CN105329923A - Crystallization process of magnesium method flue gas desulfurization by-product magnesium sulfate - Google Patents
Crystallization process of magnesium method flue gas desulfurization by-product magnesium sulfate Download PDFInfo
- Publication number
- CN105329923A CN105329923A CN201510787380.2A CN201510787380A CN105329923A CN 105329923 A CN105329923 A CN 105329923A CN 201510787380 A CN201510787380 A CN 201510787380A CN 105329923 A CN105329923 A CN 105329923A
- Authority
- CN
- China
- Prior art keywords
- magnesium sulfate
- temperature
- water
- prolong
- retort
- 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.)
- Granted
Links
Classifications
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01F—COMPOUNDS OF THE METALS BERYLLIUM, MAGNESIUM, ALUMINIUM, CALCIUM, STRONTIUM, BARIUM, RADIUM, THORIUM, OR OF THE RARE-EARTH METALS
- C01F5/00—Compounds of magnesium
- C01F5/40—Magnesium sulfates
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Life Sciences & Earth Sciences (AREA)
- Geology (AREA)
- Inorganic Chemistry (AREA)
- Treating Waste Gases (AREA)
Abstract
The invention provides a crystallization process of magnesium method flue gas desulfurization by-product magnesium sulfate. We unceasingly test and actually apply the process, a cold crystallizing process performed through circulating cooling water of a compressed air cooling tower is ereached and developed according to the physical characteristic that magnesium sulfate can be separated out by crystallization at the temperature of 25 DEG C or lower, magnesium sulfate is crystallized at normal temperature by lowering the temperature of desulfurizing liquid to be 25 DEGC or lower, a good effect is achieved in actual application, and the defects that according to a three-effect evaporation and crystallization process, pipes can be blocked easily, energy consumption is large, and safety is not sufficient are overcome.
Description
Technical field
The present invention relates to a kind of complete processing of industrially desulfurized byproduct, be specifically related to a kind of magnesium method flue gas desulphurization byproduct magnesium sulfate crystallization processes.
Background technology
Along with national environmental protection requires increasingly strict, will have higher requirement to steel industry pollution emission reduction, particularly steel industry air contaminant treatment task during " 12 " is heavy and arduous, and it is quite severe that sulfurous gas reduces discharging situation.
Current flue gas desulfurization major part adopts wet-type calcium desulfuration mode, and calcium method advantage is technology maturation, but shortcoming is also many: by-product utilization be worth low, mist eliminator easily stifled, equipment is perishable and serious wear, liquid-gas ratio is large, cycling use of water amount is large, it is high to consume energy.
According to sinter fume fluctuation and smoke pollution composition feature; and international community's environmental pollution administers the change required; in conjunction with the requirement of China " 12 " period to environment protection, and international environmental protection development trend, according to the SO produced in domestic sintering flue gas desulfurization generation skill
2, Dioxins, particulate matter, NOX, SO
3, the multiple pollutant such as HF, HCl comprehensive treating process, we have selected wet-type magnesium method flue gas desulfurization technique.
The temperature of magnesium sulfate waste liquid after desulfurization after removal of impurities is about 30 DEG C, and the content of magnesium sulfate is about 12%, and waste liquid enters triple-effect evaporator and carries out evaporation concentration after two-stage preheater preheats, is concentrated into saturated solution, is delivered to draft tube baffle crystallizer by discharging pump; Saturated solution of magnesium sulfate decrease temperature crystalline in crystallizer forms magnesium sulfate heptahydrate crystal, and crystallization solution is after centrifugation, and mother liquor Returning evaporimeter continues evaporation concentration, and isolated crystallization enters fluidized-bed and carries out drying, and last magnesium sulfate heptahydrate product is packed.Raw steam enters the shell side heat exchange condensation of an effect heating chamber after heat pump decompression, and water of condensation enters triple-effect evaporator waste heat recycling; The secondary steam part that one effect separate chamber produces is returned the shell side of an effect heating chamber after heat pump suction, compression, all the other secondary steams enter 2nd effect evaporator heat exchange condensation, and water of condensation enters triple-effect evaporator recycling; The secondary steam that two effect separate chambers produce enters triple-effect evaporator heat exchange condensation, and water of condensation enters condensate water pot recycling; The secondary steam that end effect produces enters indirect condenser and carries out condensation recovery.
The evaporation flow process of triple effect heat pump:
The temperature of the secondary steam that 1st effective evaporator produces, the lower of pressure ratio life steam, consume a part of high pressure, the pressure of part secondary steam is improved by heat pump by high-temperature steam, its temperature is also by corresponding improve, replace raw steam as the thermal source of 1st effective evaporator the secondary steam improved after pressure, remaining secondary steam is as the thermal source of lower 1st effective evaporator; Triple effect evaporation system adds the consumption that heat pump saves steam to a great extent.
