation time is 3h or less.
In one embodiment, in S2, the mixing ratio of the dewatered sludge to the dewatered tar residue is 1:3 to 1: 5.
The invention also relates to a system for the coprocessing of the coking wastewater sludge and the tar residue, which comprises a waste mixing unit, a forming unit, a carbonization furnace and an activation reaction tower which are sequentially connected through a material transfer unit;
the device is characterized by further comprising a sludge pretreatment unit for reducing the water content of the coking wastewater sludge and a tar residue pretreatment unit for reducing the water content of the tar residue, wherein a dehydrated sludge outlet of the sludge pretreatment unit and a dehydrated tar residue outlet of the tar residue pretreatment unit are respectively connected with a material inlet of the waste mixing unit through a screw conveyer.
As one of the embodiment, the sludge pretreatment unit includes pretreatment reactor, pile spiral shell machine and sludge drying machine, pretreatment reactor disposes acid-base regulator feed bin, ionic flocculant feed bin, inorganic salt pretreatment agent feed bin and first demulsifier feed bin, pile spiral shell machine's material entry pass through the thick liquid conveyer pipe with pretreatment reactor links up, pile spiral shell machine's sludge outlet pass through belt conveyor with sludge drying machine links up.
As one embodiment, the tar residue pretreatment unit comprises a conditioning demulsification reactor and a residue slurry drier, wherein the conditioning demulsification reactor is provided with a scraper stirring mechanism, a second demulsifier bin and a residue liquid heating mechanism for heating tar residue.
In one embodiment, the carbonization furnace is provided with a tail gas treatment pipeline, and a tail gas cooling mechanism and a tail gas catalytic reactor are sequentially arranged on the tail gas treatment pipeline.
The embodiment of the invention at least has the following beneficial effects:
according to the method and the system provided by the invention, the dehydrated coking wastewater sludge and the tar residue are mixed and molded to prepare the activated carbon, the dehydrated coking wastewater sludge can be used as a carbon-based framework structure of the tar residue, the looseness of the framework structure of the tar residue can be improved, the looseness and the specific surface area of the prepared activated carbon are increased, meanwhile, the cooperative treatment of the coking wastewater sludge and the tar residue is realized, the treatment problem of main solid wastes in the coking field is solved, the coking wastewater sludge and the tar residue can be changed into valuable, the prepared high-adsorbability activated carbon has wide application range and higher economic benefit, and the resource utilization and harmless treatment of the coking wastewater sludge and the tar residue are realized.
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 drawings without creative efforts.
FIG. 1 is a schematic structural diagram of a system for co-processing coking wastewater sludge and tar residue provided by an embodiment of the present invention.
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.
Example one
As shown in fig. 1, an embodiment of the present invention provides a method for co-processing coking wastewater sludge and tar residue, including:
s1, pretreating coking wastewater sludge and tar residues to reduce the water content of the coking wastewater sludge to 30% -50% and the water content of the tar residues to 70% -93%;
s2, mixing and molding the dewatered sludge and the dewatered tar residues to obtain a molded mixture;
s3, taking the formed mixture as a raw material to prepare the activated carbon.
In the method, the pretreatment of the coking wastewater sludge is mainly to dehydrate the sludge, and in one embodiment, the water content of the coking wastewater sludge is reduced to about 40%. Preferably, in S1, the method for pretreating the coking wastewater sludge includes:
s111, adding an acid-base regulator, an ionic flocculant, an inorganic salt pretreating agent and a demulsifier into the coking wastewater sludge, and carrying out pre-shrinking treatment on the coking wastewater sludge; wherein, addThe ionic flocculant is mainly PAC (Polyaluminium Chloride) and PAM (polyacrylamide) agent; the inorganic salt pretreating agent is preferably ZnCl2(ii) a The demulsifier preferably adopts a compound solution with persulfate as a main component; the acid-base regulator can adopt common acid-base regulating compounds. Inorganic salt pretreating agent ZnCl2And the adding amount of the demulsifier is adjusted according to the solid-liquid ratio of the actual solution and the components of the sludge, and the adding mass ratio ranges from 1% to 5%. The sludge is subjected to shrinking and fluffing pretreatment by the pH regulation, flocculation and oil pretreatment modes, so that a good pre-shrinking treatment effect is achieved.
