CN205269648U - Hydrolysis reaction cauldron - Google Patents

Hydrolysis reaction cauldron Download PDF

Info

Publication number
CN205269648U
CN205269648U CN201521051918.5U CN201521051918U CN205269648U CN 205269648 U CN205269648 U CN 205269648U CN 201521051918 U CN201521051918 U CN 201521051918U CN 205269648 U CN205269648 U CN 205269648U
Authority
CN
China
Prior art keywords
reaction pot
hydrolytic reaction
main body
screen plate
agitator
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.)
Expired - Fee Related
Application number
CN201521051918.5U
Other languages
Chinese (zh)
Inventor
黄丽明
王洪明
杨广华
余立清
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Longyan Cercis Innovation Research Institute
Fujian Cercis Environment Project Co Ltd
Original Assignee
Longyan Cercis Innovation Research Institute
Fujian Cercis Environment Project Co Ltd
Priority date (The priority date 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 date listed.)
Filing date
Publication date
Application filed by Longyan Cercis Innovation Research Institute, Fujian Cercis Environment Project Co Ltd filed Critical Longyan Cercis Innovation Research Institute
Priority to CN201521051918.5U priority Critical patent/CN205269648U/en
Application granted granted Critical
Publication of CN205269648U publication Critical patent/CN205269648U/en
Expired - Fee Related legal-status Critical Current
Anticipated expiration legal-status Critical

Links

Classifications

    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/50—Improvements relating to the production of bulk chemicals
    • Y02P20/584—Recycling of catalysts

Landscapes

  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Processing Of Solid Wastes (AREA)
  • Engineering & Computer Science (AREA)
  • Materials Engineering (AREA)
  • Catalysts (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Environmental & Geological Engineering (AREA)
  • General Life Sciences & Earth Sciences (AREA)
  • Geology (AREA)
  • Inorganic Chemistry (AREA)

Abstract

The utility model discloses a hydrolysis reaction cauldron, hydrolysis reaction cauldron includes charge door, filling opening, discharge opening, agitating unit and main part, and charge door and filling opening are located the upper portion region of main part, and the discharge opening is located the lower region of main part, and agitating unit is located the middle part region of main part, agitating unit includes (mixing) shaft, agitator and cross wedge head, and cross wedge head is located the agitator bottom, the (mixing) shaft can drive the agitator and rotate, also can drive the agitator and reciprocate. The utility model discloses a hydrolysis reaction cauldron simple structure, convenient operation.