The temperature that magnesium sulfate waste liquid enters vapo(u)rization system is 30 DEG C, utilize the secondary steam of triple-effect evaporator, by exhaust steam preheater, waste liquid is preheating to 50-60 DEG C, waste liquid is preheated to 70-90 DEG C by the water of condensation of recycling 1st effective evaporator, improve the temperature that waste liquid enters 1st effective evaporator, reduce the area of 1st effective evaporator and indirect condenser, used heat is utilized.
Liquid between each single-effect evaporator be by effect between pressure difference carry out carrying, investment and the power consumption of section of tubing and handling equipment between each effect can be decreased.
Vaporizer all adopts forced circulation type vaporizer, forced circulation pump is utilized between heating chamber and separate chamber, to form the impellent of circulation as liquid, control the circulation velocity of liquid in heating tube between 1.2-3.0m/s, avoid liquid local superheating or concentration in vaporizer excessively to cause fouling, scab.
Due in magnesium sulfate waste liquid containing certain impurity, in evaporative process, create a part of problem, such as: heat exchange pipe of evaporator fouling, the system continuous cycle of operation is short, energy consumption is high.When cooling water pressure is inadequate, easily cause vacuum degree deficiency; When steam is unstable, easily produce foam.Equipment is once break down, and maintenance cost is large, and there is air pressure due to equipment component, and belong to pressurized vessel, the potential safety hazard of existence is large.
The byproduct magnesium sulfate produced in wet-type magnesium method desulfurization technique is mainly with crystallization mode output.We are in conjunction with finding in practice that this crystallization processes exists many problems, and for overcoming the many shortcomings in triple effect evaporation crystallization processes, we newly develop a kind of water-cooled crystallization processes, overcome the shortcoming in triple effect evaporation crystallization processes, and have saved running cost.
Summary of the invention
For the shortcoming such as solve triple effect evaporation crystallization processes easy plugging, energy consumption is large, security is not enough, the invention provides a kind of magnesium method flue gas desulphurization byproduct magnesium sulfate crystallization processes.
The present invention through us by continuous experiment and practice, according to magnesium sulfate can when temperature is below 25 DEG C the physical property of crystallization.Develop and a set ofly utilize the solubility curve of magnesium sulfate by pressure-air cooling tower recirculated cooling water cold crystallization technique, make magnesium sulfate crystallization by reducing below doctor solution temperature to 25 DEG C at normal temperatures, and in actual motion, achieve good effect.
Core of the present invention is: magnesium sulfate slurry temperature about 50 DEG C out from thionizer 1, overboard pump is input to plate-and-frame filter press 2 and filters, filtrate water is delivered to retort 3 through filtrate water pump by the filtered liquid after filtration, by adding a small amount of reagent 10 in retort 3, by Adlerika concentrate, flow into crystallizer 5 close to saturated Adlerika after concentrate and form magnesium sulfate magma.All arrange ring stainless steel prolong 11 and agitator in retort 3, crystallizer 5 and discharge tank 6, prolong uses the recirculated cooling water in cooling tower 9, and recirculated cooling water is recycled to cooling tower 9 after being risen by ring stainless steel prolong temperature again.Adopt compressed air refrigeration to lower the temperature to recirculated water in cooling tower 9, cooling Posterior circle water is cooled doctor solution by prolong again, by continuous circulating cooling, after making doctor solution temperature be down to 25 DEG C, is delivered to discharge tank 6.After fluid temperature is reduced to about 20 DEG C, with discharging pump, magnesium sulfate magma is squeezed into whizzer 7 and dewater.The crystal of magnesium sulfate after dehydration is after the blanking of whizzer 7 discharge port, and pack with closer 8, the mother liquor that whizzer 7 separates reenters mother liquor tank 4.Mother liquor returns in retort 3 and recycles by mother liquor pump.
Reagent 10 alleged by the present invention refers to the vitriol oil and magnesium oxide.
