CN212018170U - Coal chemical industry gasification filter cake recycling system - Google Patents
Coal chemical industry gasification filter cake recycling system Download PDFInfo
- Publication number
- CN212018170U CN212018170U CN202020649016.6U CN202020649016U CN212018170U CN 212018170 U CN212018170 U CN 212018170U CN 202020649016 U CN202020649016 U CN 202020649016U CN 212018170 U CN212018170 U CN 212018170U
- Authority
- CN
- China
- Prior art keywords
- flotation
- feed inlet
- thickener
- flotation tank
- port
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
- 239000012065 filter cake Substances 0.000 title claims abstract description 54
- 238000002309 gasification Methods 0.000 title claims abstract description 39
- 239000003245 coal Substances 0.000 title claims abstract description 26
- 239000000126 substance Substances 0.000 title claims abstract description 19
- 238000004064 recycling Methods 0.000 title claims description 17
- 238000005188 flotation Methods 0.000 claims abstract description 201
- 239000002562 thickening agent Substances 0.000 claims abstract description 72
- 239000012141 concentrate Substances 0.000 claims abstract description 58
- 239000002351 wastewater Substances 0.000 claims abstract description 40
- 238000003756 stirring Methods 0.000 claims abstract description 28
- 230000003647 oxidation Effects 0.000 claims abstract description 26
- 238000007254 oxidation reaction Methods 0.000 claims abstract description 26
- 238000007599 discharging Methods 0.000 claims abstract description 6
- 239000004088 foaming agent Substances 0.000 claims description 27
- 239000003795 chemical substances by application Substances 0.000 claims description 25
- 239000006185 dispersion Substances 0.000 claims description 15
- 238000002156 mixing Methods 0.000 claims description 11
- 239000000047 product Substances 0.000 abstract description 35
- 230000008901 benefit Effects 0.000 abstract description 7
- 230000007613 environmental effect Effects 0.000 abstract description 3
- 230000026676 system process Effects 0.000 abstract description 3
- 238000000034 method Methods 0.000 description 34
- 230000002000 scavenging effect Effects 0.000 description 34
- 229910052799 carbon Inorganic materials 0.000 description 23
- 230000008569 process Effects 0.000 description 20
- 239000006260 foam Substances 0.000 description 18
- 239000002002 slurry Substances 0.000 description 17
- 230000004048 modification Effects 0.000 description 14
- 238000012986 modification Methods 0.000 description 14
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 13
- 239000003350 kerosene Substances 0.000 description 13
- 238000003825 pressing Methods 0.000 description 13
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 13
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 description 12
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 12
- 239000007788 liquid Substances 0.000 description 9
- 238000001914 filtration Methods 0.000 description 6
- 239000011268 mixed slurry Substances 0.000 description 6
- 239000011343 solid material Substances 0.000 description 6
- 239000004567 concrete Substances 0.000 description 5
- 239000004566 building material Substances 0.000 description 4
- 238000002485 combustion reaction Methods 0.000 description 4
- 239000008394 flocculating agent Substances 0.000 description 4
- 230000008676 import Effects 0.000 description 4
- TWNQGVIAIRXVLR-UHFFFAOYSA-N oxo(oxoalumanyloxy)alumane Chemical compound O=[Al]O[Al]=O TWNQGVIAIRXVLR-UHFFFAOYSA-N 0.000 description 4
- 239000000706 filtrate Substances 0.000 description 3
- 239000000446 fuel Substances 0.000 description 3
- 239000000463 material Substances 0.000 description 3
- 239000002994 raw material Substances 0.000 description 3
- 239000002893 slag Substances 0.000 description 3
- 239000006228 supernatant Substances 0.000 description 3
- 230000005540 biological transmission Effects 0.000 description 2
- 239000004568 cement Substances 0.000 description 2
- 238000005034 decoration Methods 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 238000000605 extraction Methods 0.000 description 2
- 230000002349 favourable effect Effects 0.000 description 2
- 239000002516 radical scavenger Substances 0.000 description 2
- 238000004062 sedimentation Methods 0.000 description 2
- 238000000926 separation method Methods 0.000 description 2
- 239000007787 solid Substances 0.000 description 2
- 239000000243 solution Substances 0.000 description 2
- 208000005156 Dehydration Diseases 0.000 description 1
- 239000000654 additive Substances 0.000 description 1
- 230000000996 additive effect Effects 0.000 description 1
- WUOACPNHFRMFPN-UHFFFAOYSA-N alpha-terpineol Chemical compound CC1=CCC(C(C)(C)O)CC1 WUOACPNHFRMFPN-UHFFFAOYSA-N 0.000 description 1
- 239000000567 combustion gas Substances 0.000 description 1
- 230000018044 dehydration Effects 0.000 description 1
- 238000006297 dehydration reaction Methods 0.000 description 1
- SQIFACVGCPWBQZ-UHFFFAOYSA-N delta-terpineol Natural products CC(C)(O)C1CCC(=C)CC1 SQIFACVGCPWBQZ-UHFFFAOYSA-N 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 239000002270 dispersing agent Substances 0.000 description 1
- 239000003814 drug Substances 0.000 description 1
- 229940079593 drug Drugs 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 239000008396 flotation agent Substances 0.000 description 1
- 229910052500 inorganic mineral Inorganic materials 0.000 description 1
- 239000011707 mineral Substances 0.000 description 1
- 239000011259 mixed solution Substances 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 230000003334 potential effect Effects 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 238000002791 soaking Methods 0.000 description 1
- 239000002689 soil Substances 0.000 description 1
- 238000007711 solidification Methods 0.000 description 1
- 230000008023 solidification Effects 0.000 description 1
- 230000001502 supplementing effect Effects 0.000 description 1
- 229940116411 terpineol Drugs 0.000 description 1
Images
Landscapes
- Physical Water Treatments (AREA)
Abstract
The utility model belongs to the technical field of the coal chemical industry, especially, relate to a coal chemical industry gasification filter cake resourceful system. The utility model provides a system includes: the stirring barrel is provided with a gasification filter cake inlet, a modified wastewater inlet and a discharge port; the discharge port of the oxidation modifying machine is connected with the modified wastewater inlet of the stirring barrel, and the oxidation modifying machine is provided with an oily wastewater inlet; the feeding hole of the first flotation tank is connected with the discharging hole of the stirring barrel; the feed inlet of the second flotation tank is connected with the concentrate outlet of the first flotation tank; the feed inlet of the first thickener is connected with a concentrate outlet of the second flotation tank; the feed inlet of the first filter press is connected with the underflow port of the first thickener; the feeding port of the second thickener is connected with a tailing outlet of the first flotation tank; and the feed inlet of the second filter press is connected with the bottom flow port of the second thickener. The utility model provides a resource system process flow is simple, and the running cost is low, and it is good to select separately the product index, has good economic benefits and environmental benefit.
