CN107867709A - A kind of processing technology for being concentrated by evaporation aqueous sodium persulfate solution crystallization - Google Patents
A kind of processing technology for being concentrated by evaporation aqueous sodium persulfate solution crystallization Download PDFInfo
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- CN107867709A CN107867709A CN201711304493.8A CN201711304493A CN107867709A CN 107867709 A CN107867709 A CN 107867709A CN 201711304493 A CN201711304493 A CN 201711304493A CN 107867709 A CN107867709 A CN 107867709A
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01D—COMPOUNDS OF ALKALI METALS, i.e. LITHIUM, SODIUM, POTASSIUM, RUBIDIUM, CAESIUM, OR FRANCIUM
- C01D5/00—Sulfates or sulfites of sodium, potassium or alkali metals in general
- C01D5/18—Dehydration
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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
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- Organic Chemistry (AREA)
- Engineering & Computer Science (AREA)
- Materials Engineering (AREA)
- Inorganic Chemistry (AREA)
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
Abstract
The invention discloses the processing technology that a kind of evaporation and concentration aqueous sodium persulfate solution of technical field of chemical crystallizes, the processing technology comprises the following steps that：S1：Pending metabisulfite solution is evaporated concentration；S2：Material enters forced-circulation evaporator, and afterwards into being separated in centrifuge, qualified mother liquor returns again to forced-circulation evaporator double evaporation-cooling；S3：Indirect steam is after gas-liquid separator, into Compressor Group；S4：Into MVR compressor reducers；S5：Temperature is down to 40 DEG C or so discharge systems；S6：Heat exchange evaporation is carried out, whole system reaches thermal balance, and the present invention makes the steam to be discarded originally just be fully utilized, latent heat is reclaimed, improving the thermal efficiency again reduces production cost, is not susceptible to plugging phenomenon, can accomplish the abundant reuse of indirect steam condensate.
Description
Technical field
The present invention relates to technical field of chemical, specially a kind of processing work for being concentrated by evaporation aqueous sodium persulfate solution crystallization
Skill.
Background technology
The processing technology of existing sulfate crystal uses Natural Circulation, and flow velocity of the material in heat exchanger tube is relatively low, at this
Plugging phenomenon easily occurs under kind flow velocity, while in evaporation process, due to the easy entrained liquid of solution, influences vapour compression machine
Even running.To be come into operation therefore, we have proposed a kind of processing technology for being concentrated by evaporation aqueous sodium persulfate solution crystallization, with solution
Certainly above mentioned problem.
The content of the invention
It is above-mentioned to solve it is an object of the invention to provide a kind of processing technology for being concentrated by evaporation aqueous sodium persulfate solution crystallization
The problem of being proposed in background technology.
To achieve the above object, the present invention provides following technical scheme：It is a kind of to be concentrated by evaporation what aqueous sodium persulfate solution crystallized
Processing technology, the processing technology comprise the following steps that：
S1：Pending metabisulfite solution adjusts PH between 5-6 in neutralizing tank, and metabisulfite solution comes out from neutralizing tank tank,
By condensate preheating unit preheating, feeding temperature is set to squeeze into evaporation unit close to evaporating temperature by feed pump, be evaporated dense
Contracting；
S2：Material enters forced-circulation evaporator, constantly circulation concentration process in reach hypersaturated state, afterwards enter from
Separated in scheming, obtain sodium sulfate crystal and mother liquor, qualified mother liquor returns again to forced-circulation evaporator double evaporation-cooling；
S3：For indirect steam on the top of forced-circulation evaporator after gas-liquid separator, the indirect steam after separation enters pressure
Contracting machine unit；
S4：The indirect steam come out from gas-liquid separator, into MVR compressor reducers, indirect steam intake air temperature is 85 DEG C and compressed
Afterwards, temperature can be increased to 101 DEG C or so, and the steam after compression enters back into forced-circulation evaporator heated material；
S5：During heated material, steam that this portion temperature is about 101 DEG C is condensed into that water flow to cooling unit and circulation is cold
But water exchanges heat, and temperature is down to 40 DEG C or so discharge systems；
S6：101 DEG C of steam is increased to after material enters evaporator, and after compression and carries out heat exchange evaporation, whole system reaches heat
Balance.
