CN103693676A - Waste mercury catalyst recovery technology and waste mercury catalyst recovery device - Google Patents
Waste mercury catalyst recovery technology and waste mercury catalyst recovery device Download PDFInfo
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- CN103693676A CN103693676A CN201310671649.1A CN201310671649A CN103693676A CN 103693676 A CN103693676 A CN 103693676A CN 201310671649 A CN201310671649 A CN 201310671649A CN 103693676 A CN103693676 A CN 103693676A
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- QSHDDOUJBYECFT-UHFFFAOYSA-N mercury Chemical compound [Hg] QSHDDOUJBYECFT-UHFFFAOYSA-N 0.000 title claims abstract description 39
- 229910052753 mercury Inorganic materials 0.000 title claims abstract description 38
- 239000003054 catalyst Substances 0.000 title claims abstract description 35
- 238000011084 recovery Methods 0.000 title claims abstract description 33
- 239000002699 waste material Substances 0.000 title abstract description 9
- 238000005516 engineering process Methods 0.000 title abstract description 7
- 239000007789 gas Substances 0.000 claims abstract description 59
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims abstract description 31
- LWJROJCJINYWOX-UHFFFAOYSA-L mercury dichloride Chemical compound Cl[Hg]Cl LWJROJCJINYWOX-UHFFFAOYSA-L 0.000 claims abstract description 14
- 229960002523 mercuric chloride Drugs 0.000 claims abstract description 13
- 229910052757 nitrogen Inorganic materials 0.000 claims abstract description 13
- 238000001816 cooling Methods 0.000 claims abstract description 9
- 238000010438 heat treatment Methods 0.000 claims abstract description 9
- 239000000843 powder Substances 0.000 claims abstract description 6
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 76
- 238000001179 sorption measurement Methods 0.000 claims description 52
- 239000007788 liquid Substances 0.000 claims description 42
- RCTYPNKXASFOBE-UHFFFAOYSA-M chloromercury Chemical compound [Hg]Cl RCTYPNKXASFOBE-UHFFFAOYSA-M 0.000 claims description 33
- 239000003610 charcoal Substances 0.000 claims description 32
- 239000002250 absorbent Substances 0.000 claims description 31
- 230000002745 absorbent Effects 0.000 claims description 31
- 238000005406 washing Methods 0.000 claims description 31
- 229920000742 Cotton Polymers 0.000 claims description 22
- 239000003518 caustics Substances 0.000 claims description 22
- ZHPNWZCWUUJAJC-UHFFFAOYSA-N fluorosilicon Chemical compound [Si]F ZHPNWZCWUUJAJC-UHFFFAOYSA-N 0.000 claims description 21
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 claims description 15
- 238000011067 equilibration Methods 0.000 claims description 10
- 229910001873 dinitrogen Inorganic materials 0.000 claims description 5
- VEXZGXHMUGYJMC-UHFFFAOYSA-M Chloride anion Chemical compound [Cl-] VEXZGXHMUGYJMC-UHFFFAOYSA-M 0.000 claims description 4
- 239000002826 coolant Substances 0.000 claims description 4
- 230000000694 effects Effects 0.000 claims description 4
- 239000003513 alkali Substances 0.000 claims description 3
- 239000000779 smoke Substances 0.000 claims description 3
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 abstract description 10
- 238000000197 pyrolysis Methods 0.000 abstract description 6
- 238000009835 boiling Methods 0.000 abstract description 4
- 239000002351 wastewater Substances 0.000 abstract description 4
- 238000004939 coking Methods 0.000 abstract description 3
- 239000011261 inert gas Substances 0.000 abstract description 2
- 230000003647 oxidation Effects 0.000 abstract description 2
- 238000007254 oxidation reaction Methods 0.000 abstract description 2
- 238000010792 warming Methods 0.000 abstract 1
- 238000000034 method Methods 0.000 description 14
- 238000007789 sealing Methods 0.000 description 5
- 238000004519 manufacturing process Methods 0.000 description 3
- 238000012913 prioritisation Methods 0.000 description 3
- 238000002156 mixing Methods 0.000 description 2
- 239000002244 precipitate Substances 0.000 description 2
- 239000002912 waste gas Substances 0.000 description 2
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 description 1
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 description 1
- 239000002253 acid Substances 0.000 description 1
- 230000003139 buffering effect Effects 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 239000000460 chlorine Substances 0.000 description 1
- 229910052801 chlorine Inorganic materials 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 238000004090 dissolution Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
- 238000001704 evaporation Methods 0.000 description 1
- 230000008020 evaporation Effects 0.000 description 1
- IXCSERBJSXMMFS-UHFFFAOYSA-N hydrogen chloride Substances Cl.Cl IXCSERBJSXMMFS-UHFFFAOYSA-N 0.000 description 1
- 229910000041 hydrogen chloride Inorganic materials 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 230000002269 spontaneous effect Effects 0.000 description 1