Description

A kind of hydrolytic reaction pot
Technical field
This utility model belongs to discarded SCR denitration and reclaims field, is specifically related to a kind of hydrolytic reaction pot.
Background technology
Nitrogen oxides (NOx) it is one of the main component of atmosphere pollution, such material can cause the serious environmental problems such as acid rain, endangers human health simultaneously. In numerous denitration technologies, selective catalytic reduction (SCR) is commercial Application technology the most widely, has the features such as efficient, ripe. Along with the development of Denitration Industry, create a large amount of SCR catalyst lost efficacy or discard. Pollutant also serious harm natural environment and the human healths such as such material belongs to dangerous solid waste, and arbitrarily discarded banking up does not only take up a large amount of soil, heavy metal therein.
Most commonly seen commercial SCR denitration is vanadium tungsten titanium-type, and wherein metal-oxide constitutes about 90%. Its garbage being carried out comprehensive reutilization, can not only effectively solve potential environmental problem, reclaiming the metal-oxide obtained can also recycle, and produces good environmental benefit and economic benefit.
At present, substantially high-temperature sodium (calcium) is all adopted to change roasting technique the Comprehensive Recovery Technology of discarded SCR denitration, such as, in the documents such as CN201510083924.7, CN201410534406.8, CN201410084859.5 disclosed, the energy consumption of this technique is high and complex process. Document CN201410471988.X have employed a kind of brand-new V2O5Recovery process, namely in acid condition with reducing agent by V5+It is reduced into water miscible V4+, thus other compositions of vanadium and catalyst are separated, again by V after separation4+Aoxidize back V5+, regulate pH and make its hydrolytic precipitation be reclaimed. This technique response rate is higher, but vanadium experienced by reduction and the reciprocal process of oxidation, slightly complicated.
It would therefore be highly desirable to development technology program is simpler, the response rate high, do not cause secondary pollution, cost of investment low and meet the novel recovery technology of industrial process conditions.
Utility model content
This utility model is for the problem of above discarded SCR denitration recovery technology, it is provided that a kind of simple in construction, easy to operate hydrolytic reaction pot.
For achieving the above object, this utility model provides following technical scheme:
A kind of hydrolytic reaction pot, described hydrolytic reaction pot includes charge door, filling opening, discharge port, agitating device and main body, charge door and filling opening and is positioned at the upper area of main body, and discharge port is positioned at the lower area of main body, and agitating device is positioned at the central region of main body; Described agitating device includes shaft, agitator and cross sphenocephaly, and cross sphenocephaly is positioned at stirrer bottom, and described shaft can drive agitator to rotate, it is also possible to drive agitator to move up and down; Described hydrolytic reaction pot also includes screen plate, and this screen plate is positioned at the lower area of described main body.
Further, described screen plate is divided into upper and lower two-layer, lower floor's screen plate is fixed on inside main body, upper level filter plate is rotatable, every layer of screen plate is equipped with filtering holes, the center of upper level filter plate connects a pivot protrusion, described pivot protrusion has cross recess, coordinate with described cross sphenocephaly.
Further, a metafiltration cloth it is provided with between upper and lower two-layer screen plate.
Further, described hydrolytic reaction pot lower area is additionally provided with vacuum port, for accelerated filtration.
Further, described hydrolytic reaction pot also includes chuck, and this chuck covers the region, middle and lower part of main body.
Further, described hydrolytic reaction pot also includes overfall, and this overfall is positioned at the upper area of main body.
Further, described hydrolytic reaction pot also includes bearing, and bearing is arranged on outside chuck, in order to supportive body.
Further, described hydrolytic reaction pot also includes interior cooling coil.
Further, this interior cooling coil is circumferentially positioned at the inner surface of this main body, extends to central region from the upper area of hydrolytic reaction pot main body.
The beneficial effects of the utility model are as follows:
1. simple in construction, it is simple to operation: hydrolytic reaction pot of the present utility model has easy hydrolyzable moiety and filtration fraction, can realize hydrolysis simultaneously easily and filter;
2. effectively save cost, space: simultaneously realize hydrolysis and filter can save independent defecator (such as suction filtration tank) cost and take up an area space;
3. this utility model is by arranging interior cooling coil at inner surface, it is achieved the quick cooling of described reactor.
Accompanying drawing explanation
Fig. 1 is discarded SCR denitration comprehensive recycling process flow chart.
Fig. 2 is the schematic diagram of discarded SCR denitration comprehensive recovery system.
Fig. 3 is the structure chart of acidleach oxidizing reactor.
Fig. 4 is the structure chart of hydrolytic reaction pot.
Fig. 5 is the structure chart of the screen plate in hydrolytic reaction pot.
Wherein, 1 charge door, 2 blow vents, 3 chucks, 4 bearings, 5 agitators, 6 discharge ports, 7 filling openings, 8 overfalls, 9 main bodys; 10 shafts, 11 charge doors, cooling coil in 12,13 chucks, 14 bearings, 15 pivot protrusion, 16 vacuum ports, 17 filling openings, 18 overfalls, 19 agitators, 20 cross sphenocephalys, 21 screen plates, 22 discharge ports; 23 screen plates, 24 filter clothes, 25 filtering holes, 26 cross recess
