CN106517348B - Potassium manganate continuous automatic production process - Google Patents
Potassium manganate continuous automatic production process Download PDFInfo
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- CN106517348B CN106517348B CN201610973294.5A CN201610973294A CN106517348B CN 106517348 B CN106517348 B CN 106517348B CN 201610973294 A CN201610973294 A CN 201610973294A CN 106517348 B CN106517348 B CN 106517348B
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- pipeline
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- oxidation reaction
- reaction tower
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- 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
- Y02P20/10—Process efficiency
- Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines
Abstract
The invention discloses a kind of potassium manganate continuous automatic production process, manganese powder mixing tank is connected with manganese powder storage tank by the first pipeline, manganese powder storage tank is connected by second pipe with manganese powder preheating can, manganese powder preheating can is connected by the 3rd pipeline with oxidation reaction tower material, oxidation reaction tower alkali lye charge door is connected by the 4th pipeline with alkali lye preheating can, alkali lye preheating can is connected by the 5th pipeline with alkali liquid tank, oxidation reaction tower is connected by discharge nozzle with discharging thinning tank, discharging thinning tank is connected with settling tank, the exhaust pipe of oxidation reaction tower and manganese powder preheating can is connected with air preheater, air preheater is connected with the air intlet of oxidation reaction tower, the cold side import of air preheater is connected with air compressor machine；Vapor heat exchanger is respectively arranged with by oxidation reaction tower, manganese powder preheating can and alkali lye preheating can, feed pump and two regulating valves are respectively arranged with first pipeline, second pipe, the 3rd pipeline, the 4th pipeline and the 5th pipeline, flowmeter and pressure gauge are provided between two regulating valves.
Description
Technical field
The present invention relates to a kind of potassium manganate continuous automatic production process, belong to chemical process field.
Background technology
The production technology of potassium manganate is：Manganese dioxide powder, potassium hydroxide and air are reacted to generation in oxidation reaction tower
Potassium manganate.The pretreatment of material is first mixes manganese dioxide powder with potassium hydroxide solution, by preheating of mixed material to 100-150
℃.Addition in advance is preheating at least 200 DEG C of potassium hydroxide solution in oxidation reaction tower, and heating causes in oxidation reaction tower
Temperature reaches 250 DEG C, then passes to air, adds the mixed solution of manganese dioxide powder and potassium hydroxide, is then heated to
250-265 DEG C of reaction, discharging diluted after having reacted, sedimentation obtain potassium manganate.At present present in the technological process
Problem is：Heating is mainly heated by coal, and seriously polluted, heat utilization ratio is low.Waste heat from tail gas can not be utilized rationally, be caused
A large amount of to waste, the air being passed through is cold air, will cause the temperature fluctuation in oxidation reaction tower, and charging at present is mainly people
Work feeds, and can not also realize the production of continuous and automatic.
The content of the invention
In order to solve the above-mentioned technical problem, the present invention provides a kind of potassium manganate continuous automatic production process, can the company of realization
Continuous automated production, rationally utilizes waste heat, clean environment firendly.
To achieve these goals, technical scheme is as follows：A kind of potassium manganate continuous automatic production process, bag
Production system is included, the production system includes oxidation reaction tower, and the import of the material outlet and manganese powder storage tank of manganese powder mixing tank is led to
Cross the first pipeline to be connected, the material inlet phase that the manganese powder tank bottom material outlet passes through second pipe and manganese powder preheating can
Even, the bottoms material outlet of the manganese powder preheating can is connected by the 3rd pipeline with the material inlet on oxidation reaction tower top, institute
The top for stating oxidation reaction tower and manganese powder preheating can is provided with exhaust pipe, and the top of the oxidation reaction tower is additionally provided with alkali lye
Charge door, alkali lye charge door are connected by the 4th pipeline with the discharging opening of alkali lye preheating can, the charging aperture of the alkali lye preheating can
It is connected by the 5th pipeline with alkali liquid tank, the material outlet of the oxidation reaction tower bottom passes through discharge nozzle and the thinning tank phase that discharges
Even, the discharging thinning tank is connected with settling tank, exhaust pipe and the air preheat of the oxidation reaction tower and manganese powder preheating can
The hot side import of device is connected, and the hot side outlet of the air preheater is connected with the air intlet of oxidation reaction tower bottom, described
The cold side import of air preheater is connected with air compressor machine.
Vapor heat exchanger, the oxygen are respectively arranged with by the oxidation reaction tower, manganese powder preheating can and alkali lye preheating can
Change reaction tower, the material in manganese powder preheating can and alkali lye preheating can by pipeline enter in vapor heat exchanger with after steam heat-exchanging,
Return to respectively again in oxidation reaction tower, manganese powder preheating can or alkali lye preheating can.