S112, adding a flocculating agent into the coking wastewater sludge subjected to the pre-shrinking treatment, and then feeding the coking wastewater sludge into the spiral shell stacking machine 102 for moving annular spiral dehydration and filter pressing to reduce the water content of the sludge to 75-88%; the flocculating agent mainly adopts PAC and PAM, PAC agents can be added firstly, the adding amount is 20-40 mg/L, effective coagulation aiding is carried out, PAM agents are added, the adding amount is 40-80 mg/L, stable alum floc is formed, and subsequent dehydration and filter pressing are facilitated. In the embodiment, after dehydration and filter pressing by the screw stacking machine 102, the coking wastewater sludge can be filter-pressed to reach the water content of 83-85%. In one embodiment, the separated supernatant is returned to a wastewater treatment system in a coking plant through a supernatant collection tank below the screw stack 102, so that wastewater discharge is reduced. The waste water sludge is subjected to the floating annular layer type spiral dewatering and filter pressing in the screw stacking machine 102, the effects of waste water sludge precipitation and solid-liquid separation are obvious, the subsequent sludge drying is facilitated, and the condition that the sludge blocks the pipe orifice of the screw stacking machine 102 can be avoided.
S113, contacting the coking wastewater sludge treated in the step S102 with hot air, and drying to reduce the water content of the coking wastewater sludge to 30-50% to obtain the dewatered sludge. The drying treatment process can be carried out in a sludge dryer 103, preferably a low-temperature heat source dryer is adopted, so that the coking wastewater sludge is directly contacted with low-temperature air for heat exchange; the adopted hot air can be dry air with the temperature of 80-120 ℃ generated by an air heat pump, and further can be adjusted according to the drying capacity of the sludge and the residence time of the sludge in the equipment. As described above, the water content of the dewatered sludge is preferably about 40%.
In a further preferred embodiment, organic gases (containing a certain amount of benzene and polycyclic aromatic hydrocarbons) generated during the drying process of the coking wastewater sludge enter the tail gas catalytic reactor 701, a certain amount of activated carbon catalytic bed loaded with rare heavy metals (lanthanum, Ce, etc.) and an electrical heating unit capable of heating the activated carbon catalytic bed are filled in the tail gas catalytic reactor 701, the electrical heating unit may be, for example, an electric heating plate, and after the activated carbon catalytic bed is enriched with a certain amount of toxic gases, the temperature is raised to about 200 ℃ by the electrical heating unit, so that the toxic gases enriched on the catalytic bed are catalytically combusted and decomposed. The tail gas catalytic reactor 701 can remove organic gas by more than 98%, and the remaining 2% of undecomposed gas is adsorbed by the subsequent activated carbon adsorber 702, that is, the activated carbon adsorber 702 is connected behind the tail gas catalytic reactor 701.
In the method, the pretreatment of the tar residue is mainly used for dehydrating the tar residue, and in one embodiment, the water content of the tar residue is reduced to 82-85%. Preferably, in S1, the method for pretreating tar residue includes:
s121, heating and stirring the tar residue, adjusting the fluidity of the tar residue to a homogeneous state, ensuring the dispersibility of the dried tar residue, and adding a demulsifier into the tar residue in the stirring process; in one embodiment, this step is performed in the modified emulsion breaking reactor 201, and the tar residue can be heated by an electric heater or the like disposed in the modified emulsion breaking reactor 201, preferably by stirring the tar residue at a temperature of 75-90 ℃, so as to adjust the fluidity of the tar residue to a homogeneous state. The demulsifier is added in the stirring process, so that the emulsification state of the tar residue can be improved, and the oil-water separation is increased. The demulsifier can also adopt a compound solution taking persulfate as a main component. Further preferably, the quenching and tempering demulsification reactor 201 is a semi-closed device, a micro negative pressure state is maintained in the stirring process, the tail gas generated in the heating and stirring process can be treated by the tail gas catalytic reactor 701, for example, the tail gas and the organic gas generated in the coking wastewater sludge drying process can be introduced into the same tail gas catalytic reactor 701 together, so that the volatile organic compounds in the heating and stirring process can not be leaked into the ambient air.
