CN107140693A - A kind of bodied ferric sulfate continuous process system and its method - Google Patents
A kind of bodied ferric sulfate continuous process system and its method Download PDFInfo
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- CN107140693A CN107140693A CN201710561301.5A CN201710561301A CN107140693A CN 107140693 A CN107140693 A CN 107140693A CN 201710561301 A CN201710561301 A CN 201710561301A CN 107140693 A CN107140693 A CN 107140693A
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01G—COMPOUNDS CONTAINING METALS NOT COVERED BY SUBCLASSES C01D OR C01F
- C01G49/00—Compounds of iron
- C01G49/14—Sulfates
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J2219/00002—Chemical plants
- B01J2219/00027—Process aspects
- B01J2219/00033—Continuous processes
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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
- Y02P20/50—Improvements relating to the production of bulk chemicals
- Y02P20/584—Recycling of catalysts
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- Inorganic Compounds Of Heavy Metals (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Inorganic Chemistry (AREA)
Abstract
A kind of bodied ferric sulfate continuous process system and its method, the invention belongs to chemical field, it there are problems that running under reaction time length, low production efficiency, product energy consumption height, equipment long-time HTHP strong acidic condition to solve modular reaction process, the technical scheme that the present invention is provided is as follows：A kind of bodied ferric sulfate continuous process system, described continuous process system includes dissolving tank, air and liquid mixer, gas-liquid separator, end product pool and gas collector, the beneficial effects of the present invention are, catalyst is recycled in the present system, oxidation efficiency is high, and the reaction time is short, and yield is high（Single complete equipment production capacity is 30 ton hours）；Single complete equipment production capacity is big, and operating personnel are few, and production is stable；Without reacted gas treatment equipment, occupation area of equipment is small, easy to maintenance.
Description
Technical field
The invention belongs to chemical field, and in particular to a kind of bodied ferric sulfate quantity-produced technique.
Background technology
Current bodied ferric sulfate production using direct oxidation or the modular reaction process of catalysis oxidation, by ferrous sulfate and
The feed liquid that sulfuric acid is prepared according to a certain percentage is pumped into reactor, opens and catalyst n O is added after the EGR of reactor2,
And be passed through oxygen and reacted, until complete oxidation.Have catalyst participate in reaction in the case of, oxidization time be about 60min ~
150min, in the case of participating in reaction without catalyst, oxidization time is about 8h ~ 12h, catalyst n O2Complete after reaction, pass through
Got into the air after environmental protection treatment.
But modular reaction process has reaction time length, low production efficiency（Single complete equipment production capacity be 10 tons/it is small
When）, product energy consumption is high, runs under equipment long-time HTHP strong acidic condition and is easily damaged, the equipment investment of unit production capacity
Height, if catalyst environmental protection treatment is ineffective to may also result in atmosphere pollution.
The content of the invention
In view of the above-mentioned problems, it is an object of the invention to provide a kind of energy consumption is low, operating personnel are few, catalyst can be recycled
Continuous production processes.
The technical scheme that the present invention is provided is as follows：
A kind of bodied ferric sulfate continuous process system, described continuous process system includes dissolving tank, air and liquid mixer, gas-liquid
Separator, end product pool and gas collector,
Dissolving tank, described dissolving tank be used to dissolve be connected with reaction raw materials, described dissolving tank the mixing after dissolving is molten
Liquid extracts the mixed solution pipeline to air and liquid mixer；
Ferrous ion is converted into iron ion by air and liquid mixer, described air and liquid mixer, and described air and liquid mixer bottom connects
Catalyst adding set is connected with, described air and liquid mixer is also associated with anti-in gas-liquid separator for reactant to be transferred to
Thing is answered to transfer pipeline；
Gas-liquid separator, is used for mixed gas delivery for be connected with the top of gas-liquid separation, described gas-liquid separator
To the mixed gas pipeline of gas collector, described gas-liquid separator bottom is provided with is transferred to end product pool by reaction liquid
Fluid pipeline；
End product pool, described end product pool is used for placing response liquid；
Gas collector, for collection and oxidizing gas, is connected to be passed through the oxygen of oxygen on described gas collector
Feed channel, and by the gas recycling duct in the vapor return after oxidation to air and liquid mixer.