Feed pump is respectively arranged with first pipeline, second pipe, the 3rd pipeline, the 4th pipeline and the 5th pipeline,
It is provided with two regulating valves at feed liquid pump discharge rear, flowmeter and pressure gauge is provided with the pipeline between two regulating valves；
Production stage is：
A：Potassium hydroxide solution and manganese dioxide powder are pre-mixed in mixing tank obtains mixed liquor, then enters through manganese powder storage tank
Enter manganese powder preheating can, 150-200 DEG C is heated in manganese powder preheating can；
B：Potassium hydroxide solution is preheated to 200 DEG C, then is pumped into oxidation reaction tower, continues to heat in oxidation reaction tower
To 250-265 DEG C, be passed through using exhaust pipe tail gas preheating after air；
C:The valve on the 3rd pipeline is opened, is pumped into successive reaction in oxidation reaction tower；
D, reacted material enters discharging thinning tank, and settling tank is entered after being diluted with water and is settled, supernatant reclaims to obtain
Alkali lye is reclaimed, recovery alkali lye is used in step A, and filter residue obtains product by press filtration.
Using such scheme, manganese dioxide powder is allowed first to be mixed with potassium hydroxide solution in manganese powder mixing tank so that dioxy
Change the liquid that manganese powder is changed into flowing, realize and manganese dioxide is added by pipeline.Air, manganese dioxide powder and potassium hydroxide all first pass through
Added after crossing preheating can preheating in oxidation reaction tower, avoid causing the temperature of oxidation reaction tower excessive fluctuation, influenceed anti-
That answers is normally carried out.
Connected between each storage tank and oxidation reaction tower by pipeline, and feed pump, regulating valve are set on pipeline
Flowmeter and pressure gauge, the uninterrupted for adding feed liquid is automatically controlled by switch board, realize continuous automatic production, control journey
Sequence is the conventional meanses of this area.
Air is preheated using the waste heat of tail gas, the air after preheating is added in oxidation reaction tower, on the one hand
Reach and rationally utilize waste heat, avoid the purpose of energy waste；On the other hand the air by preheating is added in oxidation reaction tower, right
Temperature fluctuation in oxidation reaction tower is smaller.
Traditional coal heating is changed to steam heating, it is only necessary to set up one by the equipment such as oxidation reaction tower and preheating can
Platform heat exchanger, equipment investment is small, and cost is low, and energy-conserving and environment-protective.
In such scheme：Two vapor heat exchangers are provided with by the oxidation reaction tower, to meet the temperature of oxidation reaction tower
Degree needs.
In such scheme：The cold side outlet port of the air preheater is connected by air-introduced machine with tail gas recycle tank.It will pass through
Tail gas recycle after heat exchange, avoid damaging to changing commanders.
In such scheme：The settling tank is divided into two-stage, and first order settling tank is connected with discharging thinning tank discharging opening, and first
The level lye export of settling tank is connected with the charging aperture of second level settling tank by the 6th pipeline, and the alkali lye of second level settling tank goes out
Mouthful it is connected by the 7th pipeline with reclaiming alkali storage tank, the material outlet of the first order settling tank and second level settling tank passes through the
Eight pipelines are connected with potassium manganate storage tank.
In such scheme：Feed pump is also respectively arranged with 6th pipeline, the 7th pipeline and the 8th pipeline, in feed liquid
Pump discharge rear is provided with two regulating valves, and flowmeter and pressure gauge are provided with the pipeline between two regulating valves.
First pipeline described in such scheme, second pipe, the 3rd pipeline, the 4th pipeline, the 5th pipeline, the 6th pipeline,
7th pipeline and the 8th pipeline also set a bypass branch respectively, and feed pump, two tune are also equipped with the bypass branch
Save valve, flowmeter and pressure gauge, the feed liquid parallel connection of pumps on feed pump and main pipeline in the bypass branch.Bypass branch is set
Pipe, when the feed pump on main pipeline breaks down, can change in bypass branch and use.
Beneficial effect：The present invention reaches by the design to potassium manganate production system and rationally utilizes waste heat from tail gas, reclaim tail
The effect of gas.Using medium of the steam as heating, improvement cost is low, clean environment firendly, by the handling of manganese dioxide powder, right
The pre-heat treatment of air, potassium hydroxide solution, the large impact excessively to temperature in oxidation reaction tower is avoided, realizes that continuous and automatic is steady
Fixed production, production efficiency greatly improve.