S122, contacting the flowing tar residue with hot air, and drying to reduce the water content of the tar residue to 70% -93%, thereby obtaining the dehydrated tar residue. The drying process can be carried out in the slag slurry dryer 202, preferably a low-temperature heat source dryer is adopted, so that tar slag is directly contacted with low-temperature air for heat exchange; the adopted hot air can be dry air with the temperature of 80-120 ℃ generated by an air heat pump, and further can be adjusted according to the drying capacity of the tar residue and the retention time of the tar residue in the equipment. As described above, the water content of the dehydrated tar residue is preferably about 82 to 85%.
Continuing with the above method, S2, the mixing ratio of the dewatered sludge and the dewatered tar residue is controlled within the range of 1:3 to 1:5 in this embodiment, and can be designed and adjusted according to the actual water content of the dewatered sludge, the water content of the dewatered tar residue and other factors, and the ratio setting is mainly based on: the dewatered sludge in the mixture should play a role of a carbon-based framework of the tar residue and have certain looseness so as to increase the looseness and the specific surface area of the prepared activated carbon. For the molding treatment of the mixture, a conventional material molding process such as pelletizing, briquetting, etc. may be used, and in this embodiment, the mixture is fed into a curing machine for press molding.
Continuing with the above method, in S3, the method for preparing activated carbon using the molding mixture as a raw material comprises:
s301, feeding the formed mixture into a carbonization furnace 500 for high-temperature carbonization to obtain an intermediate carbonized material, wherein the temperature in the carbonization furnace 500 is controlled to be 600-850 ℃, and the retention time of the formed mixture in the carbonization furnace 500 is controlled to be 4-7 h;
s302, impregnating the intermediate carbide with an activating agent, and then performing activation treatment to obtain an activated substance; in one embodiment, the activator is 40% phosphoric acid solution, which is impregnated with the above intermediate carbide in a mass ratio of 0.8:4 for 1d, although a slight adjustment of the concentration of the phosphoric acid solution, a slight adjustment of the ratio of the phosphoric acid solution to the intermediate carbide, a fine adjustment of the impregnation time, etc. are possible, and are not exemplified here. The above activation treatment is preferably performed in the activation reaction tower 600, in one embodiment, the activation temperature is within a range of 650 to 700 ℃, and the activation time is within 3 hours, so that the situation that the pore walls of the microcrystalline carbon structure in the activated carbon are burned off to collapse the originally formed microporous structure due to too long activation time can be avoided.
S303, carrying out acid washing and water washing on the activated substance, and drying to obtain the activated carbon. Wherein, the acid washing and water washing of the activator can be conventional acid washing operation and water washing operation, which are omitted here.
According to the method provided by the embodiment, the dehydrated coking wastewater sludge and the tar residue are mixed and molded to prepare the activated carbon, the dehydrated coking wastewater sludge can be used as a carbon-based framework structure of the tar residue, so that the looseness of the framework structure of the tar residue can be improved, the looseness and the specific surface area of the prepared activated carbon are increased, meanwhile, the synergistic treatment of the coking wastewater sludge and the tar residue is realized, the treatment problem of main solid wastes in the coking field is solved, the coking wastewater sludge and the tar residue can be changed into valuable, the prepared high-adsorbability activated carbon is wide in application range, higher economic benefits are realized, and the resource utilization and harmless treatment of the coking wastewater sludge and the tar residue are realized.
