CN210885600U - Extraction device of hexachlorocyclohexane hexa-holo-dihydrogen phosphate - Google Patents
Extraction device of hexachlorocyclohexane hexa-holo-dihydrogen phosphate Download PDFInfo
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- CN210885600U CN210885600U CN201921226985.4U CN201921226985U CN210885600U CN 210885600 U CN210885600 U CN 210885600U CN 201921226985 U CN201921226985 U CN 201921226985U CN 210885600 U CN210885600 U CN 210885600U
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Abstract
The utility model discloses a hexachlorocyclohexane hexa-total-dihydrogen phosphate's extraction element, including consecutive ceramic membrane piece-rate system, clarification fluid reservoir and continuous ion exchange system, ceramic membrane piece-rate system including the soaking fluid reservoir, drawing liquid pump and the ceramic membrane piece-rate unit that connect in order, the concentrate export of ceramic membrane piece-rate unit is passed through the back flow and is soaked the fluid reservoir and link to each other, the penetrant export links to each other with the inlet of clarification fluid reservoir, the back flow on be equipped with the governing valve, the liquid inlet end of continuous ion exchange system links to each other with the liquid outlet of clarification fluid reservoir. The utility model utilizes the ceramic membrane separation system to separate the suspended matters in the soak solution to obtain the clear feed solution, thereby ensuring the service life and the extraction efficiency of the ion exchange resin; by utilizing the continuous ion exchange system, the energy conservation and emission reduction of the extraction device and the automatic production are realized, and meanwhile, the production cost is reduced.
Description
Technical Field
The utility model belongs to the extraction field of hexacyclohexanol hexa-full-dihydrogen phosphate, in particular to an extraction device of hexacyclohexanol hexa-full-dihydrogen phosphate.
Background
The hexakis-dihydrogen phosphate is mainly present in seeds, roots and stems of plants, with the highest content in seeds of leguminous plants, bran and germ of cereals. The use of cyclohexanehexol-dihydrogen phosphate is very widespread. In the food industry, cyclohexanehexol hexa-mono-dihydrogen phosphate can be used as a food additive, and in the wine industry as a metal remover. Can be used for treating diabetes, renal calculus, etc. in pharmaceutical industry. The product can be widely applied in chemical industry, petroleum industry, metallurgy industry and daily chemical industry, can be used as an antioxidant of grease, a preservative of food and fruit, an anti-sticking agent of a polyvinyl chloride polymerization kettle, a quenching agent in medicine, an additive of feed, and can also be used as an anti-rust, cleaning, anti-static and metal surface treating agent and the like, and particularly can be used as one of important raw materials for producing inositol.
The traditional extraction method of the cyclohexanehexol hexa-dihydrogen phosphate adopts a fixed bed process, the fixed bed process has large resin dosage, the problems of low resource utilization rate, low product liquid content and long production period exist, and meanwhile, acid and alkali regeneration consumes a large amount of acid and alkali, so that the production cost is high, a large amount of waste water is generated, and the environment is seriously polluted.
Disclosure of Invention
In view of the above problems, an object of the present invention is to provide a device for extracting cyclohexanehexol-dihydrogen phosphate, which can solve the problems of low resource utilization rate and large amount of waste water in the conventional fixed bed system.
In order to realize the purpose, the utility model discloses a technical scheme as follows:
an extraction device of cyclohexanehexol hexa-dihydrogen phosphate comprises a ceramic membrane separation system, a clarifying liquid tank and a continuous ion exchange system which are connected in sequence. The ceramic membrane separation system comprises a soaking liquid tank, a liquid pump and a ceramic membrane separation unit which are connected in sequence, wherein a concentrated solution outlet of the ceramic membrane separation unit is connected with the soaking liquid tank through a return pipe, and a penetrating fluid outlet is connected with a liquid inlet of a clarifying liquid tank. The reflux pipe is provided with a regulating valve, and the liquid inlet end of the continuous ion exchange system is connected with the liquid outlet of the clarifying liquid tank.
Furthermore, the ceramic membrane separation system also comprises a circulating pump and an internal circulating pipe, wherein the circulating pump is arranged on a connecting pipeline of the liquid pump and the ceramic membrane separation unit, one end of the internal circulating pipe is connected with the return pipe, and the other end of the internal circulating pipe is connected to the front end of the circulating pump.
Further, the continuous ion exchange system comprises at least 2 resin columns uniformly arranged along the circumferential direction, and the inside of each resin column is filled with resin for adsorbing the hexachlorocyclohexane all-dihydrogen phosphate.
