CN102029202B - Continuous ion exchange unit for organic acid production - Google Patents
Continuous ion exchange unit for organic acid production Download PDFInfo
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- CN102029202B CN102029202B CN2010105249169A CN201010524916A CN102029202B CN 102029202 B CN102029202 B CN 102029202B CN 2010105249169 A CN2010105249169 A CN 2010105249169A CN 201010524916 A CN201010524916 A CN 201010524916A CN 102029202 B CN102029202 B CN 102029202B
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Abstract
The invention relates to a continuous ion exchange unit for organic acid production, comprising resin, at least three resin columns, feeding main pipes communicated with the upper ends of the resin columns and discharging main pipes communicated with the lower ends of the resin columns, wherein the feeding main pipes include a liquid feeding main pipe, an elution feeding main pipe and a regeneration feeding main pipe; the discharging main pipes include a liquid discharging main pipe, an elution discharging main pipe and a regeneration discharging main pipe; each resin column is respectively provided with a feeding branch pipe in one-to-one corresponding communication with the feeding main pipes and a discharging branch pipe in one-to-one corresponding communication with the discharging main pipes; and each feeding branch pipe and each discharging branch pipe are respectively provided with a control valve for cooperatively controlling all the resin columns to realize ion exchange, elution and resin regeneration in turn. The invention can reduce the usage amount of chemical agents, reduce the production cost, improve the yield of products, stabilize the quality of products, reduce the discharge of waste liquid and lighten the pressure for environment protection.
Description
Technical field
The present invention relates to a kind of continuous ionic switch, particularly relate to a kind of continuous ionic switch that organic acid is produced that is used for.
Background technology
The existing utilization in the fermentative Production organic acid production technology, ion-exchange has obtained widespread usage, is mainly used in organic acid and removes inorganic positive anion.The general equipment that adopts of existing ion exchange system is fixed bed, and it is a kind of batch-type operation, and exchange, regeneration are carried out in same bed successively; Single batch job cycle is long, discontinuous, and the ion exchange resin utilization rate is low; The equipment pipe valve is many and labour intensity is big; The chemical reagent consumption amount is big, and is uneconomical, and wastewater discharge is big etc.
Summary of the invention
For this reason, technical problem to be solved by this invention is to adopt a kind of continuous ion exchange technique to replace the fixed bed switching technology, is used for organic acid and removes inorganic positive anion, overcomes the disadvantage of existing fixed bed ion exchange technique.
A kind of continuous ionic switch that organic acid is produced that is used for of the present invention; Comprise resin, resin column, reach discharge header pipe with the connection of resin column lower end with the charging house steward who is communicated with on the resin column; Said resin column is provided with three at least; The charging house steward comprises feed liquid charging house steward, wash-out charging house steward and regeneration feed house steward; Said discharge header pipe comprises feed liquid discharge header pipe, wash-out discharge header pipe and regeneration discharge header pipe, is respectively equipped with feed-inputing branched pipe that is communicated with the charging house steward and the discharging arm that is communicated with said discharge header pipe on said each resin column;
Said feed-inputing branched pipe comprises feed liquid feed-inputing branched pipe, wash-out feed-inputing branched pipe and regeneration feed arm, and said feed liquid feed-inputing branched pipe, wash-out feed-inputing branched pipe and regeneration feed arm are communicated with described feed liquid charging house steward, wash-out charging house steward and regeneration feed house steward are corresponding one by one;
Said discharging arm comprises feed liquid discharging arm, wash-out discharging arm and regeneration discharging arm, and said feed liquid discharging arm, wash-out discharging arm and regeneration discharging arm are communicated with described feed liquid discharge header pipe, wash-out discharge header pipe and regeneration discharge header pipe are corresponding one by one;
Be respectively equipped with control valve on said each feed-inputing branched pipe, discharging arm and the series pipe, be used for periodically controlling each resin column group and between a plurality of resin columns, realize ion-exchange, wash-out and regeneration of resin process synchronously.