Example two
Referring to fig. 1, an embodiment of the present invention provides a system for co-processing coking wastewater sludge and tar residue, including a waste mixing unit 300, a forming unit 400, a carbonization furnace 500, and an activation reaction tower 600, which are sequentially connected by a material transfer unit; the system further comprises a sludge pretreatment unit for reducing the water content of the coking wastewater sludge and a tar residue pretreatment unit for reducing the water content of the tar residue, wherein a dehydrated sludge outlet of the sludge pretreatment unit and a dehydrated tar residue outlet of the tar residue pretreatment unit are respectively connected with a material inlet of the waste mixing unit 300 through a screw conveyer.
As mentioned in the first embodiment, the sludge pretreatment unit is mainly used for reducing the sludge of coking wastewaterThe water content of (b) is preferably a water content of the coking wastewater sludge reduced to 30% to 50%, and more preferably a dehydrated sludge obtained by dehydrating the coking wastewater sludge to a water content of about 40%. In one embodiment, as shown in fig. 1, the sludge pretreatment unit comprises a pretreatment reactor 101, a screw stack 102 and a sludge drier 103. This preliminary treatment reactor 101 disposes acid-base regulator feed bin, ionic flocculant feed bin, inorganic salt pretreating agent feed bin and first demulsifier feed bin, fold the material entry of snail machine 102 pass through the thick liquid conveyer pipe with preliminary treatment reactor 101 links up, fold the mud export of snail machine 102 pass through belt conveyor with sludge drying machine 103 links up. Respectively adding an acid-base regulator, an ionic flocculant, an inorganic salt pretreating agent and a demulsifier into the coking wastewater sludge through an acid-base regulator bin, an ionic flocculant bin, an inorganic salt pretreating agent bin and a first demulsifier bin, and performing pre-shrinking treatment on the coking wastewater sludge; wherein the added ionic flocculant is mainly PAC (Polyaluminium Chloride) and PAM (polyacrylamide); the inorganic salt pretreating agent is preferably ZnCl2(ii) a The demulsifier preferably adopts a compound solution with persulfate as a main component; the acid-base regulator can adopt common acid-base regulating compounds. The sludge is subjected to shrinking and fluffing pretreatment by the pH regulation, flocculation and oil pretreatment modes, so that a good pre-shrinking treatment effect is achieved. Further preferably, the pretreatment reactor 101 is sequentially provided with a lower reaction zone, a stirrer and a dosing device from bottom to top, the acid-base modifier bin, the ionic flocculant bin, the inorganic salt pretreatment agent bin and the first demulsifier bin can be correspondingly arranged above the dosing device, and the bins can be located in the same dosing box, for example, separated by a partition plate; the pretreatment reactor 101 is preferably made of corrosion resistant alloy steel.
Further, a flocculation tank can be arranged on the inlet side of the spiral shell stacking machine 102, and a flocculating agent can be added into the flocculation tank to facilitate the dewatering and filter pressing operation in the spiral shell stacking machine 102. The flocculating agent mainly adopts PAC and PAM, PAC agents can be added firstly, the adding amount is 20-40 mg/L, effective coagulation aiding is carried out, PAM agents are added, the adding amount is 40-80 mg/L, stable alum floc is formed, and subsequent dehydration and filter pressing are facilitated. In the embodiment, after dehydration and filter pressing by the screw stacking machine 102, the coking wastewater sludge can be filter-pressed to reach the water content of 83-85%. In one embodiment, the separated supernatant is returned to a wastewater treatment system in a coking plant through a supernatant collection tank below the screw stack 102, so that wastewater discharge is reduced. The waste water sludge is subjected to the floating annular layer type spiral dewatering and filter pressing in the screw stacking machine 102, the effects of waste water sludge precipitation and solid-liquid separation are obvious, the subsequent sludge drying is facilitated, and the condition that the sludge blocks the pipe orifice of the screw stacking machine 102 can be avoided.
The sludge drier 103 preferably adopts a low-temperature heat source drier to directly contact the coking wastewater sludge with low-temperature air for heat exchange; the hot air used may be dry air produced via an air heat pump at a temperature between 80 c and 120 c. That is, the sludge drying machine 103 is connected with a first low-temperature air supply pipe, and the first low-temperature air supply pipe is connected to an air heat pump.