Description
Technical Field
The utility model belongs to the technical field of the coal chemical industry, especially, relate to a coal chemical industry gasification filter cake resourceful system.
Background
The coal chemical industry in China keeps a high-speed growth situation continuously, coal chemical projects bloom all the time nationwide, and accordingly, a large amount of coal gasification ash is discharged, a large amount of land is occupied, and leachate of the coal gasification ash can seriously pollute soil and water, so that the disposal and utilization of the coal gasification ash are social problems which are not slow.
The coal gasification ash comprises two parts of gasification slag (coarse slag) and gasification filter cake (fine slag). At present, most of gasification filter cakes in coal chemical industry are used as building material raw materials at home and abroad, but building materials have economic applicable radiuses, and areas with relatively laggard economy have low building material market demand and are not enough to digest large batches of gasification filter cakes, and meanwhile, because the gasification filter cakes have high carbon content (about 20 percent), when the gasification filter cakes are used as admixture or aggregate to prepare concrete, the gasification filter cakes easily cause the consistency increase of slurry, poor flowability, long solidification time and strength reduction, and the durability of concrete opening making can be influenced.
Flotation carbon extraction is also an important research direction for resource utilization of the gasification filter cake, and the gasification filter cake contains a large amount of residual carbon, so that enrichment recovery can be performed through a flotation process, and resource utilization of the gasification filter cake is realized. However, the ash particle size of the gasified filter cake is fine, and the surface porosity is high, so that the ash of the gasified filter cake has extremely high surface energy, and the problems of large drug consumption, poor selectivity and the like exist in the flotation process, and further the flotation cost is improved and the quality of the flotation product is reduced.
SUMMERY OF THE UTILITY MODEL
In view of this, the utility model aims at providing a coal chemical industry gasification filter cake resource system, the utility model provides a resource system process flow is simple, and the running cost is low, can obtain the high carbon product and the high grey product that the index is good.
The utility model provides a coal chemical industry gasification filter cake resourceful system, include:
the stirring barrel is provided with a gasified filter cake inlet, a modified wastewater inlet, a dispersion regulator dosing port, a collecting agent dosing port, a foaming agent dosing port and a discharge port;
the discharge port of the oxidation modifying machine is connected with the modified wastewater inlet of the stirring barrel, and the oxidation modifying machine is provided with an oily wastewater inlet;
the feeding hole of the first flotation tank is connected with the discharging hole of the stirring barrel;
the feed inlet of the second flotation tank is connected with the concentrate outlet of the first flotation tank;
the feed inlet of the first thickener is connected with the concentrate outlet of the second flotation tank;
the feed inlet of the first filter press is connected with the bottom flow port of the first thickener;
the feeding hole of the second thickener is connected with a tailing outlet of the first flotation tank;
and the feed inlet of the second filter press is connected with the bottom flow port of the second thickener.
Preferably, the system further comprises a third flotation tank arranged between the tailings outlet of the first flotation tank and the feed inlet of the second thickener;
the feed inlet of third flotation cell with the tailings export of first flotation cell links to each other, the concentrate export of third flotation cell with the feed inlet of second flotation cell links to each other, the tailings export of third flotation cell with the feed inlet of second thickener links to each other.
Preferably, the third flotation tank is provided with a collector dosing port and a foaming agent dosing port.
Preferably, the system further comprises a fourth flotation tank arranged between the tailings outlet of the third flotation tank and the feed inlet of the second thickener;
the feed inlet of fourth flotation cell with the tailings export of third flotation cell links to each other, the concentrate export of fourth flotation cell with the feed inlet of second flotation cell links to each other, the tailings export of fourth flotation cell with the feed inlet of second thickener links to each other.
Preferably, the fourth flotation tank is provided with a collector dosing port and a foaming agent dosing port.
Preferably, the system further comprises a feeding bin for storing the gasified filter cake, and a discharge port of the feeding bin is connected with a gasified filter cake inlet of the stirring barrel.
Preferably, the first thickener and the second thickener are both provided with flocculant adding openings.
Preferably, the tailings outlet of the second flotation tank is connected with the feed inlet of the first flotation tank.
