CN104307369A - Ceramic membrane continuous concentration equipment - Google Patents
Ceramic membrane continuous concentration equipment Download PDFInfo
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- CN104307369A CN104307369A CN201410529050.9A CN201410529050A CN104307369A CN 104307369 A CN104307369 A CN 104307369A CN 201410529050 A CN201410529050 A CN 201410529050A CN 104307369 A CN104307369 A CN 104307369A
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Abstract
The invention relates to the technical field of continuous concentration, and in particular relates to ceramic membrane continuous concentration equipment, which comprises a raw material tank, wherein a liquid to be concentrated in the raw material tank runs through a feed pump and multiple groups of ceramic membranes which are sequentially connected in series through pipelines and then reaches a product tank; permeates of the ceramic membrane groups are communicated with a permeate tank through pipelines; an additional pipeline is arranged between the pipeline between the at least one pair of adjacent ceramic membrane groups and the raw material tank; and an additional feed pump is arranged on the additional pipeline. According to the ceramic membrane continuous concentration equipment disclosed by the invention, by setting an additional pipeline between the pipeline between the at least one pair of adjacent ceramic membrane groups and the raw material tank and by setting the additional feed pump on the additional pipeline, pressure of the corresponding ceramic membrane group system is improved, and subsequently a flux is increased.
Description
Technical field
The present invention relates to continuous concentration technical field, especially a kind of ceramic membrane continuous concentration equipment.
Background technology
Ceramic membrane continuous concentration (for 5 covers) process introduction: charging pump is carrying out in the amino acid fermentation liquid pump in head tank to first set ceramic membrane equipment filtering, concentrating, the solable matter permeation ceramic membranes such as amino acid obtain clarification, purifying, and the insolubility materials such as mycelium can not permeation ceramic membrane, thus be concentrated.First set equipment concentrate some can output to next stage ceramic membrane and carry out continuation and concentrate, can be continued to improve by the content of insoluble substance in the zymotic fluid that next stage ceramic membrane is concentrated, but the change of component of permeate is not too large.Concentrate so one by one, until the 5th grade of concentrated solution outlet, concentrated solution outlet finally obtains the concentrate product of aimed concn.And the permeate of every grade can pool together obtain refining after product.
There is following problem in existing ceramic membrane continuous concentration equipment:
1, total feed quantity of system is provided by charging pump completely, and the space that feed quantity promotes is very little, is unfavorable for improving production capacity;
2, the turnover film pressure of every complete equipment can increase along with progression and reduce that (that ceramic membrane that we define charging is at first 1 grade in system, the concentrate of 1 grade enters 2 grades, by that analogy), charging pump not only provides flow to system and provides pressure to entire system, but along with the prolongation of pipeline, pressure can lose.And the flux of ceramic membrane (i.e. the production capacity of permeate) and to enter film pressure proportional, when concentrated progression raises, entering film pressure can decline, and so directly causes the decline of membrane flux.
Summary of the invention
The technical problem to be solved in the present invention is: in order to solve the prolongation along with pipeline, and the flux of ceramic membrane (i.e. the production capacity of permeate) and to enter film pressure proportional, when concentrated progression raises, enter film pressure can decline, so directly cause the decline problem of membrane flux, the invention provides a kind of ceramic membrane continuous concentration equipment, an additional pipe is provided with between pipeline between at least one pair of adjacent ceramic film group and head tank, additional pipe is provided with extra charging pump can increase corresponding ceramic membrane group system pressure, and system pressure can improve flux after improving.
The technical solution adopted for the present invention to solve the technical problems is: a kind of ceramic membrane continuous concentration equipment, comprise head tank, solution to be concentrated in head tank arrives finished pot through the charging pump of being connected successively by pipeline and some groups of ceramic membrane groups, the permeate of each group of ceramic membrane group is communicated with through flow container by pipeline, be provided with an additional pipe between pipeline between at least one pair of adjacent ceramic film group described and head tank, described additional pipe is provided with extra charging pump.
Be provided with 2n or 2n-1 group ceramic membrane group as in preferred described ceramic membrane continuous concentration equipment, n be greater than 1 natural number, be provided with an additional pipe between the pipeline between described n-th group of ceramic membrane group and (n+1)th group of ceramic membrane group and head tank.
As preferably, described extra charging pump is the charging pump of band VFC.
In order to improve the controllability of additional pipe, described additional pipe is also provided with flowmeter, pressure sensor, the first valve and the second valve.
