CN109173324A - A kind of potassium nitrate continuous crystallisation device and method - Google Patents
A kind of potassium nitrate continuous crystallisation device and method Download PDFInfo
- Publication number
- CN109173324A CN109173324A CN201811073246.6A CN201811073246A CN109173324A CN 109173324 A CN109173324 A CN 109173324A CN 201811073246 A CN201811073246 A CN 201811073246A CN 109173324 A CN109173324 A CN 109173324A
- Authority
- CN
- China
- Prior art keywords
- level
- pump
- dtb
- potassium nitrate
- mother liquor
- 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.)
- Pending
Links
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D9/00—Crystallisation
- B01D9/0018—Evaporation of components of the mixture to be separated
- B01D9/0022—Evaporation of components of the mixture to be separated by reducing pressure
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01D—COMPOUNDS OF ALKALI METALS, i.e. LITHIUM, SODIUM, POTASSIUM, RUBIDIUM, CAESIUM, OR FRANCIUM
- C01D9/00—Nitrates of sodium, potassium or alkali metals in general
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Crystallography & Structural Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Life Sciences & Earth Sciences (AREA)
- Agronomy & Crop Science (AREA)
- Engineering & Computer Science (AREA)
- Materials Engineering (AREA)
- Inorganic Chemistry (AREA)
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The present invention relates to a kind of potassium nitrate continuous crystallisation device and methods.Described device includes level-one DTB flash evaporation crystallizer, first degree crystalline discharging pump, level-one vapor jet vacuum pump, water pot A, water pump A, second level DTB flash evaporation crystallizer, second steam ejector vacuum pump, water pot B, water pump B, secondary crystallization discharging pump, cyclone, thickener, centrifuge, mother liquor tank, mother liquor pump；Described method includes following steps: primary flash crystallization, two-stage flash crystallization, rotary filter press, thickening, centrifuge separation, mother liquor are collected；A kind of potassium nitrate continuous crystallisation device and method of the present invention has the advantages that continuous production stable operation, can be enlarged, while can be relieved equipment and frequently blocking up, and extends the cleaning frequency, improves product yield and quality.
Description
Technical field
The invention belongs to chemical production technical fields, and in particular to a kind of potassium nitrate continuous crystallisation device and method.
Background technique
China's Production of Potassium Nitrate method, traditional cooling crystallization method of use mainly have natural cooling crystallization, collet cooling
Crystallization, the crystallization of coiled pipe crystallisation by cooling, misting cooling, self cooling crystallisation by cooling, these cooling crystallization methods belong to intermittent cooling crystallization
Mode, therefore cannot achieve automatic control, all manual operations, labor intensity is very big, and production scale is small, and energy consumption is high, and production efficiency is low.
Domestic existing potassium nitrate crystal, which there is no, at present realizes all fronts continous way operating method.
The existing potassium nitrate crystal method in China is larger using cooling water inflow, and summer coolant water temperature is high, can restrict life
It produces；Heat exchange surface degree of supersaturation is often excessive, it is difficult to realize uniformly cooling, cause grain size number uneven, and be easy to cause
Equipment blocking, the cleaning frequency is frequent, and product yield is low, and quality is bad.
Summary of the invention
In order to solve above-mentioned deficiency in the prior art, the present invention provides a kind of potassium nitrate continuous crystallisation device and sides
Method has the advantages that continuous production stable operation, can be enlarged, while can be relieved equipment and frequently blocking up, and extends the cleaning frequency, mentions
High product yield and quality.
The technical solution adopted by the present invention to solve the technical problems are as follows:
A kind of potassium nitrate continuous crystallisation device, including level-one DTB flash evaporation crystallizer, first degree crystalline discharging pump, level-one steam
Ejector vacuum pump, water pot A, water pump A, second level DTB flash evaporation crystallizer, second steam ejector vacuum pump, water pot B, water pump B, second level
Crystallize discharging pump, cyclone, thickener, centrifuge, mother liquor tank, mother liquor pump.