Described resin is a kind of in gel-type strong-acid cation-exchange resin, macropore weak basic anion exchange resin and the macroporous type strong-acid cation-exchange resin.
Preferably, described resin column is 4-12.
Described control valve is magnetic valve or pneumatic operated valve, and said control valve is used for the keying of the control valve on each resin column of sequential control through the PLC programme-control.
Particularly; Technical solution of the present invention is a kind of continuous ionic switching method and device thereof that organic acid is produced that be used for; This device mainly comprises following coordinative composition of equipments and forms: (1) resin: gel-type strong-acid cation-exchange resin and macropore weak basic anion exchange resin (2) resin column: resin column quantity is n, n=4-10 (3) PLC automatic control system and peripheral matched pipeline and surge tank etc.
This method is a kind of continuous ionic switching method that organic acid is produced that is used for; Feed liquid, regenerative agent gets into different resin columns at one time through different pipelines; Move certain all after dates; Through the switching of valve, saturated resin got into regenerative agent regeneration after resin reached capacity, and the resin that regeneration is good begins feeding liquid and exchanges.Resin substitutes the position operation always continuously in system.
Technique scheme of the present invention is compared prior art and is had the following advantages:
1. exchange process carries out in resin column, and feed liquid gets into from top, and flow out the bottom.Flow rate of liquid confirms that by pending feed liquid character and resins exchange performance the mobile genus piston type of resin in bed moves, and does not produce disorderly layer phenomenon.
2. exchange is carried out in different resin columns with regeneration simultaneously, and in ion-exchange simultaneously, the resin in the part resin column is carrying out wash-out, regenerative process, and regenerative agent gets into from top, and flow out the bottom.Exchange and regenerative process are carried out simultaneously, and the resin after the ion-exchange carries out wash-out, regeneration, and the resin of having regenerated carries out ion-exchange, thereby realize the continuous process of ion-exchange.
Description of drawings
For content of the present invention is more clearly understood, below according to a particular embodiment of the invention and combine accompanying drawing, the present invention is done further detailed explanation, wherein
Fig. 1 is a structural representation of the present invention;
Fig. 2 is PLC control circuit figure of the present invention.
Reference numeral is expressed as among the figure:
1, resin column 2, feed liquid charging house steward 3, wash-out charging house steward 4, regeneration feed house steward 5, feed liquid feed-inputing branched pipe 6, wash-out feed-inputing branched pipe 7, regeneration feed arm 8, feed liquid discharge header pipe 9, wash-out discharge header pipe 10, regeneration discharge header pipe 11, regeneration discharging arm 12, wash-out discharging arm 13, feed liquid discharging arm 14, series pipe.
The specific embodiment
Referring to Fig. 1; It mainly comprises: comprise resin, resin column, reach the discharge header pipe that is communicated with the resin column lower end with the charging house steward who is communicated with on the resin column, resin column is provided with three at least, and preferred resin column quantity is that 4-12 is individual; The resin column quantity that adopts among the figure is 6; Wherein per two resin columns are one group, and the charging house steward comprises feed liquid charging house steward, wash-out charging house steward and regeneration feed house steward, and discharge header pipe comprises feed liquid discharge header pipe, wash-out discharge header pipe and regeneration discharge header pipe; Be respectively equipped with the feed-inputing branched pipe that is communicated with the charging house steward on each resin column, with the discharging arm of discharge header pipe connection;
Feed-inputing branched pipe comprises feed liquid feed-inputing branched pipe, wash-out feed-inputing branched pipe and regeneration feed arm, and feed liquid feed-inputing branched pipe, wash-out feed-inputing branched pipe and regeneration feed arm are communicated with feed liquid charging house steward, wash-out charging house steward and regeneration feed house steward are corresponding one by one;
The discharging arm comprises feed liquid discharging arm, wash-out discharging arm and regeneration discharging arm, and feed liquid discharging arm, wash-out discharging arm and regeneration discharging arm are communicated with feed liquid discharge header pipe, wash-out discharge header pipe and regeneration discharge header pipe are corresponding one by one;
Be respectively equipped with control valve on each feed-inputing branched pipe and the discharging arm, be used for coordinating realizing ion-exchange, wash-out and regeneration of resin process in turn between each resin column of control.
