US 4,127,598 AGrant
Process for Removing Biphenyls From Chlorosilanes
Issue Date:1978-11-28
•20 Claims
•1 Drawing Sheets
Abstract
A process for removing impurities such as biphenyls from impure silanes and siloxanes comprising contacting said impure silanes and siloxanes with an adsorbent bed selected from the class consisting of a molecular sieve bed and a charcoal bed such that said impurities are adsorbed on the bed and removing the purified silanes and siloxanes from said adsorbent.
Metadata
Inventor
- Harry R. McEntee
Application Information
Application Number:US 8283672
Filing Date:1977-08-29
Priority Date:1977-02-22
Art Unit:117
Classifications
IPC:
C07F 720
Field of Search:
260448.2 E
Patent Drawings (1 sheets)
Description
An exemplary schematic diagram of the instant process to be found in FIG. 1 which discloses a schematic diagram of the utilization of the most preferred embodiment of the instant invention.
In Part I of FIG. 1, line 2 shows the introduction of an impure stream of silane into the feed tank 4. From feed tank 4 through line 6 there is passed the impure stream of silanes and siloxanes from which there is to be removed biphenyls to adsorbent Columns A, B, & C connected in series by lines 6, 8, and 10. The adsorbent beds are filled with activated carbon.
Finally, the effluent stream emerges from Column C through line 12, then passes into line 14 to purified product tank 16. During such a process which is continuous Column D is shown in Part II of FIG. 1. Column D has reached its maximum point of adsorption and is thus taken off the adsorption stream of removing silanes and siloxanes from feed tank 4 through lines 6, 8 and 10. Accordingly, the silanes and siloxanes in Column D are displaced by the push hydrocarbon solvent iso-octane from tank 18. Iso-octane passes through line 20 to displace the silanes and siloxanes in Column D and the effluent in Column D passes through line 22 into distillation Column 24. In distillation Column 24 the iso-octane is purified and passed back through line 26 to the feed tank of iso-octane that is tank 18. The chlorosilanes that are removed during such distillation in distillation Column 24 are then passed through line 30 into feed tank 4 for further purification.
Column D is then processed through the desorption of the biphenyls in the adsorbent bed of Column D as shown in Part III of FIG. 1. Accordingly, chlorobenzene, a desorbent hydrocarbon solvent, is passed from tank 32 through line 34 in Column D to remove and displace the iso-octane therein and to desorb biphenyls adsorbed on the adsorbent bed.
Accordingly, the chlorobenzene effluent from Column D during this adsorption of biphenyl step is passed through line 36 to distillation Column 40 to purify and remove from distillation Column 40 purified iso-octane which passes through line 42 into iso-octane feed tank 18. It should be noted that new iso-octane is also fed into iso-octane feed tank 18 through line 19 as needed. With respect to Part III of FIG. 1, and with respect to distillation Column 40, the stream of chlorobenzene having chlorosilanes in it and biphenyls is passed from distillation Column 40 through line 44 into distillation Column 46 in which it is further purified to remove an overhead stream containing chlorobenzene and iso-octane, the push hydrocarbon solvent, as well a a minor amount of recovered chlorosilane residue from distillation Column 46, through line 48, valve 54 and line 56 in feed tank 32. A small amount of chlorosilane residue and a high concentration of biphenyls is then passed through line 50 into collection tank 52, where it is subsequently destroyed. There also may be utilized further processes to remove chlorosilanes from the contents of tank 52 before the contents are destroyed by combustion. The overhead stream from Distillation Column 46 passes through line 48 and through valve 54 and line 56 back into the chlorobenzene feed tank 32. If additional chlorobenzene is needed, it can be added to feed tank 32, through line 58.