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Abstract
The invention discloses a waste mercury catalyst mercuric chloride recovery technology. The technology comprises the following steps: putting a waste mercuric chloride catalyst of which the mercury content is 2.5-4% into a dry distillation furnace; introducing nitrogen from the bottom of the dry distillation furnace; swapping out air inside the dry distillation furnace, and then controlling the pressure inside the dry distillation furnace at -0.09 to 0MPa; heating and warming the dry distillation furnace to reach the temperature being 500-600 DEG C so as to obtain recycled activated carbon, and a mixed gas containing mercuric chloride and nitrogen; introducing the mixed gas into a cooler; cooling to obtain mercuric chloride powder. Oxidation of the activated carbon by an inert gas is protected and avoided by adopting the principle that the boiling point of the mercuric chloride is lower than the coking temperature of the activated carbon; simultaneous recovery of the HgCl2 and the activated carbon is achieved under a negative-pressure closed environment; the recovery rate of mercuric chloride can be up to 70%; the overall recovery technology is a closed circulating technology; closed circulation of a waste residue, an exhaust gas and a wastewater can be achieved; the pollution to the environment is avoided.
Description
Technical field
The present invention relates to a kind of useless mercury catalyst, specifically, relate to a kind of useless mercury catalyst recovery process and device, belong to useless mercury catalyst and reclaim mercury chloride production technical field.
Background technology
At present, useless mercury catalyst reclaims the first boiling together with liming of mercury catalyst of normally giving up, and makes mercury chloride be converted into red precipitate, then makes red precipitate become Elemental Mercury through high temperature, and this kind of method rate of recovery is low, only has the rate of recovery of 57% left and right.Because adopting a day way of recycling for pot ground kitchen range, environmental pollution is serious.Method in CN201210467481.8 patent is in to the process of mercurous refuse heating, to pass into chlorine reaction to reclaim mercury and mercury chloride, and last gas from dry distillation tail causes mercury-containing waste water after processing again.CN201210484615.7 patent can realize the recovery of mercury chloride and the recovery of gac, and the rate of recovery is high.But this technique adds the isolated electrically heated of thermal recovery, cause technique power consumption high, be unfavorable for low-carbon environment-friendly.
In realizing process of the present invention, contriver finds at least to exist in prior art following problem: the rate of recovery is low, seriously polluted.
Summary of the invention
The problem to be solved in the present invention is for above deficiency, a kind of useless mercury catalyst recovery process is provided, overcome that the existing recovery process rate of recovery is low, the defect of contaminate environment, the present invention adopts sealing and circulating technique, can reach waste residue, waste gas, waste water sealing and circulating, have advantages of that the rate of recovery is high, environmental nonpollution.
Another object of the present invention is to provide a kind of device of realizing useless mercury catalyst recovery process.
For overcoming the above problems, the present invention by the following technical solutions: a kind of useless mercury catalyst mercury chloride recovery process, is characterized in that: described recovery process comprises the following steps:
Useless mercuric chloride catalyst by mercury content at 2.5-4% is placed in gas retort, from the bottom of gas retort, passes into nitrogen, displaces the air in gas retort, then by the pressure-controlling in gas retort at-0.09-0MPa;
By gas retort heat temperature raising, temperature is 500-600 ℃, is recycled the mixed gas of gac and chloride containing mercury, nitrogen;
Mixed gas enters water cooler, the cooling mercury chloride powder that obtains.
A prioritization scheme, described recovery process is further comprising the steps of:
Mixed gas enters the cooling residual exhaust that also obtains of water cooler;
Residual exhaust enters water washing tank and washs, then enters caustic treater and neutralize; Then enter the cotton adsorption tanks of fluorosilicon oil and remove water smoke, then through the cotton adsorption tanks of fluorosilicon oil, enter one-level absorbent charcoal adsorption tank and adsorb, then under the effect of vacuum pump, enter secondary absorbent charcoal adsorption tank and adsorb, obtain circulating nitrogen gas.
