CN105016320A - Continuous refinement system and technology of ultra-pure phosphorus oxychloride of 5N grade - Google Patents
Continuous refinement system and technology of ultra-pure phosphorus oxychloride of 5N grade Download PDFInfo
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Abstract
The invention discloses a continuous refinement system of ultra-pure phosphorus oxychloride of a 5N grade. The continuous refinement system comprises feeding storage tanks, wherein the feeding storage tanks are communicated with a middle raw-material tank; a discharge opening of the middle raw-material tank is connected with a feed opening of a rectification kettle and a shell-side feed opening of a first condenser respectively; a discharge opening in the top end of the rectification kettle is connected with a tube-side steam feed opening of the first condenser through a rectification tower; a shell-side discharge opening of the first condenser is connected with a feed opening of the middle raw-material tank; a tube-side condensate-liquid discharge opening of the first condenser is connected with a finished-product collecting unit; a tube-side light-component discharge opening of the first condenser is connected with a light-component treating unit; a kettle-bottom heavy-component discharge opening of the rectification kettle is connected with a waste-liquid treating unit; a jacket of the raw-material middle tank and a jacket of the rectification kettle are connected with a circular heating unit of heat conducting oil; a vacuum pump for evacuation is arranged in the light-component treating unit. The continuous refinement system is protected by nitrogen. The invention further discloses a continuous refinement technology. The continuous refinement technology is short in engineering, and the purity of obtained products is high.
Description
Technical field
The present invention relates to electronic chemical product production technical field, be specifically related to continuous purification system and the technique of the ultra-pure phosphorus oxychloride of a kind of 5N level.
Background technology
High-purity phosphorus oxychloride is the doping agent of unicircuit, manufacture of solar cells, one of starting material manufacturing preform, its purity requirement is up to 4N level, namely purity is more than 99.9999%, particularly large-scale integrated circuit phosphorus oxychloride, requires that individual event metals content impurity is no more than 10ppb.
China Patent Publication No. CN101570323 discloses one " purity is production method and the device thereof of 99.99999% phosphorus oxychloride " on November 04th, 2009, and phosphorus oxychloride wherein obtains the phosphorus oxychloride that purity is 99.99999% after purifying and adopting rectifying, two-stage quartz sub-boiling distillation.This continuous purifying technique process is complicated, and to meet water reaction violent due to phosphorus oxychloride, and based on security consideration, common condensing works is not suitable for the condensation of phosphorus oxychloride.
China Patent Publication No. CN102126711B discloses on July 20th, 2011 production method that a kind of purity is 5N grade phosphorus oxytrichloride: add compound complex agent A in by the technical grade phosphorus oxychloride 99.5%, after stratification, first time distillation is carried out to supernatant liquid, collect the low-boiling-point substance before 100 DEG C that single flash produces and 107 DEG C of later heavy constituents, compound complex agent B is added in above-mentioned heavy constituent, after stratification, second time distillation is carried out to supernatant liquid, collect the low-boiling-point substance before 100 DEG C that second distillation produces and 107 DEG C of later heavy constituents, namely 5N grade phosphorus oxytrichloride is obtained.Compound complex agent A be by phosphoric acid and primary ammonium phosphate formulated, compound complex agent B is formulated by citric acid, oxalic acid, phosphoric acid and primary ammonium phosphate.In the product that above-mentioned technique is made, individual event metals content impurity is no more than 8ppb, as Al < 8ppb, As < 6ppb, Ba < 1ppb, Cr < 1ppb, Ca < 5ppb, Fe < 8ppb, Mg < 5ppb, Pb < 3ppb, Mn < 1ppb, Ni < 1ppb, Zn < 1ppb, 20 remainder metallic impurity total amounts are no more than 80ppb, meet solar cell doping completely, the service requirements of large-scale integrated circuit etc.US5993609 discloses a kind of recovery of purifying and comprises the continuous purifying technique with reactive organic phosphorus oxychloride, 0.1 ~ 5% massfraction organism (pyridines) is added in phosphorus oxychloride, metal ion is eliminated by its complexing action, then air distillation is carried out, the total content < 5ppm of Fe, Cr, Ni of gained phosphorus oxychloride.All adopt the metal ion in the mode complexing removal phosphorus oxychloride of adding complex compound in above-mentioned two kinds of methods of purification, need the purity strictly controlling the complexing agent raw material added, cost is high, and continuous purifying technique route growth process is complicated.