Further, it is additionally provided with agitator in described dissolving tank.
Further, described continuous process system also includes and connected on dilute sulfuric acid storage tank, described dilute sulfuric acid storage tank
There is a dilute sulfuric acid pipeline, described dilute sulfuric acid storage tank and dissolving tank are set on described dilute sulfuric acid pipeline by dilute sulfuric acid pipeline communication
There is the dilute sulfuric acid controlling pump for extracting dilute sulfuric acid.
Further, the liquid return tube being connected with described dissolving tank, institute are also associated with described fluid pipeline
First liquid control valve of the liquid return tube stated provided with control liquid backflow.
Further, it is characterised in that it is gentle that described gas collector includes gas mixer, gas buffer tank
Body storage tank；The described oxygen channel of described gas mixer connection, described gas mixer side is mixed by described
Close gas pipeline and described gas-liquid separator is communicated, described oxygen channel is described close to described mixed gas pipeline
The first NO that gas mixer opposite side, which is provided with, to be used for and described gas buffer tank is communicated2Gas pipeline；Described gas delays
Rush tank and be provided with the 2nd NO for being used for communicating with described gas storage tanks2Gas pipeline, the 2nd described NO2On gas pipeline
Provided with the compression pump for compressed gas；The NO communicated with described air and liquid mixer is provided with the top of described gas storage tanks2
Gas recycling duct.
Further, described mixed solution pipeline, which is provided with, is used to extract in described mixed solution to air and liquid mixer
Mixed solution draw-off pump.
Further, described fluid pipeline is provided with the second liquid control valve for being used for controlling liquid to flow.
Further, described gas buffer tank is provided with and the extraneous surge tank control valve communicated.
A kind of bodied ferric sulfate continuous producing method, described method includes the steps：
The first step：Ferrous sulfate heptahydrate is put into dissolving tank, it is the dilute of 25%-28% to extract mass fraction from dilute sulfuric acid storage tank
Sulfuric acid, while opening agitating device, is slowly introducing steam, temperature is increased into 60 ~ 65 DEG C in dissolving tank, the shape in dissolving tank
Into oversaturated copperas solution；
Second step：Oversaturated copperas solution is extracted out of dissolving tank into air and liquid mixer, is added and filled by catalyst
Put and be passed through catalyst n O2Reacted, obtain ferrum sulfuricum oxydatum solutum, while part NO2It is converted into NO；
3rd step：Reacted ferrum sulfuricum oxydatum solutum and mixed gas enter gas-liquid separator, and mixed gas is from mixed gas outlet
Into gas mixer, described ferrum sulfuricum oxydatum solutum enters end product pool from liquid outlet；
4th step：Oxygen is passed through to gas mixer, the NO in mixed gas is converted into NO2, the gas after conversion enters gas
Body surge tank, then into gas storage tanks after compression pump compresses, air and liquid mixer obtains NO from gas storage tanks2。
Further, described method also comprises the following steps：The complete copperas solution of unreacted and ferric sulfate solution
Liquid is entered in dissolving tank by liquid return tube.
The beneficial effects of the present invention are, catalyst is recycled in the present system, and oxidation efficiency is high, and the reaction time is short,
Yield is high（Single complete equipment production capacity is 30 ton hours）；Single complete equipment production capacity is big, and operating personnel are few, and production is stable；After reaction
Gas treatment equipment, occupation area of equipment is small, easy to maintenance.
Brief description of the drawings
Fig. 1 is artwork of the invention.
Specific embodiment
Embodiment 1
Fig. 1 is refer to, a kind of bodied ferric sulfate continuous process system, described continuous process system includes dissolving tank（1）, gas
Liquid mixer（2）, gas-liquid separator（3）, end product pool（4）And gas collector,
Dissolving tank（1）, for dissolving reaction raw materials, reaction raw materials are the supersaturated seven water sulphur that mass fraction is 25%-28% dissolvings
Sour ferrous iron solution, described dissolving tank（1）On be connected with supersaturated ferrous sulfate heptahydrate solution extraction to air and liquid mixer（2）
Interior mixed solution pipeline（11）；Described mixed solution pipeline（11）Being provided with is used to extract described supersaturated seven water sulfuric acid
Ferrous iron solution is to air and liquid mixer（2）Interior mixed solution draw-off pump；Described dissolving tank（1）Agitator is inside additionally provided with, is stirred
Device opens the dissolving having using ferrous sulfate heptahydrate；
Described air and liquid mixer（2）Bottom is communicated with catalyst adding set, and described catalyst adding set is used for from gas
Liquid mixer bottom is to air and liquid mixer（2）Interior confession catalyst n O2Gas, described air and liquid mixer（2）It is also associated with being used for
Reactant is transferred to gas-liquid separator（3）Interior reactant transfer pipeline（21）；In supersaturated ferrous sulfate heptahydrate solution
Ferrous ion is in catalyst n O2In the presence of gas, iron ion is converted into, and NO2Then part switchs to NO to gas.
Described gas-liquid separator（3）Top is connected with for by the gaseous mixture of mixed gas delivery to gas collector
Body pipeline（31）, described gas-liquid separator（3）Bottom is provided with ferric ion solutions（The mixing of ferric sulfate and sulfuric acid）It is transferred to
End product pool（4）Fluid pipeline（32）.
Described end product pool（4）For placing ferric ion solutions（Polyaluminum sulfate iron semi-finished product）；
Described gas collector includes gas mixer（5）, gas buffer tank（6）And gas storage tanks（7）；Described
Gas mixer（5）The described oxygen channel of connection（51）, described gas mixer（5）Side passes through described mixed gas
Pipeline（31）With described gas-liquid separator（3）Communicate, described oxygen channel（51）Close to described mixed gas pipeline
（31）, it is ensured that NO2With NO mixed gas from mixed gas pipeline（31）Contacted after out with oxygen, NO gases are oxidized to
NO2, described gas mixer（5）Opposite side, which is provided with, to be used for and described gas buffer tank（6）The first gas pipeline communicated
（52）；Described gas buffer tank（6）Being provided with is used for and described gas storage tanks（7）The 2nd NO communicated2Gas pipeline
（61）, described the 2nd NO2Gas pipeline（61）It is provided with the compression pump for compressed gas（62）；Described gas storage tanks
（7）Top is provided with and described air and liquid mixer（2）The NO communicated2Gas recycling duct（71）, the NO of oxidation2Gas is through gas
Circulating line（71）Come back to air and liquid mixer（2）It is interior to participate in reacting as catalyst.
In addition, described continuous process system also includes dilute sulfuric acid storage tank（8）, described dilute sulfuric acid storage tank（8）
On be connected with dilute sulfuric acid pipeline（81）, described dilute sulfuric acid storage tank（8）And dissolving tank（1）Pass through dilute sulfuric acid pipeline（81）Connection,
Described dilute sulfuric acid pipeline（81）It is provided with the dilute sulfuric acid controlling pump for being used for extracting dilute sulfuric acid（82）, realize automatic addition dilute sulfuric acid
Solution.
Described fluid pipeline（32）On be also associated with and described dissolving tank（1）The liquid return tube being connected（12）,
Described liquid return tube（12）The first liquid control valve provided with control liquid backflow, if reaction thoroughly or does not have it
When his situation needs to restart reaction, first liquid control valve is opened so that reacted liquid enters dissolving tank（1）Weight
Newly start.
Described fluid pipeline（32）It is provided with the second liquid control valve for being used for controlling liquid to flow, the second liquid control
Valve processed is located at gas-liquid separator（3）And liquid return tube（12）Between.
Described gas buffer tank（6）It is provided with and the extraneous surge tank control valve communicated, likewise, gas storage tanks
（7）On also be provided with storage tank control valve, open surge tank control valve and storage tank control valve so that gas buffer tank（6）It is gentle
Body storage tank（7）Communicated with other extraneous devices, in emergency circumstances realize decompression or other processing.