Wherein the resin in the resin column is a kind of in gel-type strong-acid cation-exchange resin, macropore weak basic anion exchange resin and the macroporous type strong-acid cation-exchange resin.
The control valve that is used to control each arm is magnetic valve or pneumatic operated valve; Control valve adopts the PLC programme-control; Be used for periodically controlling the keying of the control valve on each arm, make each resin column group between a plurality of resin columns, realize ion-exchange, wash-out and regeneration of resin process synchronously.
The concrete operations technology of this method is:
Feed liquid, eluant, eluent and regenerative agent pass through charging house steward separately respectively, get into different resin columns at one time, in the different resins post, accomplish exchange, wash-out and the regeneration of ion; After the resin in the resin column that carries out ion-exchange reaches capacity; Opening feed liquid discharging arm control valve emits the feed liquid in this resin column; After treating that feed liquid has discharged, close the feed liquid discharging arm control valve of this resin column lower end, open wash-out charging house steward control valve and get into elution process; One group of resin column in other two groups has been accomplished the regeneration of resin process at this moment; Open the fill process that feed liquid feed-inputing branched pipe control valve gets into feed liquid, another group resin column has been accomplished elution process, opens regeneration feed arm control valve and gets into the regeneration of resin process;
Through the control valve on each resin column of PLC control; The resin column that wash-out is good carries out the regeneration of regenerative agent; The resin column that regeneration is good carries out the feeding liquid exchange, and the resin column after ion-exchange is accomplished carries out the wash-out of eluant, eluent, and resin substitutes the position operation always continuously in system like this.
In exchange simultaneously, the part resin is carrying out wash-out and regenerative process, and regenerative agent gets into from top, and flow out the bottom, and regenerant consumption is wherein confirmed by pending material liquid component.
Exchange and regenerative process are carried out simultaneously, and the resin after the exchange carries out wash-out and regeneration, and the resin of having regenerated exchanges.
Method and apparatus of the present invention is used for the ion-exchange operation of following organic acid production technology: the production of desalination (3) ascorbic acid of desalination (2) citric acid of (1) lactic acid
As shown in Figure 2, all corresponding technological process controls are carried out relevant operation through the CPU in the PLC system.Each pillar operating unit is divided into exchange, wash-out, and three steps of regenerating are continuous, and each step, the continuous feeding liquid (eluent, regenerated liquid) that is divided into again started (closing), valve open (closing), sensor starts (cutting out) three and column unit.At a time, all pillars are in operation exchange, wash-out, a certain step in the regeneration step.As being example with the 1# post, give 1# post exchange instruction through CPU, this moment, sensor obtained giving the inlet valve gate signal, the charging valve open after the order of CPU.After preset time, CPU gives 1# post exchange END instruction, and this moment, sensor obtained giving the inlet valve gate signal after the order of CPU, the charging valve closing, exchange finishes, and with this signal feedback to CPU.This moment, CPU gave 1# post wash-out instruction, and this moment, sensor obtained advancing eluent valve signal after the order of CPU, advanced the eluent valve open.After preset time, CPU gives the END instruction of 1# post wash-out, and this moment, sensor obtained advancing eluent valve signal after the order of CPU, advanced the eluent valve closing, and wash-out finishes, and the 1# post begins next job step.The control principle of other posts is identical with the 1# post with step.