The feed inlet of the level-one DTB flash evaporation crystallizer is connect with feedstock transportation pipeline, and flash evaporation crystallizer is true using DTB type
Empty flash evaporation crystallizer, the discharge port connection first degree crystalline discharging pump feed inlet of the level-one DTB flash evaporation crystallizer, described one
Grade crystallization discharging pumps out material mouth and connect with the second level DTB flash evaporation crystallizer feed inlet, the second level DTB flash evaporation crystallizer discharging
Mouth is connect with the secondary crystallization discharging pump feed inlet, and the secondary crystallization discharging pump discharge port and the cyclone feed inlet connect
It connects, the cyclone supernatant discharge port is connect with the mother liquor tank supernatant feed inlet, the cyclone concentrate discharge port
It is connect with the thickener feed inlet, the thickener discharge port connects the centrifugation machine inlet, the discharge hole of centrifugal machine
It is connect with the mother liquor tank import, the mother liquor discharge port of the mother liquor tank is connect with mother liquor pump feed inlet, the mother liquor pump
Discharge port connects the feed inlet of lower one of evaporization process, and the discharge hole of centrifugal machine obtains potassium nitrate product；
The secondary gas outlet of the level-one DTB flash evaporation crystallizer connects the level-one vapor jet vacuum pump, the level-one
Vapor jet vacuum pump discharge connects the water pot A import, and the outlet water pot A is connect with the water pump A feed inlet, the water
Pump A water outlet is connect with subsequent processing import, and the secondary gas outlet of the second level DTB flash evaporation crystallizer connects the second steam
Ejector vacuum pump, the second steam ejector vacuum pump outlet connect the water pot B import, the outlet water pot B and the water
The connection of B feed inlet is pumped, the water pump B water outlet is connect with subsequent processing import.
Preferably, the level-one DTB flash evaporation crystallizer and the second level DTB flash evaporation crystallizer include: baffle plate, spiral shell
It revolves paddle, guide shell, eluriate leg.
The middle part of the crystallizer has the guide shell, and the surrounding of the crystallizer has the baffle plate, described to lead
There is the propeller close at lower end, the crystallizer lower part connects the elutriation leg in flow cartridge.
It is preferably in any of the above-described scheme, the shape for eluriating leg is barrel-shaped, a diameter of 100-800mm.It can be into
Row on-line rinsing realizes continuous production operation.
It is preferably in any of the above-described scheme, the dedicated propeller works revolving speed are as follows: 32-60r/min.This propeller is
Dedicated propeller, airscrew diameter is smaller, handles the material of same treating capacity, and the diameter of propeller is only the 0.7- of conventional equipment
0.8 times, manufacture difficulty reduces many compared with the prior art, realizes high-efficiency internal circulation, and material is avoided to distribute non-uniform problem, system
Hardly there is secondary nucleus in the crystal grain obtained.
It is preferably in any of the above-described scheme, handles the material of same treating capacity, the diameter of the spiral shell guide shell is only general
0.7-0.8 times of logical equipment.
The present invention also provides a kind of potassium nitrate continuous crystallisation process, characterized in that includes the following steps:
Step S1, primary flash crystallizes: the material that temperature is 48 DEG C being delivered into level-one DTB flash evaporation crystallizer and is followed
Ring flash distillation；
Step S2, two-stage flash crystallizes: material obtained in the step S1 being pumped into second level DTB flash evaporation crystallizer and is carried out
It flashes and crystallizes；
Step S3, rotary filter press: material obtained in the step S2 is delivered into cyclone and carries out rotary filter press, is obtained
To supernatant and bottom concentrate；
Step S4, it thickens: bottom concentrate obtained in the step S3 being entered into thickener and is thickened；
Step S5, it is centrifugated: material will be obtained in the step S4 and enter centrifuge being centrifuged, obtain solid
Potassium nitrate and potassium nitrate centrifuge mother liquor；
Step S6, mother liquor collect: will be obtained in supernatant obtained in the step S3 and the step S5 potassium nitrate from
Heart mother liquor, which is collected, enters mother liquor tank, handles wait enter next evaporization process.