Compared with the prior art, the utility model provides a coal industry gasification filter cake resourceful system. The utility model provides a resource system includes: the stirring barrel is provided with a gasified filter cake inlet, a modified wastewater inlet, a dispersion regulator dosing port, a collecting agent dosing port, a foaming agent dosing port and a discharge port; the discharge port of the oxidation modifying machine is connected with the modified wastewater inlet of the stirring barrel, and the oxidation modifying machine is provided with an oily wastewater inlet; the feeding hole of the first flotation tank is connected with the discharging hole of the stirring barrel; the feed inlet of the second flotation tank is connected with the concentrate outlet of the first flotation tank; the feed inlet of the first thickener is connected with the concentrate outlet of the second flotation tank; the feed inlet of the first filter press is connected with the bottom flow port of the first thickener; the feeding hole of the second thickener is connected with a tailing outlet of the first flotation tank; and the feed inlet of the second filter press is connected with the bottom flow port of the second thickener. When the system is operated, firstly conveying the gasified filter cake and the oily wastewater treated by the oxidation modification machine into a stirring barrel, adding a dispersion regulator into the stirring barrel, and simultaneously adding a proper amount of a collecting agent and a foaming agent to obtain mixed slurry; then, the mixed slurry enters a flotation tank for flotation to obtain flotation concentrate (high-carbon foam) and flotation tailings (high-ash tailing pulp); and finally, treating the flotation concentrate and the tailings in corresponding thickeners and filter presses respectively to obtain high-carbon products and high-ash products. The recycling system provided by the utility model can achieve the purpose of forced dispersion by adding the dispersant to adjust the rheological property of the filter cake slurry system and the electrical property of the material surface, thereby creating favorable conditions for the next flotation process; the oily wastewater is subjected to corresponding oxidation modification treatment, so that a collector in the flotation process can be completely or partially replaced, and the cost of the flotation process is reduced to a great extent. In the utility model, after the filter cake is subjected to the flotation carbon extraction process and the dehydration treatment, the ash content of the high-carbon product is reduced, the volatile component and the carbon content are obviously improved, the combustion characteristic is improved, the calorific value is close to the calorific value of coal, and the high-carbon product can be directly put into boiler equipment to be mixed with coal-fired fuel for combustion; the carbon content of the tailing product can be as low as below 1 wt%, and the ash content can be as high as above 95 wt%, so that the tailing product can be used for preparing the additive of concrete. The utility model provides a resource system process flow is simple, and the running cost is low, and it is good to select separately the product index, has good economic benefits and environmental benefit.
Drawings
In order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the drawings required to be 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 embodiments of the present invention, and for those skilled in the art, other drawings can be obtained according to the provided drawings without creative efforts.
FIG. 1 is a schematic view of a process flow of a coal chemical gasification filter cake recycling system provided by an embodiment of the present invention;
fig. 2 is a schematic view of a process flow of a coal chemical gasification filter cake recycling system provided in embodiment 1 of the present invention.
Detailed Description
The technical solutions in the embodiments of the present invention will be described clearly and completely with reference to the accompanying drawings in the embodiments of the present invention, and it is obvious that the described embodiments are only some embodiments of the present invention, not all embodiments. Based on the embodiments in the present invention, all other embodiments obtained by a person skilled in the art without creative work belong to the protection scope of the present invention.
The utility model provides a coal chemical industry gasification filter cake resourceful system, include:
the stirring barrel is provided with a gasified filter cake inlet, a modified wastewater inlet, a dispersion regulator dosing port, a collecting agent dosing port, a foaming agent dosing port and a discharge port;
the discharge port of the oxidation modifying machine is connected with the modified wastewater inlet of the stirring barrel, and the oxidation modifying machine is provided with an oily wastewater inlet;
the feeding hole of the first flotation tank is connected with the discharging hole of the stirring barrel;
the feed inlet of the second flotation tank is connected with the concentrate outlet of the first flotation tank;
the feed inlet of the first thickener is connected with the concentrate outlet of the second flotation tank;
the feed inlet of the first filter press is connected with the bottom flow port of the first thickener;
the feeding hole of the second thickener is connected with a tailing outlet of the first flotation tank;
and the feed inlet of the second filter press is connected with the bottom flow port of the second thickener.
Referring to fig. 1, fig. 1 is a schematic diagram of a process flow of a coal chemical gasification filter cake recycling system provided by an embodiment of the present invention.
The utility model provides a resource system includes agitator, oxidation modification machine, first flotation cell, second flotation cell, first thickener, first pressure filter, second thickener and second pressure filter. The stirring barrel is used for forcibly dispersing the gasified filter cake and uniformly mixing all materials, and is provided with a gasified filter cake inlet, a modified wastewater inlet, a dispersing regulator dosing port, a collecting agent dosing port, a foaming agent dosing port and a discharge port.
The utility model provides an among the resource system, the modified machine of oxidation is used for carrying out the oxidation modification to oily waste water, is provided with oily waste water import and discharge gate on it, the discharge gate of the modified machine of oxidation with the modified waste water import of agitator links to each other.
The utility model provides an among the resource system, first flotation cell is provided with feed inlet, concentrate export and tailings export, the feed inlet of first flotation cell with the discharge gate of agitator links to each other, is used for right the gasification filter cake mixed slurry of agitator discharge gate combustion gas carries out the rough concentration. In one embodiment of the present invention, the first flotation cell is a gearless flotation cell.
The utility model provides an among the resource system, the second flotation cell is provided with feed inlet, concentrate export and tailings export, the feed inlet of second flotation cell with the concentrate export of first flotation cell links to each other, is used for right first flotation cell concentrate export exhaust rougher concentrate foam carries out the choice. In one embodiment of the present invention, the second flotation tank is a non-driven flotation tank. In one embodiment of the present invention, the tailings outlet of the second flotation tank is connected to the feed inlet of the first flotation tank.