Further, the continuous ion exchange system comprised 24 resin columns each filled with a resin for adsorbing a hexahexitol all-dihydrogenphosphate inside, was divided into 7 zones, each of which consisted of:
an adsorption zone: contain 12 resin columns, 12 resin columns divide into series connection's first adsorption zone, second adsorption zone and third adsorption zone in proper order, and 4 resin columns that first adsorption zone, second adsorption zone and third adsorption zone include mutual parallel connection respectively, and the top feed liquor end in first adsorption zone links to each other with the liquid outlet of clarification fluid reservoir, and the bottom of third adsorption zone goes out the liquid end and connects down column liquid delivery pipe.
Compressed air blowing area: comprises 1 resin column, the top of the compressed air discharge area is connected with a compressed air pipe, and the bottom of the compressed air discharge area is connected with the liquid outlet end at the bottom of the first adsorption area.
A water washing area: contains 1 resin column, and the bottom inlet end of washing district is connected with the water pipe, and the top play liquid end is connected with the impurity discharge pipe.
Eluent top water area: contains 1 resin column, and the bottom inlet end of the eluent water-lifting area is connected with an eluent discharge pipe, and the top outlet end is connected with a material-lifting water discharge pipe.
A hydrochloric acid elution area: contain 4 resin columns, 4 resin columns divide into series connection's first elution district and second elution district, and first elution district and second elution are distinguished including 2 resin columns of mutual parallel connection, and hydrochloric acid pipe is connected to the bottom feed liquor end in first elution district, and the top play liquid end in second elution district connects the eluant delivery pipe.
An acid washing area: contain 4 resin columns, 4 resin columns divide into the first acid washing district and the second acid washing district of series connection, and first acid washing district and second acid washing district are respectively including 2 resin columns of mutual parallel connection, and the bottom feed liquor end in first acid washing district is connected from the water pipe, and the top that the second acid washing district goes out the liquid end and goes out the liquid end pipeline with the top in first elution district and link to each other.
Lower column liquid top water zone: comprises 1 resin column, the bottom liquid inlet end of the lower liquid injection and water ejection area is connected with a lower column liquid discharge pipe, and the top liquid outlet end is connected with a washing acid water discharge pipe.
Wherein, the compressed air blowing area, the adsorption area, the lower column liquid top water area, the acid washing area, the hydrochloric acid elution area, the eluent top water area and the water washing area are sequentially arranged along the circumferential direction.
Wherein, the resin filled in each resin column is macroporous anion resin.
Furthermore, the aperture of the ceramic membrane adopted by the ceramic membrane separation system is 50-200 nm.
The utility model discloses following beneficial effect has: 1. separating suspended matters in the soaking solution by using a ceramic membrane separation system so as to obtain clear feed liquid, thereby ensuring the service life and the extraction efficiency of the ion exchange resin; 2. the traditional fixed bed extraction method of the cyclohexanehexol-dihydrogen phosphate is broken through, the utilization rate of the resin can be effectively improved, the usage amount of the resin is reduced, the usage amount of the eluent is reduced, the concentration of the eluent is improved, the production period of the cyclohexanehexol-dihydrogen phosphate is shortened, and the production efficiency and the production quality are improved; 3. the use of water is effectively saved, and the discharge of waste water is reduced; 4. the traditional manual operation is changed into automatic production, so that the equipment investment is reduced, and the occupied area is reduced.
Drawings
Fig. 1 is a schematic structural diagram of the present invention.
Fig. 2 is a schematic diagram of a ceramic membrane separation system.
FIG. 3 is a schematic diagram of the structure of a continuous ion exchange system.
Description of the main component symbols: 1. a ceramic membrane separation system; 11. a soaking liquid tank; 12. a liquid pump; 13. a circulation pump; 14. a ceramic membrane separation unit; 15. a return pipe; 16. adjusting a valve; 17. an inner circulation pipe; 2. a clarifying liquid tank; 3. a continuous ion exchange system; 301. a lower column liquid discharge pipe; 302. a compressed air pipe; 303. a tap water pipe; 304. an impurity discharge pipe; 305. an eluent discharge pipe; 306. a top water discharge pipe; 307. a hydrochloric acid pipe; 308. a tap water pipe; 309. a washing acid water discharge pipe.
Detailed Description
The present invention will be further described with reference to the accompanying drawings and the following detailed description.
As shown in fig. 1-3, an extraction device of cyclohexanehexol-dihydrogen phosphate comprises a ceramic membrane separation system 1, a clarifying liquid tank 2 and a continuous ion exchange system 3 which are connected in sequence. The ceramic membrane separation system 1 comprises a soaking liquid tank 11, a liquid pump 12, a circulating pump 13 and a ceramic membrane separation unit 14 which are connected in sequence, wherein a concentrated liquid outlet of the ceramic membrane separation unit 14 is connected with the soaking liquid tank 11 through a return pipe 15, a penetrating liquid outlet is connected with a liquid inlet of the clarification liquid tank 2, and the aperture of a ceramic membrane adopted by the ceramic membrane separation unit 14 is 100 nm. The return pipe 15 is provided with a regulating valve 16, the return pipe 15 is provided with an internal circulation pipe 17 between the regulating valve 16 and the ceramic membrane concentrated solution outlet, and the internal circulation pipe 17 is connected with the front end of the circulation pump 13.