Another kind of prioritization scheme, described gas retort type of heating is to utilize hotblast stove that Hot-blast Heating is provided, and by fan, hot blast is transported in gas retort, and useless mercury catalyst is heated.
Another prioritization scheme, in described water cooler, the temperature of water coolant is 60-80 ℃;
The temperature 30-40 ℃ of described water washing tank;
In described caustic treater, fill sodium hydroxide solution, the liquid level 30-50% of alkali lye, temperature 20-30 ℃.
Based on above useless mercury catalyst recovery process, the invention provides a kind of useless mercury catalyst retrieving arrangement, comprise the cotton adsorption tanks of gas retort, water cooler, water washing tank, caustic treater, fluorosilicon oil, one-level absorbent charcoal adsorption tank, secondary absorbent charcoal adsorption tank and the vacuum pump of connection.
Described gas retort, is provided with opening for feed and escape pipe, and opening for feed is used for inputting useless mercuric chloride catalyst, and the bottom of gas retort is provided with nitrogen inlet;
Described water cooler, has inlet pipe and escape pipe, and inlet pipe is communicated with the escape pipe of gas retort, is jacketed type double-layer structure, and heat-eliminating medium passes through from chuck, and the bottom of water cooler is provided with relief outlet;
Described water washing tank, has inlet pipe, escape pipe and liquid adding bottle, and inlet pipe is communicated with the escape pipe of water cooler, and inlet pipe is deep in liquid, and liquid adding bottle is for liquid feeding;
Described caustic treater, has inlet pipe, escape pipe, and inlet pipe is communicated with the escape pipe of water washing tank, and inlet pipe is deep in liquid;
The cotton adsorption tanks of described fluorosilicon oil, for being provided with the adsorption tanks of fluorosilicon oil cotton, have inlet pipe, escape pipe, and inlet pipe is communicated with the escape pipe of caustic treater;
Described one-level absorbent charcoal adsorption tank, has inlet pipe, escape pipe, and inlet pipe is communicated with the escape pipe of the cotton adsorption tanks of fluorosilicon oil;
Described secondary absorbent charcoal adsorption tank, has inlet pipe, escape pipe, and inlet pipe is communicated with the escape pipe of one-level absorbent charcoal adsorption tank;
Described vacuum pump, is arranged between the escape pipe of one-level absorbent charcoal adsorption tank and the inlet pipe of secondary absorbent charcoal adsorption tank.
Further, the quantity of described water cooler is two.
Further, the bottom of described water cooler is provided with dissolving tank, and the relief outlet of water cooler is deep in dissolving tank.
Further, the liquid level 30-45% in described water washing tank.
Further, on described water washing tank, be communicated with equilibration tube, connectivity part is concordant with the liquid level in water washing tank, and equilibration tube is communicated with liquid collecting tank, and liquid collecting tank is communicated with collecting tank, and the bottom of water washing tank is communicated with liquid collecting tank.
Further, the liquid level 30-50% in described caustic treater, the bottom of caustic treater is communicated with collecting tank.The present invention adopts above technical scheme, compared with prior art, has the following advantages: utilize mercury chloride
The low principle of boiling point specific activity charcoal coking temperature, adopt protection of inert gas to avoid the oxidation of gac, under negative pressure closed environment, realized HgCl
2in the time of with gac, reclaim.Not only can reclaim mercury chloride and gac simultaneously, realize comprehensive utilization of resources, also can effectively avoid the loss of mercury in removal process, make the rate of recovery of mercury chloride reach 70%.And whole recovery process is sealing and circulating technique entirely, can reach waste residue, waste gas, waste water sealing and circulating, environmentally safe.This process using coal direct heating, thermo-efficiency utilization ratio is high, consumes energy low.This process tail gas is processed the chloride containing mercury solution produce and is not had other materials, reaches the production that can be directly used in mercuric chloride catalyst after concentration.The mercury chloride simultaneously reclaiming in this technology and gac can be applied again and produce, and have realized the recycle of mercury chloride; Improved the organic efficiency of mercury chloride.
Below in conjunction with drawings and Examples, the invention will be further described.