As preferably, described additional pipe is provided with from head tank the first valve, extra charging pump, pressure sensor, flowmeter and the second valve successively.
The invention has the beneficial effects as follows: a kind of ceramic membrane continuous concentration equipment provided by the invention, an additional pipe is provided with between pipeline between at least one pair of adjacent ceramic film group and head tank, additional pipe is provided with extra charging pump can increase corresponding ceramic membrane group system pressure, and system pressure can improve flux after improving.
Accompanying drawing explanation
Below in conjunction with drawings and Examples, the present invention is further described.
Fig. 1 is the schematic diagram of ceramic membrane continuous concentration equipment of the present invention.
In figure: 1. head tank, 2. charging pump, 3. ceramic membrane group, 4. finished pot, 5. pipeline, 6. through flow container, 7. additional pipe, 81. flowmeters, 82. pressure sensors, 83. first valves, 84. second valves.
Detailed description of the invention
In conjunction with the accompanying drawings, the present invention is further detailed explanation.These accompanying drawings are the schematic diagram of simplification, only basic structure of the present invention are described in a schematic way, and therefore it only shows the formation relevant with the present invention.
As shown in Figure 1, a kind of ceramic membrane continuous concentration equipment, comprise head tank 1, solution to be concentrated in head tank 1 arrives finished pot 4 through the charging pump 2 of the band VFC of being connected successively by pipeline 5 and 5 groups of ceramic membrane groups 3, the permeate of each group of ceramic membrane group (3) is communicated with through flow container (6) by pipeline (5), an additional pipe 7 is provided with between pipeline 5 between 3rd group of ceramic membrane group 3 and the 4th group of ceramic membrane group 3 and head tank 1, additional pipe 7 is provided with the first valve 83 successively from head tank 1, extra charging pump 9, pressure sensor 82, flowmeter 81 and the second valve 84.Additional pipe 7 is provided with extra charging pump 9.
The description of the process (for lysine fermentation liquor) of former continuous concentration equipment:
The application target of equipment is that lysine fermentation liquor is made into a kind of purified product (lysine content higher than 95%, dry powder) and a kind of coarse products (lysine content about 70%, dry powder) by ceramic device.Ceramic membrane is to lysine without retaining, and in raw material, the concentration of lysine is how many, and the concentration of the lysine of permeate is also how many.Certain ceramic membrane does not also retain for water.Although the concentration of permeate lysine component is constant, the impurity of the inside but lacks a lot, so the purity of lysine can reach more than 95% after final evaporate to dryness.
Most impurity and thalline are concentrated, although lysine concentration is constant, relative to these impurity and thalline, the concentration of lysine reduces.
Although stage casing feed supplement can cause the concentration of rear two sections of impurity and thalline to be lowered, words be as a whole do not have influential.As long as we control total load of total feed and permeate well, that finally concentrated feed concentration is relative to being constant before transformation.
Cocnentration factor=total feed/final load
Amount+final the load of total feed=total permeate
Former continuous concentration equipment, total feed is at 55m3/h, and cocnentration factor controls 3.5, and the total amount of permeate is 39.3 m3/h, and final load is at 15.7 m3/h.
Ceramic membrane continuous concentration equipment of the present invention, total feed=55 m3/h+10 m3/h=65 m3/h.The inlet amount of stage casing feed supplement pump is 10 m3/h.Permeate total amount is 46.42 m3/h.
Former continuous concentration equipment, film inlet and outlet pressure (bar): the former feed pump outlet pressure of 1# 4.93/2.80 2# 4.47/2.29 3#4.15/1.98 4# 4.07/1.90 5#3.82/1.84 is 3.07
Ceramic membrane continuous concentration equipment of the present invention, film inlet and outlet pressure (bar): the former feed pump outlet pressure of 1# 4.91/2.78 2# 4.27/2.08 3#3.79/1.61 4# 3.49/1.37 5#3.28/1.31 is 3.15
As can be seen from data above, increase extra charging pump obvious to 3#, 4#, 5# film device pressurized effect.Enter film pressure and add 4.15-3.79=0.36,4.07-3.49=0.58,3.82-3.28=0.54 respectively, outlet pressure also approximately adds about 0.5bar.System boost is obvious, and inlet and outlet pressure increases the also corresponding increase of rear permeate flow, and recruitment is 46.42-39.3=7.12 m3/h.
