CN101732885B - Continuous crystallizer - Google Patents
Continuous crystallizer Download PDFInfo
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- CN101732885B CN101732885B CN2010100055133A CN201010005513A CN101732885B CN 101732885 B CN101732885 B CN 101732885B CN 2010100055133 A CN2010100055133 A CN 2010100055133A CN 201010005513 A CN201010005513 A CN 201010005513A CN 101732885 B CN101732885 B CN 101732885B
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Abstract
The invention relates to a continuous crystallizer mainly used for concentrative crystallization in monosidum glutamate production of food industry, which comprises a crystallizer (3), a raw liquid and mother liquid mixing tank (1), a feeding pump (2), a plate type heater (14), an outer circulating pump (11), a heater (5), an inner circulating pump (4) and a discharging pump (10), wherein the raw liquid and mother liquid mixing tank (1) is connected with the feeding pump (2) connected with the plate type heater (14) which is communicated with the outer circulating pump (11), the outer circulating pump (11) is connected with the heater (5) communicated with a circulated flow returning port (3.2) of the crystallizer (3), and an circulated discharging port (3.18) of the crystallizer (3) is communicated with the outer circulating pump (11); the inner circulating pump (4) is arranged at the bottom of the crystallizer (3); and an outlet of the discharging pump (10) is respectively connected with a crystal paste circulating port (3.11) of the crystallizer (3) and a crystallization-assistant slot (8). The continuous crystallizer has the characteristics of low steam consumption, high equipment yield, high degree of the automation and the like.
Description
(1) background technology
The present invention 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, and technology is unstable, and the ability of resisting the raw materials quality fluctuation is also poor, thereby impurity content is higher in the monosodium glutamate finished product, and production cost is high.
(3) summary of the invention
The objective of the invention is to overcome above-mentioned deficiency, a kind of continuous crystallizer that steam is low, equipment capacity is high and automaticity is high that consumes is provided.
The objective of the invention is to realize like this: a kind of continuous crystallizer, said device comprise crystallizer, stoste and mother liquor blending tank, feed pump, baffle heater, outer circulation pump, heater, internal circulation pump, discharging pump and surface cooler;
Said 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; Said going up in the cylinder is horizontally arranged with a shower; Be connected with a magma circulation port and inoculation mouthful on below the said shower on the cylinder barrel; In said 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, in said inner cone, inner barrel and lower cone, is provided with a guide shell; The cylinder barrel is provided with a circulation discharging opening in said; Said lower cone barrel is provided with one and loops back head piece and magma outlet; Be provided with trap at said upper cover top, this trap has umbrella-shaped baffle, is provided with indirect steam outlet at the trap side;
Said 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, and heater outlet is connected with the head piece that loops back of said crystallizer, and the circulation discharging opening of said crystallizer is connected with the outer circulation pump inlet;
Said internal circulation pump is arranged on the bottom of said 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 said guide shell;
The import of said discharging pump links to each other with the outlet of the magma of said crystallizer; The discharging delivery side of pump links to each other with a crystallization in motion groove import with the magma circulation port of said 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 said surface cooler is connected with the indirect steam outlet at the top of said 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 invention has the beneficial effects as follows:
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; As will reduce viscosity and must improve crystallization temperature again, 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 invention has production capacity height, characteristic of low energy consumption.
(4) description of drawings
Fig. 1 is a mold structure sketch map of the present invention.
Fig. 2 is the vertical view of Fig. 1.
Fig. 3 is the general structure sketch map of continuous crystallizer of the present invention.
Fig. 4 is the sketch map that moves towards of the present invention's 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 I3.5, 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 invention.Fig. 2 is the vertical view of Fig. 1.Can find out that by Fig. 1 and Fig. 2 crystallizer 3 of the present invention is 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 bottom (head) 3.1 end to end forming.Said 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 said shower 3.13 on cylinder 3.12 barrels; In order to prevent crystallization deposition and poor circulation; In said 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, and said inner barrel 3.8 outer rims link to each other with the inwall of said lower cone 3.3 through gusset I 3.5, in said inner cone 3.10, inner barrel 3.8 and lower cone 3.3, is provided with a guide shell 3.4; Guide shell 3.4 outer rim tops link to each other with the inwall of inner barrel 3.8 through gusset II 3.6, and guide shell 3.4 outer rim bottoms link to each other with the inwall of said lower cone 3.3 through gripper shoe 3.19; Cylinder 3.7 barrels are provided with a circulation discharging opening 3.18 in said, and said 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 said 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 sketch map of continuous crystallizer of the present invention.Fig. 4 is the sketch map that moves towards of the present invention's double fluid journey material.Can find out by Fig. 3 and Fig. 4; Continuous crystallizer of the present invention; 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; Said stoste links to each other with feed pump 2 with 1 outlet of mother liquor blending tank, and feed pump 2 links to each other with baffle heater 14 imports, and 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 said crystallizer 3, and the circulation discharging opening 3.18 of said 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 said 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 said discharging pump 10 links to each other with the magma outlet 3.20 of said crystallizer 3; 8 imports link to each other with a crystallization in motion groove with the magma circulation port 3.11 of said 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 said surface cooler 6 is connected with the indirect steam outlet 3.16 at the top of said 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; Said 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, gets into the bottom condensate drum, and uncondensed gas is extracted out emptying by vavuum pump.
The crystallization in motion device is the intermediate equipment that supplies the extraction of crystallizer magma to store, and 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 is high, 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 warp than, generally be no more than 2, can cause after excessive boiling point to rise, 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, the rotating speed (frequency control) that adopts double flanges differential pressure transmitter output signal feedback to regulate feed pump is realized 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 said 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);
Said 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); Said going up in the cylinder (3.12) is horizontally arranged with a shower (3.13); On last cylinder (3.12) barrel of said shower (3.13) below, be connected with a magma circulation port (3.11) and inoculation mouthful (3.17); In said 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 said inner cone (3.10), inner barrel (3.8) and lower cone (3.3), is provided with a guide shell (3.4); Cylinder (3.7) barrel is provided with a circulation discharging opening (3.18) in said; Said 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 said 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;
Said 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, and heater (5) outlet is connected with the head piece (3.2) that loops back of said crystallizer (3), and the circulation discharging opening (3.18) of said crystallizer (3) is connected with outer circulation pump (11) import;
Said internal circulation pump (4) is arranged on the bottom of said 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 said guide shell (3.4);
The import of said discharging pump (10) links to each other with the magma outlet (3.20) of said 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 said 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 said surface cooler (6) is connected with the indirect steam outlet (3.16) at the top of said 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 said inner barrel (3.8) outer rim links to each other with the inwall of said lower cone (3.3) through gusset I (3.5); Guide shell (3.4) outer rim top links to each other with the inwall of inner barrel (3.8) through gusset II (3.6), and guide shell (3.4) outer rim bottom links to each other with the inwall of said lower cone (3.3) through gripper shoe (3.19).
3. a kind of continuous crystallizer according to claim 1 and 2 is characterized in that said 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 said 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 said heater (5) selects the round trip tube still heater for use.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2010100055133A CN101732885B (en) | 2010-01-16 | 2010-01-16 | Continuous crystallizer |
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|---|---|---|---|
| CN2010100055133A CN101732885B (en) | 2010-01-16 | 2010-01-16 | Continuous crystallizer |
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| CN101732885B true CN101732885B (en) | 2012-07-18 |
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| CN102462975A (en) * | 2010-11-17 | 2012-05-23 | 天津长芦汉沽盐场有限责任公司 | Continuous crystallizing and precipitating device and method |
| CN102614679B (en) * | 2012-03-19 | 2014-10-22 | 通辽梅花生物科技有限公司 | Continuous crystallizing tank and continuous evaporative crystallization process |
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| CN102921185B (en) * | 2012-10-31 | 2015-04-22 | 江阴丰力生化工程装备有限公司 | Double-effect continuous crystallization device |
| CN105439344B (en) * | 2014-09-30 | 2017-09-01 | 海洲环保集团有限公司 | High-concentration salt-containing wastewater saves crystallization apparatus |
| CN105509803A (en) * | 2015-12-02 | 2016-04-20 | 中盐工程技术研究院有限公司 | Device for accurately measuring liquid level and solid liquid ratio of salt-making evaporation equipment |
| CN105771304B (en) * | 2016-05-05 | 2017-11-10 | 无锡荣丰生物工程有限公司 | Monosodium glutamate two imitates countercurrent evaporation crystal system and its course of work |
| CN108164413B (en) * | 2016-12-07 | 2021-09-28 | 上海凯赛生物技术股份有限公司 | Continuous crystallization equipment, system and method for long-chain dibasic acid |
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| CN88103158A (en) * | 1988-06-06 | 1988-12-21 | 天津市轻工业设计院 | Extract the method and the device thereof of L-glutamic acid continuously |
| CN1058541A (en) * | 1991-07-16 | 1992-02-12 | 山东新华制药厂 | Self-circulating vacuum crystallizer |
| US5941165A (en) * | 1998-07-06 | 1999-08-24 | Butte; Jeffrey C. | Apparatus for continuously processing dried solid products |
| CN1252734A (en) * | 1997-02-27 | 2000-05-10 | 味之素株式会社 | Crystillization apparatus and crystallization method |
| CN201271520Y (en) * | 2008-09-28 | 2009-07-15 | 江苏纵横浓缩干燥设备有限公司 | Self-cleaning crystallization tank |
| CN201350354Y (en) * | 2009-01-13 | 2009-11-25 | 姜新明 | Evaporated crystallizer |
| CN201586401U (en) * | 2010-01-16 | 2010-09-22 | 江阴丰力生化工程装备有限公司 | Continuous crystallizer device |
-
2010
- 2010-01-16 CN CN2010100055133A patent/CN101732885B/en not_active Expired - Fee Related
Patent Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN88103158A (en) * | 1988-06-06 | 1988-12-21 | 天津市轻工业设计院 | Extract the method and the device thereof of L-glutamic acid continuously |
| CN1058541A (en) * | 1991-07-16 | 1992-02-12 | 山东新华制药厂 | Self-circulating vacuum crystallizer |
| CN1252734A (en) * | 1997-02-27 | 2000-05-10 | 味之素株式会社 | Crystillization apparatus and crystallization method |
| US5941165A (en) * | 1998-07-06 | 1999-08-24 | Butte; Jeffrey C. | Apparatus for continuously processing dried solid products |
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| CN201586401U (en) * | 2010-01-16 | 2010-09-22 | 江阴丰力生化工程装备有限公司 | Continuous crystallizer device |
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