The utility model provides an among the resource system, first thickener is provided with feed inlet, overflow mouth and underflow opening, the feed inlet of first thickener with the concentrate export of second flotation cell links to each other, is used for right second flotation cell concentrate export exhaust choice concentrate foam is concentrated. In one embodiment of the present invention, the first thickener is further provided with a flocculant feeding port. In one embodiment of the present invention, the first and second,the inner diameter of the tank body of the first thickener is preferably 3000-8000 mm, and particularly can be 6000 mm; the height of the groove body is preferably 1000-5000 mm, and specifically can be 2300 mm; the settlement area is preferably 20-40 m2Specifically, it may be 27.6m2. In one embodiment of the present invention, the model of the first thickener is GX-6.
The utility model provides an among the resource system, first pressure filter is provided with feed inlet, filtrating export and solid material export, the feed inlet of first pressure filter with the underflow opening of first thickener links to each other, is used for right the first thickener underflow ore pulp of underflow opening exhaust carries out the filter-pressing and obtains high carbon product (solid material). In one embodiment of the present invention, the filtering area of the first filter press is preferably 50-200 m2Specifically, it may be 50m2、100m2、150m2Or 200m2. In one embodiment of the present invention, the first filter press has a model number of Z100/1250-30U.
The utility model provides an among the resource system, the second thickener is provided with feed inlet, overflow mouth and underflow opening, the feed inlet of second thickener with the tailing export of first flotation cell links to each other, is used for right the tailing of first flotation cell export exhaust rougher tailing thick pulp carries out the concentration. In one embodiment of the present invention, the second thickener is further provided with a flocculant feeding port. In an embodiment of the present invention, the inner diameter of the tank body of the second thickener is preferably 3000 to 8000mm, and specifically may be 6000 mm; the height of the groove body is preferably 1000-5000 mm, and specifically can be 2300 mm; the settlement area is preferably 20-40 m2Specifically, it may be 27.6m2. In one embodiment of the present invention, the model of the second thickener is GX-6.
The utility model provides an among the resource system, the second pressure filter is provided with feed inlet, filtrating export and solid material export, the feed inlet of second pressure filter with the underflow opening of second thickener links to each other, and it is right to be used for the second thickener underflow ore pulp of underflow opening exhaust carries out the filter-pressing and obtains high ash product (solid material). The utility model discloses carryIn one embodiment, the filtering area of the second filter press is preferably 50-200 m2Specifically, it may be 50m2、100m2、150m2Or 200m2. In one embodiment of the present invention, the second filter press has a model number of Z100/1250-30U.
In an embodiment of the utility model, the system still includes the feed bin, the feed bin is used for storing the gasification filter cake, is provided with feed inlet and discharge gate on it, the discharge gate of feed bin with the gasification filter cake import of agitator links to each other. In one embodiment of the utility model, the discharge gate of feeding bin with link to each other through the batcher between the gasification filter cake import of agitator.
In an embodiment of the utility model, the system still includes the third flotation cell, the third flotation cell sets up between the tailing export of first flotation cell and the feed inlet of second thickener, is provided with feed inlet, concentrate export and tailing export on it, the feed inlet of third flotation cell with the tailing export of first flotation cell links to each other, the concentrate export of third flotation cell with the feed inlet of second flotation cell links to each other, the tailing export of third flotation cell with the feed inlet of second thickener links to each other. The utility model discloses in, the third flotation cell is used for right first flotation cell tailings export exhaust rougher tailings pulp is swept and is selected, and the second flotation cell is carried to the sweep concentrate foam that the scavenging obtained carries and is selected, and the sweep tailing pulp that the scavenging obtained carries the second thickener and concentrates. In one embodiment provided by the present invention, the third flotation tank is further provided with a collector dosing port and a frother dosing port. In one embodiment of the present invention, the third flotation tank is a non-driven flotation tank.
In an embodiment of the utility model provides an, the system still includes the fourth flotation cell, the fourth flotation cell sets up the tailings export of third flotation cell with between the feed inlet of second thickener, be provided with feed inlet, concentrate export and tailings export on it, the feed inlet of fourth flotation cell with the tailings export of third flotation cell links to each other, the concentrate export of fourth flotation cell with the feed inlet of second flotation cell links to each other, the tailings export of fourth flotation cell with the feed inlet of second thickener links to each other. The utility model discloses in, the fourth flotation cell is used for right the third flotation cell tailings export exhaust scavenging tailing pulp carries out the secondary scavenging, and the secondary scavenging that the secondary scavenged the selection obtains sweeps the concentrate foam and carries the second flotation cell and carry out the choice, and the secondary scavenging that the secondary scavenged the selection obtains sweeps the tailing pulp and carries the second thickener and concentrate. In one embodiment of the present invention, the fourth flotation cell is further provided with a collector dosing port and a frother dosing port. In one embodiment of the present invention, the fourth flotation tank is a non-transmission flotation tank.
The utility model also provides a coal chemical industry gasification filter cake resourceful method, including following step:
a) mixing the gasified filter cake, the dispersion regulator, the collecting agent, the foaming agent and the oxidized and modified oily wastewater to obtain slurry;
b) performing flotation and roughing on the slurry to obtain roughing concentrate foam and roughing tailing slurry;
c) carrying out flotation and concentration on the roughing concentrate foam, and then concentrating and filter-pressing the obtained concentrated concentrate foam to obtain a high-carbon product;
d) concentrating and filter-pressing the roughed tailing pulp to obtain a high-ash product;
the step c) and the step d) have no precedence requirement.