Two kinds of process operation Cost comparisons (calculating with 126m3/h exhaust gas volumn)
marginal data:
Fig. 1 is magnesium method flue gas desulphurization byproduct magnesium sulfate crystallization processes schema
In figure: 1-thionizer; 2-plate-and-frame filter press; 3-retort; 4-mother liquor tank; 5-crystallizer; 6-discharge tank; 7-whizzer; 8-magnesium sulfate closer; 9-circulating cooling tower; 10-reagent; 11-stainless steel condensate pipe.
specific embodiment:
First, assemble by process flow sheet, then run.I.e. magnesium sulfate slurries out from thionizer 1, be input to plate-and-frame filter press 2 by overboard pump to filter, filtrate water is delivered to retort 3 through filtrate water pump by the filtered liquid after filtration, by adding a small amount of reagent 10 in retort 3, by Adlerika concentrate, flow into crystallizer 5 close to saturated Adlerika after concentrate and form magnesium sulfate magma.In retort 3, crystallizer 5 and discharge tank 6, ring stainless steel prolong 11 and agitator are all set.Prolong uses the recirculated cooling water in cooling tower 9, and recirculated cooling water is recycled to cooling tower 9 after being risen by ring stainless steel prolong temperature again.Adopt compressed air refrigeration to lower the temperature to recirculated water in cooling tower 9, cooling Posterior circle water is cooled doctor solution by prolong again, by continuous circulating cooling, after making doctor solution temperature be down to 25 DEG C, is delivered to discharge tank 6.In discharge tank 6, ring stainless steel prolong and agitator are set equally, after fluid temperature is reduced to about 20 DEG C, with discharging pump, magnesium sulfate magma is squeezed into whizzer 7 and dewater.The crystal of magnesium sulfate after dehydration is after the blanking of whizzer 7 discharge port, and pack with closer 8, the mother liquor that whizzer 7 separates reenters mother liquor tank 4.Mother liquor returns in retort 3 and recycles by mother liquor pump.
Claims (1)
1. magnesium method flue gas desulphurization byproduct magnesium sulfate crystallization processes, it is characterized in that: from thionizer (1), magnesium sulfate slurries are out input to plate-and-frame filter press (2) through overboard pump and filter, filtrate water is delivered to retort (3) through filtrate water pump by the filtered liquid after filtration, by adding a small amount of reagent (10) in retort (3), by Adlerika concentrate, flow into crystallizer (5) close to saturated Adlerika after concentrate and form magnesium sulfate magma, retort (3), in crystallizer (5) and discharge tank (6), ring stainless steel prolong (11) and agitator are all set, prolong uses recirculated cooling water, after recirculated cooling water is risen by ring stainless steel prolong temperature, be recycled to cooling tower (9), compressed air refrigeration is adopted to lower the temperature to recirculated water in cooling tower (9), cooling Posterior circle water is cooled doctor solution by prolong again, by continuous circulating cooling, after making doctor solution temperature be down to 25 DEG C, be delivered to discharge tank (6), discharge tank arranges ring stainless steel prolong and agitator in (6) equally, after fluid temperature is reduced to about 20 DEG C, with discharging pump, magnesium sulfate magma is squeezed into whizzer (7) dehydration, the crystal of magnesium sulfate after dehydration is after whizzer (7) discharge port blanking, pack with closer (8), the mother liquor that whizzer (7) separates reenters mother liquor tank (4), mother liquor is returned to recycling in retort (3) by mother liquor pump.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201510787380.2A CN105329923B (en) | 2015-11-17 | 2015-11-17 | Crystallization process of magnesium method flue gas desulfurization by-product magnesium sulfate |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201510787380.2A CN105329923B (en) | 2015-11-17 | 2015-11-17 | Crystallization process of magnesium method flue gas desulfurization by-product magnesium sulfate |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN105329923A true CN105329923A (en) | 2016-02-17 |
| CN105329923B CN105329923B (en) | 2017-01-25 |
Family
ID=55280730
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201510787380.2A Active CN105329923B (en) | 2015-11-17 | 2015-11-17 | Crystallization process of magnesium method flue gas desulfurization by-product magnesium sulfate |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN105329923B (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108706613A (en) * | 2018-08-06 | 2018-10-26 | 山东大学 | A kind of system and method preparing magnesium sulfate using steam source cycle |
Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1148516A (en) * | 1996-08-08 | 1997-04-30 | 刘家栋 | Continuously self-cooling crystalizing technology |
| CN101407325A (en) * | 2008-11-11 | 2009-04-15 | 大连市中山区鑫阳矿业化工研究所 | Method for separating boric acid and magnesium sulphate in boric acid production mother liquor by using magnesium sulphate |