Adsorption bed Column D is then subjected to the displacement of the chlorobenzene desorbent hydrocarbon solvent with purified chlorosilanes as shown in Part IV of FIG. 1. Purified chlorosilane product is passed from tank 16 in Part I through lines 14 and 58 into high purity chlorosilane tank 60. From tank 60, the purified chlorosilane is passed through line 62 into tank D to displace the chlorobenzene in the adsorbent bed in Column D. From Column D, the chlorobenzene and purified chlorosilanes are passed through overhead line 64 to distillation column 66. In distillation Column 66 the chlorobenzene desorbent hydrocarbon solvent is distilled overhead and passes through line 68, valve 54 and line 56 back into the chlorobenzene feed tank 32. The purified stream of chlorosilane product, as purified or separated from the chlorobenzene in distillation Column 66, then passes through line 70 into high purity chlorosilane feed tank 60, where it is kept for further use in the rejuvenation process of the adsorbent bed columns. At this point, Column D may now be reinserted into the adsorbent bed for adsorption of the biphenyls from the impure stream of chlorosilanes coming from tank 4, as shown in part I of FIG. 1, and another column may be taken out if it has reached its adsorption capacity and subjected to the rejuvenation procedures of Parts II, III and IV as explained above, of FIG. 1.
By the above explained procedure and as forth in the schematic diagram of FIG. 1, under the most preferred embodiment of the instant case there is a continuous process for the adsorbing of biphenyls from an impure stream of silanes and/or siloxanes as may be desired. It should be noted that the schematic diagram of FIG. 1, and as explained above, contains only one preferred embodiment in which the instant process may be utilized in a continuous manner. It should be noted that there may be any modifications to this process than as set forth in the drawing and as is desired and that the instant process can be continuous or may be batch in which the impure stream of silanes and siloxanes are passed through a single column or a number of columns and the columns may be simply shutdown for rejuvenation instead of utilizing the steps set forth in the embodiment of FIG. 1. Such modifications of the process of FIG. 1 or of any of the steps of the instant process will not be explained in detail since such modifications are obvious to a worker skilled in the art. Suffice to state that the process of the instant case may be modified as is desired to meet a particular need or to be utilized in a manner that produces the most efficiency in a particular purification situation of specific silanes and siloxanes. Although the schematic diagram of FIG. 1 shows a specific procedural set-up for chlorosilanes it may be utilized with well known modifications for the purification of siloxanes. It should be noted that the instant process with the above limitations and having an adsorbent bed to adsorb biphenyls from a stream of silanes and siloxanes may be modified in any way or manner to accomplish a specific purpose or meet a suitable need in the removal of biphenyls from streams of silanes or siloxanes.
The examples below are given for the purpose of illustrating the reduction to practice of the instant case. They are not given for any reason or purpose to limit the definition and scope of the instant invention. In the examples and in the disclosure above, the concentration of the biphenyls in the chlorosilane stream was determined as follows. A weighted portion of the chlorosilane effluent was taken and it was contacted with aqueous potassium hydroxide and hexane. The potassium hydroxide reacted with the chlorosilane and specifically the diphenyldichlorosilane so as to retain it in the aqueous phase and the biphenyls to migrate to the hexane phase. The hexane was then taken and separated and concentrated by stripping so as to concentrate the biphenyls. The hexane stream was then passed through gas chromatography to detect the amount of biphenyls in the initial sample in parts per billion. This method was used throughout the instant examples for measuring the concentration of biphenyls, either in the feed stream or in any of the samples from the product effluent streams as set forth in the examples. It should be noted that while the examples below describe the removal of biphenyls from diphenyldichlorosilanes, the same procedures can be used to remove biphenyls and the other impurities from any stream of silanes or siloxanes.