Present embodiment is that lactic acid removes the cation process, adopts method of the present invention and device, and pending feed liquid is a feed liquid behind the production of lactic acid decolorizing with activated carbon second time; Concentration 18%-19%, viscosity: 1.05cP-1.10cP, temperature 30-40 ℃; Ion exchange resin is the gel-type strong-acid cation-exchange resin; The seplite LSI-010 that adopts Xi'an Lanxiao Sci-Tech Co., Ltd. to produce, swap time 2h, feed rate is controlled to be 5-10m
3/ h.Regenerative agent uses 4-7% hydrochloric acid solution, regenerant consumption 1-3 times of resin bed volume.The product cation removal can reach more than 98%, and product yield reaches more than 99%.
Present embodiment is that lactic acid removes the anion process, adopts method of the present invention and device, and pending feed liquid removes cation feed liquid afterwards for process; Concentration 17.5%-18.5%, viscosity 1.05cP-1.10cP, temperature 30-40 ℃; Ion exchange resin is the macroporous type weak basic anion exchange resin; The seplite LSI-363 that adopts Xi'an Lanxiao Sci-Tech Co., Ltd. to produce, swap time 3h, feed rate 8-12m
3/ h.Regenerative agent uses the 5-7% aqueous slkali, and regenerant consumption 1-3 is by the resin bed volume.Product anion clearance can reach more than 98%, and product yield reaches more than 99%.
Present embodiment is that citric acid removes positive anion process.Adopt method and apparatus of the present invention, pending feed liquid is the citric acid solution of 20%-22%, PH:1-2.Ion exchange resin is the macroporous type strong-acid cation-exchange resin, and the sepliteD001 that adopts Xi'an Lanxiao Sci-Tech Co., Ltd. to produce transfers the H+ type to 4%Hcl before using, swap time 3h, flow-control is 8-10m
3/ h.
Exchange process among the present invention, resin can all reach industrial saturated exchange, can make full use of the exchange capacity of resin; The exchange regenerative process is carried out continuously; And exchange regeneration is not carried out in same bed, and the utilization rate of resin improves 30-50%, and regenerative agent is practiced thrift 50-60%; The discharging of waste liquid amount reduces, and has alleviated environmental protection pressure.
Obviously, the foregoing description only be for explanation clearly done for example, and be not qualification to embodiment.For the those of ordinary skill in affiliated field, on the basis of above-mentioned explanation, can also make other multi-form variation or change.Here need not also can't give exhaustive to all embodiments.And conspicuous variation of being extended out thus or change still are among the protection domain of the invention.
Claims (4)
1. one kind is used for the continuous ionic switch that organic acid is produced, and comprises resin, resin column, reaches the discharge header pipe that is communicated with the resin column lower end with the charging house steward who is communicated with on the resin column, it is characterized in that:
Said resin column is provided with three at least; The charging house steward comprises feed liquid charging house steward, wash-out charging house steward and regeneration feed house steward; Said discharge header pipe comprises feed liquid discharge header pipe, wash-out discharge header pipe and regeneration discharge header pipe, is respectively equipped with feed-inputing branched pipe that is communicated with the charging house steward and the discharging arm that is communicated with said discharge header pipe on said each resin column;
Said feed-inputing branched pipe comprises feed liquid feed-inputing branched pipe, wash-out feed-inputing branched pipe and regeneration feed arm, and said feed liquid feed-inputing branched pipe, wash-out feed-inputing branched pipe and regeneration feed arm are communicated with described feed liquid charging house steward, wash-out charging house steward and regeneration feed house steward are corresponding one by one;
Said discharging arm comprises feed liquid discharging arm, wash-out discharging arm and regeneration discharging arm, and said feed liquid discharging arm, wash-out discharging arm and regeneration discharging arm are communicated with described feed liquid discharge header pipe, wash-out discharge header pipe and regeneration discharge header pipe are corresponding one by one;
Be respectively equipped with control valve on said each feed-inputing branched pipe, discharging arm and the series pipe, be used for periodically controlling each resin column group and between a plurality of resin columns, realize ion-exchange, wash-out and regeneration of resin process synchronously.
2. continuous ionic switch according to claim 1 is characterized in that:
Described resin is a kind of in gel-type strong-acid cation-exchange resin, macropore weak basic anion exchange resin and the macroporous type strong-acid cation-exchange resin.