| CN101423234A (en) * | 2008-11-27 | 2009-05-06 | 六合天融（北京）环保科技有限公司 | Process for preparing heptahydrate magnesium sulfate and liquid sulphur dioxide |
| CN101549210A (en) * | 2008-04-03 | 2009-10-07 | 上海瑞惠机械设备制造有限公司 | Fume wet-type magnesia desulfated waste-liquid recovery method |
| CN102205201A (en) * | 2011-06-10 | 2011-10-05 | 赵玉斌 | Recovering process for desulphurized ammonium sulfate/magnesium sulfate |
| CN103382035A (en) * | 2013-08-01 | 2013-11-06 | 河北诺达化工设备有限公司 | Magnesium sulfate heptahydrate producing process with fully-continuous method |
| CN104058429A (en) * | 2014-07-04 | 2014-09-24 | 中节能六合天融环保科技有限公司 | Method for magnesium sulfate continuous crystallization |
-
2015
- 2015-11-17 CN CN201510787380.2A patent/CN105329923B/en active Active
Patent Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1148516A (en) * | 1996-08-08 | 1997-04-30 | 刘家栋 | Continuously self-cooling crystalizing technology |
| CN101549210A (en) * | 2008-04-03 | 2009-10-07 | 上海瑞惠机械设备制造有限公司 | Fume wet-type magnesia desulfated waste-liquid recovery method |
| CN101407325A (en) * | 2008-11-11 | 2009-04-15 | 大连市中山区鑫阳矿业化工研究所 | Method for separating boric acid and magnesium sulphate in boric acid production mother liquor by using magnesium sulphate |
| CN101423234A (en) * | 2008-11-27 | 2009-05-06 | 六合天融（北京）环保科技有限公司 | Process for preparing heptahydrate magnesium sulfate and liquid sulphur dioxide |
| CN102205201A (en) * | 2011-06-10 | 2011-10-05 | 赵玉斌 | Recovering process for desulphurized ammonium sulfate/magnesium sulfate |
| CN103382035A (en) * | 2013-08-01 | 2013-11-06 | 河北诺达化工设备有限公司 | Magnesium sulfate heptahydrate producing process with fully-continuous method |
| CN104058429A (en) * | 2014-07-04 | 2014-09-24 | 中节能六合天融环保科技有限公司 | Method for magnesium sulfate continuous crystallization |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108706613A (en) * | 2018-08-06 | 2018-10-26 | 山东大学 | A kind of system and method preparing magnesium sulfate using steam source cycle |
Also Published As
| Publication number | Publication date |
|---|---|
| CN105329923B (en) | 2017-01-25 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN104445306B (en) | Manufacture the apparatus and method of magnesium sulfate | |
| CN101665301A (en) | Resource treatment method for hydrochloric acid pickling waste liquor | |
| CN103936220A (en) | Zero discharge treatment process of saline sewage produced by refining | |
| CN103552992A (en) | System and method for preparing acid by using sulfur-containing wastewater through dry method | |
| CN104495886A (en) | Device and method for producing magnesium sulfate | |
| CN106377993B (en) | SO in pyrolusite slurry desorption flue gas 2 And method and device for recycling thereof | |
| CN108117210B (en) | Treatment method and treatment device for flue gas desulfurization waste liquid | |
| CN102887529B (en) | Ammonium sulfate production system and preparation method thereof | |
| CN102806004A (en) | Magnesium desulfurization byproduct recovery process | |
| CN106512450A (en) | Miniaturized energy-saving evaporative regeneration device | |
| CN206381655U (en) | Minimize energy-saving evaporation regenerating unit | |
| CN105329923A (en) | Crystallization process of magnesium method flue gas desulfurization by-product magnesium sulfate | |
| CN108658353B (en) | Calcium chloride wastewater treatment process | |
| CN209922933U (en) | Sodium chloride forced circulation crystallization device in flue gas desulfurization waste water | |
| CN111672879A (en) | Waste salt recycling system and method based on energy conservation and environment protection integration of thermal power plant | |
| CN104016382B (en) | Flue gas is carried out the method that desulfurization produces sodium sulfite by a kind of Dual alkali | |
| WO2019001430A1 (en) | Treatment system and method for process for preparing magnesium sulfate heptahydrate through refining by-product from desulfurization by magnesium oxide | |
| CN104445275B (en) | A kind of recycle the technique that gas cleaning waste liquid prepares ammonium salt | |
| CN209338304U (en) | A kind of waste heat vaporation-type desulfurization wastewater Zero discharging system | |
| CN103848443B (en) | Sodium nitrate/sodium nitrite produces steam self-support system | |
| CN112279443A (en) | System and method for simultaneously concentrating desulfurized saline wastewater and relieving' white smoke | |
| CN205556134U (en) | Energy -concerving and environment -protective type red fuming nitric acid (RFNA) production magnesium tail water recovery unit | |
| CN110627098A (en) | High-efficient environmental protection production system of solid polyaluminium chloride | |
| CN216445186U (en) | Heat pump heat supply and waste water evaporation crystallization integrated system driven by flue gas waste heat | |
| CN218740315U (en) | Prevent evaporation crystallization system outside ammonium sulfate tower of tube side jam |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant |