CN202705273U - D-ribose extraction and purification production line - Google Patents
D-ribose extraction and purification production line Download PDFInfo
- Publication number
- CN202705273U CN202705273U CN 201220317789 CN201220317789U CN202705273U CN 202705273 U CN202705273 U CN 202705273U CN 201220317789 CN201220317789 CN 201220317789 CN 201220317789 U CN201220317789 U CN 201220317789U CN 202705273 U CN202705273 U CN 202705273U
- Authority
- CN
- China
- Prior art keywords
- storage tank
- nanofiltration
- ultrafiltration
- pipeline
- reverse osmosis
- 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 - Fee Related
Links
Landscapes
- Separation Using Semi-Permeable Membranes (AREA)
Abstract
The utility model belongs to the field of fermentation liquor extraction process devices, and particularly relates to a D-ribose extraction and purification production line. The D-ribose extraction and purification production line comprises a plurality of material storage devices, a filtration device, and pipelines communicated with the material storage devices and the filtration device. A valve and a pump are mounted on each pipeline, the material storage devices comprise a material storage tank, an ultrafiltration front storage tank, a nanofiltration front storage tank, a nanofiltration rear storage tank and a reverse-osmosis storage tank, and the filtration device comprises a pre-filter, an ultrafiltration membrane device, a nanofiltration membrane device and a reverse-osmosis device. According to the D-ribose extraction and purification production line, all the devices are connected in series through the pipelines, and therefore an ultrafiltration circulation system, a nanofiltration circulation system and a reverse-osmosis circulation system are formed. The systems are communicated with one another and work continuously and circularly, the devices can be recycled, long-cycle operation is achieved, labor intensity is reduced, environment pollution is reduced, and production cost is saved.
Description
Technical field
The utility model belongs to broth extraction processing unit field, is specifically related to a kind of extraction production line of D-ribose fermented liquid.
Background technology
The production and preparation of D-ribose was with enzymatic hydrolysis yeast rna and chemical synthesis in the past, but because these two kinds of method costs are high, and yield is low, the factors such as contaminate environment are not suitable for industrial mass production.Along with the maturation of metabolic control fermentation theory, set up the method for producing D-ribose with the transketolase deficient strain take glucose as fermenting raw materials.The Production by Microorganism Fermentation D-ribose is extensively utilized now, has realized the large-scale production of D-ribose.
The Production by Microorganism Fermentation D-ribose is divided into two stages, and the one, fermentation, the one, extract purifying.Extraction and purification process has determined yield, purity, quality, production cost and the range of application in the future of the finished product.Therefore, strengthen technical study and exploitation that D-ribose extracts purifying, the development of D-ribose industry is had important industrial value.At present the industrial method of extracting the purifying D-ribose from the D-ribose fermented liquid mainly is centrifugal or the method that adds the flocculation agent flocculation is removed thalline in the fermented liquid, and then activated carbon decolorizing directly advances ion exchange column exhaustion of yin positively charged ion, enters enrichment process.But because the fermentation liquid measure of industrial production D-ribose is very large, less whizzer can not satisfy industrial requirements, and large centrifugal is confidential, and to satisfy the performance needs such as centrifugal force higher, and the method steps of bactofugation body is numerous and diverse, and is not easy to operate; The method of Flocculation body not only need add a large amount of flocculation agents, but also needs a large amount of acid, alkali, sorbent material, and the recovery of these materials is difficult, in addition the separation of throw out is also needed extensive work.Not only activated carbon dosage is large with the activated carbon decolorizing step, and discarded gac easily causes environmental pollution.Through above-mentioned steps, also there are a large amount of impurity in the fermented liquid, directly advance from the glue post and easily cause from the pollution of glue post, increase running cost.To sum up, D-ribose extracts the purifier apparatus inefficiency in the prior art, product yield is low, and product quality can not guarantee, easily causes environmental pollution, production cost high.For the above-mentioned reasons, need the novel D-ribose of design one cover to extract purifier apparatus and form new production line, improve yield, purity, the quality of product, and reduce production costs.