Example 1
To a vessel constructed of a 16 inch schedule 40 steel, ten feet long pipe, filled with 322 lbs. of dry adsorbent (activated carbon, type Pittsburgh CAL, 12 .times. 40 mesh, manufactured by Calgon Corp.) impure diphenyldichlorosilane (.phi..sub.2 SiCl.sub.2) containing 2060 PPM of biphenyls was pumped at a mass velocity of 175 lbs. per hour per square foot of vessel cross sectional area and the concentration of biphenyls in the stream as it left the vessel monitored with the following results:
Example 2
At the completion of Example 1, a total of 3630 lbs. of chlorobenzene was passed through the same bed of adsorbent to desorb the biphenyls and regenerate the bed. Impure .phi..sub.2 SiCl.sub.2 containing 1960 PPM of biphenyls was then passed through the bed at the same mass velocity used in Example 1 and the concentration of biphenyls in the effluent leaving the vessel monitored with the following results:
Example 3
At the completion of Example 2, the same bed was regenerated by passing chlorobenzene through bed, and then impure .phi..sub.2 SiCl.sub.2 containing 2780 PPM of biphenyls fed through the bed at the same mass velocity used in Example 1, and as before the concentration of biphenyls in the effluent leaving the vessel monitored with the following results:
Example 4
To the bed used in the above Examples, after regeneration by passing chlorobenzene through the bed, impure .phi..sub.2 SiCl.sub.2 containing 780 PPM of biphenyls was fed through the bed at the same mass velocity used in Example 1, and the concentration of biphenyls in the effluent leaving the vessel monitored with the following results:
The following two Examples demonstrate the efficacy of using a "Push Solvent" which is weakly adsorbed relative to biphenyls, for displacing and recovering the .phi..sub.2 SiCl.sub.2 left in the bed at the completion of adsorption steps (1) and (2) in the above description of the process.
Example 5
To a bed of 347 grams of dry adsorbent (activated carbon, type Pittsburgh CAL, 12 .times. 40 mesh, manufactured by Calgon Corp.) packed in a one inch, schedule 40 steel pipe, four feet long, impure .phi..sub.2 SiCl.sub.2 containing 4080 PPM of biphenyls was fed. When the effluent .phi..sub.2 SiCl.sub.2 contained 3380 PPM of biphenyls, impure .phi..sub.2 SiCl.sub.2 feed was stopped, and chlorobenzene was fed at a rate of 184 milliliters per hour. The concentrations of biphenyls and .phi..sub.2 SiCl.sub.2 in the effluent from the bed while the chlorobenzene was being fed were monitored with the following results:
Example 6
To a bed of 347 grams of dry absorbent (activated carbon, type Pittsburgh CAL, 12 .times. 40 mesh, manufactured by Calgon Corp.) packed in a one inch, schedule 40 steel pipe, 4 feet long, the same impure .phi..sub.2 SiCl.sub.2 used in Example 5 was fed. When the effluent .phi..sub.2 SiCl.sub.2 contained 3150 PPM of biphenyls impure .phi..sub.2 SiCl.sub.2 feed was stopped, and one liter of iso-octane was fed at a rate of 180 milliliters per hour. After completion of the feeding of iso-octane, chlorobenzene was then fed at the same rate. The concentration of biphenyls and .phi..sub.2 SiCl.sub.2 in the effluent from the bed while the iso-octane was being fed were monitored with the following results:
Comparison of the results of Examples 5 and 6 shows that the use of a solvent which is relatively weakly adsorbed by the bed, e.g. iso-octane as compared to a solvent which is more strongly adsorbed relative to the biphenyls, e.g. chlorobenzene, recovers the .phi..sub.2 SiCl.sub.2 left in the bed at the end of adsorption in a purer form. Thus, less processing of the recovered .phi..sub.2 SiCl.sub.2 to further purify is required and an overall improvement in the yield of purified .phi..sub.2 SiCl.sub.2 from the process realized. This is particularly important if product of very high purity is desired since the capacity of the bed, expressed as lbs of purified product per lb of adsorbent, decreases as the specification on the purity of the product is lowered, and because of the lowered purity specification more regeneration and reprocessing per lb of purified product is required. The increase in PPM of biphenyls in the recovered .phi..sub.2 SiCl.sub.2 for the last two data points in the above table are due to the appearance of chlorobenzene in the effluent which is beginning the desorption of the biphenyls from the bed. The following two Examples demonstrate the efficacy of displacing the desorption solvent by feeding purified .phi..sub.2 SiCl.sub.2 through the bed.