The invention two-stage flash crystallizes process compared with single-stage process flow, and the cooling extent of every grade of vacuum crystallizer is 12-16
DEG C (single stage vacuum crystallization be 24-32 DEG C), low temperature become to reduce in internal circulating load, diameter and the blender for reducing inner draft tube be straight
Diameter reduces the manufacture difficulty of agitating paddle, and material can also be avoided to distribute non-uniform problem, realizes continuous production, especially suitable
Production for potassium nitrate in fertilizer industry.
Preferably, temperature control is at 32 DEG C in primary flash crystallizer in the step S1, vacuum degree 97.7KPa.
It is preferably in any of the above-described scheme, temperature control is at 20 DEG C in two-stage flash crystallizer in the step S2, very
Reciprocal of duty cycle is 99.7KPa.
It is preferably in any of the above-described scheme, the solid content content of the material come out after thickener is entered in the step S4
Control is 45%.
It is preferably in any of the above-described scheme, it is above-mentioned to implement using any of the above-described potassium nitrate continuous crystallisation device
Any potassium nitrate continuous crystallisation process.
The present invention also provides a kind of potassium nitrate continuous crystallisation process, which is characterized in that uses above-mentioned one nitric acid of meaning
Potassium continuous crystallisation device.
Compared with prior art, the invention has the following advantages:
1, a kind of potassium nitrate continuous crystallisation device in the present invention；The present apparatus can carry out potassium nitrate continuous production operation, tool
Have equipment it is stable, can enlargement, reasonable structure design can be relieved the problem that equipment is frequently blocked up to make the equipment cleaning frequency prolong
It is long.Crystalliser feet can carry out on-line rinsing equipped with leg is eluriated, and realize continuous production operation；Dedicated propeller is developed, is realized
High-efficiency internal circulation, and hardly there is secondary nucleus；It is used in series using two-stage DTB flash evaporation crystallizer, reduces cooling water
Usage amount solves the high bottleneck of summer water temperature；Low-temperature gradient can reduce the diameter and stirrer diameter of inner draft tube, reduce
The manufacture difficulty of agitating paddle can also avoid material from distributing non-uniform problem, and obtained grain size number is uniform, residence time contracting
It is short, improve the quality of yield and product.
2, one of present invention potassium nitrate continuous crystallisation process, using a kind of successive flash vaporization method for crystallising, between overcoming
It has a rest all disadvantages of operation；Crystalliser feet can carry out on-line rinsing equipped with leg is eluriated, and realize continuous production operation；It develops
Dedicated propeller realizes high-efficiency internal circulation, and secondary nucleus hardly occurs；Using two-stage DTB flash crystallization method, reduce
Cooling water usage amount solves the high bottleneck of summer water temperature and to solve heat exchange surface degree of supersaturation often excessive, it is difficult to real
It is now uniformly cooling, cause grain size number uneven, and be easy to cause blocking, the cleaning frequency is frequent, and product yield is low, and quality is not
Well the shortcomings that equal conventional methods, obtained product grain size number is uniform, shorter residence time, improves the quality of yield and product.
This method has the advantages that continuous production stable operation, can be enlarged, while can be relieved equipment and frequently blocking up, and extends cleaning week
Phase improves product yield and quality.
Detailed description of the invention
Fig. 1 is a kind of structural schematic diagram of potassium nitrate continuous crystallisation device of the embodiment of the present invention；
Fig. 2 is a kind of DTB flash evaporation crystallizer apparatus structure schematic diagram of the embodiment of the present invention.
Explanation: 1- level-one DTB flash evaporation crystallizer, 2- first degree crystalline discharging pump, 3- level-one vapor jet vacuum is marked in figure
Pump, 4- water pot A, 5- water pump A, 6- second level DTB flash evaporation crystallizer, 7- second steam ejector vacuum pump, 8- water pot B, 9- water pump B,
10- secondary crystallization discharging pump, 11- cyclone, 12- thickener, 13- centrifuge, 14- mother liquor tank, 15- mother liquor pump, 16- baffling
Plate, 17- propeller, 18- guide shell, 19- eluriate leg.
Specific embodiment
The application is described in further detail with reference to the accompanying drawings and examples.It is understood that this place is retouched
The specific embodiment stated is used only for explaining related invention, rather than the restriction to the invention.It also should be noted that in order to
Convenient for description, part relevant to invention is illustrated only in attached drawing.