As mentioned in the first embodiment, the tar residue pretreatment unit is mainly used for reducing the water content of the tar residue, preferably reducing the water content of the tar residue to 70% -93%, and more preferably dewatering the tar residue to a dewatered tar residue with a water content of 82-85%. In one embodiment, as shown in fig. 1, the tar residue pretreatment unit comprises a conditioning demulsification reactor 201 and a slurry drier 202, wherein the conditioning demulsification reactor 201 is provided with a scraper stirring mechanism, a second demulsification agent bin and a residue heating mechanism for heating tar residue. The slag liquid heating mechanism can be an electric heating device such as an electric heater arranged in the quenching and tempering demulsification reactor 201, realizes heating of tar slag, preferably stirs the tar slag at the temperature of 75-90 ℃, and adjusts the fluidity of the tar slag to be in a homogeneous state. The second demulsifier bin can add demulsifier into the tar residue during the stirring process, can improve the emulsification state of the tar residue and can increase oil-water separation. The demulsifier can also adopt a compound solution taking persulfate as a main component.
The slag slurry drier 202 preferably adopts a low-temperature heat source drier, so that tar slag is directly contacted with low-temperature air for heat exchange; the hot air used may be dry air produced via an air heat pump at a temperature between 80 c and 120 c. That is, the slurry dryer 202 is connected with a second low-temperature air supply pipe, and the second low-temperature air supply pipe is connected to the air heat pump; the second low-temperature air supply pipe and the first low-temperature air supply pipe can share one air heat pump.
In another embodiment, the drying of the coking wastewater sludge and the drying of the tar residue are performed in the same drying device, and the drying of the coking wastewater sludge and the drying of the tar residue can be performed simultaneously or in stages, that is, the sludge drying machine 202 and the sludge drying machine 103 are the same low-temperature heat source drying machine.
The waste mixing unit 300 is used for mixing dewatered sludge and dewatered tar residue, that is, the dewatered sludge outlet of the sludge dryer 103 and the dewatered tar residue outlet of the residue slurry dryer 202 are respectively connected with the material inlet of the waste mixing unit 300 through screw conveyors. In this embodiment, the waste mixing unit 300 includes a metering electronic scale, a stirring preparation machine and a tank body thereof, wherein a plurality of anti-adhesion chains are disposed on the conveying blades and the stirrer blades of the screw conveyer, and a plurality of sets of arch breaking devices are disposed at the feed opening of the stirring preparation machine to prevent tar slag from adhering to the equipment during the conveying and stirring processes.
For the above-mentioned forming unit 400, conventional material forming equipment such as a ball making machine, a briquetting machine, etc. may be used, and in this embodiment, the forming unit 400 includes a solidifying machine into which the mixture is fed for press forming.
The carbonization furnace 500 and the activation reaction tower 600 are conventional devices, and the detailed structure thereof is not described herein. It is further preferable that an impregnation device, such as an impregnation tank, or the like, is further provided between the carbonization furnace 500 and the activation reaction tower 600, for impregnating the intermediate carbonized material discharged from the carbonization furnace 500 with an activating agent, so as to ensure the effect of the activation treatment in the activation reaction tower 600. In one embodiment, the activator is 40% phosphoric acid solution, and the activator and the intermediate carbide are impregnated for 1d according to the mass ratio of 0.8:4, namely the impregnation equipment is connected with an activator supply pipe.
Further preferably, the system further includes a pickling device and a washing device, which are configured to pickle and wash the activated product generated by the activation reaction tower 600, that is, the activated product outlet of the activation reaction tower 600 is connected to the pickling device and the washing device through a material transfer unit, the material transfer unit may be, for example, a belt conveyor, and the pickling and washing of the activated product may be a conventional pickling operation and a washing operation, that is, the pickling device and the washing device are conventional devices in the field of activated carbon preparation, and specific structures are not described herein.