The continuous ion exchange system 3 comprises 24 resin columns in total, wherein the number of the resin columns is 1-24, the resin columns are uniformly distributed along the circumferential direction, macroporous anion resin used for adsorbing hexachlorocyclohexane hexa-perhydrogenphosphate is filled in each resin column, the continuous ion exchange system is divided into 7 areas, and each area comprises the following components:
an adsorption zone: contain 2 ~ 13 totally 12 resin columns, 12 resin columns divide into series connection's first adsorption zone (2 ~ 5), second adsorption zone (6 ~ 9) and third adsorption zone (10 ~ 13) in proper order, and first adsorption zone (2 ~ 5), second adsorption zone (6 ~ 9) and third adsorption zone (10 ~ 13) include 4 resin columns of mutual parallel connection respectively. The top liquid inlet end of the first adsorption zone (No. 2-5) is connected with the liquid outlet of the clarification liquid tank 2, and the bottom liquid outlet end of the third adsorption zone (No. 10-13) is connected with the lower column liquid discharge pipe 301.
Compressed air blowing area: contain 1 resin post (1), compressed air discharge area's top is connected compressed air pipe 302, and the bottom links to each other with the bottom play liquid end in first adsorption zone (2 ~ 5).
A water washing area: contains 1 resin column (No. 24), and the bottom inlet end of washing district is connected with water pipe 303, and the top play liquid end is connected with impurity discharge pipe 304.
Eluent top water area: comprises 1 resin column (No. 23), the bottom liquid inlet end of the eluent top water area is connected with an eluent discharge pipe 305, and the top liquid outlet end is connected with a top water discharge pipe 306.
A hydrochloric acid elution area: contain 4 resin column (19 ~ 22 No.), 4 resin column divide into series connection's first elution district (19, 20) and second elution district (21, 22 No.), first elution district (19, 20) and second elution district (21, 22 No.) include 2 resin column of mutual parallel connection respectively, hydrochloric acid pipe 307 is connected to the bottom feed liquor end in first elution district (19, 20 No.), the top play liquid end in second elution district (21, 22 No.) connects eluent discharge pipe 305.
An acid washing area: contain 4 resin columns (15 ~ 18), 4 resin columns divide into the first acid washing district (15, 16) and the second acid washing district (17, 18) of series connection, first acid washing district (15, 16) and second acid washing district (17, 18) are including 2 resin columns of mutual parallel connection respectively, water pipe 308 is connected to the bottom feed liquor end in first acid washing district (15, 16), the top that the second acid washing district (17, 18) goes out the liquid end and goes out the liquid end pipeline with the top that first elution district (19, 20) and link to each other.
Lower column liquid top water zone: comprises 1 resin column (No. 14), the liquid inlet end at the bottom of the lower liquid injection top water area is connected with a lower column liquid discharge pipe 301, and the liquid outlet end at the top is connected with a washing acid water discharge pipe 309.
Table 1 does the utility model discloses relevant parameter in the operation process:
TABLE 1
While the invention has been particularly shown and described with reference to a preferred embodiment, it will be understood by those skilled in the art that various changes in form and detail may be made therein without departing from the spirit and scope of the invention as defined by the appended claims.
Claims (7)
1. The utility model provides an extraction element of hexachlorocyclohexane hexa-per-dihydrogen phosphate which characterized in that: including consecutive ceramic membrane separation system, clarification fluid reservoir and continuous ion exchange system, ceramic membrane separation system including the soaking fluid reservoir, drawing liquid pump and the ceramic membrane separation unit that connect in order, the concentrate export of ceramic membrane separation unit passes through the back flow and links to each other with the soaking fluid reservoir, and the penetrant export links to each other with the inlet of clarification fluid reservoir, the back flow on be equipped with the governing valve, the inlet end of continuous ion exchange system links to each other with the liquid outlet of clarification fluid reservoir.
2. The apparatus for extracting cyclohexanehexol-perhydro phosphate according to claim 1, wherein: the ceramic membrane separation system also comprises a circulating pump and an internal circulating pipe, wherein the circulating pump is arranged on a connecting pipeline of the liquid pump and the ceramic membrane separation unit, one end of the internal circulating pipe is connected with the return pipe, and the other end of the internal circulating pipe is connected to the front end of the circulating pump.