It should be noted that in the absence of conflict, the features in the embodiments and the embodiments of the present application can phase
Mutually combination.The application is described in detail below with reference to the accompanying drawings and in conjunction with the embodiments.
As shown in Figure 1, a kind of potassium nitrate continuous crystallisation device, including the discharging of level-one DTB flash evaporation crystallizer 1, first degree crystalline
Pump 2, level-one vapor jet vacuum pump 3, water pot A4, water pump A5, second level DTB flash evaporation crystallizer 6, second steam ejector vacuum pump 7,
Water pot B8, water pump B9, secondary crystallization discharging pump 10, cyclone 11, thickener 12, centrifuge 13, mother liquor tank 14, mother liquor pump 15.
Feedstock transportation pipeline is connect with the feed inlet of level-one DTB flash evaporation crystallizer 1, the discharging of level-one DTB flash evaporation crystallizer 1
Mouth connection 2 feed inlet of first degree crystalline discharging pump, 2 discharge port of first degree crystalline discharging pump and 6 feed inlet of second level DTB flash evaporation crystallizer connect
It connects, 6 discharge port of second level DTB flash evaporation crystallizer is connect with 10 feed inlet of secondary crystallization discharging pump, and secondary crystallization discharging pump 10 discharges
Mouth is connect with 11 feed inlet of cyclone, and 11 supernatant discharge port of cyclone is connect with 14 supernatant feed inlet of mother liquor tank, cyclone
11 concentrate discharge ports are connect with 12 feed inlet of thickener, and 12 discharge port of thickener connects 13 feed inlet of centrifuge, centrifuge 13
Discharge port is connect with 14 import of mother liquor tank, and the mother liquor discharge port of mother liquor tank 14 pumps 15 feed inlets with mother liquor and connect, and mother liquor pump 15 goes out
Material mouth connects the feed inlet of lower one of evaporization process, and 13 discharge port of centrifuge obtains potassium nitrate product；
The secondary gas outlet connection level-one vapor jet vacuum of level-one DTB flash evaporation crystallizer 1 pumps 3 level-one vapor jet vacuums
3 outlet connection water pot A4 import of pump, the outlet water pot A4 are connect with water pump A5 feed inlet, the A5 water outlet and subsequent processing import
Connection, the secondary gas outlet connection second steam ejector vacuum pump 7 of second level DTB flash evaporation crystallizer 6, second steam ejector vacuum pump
7 outlet connection water pot B8 imports, the outlet water pot B8 are connect with water pump B9 feed inlet, and water pump B9 water outlet and subsequent processing import connect
It connects.
As shown in Fig. 2, level-one DTB flash evaporation crystallizer and the second level DTB flash evaporation crystallizer include: baffle plate 16, spiral
Paddle 17, eluriates leg 19 at guide shell 18.
The middle part of crystallizer has the guide shell 18, and the surrounding of crystallizer has baffle plate 16, approaches in guide shell 18
There is propeller 17, leg 19 is eluriated in the connection of crystallizer lower part at lower end.The barrel-shaped diameter for eluriating leg 19 is 600mm.Dedicated spiral
17 working speed of paddle are as follows: 32r/min.
A kind of potassium nitrate continuous crystallisation process, characterized in that include the following steps:
Step S1, primary flash crystallizes: the material that temperature is 48 DEG C being delivered into level-one DTB flash evaporation crystallizer and is followed
Ring flash distillation, temperature control is at 32 DEG C in flash evaporation crystallizer, vacuum degree 97.7KPa.；
Step S2, two-stage flash crystallizes: material obtained in step S1 being pumped into second level DTB flash evaporation crystallizer and is flashed
And crystallize, temperature control is at 20 DEG C in two-stage flash crystallizer, vacuum degree 99.7KPa；
Step S3, rotary filter press: material obtained in step S2 is delivered into cyclone and carries out rotary filter press, is obtained
Clear liquid and bottom concentrate；
Step S4, it thickens: bottom concentrate obtained in step S3 being entered into thickener and is thickened, material out
Solid content content is controlled 45%；
Step S5, it is centrifugated: material will be obtained in step S4 and enter centrifuge being centrifuged, obtain solid nitric acid
Potassium and potassium nitrate centrifuge mother liquor；
Step S6, mother liquor is collected: potassium nitrate centrifuge mother liquor receipts will be obtained in supernatant obtained in step S3 and S5 step
Collection enters mother liquor tank, handles wait enter next evaporization process.