3. continuous ionic switch according to claim 1 is characterized in that:
Described resin column is 4-12.
4. according to the described continuous ionic switch of the arbitrary claim of claim 1-3, it is characterized in that:
Described control valve is magnetic valve or pneumatic operated valve, and said control valve is used for the keying of the control valve on each resin column of sequential control through the PLC programme-control.
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| CN2010105249169A CN102029202B (en) | 2010-10-29 | 2010-10-29 | Continuous ion exchange unit for organic acid production |
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| CN2010105249169A CN102029202B (en) | 2010-10-29 | 2010-10-29 | Continuous ion exchange unit for organic acid production |
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| CN102029202B true CN102029202B (en) | 2012-12-12 |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN107382799A (en) * | 2014-03-03 | 2017-11-24 | 宁夏紫光天化蛋氨酸有限责任公司 | Ion exchange acidifying methionine salt prepares the method and special equipment of methionine |
| CN106582896B (en) * | 2016-12-27 | 2019-04-02 | 宜昌三峡制药有限公司 | The continuous ion-exchange system of automation and control method of production are extracted for isoleucine scale |
| CN106669867A (en) * | 2017-03-21 | 2017-05-17 | 南京凯通粮食生化研究设计有限公司 | Continuous and automatic ion exchange device |
| CN108893605B (en) * | 2018-05-25 | 2020-03-10 | 西安蓝晓科技新材料股份有限公司 | Continuous ion exchange device and method capable of realizing lithium-sodium separation |
| CN111450903A (en) * | 2020-05-21 | 2020-07-28 | 浙江华康药业股份有限公司 | Continuous ion exchange system for xylose production and use method thereof |
| CN112546673B (en) * | 2020-12-18 | 2022-07-08 | 欧尚元(天津)有限公司 | Parallel uniform-feeding resin column system and feeding control method |
| CN114522743B (en) * | 2022-03-09 | 2023-07-28 | 欧尚元智能装备有限公司 | Method for preparing sodium iso-vitamin C and decalcification method and system thereof |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US6527958B1 (en) * | 1997-11-27 | 2003-03-04 | T & P S.P.A. | Device for reducing water hardness (softener) having a resins exhaustion sensor, and washing machine having said device |
| CN1443751A (en) * | 2003-04-18 | 2003-09-24 | 张启修 | Continuous ion exchange method for producing amino acid and its equipment |
| CN2865851Y (en) * | 2005-12-23 | 2007-02-07 | 鲁洲生物科技（山东）有限公司 | Ion exchange regenerative liquid recirculation equipment |
| CN201823538U (en) * | 2010-10-29 | 2011-05-11 | 西安蓝晓科技有限公司 | Continuous ion exchanging device for producing organic acid |
-
2010
- 2010-10-29 CN CN2010105249169A patent/CN102029202B/en active Active
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US6527958B1 (en) * | 1997-11-27 | 2003-03-04 | T & P S.P.A. | Device for reducing water hardness (softener) having a resins exhaustion sensor, and washing machine having said device |
| CN1443751A (en) * | 2003-04-18 | 2003-09-24 | 张启修 | Continuous ion exchange method for producing amino acid and its equipment |
| CN2865851Y (en) * | 2005-12-23 | 2007-02-07 | 鲁洲生物科技（山东）有限公司 | Ion exchange regenerative liquid recirculation equipment |
| CN201823538U (en) * | 2010-10-29 | 2011-05-11 | 西安蓝晓科技有限公司 | Continuous ion exchanging device for producing organic acid |
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Address after: High tech Zone technology two road 710075 Shaanxi city of Xi'an province No. 72 Chak tower 4 Applicant after: Sunresin New Materials Co., Ltd., Xi'an Address before: High tech Zone technology two road 710075 Shaanxi city of Xi'an province No. 72 Chak tower 4 Applicant before: Xian Sunresin Technology Co., Ltd. |
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