Brief description of the drawings
Fig. 1 is the process chart of the present invention.
Fig. 2 is partial enlarged drawing at Fig. 1 A.
Fig. 3 is partial enlarged drawing at Fig. 1 B.
Embodiment
The invention will be further described with reference to the accompanying drawings and examples：
Embodiment 1, as Figure 1-3：The potassium manganate continuous automatic production process of the present invention is by manganese powder mixing tank 1, manganese
Powder storage tank 2, manganese powder preheating can 3, oxidation reaction tower 4, exhaust pipe 5, alkali lye preheating can 6, alkali liquid tank 7, vapor heat exchanger 8, go out
Expect thinning tank 9, air preheater 10, air compressor machine 11, tail gas recycle tank 12, feed pump 13, regulating valve 14, flowmeter 15, pressure
The compositions such as table 16, first order settling tank 17, second level settling tank 18, recovery alkali storage tank 19, potassium manganate storage tank 20
The material outlet of manganese powder mixing tank 1 is connected with the import of manganese powder storage tank 2 by the first pipeline, on manganese powder mixing tank 1
It is provided with potassium hydroxide filler and manganese dioxide powder adds mouth, stirring is additionally provided with manganese powder mixing tank 1, in manganese powder mixing tank
In 1, manganese dioxide powder and potassium hydroxide solution first mix, and increase the mobility of manganese dioxide powder, realize pipeline.Manganese powder stores up
It is also provided with stirring in tank 2 and manganese powder preheating can 3, the outlet of the bottoms material of manganese powder storage tank 2 passes through second pipe and manganese powder preheating can 3
Material inlet is connected, and the bottoms material outlet of manganese powder preheating can 3 passes through the 3rd pipeline and the material inlet on the top of oxidation reaction tower 4
It is connected, the top of oxidation reaction tower 4 and manganese powder preheating can 3 is provided with exhaust pipe 5, and the top of oxidation reaction tower is additionally provided with alkali
Liquid charge door, alkali lye charge door are connected by the 4th pipeline with the discharging opening of alkali lye preheating can 6, the charging aperture of alkali lye preheating can 6
It is connected by the 5th pipeline with alkali liquid tank 7, the material outlet of the bottom of oxidation reaction tower 4 passes through discharge nozzle and the phase of thinning tank 9 that discharges
Even, the dilution import of discharging thinning tank 9 is connected with dilute water pot 21, and is provided with regulating valve on the pipeline that they are connected, and goes out
Material thinning tank 9 is connected with settling tank, and settling tank is divided into two-stage, and first order settling tank 17 is connected with the discharging discharging opening of thinning tank 9, the
The lye export of one-level settling tank 17 is connected with the charging aperture of second level settling tank 18 by the 6th pipeline, second level settling tank 18
Lye export be connected by the 7th pipeline with recovery alkali storage tank 19, the alkali lye devaporation in recovery alkali storage tank 19 is reclaimed, first
The material outlet of level settling tank 17 and second level settling tank 18 is connected by the 8th pipeline with potassium manganate storage tank 20, is obtained by press filtration
To product.
First pipeline, second pipe, the 3rd pipeline, the 4th pipeline, the 5th pipeline, the 6th pipeline, the 7th pipeline and the 8th
Feed pump 13 is respectively arranged with pipeline, exporting rear in feed pump 13 is provided with two regulating valves 14, two regulating valves 14 it
Between pipeline on be provided with flowmeter 15 and pressure gauge 16, material is after feed pump 13 to first regulating valve 14, Ran Houjing
15 to the second regulating valve of excessively stream gauge, finally reaches next unit.
First pipeline, second pipe, the 3rd pipeline, the 4th pipeline, the 5th pipeline, the 6th pipeline, the 7th pipeline and the 8th
Pipeline also sets a bypass branch respectively, and feed pump 13, two regulating valves 14, flowmeters are also equipped with the bypass branch
15 and pressure gauge 16, the feed pump 13 in bypass branch is in parallel with the feed pump 13 on main pipeline, so when the material on main pipeline
When liquid pump 13 goes wrong, it can in time change and be used in bypass branch.
The exhaust pipe 5 of oxidation reaction tower 4 and manganese powder preheating can 3 is connected with the hot side import of air preheater 10, air
The hot side outlet of preheater 10 is connected with the air intlet of the bottom of oxidation reaction tower 4, cold side import and the sky of air preheater 10
Press 11 is connected；The cold side outlet port of air preheater 10 is connected by air-introduced machine with tail gas recycle tank 12, using waste heat from tail gas pair
Air is preheated, and all connecting pipes have heat-insulation layer, and the tail gas come out from air preheater 10 can be also used for each pipe
The insulation in road.