Above description is only the preferred embodiment of the application and the explanation to institute's application technology principle.Those skilled in the art
Member is it should be appreciated that invention scope involved in the application, however it is not limited to technology made of the specific combination of above-mentioned technical characteristic
Scheme, while should also cover in the case where not departing from the inventive concept, it is carried out by above-mentioned technical characteristic or its equivalent feature
Any combination and the other technical solutions formed.Such as features described above has similar function with (but being not limited to) disclosed herein
Can technical characteristic replaced mutually and the technical solution that is formed.
Claims (9)
1. a kind of potassium nitrate continuous crystallisation device, including the spray of level-one DTB flash evaporation crystallizer, first degree crystalline discharging pump, level-one steam
Penetrate vacuum pump, water pot A, water pump A, second level DTB flash evaporation crystallizer, second steam ejector vacuum pump, water pot B, water pump B, second level knot
Brilliant discharging pump, cyclone, thickener, centrifuge, mother liquor tank, mother liquor pump；
The feed inlet of the level-one DTB flash evaporation crystallizer is connect with feedstock transportation pipeline, and the level-one DTB flash evaporation crystallizer goes out
Material mouth connects the first degree crystalline discharging pump feed inlet, and the first degree crystalline discharging pump discharge port and second level DTB flash distillation are tied
Brilliant device feed inlet connection, the second level DTB flash evaporation crystallizer discharge port is connect with the secondary crystallization discharging pump feed inlet, described
Secondary crystallization discharging pump discharge port is connect with the cyclone feed inlet, the cyclone supernatant discharge port and the mother liquor tank
The connection of supernatant feed inlet, the cyclone concentrate discharge port are connect with the thickener feed inlet, the thickener discharging
Mouth connects the centrifugation machine inlet, and the discharge hole of centrifugal machine is connect with the mother liquor tank import, the mother liquor of the mother liquor tank
Discharge port is connect with mother liquor pump feed inlet, and the mother liquor pumps out the feed inlet that material mouth connects lower one of evaporization process；
The secondary gas outlet of the level-one DTB flash evaporation crystallizer connects the level-one vapor jet vacuum pump, the level-one steam
Ejector vacuum pump outlet connects the water pot A import, and the outlet water pot A is connect with the water pump A feed inlet, the water pump A
Water outlet is connect with subsequent processing import；The secondary gas outlet of the second level DTB flash evaporation crystallizer connects the second steam spray
Vacuum pump is penetrated, the second steam ejector vacuum pump outlet connects the water pot B import, the outlet water pot B and the water pump B
Feed inlet connection, the water pump B water outlet are connect with subsequent processing import.
2. potassium nitrate continuous crystallisation device according to claim 1, characterized in that the level-one DTB flash evaporation crystallizer and
The second level DTB flash evaporation crystallizer includes baffle plate, propeller, guide shell, eluriates leg；
The middle part of the crystallizer has the guide shell, and the surrounding of the crystallizer has the baffle plate, the guide shell
Interior to have the propeller close at lower end, the crystallizer lower part connects the elutriation leg.
3. potassium nitrate continuous crystallisation device according to claim 2, characterized in that it is described eluriate leg shape be it is barrel-shaped,
A diameter of 100-800mm.
4. potassium nitrate continuous crystallisation device according to claim 3, characterized in that the working speed of the dedicated propeller
For 32-60r/min.
