CN201586401U - Continuous crystallizer device - Google Patents
Continuous crystallizer device Download PDFInfo
- Publication number
- CN201586401U CN201586401U CN2010200043606U CN201020004360U CN201586401U CN 201586401 U CN201586401 U CN 201586401U CN 2010200043606 U CN2010200043606 U CN 2010200043606U CN 201020004360 U CN201020004360 U CN 201020004360U CN 201586401 U CN201586401 U CN 201586401U
- Authority
- CN
- China
- Prior art keywords
- crystallizer
- pump
- outlet
- links
- heater
- 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.)
- Expired - Lifetime
Links
- 238000002425 crystallisation Methods 0.000 claims abstract description 23
- 230000008025 crystallization Effects 0.000 claims abstract description 23
- 239000012452 mother liquor Substances 0.000 claims abstract description 13
- 238000002156 mixing Methods 0.000 claims abstract description 9
- 239000013078 crystal Substances 0.000 claims abstract description 7
- 230000008676 import Effects 0.000 claims description 25
- 238000007599 discharging Methods 0.000 claims description 18
- 238000011081 inoculation Methods 0.000 claims description 4
- 238000009413 insulation Methods 0.000 claims description 2
- 238000004519 manufacturing process Methods 0.000 abstract description 10
- 239000007788 liquid Substances 0.000 abstract description 8
- LPUQAYUQRXPFSQ-DFWYDOINSA-M monosodium L-glutamate Chemical compound [Na+].[O-]C(=O)[C@@H](N)CCC(O)=O LPUQAYUQRXPFSQ-DFWYDOINSA-M 0.000 abstract description 6
- 235000013923 monosodium glutamate Nutrition 0.000 abstract description 6
- 239000004223 monosodium glutamate Substances 0.000 abstract description 5
- 235000013305 food Nutrition 0.000 abstract description 2
- 239000002002 slurry Substances 0.000 abstract 2
- 238000005516 engineering process Methods 0.000 description 6
- 238000010586 diagram Methods 0.000 description 5
- 238000000034 method Methods 0.000 description 4
- 239000012535 impurity Substances 0.000 description 3
- 229910001220 stainless steel Inorganic materials 0.000 description 3
- 239000010935 stainless steel Substances 0.000 description 3
- WHUUTDBJXJRKMK-VKHMYHEASA-N L-glutamic acid Chemical compound OC(=O)[C@@H](N)CCC(O)=O WHUUTDBJXJRKMK-VKHMYHEASA-N 0.000 description 2
- 230000015572 biosynthetic process Effects 0.000 description 2
- 238000009833 condensation Methods 0.000 description 2
- 230000005494 condensation Effects 0.000 description 2
- 238000000605 extraction Methods 0.000 description 2
- 239000012530 fluid Substances 0.000 description 2
- 229930195712 glutamate Natural products 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 2
- ODHCTXKNWHHXJC-VKHMYHEASA-N 5-oxo-L-proline Chemical compound OC(=O)[C@@H]1CCC(=O)N1 ODHCTXKNWHHXJC-VKHMYHEASA-N 0.000 description 1
- ODHCTXKNWHHXJC-GSVOUGTGSA-N Pyroglutamic acid Natural products OC(=O)[C@H]1CCC(=O)N1 ODHCTXKNWHHXJC-GSVOUGTGSA-N 0.000 description 1
- 239000002253 acid Substances 0.000 description 1
- ODHCTXKNWHHXJC-UHFFFAOYSA-N acide pyroglutamique Natural products OC(=O)C1CCC(=O)N1 ODHCTXKNWHHXJC-UHFFFAOYSA-N 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000009835 boiling Methods 0.000 description 1
- 239000000498 cooling water Substances 0.000 description 1
- 239000011549 crystallization solution Substances 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 230000008021 deposition Effects 0.000 description 1
- 238000013461 design Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 238000001704 evaporation Methods 0.000 description 1
- 230000008020 evaporation Effects 0.000 description 1
- 230000002349 favourable effect Effects 0.000 description 1
- 230000009123 feedback regulation Effects 0.000 description 1
- 239000007791 liquid phase Substances 0.000 description 1