Detailed description of the invention
Below by way of detailed description of the invention, the utility model is described in further detail, but this should not being interpreted as, scope of the present utility model is only limitted to Examples below. When without departing from this utility model said method thought, the various replacements made according to ordinary skill knowledge and customary means or change, should be included in scope of the present utility model.
Discarded SCR denitration described in this utility model refers to the non-renewable inactivation SCR denitration catalyst of formation such as causing sintering of catalyst, mechanical performance to reduce owing to long-lasting catalytic runs, structure is imperfect, the out of stock catalyst of SCR of inactivation again non-renewable after also including regeneration. " inactivation SCR denitration catalyst " refers to: SCR denitration is in running, due to catalyst dust stratification, active component passage and the reason such as active sites is poisoning, catalyst activity is gradually lowered, when its activity is reduced to the needs that cannot meet the out of stock system of SCR, just it is referred to as " inactivation SCR denitration catalyst ". Described SCR denitration refers to that utilizing selective catalytic reduction the nitrogen oxides catalysis in pending flue gas to be reduced is converted into N2Medium (catalyst) with innocuous substances such as water. Preferably, described SCR denitration is vanadium tungsten titanium-type SCR denitration, mainly comprises as V2O5-WO3/TiO2, wherein V2O5For active component, WO3For auxiliary agent, TiO2For carrier.
As mentioned above, a kind of method that the utility model discloses discarded SCR denitration comprehensive reutilization, adopt brand-new acidleach oxidation technology, the vanadium in discarded SCR denitration, titanium are converted into pentavalent vanadium and the titanyl sulfate of solubility, and reclaim WO3Rough; Pentavalent vanadium hydrolysis obtains vanadium crude product, it is achieved the initial gross separation of vanadium and titanium; Titanyl sulfate hydrolysis produces metatitanic acid precipitation, completes TiO through filtration washing drying and roasting2Reclaiming, the sulphuric acid of filtrate desalination concentration and recovery can recycle in step of acid dipping. This utility model reclaims efficiently, technique is simple and easy, cost is low, and recycling of spent acid not only solves waste water handling problem but also saved resource.
Below acidleach oxidizing reactor of the present utility model is described in detail, as it is shown on figure 3, acidleach oxidizing reactor of the present utility model includes charge door 1, blow vent 2, chuck 3, bearing 4, agitator 5, discharge port 6, filling opening 7, overfall 8 and main body 9. Wherein, the middle and lower part of chuck parcel main body 9, play heating and thermal insulation effect; Charge door 1 and filling opening 7 are positioned at the tip position of main body 9; Overfall 8 is positioned at the upper area of main body 9; Blow vent is arranged on the top of main body 9, blow vent place is sealedly connected with appendix, oxidant (such as oxygen or ozone) to be introduced directly into the lower section of agitator, pass through this setup, can ensure that chuck wraps up main body middle and lower part to greatest extent, thus improving the heating and thermal insulation effect of acidleach oxidizing reactor, and, oxidant is delivered directly to the lower section of agitator by appendix, can by oxidant quickly, evenly spread in reactor material, be effectively improved the reaction effect of acidleach oxidizing reactor; Agitator is positioned at body interior; Discharge port is arranged on the bottom of main body; Bearing 4 is positioned at the medium position of acidleach oxidizing reactor, it is preferable that be positioned at outside chuck, is used for supporting acidleach oxidizing reactor.
The compressed air soot blowing of described discarded SCR denitration and ultrasonic cleaning arsenic removal, hydrargyrum, after the pretreatment such as alkali metal salt, size-reduced device is crushed to 100��200 orders, communicated band and charge door 1 send into this acidleach oxidizing reactor, the sulphuric acid of existing 1��3 times of volume (volume relative to affiliated catalyst) added through filling opening 7 in described still, reactor heats through chuck 3 and is incubated down stirring and leads to oxidant through described blow vent 2, the vanadium in discarded SCR denitration and titanium is made to gradate as water miscible salt, it is drained in the first described filter tank through discharge port 6 after having reacted.
As shown in Figure 4, hydrolytic reaction pot of the present utility model includes charge door 11, chuck 13, bearing 14, pivot protrusion 15, filling opening 17, overfall 18, agitating device, screen plate 21 and discharge port 22, described agitating device includes shaft 10, agitator 19 and cross sphenocephaly 20, cross sphenocephaly 20 is positioned at bottom agitator 19, and described shaft 10 can drive agitator to rotate, it is also possible to drive agitator to move up and down. Aforesaid first hydrolytic reaction pot and the second hydrolytic reaction pot can all adopt this hydrolytic reaction pot, it is also possible to one of them adopts this hydrolytic reaction pot.