In sum: after adding extra charging pump, total feed adds 10 m3/h, permeate total amount adds 7.12 m3/h, pressure too increases similar about 0.5bar for rear 3 groups of films, and ensure that the cocnentration factor of system is constant, the product of discharging does not also change relative to before transformation.
With above-mentioned according to desirable embodiment of the present invention for enlightenment, by above-mentioned description, relevant staff in the scope not departing from this invention technological thought, can carry out various change and amendment completely.The technical scope of this invention is not limited to the content on description, must determine its technical scope according to right.
Claims (5)
1. a ceramic membrane continuous concentration equipment, comprise head tank (1), solution to be concentrated in head tank (1) arrives finished pot (4) through the charging pump (2) of being connected successively by pipeline (5) and some groups of ceramic membrane groups (3), the permeate of each group of ceramic membrane group (3) is communicated with through flow container (6) by pipeline (5), it is characterized in that: be provided with an additional pipe (7) between the pipeline (5) between at least one pair of adjacent ceramic film group (3) described and head tank (1), described additional pipe (7) is provided with extra charging pump (9).
2. ceramic membrane continuous concentration equipment as claimed in claim 1, it is characterized in that: in described ceramic membrane continuous concentration equipment, be provided with 2n or 2n-1 group ceramic membrane group (3), n be greater than 1 natural number, be provided with an additional pipe (7) between the pipeline (5) between described n-th group of ceramic membrane group (3) and (n+1)th group of ceramic membrane group (3) and head tank (1).
3. ceramic membrane continuous concentration equipment as claimed in claim 1 or 2, is characterized in that: described extra charging pump (9) is the charging pump of band VFC.
4. ceramic membrane continuous concentration equipment as claimed in claim 1 or 2, is characterized in that: described additional pipe (7) is also provided with flowmeter (81), pressure sensor (82), the first valve (83) and the second valve (84).
5. ceramic membrane continuous concentration equipment as claimed in claim 4, is characterized in that: described additional pipe (7) is provided with from head tank (1) the first valve (83), extra charging pump (9), pressure sensor (82), flowmeter (81) and the second valve (84) successively.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201410529050.9A CN104307369A (en) | 2014-10-09 | 2014-10-09 | Ceramic membrane continuous concentration equipment |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201410529050.9A CN104307369A (en) | 2014-10-09 | 2014-10-09 | Ceramic membrane continuous concentration equipment |
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| Publication Number | Publication Date |
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| CN104307369A true CN104307369A (en) | 2015-01-28 |
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| CN201410529050.9A Pending CN104307369A (en) | 2014-10-09 | 2014-10-09 | Ceramic membrane continuous concentration equipment |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109096381A (en) * | 2018-08-17 | 2018-12-28 | 河南民兴生物科技股份有限公司 | It is a kind of to spit the method and ultra-filtration membrane device that sericin is extracted in refining liquid from mulberry shoot |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN2852711Y (en) * | 2004-12-02 | 2007-01-03 | 上海高砂·鉴臣香料有限公司 | Refining device for producing water soluble flavouring essence |
| CN201762181U (en) * | 2010-06-25 | 2011-03-16 | 肖应东 | High-efficiency concentration system with low energy consumption |
| CN202322680U (en) * | 2011-12-13 | 2012-07-11 | 厦门市威士邦膜科技有限公司 | Fermentation mother liquor recovering system |
| CN204051441U (en) * | 2014-10-09 | 2014-12-31 | 江苏凯米膜科技股份有限公司 | Ceramic membrane continuous concentration equipment |
-
2014
- 2014-10-09 CN CN201410529050.9A patent/CN104307369A/en active Pending
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN2852711Y (en) * | 2004-12-02 | 2007-01-03 | 上海高砂·鉴臣香料有限公司 | Refining device for producing water soluble flavouring essence |
| CN201762181U (en) * | 2010-06-25 | 2011-03-16 | 肖应东 | High-efficiency concentration system with low energy consumption |
| CN202322680U (en) * | 2011-12-13 | 2012-07-11 | 厦门市威士邦膜科技有限公司 | Fermentation mother liquor recovering system |
| CN204051441U (en) * | 2014-10-09 | 2014-12-31 | 江苏凯米膜科技股份有限公司 | Ceramic membrane continuous concentration equipment |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109096381A (en) * | 2018-08-17 | 2018-12-28 | 河南民兴生物科技股份有限公司 | It is a kind of to spit the method and ultra-filtration membrane device that sericin is extracted in refining liquid from mulberry shoot |
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Application publication date: 20150128 |
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