Further optimizing the above system, as shown in fig. 1, the carbonization furnace 500 is configured with a tail gas treatment pipeline, and a tail gas cooling mechanism and a tail gas catalytic reactor 701 are sequentially arranged on the tail gas treatment pipeline. The exhaust gas generated in the carbonization furnace 500 can be treated through the exhaust gas treatment pipeline, so that harmless emission is realized; the tail gas cooling mechanism may be a water cooling mechanism, for example, a water cooling tower, or another heat exchanger, and preferably, the tail gas cooling mechanism reduces the temperature of the exhaust gas to about 200 ℃, and introduces the exhaust gas into the tail gas catalytic reactor 701 for catalytic combustion.
In a further effective embodiment, a gas detection unit for detecting the content of organic benzene in the gas in the carbonization furnace 500 is arranged in the carbonization furnace, an induced draft fan is arranged on the tail gas treatment pipeline, the gas detection unit and the induced draft fan are in interlocking control, and for the interlocking control of the gas detection unit and the induced draft fan, the conventional automatic control mode is adopted, and additional programming is not needed, which is easy to design by a person skilled in the art, and is not described herein again. When detecting that the benzene content of the gas organic matters in the carbonization furnace 500 reaches a preset value, introducing the gas in the carbonization furnace 500 into a tail gas treatment pipeline through the induced draft fan for treatment.
Further preferably, the above-mentioned exhaust gas catalytic reactor 701 is provided with an activated carbon catalytic bed and an electric heating unit for heating the activated carbon catalytic bed, and the activated carbon catalytic bed is loaded with rare heavy metals (lanthanum, Ce, etc.). The electric heating unit can be an electric heating plate, for example, after the activated carbon catalytic bed is enriched with a certain amount of toxic gas, the activated carbon catalytic bed is heated to about 200 ℃ by the electric heating unit, and the toxic gas enriched on the catalytic bed is subjected to catalytic combustion decomposition. The tail gas catalytic reactor 701 can remove organic gas by more than 98%, and the remaining 2% of undecomposed gas is adsorbed by the subsequent activated carbon adsorber 702, that is, the activated carbon adsorber 702 is connected behind the tail gas catalytic reactor 701.
In an optional embodiment, the exhaust gas generated in the coking wastewater sludge drying process and the tar residue drying process may also be introduced into the exhaust gas catalytic reactor 701 for treatment, that is, the exhaust gas outlets of the sludge dryer 103 and the residue slurry dryer 202 are both communicated with the exhaust gas catalytic reactor 701. Of course, the waste gas generated in the drying process of the coking wastewater sludge and the drying process of the tar residue can be independently treated and is not expanded.
Further preferably, the quenching and tempering demulsification reactor 201 is a semi-closed device, a micro-negative pressure state is maintained in the stirring process, tail gas generated in the heating and stirring process can be treated by the tail gas catalytic reactor 701, and volatile organic compounds are prevented from leaking into the surrounding air in the heating and stirring process; for example, the tail gas outlet pipe of the modified demulsification reactor 201 is connected to the tail gas treatment pipeline.
Obviously, the first embodiment and the second embodiment are both designed for the synergistic treatment of the coking wastewater sludge and the tar residue, and the related contents of the two embodiments can complement and support each other.
The above description is only for the purpose of illustrating the preferred embodiments of the present invention and is not to be construed as limiting the invention, and any modifications, equivalents, improvements and the like that fall within the spirit and principle of the present invention are intended to be included therein.
Claims (10)
1. A method for the synergistic treatment of coking wastewater sludge and tar residue is characterized by comprising the following steps:
s1, pretreating coking wastewater sludge and tar residues to reduce the water content of the coking wastewater sludge to 30% -50% and the water content of the tar residues to 70% -93%;
s2, mixing and molding the dewatered sludge and the dewatered tar residues to obtain a molded mixture;
s3, taking the formed mixture as a raw material to prepare the activated carbon.