Summary of the invention
The object of the invention is to the defect overcoming prior art, the continuous purification system of the ultra-pure phosphorus oxychloride of 5N level that a kind of operational path is short, product purity is high is provided.
Another object of the present invention is to the defect overcoming prior art, the continuous purifying technique of the ultra-pure phosphorus oxychloride of 5N level that a kind of operational path is short, product purity is high is provided.
For achieving the above object, technical scheme of the present invention is the continuous purification system of the ultra-pure phosphorus oxychloride of a kind of 5N level, it is characterized in that, comprise feed storage tank, feed storage tank is communicated with raw material tundish, the discharge port of raw material tundish is connected with the opening for feed of rectifying still and the shell side opening for feed of the first condenser respectively, the top discharge port of rectifying still is connected with the tube side vapor feed of the first condenser by rectifying tower, the shell side discharge port of the first condenser is connected with the opening for feed of raw material tundish, the tube side phlegma discharge port of the first condenser is connected with finished product collector unit, the tube side light constituent discharge port of the first condenser is connected with light constituent processing unit, at the bottom of the still of rectifying still, heavy constituent discharge port is connected with waste disposal unit, raw material tundish are connected with thermal oil circulating-heating unit with the chuck of rectifying still, be communicated with in described light constituent processing unit and be provided with vacuum buffer tank, described vacuum buffer tank is communicated with vacuum pump by valve tube, feed storage tank, raw material tundish, rectifying still is communicated with Nitrogen source gases respectively.
In order to accurately control the temperature of raw material tundish Raw, namely the feeding temperature as the shell side phosphorus oxychloride of cooling medium in the first condenser is controlled, preferred technical scheme is, thermal oil circulating-heating unit comprises thermal oil surge tank, thermal oil cooling loop is formed by pipeline between thermal oil surge tank and freezing unit, the discharge port of thermal oil surge tank is communicated with the chuck of the second branch road with raw material tundish by the first branch road, second branch road is connected with hot oil heater, the thermal oil outlet of hot oil heater is communicated with the chuck of rectifying still, the chuck of raw material tundish is connected with thermal oil surge tank with the thermal oil outlet of the chuck of rectifying still.
Preferred technical scheme is, the pipeline between the shell side opening for feed of rectifying tower top end discharge port and the first condenser is connected with POLYTETRAFLUOROETHYLSIFTER SIFTER mist eliminator, can plays gas-liquid separation and heavy metal particles, makes the metals content impurity of product less.
In order to realize being further processed light constituent, avoid directly emptyingly causing topsoil, preferred technical scheme is, light constituent processing unit comprises the light constituent receiving tank be connected with the tube side light constituent discharge port of the first condenser, the top vapor outlet port of described light constituent receiving tank is provided with the second condenser, and the top discharge port of the second condenser is connected with vacuum buffer tank.
Preferred technical scheme is, waste disposal unit comprises the first waste liquid surge tank and the second waste liquid surge tank that are connected with heavy constituent discharge port at the bottom of the still of rectifying still respectively, and the first waste liquid surge tank is connected with waste material storage tank with the discharge port of the second waste liquid surge tank.Be parallel relationship between first waste liquid surge tank and the second waste liquid surge tank, when a waste liquid surge tank breaks down and closes wherein, another waste liquid surge tank can normally work, and ensures the normal operation of brush system.
Preferred technical scheme is, the connecting pipeline between the discharge port of raw material tundish and the opening for feed of rectifying still is provided with raw material and refluxes branch road, and described raw material backflow branch road is connected with raw material tundish.Continuous seepage need to ensure the phosphorus oxychloride temperature charging in rectifying still before and after the temperature difference less, do not affect the steam discharging in rectifying still, therefore need to control inlet amount, the inlet amount that moment opened by feed valve is larger, when controlling feed valve closedown according to the temperature of material in rectifying still, pressure in feeding pipe is higher, and high line pressure can affect the life-span of production system, and the raw material when road arranging raw material backflow can make feed valve close in feeding pipe is back in raw material tundish.
