Patent Application
20090026062
NONE
NONE
This invention is directed to a method of separating crude chlorosilane streams containing mixtures of close-boiling chlorosilanes with a distillation aid that is a mono-cyano-substituted organic compound, a nitro-substituted organic compound, a mono-cyano-substituted organosilicon compound, a nitro-substituted organosilicon compound, or a mixture thereof. Lower-boiling chlorosilanes are removed from the crude chlorosilane stream, and the distillation aid and the higher-boiling chlorosilanes are separated from one another.
During the reaction of methyl chloride with silicon, a crude chlorosilane stream is produced. These are normally separated by distillation. Two of the largest volume chlorosilanes are dimethyldichlorosilane Me2SiCl2 and methyltrichlorosilane MeSiCl3. In order to prepare satisfactory siloxane polymers from dimethyldichlorosilane, it is sometimes necessary that the methyltrichlorosilane content of the dimethyldichlorosilane be reduced to trace amounts. The boiling points of methyltrichlorosilane (66.1° C.) and dimethyldichlorosilane (70.1° C.) are sufficiently close that distillation columns of 200 stages or more are required to satisfactorily separate these materials in commercial operations. Consequently, a large capital investment is required in order to install these columns, and it would be highly desirable to reduce this capital investment. Also, a large column generally requires more energy to operate than a smaller column. Careful fractional distillation is also employed by the organosilicon industry to separate other close-boiling chlorosilanes. The present invention is therefore directed to a method of separating crude chlorosilane streams containing close-boiling chlorosilanes such as dimethyldichlorosilane and methyltrichlorosilane which uses smaller distillation columns, and that requires less energy, thereby reducing the capital investment necessary in basic chlorosilane plants.
It is known in the art to use dinitrile compounds which form a separate extract phase that is enriched in difunctional chlorosilane, or dinitrile compounds are used with an additional non-polar wash solvent with low miscibility with the dinitriles, or dinitrile compounds are used as an extraction solvent. By contrast, the present invention does not involve formation of an extract phase with dinitriles, the use of dinitriles with an additional low miscibility non-polar wash solvents, nor does it utilize di-nitrile compounds as an extraction solvent. The present invention uses a mono-cyano-substituted organic compound, a nitro-substituted organic compound, a mono-cyano-substituted organosilicon compound, a nitro-substituted organosilicon compound, or a mixture thereof for separating crude chlorosilane streams containing mixtures of close-boiling chlorosilanes. Mono-cyano-substituted organic compounds are lower boiling materials with normal boiling points that are more than 100° C. lower than the corresponding dinitrile compounds. This distinction allows the separation steps to be conducted at correspondingly lower temperatures, thus avoiding the risk of decomposing the distillation aid in operation.
The invention relates to a method of separating crude chlorosilane streams of lower-boiling chlorosilanes and higher-boiling chlorosilanes. The method comprises contacting the crude chlorosilane stream with a distillation aid selected from the group consisting of mono-cyano-substituted organic compounds, nitro-substituted organic compounds, mono-cyano-substituted organosilicon compounds, nitro-substituted organosilicon compounds, and mixtures thereof. The lower-boiling chlorosilanes are recovered from the crude chlorosilane stream. The distillation aid is separated from the higher-boiling chlorosilanes.
The invention relates to a method of separating crude chlorosilane streams containing mixtures of chlorosilanes. The method comprises contacting the crude chlorosilane stream with a distillation aid, separating the lower-boiling chlorosilanes from the crude chlorosilane stream and separating the distillation aid from the higher-boiling chlorosilanes.
As used herein, crude chlorosilane streams means mixtures of lower-boiling chlorosilanes and higher-boiling chlorosilanes. In one embodiment, the crude chlorosilane stream contains close-boiling chlorosilanes. Representative examples of crude chlorosilane streams include those produced in the so-called direct process reaction of methyl chloride and silicon and mixtures of chlorosilane products utilized in the organosilicon industry. Another example of a crude chlorosilane stream is one containing methyltrichlorosilane and dimethyldichlorosilane. Still other examples of crude close-boiling chlorosilane streams which can be separated by the process of the invention include (i) crude streams containing dimethyldichlorosilane (b.p. ˜70.1° C.) and ethyldichlorosilane (74.6° C.) C2H5SiHCl2, (ii) crude streams containing phenyltrichlorosilane (201° C.) C6H5SiCl3 and phenylmethyldichlorosilane (205.6° C.) (CH3)(C6H5)SiCl2, and (iii) crude streams containing methylvinyldichlorosilane (92.3° C.) CH2═CH(CH3)SiCl2 and vinyltrichlorosilane (93° C.) CH2═CHSiCl3. As used herein, close-boiling chlorosilanes is intended to mean chlorosilanes which have boiling points within about 25° C. of each other at atmospheric pressure, alternatively within about 10° C. of each other at atmospheric pressure.