Only for ease of describing, hydrolytic reaction pot main body being divided into three regions of upper, middle and lower, the upper area of hydrolytic reaction pot main body is provided with charge door 11, filling opening 17, overfall 18, charge door 11 and filling opening 17 and is generally located on tip position; Chuck 13 covers the central region of hydrolytic reaction pot main body, is hydrolytic reaction pot main body heating and thermal insulation when hydrolysis; Bearing 14 is arranged on outside chuck 13, in order to support whole hydrolytic reaction pot; Agitating device is positioned at the central region of reactor main body, and the axis along reactor main body is arranged; The lower area of hydrolytic reaction pot main body is provided with discharge port 22.
Hydrolytic reaction pot lower area is additionally provided with vacuum port 16, for accelerated filtration.
As shown in Figure 5, the material of described screen plate 21 is 304 steel, it is divided into upper and lower two-layer, lower floor's screen plate is fixed on inside main body, and upper level filter plate is rotatable, and every layer of screen plate is equipped with filtering holes 25, the center of upper level filter plate 23 connects described pivot protrusion 15, described pivot protrusion has cross recess 26, it is possible to coordinate with described cross sphenocephaly 20, between upper and lower two-layer screen plate, have a metafiltration cloth 24.
During hydrolysis, cross sphenocephaly 20 separates with pivot protrusion 15, and the filtering holes of upper and lower two-layer screen plate seals, and adds alkali from filling opening and regulates material in reactor to hydrolysis pH, and the lower stirring of insulation then stops stirring insulation and stands; When filtering after being hydrolyzed, shaft 10 moves down, cross sphenocephaly 20 coordinates with cross recess 26, rotating shaft 10 drives upper level filter plate 23 to rotate, the filtering holes 25 making upper and lower two-layer screen plate is corresponding, then evacuating gas from vacuum port 16 makes reactor lower space form vacuum, and accelerated filtration, the material after having filtered enters next device through discharge port.
Second hydrolytic reaction pot also includes interior cooling coil 12, and interior cooling coil 12 is circumferentially positioned at the inner surface of this main body, extends to central region from the upper area of hydrolytic reaction pot main body; For realizing the quick cooling of described reactor.
As in figure 2 it is shown, the system of discarded SCR denitration comprehensive reutilization of the present utility model includes pretreatment unit, reducing mechanism, above-mentioned acidleach oxidizing reactor, first filter tank, the first above-mentioned hydrolytic reaction pot, the second above-mentioned hydrolytic reaction pot and vacuum evaporation groove; Wherein, preprocessed device pretreatment (includes compression air to purge and ultrasonic cleaning, wherein, purge and remove surface dust, clean remove surface adsorption thing such as arsenic, hydrargyrum, alkali metal salt etc.) after discarded SCR denitration through described reducing mechanism pulverize after, be transported to described acidleach oxidizing reactor by conveyer belt; After described acidleach oxidizing reactor processes, described treatment fluid enters described first filter tank by pipeline; The filtrate of described first filter tank is pipelined to described first hydrolytic reaction pot; After described first hydrolytic reaction pot processes, filtrate enters described second hydrolytic reaction pot by pipeline; After described second hydrolytic reaction pot processes, filtrate enters described vacuum evaporation groove by pipeline; After described vacuum evaporation groove processes, the sulphuric acid obtained enters described acidleach oxidizing reactor by pipeline, is circulated use.
Wherein, the work process of this system is as follows: discarded SCR denitration is preprocessed (to be included compression air to purge and ultrasonic cleaning, wherein, purge and remove surface dust, clean remove surface adsorption thing such as arsenic, hydrargyrum, alkali metal salt etc.) after in reducing mechanism pulverize, acidleach oxidizing reactor sent into by communicated band, reactor heating and thermal insulation, stirring logical oxidant, the vanadium in discarded SCR denitration and titanium is made to gradate as water miscible salt, it is then fed into the first filter tank (such as suction filtration tank), must containing filtrate I and WO of vanadium, titanium3Rough filter cake. Filtrate I is sent to the first hydrolytic reaction pot, adds alkali from filling opening and makes reactor pH be 1��2, insulation, stirring, then stop stirring insulation to stand, sucking filtration, obtains containing vanadium crude product (being mainly vanadium crude product precipitation, be also mixed with a small amount of metatitanic acid precipitation) and filtrate II simultaneously. Filtrate II is sent to the second hydrolytic reaction pot, add alkali and regulate pH to 6��8, and put into a small amount of crystal seed, stirring, heated and boiled stops agitating heating to graying point and stands, and again boils, quickly cooling, sucking filtration, obtains metatitanic acid precipitation and filtrate II I, and metatitanic acid precipitation is scrubbed, dry roasting obtains TiO2. Filtrate II I sends into the concentration of vacuum evaporation groove desalination and successively reclaims sulfate and sulphuric acid, and sulphuric acid returns in acidleach oxidizing reactor and recycles. The WO reclaimed3The most Zhongdao smelter of rough and vanadium crude product completes to refine.
Embodiment 1
As Figure 1-5, the method and apparatus that present embodiment discloses a kind of discarded SCR denitration comprehensive reutilization, carry out according to the following steps.