Summary of the invention
The purpose of this utility model is to overcome the shortcoming of prior art, and provides a kind of D-ribose to extract purifying production line, improve production efficiency and product quality.
The technical solution of the utility model is: a kind of D-ribose extracts purifying production line, production line comprises several storage devices and filtration unit, and the pipeline that is communicated with each storage device and filtration unit, valve and pump are installed on the pipeline, described storage device comprises storage tank and reverse osmosis storage tank after storage tank before storage tank before the material storage tank, ultrafiltration, the nanofiltration, the nanofiltration, and filtration unit comprises prefilter, device for ultrafiltration membrane, nano-filtration membrane equipment and reverse osmosis equipment; Described material storage tank is connected with the prefilter entrance by pipeline, prefilter outlet is connected to storage tank entrance before the ultrafiltration by pipeline, the storage tank outlet is communicated with the device for ultrafiltration membrane entrance by pipeline before the ultrafiltration, and the device for ultrafiltration membrane trapped fluid exports by pipeline and takes back before the ultrafiltration in the storage tank; Storage tank forms a little loop before device for ultrafiltration membrane and the ultrafiltration, forms the ultrafiltration recycle system; The device for ultrafiltration membrane filtrate outlet is communicated with storage tank entrance before the nanofiltration by pipeline, and the storage tank outlet is communicated with the nano-filtration membrane equipment entrance by pipeline before the nanofiltration, and the nano-filtration membrane equipment trapped fluid exports by pipeline and takes back storage tank before the nanofiltration; Form a loop before the nanofiltration between storage tank and the nano-filtration membrane equipment, form the nanofiltration recycle system; Described nano-filtration membrane equipment filtrate outlet links to each other with storage tank entrance after the nanofiltration by pipeline, and the storage tank outlet is connected with ion exchange column after the nanofiltration, and the ion-exchange column outlet is communicated with reverse osmosis storage tank entrance; The outlet of reverse osmosis storage tank is communicated with the reverse osmosis equipment entrance, and the reverse osmosis equipment outlet takes back the reverse osmosis storage tank, connects into a minor loop, forms the reverse-osmosis circulating system; Reverse osmosis storage tank outlet pipe connects discharge nozzle simultaneously.
The beneficial effects of the utility model are: D-ribose of the present utility model extracts purifying production line in conjunction with micro-filtration, ultrafiltration, nanofiltration equipment characteristic, take full advantage of the advantage of each equipment, selectivity is good, and the equal reusable edible of each equipment, can realize long-term operation, reduce labour intensity, environmental contamination reduction has been saved production cost.Can draw thus, the utlity model has certain progressive and practicality, very large popularizing value is arranged.
Description of drawings:
Fig. 1 is equipment connection schematic diagram of the present utility model;
Wherein, 1. material storage tank, 2. prefilter, 3. storage tank before the ultrafiltration, 4. device for ultrafiltration membrane, 5. storage tank before the nanofiltration, 6. nano-filtration membrane equipment, 7. storage tank after the nanofiltration, 8. ion exchange column, 9. reverse osmosis storage tank, 10. reverse osmosis equipment, 11 discharge nozzles.
Embodiment:
In order to understand better the utility model, explain in detail embodiment of the present utility model below in conjunction with accompanying drawing.
Embodiment: as shown in Figure 1, a kind of novel D-ribose extracts purifying production line, production line comprises several storage devices and filtration unit, and the pipeline that is communicated with each storage device and filtration unit, valve and pump are installed on the pipeline, described storage device comprises storage tank 7 and reverse osmosis storage tank 9 after storage tank 5 before storage tank 3 before the material storage tank 1, ultrafiltration, the nanofiltration, the nanofiltration, and filtration unit comprises prefilter 2, device for ultrafiltration membrane 4, nano-filtration membrane equipment 6 and reverse osmosis equipment 10.Material storage tank 1 is connected with prefilter 2 entrances by pipeline, and prefilter 2 outlet is connected to storage tank 3 entrances before the ultrafiltration by pipeline.Storage tank 3 outlets are communicated with device for ultrafiltration membrane 4 entrances by pipeline before the ultrafiltration, and the outlet of device for ultrafiltration membrane 4 trapped fluids takes back the front storage tank 3 of ultrafiltration, and storage tank 3 forms a little loop before device for ultrafiltration membrane 4 and the ultrafiltration, forms the ultrafiltration recycle system.Device for ultrafiltration membrane 4 filtrate outlets are communicated with storage tank 5 entrances before the nanofiltration by pipeline, storage tank 5 outlets are communicated with nano-filtration membrane equipment 6 entrances by pipeline before the nanofiltration, nano-filtration membrane equipment 6 trapped fluids outlets takes back storage tank 5 before the nanofiltration by pipeline, storage tank 5 and nano-filtration membrane equipment 6 form a loop before the nanofiltration, form the nanofiltration recycle system.Nano-filtration membrane equipment 6 filtrate outlets link to each other with storage tank 7 entrances after the nanofiltration by pipeline, storage tank 7 outlets link to each other with ion exchange column 8 entrances after the nanofiltration, ion exchange column 8 is the cascaded structure of cationic exchange coloum and anion-exchange column, three groups are arranged in parallel, and filtrate is through the zwitterion in the ion exchange column removal filtrate.Ion exchange column 8 outlets are communicated with reverse osmosis storage tank 9 entrances.9 outlets of reverse osmosis storage tank are communicated with reverse osmosis equipment 10 entrances, and reverse osmosis equipment 10 outlets take back reverse osmosis storage tank 9, connect into a minor loop, form the reverse-osmosis circulating system.Feed liquid after the process reverse osmosis has been pure D-ribose solution, can by discharge nozzle 11 outputs, enter next enrichment process.
Using method of the present utility model and application production process are: fermented liquid is storage tank 3 before material storage tank 1 is squeezed into ultrafiltration by pump through prefilter 2, and prefilter 2 is 80 mesh filter screens, mainly removes the larger impurity in the fermented liquid.Fermented liquid storage tank 3 before the ultrafiltration pumps into device for ultrafiltration membrane 4, filtering fermentating liquid, mainly be degerming, removal of impurities (may cause the macromolecular substance of rear muddiness such as protein, pectin, starch etc.), make filtrate limpid bright, the main effective constituent in the basic guarantee material sees through simultaneously.Molecular weight cut-off is 100K～300K dalton, and filtration area is 66 m
2, operating temperature range is 15～50 ℃, and working pressure range is 0.2～0.4Mpa, and the working pH scope is 3～10.During filtration fermented liquid before ultrafiltration the storage tank 3 by pump delivery to device for ultrafiltration membrane 4 since film inside and outside have pressure reduction, deliquescent material or particle diameter see through film less than the material (or solvent) of membrane pore size and enter into per-meate side.Macromolecular substance (or solid) tunicle is held back and is taken out of membrane module and is back to the front storage tank 3 of ultrafiltration.So continuous cycle operation, along with filtrate continuously outflows, the content of trapped substance is just more and more higher, finally reaches the purpose of separation, concentrated, purifying.Behind end-of-job, by taking suitable purging method membrane flux is recovered fully, realize long-term operation.Filtrate after the ultrafiltration is stored in the front storage tank 5 of nanofiltration, filtrate by nanofiltration before storage tank 5 after force (forcing) pump pressurization, send into nano-filtration membrane equipment 6, nanofiltration membrane is that 150～1000 dalton's organic molecules have separation performance for the molecular weight in the solution, the operator scheme of film adopts cross flow filter, therefore work the time has been cleared up the trapped substance of fenestra surface detention voluntarily, thus implementation phase work continuously, until reach the purpose of predetermined purifies and separates.Material is divided into filtered solution and trapped fluid after nanofiltration membrane is filtered, filtered solution advances storage tank 7 after the nanofiltration, and trapped fluid is from getting back to storage tank 5 before the nanofiltration after nano-filtration membrane equipment 6 flows out, and so constantly circulation realizes the concentrated of feed liquid and separates.Filtrate by nanofiltration after storage tank 7 after force (forcing) pump pressurization, send into ion exchange column 8, ion exchange column 8 be the cascaded structure of cationic exchange coloum and anion-exchange column, three groups are arranged in parallel, filtrate is passed through the zwitterion in the ion exchange column removal filtrate.Filtered solution advances reverse osmosis storage tank 9, and pump into reverse osmosis equipment 10 by force (forcing) pump, the membrane element of this reverse osmosis equipment 10 is that level is installed on the equipment, consistent with the flow direction of material, in the material concentration process, material enters the reverse-osmosis membrane element system under the pressure of pump, under the effect of feeding pump, material constantly carries out high-speed and continuous and flows, and will concentrate material output, enters reverse osmosis storage tank 9, circulate concentrated, in sepn process, be pure physical process, product is without phase transformation, effective constituent and local flavor keep fully, because the operator scheme of film adopts cross flow filter, both are orthogonal, and the solute of holding back is taken away by tangential flow, cleared up voluntarily the trapped substance of fenestra surface detention, reduced the concentration polarization rate, until reach the purpose of predetermined purifies and separates, thus implementation phase is worked continuously.Behind end-of-job, by taking suitable purging method membrane flux is recovered fully, realize long-term operation.
Above-mentioned explanation is not to be to restriction of the present utility model; the utility model also is not limited in above-mentioned giving an example; the variation that those skilled in the art make in essential scope of the present utility model, remodeling, interpolation or replacement also should belong to protection domain of the present utility model.
Claims (2)
1. a D-ribose extracts purifying production line, production line comprises several storage devices and filtration unit, and the pipeline that is communicated with each storage device and filtration unit, valve and pump are installed on the pipeline, it is characterized in that: described storage device comprises storage tank and reverse osmosis storage tank after storage tank before storage tank before the material storage tank, ultrafiltration, the nanofiltration, the nanofiltration, and filtration unit comprises prefilter, device for ultrafiltration membrane, nano-filtration membrane equipment and reverse osmosis equipment; Described material storage tank is connected with the prefilter entrance by pipeline, prefilter outlet is connected to storage tank entrance before the ultrafiltration by pipeline, the storage tank outlet is communicated with the device for ultrafiltration membrane entrance by pipeline before the ultrafiltration, and the device for ultrafiltration membrane trapped fluid exports by pipeline and takes back before the ultrafiltration in the storage tank; Storage tank forms a little loop before device for ultrafiltration membrane and the ultrafiltration, forms the ultrafiltration recycle system; The device for ultrafiltration membrane filtrate outlet is communicated with storage tank entrance before the nanofiltration by pipeline, and the storage tank outlet is communicated with the nano-filtration membrane equipment entrance by pipeline before the nanofiltration, and the nano-filtration membrane equipment trapped fluid exports by pipeline and takes back storage tank before the nanofiltration; Form a loop before the nanofiltration between storage tank and the nano-filtration membrane equipment, form the nanofiltration recycle system; Described nano-filtration membrane equipment filtrate outlet links to each other with storage tank entrance after the nanofiltration by pipeline, and the storage tank outlet is connected with ion exchange column after the nanofiltration, and the ion-exchange column outlet is communicated with reverse osmosis storage tank entrance; The outlet of reverse osmosis storage tank is communicated with the reverse osmosis equipment entrance, and the reverse osmosis equipment outlet takes back the reverse osmosis storage tank, connects into a minor loop, forms the reverse-osmosis circulating system; Reverse osmosis storage tank outlet pipe connects discharge nozzle simultaneously.
2. D-ribose according to claim 1 extracts purifying production line, and it is characterized in that: described ion exchange column is the cascaded structure of cationic exchange coloum and anion-exchange column.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 201220317789 CN202705273U (en) | 2012-07-03 | 2012-07-03 | D-ribose extraction and purification production line |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 201220317789 CN202705273U (en) | 2012-07-03 | 2012-07-03 | D-ribose extraction and purification production line |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN202705273U true CN202705273U (en) | 2013-01-30 |
Family
ID=47585594
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 201220317789 Expired - Fee Related CN202705273U (en) | 2012-07-03 | 2012-07-03 | D-ribose extraction and purification production line |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN202705273U (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104370978A (en) * | 2014-12-08 | 2015-02-25 | 山东润德生物科技有限公司 | Method and device for extracting D-ribose from D-ribose crystalline mother solution |
| CN108504562A (en) * | 2018-06-21 | 2018-09-07 | 江苏澳创生物科技有限公司 | A kind of system of production of L-threonine by fermentation and its application |
-
2012
- 2012-07-03 CN CN 201220317789 patent/CN202705273U/en not_active Expired - Fee Related
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104370978A (en) * | 2014-12-08 | 2015-02-25 | 山东润德生物科技有限公司 | Method and device for extracting D-ribose from D-ribose crystalline mother solution |
| CN108504562A (en) * | 2018-06-21 | 2018-09-07 | 江苏澳创生物科技有限公司 | A kind of system of production of L-threonine by fermentation and its application |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN102040531B (en) | Method for extracting L-isoleucine | |
| CN105669560A (en) | Method for separating and extracting tetrahydropyrimidine from fermentation broth | |
| CN103232353A (en) | Method for separating and extracting L-valine from broth with high efficiency | |
| CN101503366B (en) | Method for extracting and separating L-valine by membrane separation and plant chromatography separation | |
| CN101497574B (en) | Method for extracting and separating L-isoleucine by membrane separation and plant chromatography separation | |
| CN102586361A (en) | Manufacturing method of glucose | |
| CN102241706B (en) | D-ribose purification and separation method | |
| CN202705273U (en) | D-ribose extraction and purification production line | |
| CN103815405B (en) | The production system of cistanche extracts | |
| CN210434309U (en) | Device for removing inorganic acid in xylose solution | |
| CN201485313U (en) | Mixed loading membrane separation device | |
| CN101805382A (en) | Separation and purification method of high-purity netilmicin | |
| CN102146104B (en) | Method for removing divalent metal ion from antibiotic etimicin liquid medicine | |
| CN102161625A (en) | Method for extracting and separating L-phenylalanine by utilizing combined technology of membrane separation and industrial chromatographic separation | |
| CN210560185U (en) | Device for purifying and recovering protein peptide by membrane method | |
| CN2853796Y (en) | Ketogulonic acid production device in vitamin C cleaning production | |
| CN102559940A (en) | Separation and purification method of glucose | |
| CN102586492A (en) | Method for removing impurities from saccharification solution in glucose production process | |
| CN113387774A (en) | Erythritol extraction process and system | |
| CN102659564A (en) | Method for extracting lactic acid from wastewater generated in lactic acid production | |
| CN210495953U (en) | Forward osmosis comprehensive treatment device for concentration of traditional Chinese medicine extracting solution | |
| CN203828006U (en) | Production system of cistanche extract | |
| CN203139910U (en) | Nanofiltration membrane system applied to fermentation liquor purification | |
| CN214060479U (en) | Sugar alcohol chromatogram raffinate recovery processing device | |
| CN216630340U (en) | Desalination system for purifying ergothioneine fermentation liquor |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20130130 Termination date: 20140703 |
|
| EXPY | Termination of patent right or utility model |