3. The apparatus for extracting cyclohexanehexol-perhydro phosphate according to claim 1, wherein: the continuous ion exchange system comprises at least 2 resin columns which are uniformly distributed along the circumferential direction, and the inside of each resin column is filled with resin for adsorbing the hexachlorocyclohexane all-dihydrogen phosphate.
4. The apparatus for extracting cyclohexanehexol-perhydro-phosphate according to claim 3, wherein: the continuous ion exchange system comprises 24 resin columns, and is divided into 7 regions, wherein each region comprises the following components:
an adsorption zone: the device comprises 12 resin columns, wherein the 12 resin columns are divided into a first adsorption area, a second adsorption area and a third adsorption area which are sequentially connected in series, the first adsorption area, the second adsorption area and the third adsorption area respectively comprise 4 resin columns which are mutually connected in parallel, the liquid inlet end at the top of the first adsorption area is connected with the liquid outlet of a clarification liquid tank, and the liquid outlet end at the bottom of the third adsorption area is connected with a lower column liquid discharge pipe;
compressed air blowing area: the device comprises 1 resin column, the top of the compressed air discharging area is connected with a compressed air pipe, and the bottom of the compressed air discharging area is connected with the liquid outlet end at the bottom of the first adsorption area;
a water washing area: comprises 1 resin column, the bottom liquid inlet end of the washing area is connected with a running water pipe, and the top liquid outlet end is connected with an impurity discharge pipe;
eluent top water area: the device comprises 1 resin column, wherein the liquid inlet end at the bottom of an eluent water-lifting area is connected with an eluent discharge pipe, and the liquid outlet end at the top is connected with a material-lifting water discharge pipe;
a hydrochloric acid elution area: the elution device comprises 4 resin columns, wherein the 4 resin columns are divided into a first elution area and a second elution area which are connected in series, the first elution area and the second elution area respectively comprise 2 resin columns which are connected in parallel, the liquid inlet end at the bottom of the first elution area is connected with a hydrochloric acid pipe, and the liquid outlet end at the top of the second elution area is connected with an eluent discharge pipe;
an acid washing area: the device comprises 4 resin columns, wherein the 4 resin columns are divided into a first acid washing area and a second acid washing area which are connected in series, the first acid washing area and the second acid washing area respectively comprise 2 resin columns which are connected in parallel, the liquid inlet end at the bottom of the first acid washing area is connected with a tap water pipe, and the liquid outlet end at the top of the second acid washing area is connected with a liquid outlet end pipeline at the top of a first elution area;
lower column liquid top water zone: comprises 1 resin column, the bottom liquid inlet end of the lower liquid injection and water ejection area is connected with a lower column liquid discharge pipe, and the top liquid outlet end is connected with a washing acid water discharge pipe.
5. The apparatus for extracting cyclohexanehexol-perhydro-phosphate according to claim 4, wherein: the compressed air blowing area, the adsorption area, the lower column liquid top water area, the acid washing area, the hydrochloric acid elution area, the eluent top water area and the water washing area are sequentially arranged along the circumferential direction.
6. The apparatus for extracting cyclohexanehexol-perhydro-phosphate according to claim 4, wherein: the resin filled in each resin column is macroporous anion resin.
7. The apparatus for extracting cyclohexanehexol-perhydro-phosphate according to any one of claims 1 to 6, wherein: the ceramic membrane separation system adopts a ceramic membrane with the aperture of 50-200 nm.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201921226985.4U CN210885600U (en) | 2019-07-31 | 2019-07-31 | Extraction device of hexachlorocyclohexane hexa-holo-dihydrogen phosphate |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201921226985.4U CN210885600U (en) | 2019-07-31 | 2019-07-31 | Extraction device of hexachlorocyclohexane hexa-holo-dihydrogen phosphate |
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| CN210885600U true CN210885600U (en) | 2020-06-30 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201921226985.4U Withdrawn - After Issue CN210885600U (en) | 2019-07-31 | 2019-07-31 | Extraction device of hexachlorocyclohexane hexa-holo-dihydrogen phosphate |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110372127A (en) * | 2019-07-31 | 2019-10-25 | 赛普特环保技术(厦门)有限公司 | The extraction element and technique of a kind of complete-dihydrogen orthophosphate of inositol six |
-
2019
- 2019-07-31 CN CN201921226985.4U patent/CN210885600U/en not_active Withdrawn - After Issue
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110372127A (en) * | 2019-07-31 | 2019-10-25 | 赛普特环保技术(厦门)有限公司 | The extraction element and technique of a kind of complete-dihydrogen orthophosphate of inositol six |
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Granted publication date: 20200630 Effective date of abandoning: 20230530 |
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| AV01 | Patent right actively abandoned |
Granted publication date: 20200630 Effective date of abandoning: 20230530 |