It is crushed to 120 orders after the discarded pretreatment such as the compressed air soot blowing of SCR denitration and ultrasonic cleaning arsenic removal, hydrargyrum, alkali metal salt, the communicated acidleach oxidizing reactor having 1.5 times of volumes (relative to catalyst volume), concentration to be 40g/L sulphuric acid with feeding, reactor stirs and logical O at keeping 80 DEG C2, make the vanadium in discarded SCR denitration and titanium gradate as water miscible salt, after 0.5 hour, send into suction filtration tank sucking filtration, must containing filtrate I and WO of vanadium, titanium3Rough filter cake. Filtrate I is sent to the first hydrolytic reaction pot, adds appropriate 20%NaOH from filling opening and makes reactor pH be 1.2, keeps stirring 1h with the speed of 100r/min under temperature 50 C, then stops stirring insulation and stands 30min, sucking filtration, obtains containing vanadium crude product and filtrate II. Filtrate II is sent to the second hydrolytic reaction pot, adds 20%NaOH and regulates pH to 6, and puts into a small amount of crystal seed (Detitanium-ore-type TiO2Its addition is 0.8%wt), it is kept stirring for speed 200r/min, heated and boiled stops agitating heating to graying point and stands 30min, again boil 2h, be quickly cooled to 40 DEG C, sucking filtration, obtaining metatitanic acid precipitation and filtrate III, metatitanic acid precipitation is scrubbed, at 600 DEG C, roasting 3h recovery obtains TiO after drying2. Filtrate III is sent into the concentration of vacuum evaporation groove desalination and is successively reclaimed Na2SO4And sulphuric acid, sulphuric acid returns in acidleach oxidizing reactor and recycles. The WO reclaimed3The most Zhongdao smelter of rough and vanadium crude product completes to refine.
This technique has quickly and efficiently reclaimed V in discarded SCR denitration2O5��TiO2And WO3, the response rate respectively 90.63%, 93.74%, 99.58%, wherein TiO2Purity is 99.51%.
Embodiment 2
As Figure 1-5, the method and apparatus that present embodiment discloses a kind of discarded SCR denitration comprehensive reutilization, carry out according to the following steps.
It is crushed to 150 orders after the discarded pretreatment such as the compressed air soot blowing of SCR denitration and ultrasonic cleaning arsenic removal, hydrargyrum, alkali metal salt, the communicated acidleach oxidizing reactor having 1.5 times of volumes (relative to catalyst volume), concentration to be 50g/L sulphuric acid with feeding, reactor stirs and logical O at keeping 90 DEG C2, make the vanadium in discarded SCR denitration and titanium gradate as water miscible salt, after 1h, send into suction filtration tank sucking filtration, must containing filtrate I and WO of vanadium, titanium3Rough filter cake. Filtrate I is sent to the first hydrolytic reaction pot, adds appropriate 20%NaOH from filling opening and makes reactor pH be 1.5, keeps stirring 1.5h with the speed of 150r/min under temperature 60 C, then stops stirring insulation and stands 60min, sucking filtration, obtains containing vanadium crude product and filtrate II. Filtrate II is sent to the second hydrolytic reaction pot, adds alkali and regulates pH to 7, and puts into a small amount of crystal seed (Detitanium-ore-type TiO2Its addition is 0.5%wt), it is kept stirring for speed 300r/min, heated and boiled stops agitating heating to graying point and stands 60min, again boil 3h, be quickly cooled to 50 DEG C, sucking filtration, obtaining metatitanic acid precipitation and filtrate III, metatitanic acid precipitation is scrubbed, at 550 DEG C, roasting 2h recovery obtains TiO after drying2. Filtrate III is sent into the concentration of vacuum evaporation groove desalination and is successively reclaimed Na2SO4And sulphuric acid, sulphuric acid returns in acidleach oxidizing reactor and recycles. The WO reclaimed3The most Zhongdao smelter of rough and vanadium crude product completes to refine.
This technique has quickly and efficiently reclaimed V in discarded SCR denitration2O5��TiO2And WO3, the response rate respectively 93.49%, 94.72%, 99.26%, wherein TiO2Purity is 99.18%.
Embodiment 3
As Figure 1-5, the method and apparatus that present embodiment discloses a kind of discarded SCR denitration comprehensive reutilization, carry out according to the following steps.
It is crushed to 180 orders after the discarded pretreatment such as the compressed air soot blowing of SCR denitration and ultrasonic cleaning arsenic removal, hydrargyrum, alkali metal salt, the communicated acidleach oxidizing reactor having 2 times of volumes (relative to catalyst volume), concentration to be 60g/L sulphuric acid with feeding, reactor stirs and logical O at keeping 85 DEG C2, make the vanadium in discarded SCR denitration and titanium gradate as water miscible salt, after 1.5h, send into suction filtration tank sucking filtration, must containing filtrate I and WO of vanadium, titanium3Rough filter cake. Filtrate I is sent to the first hydrolytic reaction pot, adds appropriate 20%NaOH from filling opening and makes reactor pH be 1.8, keeps stirring 2h with the speed of 200r/min under temperature 70 C, then stops stirring insulation and stands 90min, sucking filtration, obtains containing vanadium crude product and filtrate II. Filtrate II is sent to the second hydrolytic reaction pot, adds 20%NaOH and regulates pH to 8, and puts into a small amount of crystal seed (Detitanium-ore-type TiO2Its addition is 1%wt), it is kept stirring for speed 350r/min, heated and boiled stops agitating heating to graying point and stands 90min, again boil 4h, be quickly cooled to 60 DEG C, sucking filtration, obtaining metatitanic acid precipitation and filtrate III, metatitanic acid precipitation is scrubbed, at 500 DEG C, roasting 3h recovery obtains TiO after drying2. Filtrate III is sent into the concentration of vacuum evaporation groove desalination and is successively reclaimed Na2SO4And sulphuric acid, sulphuric acid returns in acidleach oxidizing reactor and recycles. The WO reclaimed3The most Zhongdao smelter of rough and vanadium crude product completes to refine.
This technique has quickly and efficiently reclaimed V in discarded SCR denitration2O5��TiO2And WO3, the response rate respectively 92.58%, 93.86%, 99.37%, wherein TiO2Purity is 99.27%.