2. The coking wastewater sludge and tar residue co-processing method of claim 1, wherein in S1, the coking wastewater sludge pretreatment method comprises:
s111, adding an acid-base regulator, an ionic flocculant, an inorganic salt pretreating agent and a demulsifier into the coking wastewater sludge, and carrying out pre-shrinking treatment on the coking wastewater sludge;
s112, adding a flocculating agent into the coking wastewater sludge subjected to the pre-shrinking treatment, and then feeding the coking wastewater sludge into a spiral stacking machine for moving annular spiral dewatering and filter pressing to reduce the water content of the sludge to 75-88%;
s113, contacting the coking wastewater sludge treated in the step S102 with hot air, and drying to reduce the water content of the coking wastewater sludge to 30-50% to obtain the dewatered sludge.
3. The coking wastewater sludge and tar residue co-processing method of claim 1, wherein in S1, the tar residue pre-processing method comprises the following steps:
s121, heating and stirring the tar residue, adjusting the fluidity of the tar residue to be in a homogeneous state, and adding a demulsifier into the tar residue in the stirring process;
s122, contacting the flowing tar residue with hot air, and drying to reduce the water content of the tar residue to 70% -93%, thereby obtaining the dehydrated tar residue.
4. The method for the synergistic treatment of coking wastewater sludge and tar residue as claimed in claim 1, wherein in S3, the method for preparing activated carbon by using the formed mixture as a raw material comprises the following steps:
s301, feeding the formed mixture into a carbonization furnace for high-temperature carbonization to obtain an intermediate carbide, wherein the temperature in the carbonization furnace is controlled to be 600-850 ℃, and the residence time of the formed mixture in the carbonization furnace is controlled to be 4-7 hours;
s302, impregnating the intermediate carbide with an activating agent, and then performing activation treatment to obtain an activated substance;
s303, carrying out acid washing and water washing on the activated substance, and drying to obtain the activated carbon.
5. The coking wastewater sludge and tar residue co-processing method according to claim 4, characterized in that: in S302, the activation temperature is 650-700 ℃, and the activation time is within 3 h.
6. The coking wastewater sludge and tar residue co-processing method according to claim 1, characterized in that: in S2, the mixing ratio of the dewatered sludge to the dewatered tar residue is 1: 3-1: 5.
7. The utility model provides a coking wastewater mud and tar sediment cooperative processing system which characterized in that: comprises a waste mixing unit, a forming unit, a carbonization furnace and an activation reaction tower which are sequentially connected through a material transfer unit;
the device is characterized by further comprising a sludge pretreatment unit for reducing the water content of the coking wastewater sludge and a tar residue pretreatment unit for reducing the water content of the tar residue, wherein a dehydrated sludge outlet of the sludge pretreatment unit and a dehydrated tar residue outlet of the tar residue pretreatment unit are respectively connected with a material inlet of the waste mixing unit through a screw conveyer.
8. The coking wastewater sludge and tar residue co-processing system of claim 7, wherein: sludge pretreatment unit includes pretreatment reactor, folds spiral shell machine and sludge drying machine, pretreatment reactor disposes acid-base regulator feed bin, ionic flocculant feed bin, inorganic salt pretreatment agent feed bin and first demulsifier feed bin, the material entry of folding spiral shell machine pass through the thick liquid conveyer pipe with pretreatment reactor links up, the sludge outlet of folding spiral shell machine pass through belt conveyor with sludge drying machine links up.
9. The coking wastewater sludge and tar residue co-processing system of claim 7, wherein: the tar residue pretreatment unit comprises a conditioning demulsification reactor and a residue slurry drying machine, wherein the conditioning demulsification reactor is provided with a scraper stirring mechanism, a second demulsifier bin and a residue liquid heating mechanism for heating tar residues.
10. The coking wastewater sludge and tar residue co-processing system of claim 7, wherein: the carbonization furnace is provided with a tail gas treatment pipeline, and a tail gas cooling mechanism and a tail gas catalytic reactor are sequentially arranged on the tail gas treatment pipeline.