The utility model provides an among the resourceful method, at first will gasify filter cake, dispersion adjustment agent, collecting agent, foaming agent and mix through the oily waste water of oxidation modification. Wherein the water content of the gasified filter cake is preferably 40-60 wt%, and specifically can be 40 wt%, 45 wt%, 50 wt%, 55 wt% or 60 wt%; the carbon content of the gasification filter cake is preferably 10-30 wt%, and specifically can be 10 wt%, 15 wt%, 20 wt%, 25 wt% or 30 wt%; the oily wastewater after oxidation modification is obtained by treating oily wastewater in an oxidation modification machine; the oil content of the oily wastewater is preferably 400-600 g/L, and specifically can be 400g/L, 450g/L, 500g/L, 550g/L or 600 g/L; the specific process of the treatment comprises the following steps: mixing oily wastewater with methanol, and then carrying out oxidation modification in the presence of sodium hydroxide and aluminum oxide; the molar ratio of the oily wastewater to the methanol is preferably (3-8) in terms of pure water: 1, specifically 3:1, 4:1, 5:1, 6:1, 7:1 or 8: 1; the dosage of the sodium hydroxide is preferably 0.5-3 wt% of the oil-containing wastewater, and more preferably 1-1.8 wt%; the dosage of the aluminum oxide is preferably 0.01-0.1 wt% of the mass of the oily wastewater, and more preferably 0.03-0.05 wt%; the oxidation modification machine is preferably the oxidation modification machine introduced above; the grade of the dispersion regulator is preferably HXAD-3#, and the dispersion regulator of the grade is provided by Xin flotation company; the addition amount of the dispersion regulator is preferably 1-5 kg/t, and specifically can be 1kg/t, 1.5kg/t, 2kg/t, 2.5kg/t, 3kg/t, 3.5kg/t, 4kg/t, 4.5kg/t or 5kg/t, based on the dry gasification filter cake of unit mass; the collector is preferably kerosene; the addition amount of the collecting agent is preferably 1-10 kg/t, and specifically can be 1kg/t, 2kg/t, 3kg/t, 4kg/t, 5kg/t, 6kg/t, 7kg/t, 8kg/t, 9kg/t or 10kg/t, calculated by unit mass of the dry gasification filter cake; the frothing agent is preferably # 2 oil (terpineol oil); the addition amount of the foaming agent is preferably 500-1000 g/t, and specifically can be 500g/t, 550g/t, 600g/t, 650g/t, 700g/t, 750g/t, 800g/t, 850g/t, 900g/t, 950g/t or 1000g/t, based on the dry gasification filter cake of unit mass; the mixing is preferably carried out in the mixing tank described above. And (3) uniformly mixing to obtain a slurry, wherein the solid content of the slurry is preferably 10-20 wt%, and specifically can be 10 wt%, 11 wt%, 12 wt%, 13 wt%, 14 wt%, 15 wt%, 16 wt%, 17 wt%, 18 wt%, 19 wt% or 20 wt%.
The utility model provides an among the resource method, after obtaining mixed thick liquids, right the thick liquids carry out the flotation rougher. Wherein the flotation rougher flotation is preferably carried out in the first flotation cell described above; the foaming agent added in the flotation roughing is preferably 2# oil, and the addition amount of the foaming agent in a flotation roughing system is preferably 100-1000 g/t, and specifically can be 100g/t, 200g/t, 300g/t, 400g/t, 500g/t, 600g/t, 700g/t, 800g/t, 900g/t or 1000 g/t; the collecting agent added in the flotation roughing is preferably kerosene, the addition amount of the kerosene in a flotation roughing system is preferably 1-10 kg/t, and specifically can be 1kg/t, 2kg/t, 3kg/t, 4kg/t, 4.2kg/t, 5kg/t, 6kg/t, 7kg/t, 8kg/t, 9kg/t or 10 kg/t. After flotation and roughing, roughing concentrate foam and roughing tailing slurry are obtained.
In the resource method provided by the utility model, after the rougher concentrate foam is obtained, the rougher concentrate foam is subjected to flotation and fine selection. Wherein the flotation concentration is preferably carried out in the second flotation cell described above; the foaming agent added in the flotation concentration is preferably No. 2 oil, and the addition amount of the foaming agent in a flotation concentration system is preferably 100-1000 g/t, and specifically can be 100g/t, 200g/t, 300g/t, 400g/t, 500g/t, 600g/t, 700g/t, 800g/t, 900g/t or 1000 g/t; the collecting agent added in the flotation concentration is preferably kerosene, the addition amount of the kerosene in a flotation concentration system is preferably 1-10 kg/t, and specifically can be 1kg/t, 2kg/t, 3kg/t, 4kg/t, 5kg/t, 5.1kg/t, 6kg/t, 7kg/t, 8kg/t, 9kg/t or 10 kg/t. After flotation and concentration, concentrated concentrate foam and concentrated tailing slurry are obtained.
In the resource method provided by the utility model, after the selected tailing pulp and the selected concentrate foam are obtained, the selected tailing pulp is preferably returned to the flotation roughing procedure for flotation roughing again; and the fine concentrate soaking is sequentially concentrated and filter-pressed. Wherein, preferably, a certain amount of flocculant is added to the concentrate froth during concentration; the flocculant is preferably of the grade H66, supplied by the company buff flotation; the addition amount of the flocculating agent in the concentrated concentrate foam is preferably 10-40 g/t, and specifically can be 10g/t, 15g/t, 20g/t, 25g/t, 30g/t, 35g/t or 40 g/t; the concentration is preferably carried out in the first thickener described above; the press filtration is preferably carried out in the first press filter described above. And after the filter pressing is finished, obtaining a high-carbon product, wherein the water content of the high-carbon product is preferably less than or equal to 20 wt%, and more preferably less than or equal to 18 wt%. The utility model discloses in, the supernatant of overflow and the filtrating that the filter-pressing in-process produced can return to the flotation process or do other usefulness as the reuse water among the concentration process.