Accompanying drawing explanation
Accompanying drawing 1 is the schema of useless mercury catalyst mercury chloride recovery process in the embodiment of the present invention;
In figure,
1-gas retort, 2-water cooler, 3-water washing tank, 4-caustic treater, the cotton adsorber of 5-fluorosilicon oil, 6-one-level absorbent charcoal adsorption tank, 7-secondary absorbent charcoal adsorption tank, 8-equilibration tube, 9-liquid collecting tank, 10-collecting tank, 11-dissolving tank, 12-vacuum pump, 13-surge tank.
Embodiment
Below the preferred embodiments of the present invention are described, should be appreciated that preferred embodiment described herein, only for description and interpretation the present invention, is not intended to limit the present invention.Except as otherwise noted, the percentage ratio adopting in the present invention is percent by volume.
Embodiment, as shown in Figure 1, a useless mercury catalyst mercury chloride retrieving arrangement, comprises the cotton adsorption tanks 5 of gas retort 1, water cooler 2, water washing tank 3, caustic treater 4, fluorosilicon oil, one-level absorbent charcoal adsorption tank 6, secondary absorbent charcoal adsorption tank 7, equilibration tube 8, liquid collecting tank 9, collecting tank 10, dissolving tank 11, vacuum pump 12 and the surge tank 13 of connection.
The cotton adsorption tanks 5 of fluorosilicon oil, for being provided with the adsorption tanks of fluorosilicon oil cotton, have inlet pipe, escape pipe, and inlet pipe is arranged on the middle part of the cotton adsorption tanks 5 of fluorosilicon oil, and inlet pipe is communicated with the escape pipe of caustic treater 4.
One-level absorbent charcoal adsorption tank 6, has inlet pipe, escape pipe, and inlet pipe is communicated with the escape pipe of the cotton adsorption tanks 5 of fluorosilicon oil.
Secondary absorbent charcoal adsorption tank 7, has inlet pipe, escape pipe, and inlet pipe is communicated with the escape pipe of one-level absorbent charcoal adsorption tank 6.
The inlet pipe of secondary absorbent charcoal adsorption tank 7 is also communicated with surge tank 13, the buffering when going workshop steeping tank to do pneumatic blending.
More than the flow process of useless mercury catalyst mercury chloride retrieving arrangement is:
Useless mercuric chloride catalyst by mercury content in 2.5-4% left and right is placed in gas retort 1, first from the bottom of gas retort 1, pass into nitrogen, displace the air in gas retort 1, utilize vacuum pump to be pumped into micro-negative pressure, make mercury chloride gas and nitrogen sealing and circulating circulation under micro-vacuum state in gas retort 1;
It is cooling that mixed gas enters two groups of water coolers 2, also can adopt one group herein, cooling performance is poor, adopt three groups of water coolers also passable, but can cause, waste energy, water cooler 2 is jacketed type double-layer structure, mixed gas passes through from the centre of water cooler 2, water coolant passes through from chuck, and the temperature of water coolant is 60-80 ℃, cooling mercury chloride powder and the residual exhaust obtaining, mercury chloride powder is collected from water cooler 2 bottoms, water cooler 2 bottoms can be connected with dissolving tank 11, in dissolving tank 11, fill acid solution, dissolve cooled mercury chloride powder.
Residual exhaust enters water washing tank 3 and washs, and the temperature 30-40 ℃ of water washing tank 3 dissolves the micro-HgCl wherein carrying secretly
2; On water washing tank 3, be communicated with equilibration tube 8, connectivity part is apart from the bottom 35% of water washing tank 3, also can 30-45%; Equilibration tube 8, for the liquid level in equilibrium water cleaning of evaporator 3, prevents that water level is too high, and liquid collecting tank 9 is temporarily stored in liquid collecting tank 9 while reaching 6% for the water dissolution mercury chloride content in water washing tank 3, after liquid collecting tank 9 is full, is stored in collecting tank 10.
Tail gas enters caustic treater 4 again and neutralizes, and in caustic treater 4, fills sodium hydroxide solution, removes the hydrogen chloride gas in tail gas, the liquid level 30-50% of alkali lye, temperature 20-30 ℃.
Tail gas enters the cotton adsorption tanks 5 of fluorosilicon oil again and removes water smoke, and the cotton adsorption tanks 5 of fluorosilicon oil are for being provided with the adsorption tanks of fluorosilicon oil cotton, now in tail gas moisture content in 500ppm left and right.