Embodiment 2
A kind of bodied ferric sulfate continuous producing method, described method includes the steps：
The first step：Ferrous sulfate heptahydrate is put into dissolving tank（1）It is interior, from dilute sulfuric acid storage tank（8）Extraction mass fraction is 25%-
28% dilute sulfuric acid is to dissolving tank（1）It is interior, while opening agitating device, steam is slowly introducing, temperature is increased to 60 ~ 65 DEG C, plus
Heat of solution, in dissolving tank（1）It is interior to form dispersed oversaturated copperas solution；
Second step：From dissolving tank（1）It is interior to extract oversaturated copperas solution to air and liquid mixer（2）In, pass through catalyst
Adding set is passed through catalyst n O2Reacted, obtain ferrum sulfuricum oxydatum solutum, while part NO2It is converted into NO；
3rd step：Reacted ferrum sulfuricum oxydatum solutum and mixed gas enter gas-liquid separator（3）, mixed gas passes through mixed gas
Pipeline（31）Into gas mixer（5）, described ferrum sulfuricum oxydatum solutum enters end product pool from liquid outlet（4）, in end product pool（4）
Interior, ferrum sulfuricum oxydatum solutum is further cured；
4th step：To gas mixer（5）Oxygen is passed through, the NO in mixed gas is converted into NO2, the NO after conversion2Gas
Into gas buffer tank（6）, then into gas storage tanks after compression pump compresses（7）, air and liquid mixer（2）From gas storage
Tank（7）Pass through gas recycling duct（71）Obtain NO2。
Described method can also comprise the following steps：The complete copperas solution of unreacted and ferrum sulfuricum oxydatum solutum pass through
Liquid return tube（12）Into dissolving tank（1）It is interior.
Claims (10)
1. a kind of bodied ferric sulfate continuous process system, it is characterised in that described continuous process system includes dissolving tank, gas
Liquid mixer, gas-liquid separator, end product pool and gas collector,
Dissolving tank, described dissolving tank be used to dissolve be connected with reaction raw materials, described dissolving tank the mixing after dissolving is molten
Liquid extracts the mixed solution pipeline to air and liquid mixer；
Ferrous ion is converted into iron ion by air and liquid mixer, described air and liquid mixer, and described air and liquid mixer bottom connects
Catalyst adding set is connected with, described air and liquid mixer is also associated with anti-in gas-liquid separator for reactant to be transferred to
Thing is answered to transfer pipeline；
Gas-liquid separator, is used for mixed gas delivery for be connected with the top of gas-liquid separation, described gas-liquid separator
To the mixed gas pipeline of gas collector, described gas-liquid separator bottom is provided with is transferred to end product pool by reaction liquid
Fluid pipeline；
End product pool, described end product pool is used for placing response liquid；
Gas collector, for collection and oxidizing gas, is connected to be passed through the oxygen of oxygen on described gas collector
Feed channel, and by the gas recycling duct in the vapor return after oxidation to air and liquid mixer.
2. a kind of bodied ferric sulfate continuous process system as claimed in claim 1, it is characterised in that in described dissolving tank also
Provided with agitator.
3. a kind of bodied ferric sulfate continuous process system as claimed in claim 1, it is characterised in that described continuous production system
System also includes dilute sulfuric acid pipeline is connected with dilute sulfuric acid storage tank, described dilute sulfuric acid storage tank, described dilute sulfuric acid storage tank and molten
Xie Chi is provided with the dilute sulfuric acid controlling pump for being used for extracting dilute sulfuric acid by dilute sulfuric acid pipeline communication, described dilute sulfuric acid pipeline.
4. a kind of bodied ferric sulfate continuous process system as claimed in claim 1, it is characterised in that on described fluid pipeline
The liquid return tube being connected with described dissolving tank is also associated with, described liquid return tube is provided with control liquid backflow
First liquid control valve.
5. a kind of bodied ferric sulfate continuous process system as claimed in claim 1, it is characterised in that described gas collection dress
Put and include gas mixer, gas buffer tank and gas storage tanks；The described oxygen channel of described gas mixer connection,
Described gas mixer side is communicated by described mixed gas pipeline and described gas-liquid separator, described oxygen hose
Road is close to described mixed gas pipeline, and described gas mixer opposite side, which is provided with, to be used for and described gas buffer tank is communicated
The first NO2Gas pipeline；The 2nd NO that described gas buffer tank, which is provided with, to be used for and described gas storage tanks are communicated2Gas
Body pipeline, the 2nd described NO2Gas pipeline is provided with the compression pump for compressed gas；Set at the top of described gas storage tanks
There is the NO communicated with described air and liquid mixer2Gas recycling duct.