5. a kind of potassium nitrate continuous crystallisation process, includes the following steps:
Step S1, primary flash crystallizes: the material that temperature is 48 DEG C being delivered into level-one DTB flash evaporation crystallizer and carries out circulation sudden strain of a muscle
It steams；
Step S2, two-stage flash crystallizes: material obtained in the step S1 being pumped into second level DTB flash evaporation crystallizer and is flashed
And it crystallizes；
Step S3, rotary filter press: material obtained in the step S2 is delivered into cyclone and carries out rotary filter press, is obtained
Clear liquid and bottom concentrate；
Step S4, it thickens: bottom concentrate obtained in the step S3 being entered into thickener and is thickened；
Step S5, it is centrifugated: material will be obtained in the step S4 and enter centrifuge being centrifuged, obtain solid nitric acid
Potassium and potassium nitrate centrifuge mother liquor；
Step S6, mother liquor is collected: it is female that potassium nitrate centrifugation will be obtained in supernatant obtained in the step S3 and the step S5
Liquid, which is collected, enters mother liquor tank, handles wait enter next evaporization process.
6. potassium nitrate continuous crystallisation process according to claim 5, characterized in that primary flash crystallizes in the step S1
Temperature control is at 32 DEG C in device, vacuum degree 97.7KPa.
7. potassium nitrate continuous crystallisation process according to claim 5, characterized in that two-stage flash crystallizes in the step S2
Temperature control is at 20 DEG C in device, vacuum degree 99.7KPa.
8. potassium nitrate continuous crystallisation process according to claim 5, characterized in that after entering thickener in the step S4
The solid content of material out is controlled 45%.
9. potassium nitrate continuous crystallisation process according to claim 5, characterized in that utilize any one of claim 1-4
The potassium nitrate continuous crystallisation device.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201811073246.6A CN109173324A (en) | 2018-09-14 | 2018-09-14 | A kind of potassium nitrate continuous crystallisation device and method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201811073246.6A CN109173324A (en) | 2018-09-14 | 2018-09-14 | A kind of potassium nitrate continuous crystallisation device and method |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN109173324A true CN109173324A (en) | 2019-01-11 |
Family
ID=64910999
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201811073246.6A Pending CN109173324A (en) | 2018-09-14 | 2018-09-14 | A kind of potassium nitrate continuous crystallisation device and method |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN109173324A (en) |
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110613951A (en) * | 2019-10-08 | 2019-12-27 | 深圳市瑞升华科技股份有限公司 | Evaporation concentration flash evaporation cooling crystallization equipment and process thereof |
| CN113521777A (en) * | 2021-08-09 | 2021-10-22 | 常州市乐萌压力容器有限公司 | High-efficiency energy-saving triple-effect forced circulation evaporation system |
| CN113521793A (en) * | 2021-08-09 | 2021-10-22 | 常州市乐萌压力容器有限公司 | Continuous crystallization separation system for circulating evaporation device |
| WO2021248775A1 (en) * | 2020-06-12 | 2021-12-16 | 金钾科技有限公司 | Potassium nitrate crystallizer internally provided with accelerating tubes |
| CN114632344A (en) * | 2022-03-24 | 2022-06-17 | 兰州交通大学 | Copper sulfate continuous crystallization system |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101531382A (en) * | 2008-12-29 | 2009-09-16 | 卫宏远 | Production process and crystallization device for large-particle ammonium sulfate |
| JP2011510895A (en) * | 2008-02-01 | 2011-04-07 | ゲア メッソ ゲーエムベーハー | Method for producing coarse ammonium sulfate crystal product by crystallization, and equipment for carrying out said production method |
| CN104787783A (en) * | 2015-04-14 | 2015-07-22 | 四川米高化肥有限公司 | Method for preparing industrial potassium nitrate by virtue of recrystallization method |
| CN107140661A (en) * | 2017-06-08 | 2017-09-08 | 云南欧罗汉姆肥业科技有限公司 | A kind of method for flashing cooling production potassium nitrate |
| CN108514754A (en) * | 2018-03-29 | 2018-09-11 | 昆山三环保科技有限公司 | A kind of MVR novel crystallizations device goes out salt system |
-
2018
- 2018-09-14 CN CN201811073246.6A patent/CN109173324A/en active Pending