Tail gas enters one-level absorbent charcoal adsorption tank 6 and adsorbs from the cotton adsorption tanks 5 of fluorosilicon oil are processed, and tail gas enters secondary absorbent charcoal adsorption tank 7 under the effect of vacuum pump 12, obtains circulating nitrogen gas; In circulating nitrogen gas, mercury chloride content is less than 10ppm, 25 ℃ of temperature, and moisture content is less than 10ppm, turns back to vertical dry furnace 1 and recycles, and forms and closes circulation, be controlled at-0.09--0MPa of system pressure.
For removing the air that enters gas retort 1 system in reinforced discharging process, need nitrogen replacement, the tail gas displacing goes steeping tank to do pneumatic blending to use directly delivering to production process by vacuum pump after one-level absorbent charcoal adsorption tank 6.
In the equipment of a whole set of flow process, by using nitrogen gas to seal off circulation, the mercury chloride gas of evaporation is formed to power-assisted circulation, and intrasystem air is suppressed, prevent gac spontaneous combustion under high temperature.
Above equipment is commercially available known equipment at present.
Finally it should be noted that: the foregoing is only the preferred embodiments of the present invention, be not limited to the present invention, although the present invention is had been described in detail with reference to previous embodiment, for a person skilled in the art, its technical scheme that still can record aforementioned each embodiment is modified, or part technical characterictic is wherein equal to replacement.Within the spirit and principles in the present invention all, any modification of doing, be equal to replacement, improvement etc., within all should being included in protection scope of the present invention.
Claims (10)
1. a useless mercury catalyst mercury chloride recovery process, is characterized in that: described recovery process comprises the following steps:
Useless mercuric chloride catalyst by mercury content at 2.5-4% is placed in gas retort (1), from the bottom of gas retort (1), passes into nitrogen, displaces the air in gas retort (1), then by the pressure-controlling in gas retort (1) at-0.09-0MPa;
By gas retort (1) heat temperature raising, temperature is 500-600 ℃, is recycled the mixed gas of gac and chloride containing mercury, nitrogen;
Mixed gas enters water cooler (2), the cooling mercury chloride powder that obtains.
2. recovery process as claimed in claim 1, is characterized in that: described recovery process is further comprising the steps of:
Mixed gas enters the cooling residual exhaust that also obtains of water cooler (2);
Residual exhaust enters water washing tank (3) and washs, then enters caustic treater (4) and neutralize; Then enter the cotton adsorption tanks of fluorosilicon oil (5) and remove water smoke, through the cotton adsorption tanks of fluorosilicon oil (5), entering one-level absorbent charcoal adsorption tank (6) again adsorbs, under the effect of vacuum pump (12), enter again secondary absorbent charcoal adsorption tank (7) and adsorb, obtain circulating nitrogen gas.
3. recovery process as claimed in claim 1, is characterized in that: described gas retort (1) type of heating is to utilize hotblast stove that Hot-blast Heating is provided, and by fan, hot blast is transported in gas retort (1), and useless mercury catalyst is heated.
4. recovery process as claimed in claim 1, is characterized in that: in described water cooler (2), the temperature of water coolant is 60-80 ℃;
The temperature 30-40 ℃ of described water washing tank (3);
Described caustic treater fills sodium hydroxide solution in (4), the liquid level 30-50% of alkali lye, temperature 20-30 ℃.