Compounds suitable for use herein as the distillation aid include mono-cyano-substituted organic compounds, nitro-substituted organic compounds, mono-cyano-substituted organosilicon compounds, nitro-substituted organosilicon compounds, or mixtures thereof. The distillation aid should be a liquid at the separation temperature and preferably at ambient temperature. Additionally, the distillation aid should generally have a boiling point higher than that of the chlorosilanes to be separated, and should generally not react with the chlorosilanes nor decompose at the maximum separation temperatures employed.
Some examples of mono-cyano-substituted organic compounds that can be used include acrylonitrile, benzonitrile, butyronitrile, caprylonitrile, propionitrile, 2-methyl-2-butenenitrile, 2-pentenenitrile, 4-pentenitrile, and cyanoacetate esters. Some preferred examples are caprylonitrile CH3(CH2)6CN and benzonitrile C6H5CN.
Some examples of mono-cyano-substituted organosilicon compounds that can be used include 3-cyanopropyldimethylchlorosilane N≡C—CH2CH2CH2Si(CH3)2Cl, 3-cyanopropylmethyldichlorosilane N≡C—CH2CH2CH2Si(CH3)Cl2, 3-cyanopropylphenyldichlorosilane N—C—CH2CH2CH2SiC6H5Cl2, 3-cyanopropyltrichlorosilane N≡C—CH2CH2CH2SiCl3, and 3-cyanoethyltrichlorosilane N≡C—CH2CH2SiCl3.
Some examples of nitro-substituted organic compounds that can be used include nitroethane C2H5NO2, and 1-nitropropane CH3CH2CH2NO2. A preferred example is 1-nitropropane.
Some examples of nitro-substituted organosilicon compounds that can be used include trichloro(nitropropyl)silane Cl3Si(CH2)3NO2, methyldichloro(nitropropyl)silane CH3Cl2Si(CH2)3NO2, ethyldichloro(nitropropyl)silane C2HSCl2Si(CH2)3NO2, and methyldichloro(nitroethyl)silane CH3Cl2Si(CH2)2NO2.
The distillation aid should generally be as dry as possible to minimize hydrolysis of the chlorosilanes. One method of removing residual water from the distillation aid is to dry the distillation aid over molecular sieves. To prevent the reintroduction of water, the dried distillation aid should not be exposed to water vapor.
It has been found that any concentration of distillation aid enhances the separation of close-boiling chlorosilanes by promoting, in the case of crude chlorosilane streams containing dimethyldichlorosilane (70.1° C.) and methyltrichlorosilane (66.1° C.), the removal of methyltrichlorosilane from the crude chlorosilane stream.
According to the method, the crude chlorosilane streams are contacted with a distillation aid, and the lower-boiling chlorosilanes are separated from the crude chlorosilane stream. The separation can be carried out in any suitable manner such as by mixing the crude chlorosilane stream and the distillation aid in a retort, and then heating the mixture to remove the lower-boiling chlorosilane. Alternatively, the vapors of the mixed chlorosilanes (crude chlorosilane) can be passed into the distillation aid which is maintained at a temperature above the boiling point of the lower-boiling chlorosilane.
In one method, the distillation aid is passed counter-currently to the vapors of the mixed silanes in a distillation column or tower. The temperature of the column or tower should be regulated so that liquid distillation aid flowing to the column or tower comes into contact with the vapors of the mixed chlorosilanes rising in the column or tower, and with the condensed vapors on each tray or stage in the column or tower below the distillation aid feed point.
After removal of the lower-boiling chlorosilane, the distillation aid and the higher-boiling chlorosilane can be separated in any suitable manner such as by gas-liquid chromatography, distillation, or flash distillation.
The method of the instant invention can be carried out at above atmospheric pressure, at atmospheric pressure, or at reduced pressure. It is preferred that the pressure should be sufficiently low so that the re-boiler temperature is not high enough to thermally decompose the distillation aid to a significant extent.
In large scale commercial operations, the distillation aid is employed in amounts which reduce the required distillation reflux ratio and corresponding energy requirements on the one hand, while minimizing the required distillation column size (contacting stages and column diameter) to reduce capital costs on the other hand. As is known in the art, this requires balancing capital equipment costs, energy costs and distillation aid costs, along with business expectations for return on investment. Examples of workable distillation aid concentrations are up to 50 weight % concentration of distillation aid in the chlorosilane mixture, or alternately 1% to 50 weight % concentration of distillation aid in the chlorosilane mixture, or alternately between 25% and 45 weight % concentration of distillation aid in the chlorosilane mixture.