Preferred technical scheme is, the connecting pipeline between the discharge port of raw material tundish and the shell side opening for feed of the first condenser is provided with safety return-flow branch road, and described safety return-flow branch road is connected with raw material tundish.During whole system start work, material temperature is lower, is not suitable for the heat-eliminating medium as phosphorus oxychloride steam, needs to reflux for some time to condensing temperature to the raw material in raw material tundish.Valve open on safety return-flow branch road, the valve closes of the shell side opening for feed of the first condenser can realize the raw material backflow in raw material tundish simultaneously; Valve closes under condensing state on safety return-flow branch road, the simultaneously valve open of the shell side opening for feed of the first condenser.
For achieving the above object, another technical scheme of the present invention is the continuous purifying technique of the ultra-pure phosphorus oxychloride of a kind of 5N level, it is characterized in that, technological process is: open nitrogen air valve and make continuous purification system emptying, raw material phosphorus oxychloride pumps in raw material tundish, the discharging of raw material tundish is in rectifying still, heat-conducting oil heating in rectifying still chuck, phosphorus oxychloride in rectifying still enters the tube side of the first condenser through rectifying tower and mist eliminator, raw material in raw material tundish imports the shell side of the first condenser as cooling medium after reaching condensing temperature, tube side gained phlegma imports finished product collector unit, tube side gained light constituent steam imports light constituent processing unit, at the bottom of still residual in rectifying still, heavy constituent imports waste disposal unit.
Preferred technical scheme is, entering in the first condenser as the phosphorus oxychloride material temperature of cooling medium is 55 ~ 70 DEG C.In phosphorus oxychloride, the boiling point of high price arsenic is lower, discharges with phosphorus oxychloride steam, and in the first condenser, the too low meeting of the temperature of cooling medium causes the direct condensation of high price arsenic compound, derives with finished product; Otherwise the too high yield that can affect finished product of temperature of cooling medium, controls the temperature of cooling medium in 55 ~ 70 DEG C of intervals, the yield that phosphorus oxychloride is purified can be improved as far as possible, reduce the content of wherein arsenic compound simultaneously.
In order to ensure production safety, preferred technical scheme is, the working pressure of raw material tundish is 0.1 ~ 0.2bar.
Advantage of the present invention and beneficial effect are:
The continuous purification system of the ultra-pure phosphorus oxychloride of 5N level of the present invention adopts phosphorus oxychloride raw material as the heat-eliminating medium of condenser in rectification process, can avoid completely adopting other heat-eliminating mediums and the potential safety hazard that produces, equipment for purifying safety and reliability;
By arranging raw material tundish, chuck heat-conducting oil heating makes the raw material in it keep constant temperature, contributes to the yield improving 5N grade phosphorus oxytrichloride purification system; Feed storage tank in purification system, raw material tundish, rectifying still are communicated with Nitrogen source gases respectively, can phosphorus oxychloride be avoided completely to contact with water vapour, reduce industrial accident probability, ensure phosphorus oxychloride purity;
The continuous purification system of the ultra-pure phosphorus oxychloride of 5N level of the present invention does not need to add the materials such as complexing agent in addition, and therefore can avoid introducing new impurity in raw material, operational path is simple to operation short across journey, and cost is lower, is more suitable for scale production;
Detect through ICP-MS, products obtained therefrom purity reaches 5N level, and wherein arsenic impurities content is less than 10ppb.
Accompanying drawing explanation
Fig. 1 is the structural representation of the continuous purification system of the ultra-pure phosphorus oxychloride of 5N level of the present invention;
Fig. 2 is the structural representation of thermal oil circulating-heating unit in the present invention.
In figure: 1, feed storage tank; 2, raw material tundish; 3, rectifying still; 4, the first condenser; 5, rectifying tower; 6, vacuum buffer tank; 7, vacuum pump; 8, thermal oil surge tank; 9, freezing unit; 10, hot oil heater; 11, POLYTETRAFLUOROETHYLSIFTER SIFTER mist eliminator; 12, light constituent receiving tank; 13, the second condenser; 14, the first waste liquid surge tank; 15, the second waste liquid surge tank; 16, waste material storage tank.
Embodiment
Below in conjunction with drawings and Examples, the specific embodiment of the present invention is further described.Following examples only for technical scheme of the present invention is clearly described, and can not limit the scope of the invention with this.
Embodiment 1
As depicted in figs. 1 and 2, the continuous purification system of the ultra-pure phosphorus oxychloride of 5N level of embodiment, comprise feed storage tank 1, feed storage tank 1 is communicated with raw material tundish 2, the discharge port of raw material tundish 2 is connected with the opening for feed of rectifying still 3 and the shell side opening for feed of the first condenser 4 respectively, the top discharge port of rectifying still 3 is connected with the tube side vapor feed of the first condenser 4 by rectifying tower 5, the shell side discharge port of the first condenser 4 is connected with the opening for feed of raw material tundish 2, the tube side phlegma discharge port of the first condenser 4 is connected with finished product collector unit, the tube side light constituent discharge port of the first condenser 4 is connected with light constituent processing unit, at the bottom of the still of rectifying still 3, heavy constituent discharge port is connected with waste disposal unit, raw material tundish 2 are connected with thermal oil circulating-heating unit with the chuck of rectifying still 3, be communicated with in light constituent processing unit and be provided with vacuum buffer tank 6, vacuum buffer tank 6 is communicated with vacuum pump 7 by valve tube, feed storage tank 1, raw material tundish 2, rectifying still 3 is communicated with Nitrogen source gases respectively.In Fig. 1, arrow represents the flow direction of material in phosphorus oxychloride purification system, and in Fig. 2, arrow represents the flow direction of thermal oil in thermal oil circulating-heating unit.
Thermal oil circulating-heating unit comprises thermal oil surge tank 8, thermal oil cooling loop is formed by pipeline between thermal oil surge tank 8 and freezing unit 9, the discharge port of thermal oil surge tank 8 is communicated with the chuck of the second branch road with raw material tundish 2 by the first branch road, second branch road is connected with hot oil heater 10, the thermal oil outlet of hot oil heater 10 is communicated with the chuck of rectifying still 3, and the chuck of raw material tundish 2 is connected with thermal oil surge tank 8 with the thermal oil outlet of the chuck of rectifying still 3.
Pipeline between the shell side opening for feed of rectifying tower 3 top discharge port and the first condenser 4 is connected with POLYTETRAFLUOROETHYLSIFTER SIFTER mist eliminator 11.
Light constituent processing unit comprises the light constituent receiving tank 12 be connected with the tube side light constituent discharge port of the first condenser 4, the top discharge port that the top vapor outlet port of light constituent receiving tank 12 is provided with the second condenser 13, second condenser 13 is connected with vacuum buffer tank 6.
Waste disposal unit comprises the first waste liquid surge tank 14 of being connected with heavy constituent discharge port at the bottom of the still of rectifying still 3 respectively and the second waste liquid surge tank 15, first waste liquid surge tank 14 is connected with waste material storage tank 16 with the discharge port of the second waste liquid surge tank 15.
Connecting pipeline between the discharge port of raw material tundish 2 and the opening for feed of rectifying still 3 is provided with raw material to reflux branch road, raw material backflow branch road is connected with raw material tundish 2.
Connecting pipeline between the discharge port of raw material tundish 2 and the shell side opening for feed of the first condenser 4 is provided with safety return-flow branch road, and safety return-flow branch road is connected with raw material tundish 2.
Concrete, need to be provided with at least two feed storage tanks in purification system, to meet the continuous feeding of purifying continuously; Usually the finished pot that at least two parallel waies connect also is comprised in finished product collector unit, the discharging of finished pot exports to finished product dispensing apparatus or finished product holding tank by conduit, finished pot discharging pipeline is provided with finished product loop, and finished product loop is connected with raw material tundish; Second condenser adopts the mode of pressurized air condensation, and that avoids the phosphorus oxychloride contained in condenser fault light constituent to contact with large water gaging may; The discharge port of raw material tundish is same with on the pipeline that the opening for feed of rectifying still and the shell side opening for feed of the first condenser connect respectively is provided with two cover discharging recycle pumps and corresponding valve, and wherein a set of discharging recycle pump and corresponding valve are as emergency power during fault.
The continuous purifying technique of the ultra-pure phosphorus oxychloride of 5N level in embodiment 1, technological process is: open nitrogen air valve and make continuous purification system emptying, raw material phosphorus oxychloride pumps in raw material tundish, the discharging of raw material tundish is in rectifying still, heat-conducting oil heating in rectifying still chuck, phosphorus oxychloride in rectifying still enters the tube side of the first condenser through rectifying tower and mist eliminator, raw material in raw material tundish imports the shell side of the first condenser as cooling medium after reaching condensing temperature, tube side gained phlegma imports finished product collector unit, tube side gained light constituent steam imports light constituent processing unit, at the bottom of still residual in rectifying still, heavy constituent imports waste disposal unit.
Entering in the first condenser as the phosphorus oxychloride material temperature of cooling medium is 55 DEG C; The working pressure of raw material tundish is 0.1bar.
Product detects through ICP-MS, every metals content impurity: Al=11.67ppb, Ag=0.45ppb, As=23.86ppb, Au=0.33ppb, Ba=2.82ppb, Bi=0.23ppb, Ca=15.24ppb, Co=0.35ppb, Cu=3.27ppb, Fe=8.72ppb, Ga=0.32ppb, Hg=3.58ppb, K=4.01ppb, Li=0.77ppb, Mg=3.11ppb, Mn=1.08ppb, Na=7.26ppb, Ni==2.47ppb, Nb=2.95ppb, Pb=1.26ppb, Sn=1.28ppb, Sr=0.43ppb, Ti=0.8ppb, Zn=3.92ppb.
Embodiment 2
Embodiment 2 is with the difference of embodiment 1, and entering in the first condenser as the phosphorus oxychloride material temperature of cooling medium is 60 DEG C; The working pressure of raw material tundish is 0.15bar.
Product detects through ICP-MS, every metals content impurity: Al=10.52ppb, Ag=0.48ppb, As=2.87ppb, Au=0.28ppb, Ba=1.74ppb, Bi=0.25ppb, Ca=13.61ppb, Co=0.25ppb, Cu=3.34ppb, Fe=7.53ppb, Ga=0.62ppb, Hg=2.82ppb, K=5.2ppb, Li=1.37ppb, Mg=2.47ppb, Mn=1.4ppb, Na=5.95ppb, Ni==3.68ppb, Nb=1.6ppb, Pb=1.21ppb, Sn=1.1ppb, Sr=0.5ppb, Ti=1.37ppb, Zn=2.17ppb.
Embodiment 3
Embodiment 2 is with the difference of embodiment 1, and entering in the first condenser as the phosphorus oxychloride material temperature of cooling medium is 70 DEG C; The working pressure of raw material tundish is 0.2bar.
Product detects through ICP-MS, every metals content impurity: Al=9.53ppb, Ag=0.59ppb, As=3.51ppb, Au=0.6ppb, Ba=1.8ppb, Bi=1.35ppb, Ca=3.85ppb, Co=0.23ppb, Cu=0.52ppb, Fe=7.41ppb, Ga=0.24ppb, Hg=2.29ppb, K=1.37ppb, Li=3.35ppb, Mg=4.58ppb, Mn=0.57ppb, Na=2.14ppb, Ni==0.38ppb, Nb=0.74ppb, Pb=2.74ppb, Sn=0.19ppb, Sr=0.1ppb, Ti=0.15ppb, Zn=0.32ppb.
Consider the thermal losses of material pipeline, the temperature of raw material tundish needs a little higher than above-mentioned phosphorus oxychloride feeding temperature, and raw material tundish general control is at 70 DEG C, and product yield is 85%, and wherein, the phosphorus oxychloride purified product yield of embodiment 1 is the highest.
In embodiment, the material of raw material tundish and rectifying still is enamel, and the material of feed storage tank, the first condenser, the second condenser, waste liquid surge tank is the low borosilicate glass of electronic-grade.
The above is only the preferred embodiment of the present invention; it should be pointed out that for those skilled in the art, under the prerequisite not departing from the technology of the present invention principle; can also make some improvements and modifications, these improvements and modifications also should be considered as protection scope of the present invention.
Claims (10)
1. the continuous purification system of the ultra-pure phosphorus oxychloride of 5N level, it is characterized in that, comprise feed storage tank, feed storage tank is communicated with raw material tundish, the discharge port of raw material tundish is connected with the opening for feed of rectifying still and the shell side opening for feed of the first condenser respectively, the top discharge port of rectifying still is connected with the tube side vapor feed of the first condenser by rectifying tower, the shell side discharge port of the first condenser is connected with the opening for feed of raw material tundish, the tube side phlegma discharge port of the first condenser is connected with finished product collector unit, the tube side light constituent discharge port of the first condenser is connected with light constituent processing unit, at the bottom of the still of rectifying still, heavy constituent discharge port is connected with waste disposal unit, raw material tundish are connected with thermal oil circulating-heating unit with the chuck of rectifying still, be communicated with in described light constituent processing unit and be provided with vacuum buffer tank, described vacuum buffer tank is communicated with vacuum pump by valve tube, feed storage tank, raw material tundish, rectifying still is communicated with Nitrogen source gases respectively.
2. the continuous purification system of the ultra-pure phosphorus oxychloride of 5N level according to claim 1, it is characterized in that, thermal oil circulating-heating unit comprises thermal oil surge tank, thermal oil cooling loop is formed by pipeline between thermal oil surge tank and freezing unit, the discharge port of thermal oil surge tank is communicated with the chuck of the second branch road with raw material tundish by the first branch road, second branch road is connected with hot oil heater, the thermal oil outlet of hot oil heater is communicated with the chuck of rectifying still, the chuck of raw material tundish is connected with thermal oil surge tank with the thermal oil outlet of the chuck of rectifying still.
3. the continuous purification system of the ultra-pure phosphorus oxychloride of 5N level according to claim 1, is characterized in that, the pipeline between the shell side opening for feed of rectifying tower top end discharge port and the first condenser is connected with POLYTETRAFLUOROETHYLSIFTER SIFTER mist eliminator.
4. the continuous purification system of the ultra-pure phosphorus oxychloride of 5N level according to claim 1, it is characterized in that, light constituent processing unit comprises the light constituent receiving tank be connected with the tube side light constituent discharge port of the first condenser, the top vapor outlet port of described light constituent receiving tank is provided with the second condenser, and the top discharge port of the second condenser is connected with vacuum buffer tank.
5. the continuous purification system of the ultra-pure phosphorus oxychloride of 5N level according to claim 1, it is characterized in that, waste disposal unit comprises the first waste liquid surge tank and the second waste liquid surge tank that are connected with heavy constituent discharge port at the bottom of the still of rectifying still respectively, and the first waste liquid surge tank is connected with waste material storage tank with the discharge port of the second waste liquid surge tank.
6. the continuous purification system of the ultra-pure phosphorus oxychloride of 5N level according to claim 1, it is characterized in that, connecting pipeline between the discharge port of raw material tundish and the opening for feed of rectifying still is provided with raw material to reflux branch road, described raw material backflow branch road is connected with raw material tundish.
7. the continuous purification system of the ultra-pure phosphorus oxychloride of 5N level according to claim 1, it is characterized in that, connecting pipeline between the discharge port of raw material tundish and the shell side opening for feed of the first condenser is provided with safety return-flow branch road, and described safety return-flow branch road is connected with raw material tundish.
8. the continuous purifying technique of the ultra-pure phosphorus oxychloride of 5N level, it is characterized in that, technological process is: open nitrogen air valve and make continuous purification system emptying, raw material phosphorus oxychloride pumps in raw material tundish, the discharging of raw material tundish is in rectifying still, heat-conducting oil heating in rectifying still chuck, phosphorus oxychloride in rectifying still enters the tube side of the first condenser through rectifying tower and mist eliminator, raw material in raw material tundish imports the shell side of the first condenser as cooling medium after reaching condensing temperature, tube side gained phlegma imports finished product collector unit, tube side gained light constituent steam imports light constituent processing unit, at the bottom of still residual in rectifying still, heavy constituent imports waste disposal unit.
9. the continuous purifying technique of the ultra-pure phosphorus oxychloride of 5N level according to claim 8, is characterized in that, entering in the first condenser as the phosphorus oxychloride material temperature of cooling medium is 55 ~ 70 DEG C.
10. the continuous purifying technique of the ultra-pure phosphorus oxychloride of 5N level according to claim 9, is characterized in that, the working pressure of raw material tundish is 0.1 ~ 0.2bar.
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106237645A (en) * | 2016-10-19 | 2016-12-21 | 天津瑞岭化工有限公司 | A kind of water vapor distillation apparatus and its implementation |
| CN108950208A (en) * | 2018-06-04 | 2018-12-07 | 山东习尚喜新材料科技股份有限公司 | A kind of continuous production device and technique of metallic potassium |
| CN110203897A (en) * | 2018-02-28 | 2019-09-06 | 彩客科技（北京）有限公司 | A kind of purification process of industrial phosphorus oxychloride |
| CN115231535A (en) * | 2022-06-15 | 2022-10-25 | 浙江海昇药业股份有限公司 | Environment-friendly and safe phosphorus oxychloride taking system and method |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH1192121A (en) * | 1997-07-15 | 1999-04-06 | Bayer Ag | Method for purifying phosphorus oxychloride |
| CN101570323A (en) * | 2009-06-10 | 2009-11-04 | 向东 | Method for producing phosphorus oxychloride with purity of 99.99999 percent and device thereof |
| CN202214221U (en) * | 2011-07-15 | 2012-05-09 | 株洲石英化玻有限公司 | Phosphorus oxychloride purification device |
| CN204824176U (en) * | 2015-07-10 | 2015-12-02 | 江阴江化微电子材料股份有限公司 | Pure phosphorous oxychloride's of 5N level superelevation continuous purification system |
-
2015
- 2015-07-10 CN CN201510402701.2A patent/CN105016320B/en active Active
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH1192121A (en) * | 1997-07-15 | 1999-04-06 | Bayer Ag | Method for purifying phosphorus oxychloride |
| CN101570323A (en) * | 2009-06-10 | 2009-11-04 | 向东 | Method for producing phosphorus oxychloride with purity of 99.99999 percent and device thereof |
| CN202214221U (en) * | 2011-07-15 | 2012-05-09 | 株洲石英化玻有限公司 | Phosphorus oxychloride purification device |
| CN204824176U (en) * | 2015-07-10 | 2015-12-02 | 江阴江化微电子材料股份有限公司 | Pure phosphorous oxychloride's of 5N level superelevation continuous purification system |
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106237645A (en) * | 2016-10-19 | 2016-12-21 | 天津瑞岭化工有限公司 | A kind of water vapor distillation apparatus and its implementation |
| CN110203897A (en) * | 2018-02-28 | 2019-09-06 | 彩客科技（北京）有限公司 | A kind of purification process of industrial phosphorus oxychloride |
| CN108950208A (en) * | 2018-06-04 | 2018-12-07 | 山东习尚喜新材料科技股份有限公司 | A kind of continuous production device and technique of metallic potassium |
| CN108950208B (en) * | 2018-06-04 | 2023-09-29 | 山东习尚喜新材料科技股份有限公司 | Continuous production device and process of metal potassium |
| CN115231535A (en) * | 2022-06-15 | 2022-10-25 | 浙江海昇药业股份有限公司 | Environment-friendly and safe phosphorus oxychloride taking system and method |
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| CN105016320B (en) | 2017-03-08 |
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