Claims (9)

1. a hydrolytic reaction pot, it is characterized in that, described hydrolytic reaction pot includes charge door, filling opening, discharge port, agitating device and main body, charge door and filling opening and is positioned at the upper area of main body, discharge port is positioned at the lower area of main body, and agitating device is positioned at the central region of main body; Described agitating device includes shaft, agitator and cross sphenocephaly, and cross sphenocephaly is positioned at stirrer bottom, and described shaft can drive agitator to rotate, it is also possible to drive agitator to move up and down; Described hydrolytic reaction pot also includes screen plate, and this screen plate is positioned at the lower area of described main body.
2. hydrolytic reaction pot according to claim 1, it is characterised in that described screen plate is divided into upper and lower two-layer, and lower floor's screen plate is fixed on inside main body, upper level filter plate is rotatable, and every layer of screen plate is equipped with filtering holes; The center of upper level filter plate connects a pivot protrusion, described pivot protrusion has cross recess, coordinate with described cross sphenocephaly.
3. hydrolytic reaction pot according to claim 2, it is characterised in that be provided with a metafiltration cloth between two-layer screen plate up and down.
4. hydrolytic reaction pot according to claim 1, it is characterised in that described hydrolytic reaction pot lower area is additionally provided with vacuum port, for accelerated filtration.
5. hydrolytic reaction pot according to claim 1, it is characterised in that described hydrolytic reaction pot also includes chuck, this chuck covers the region, middle and lower part of main body.
6. hydrolytic reaction pot according to claim 1, it is characterised in that described hydrolytic reaction pot also includes overfall, this overfall is positioned at the upper area of main body.
7. hydrolytic reaction pot according to claim 5, it is characterised in that described hydrolytic reaction pot also includes bearing, bearing is arranged on outside chuck, in order to supportive body.
8. hydrolytic reaction pot according to claim 1, it is characterised in that described hydrolytic reaction pot also includes interior cooling coil.
9. hydrolytic reaction pot according to claim 8, it is characterised in that this interior cooling coil is circumferentially positioned at the inner surface of this main body, extends to central region from the upper area of hydrolytic reaction pot main body.
CN201521051918.5U 2015-09-11 2015-12-16 Hydrolysis reaction cauldron Expired - Fee Related CN205269648U (en)