- 239000002932 luster Substances 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 238000002161 passivation Methods 0.000 description 1
- 238000005498 polishing Methods 0.000 description 1
- 238000012545 processing Methods 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 230000000306 recurrent effect Effects 0.000 description 1
- 238000004062 sedimentation Methods 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 238000003756 stirring Methods 0.000 description 1
- 239000000725 suspension Substances 0.000 description 1
- 238000012546 transfer Methods 0.000 description 1
Images
Classifications
-
- 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
Landscapes
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
本实用新型一种连续结晶器装置，主要用于食品行业味精生产的浓缩结晶。包括结晶器(3)、原液与母液混合罐(1)、进料泵(2)、板式加热器(14)、外循环泵(11)、加热器(5)、内循环泵(4)和出料泵(10)；原液与母液混合罐(1)与进料泵(2)相连，进料泵(2)与板式加热器(14)相连，板式加热器(14)与外循环泵(11)相连通，外循环泵(11)与加热器(5)相连，加热器(5)与结晶器(3)的循环回流口(3.2)相连通，结晶器(3)的循环出料口(3.18)与外循环泵(11)相连通；内循环泵(4)设置在所述结晶器(3)的底端；所述出料泵(10)的进口与所述结晶器(3)的晶浆出口(3.20)相连，出料泵(10)的出口分别与所述结晶器(3)的晶浆循环口(3.11)和一助晶槽(8)相连。本实用新型具有装置耗蒸汽低、设备产能高和自动化程度高等特点。
The utility model relates to a continuous crystallizer device, which is mainly used for concentrated crystallization in the production of monosodium glutamate in the food industry. Including crystallizer (3), raw liquid and mother liquid mixing tank (1), feed pump (2), plate heater (14), external circulation pump (11), heater (5), internal circulation pump (4) and The discharge pump (10); the raw liquid and mother liquor mixing tank (1) is connected to the feed pump (2), the feed pump (2) is connected to the plate heater (14), and the plate heater (14) is connected to the external circulation pump ( 11) are connected, the external circulation pump (11) is connected to the heater (5), the heater (5) is connected to the circulation return port (3.2) of the crystallizer (3), and the circulation outlet of the crystallizer (3) (3.18) communicate with the external circulation pump (11); the internal circulation pump (4) is arranged on the bottom of the crystallizer (3); the inlet of the discharge pump (10) is connected to the crystallizer (3) The crystal slurry outlet (3.20) is connected to each other, and the outlet of the discharge pump (10) is connected to the crystal slurry circulation port (3.11) of the crystallizer (3) and a crystallization aid tank (8) respectively. The utility model has the characteristics of low steam consumption of the device, high equipment production capacity and high degree of automation.
Description
(1) background technology
The utility model relates to a kind of continuous crystallizer.Be mainly used in the condensing crystallizing of food service industry glutamate production.The condensing crystallizing that also can be used for other industry.
(2) background technology
At present, the monosodium glutamate crystallization processes adopts gap single-action concentration and crystallization process mode basically.All there be not big breakthrough aspect the production capacity of equipment, the production serialization.The major defect of traditional gap crystallization processes is:
1, integrated steam using is poor, and consumption vapour quota is high.
According to related data, 4 tons of/ton monosodium glutamates of the consumption vapour of glutamate production quota average out to.
2, crystalliser volume is little, and equipment capacity is low.
At present, the crystalliser volume generally used of monosodium glutamate industry is 12m
3, 15m
3More, maximum also is no more than 50m
3
3, automaticity is low, the technology instability, and the ability of resisting the raw material quality fluctuation is also poor, thereby impurity content is higher in the monosodium glutamate finished product, the production cost height.
(3) summary of the invention
The purpose of this utility model is to overcome above-mentioned deficiency, and a kind of continuous crystallizer that steam is low, equipment capacity is high and automaticity is high that consumes is provided.
The purpose of this utility model is achieved in that a kind of continuous crystallizer, and described device comprises crystallizer, stoste and mother liquor blending tank, feed pump, baffle heater, outer circulation pump, heater, internal circulation pump, discharging pump and surface cooler;
Described crystallizer, from top to bottom successively by upper cover, go up cylinder, upper cone, middle cylinder, lower cone and bottom (head) is end to end forms, described going up in the cylinder is horizontally arranged with a shower, be connected with a magma circulation port and inoculation mouthful on below the described shower on the cylinder barrel, in described upper cone and middle cylinder, be respectively arranged with an inner cone and an inner barrel, inner cone is inverted cone shape and is connected in the inner barrel top, is provided with a guide shell in described inner cone, inner barrel and lower cone; The cylinder barrel is provided with a circulation discharging opening in described, described lower cone barrel is provided with one and loops back head piece and magma outlet, be provided with trap at described upper cover top, this trap has umbrella-shaped baffle, is provided with indirect steam outlet at the trap side;
Described stoste links to each other with feed pump with the outlet of mother liquor blending tank, feed pump links to each other with the baffle heater import, the baffle heater outlet is connected with the outer circulation pump inlet, the outer circulation pump discharge links to each other with the heater import, heater outlet is connected with the head piece that loops back of described crystallizer, and the circulation discharging opening of described crystallizer is connected with the outer circulation pump inlet;
Described internal circulation pump is arranged on the bottom of described crystallizer, the import of this internal circulation pump and the intracavity inter-connection of crystallizer, and the outlet of this internal circulation pump is arranged in the described guide shell;
The import of described discharging pump links to each other with the outlet of the magma of described crystallizer, the discharging delivery side of pump links to each other with a crystallization in motion groove import with the magma circulation port of described crystallizer respectively, the outlet of crystallization in motion groove links to each other with a centrifuge import, and the centrifuge outlet links to each other with a centrifuge mother liquor groove import;
The steam inlet of described surface cooler is connected with the indirect steam outlet at the top of described crystallizer, the condensate outlet of this surface cooler is connected with a bottom condensate drum, this bottom condensate drum links to each other with a condensate pump, and the outlet of surface cooler uncondensed gas links to each other with vavuum pump.
The beneficial effects of the utility model are:
1, crystallizer equipment enlarging, production capacity increases.
The volume of crystallizer has been broken through the conventional size of gap single-action condensing crystallizing device, can reach 80m
3More than.And general gap crystallizer has only 20m
3About, amplify doubly a lot of.Not only equipment capacity is greatly improved, but also has saved the table of equipment number, has reduced investment cost.It is reported, build identical production-scale monosodium glutamate device.The investment of continuous crystalizer technology will be saved more than 30%.
2, continuous crystalizer operation serialization, production cost descends.
Continuous crystalizer technology has been improved the recurrent state of crystallization solution, has reduced degree of supersaturation, and is very favourable to the growth of the formation of nucleus and crystal.Thereby crystallization temperature has descended, and percent crystallization in massecuite is enhanced, and magma can be from extraction continuously in the crystallizer.Realized the operation serialization, required operating personnel reduce significantly, and labor productivity is enhanced.
3, continuous crystalizer can be realized automation control, and quality further improves.Show that mainly impurity is few, the appearance luster light, long crystal formation crystallization is evenly neat.
The gap crystallizer is in order to obtain higher percent crystallization in massecuite, have to rely on the means that improve degree of supersaturation to realize, but degree of supersaturation is high more, the viscosity of magma also sharply raises, viscosity raises and is unfavorable for crystallization, must improve crystallization temperature again as reducing viscosity, chromogenesis and pyroglutamic acid influence product quality and crystalline rate so inevitably.Continuous crystalizer has been implemented the key process parameter feedback controls, and inside and outside internal circulating load and advance jar steam and rationally set has been optimized technology greatly, and impurity obviously reduces in the product, and quality is greatly improved.
Comprehensively above-mentioned, continuous crystalizer of the present utility model has production capacity height, characteristic of low energy consumption.
(4) description of drawings
Fig. 1 is a mold structure schematic diagram of the present utility model.
Fig. 2 is the vertical view of Fig. 1.
Fig. 3 is the general structure schematic diagram of the utility model continuous crystallizer.
Fig. 4 is the schematic diagram that moves towards of the utility model double fluid journey material.
Among the figure:
Bottom (head) 3.1, loop back head piece 3.2, lower cone 3.3, guide shell 3.4, gusset I 3.5, gusset II 3.6, middle cylinder 3.7, inner barrel 3.8, upper cone 3.9, inner cone 3.10, magma circulation port 3.11, go up cylinder 3.12, shower 3.13, upper cover 3.14, trap 3.15, indirect steam outlet 3.16, inoculation mouthfuls 3.17, circulation discharging opening 3.18, gripper shoe 3.19, magma outlet 3.20.
Stoste and mother liquor blending tank 1, feed pump 2, crystallizer 3, internal circulation pump 4, heater 5, surface cooler 6, vavuum pump 7, crystallization in motion groove 8, centrifuge 9, discharging pump 10, outer circulation pump 11, take out condensate pump 12, condensed water bucket 13, baffle heater 14, bottom condensate drum 15, condensate pump 16, centrifuge mother liquor groove 17.
(5) specific embodiment
Referring to Fig. 1～2, Fig. 1 is a continuous crystalizer structural representation of the present utility model.Fig. 2 is the vertical view of Fig. 1.By Fig. 1 and Fig. 2 as can be seen, crystallizer 3 of the present utility model, from top to bottom successively by upper cover 3.14, go up cylinder 3.12, upper cone 3.9, middle cylinder 3.7, lower cone 3.3 and bottom (head) 3.1 end to end forming.Described going up in the cylinder 3.12 is horizontally arranged with a shower 3.13, be connected with a magma circulation port 3.11 and inoculation mouthfuls 3.17 on below the described shower 3.13 on cylinder 3.12 barrels, in order to prevent crystallization deposition and poor circulation, in described upper cone 3.9 and middle cylinder 3.7, be respectively arranged with an inner cone 3.10 and an inner barrel 3.8, inner cone 3.10 is inverted cone shape and is connected in inner barrel 3.8 tops, described inner barrel 3.8 outer rims link to each other with the inwall of described lower cone 3.3 by gusset I 3.5, at described inner cone 3.10, be provided with a guide shell 3.4 in inner barrel 3.8 and the lower cone 3.3, guide shell 3.4 outer rim tops link to each other with the inwall of inner barrel 3.8 by gusset II 3.6, and guide shell 3.4 outer rim bottoms link to each other with the inwall of described lower cone 3.3 by gripper shoe 3.19; Cylinder 3.7 barrels are provided with a circulation discharging opening 3.18 in described, and described lower cone 3.3 barrels are provided with one and loop back head piece 3.2 and magma outlet 3.20, and this magma outlet 3.20 adopts crystal to eluriate the structure of leg; Be provided with trap 3.15 at described upper cover 3.14 tops, this trap 3.15 has umbrella-shaped baffle, to preventing to escape liquid, reducing the loss of operation entrainment and played fine effect.Be provided with indirect steam outlet 3.16 at trap 3.15 sides.
Referring to Fig. 3 and Fig. 4, Fig. 3 is the general structure schematic diagram of the utility model continuous crystallizer.Fig. 4 is the schematic diagram that moves towards of the utility model double fluid journey material.By Fig. 3 and Fig. 4 as can be seen, the utility model continuous crystallizer, comprise stoste and mother liquor blending tank 1, feed pump 2, baffle heater 14, outer circulation pump 11, heater 5, crystallizer 3, internal circulation pump 4, discharging pump 10 and surface cooler 6, described stoste links to each other with feed pump 2 with 1 outlet of mother liquor blending tank, feed pump 2 links to each other with baffle heater 14 imports, baffle heater 14 outlets are connected with 11 imports of outer circulation pump, 11 outlets of outer circulation pump link to each other with heater 5 imports, heater 5 outlets are connected with the head piece 3.2 that loops back of described crystallizer 3, and the circulation discharging opening 3.18 of described crystallizer 3 is connected with 11 imports of outer circulation pump, has formed top-down external circulating system; Internal circulation pump 4 is arranged on the bottom of described crystallizer 3, the intracavity inter-connection of the import of this internal circulation pump 4 and crystallizer 3, and the outlet of this internal circulation pump 4 is arranged in the guide shell 3.4, has constituted internal circulation system.The import of described discharging pump 10 links to each other with the magma outlet 3.20 of described crystallizer 3,8 imports link to each other with a crystallization in motion groove with the magma circulation port 3.11 of described crystallizer 3 respectively in the outlet of discharging pump 10,8 outlets of crystallization in motion groove link to each other with a centrifuge 9 imports, and centrifuge 9 outlets link to each other with a centrifuge mother liquor groove 17 imports.The steam inlet of described surface cooler 6 is connected with the indirect steam outlet 3.16 at the top of described crystallizer 3, and the condensate outlet of this surface cooler 6 is connected with a bottom condensate drum 15, and this bottom condensate drum 15 links to each other with a condensate pump 16; Described surface cooler 6 uncondensed gas outlet links to each other with vavuum pump 7 (preferably adopting water-ring vacuum pump).Crystallization in motion groove 8, centrifuge 9 and centrifuge mother liquor groove 17 constitute the capital equipment of magma separation process.The indirect steam that comes out in the crystallizer top through the surface cooler condensation, enters the bottom condensate drum, and uncondensed gas is extracted out emptying by vavuum pump.
The crystallization in motion device is the intermediate equipment of storing for the extraction of crystallizer magma, is same as the state of crystallizer in order to keep the magma liquid phase, and the crystallization in motion device also is provided with insulation jacket and makes not sedimentation of crystal, and that still keeps suspension stirs the belt mixer.
Heater 5 is selected the round trip tube still heater for use.The housing of heater 5 and tubulation all are stainless steel.This heater form, simple in structure, heat transfer efficiency height, easy to maintenance.
Internal circulation pump adopts vertical centrifugal pump, outer circulation pump to adopt centrifugal pump of single stage type.The characteristics of centrifugal pump, simple in structure, lift is low, stability of flow.
In the design of crystallizer structural dimensions, also taken into full account high through than, generally be no more than 2, can cause boiling point to rise after excessive, influence evaporation rate; The highest liquid level of umbrella shape plate washer distance should keep more than the 1m.The magma loss is little like this.
All parts of crystallizer all adopt stainless steel, and stainless steel surfaces also will carry out acid wash passivation processing, inner surface polishing.
Crystallizer drops into quadruplet technological parameter feedback controls instrument, sets three flow values, has realized the crystallizer operation automation.
Quadruplet technological parameter feedback controls instrument is respectively:
1, solid-to-liquid ratio parameter feedback controls inlet amount adopts the rotating speed (frequency control) of double flanges differential pressure transmitter output signal feedback regulation feed pump to realize automatic control.
2, liquid level parameter feedback controls load in the crystallizer.Adopt two flange differential pressure device transmitters to carry signal feedback to regulate discharging revolution speed (frequency control) and realize automatic control.
3, heater condensation water pot liquid level parameter feedback controls is taken out the condensate pump flow, adopts control valve control.
4, surface cooler temperature parameter feedback controls cooling water flow adopts control valve control.
Three flow values are set and are respectively: advance circular flow and outer circulation flow in heater steam flow, the crystallizer.
Claims (5)
1. a continuous crystallizer is characterized in that described device comprises crystallizer (3), stoste and mother liquor blending tank (1), feed pump (2), baffle heater (14), outer circulation pump (11), heater (5), internal circulation pump (4), discharging pump (10) and surface cooler (6);
Described crystallizer (3), from top to bottom successively by upper cover (3.14), last cylinder (3.12), upper cone (3.9), middle cylinder (3.7), lower cone (3.3) and end to end the forming of bottom (head) (3.1), described going up in the cylinder (3.12) is horizontally arranged with a shower (3.13), on last cylinder (3.12) barrel of described shower (3.13) below, be connected with a magma circulation port (3.11) and inoculation mouthful (3.17), in described upper cone (3.9) and middle cylinder (3.7), be respectively arranged with an inner cone (3.10) and an inner barrel (3.8), inner cone (3.10) is inverted cone shape and is connected in inner barrel (3.8) top, in described inner cone (3.10), be provided with a guide shell (3.4) in inner barrel (3.8) and the lower cone (3.3); Cylinder (3.7) barrel is provided with a circulation discharging opening (3.18) in described, described lower cone (3.3) barrel is provided with one and loops back head piece (3.2) and magma outlet (3.20), be provided with trap (3.15) at described upper cover (3.14) top, this trap (3.15) has umbrella-shaped baffle, is provided with indirect steam outlet (3.16) at trap (3.15) side;
Described stoste links to each other with feed pump (2) with mother liquor blending tank (1) outlet, feed pump (2) links to each other with baffle heater (14) import, baffle heater (14) outlet is connected with outer circulation pump (11) import, outer circulation pump (11) outlet links to each other with heater (5) import, heater (5) outlet is connected with the head piece (3.2) that loops back of described crystallizer (3), and the circulation discharging opening (3.18) of described crystallizer (3) is connected with outer circulation pump (11) import;
Described internal circulation pump (4) is arranged on the bottom of described crystallizer (3), the intracavity inter-connection of import of this internal circulation pump (4) and crystallizer (3), and the outlet of this internal circulation pump (4) is arranged in the described guide shell (3.4);
The import of described discharging pump (10) links to each other with the magma outlet (3.20) of described crystallizer (3), the outlet of discharging pump (10) links to each other with crystallization in motion groove (a 8) import with the magma circulation port (3.11) of described crystallizer (3) respectively, crystallization in motion groove (8) outlet links to each other with a centrifuge (9) import, and centrifuge (9) outlet links to each other with centrifuge mother liquor groove (a 17) import;
The steam inlet of described surface cooler (6) is connected with the indirect steam outlet (3.16) at the top of described crystallizer (3), the condensate outlet of this surface cooler (6) is connected with a bottom condensate drum (15), this bottom condensate drum (15) links to each other with a condensate pump (16), and the outlet of surface cooler (6) uncondensed gas links to each other with vavuum pump (7).
2. a kind of continuous crystallizer according to claim 1, it is characterized in that described inner barrel (3.8) outer rim links to each other with the inwall of described lower cone (3.3) by gusset I (3.5), guide shell (3.4) outer rim top links to each other with the inwall of inner barrel (3.8) by gusset II (3.6), and guide shell (3.4) outer rim bottom links to each other with the inwall of described lower cone (3.3) by gripper shoe (3.19).
3. a kind of continuous crystallizer according to claim 1 and 2 is characterized in that described magma exports (3.20) and adopts crystal to eluriate the structure of leg.
4. a kind of continuous crystallizer according to claim 1 and 2 is characterized in that described crystallization in motion groove (8) is provided with insulation jacket and mixer.
5. a kind of continuous crystallizer according to claim 1 and 2 is characterized in that described heater (5) selects the round trip tube still heater for use.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2010200043606U CN201586401U (en) | 2010-01-16 | 2010-01-16 | Continuous crystallizer device |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2010200043606U CN201586401U (en) | 2010-01-16 | 2010-01-16 | Continuous crystallizer device |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN201586401U true CN201586401U (en) | 2010-09-22 |
Family
ID=42746168
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN2010200043606U Expired - Lifetime CN201586401U (en) | 2010-01-16 | 2010-01-16 | Continuous crystallizer device |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN201586401U (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101732885B (en) * | 2010-01-16 | 2012-07-18 | 江阴丰力生化工程装备有限公司 | Continuous crystallizer |
| CN115068972A (en) * | 2021-03-16 | 2022-09-20 | 上海梅山钢铁股份有限公司 | Crystallization tank capable of adjusting solid-liquid ratio of ammonium sulfate mother liquor |
-
2010
- 2010-01-16 CN CN2010200043606U patent/CN201586401U/en not_active Expired - Lifetime
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101732885B (en) * | 2010-01-16 | 2012-07-18 | 江阴丰力生化工程装备有限公司 | Continuous crystallizer |
| CN115068972A (en) * | 2021-03-16 | 2022-09-20 | 上海梅山钢铁股份有限公司 | Crystallization tank capable of adjusting solid-liquid ratio of ammonium sulfate mother liquor |
| CN115068972B (en) * | 2021-03-16 | 2023-08-15 | 上海梅山钢铁股份有限公司 | Crystallization tank capable of adjusting solid-to-liquid ratio of ammonium sulfate mother liquor |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN101732885B (en) | Continuous crystallizer | |
| CN106115804B (en) | A kind of apparatus system for cobaltous sulfate efficient concentration and continuous crystallisation | |
| CN203763891U (en) | Vacuum low-temperature evaporating crystallizer | |
| CN108726578B (en) | Ferrous sulfate continuous crystallization process in sulfuric acid method titanium dioxide production | |
| CN105435482B (en) | A kind of multi-stage vacuum adiabatic flash continuous crystallisation process and equipment | |
| CN201586401U (en) | Continuous crystallizer device | |
| CN105771304A (en) | Double-effect countercurrent evaporation crystallization system for monosodium glutamate and working process thereof | |
| CN101732886A (en) | Continuous crystallizer | |
| CN105879424A (en) | Continuous vacuum crystallization device with flash vaporization and cooling | |
| CN201586400U (en) | Continuous crystallizer | |
| CN207085388U (en) | A kind of special large particle crystal device of medium temperature Klorvess Liquid | |
| CN108341429A (en) | A kind of post-processing approach of black titanium liquid and its device used | |
| CN100374372C (en) | A kind of double decomposition method prepares the method for potassium nitrate | |
| CN203196371U (en) | Continuous potassium dihydrogen phosphate crystallization device | |
| CN202226659U (en) | Equipment evaporating sodium persulfate with low temperature | |
| CN201182916Y (en) | Irrotational impact-flow heat exchange type crystallizer | |
| CN202961950U (en) | Double-effect continuous crystallization device | |
| CN205340185U (en) | Continuous crystallization equipment of multistage high vacuum insulation flash distillation | |
| CN214458078U (en) | A boiling sugar crystallizing tank | |
| CN107626112A (en) | A kind of continuous production vacuum cooling crystallizer | |
| CN214861311U (en) | Continuous device for chlorfenapyr crystallization | |
| CN207108952U (en) | The small-sized Craft Beer saccharification system of two device list pumps | |
| JP4837775B2 (en) | Improved vertical continuous vacuum kettle | |
| CN207356613U (en) | A kind of continuous production vacuum cooling crystallizer | |
| CN212491600U (en) | A new type of stirring and dehydrating device for proline self-controlling temperature |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| AV01 | Patent right actively abandoned |
Granted publication date: 20100922 Effective date of abandoning: 20100116 |
|
| AV01 | Patent right actively abandoned |
Granted publication date: 20100922 Effective date of abandoning: 20100116 |