The invention can be carried out in the presence of other silanes which may be present in the crude chlorosilane streams. For example, the presence of silicon tetrachloride SiCl4, trimethylchlorosilane (CH3)3SiCl, methyldichlorosilane CH3SiHCl, and dimethylchlorosilane (CH3)2SiHCl, do not inhibit the removal of the methyltrichlorosilane from a crude chlorosilane streams containing dimethyldichlorosilane and methyltrichlorosilane, produced by the direct reaction of silicon metal and methyl chloride. These other silanes will distill before, or along with methyltrichlorosilane.
The following examples are included to demonstrate embodiments of the invention. It should be appreciated by those of skill in the art that the techniques disclosed in the examples which follow represent techniques discovered by the inventor to function well in the practice of the invention, and thus can be considered to constitute preferred modes for its practice. However, those of skill in the art should, in light of the present disclosure, appreciate that many changes can be made in the specific embodiments which are disclosed and still obtain a like or similar result without departing from the spirit and scope of the invention. All percentages are in wt. %. In each example embodiment, a mono-cyano or nitro-functional distillation aid was utilized which did not form a separate extract phase, was miscible with the crude chlorosilane stream and which did not employ an additional non-polar solvent.
One gram of a 50/50 mole percent mixture of MeSiCl3 and Me2SiCl2, and one gram of the mono-cyano-functional compound or nitro-functional compound to be tested were weighed into a 20 mL headspace vial at room temperature, and allowed to equilibrate. The headspace and liquid phases were analyzed by a gas chromatograph equipped with a thermal conductivity detector (GC-TCD) to determine the relative volatility of the mixture according to the following equation:
α={[MeSiCl3]v[Me2SiCl2]l}÷{[MeSiCl3]l[Me2SiCl2]v}
where α is the relative volatility, Me is methyl and v and l are the measured mole percent concentrations of MeSiCl3 and Me2SiCl2 in the vapor and liquid phases, respectively. The relative volatility of a 50/50 mole percent mixture of MeSiCl3 and Me2SiCl2 was measured in the same way as a control for comparison. The results are shown in Table 1. Values for a which are greater than the control value show that the corresponding example compounds when contacted with crude chlorosilanes will enhance the recovery of the lower boiling chlorosilane (MeSiCl3 in this example) from the crude chlorosilane stream. Since the example compounds can be chosen with normal boiling points which are significantly different from the chlorosilane boiling points, separation of the distillation aid from the higher boiling chlorosilanes is easily accomplished, for example, through distillation.
Approximately 1.5 grams of a 10/90 mole percent mixture of MeSiCl3 and Me2SiCl2, were weighed into 20-mL headspace vials. Varying amounts of benzonitrile were added along with an amount of inert glass beads required to keep the total headspace volume in the vials constant. The vials were allowed to equilibrate at room temperature and the headspace and liquid phases were analyzed by a GC-TCD to determine the relative volatility of the mixture according to the equations given in example 1 above. The relative volatility of a 10/90 mole percent mixture of MeSiCl3 and Me2SiCl2 was measured in the same way as a control for comparison. The results are shown in Table 2 and show that increasing amounts of additive enhance relative volatility.
Relative volatilities for MeSiCl3/Me2SiCl2 were calculated from rigorous VLE data collected for mixtures of MeSiCl3/Me2SiCl2/Benzonitrile, where the Benzonitrile/Me2SiCl2 ratio was fixed at one, and the molar ratio of MeSiCl3/Me2SiCl2 was varied between 10:90 and 50:50. The relative volatilities for the ternary system were than compared to results obtained for the MeSiC13/Me2SiCl2 binary system. Graphical representation of the results is shown in
Aspen modeling was used to estimate the benefits associated with using benzonitrile as a distillation aid in the separation of MeSiCl3 from Me2SiCl2. This is one of many known computer programs that are capable of providing rigorous solutions to complex mathematical problems. VLE data for the ternary system in Example 2 was used to calculate Wilson binary interaction coefficients required for the modeling. The Wilson equation for prediction of multi-component vapor-liquid equilibria is a procedure known in the art. The binary interaction parameters, when combined with parameters reported in the literature, can be used to predict binary and multi-component vapor-liquid equilibrium data for multi-component systems. The benefits included capital cost savings, i.e., reduction in column size, shown in
It is apparent from
Table 3 shows that at the re-boiler duty, i.e., energy normally required to separate MeSiCl3 from Me2SiCl2, the addition of benzonitrile approximately doubled the throughput, i.e., distillate rate, of the column.
Other variations may be made in compounds, compositions, and methods described herein without departing from the essential features of the invention. The embodiments of the invention specifically illustrated herein are exemplary only and not intended as limitations on their scope except as defined in the appended claims.
| Filing Document | Filing Date | Country | Kind | 371c Date |
|---|---|---|---|---|
| PCT/US2006/046809 | 12/6/2006 | WO | 00 | 9/15/2008 |
| Number | Date | Country | |
|---|---|---|---|
| 60742690 | Dec 2005 | US |