Priority Applications (1)

Application Number Priority Date Filing Date Title
CN201521051918.5U CN205269648U (en) 2015-09-11 2015-12-16 Hydrolysis reaction cauldron

Applications Claiming Priority (3)

Application Number Priority Date Filing Date Title
CN201510577559 2015-09-11
CN2015105775595 2015-09-11
CN201521051918.5U CN205269648U (en) 2015-09-11 2015-12-16 Hydrolysis reaction cauldron

Publications (1)

Publication Number Publication Date
CN205269648U true CN205269648U (en) 2016-06-01

Family

ID=55816653

Family Applications (3)

Application Number Title Priority Date Filing Date
CN201521051918.5U Expired - Fee Related CN205269648U (en) 2015-09-11 2015-12-16 Hydrolysis reaction cauldron
CN201510943530.4A Expired - Fee Related CN105536817B (en) 2015-09-11 2015-12-16 A kind of method and system of discarded SCR denitration comprehensive reutilization
CN201521052158.XU Expired - Fee Related CN205269612U (en) 2015-09-11 2015-12-16 A acidleach oxidation reation kettle for $discarding SCR denitration catalyst comprehensive recovery utilization

Family Applications After (2)

Application Number Title Priority Date Filing Date
CN201510943530.4A Expired - Fee Related CN105536817B (en) 2015-09-11 2015-12-16 A kind of method and system of discarded SCR denitration comprehensive reutilization
CN201521052158.XU Expired - Fee Related CN205269612U (en) 2015-09-11 2015-12-16 A acidleach oxidation reation kettle for $discarding SCR denitration catalyst comprehensive recovery utilization

Country Status (1)

Country Link
CN (3) CN205269648U (en)

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN109939634A (en) * 2019-04-08 2019-06-28 南京威安新材料科技有限公司 Nanocatalyst industrial water solution device

Families Citing this family (10)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN106732206B (en) * 2016-11-11 2020-07-21 衢州信步化工科技有限公司 Intelligent reaction kettle and recycling method of hydrofluoric acid and hydrochloric acid mixed acid
CN109666795B (en) * 2017-10-17 2020-12-15 国家能源投资集团有限责任公司 Recovery method of waste SCR denitration catalyst and vanadium-tungsten-titanium-containing nano powder
CN107998989A (en) * 2017-12-11 2018-05-08 合肥右传媒科技有限公司 A kind of reaction kettle for preparing trifluoromethyl Luization zinc
CN108998670A (en) * 2018-07-05 2018-12-14 安徽思凯瑞环保科技有限公司 Thick titanium valve device and method thereof are extracted in SCR catalyst
CN110193364A (en) * 2019-06-04 2019-09-03 河北惠尔信新材料有限公司 A kind of discarded SCR catalyst recycling technique
CN111003728B (en) * 2019-11-28 2023-09-29 国惠环保新能源有限公司 Device and method for preparing titanium oxide nanorods by using waste denitration catalyst
CN111302397B (en) * 2020-03-13 2022-06-24 中国科学院城市环境研究所 Method and device for recovering waste denitration catalyst
CN112873933A (en) * 2020-12-30 2021-06-01 安徽博润纺织品有限公司 Polyester fiber screen mesh's clout is retrieved and is recycled device
CN115818725B (en) * 2023-02-14 2023-05-05 国能龙源环保有限公司 Method for preparing ferric oxide by using waste denitration catalyst
CN116053546B (en) * 2023-02-24 2023-12-05 浙江大学 Method for preparing electrolyte of all-vanadium redox flow battery by recycling waste denitration catalyst