Vapor heat exchanger 8 is respectively arranged with by oxidation reaction tower 4, manganese powder preheating can 3 and alkali lye preheating can 6, oxidation is anti-
The material in tower 4, manganese powder preheating can 3 and alkali lye preheating can 6 is answered to enter by pipeline in vapor heat exchanger 8 and after steam heat-exchanging,
Return in oxidation reaction tower 4, manganese powder preheating can 3 or alkali lye preheating can 6；In order to meet the heat demand of oxidation reaction tower, oxygen
Change and be provided with two vapor heat exchangers 8 by reaction tower 4.
The premixing in mixing tank 1 of potassium hydroxide solution and manganese dioxide powder obtains mixed liquor, then enters through manganese powder storage tank 2
Enter manganese powder preheating can 3,150-200 DEG C is heated in manganese powder preheating can 3.
Potassium hydroxide solution is preheated to 200 DEG C, then is pumped into oxidation reaction tower 4, continues to heat in oxidation reaction tower
To 250-265 DEG C, be passed through using exhaust pipe tail gas preheating after air.
C:The valve on the 3rd pipeline is opened, is pumped into successive reaction in oxidation reaction tower 4.
D, reacted material enters discharging thinning tank 9, and settling tank is entered after being diluted with water and is settled, supernatant reclaims to obtain
Alkali lye is reclaimed, recovery alkali lye is used in step A, and filter residue obtains product by press filtration.During the course of the reaction, adjusted by regulating valve
It is pumped into the flow of the potassium hydroxide solution of oxidation reaction tower, mixed liquor and air, control continuous feed, discharging.
The present invention is not limited to above-mentioned specific embodiment, it will be appreciated that one of ordinary skill in the art is without creative
Work can makes many modifications and variations according to the design of the present invention.In a word, all technician in the art are according to this
The design of invention passes through the available technical side of logical analysis, reasoning, or a limited experiment on the basis of existing technology
Case, all should be in the protection domain being defined in the patent claims.
Claims (6)
1. a kind of potassium manganate continuous automatic production process, including production system, the production system includes oxidation reaction tower
(4), the material outlet of manganese powder mixing tank (1) is connected with the import of manganese powder storage tank (2) by the first pipeline, the manganese powder storage tank
(2) bottoms material outlet is connected by second pipe with the material inlet of manganese powder preheating can (3), the manganese powder preheating can (3)
Bottoms material outlet is connected by the 3rd pipeline with the material inlet on oxidation reaction tower (4) top, the oxidation reaction tower (4) and
The top of manganese powder preheating can (3) is provided with exhaust pipe (5), and the top of the oxidation reaction tower is additionally provided with alkali lye charge door,
Alkali lye charge door is connected by the 4th pipeline with the discharging opening of alkali lye preheating can (6), and the charging aperture of the alkali lye preheating can (6) leads to
Cross the 5th pipeline with alkali liquid tank (7) to be connected, the material outlet of oxidation reaction tower (4) bottom is diluted by discharge nozzle and discharging
Tank (9) is connected, and the discharging thinning tank (9) is connected with settling tank, the tail of the oxidation reaction tower (4) and manganese powder preheating can (3)
Feed channel (5) is connected with the hot side import of air preheater (10), and the hot side outlet of the air preheater (10) and oxidation are anti-
The air intlet of tower (4) bottom is answered to be connected, the cold side import of the air preheater (10) is connected with air compressor machine (11)；
Vapor heat exchanger is respectively arranged with by the oxidation reaction tower (4), manganese powder preheating can (3) and alkali lye preheating can (6)
(8), the material in the oxidation reaction tower (4), manganese powder preheating can (3) and alkali lye preheating can (6) is changed by pipeline into steam
In hot device (8) and after steam heat-exchanging, then return to respectively in oxidation reaction tower (4), manganese powder preheating can (3) or alkali lye preheating can (6)；
Feed pump (13) is respectively arranged with first pipeline, second pipe, the 3rd pipeline, the 4th pipeline and the 5th pipeline,
Feed pump (13) outlet rear is provided with two regulating valves (14), flow is provided with the pipeline between two regulating valves (14)
Count (15) and pressure gauge (16)；
Production stage is：
A：The premixing in mixing tank (1) of potassium hydroxide solution and manganese dioxide powder obtains mixed liquor, then through manganese powder storage tank (2)
Into manganese powder preheating can (3), 150-200 DEG C is heated in manganese powder preheating can (3)；
B：Potassium hydroxide solution is preheated to 200 DEG C, then is pumped into oxidation reaction tower (4), continues to heat in oxidation reaction tower
To 250-265 DEG C, be passed through using exhaust pipe tail gas preheating after air；
C:The valve on the 3rd pipeline is opened, is pumped into oxidation reaction tower (4) interior successive reaction；
D, reacted material enters discharging thinning tank (9), and settling tank is entered after being diluted with water and is settled, supernatant reclaims back
Alkali lye is received, recovery alkali lye is used in step A, and filter residue obtains product by press filtration.