Example 7
To a bed of 347 grams of adsorbent (activated carbon, type Pittsburgh CAL, 12 .times. 40 mesh, manufactured by Calgon Corp.) packed in a 1 inch, schedule 40 steel pipe, four feet long, which had been previously used for adsorption of biphenyls from impure .phi..sub.2 SiCl.sub.2 and regenerated with chlorobenzene, impure .phi..sub.2 SiCl.sub.2 containing 4080 PPM of biphenyls was fed at a rate of 94 milliliters per hour. The bed was filled with chlorobenzene at the start of the impure .phi..sub.2 SiCl.sub.2 feeding. The concentration of biphenyls and .phi..sub.2 SiCl.sub.2 in the effluent from the bed were monitored with the following results:
Example 8
To a bed of 347 grams of adsorbent (activated carbon, type Pittsburgh CAL, 12 .times. 40 mesh, manufactured by Calgon Corp.) packed in a one inch, schedule 40 steel pipe, four feet long, which had been previously used for adsorption of biphenyls from impure .phi..sub.2 SiCl.sub.2 and regenerated with chlorobenzene, two liters of purified .phi..sub.2 SiCl.sub.2 containing three PPM of biphenyls was fed to displace the chlorobenzene from the bed. The same impure .phi..sub.2 SiCl.sub.2 used in Example 7 was then fed at a rate of 94 milliliters per hour. The concentration of biphenyls and .phi..sub.2 SiCl.sub.2 in the effluent from the bed were monitored with the following results for the effluent from the impure .phi..sub.2 SiCl.sub.2 after it had passed through the bed.
Comparison of the results of Examples 7 and 8 shows that displacement of the desorption solvent, e.g. chlorobenzene with purified .phi..sub.2 SiCl.sub.2 provides a product of improved purity when the adsorption step is resumed.
The following Example demonstrates the removal of biphenyls from .phi..sub.2 SiCl.sub.2 by various adsorbents of different types.
Example 9
Adsorbents listed below were each individually batch contacted with .phi..sub.2 SiCl.sub.2 containing biphenyls in the concentrations shown by shaking for 24 hours and the concentration of biphenyls in the treated .phi..sub.2 SiCl.sub.2 measured with the following results. In all experiments the weight ratio of untreated impure .phi..sub.2 SiCl.sub.2 to dry adsorbent was four.
Claims
I claim:
1. A process for removing biphenyls from impure silanes and siloxanes comprising ( 1) passing a first stream of impure silanes and siloxanes containing biphenyls into contact with an adsorbent bed selected from the class consisting of molecular sieves and charcoal and (2) adsorbing the biphenyls from said first stream of silanes and siloxanes on said adsorbent bed, and (3) removing a second stream of purified silanes and siloxanes from said adsorbent bed containing a smaller amount of biphenyls than said first stream.
2. The process of claim 1 wherein said first stream of silanes and siloxanes are passed into contact with said adsorbent bed until the silanes and siloxanes reach the desired purity and removing the second stream of the purified silanes and siloxanes from said adsorbent bed and then further comprising passing said first stream of impure silanes and siloxanes through said adsorbent bed until the adsorbent bed reaches a saturation point with respect to said biphenyls and removing partially purified silanes and siloxanes.
3. The process of claim 2 wherein said partially purified silanes and siloxanes are passed through additional adsorbent beds until the silanes and siloxanes reach the desired purity.
4. The process of claim 1 wherein after said adsorbent bed has reached the saturation point further comprising transmitting a push hydrocarbon solvent which is weakly adsorbed relative to said biphenyls to replace the purified silanes and siloxanes in said adsorbent bed.
5. The process of claim 4 further comprising passing into said adsorbent bed, a desorbent hydrocarbon solvent which is strongly adsorbent of said biphenyls relative to said adsorbent bed and which replaces said push hydrocarbon solvent in said adsorbent bed and recovering amount of said silanes and siloxanes from said push hydrocarbon solvent for further purification in an adsorbent bed.
6. The process of claim 1 comprising passing into said adsorbent bed, a desorbent hydrocarbon solvent which strongly adsorbs biphenyls from said adsorbent bed and which replaces the purified silanes and siloxanes in said adsorbent bed.