5. as the useless mercury catalyst mercury chloride retrieving arrangement of claim 1-4 as described in one of them, it is characterized in that: described retrieving arrangement comprises the cotton adsorption tanks (5) of gas retort (1), water cooler (2), water washing tank (3), caustic treater (4), fluorosilicon oil, one-level absorbent charcoal adsorption tank (6), secondary absorbent charcoal adsorption tank (7) of connection and very
Empty pump (12);
Described gas retort (1), is provided with opening for feed and escape pipe, and opening for feed is used for inputting useless mercuric chloride catalyst, and the bottom of gas retort (1) is provided with nitrogen inlet;
Described water cooler (2), has inlet pipe and escape pipe, and inlet pipe is communicated with the escape pipe of gas retort (1), is jacketed type double-layer structure, and heat-eliminating medium passes through from chuck, and the bottom of water cooler (2) is provided with relief outlet;
Described water washing tank (3), has inlet pipe, escape pipe and liquid adding bottle, and inlet pipe is communicated with the escape pipe of water cooler (2), and inlet pipe is deep in liquid, and liquid adding bottle is for liquid feeding;
Described caustic treater (4), has inlet pipe, escape pipe, and inlet pipe is communicated with the escape pipe of water washing tank (3), and inlet pipe is deep in liquid;
The cotton adsorption tanks (5) of described fluorosilicon oil, for being provided with the adsorption tanks of fluorosilicon oil cotton, have inlet pipe, escape pipe, and inlet pipe is communicated with the escape pipe of caustic treater (4);
Described one-level absorbent charcoal adsorption tank (6), has inlet pipe, escape pipe, and inlet pipe is communicated with the escape pipe of the cotton adsorption tanks of fluorosilicon oil (5);
Described secondary absorbent charcoal adsorption tank (7), has inlet pipe, escape pipe, and inlet pipe is communicated with the escape pipe of one-level absorbent charcoal adsorption tank (6);
Described vacuum pump (12), is arranged between the escape pipe of one-level absorbent charcoal adsorption tank (6) and the inlet pipe of secondary absorbent charcoal adsorption tank (7).
6. useless mercury catalyst mercury chloride retrieving arrangement as claimed in claim 5, is characterized in that: the quantity of described water cooler (2) is two.
7. useless mercury catalyst mercury chloride retrieving arrangement as claimed in claim 6, is characterized in that: the bottom of described water cooler (2) is provided with dissolving tank (11), and the relief outlet of water cooler (2) is deep in dissolving tank (11).
8. useless mercury catalyst mercury chloride retrieving arrangement as claimed in claim 7, is characterized in that: the liquid level 30-45% in described water washing tank (3).
9. useless mercury catalyst mercury chloride retrieving arrangement as claimed in claim 8, it is characterized in that: on described water washing tank (3), be communicated with equilibration tube (8), connectivity part is concordant with the liquid level in water washing tank (3), equilibration tube (8) is communicated with liquid collecting tank (9), liquid collecting tank (9) is communicated with collecting tank (10), and the bottom of water washing tank (3) is communicated with liquid collecting tank (9).
10. useless mercury catalyst mercury chloride retrieving arrangement as claimed in claim 9, is characterized in that: the liquid level 30-50% in described caustic treater (4), the bottom of caustic treater (4) is communicated with collecting tank (10).
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| CN201310671649.1A CN103693676B (en) | 2013-12-12 | 2013-12-12 | Waste mercury catalyst recovery technology and waste mercury catalyst recovery device |
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| CN201310671649.1A CN103693676B (en) | 2013-12-12 | 2013-12-12 | Waste mercury catalyst recovery technology and waste mercury catalyst recovery device |
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| CN104197692A (en) * | 2014-08-04 | 2014-12-10 | 贵州省万山银河化工有限责任公司 | Drying system and method for mercury catalyst production tail gas recycling |
| CN104451204A (en) * | 2013-09-25 | 2015-03-25 | 新疆天业（集团）有限公司 | Mercury recovering and dry distillation device for waste mercury catalyst |
| CN104451154A (en) * | 2014-11-14 | 2015-03-25 | 北京化工大学 | New technology for recovering mercury in mercury-containing catalyst by wet method |
| CN105148896A (en) * | 2015-08-03 | 2015-12-16 | 贵州蓝天固废处置有限公司 | Method for recycling activated carbon in waste mercury catalyst |
| CN107344100A (en) * | 2016-05-06 | 2017-11-14 | 北京华宇同方化工科技开发有限公司 | One kind inactivation HgCl2The renovation process of/AC catalyst |
| CN108545741A (en) * | 2018-05-10 | 2018-09-18 | 张良儒 | Useless mercury catalyst high efficiente callback technique and device |
| CN108624756A (en) * | 2018-04-28 | 2018-10-09 | 张良儒 | A kind of recovery process of the useless mercury catalyst of low-consumption high-efficiency |
| CN109536743A (en) * | 2018-12-15 | 2019-03-29 | 山东科技大学 | A kind of pulse hoisting type mill tailings continuously recycles the system and technique of mercury |
| CN114653387A (en) * | 2022-04-12 | 2022-06-24 | 内蒙古圣龙大地科技有限公司 | Mercury-free catalyst for producing and synthesizing chloroethylene by using noble metal |
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