Preferably, in the step S1, condensate temperature is 85 DEG C, and flow hourly is 5400kg/h, effectively heat transfer temperature
Poor 25.4 DEG C, the heat exchanger for being designed as 2 50 ㎡ is combined as a preheating unit.
Preferably, in the step S2, forced-circulation evaporator evaporation capacity hourly is 5400kg, forced circulation steam
Density is 0.2531kg/m3, and it is 2--5m/s to control gas flow rate, and forced-circulation evaporator diameter design is 2200mm, forces to follow
Ring evaporator tube Partial Height is designed as 4000mm, and using the design of upper cover conical structures.
Preferably, in the step S2, when the liquid level in forced-circulation evaporator is less than certain liquid level, internally piloted valve is fed
Unlatching starts to feed, and when the liquid level of material is higher than setting value, material inlet valve is closed, and stops charging.
Preferably, in the step S2, when being controlled to the solution temperature of forced-circulation evaporator, setting is corresponding true
Reciprocal of duty cycle, temperature of charge, which reaches boiling point corresponding to vacuum, to be evaporated, and using the evaporating temperature of material as feedback signal, steamed when raw
Temperature of charge is risen to evaporating temperature by vapour, and steam control valve may turn off, but temperature of charge is less than evaporating temperature, steam control valve
It may turn on, as compensation heat loss.
Compared with prior art, the beneficial effects of the invention are as follows：The present invention utilizes caused indirect steam in evaporator, warp
Compressor compresses, pressure, temperature is allowed to raise, heat content increase, the heating chamber for being then then sent through evaporator uses as heating steam,
Processed feed liquid is maintained fluidized state, and heat steam and be then condensed into water in itself, the steam to be discarded originally is just obtained
Sufficient utilization, has reclaimed latent heat, improving the thermal efficiency again reduces production cost；
The present invention uses the evaporation technology of forced circulation, and flow velocity of the material in heat exchanger tube reaches 1.5--2m/s, in this flow velocity
Under be not susceptible to plugging phenomenon；
Present invention design gas-liquid separator is thoroughly separated to indirect steam, is ensured into the pure of the secondary steam of compressor
Only, so as to be effectively protected the cleaning of the steady and indirect steam condensate of vapour compression machine high-speed cruising, secondary steaming can be accomplished
The abundant reuse of vapor condensed water.
Brief description of the drawings
Fig. 1 is processing process figure of the present invention.
Embodiment
Below in conjunction with the accompanying drawing in the embodiment of the present invention, the technical scheme in the embodiment of the present invention is carried out clear, complete
Site preparation describes, it is clear that described embodiment is only part of the embodiment of the present invention, rather than whole embodiments.It is based on
Embodiment in the present invention, those of ordinary skill in the art are obtained every other under the premise of creative work is not made
Embodiment, belong to the scope of protection of the invention.