The utility model provides an among the resourceful method, after obtaining the rougher tailing thick liquid, it is right rougher tailing thick liquid carries out concentration and filter-pressing in proper order. Wherein, a certain amount of flocculating agent is preferably added into the tailing pulp in the concentration process; the flocculant is preferably of the grade H66; the addition amount of the flocculating agent in the tailing pulp is preferably 5-30 g/t, and specifically can be 5g/t, 10g/t, 15g/t, 20g/t, 25g/t or 30 g/t; the concentration is preferably carried out in the second thickener described above; the press filtration is preferably carried out in the second filter press described above. And after the filter pressing is finished, obtaining a high ash product, wherein the water content of the high ash product is preferably less than or equal to 35 wt%, and more preferably less than or equal to 30 wt%. The utility model discloses in, the supernatant of overflow and the filtrating that the filter-pressing in-process produced can return to the flotation process or do other usefulness as the reuse water among the concentration process.
The utility model provides an among the resourceful method, in order to improve the flotation effect, reduce the carbon content of high grey product, it is preferred not right rougher tailing thick liquid directly carries out concentration and filter-pressing, but earlier right rougher tailing liquid carries out the flotation scavenging, then carries out concentration and filter-pressing to scavenging tailing liquid again, obtains high grey product. The method comprises the following specific steps:
d1) performing flotation scavenging on the roughing tailing slurry to obtain scavenging concentrate foam and scavenging tailing slurry;
d2) incorporating the scavenger concentrate foam into the rougher concentrate foam; and concentrating and filter-pressing the scavenging tailing slurry to obtain a high-ash product.
In the above step provided by the present invention involving a scavenging process, the flotation scavenging is preferably carried out in the third flotation cell described above; the foaming agent added in the flotation scavenging is preferably 2# oil, and the addition amount of the foaming agent in a flotation scavenging system is preferably 100-500 g/t, and specifically can be 100g/t, 150g/t, 200g/t, 250g/t, 300g/t, 350g/t, 400g/t, 450g/t or 500 g/t; the collecting agent added in the flotation scavenging is preferably kerosene, the addition amount of the kerosene in a flotation scavenging system is preferably 1-5 kg/t, and specifically can be 1kg/t, 1.5kg/t, 2kg/t, 2.5kg/t, 3kg/t, 3.5kg/t, 3.8kg/t, 4kg/t, 4.5kg/t or 5 kg/t.
The utility model provides an in the above-mentioned step that contains scavenging technology, accomplish the flotation and scavenge the back, the preferred scavenging tailing pulp that obtains carries out the flotation of second time and scavenges, obtains the secondary scavenging concentrate foam and the secondary scavenging tailing pulp. Wherein the secondary scavenger concentrate froth is incorporated into the rougher concentrate froth; and concentrating and filter-pressing the secondary scavenging tailing slurry to obtain a high-ash product. In the present invention, the secondary flotation scavenging is preferably performed in the fourth flotation cell described above; the foaming agent added in the secondary flotation scavenging is preferably 2# oil, and the addition amount of the foaming agent in a secondary flotation scavenging system is preferably 100-500 g/t, and specifically can be 100g/t, 150g/t, 200g/t, 250g/t, 300g/t, 350g/t, 400g/t, 450g/t or 500 g/t; the collecting agent added in the secondary flotation scavenging is preferably kerosene, and the addition amount of the kerosene in a secondary flotation scavenging system is preferably 1-5 kg/t, and specifically can be 1kg/t, 1.5kg/t, 2kg/t, 2.5kg/t, 3kg/t, 3.5kg/t, 3.8kg/t, 4kg/t, 4.5kg/t or 5 kg/t.
The utility model provides a resource system and resource method process flow are simple, and the running cost is low, and it is good to select separately the product index, has good economic benefits and environmental benefit. More specifically, the utility model provides a resource system and method includes following advantage at least:
1) the rheological property of a filter cake mixed slurry system and the electric property of the surface of the material are adjusted by using the dispersion regulator, so that the aim of forced dispersion is fulfilled, and favorable conditions are created for the next flotation process;
2) the oxidized and modified oily wastewater replaces part of collecting agents in the flotation process, so that the cost of the flotation agents is greatly saved;
3) the ash content of the high-carbon product obtained by sorting is low, the volatile matter and carbon content are high, the combustion characteristic is good, and the calorific value is close to the calorific value of coal; the high-carbon product has large specific surface area and strong activity, is easy to catch fire and burn out, and can be directly put into boiler equipment to be mixed and combusted with coal-fired fuel;
4) the high ash product obtained by sorting has large water content, fine granularity, large reserve and certain potential activity, and can be directly used for producing premixed concrete as a mineral admixture; in addition, the high ash product can be used as a siliceous raw material for producing cement or a cement admixture after being dried.
For the sake of clarity, the following examples are given in detail.
Example 1
A coal chemical gasification filter cake recycling system as shown in fig. 2, comprising: the device comprises a feeding bin, a stirring barrel, an oxidation modification machine, a first flotation tank, a second flotation tank, a third flotation tank, a fourth flotation tank, a first thickener, a first filter press, a second thickener and a second filter press.