7. The process of claim 5, further comprising replacing said desorbent hydrocarbon solvent in said adsorbent bed with purified silanes and siloxanes and removing amounts of said silanes or siloxanes from said desorbent hydrocarbon solvent for further purification in an adsorbent bed.
8. The process of claim 7 further comprising removing said second stream of purified silanes and siloxanes from said adsorbent bed, collecting said silanes and siloxanes as purified product and passing said first stream of impure silanes and siloxanes through said adsorbent bed until said silanes or siloxanes reach the desired purity.
9. The process of claim 1 wherein the impure silanes and siloxanes are impure phenylchlorosilanes.
10. The process of claim 9 wherein said impure phenylchlorosilanes are diphenyldichlorosilanes.
11. The process of claim 1 wherein the process is carried out at ambient temperatures.
12. The process of claim 4 wherein said push hydrocarbon solvent is a saturated aliphatic hydrocarbon solvent of 4 to 16 carbon atoms.
13. The process of claim 12 wherein said push hydrocarbon solvent is iso-octane.
14. The process of claim 6 wherein said desorbent hydrocarbon solvent is selected from the class consisting of aromatic solvents, chlorinated aromatic solvents and chlorinated aliphatic solvents.
15. The process of claim 14 wherein said desorbent hydrocarbon solvent is chlorobenzene.
16. The process of claim 1 wherein said adsorbent bed comprises activated carbon of a size varying from 4000 mesh to one quarter of an inch.
17. The process of claim 1 wherein said silanes and siloxanes are fed through said adsorbent bed at a rate varying from 5 to 500 lbs. per hour, per square foot of the cross-section of the adsorbent bed.
18. The process of claim 1 further comprising transmitting inert gas through said adsorbent bed to remove said silane and siloxanes that fill the voids in said adsorbent bed and removing partially purified silanes and siloxanes for further purification.
19. The process of claim 18 further comprising heating said adsorbent bed to above 100.degree. C for a sufficient time to remove the biphenyls and silanes and siloxanes adsorbed in said adsorbent bed with a stream of an inert gas and further purifying said impure silanes and siloxanes by passing through an adsorbent bed.
20. A process for removing biphenyls from impure silanes and siloxanes comprising (1) passing a first stream of impure silanes and siloxanes containing biphenyls into contact with an adsorbent bed selected from the class consisting of molecular sieves and charcoal; (2) adsorbing the biphenyls from said first stream on said adsorbent bed; (3) removing a second stream of purified silanes and siloxanes from said adsorbent bed containing a lesser amount of biphenyls than said first stream while said purified silanes and siloxanes do not exceed the desire purity; (4) continuing transmitting of said first stream of impure silanes and siloxanes through said adsorbent bed until said adsorbent bed reaches the saturation point with respect to the adsorption of said biphenyls; (5) adding a push hydrocarbon solvent to said adsorbent bed to displace and recover a quantity of silanes and siloxanes with a large quantity of biphenyls from said adsorbent bed for further purification; (6) passing a desorbent hydrocarbon solvent through said adsorbent bed to remove said push hydrocarbon solvent and removing a quantity of impure silanes and siloxanes containing large amounts of biphenyls from said push hydrocarbon solvent for further purification and said desorbent solvent adsorbing the biphenyls from the adsorbent bed (7) replacing said desorbent hydrocarbon solvent in said adsorbent bed with a quantity of purified silanes and siloxanes containing a small quantity of biphenyls (8) recovering said purified silanes and siloxanes containing a small quantity of biphenyls from said adsorbent bed; and (9) passing said first stream of impure silanes or siloxanes through said adsorbent bed and recovering said second stream of purified silanes and siloxanes containing a smaller quantity of biphenyls then said first stream therefrom.
Patent Citations (1)
| Patent | Date | Inventor | Cited By |
|---|---|---|---|
| US2972626 | 1961-02-01 | Marotta |
Non-Patent Literature (1)
- Bernardin, "Results of Field Tests to Determine Effectiveness of Granular Carbon for Removal of Polychlorinated Biphenyls from Industrial Effluent", Calgon Corp.