Family Cites Families (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
ATE45295T1 (en) * 1985-08-19 1989-08-15 Siemens Ag PROCESS FOR MANUFACTURING A CATALYST FOR SELECTIVE REDUCTION OF NITROUS OXIDES IN EXHAUST GASES.
CN102936049B (en) * 2012-11-26 2014-06-04 西南民族大学 Method for extracting tungsten, titanium and vanadium from waste SCR (selective catalytic reduction) catalyst
CN102962079B (en) * 2012-11-27 2014-06-25 南京工业大学 Regeneration method for waste vanadium-titanium-based SCR (Selective Catalytic Reduction) flue gas denitrification catalyst
CN103508491B (en) * 2013-09-23 2015-12-02 宜兴市宜刚环保工程材料有限公司 Discarded honeycomb type denitrification catalyst regeneration and resource utilization method
CN104195342B (en) * 2014-09-17 2016-06-01 华北电力大学 A kind of method reclaiming Vanadium Pentoxide in FLAKES composition in waste and old SCR denitration
CN104549380A (en) * 2015-01-22 2015-04-29 龙岩紫荆创新研究院 Method for phosphoric acidification modification of TiO2 carrier for preparing V2O5-WO3/TiO2 based SCR (selective catalytic reduction) denitration catalyst

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN109939634A (en) * 2019-04-08 2019-06-28 南京威安新材料科技有限公司 Nanocatalyst industrial water solution device

Also Published As

Publication number Publication date
CN205269612U (en) 2016-06-01
CN105536817A (en) 2016-05-04
CN105536817B (en) 2018-03-30

Similar Documents

Publication Publication Date Title
CN205269648U (en) Hydrolysis reaction cauldron
CN103846112B (en) A kind of method utilizing discarded SCR catalyst Ethylene recov to regenerate denitrating catalyst
CN105256146B (en) A kind of method that Metal Palladium is reclaimed from useless palladium aluminium oxide catalyst
CN106623370A (en) Treatment process and system for organic silica mud
CN108043404A (en) Catalyst of removing volatile organic compounds prepared by a kind of red mud and preparation method thereof
CN102020307A (en) Disposal method of organic silicon copper-containing waste catalyst
CN104451152B (en) Vanadium, molybdenum, the device for continuously recycling of titanium and recovery process in SCR spent catalyst
CN110653010A (en) Recycling method and processing system for waste SCR denitration catalyst
CN106277048A (en) A kind of titanium slag is utilized to prepare the method and system of anatase titanium dioxide for raw material
CN105152205B (en) Method and device for recycling Ti and V from waste flue gas denitrification catalyst
CN205833182U (en) A kind of industrial waste Al2o3bead micropore activation system
CN106964333A (en) The method that rare earth loaded catalyst for handling sewage and its preparation method and application and catalytic ozonation handle sewage
CN202740999U (en) Novel flue gas desulfurization device
CN2820301Y (en) Device for regenerating smoke desulfurizing liquid by double alkali method
CN214192593U (en) Production of H from sulfur-containing waste2SO4System for controlling a power supply
CN102674251A (en) Waste acid recovery and treatment process
CN206424964U (en) Regenerating active carbon system
CN106693639A (en) Treatment method and system for waste gas and waste liquid in bio-fermentation production of fuel ethanol
CN207016586U (en) A kind of processing unit of industrial wastewater
CN106861410B (en) A kind of flue gas deep desulfuration denitration dry type integral method using manganous hydroxide as cycle operation medium
CN110015686A (en) Titanium slag recycles the method for titanium dioxide and the method from denitrating catalyst recycling tungsten, titanium and vanadium
CN108383142A (en) A kind of method of secondary aluminium aluminium cinder resource metaplasia production aluminium oxide
CN115569479A (en) Tail gas treatment system in crushing and sorting process of scrapped power lithium battery
CN213569539U (en) Utilize industry to contain sour system of sulphur waste system
CN108392891A (en) A kind of carbide slag slurries processing system

Legal Events

Date Code Title Description
C14 Grant of patent or utility model
GR01 Patent grant
CF01 Termination of patent right due to non-payment of annual fee
CF01 Termination of patent right due to non-payment of annual fee

Granted publication date: 20160601

Termination date: 20181216