Wherein the feeding bin is provided with a feeding hole and a discharging hole;
the stirring barrel is provided with a gasified filter cake inlet, a modified wastewater inlet, a dispersion regulator dosing port, a collecting agent dosing port, a foaming agent dosing port and a discharge port, and the gasified filter cake inlet of the stirring barrel is connected with the discharge port of the feeding bin through a feeder;
the oxidation modifying machine is provided with an oily wastewater inlet and a discharge port, and the discharge port of the oxidation modifying machine is connected with the modified wastewater inlet of the stirring barrel;
the first flotation tank is provided with a feed inlet, a concentrate outlet and a tailing outlet, and the feed inlet of the first flotation tank is connected with the discharge outlet of the stirring barrel;
the second flotation tank is provided with a feed inlet, a concentrate outlet and a tailing outlet, the feed inlet of the second flotation tank is connected with the concentrate outlet of the first flotation tank, and the tailing outlet of the second flotation tank is connected with the feed inlet of the first flotation tank;
the third flotation tank is provided with a feed inlet, a collecting agent dosing port, a foaming agent dosing port, a concentrate outlet and a tailing outlet, the feed inlet of the third flotation tank is connected with the tailing outlet of the first flotation tank, and the concentrate outlet of the third flotation tank is connected with the feed inlet of the second flotation tank;
the fourth flotation tank is provided with a feed inlet, a collecting agent dosing port, a foaming agent dosing port, a concentrate outlet and a tailing outlet, the feed inlet of the fourth flotation tank is connected with the tailing outlet of the third flotation tank, and the concentrate outlet of the fourth flotation tank is connected with the feed inlet of the second flotation tank;
the first flotation tank, the second flotation tank, the third flotation tank and the fourth flotation tank are all non-transmission flotation tanks;
the first thickener is provided with a feed inlet, a flocculant dosing port, an overflow port and a bottom flow port, and the feed inlet of the first thickener is connected with a concentrate outlet of the second flotation tank; the type of the first thickener is GX-6, the inner diameter of the tank body is 6000mm, the height of the tank body is 2300mm, and the sedimentation area is 27.6m2；
The first filter press is provided with a feed inlet, a filtrate outlet and a solid material outlet, and the feed inlet of the first filter press is connected with the underflow port of the first thickener; the model of the first filter press is Z100/1250-30U, and the filtering area is 100m2；
The second thickener is provided with a feed inlet, a flocculant dosing port, an overflow port and a bottom flow port, and the feed inlet of the second thickener is connected with a tailing outlet of the fourth flotation tank; the model of the second thickener is GX-6, the inner diameter of the tank body is 6000mm, the height of the tank body is 2300mm, and the sedimentation area is 27.6m2；
The second filter press is provided with a feed inlet, a filtrate outlet and a solid material outlet, and the feed inlet of the second filter press is connected with the underflow port of the second thickener; the model of the second filter press is Z100/1250-30U, and the filtering area is 100m2。
Example 2
A method for recycling a coal chemical gasification filter cake is carried out in the recycling system of the embodiment 1, and the specific process flow is as follows:
1) the gasified filter cake (the water content is about 50 wt%, and the carbon content is about 20 wt%) is transferred to a feeding bin through an automobile, and then is uniformly conveyed to a stirring barrel through a feeding machine;
2) mixing oily wastewater (with the oil content of 500-550 g/L) and methanol according to the molar ratio of 5:1 of water to methanol, adding a mixed solution containing sodium hydroxide and aluminum oxide, wherein the amount of the sodium hydroxide is 1.0-1.8 wt% of the oily wastewater, and the amount of the aluminum oxide is 0.03-0.05 wt% of the oily wastewater, and carrying out oxidation modification on the oily wastewater to obtain oxidation-modified oily wastewater; then, conveying the oxidized and modified oily wastewater into a stirring barrel, and controlling the solid content of slurry in the stirring barrel to be about 15 wt%; adding 2.5kg/t of HXAD-3# serving as a dispersion regulator into a stirring barrel by taking the dry gasification filter cake of unit mass as a basis, and simultaneously supplementing 700g/t of 2# oil serving as a foaming agent and 6kg/t of kerosene serving as a collecting agent to obtain slurry after size mixing;
3) performing flotation on the size-mixed slurry, wherein the flotation process comprises primary roughing, secondary scavenging and primary concentration, and is performed in a first flotation tank (roughing), a third flotation tank (scavenging I), a fourth flotation tank (scavenging II) and a second flotation tank (concentrating) respectively; 500g/t of 2# oil is added in the roughing flow to serve as a foaming agent and 4.2kg/t of kerosene is added in the roughing flow to serve as a collecting agent, 600g/t of 2# oil is added in the concentrating flow to serve as the foaming agent and 5.1kg/t of kerosene is added in the concentrating flow to serve as the collecting agent; 350g/t of 2# oil is added as a foaming agent and 3.8kg/t of kerosene is added as a collecting agent in the two times of scavenging; meanwhile, adding collecting agents, foaming agents and other agents according to actual conditions in the scavenging operation;
4) after the slurry is subjected to flotation after size mixing, the obtained concentrated concentrate foam is sequentially treated in a first thickener and a first filter press, and 20g/t of H66 flocculant is added into the first thickener during treatment to strengthen solid-liquid separation, so that a high-carbon product with the water content of less than 18 wt% is obtained;
after the size-mixed slurry is subjected to flotation, the obtained scavenging II tailing slurry is sequentially treated in a second thickener and a second filter press, and during treatment, 15g/t of H66 flocculating agent is added into the second thickener to strengthen solid-liquid separation, so that a high-ash product with the water content of less than 30 wt% is obtained;
5) the supernatant from the thickener overflow and the filtrate from the filter press are used as reuse water as the case may be.
The carbon content of the high-carbon product obtained by the embodiment is more than 40 wt%, and the product accounts for 25-30 wt%, and can be used for fuel blending combustion; the ash content of the obtained high-ash product is more than 95 wt%, the product accounts for 70-75 wt%, and the high-ash product can be used as a building material raw material for preparing concrete and the like.