Referring to Fig. 1, the present invention provides a kind of technical scheme：A kind of processing work for being concentrated by evaporation aqueous sodium persulfate solution crystallization
Skill, the processing technology comprise the following steps that：
S1：Pending metabisulfite solution adjusts PH between 5-6 in neutralizing tank, and metabisulfite solution comes out from neutralizing tank tank,
By condensate preheating unit preheating, feeding temperature is set to squeeze into evaporation unit close to evaporating temperature by feed pump, be evaporated dense
Contracting, condensate temperature are 85 DEG C, and flow hourly is 5400kg/h, effective 25.4 DEG C of heat transfer temperature difference, are designed as 2 50 ㎡'s
Heat exchanger is combined as a preheating unit；
S2：Material enters forced-circulation evaporator, constantly circulation concentration process in reach hypersaturated state, afterwards enter from
Separated in scheming, obtain sodium sulfate crystal and mother liquor, qualified mother liquor returns again to forced-circulation evaporator double evaporation-cooling, forces
Circulating evaporator evaporation capacity hourly is 5400kg, and forced circulation vapour density is 0.2531kg/m3, controls the gas flow rate to be
2--5m/s, forced-circulation evaporator diameter design are 2200mm, and forced-circulation evaporator shell portion is highly designed as
4000mm, and using the design of upper cover conical structures, when the liquid level in forced-circulation evaporator is less than certain liquid level, enter
Material internally piloted valve starts to feed, and when the liquid level of material is higher than setting value, material inlet valve is closed, and stops charging, and pressure is followed
When the solution temperature of ring evaporator is controlled, corresponding vacuum is set, temperature of charge reaches boiling point corresponding to vacuum just
It can evaporate, using the evaporating temperature of material as feedback signal, when temperature of charge is risen to evaporating temperature, steam control valve by raw steam
It may turn off, but temperature of charge is less than evaporating temperature, and steam control valve may turn on, as compensation heat loss；
S3：For indirect steam on the top of forced-circulation evaporator after gas-liquid separator, the indirect steam after separation enters pressure
Contracting machine unit；
S4：The indirect steam come out from gas-liquid separator, into MVR compressor reducers, indirect steam intake air temperature is 85 DEG C and compressed
Afterwards, temperature can be increased to 101 DEG C or so, and the steam after compression enters back into forced-circulation evaporator heated material；
S5：During heated material, steam that this portion temperature is about 101 DEG C is condensed into that water flow to cooling unit and circulation is cold
But water exchanges heat, and temperature is down to 40 DEG C or so discharge systems；
S6：101 DEG C of steam is increased to after material enters evaporator, and after compression and carries out heat exchange evaporation, whole system reaches heat
Balance.
Although an embodiment of the present invention has been shown and described, for the ordinary skill in the art, can be with
A variety of changes, modification can be carried out to these embodiments, replace without departing from the principles and spirit of the present invention by understanding
And modification, the scope of the present invention is defined by the appended.
Claims (5)
- A kind of 1. processing technology for being concentrated by evaporation aqueous sodium persulfate solution crystallization, it is characterised in that：The specific steps of the processing technology It is as follows：S1：Pending metabisulfite solution adjusts PH between 5-6 in neutralizing tank, and metabisulfite solution comes out from neutralizing tank tank, By condensate preheating unit preheating, feeding temperature is set to squeeze into evaporation unit close to evaporating temperature by feed pump, be evaporated dense Contracting；S2：Material enters forced-circulation evaporator, constantly circulation concentration process in reach hypersaturated state, afterwards enter from Separated in scheming, obtain sodium sulfate crystal and mother liquor, qualified mother liquor returns again to forced-circulation evaporator double evaporation-cooling；S3：For indirect steam on the top of forced-circulation evaporator after gas-liquid separator, the indirect steam after separation enters pressure Contracting machine unit；S4：The indirect steam come out from gas-liquid separator, into MVR compressor reducers, indirect steam intake air temperature is 85 DEG C and compressed Afterwards, temperature can be increased to 101 DEG C or so, and the steam after compression enters back into forced-circulation evaporator heated material；S5：During heated material, steam that this portion temperature is about 101 DEG C is condensed into that water flow to cooling unit and circulation is cold But water exchanges heat, and temperature is down to 40 DEG C or so discharge systems；S6：101 DEG C of steam is increased to after material enters evaporator, and after compression and carries out heat exchange evaporation, whole system reaches heat Balance.
- A kind of 2. processing technology for being concentrated by evaporation aqueous sodium persulfate solution crystallization according to claim 1, it is characterised in that：Institute State in step S1, condensate temperature is 85 DEG C, and flow hourly is 5400kg/h, effective 25.4 DEG C of heat transfer temperature difference, is designed as 2 50 ㎡ heat exchanger is combined as a preheating unit.
- A kind of 3. processing technology for being concentrated by evaporation aqueous sodium persulfate solution crystallization according to claim 1, it is characterised in that：Institute State in step S2, forced-circulation evaporator evaporation capacity hourly is 5400kg, and forced circulation vapour density is 0.2531kg/m 3, it is 2--5m/s to control gas flow rate, and forced-circulation evaporator diameter design is 2200mm, forced-circulation evaporator shell portion 4000mm is highly designed as, and using the design of upper cover conical structures.