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2011510895A (en) * | 2008-02-01 | 2011-04-07 | ゲア メッソ ゲーエムベーハー | Method for producing coarse ammonium sulfate crystal product by crystallization, and equipment for carrying out said production method |
| CN101531382A (en) * | 2008-12-29 | 2009-09-16 | 卫宏远 | Production process and crystallization device for large-particle ammonium sulfate |
| CN104787783A (en) * | 2015-04-14 | 2015-07-22 | 四川米高化肥有限公司 | Method for preparing industrial potassium nitrate by virtue of recrystallization method |
| CN107140661A (en) * | 2017-06-08 | 2017-09-08 | 云南欧罗汉姆肥业科技有限公司 | A kind of method for flashing cooling production potassium nitrate |
| CN108514754A (en) * | 2018-03-29 | 2018-09-11 | 昆山三环保科技有限公司 | A kind of MVR novel crystallizations device goes out salt system |
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110613951A (en) * | 2019-10-08 | 2019-12-27 | 深圳市瑞升华科技股份有限公司 | Evaporation concentration flash evaporation cooling crystallization equipment and process thereof |
| WO2021248775A1 (en) * | 2020-06-12 | 2021-12-16 | 金钾科技有限公司 | Potassium nitrate crystallizer internally provided with accelerating tubes |
| CN113521777A (en) * | 2021-08-09 | 2021-10-22 | 常州市乐萌压力容器有限公司 | High-efficiency energy-saving triple-effect forced circulation evaporation system |
| CN113521793A (en) * | 2021-08-09 | 2021-10-22 | 常州市乐萌压力容器有限公司 | Continuous crystallization separation system for circulating evaporation device |
| CN114632344A (en) * | 2022-03-24 | 2022-06-17 | 兰州交通大学 | Copper sulfate continuous crystallization system |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN109173324A (en) | A kind of potassium nitrate continuous crystallisation device and method | |
| CN106115804B (en) | A kind of apparatus system for cobaltous sulfate efficient concentration and continuous crystallisation | |
| CN206553207U (en) | It is a kind of to be used for the apparatus system of cobaltous sulfate efficient concentration and continuous crystallisation | |
| CN109437238A (en) | A kind of ammonium chloride solution processing system and ammonium chloride solution processing method | |
| CN105435482B (en) | A kind of multi-stage vacuum adiabatic flash continuous crystallisation process and equipment | |
| CN102210941A (en) | Impinging stream evaporation crystallizer | |
| CN108341429A (en) | A kind of post-processing approach of black titanium liquid and its device used | |
| CN208525882U (en) | Vacuum flash evaporation mould and multistage flash distillation crystallization apparatus | |
| CN203816265U (en) | Inorganic salt continuous crystallization device | |
| CN203196371U (en) | Continuous potassium dihydrogen phosphate crystallization device | |
| CN107626112A (en) | A kind of continuous production vacuum cooling crystallizer | |
| CN108651932A (en) | A kind of honey process units and its application method | |
| CN202638034U (en) | Lysine hydrochloride evaporation crystallization tank | |
| CN205146818U (en) | Rotating wash bowl belt cleaning device of multiple effect evaporation ware | |
| CN104524806B (en) | A kind of hexamethylenamine complete continuous crystallisation production technology and equipments | |
| CN207845410U (en) | A kind of zinc borate production wastewater treatment equipment | |
| CN109568997A (en) | Seed precipitation solution seven imitates evaporating and concentrating process and seven effect tube-type down-flow evaporator groups | |
| CN110436546A (en) | A kind of evaporative crystallization isolation integral system | |
| CN110237558A (en) | A kind of integrated crystallization apparatus and method for crystallising with continuous fine crystal elimination circulation | |
| CN206793092U (en) | A kind of continuous evaporative crystallization device for recovery of acetic acid sodium | |
| CN208292675U (en) | A kind of black titanium liquid continuously post-processes process units | |
| CN108373162A (en) | A kind of equipment of crystallisation by cooling of potassium nitrate | |
| CN202263416U (en) | Monosodium glutamate normal-pressure crystallizing equipment | |
| CN210302497U (en) | Hot reflux extraction and concentration equipment | |
| CN204428875U (en) | The complete continuous crystallisation production process equipment of a kind of methenamine |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| RJ01 | Rejection of invention patent application after publication | ||
| RJ01 | Rejection of invention patent application after publication |
Application publication date: 20190111 |