The foregoing is only a preferred embodiment of the present invention, and it should be noted that, for those skilled in the art, a plurality of modifications and decorations can be made without departing from the principle of the present invention, and these modifications and decorations should also be regarded as the protection scope of the present invention.
Claims (8)
1. A coal chemical industry gasification filter cake recycling system includes:
the stirring barrel is provided with a gasified filter cake inlet, a modified wastewater inlet, a dispersion regulator dosing port, a collecting agent dosing port, a foaming agent dosing port and a discharge port;
the discharge port of the oxidation modifying machine is connected with the modified wastewater inlet of the stirring barrel, and the oxidation modifying machine is provided with an oily wastewater inlet;
the feeding hole of the first flotation tank is connected with the discharging hole of the stirring barrel;
the feed inlet of the second flotation tank is connected with the concentrate outlet of the first flotation tank;
the feed inlet of the first thickener is connected with the concentrate outlet of the second flotation tank;
the feed inlet of the first filter press is connected with the bottom flow port of the first thickener;
the feeding hole of the second thickener is connected with a tailing outlet of the first flotation tank;
and the feed inlet of the second filter press is connected with the bottom flow port of the second thickener.
2. The recycling system according to claim 1, further comprising a third flotation tank disposed between the tailings outlet of the first flotation tank and the feed inlet of the second thickener;
the feed inlet of third flotation cell with the tailings export of first flotation cell links to each other, the concentrate export of third flotation cell with the feed inlet of second flotation cell links to each other, the tailings export of third flotation cell with the feed inlet of second thickener links to each other.
3. The recycling system according to claim 2, wherein the third flotation cell is provided with a collector dosing port and a frother dosing port.
4. The recycling system according to claim 2, further comprising a fourth flotation tank disposed between the tailings outlet of the third flotation tank and the feed inlet of the second thickener;
the feed inlet of fourth flotation cell with the tailings export of third flotation cell links to each other, the concentrate export of fourth flotation cell with the feed inlet of second flotation cell links to each other, the tailings export of fourth flotation cell with the feed inlet of second thickener links to each other.
5. The recycling system according to claim 4, wherein the fourth flotation cell is provided with a collector dosing port and a frother dosing port.
6. The recycling system according to claim 1, further comprising a feed bin for storing the gasified cake, wherein the discharge port of the feed bin is connected to the gasified cake inlet of the mixing drum.
7. The recycling system according to claim 1, wherein the first thickener and the second thickener are each provided with a flocculant addition port.
8. The recycling system according to any one of claims 1 to 7, wherein the tailings outlet of the second flotation tank is connected to the feed inlet of the first flotation tank.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202020649016.6U CN212018170U (en) | 2020-04-26 | 2020-04-26 | Coal chemical industry gasification filter cake recycling system |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202020649016.6U CN212018170U (en) | 2020-04-26 | 2020-04-26 | Coal chemical industry gasification filter cake recycling system |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN212018170U true CN212018170U (en) | 2020-11-27 |
Family
ID=73497037
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202020649016.6U Active CN212018170U (en) | 2020-04-26 | 2020-04-26 | Coal chemical industry gasification filter cake recycling system |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN212018170U (en) |
-
2020
- 2020-04-26 CN CN202020649016.6U patent/CN212018170U/en active Active
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN1322934C (en) | Collophanite direct flotation and reverse flotation technique | |
| CN106047426B (en) | A kind of method that low grey low-sulfur water-coal-slurry is prepared using coal slime | |
| CN105524669B (en) | Coal gasification fine slag sorts and the method for reuse | |
| CN102085526B (en) | Recycling method of blast furnace dust generated in steel making industry | |
| CN107303539A (en) | A kind of floatation process of coal gasification fine slag | |
| CN102029220A (en) | Separating flotation method of low-grade complex lead-antimony-zinc | |
| CN213350162U (en) | Fine sediment recycle system of coal slurry gasification | |
| CN102744146A (en) | Ore-dressing method for low-grade bauxite | |
| CN107057787A (en) | The method that coal conversion waste water cascade utilization prepares fuel slurry | |
| CN110422975A (en) | Oily waste hot wash-fine slag high-value-use integrated technique based on gasification Heisui River | |
| CN102851414A (en) | Treatment technique of blast furnace fly ash | |
| CN100562368C (en) | Oxygen-sulfur paragenesis zinc mine flotation method | |
| CN205851092U (en) | The secondary recovery system of coal in a kind of texaco gasification lime-ash | |
| CN101067100B (en) | Clean green fuel and its preparation process | |
| CN111408473A (en) | Coal chemical gasification filter cake recycling system and method | |
| CN212018170U (en) | Coal chemical industry gasification filter cake recycling system | |
| CN112916582B (en) | Gasification fly ash decarbonization method by combined flotation of mechanical activation and compound reagent | |
| CN102500472A (en) | Concentrating, filtering and dehydrating process for flotation clean coal | |
| CN111389597B (en) | Polar mixed reagent for low-rank coal flotation and flotation process | |
| CN104841563A (en) | Multistage foam floatation method of titanium chloride slags | |
| CN114749269B (en) | Full-size recycling process for gasified fine slag of coal water slurry | |
| CN106635208B (en) | The technique that a kind of coal preparation plant's thickener underflow directly prepares water-coal-slurry | |
| CN110790469A (en) | Process and device for improving pressure filtration performance of tail coal slime by coal gasification fine slag | |
| CN111659707B (en) | Gasification fine slag carbon-ash separation and high-carbon product dehydration integrated device and method | |
| CN102674720B (en) | Preparation technology for extracting carbon powder, iron core powder, primary pulverized fuel ash and secondary pulverized fuel ash from pulverized fuel ash |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| GR01 | Patent grant | ||
| GR01 | Patent grant |