2. potassium manganate continuous automatic production process according to claim 1, it is characterised in that：The oxidation reaction tower (4)
Side is provided with two vapor heat exchangers (8).
3. potassium manganate continuous automatic production process according to claim 1 or claim 2, it is characterised in that：The air preheater
(10) cold side outlet port is connected by air-introduced machine with tail gas recycle tank (12).
4. potassium manganate continuous automatic production process according to claim 3, it is characterised in that：The settling tank is divided into two
Level, first order settling tank (17) are connected with discharging thinning tank (9) discharging opening, the lye export and second of first order settling tank (17)
The charging aperture of level settling tank (18) is connected by the 6th pipeline, the lye export of second level settling tank (18) by the 7th pipeline with
Reclaim alkali storage tank (19) to be connected, the material outlet of the first order settling tank (17) and second level settling tank (18) passes through the 8th pipe
Road is connected with potassium manganate storage tank (20).
5. potassium manganate continuous automatic production process according to claim 4, it is characterised in that：6th pipeline, the 7th
Feed pump (13) is also respectively arranged with pipeline and the 8th pipeline, feed pump (13) outlet rear is provided with two regulating valves
(14) flowmeter (15) and pressure gauge (16), are provided with the pipeline between two regulating valves (14).
6. potassium manganate continuous automatic production process according to claim 5, it is characterised in that：First pipeline, second
Pipeline, the 3rd pipeline, the 4th pipeline, the 5th pipeline, the 6th pipeline, the 7th pipeline and the 8th pipeline also set a bypass respectively
Branch pipe, feed pump (13), two regulating valves (14), flowmeter (15) and pressure gauge (16) are also equipped with the bypass branch,
Feed pump (13) in the bypass branch is in parallel with the feed pump (13) on main pipeline.
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Families Citing this family (5)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN107720830A (en) * | 2017-11-29 | 2018-02-23 | 白银昌元化工有限公司 | The device and UTILIZATION OF VESIDUAL HEAT IN technique that a kind of Pneumatic fluidized tower UTILIZATION OF VESIDUAL HEAT IN is evaporated in potassium permanganate |
| CN109909255A (en) * | 2017-12-12 | 2019-06-21 | 云南建水锰矿有限责任公司 | The method for the waste residue that process for producing potassium permanganate generates |
| CN110980812B (en) * | 2019-12-26 | 2022-09-02 | 广东航鑫科技股份公司 | Production system and production method of potassium manganate |
| CN111302309B (en) * | 2020-01-20 | 2023-05-23 | 泰安渤洋化工科技有限公司 | Process device and method for continuous crystal form passivation and modification of hydrotalcite-like products |
| CN111905682B (en) * | 2020-08-18 | 2022-03-25 | 萍乡市利升科技有限公司 | Oxidation tower and molten salt method continuous oxidation process for producing potassium permanganate by using same |
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| US5660712A (en) * | 1995-06-07 | 1997-08-26 | Carus, Iii; Paul | Electrolytic production of potassium permanganate using a cationic membrane in an electrolytic cell |
| CN101439879A (en) * | 2008-12-22 | 2009-05-27 | 昆明冶金研究院 | Method for preparing potassium manganate by three-phase pressurization continuous oxidation |
| CN101492182A (en) * | 2008-01-22 | 2009-07-29 | 遵义双源化工（集团）有限责任公司 | Method and equipment for manufacturing potassium manganate |
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| US2940823A (en) * | 1956-10-10 | 1960-06-14 | Carus Chemical Company | Production of potassium manganates |
| US5011672A (en) * | 1986-05-16 | 1991-04-30 | Industrial Quimica Del Nalon, S.A. | Process for producing potassium manganate |
| US5660712A (en) * | 1995-06-07 | 1997-08-26 | Carus, Iii; Paul | Electrolytic production of potassium permanganate using a cationic membrane in an electrolytic cell |
| CN101492182A (en) * | 2008-01-22 | 2009-07-29 | 遵义双源化工（集团）有限责任公司 | Method and equipment for manufacturing potassium manganate |
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