- A kind of 4. processing technology for being concentrated by evaporation aqueous sodium persulfate solution crystallization according to claim 1, it is characterised in that：Institute State in step S2, when the liquid level in forced-circulation evaporator is less than certain liquid level, charging internally piloted valve starts to feed, and works as thing When the liquid level of material is higher than setting value, material inlet valve is closed, and stops charging.
- A kind of 5. processing technology for being concentrated by evaporation aqueous sodium persulfate solution crystallization according to claim 1, it is characterised in that：Institute State in step S2, when being controlled to the solution temperature of forced-circulation evaporator, set corresponding vacuum, temperature of charge reaches Boiling point corresponding to vacuum will evaporate, using the evaporating temperature of material as feedback signal, when raw steam rises to temperature of charge Evaporating temperature, steam control valve may turn off, but temperature of charge is less than evaporating temperature, and steam control valve may turn on, as benefit Repay heat loss.
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| CN201711304493.8A CN107867709A (en) | 2017-12-11 | 2017-12-11 | A kind of processing technology for being concentrated by evaporation aqueous sodium persulfate solution crystallization |
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| CN201711304493.8A CN107867709A (en) | 2017-12-11 | 2017-12-11 | A kind of processing technology for being concentrated by evaporation aqueous sodium persulfate solution crystallization |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109550274A (en) * | 2018-12-13 | 2019-04-02 | 云南锡业股份有限公司化工材料分公司 | A kind of highly acidity thermal crystalline substance continuous crystallisation device |
| CN112707417A (en) * | 2021-01-14 | 2021-04-27 | 江苏赛德力制药机械制造有限公司 | Sodium sulfate and sodium chloride salt separation method |
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| CN101966997A (en) * | 2010-10-29 | 2011-02-09 | 江苏瑞普膜技术有限公司 | Process and device for producing pyrotechnite from sodium sulfate decahydrate |
| CN102936075A (en) * | 2012-11-13 | 2013-02-20 | 常州大学 | Method for recycling industrial wastewater generated during alanine production |
| CN203425552U (en) * | 2013-07-24 | 2014-02-12 | 深圳市捷晶能源科技有限公司 | Concentration and crystallization equipment for sodium sulfite |
| CN106587477A (en) * | 2016-12-21 | 2017-04-26 | 北京燕山翔宇环保工程技术有限公司 | System and method for treating industrial waste lye |
| CN106698481A (en) * | 2016-12-15 | 2017-05-24 | 袁超鹏 | Device and method for environmental-protection recycling of solid wastes in production process of sodium sulfide |
-
2017
- 2017-12-11 CN CN201711304493.8A patent/CN107867709A/en active Pending
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101966997A (en) * | 2010-10-29 | 2011-02-09 | 江苏瑞普膜技术有限公司 | Process and device for producing pyrotechnite from sodium sulfate decahydrate |
| CN102936075A (en) * | 2012-11-13 | 2013-02-20 | 常州大学 | Method for recycling industrial wastewater generated during alanine production |
| CN203425552U (en) * | 2013-07-24 | 2014-02-12 | 深圳市捷晶能源科技有限公司 | Concentration and crystallization equipment for sodium sulfite |
| CN106698481A (en) * | 2016-12-15 | 2017-05-24 | 袁超鹏 | Device and method for environmental-protection recycling of solid wastes in production process of sodium sulfide |
| CN106587477A (en) * | 2016-12-21 | 2017-04-26 | 北京燕山翔宇环保工程技术有限公司 | System and method for treating industrial waste lye |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109550274A (en) * | 2018-12-13 | 2019-04-02 | 云南锡业股份有限公司化工材料分公司 | A kind of highly acidity thermal crystalline substance continuous crystallisation device |
| CN112707417A (en) * | 2021-01-14 | 2021-04-27 | 江苏赛德力制药机械制造有限公司 | Sodium sulfate and sodium chloride salt separation method |
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