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111349450A (en) * | 2020-03-19 | 2020-06-30 | 山西潞安矿业(集团)有限责任公司 | Method for preparing high-specific-surface-area coke powder from tar residues |
| CN113877537A (en) * | 2021-11-19 | 2022-01-04 | 中国林业科学研究院林产化学工业研究所 | Method for preparing granular activated carbon from sludge |
Citations (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2000072427A (en) * | 1998-09-03 | 2000-03-07 | Kawasaki City | Production of active carbon by sludge |
| WO2008046298A1 (en) * | 2006-10-11 | 2008-04-24 | Dawei Zhang | A waste gas recovering method in regenerative process of the filtering-absorption material |
| CN102381705A (en) * | 2011-07-27 | 2012-03-21 | 西南科技大学 | Method for producing activated carbon by thermally activating coal tar dreg/ sludge fermentation body by using microwaves |
| CN103551137A (en) * | 2013-10-29 | 2014-02-05 | 天津市联合环保工程设计有限公司 | Preparation method and application of solid catalyst using sludge-based activated carbon as matrix material |
| JP5462503B2 (en) * | 2009-03-09 | 2014-04-02 | 新日鐵住金株式会社 | Recycling method of tar sludge discharged from coke oven |
| CN107557044A (en) * | 2017-10-24 | 2018-01-09 | 西北大学 | A kind of tar slag recycling treatment process |
| CN108504412A (en) * | 2018-04-24 | 2018-09-07 | 佛山市尚柏科技有限公司 | A kind of preparation method of sludge solid fuel |
| CN211366975U (en) * | 2019-11-06 | 2020-08-28 | 中冶南方都市环保工程技术股份有限公司 | Coking wastewater sludge and tar residue co-processing system |
-
2019
- 2019-11-06 CN CN201911075728.XA patent/CN110713182A/en active Pending
Patent Citations (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2000072427A (en) * | 1998-09-03 | 2000-03-07 | Kawasaki City | Production of active carbon by sludge |
| WO2008046298A1 (en) * | 2006-10-11 | 2008-04-24 | Dawei Zhang | A waste gas recovering method in regenerative process of the filtering-absorption material |
| JP5462503B2 (en) * | 2009-03-09 | 2014-04-02 | 新日鐵住金株式会社 | Recycling method of tar sludge discharged from coke oven |
| CN102381705A (en) * | 2011-07-27 | 2012-03-21 | 西南科技大学 | Method for producing activated carbon by thermally activating coal tar dreg/ sludge fermentation body by using microwaves |
| CN103551137A (en) * | 2013-10-29 | 2014-02-05 | 天津市联合环保工程设计有限公司 | Preparation method and application of solid catalyst using sludge-based activated carbon as matrix material |
| CN107557044A (en) * | 2017-10-24 | 2018-01-09 | 西北大学 | A kind of tar slag recycling treatment process |
| CN108504412A (en) * | 2018-04-24 | 2018-09-07 | 佛山市尚柏科技有限公司 | A kind of preparation method of sludge solid fuel |
| CN211366975U (en) * | 2019-11-06 | 2020-08-28 | 中冶南方都市环保工程技术股份有限公司 | Coking wastewater sludge and tar residue co-processing system |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111349450A (en) * | 2020-03-19 | 2020-06-30 | 山西潞安矿业(集团)有限责任公司 | Method for preparing high-specific-surface-area coke powder from tar residues |
| CN111349450B (en) * | 2020-03-19 | 2021-01-29 | 山西潞安矿业(集团)有限责任公司 | Method for preparing high-specific-surface-area coke powder from tar residues |
| CN113877537A (en) * | 2021-11-19 | 2022-01-04 | 中国林业科学研究院林产化学工业研究所 | Method for preparing granular activated carbon from sludge |
| CN113877537B (en) * | 2021-11-19 | 2023-11-17 | 中国林业科学研究院林产化学工业研究所 | Method for preparing granular activated carbon from sludge |
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