6. a kind of bodied ferric sulfate continuous process system as claimed in claim 1, it is characterised in that described mixed liquor pipe
Road, which is provided with, to be used to extract the mixed solution draw-off pump in described mixed solution to air and liquid mixer.
7. a kind of bodied ferric sulfate continuous process system as claimed in claim 1, it is characterised in that on described fluid pipeline
Provided with the second liquid control valve for controlling liquid to flow.
8. a kind of bodied ferric sulfate continuous process system as claimed in claim 1, it is characterised in that described gas buffer tank
It is provided with and the extraneous surge tank control valve communicated.
9. a kind of bodied ferric sulfate continuous producing method, its feature is that described method includes the steps：
The first step：Ferrous sulfate heptahydrate is put into dissolving tank, it is the dilute of 25%-28% to extract mass fraction from dilute sulfuric acid storage tank
Sulfuric acid, while opening agitating device, is slowly introducing steam, temperature is increased into 60 ~ 65 DEG C in dissolving tank, the shape in dissolving tank
Into oversaturated copperas solution；
Second step：Oversaturated copperas solution is extracted out of dissolving tank into air and liquid mixer, is added and filled by catalyst
Put and be passed through catalyst n O2Reacted, ferrous ion is converted into iron ion, while part NO2It is converted into NO；
3rd step：Reacted solution and mixed gas enter gas-liquid separator, and mixed gas is entered by mixed gas pipeline
Gas mixer, described solution enters end product pool from liquid outlet；
4th step：Oxygen is passed through to gas mixer, the NO in mixed gas is converted into NO2, the gas after conversion enters gas
Surge tank, then into gas storage tanks after compression pump compresses, air and liquid mixer obtains NO from gas storage tanks2。
10. a kind of bodied ferric sulfate continuous producing method as claimed in claim 9, it is characterised in that described method is also wrapped
Include following steps：The complete copperas solution of unreacted and ferrum sulfuricum oxydatum solutum are entered in dissolving tank by liquid return tube.
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| CN201710561301.5A CN107140693B (en) | 2017-07-11 | 2017-07-11 | A kind of bodied ferric sulfate continuous process system and its method |
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| CN201710561301.5A CN107140693B (en) | 2017-07-11 | 2017-07-11 | A kind of bodied ferric sulfate continuous process system and its method |
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Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2007106655A (en) * | 2005-10-17 | 2007-04-26 | Nittetsu Mining Co Ltd | Method for efficiently producing polyferric sulfate by using ferric oxide sludge as iron raw material |
| CN101116792A (en) * | 2007-09-13 | 2008-02-06 | 大连理工大学 | Technics of flue gas desulfurizing through catalytic oxidation method and by-product polymerizing iron sulfate through catalytic method |
| CN104591297A (en) * | 2015-01-09 | 2015-05-06 | 嘉兴艾尔瑞环境科技有限公司 | Method and device for preparing polymeric ferric sulfate |
| CN105692717A (en) * | 2016-03-21 | 2016-06-22 | 广西福斯特再生资源环保科技有限公司 | Polyferric sulfate and preparation method of polyferric sulfate |
| CN206985743U (en) * | 2017-07-11 | 2018-02-09 | 深圳市长隆科技有限公司 | A kind of bodied ferric sulfate continuous process system |
-
2017
- 2017-07-11 CN CN201710561301.5A patent/CN107140693B/en active Active
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2007106655A (en) * | 2005-10-17 | 2007-04-26 | Nittetsu Mining Co Ltd | Method for efficiently producing polyferric sulfate by using ferric oxide sludge as iron raw material |
| CN101116792A (en) * | 2007-09-13 | 2008-02-06 | 大连理工大学 | Technics of flue gas desulfurizing through catalytic oxidation method and by-product polymerizing iron sulfate through catalytic method |
| CN104591297A (en) * | 2015-01-09 | 2015-05-06 | 嘉兴艾尔瑞环境科技有限公司 | Method and device for preparing polymeric ferric sulfate |
| CN105692717A (en) * | 2016-03-21 | 2016-06-22 | 广西福斯特再生资源环保科技有限公司 | Polyferric sulfate and preparation method of polyferric sulfate |
| CN206985743U (en) * | 2017-07-11 | 2018-02-09 | 深圳市长隆科技有限公司 | A kind of bodied ferric sulfate continuous process system |
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