GB2090282A - Process and apparatus for the production of vinyltoluene - Google Patents

Abstract

A process for preparing vinyltoluene comprising passing ethyltoluene through a dehydrogenation zone to form vaporous crude vinyltoluene, adding from 50 to 100 parts per million by weight of a polymerization inhibitor such as a nitrated phenol to the vaporous crude vinyltoluene at a temperature of from 200 to 300 DEG C, condensing the vaporous crude vinyltoluene, maintaining the pH of the aqueous phase of the condensed crude vinyltoluene at a value from 5.5 to 6.5 sufficient to maintain the inhibitor in the organic phase of the condensed crude vinlyltoluene, adding a second portion of polymerization inhibitor to the condensed crude vinlyltoluene until the inhibitor concentration totals about 500 parts per million by weight relative to the vinyltoluene content of the crude vinyltoluene, filtering the condensed crude vinyltoluene to remove seed polymer, and distilling the condensed crude vinyltoluene to recover substantially pure vinyltoluene; and apparatus for carrying out said method. <IMAGE>

Description

SPECIFICATION Process and apparatus for the production of vinyltoluene The present invention pertains to a process and apparatus for the production of vinyltoluene, and more specifically to a method and means for inhibiting the formation of undesirable thermal polymers in the manufacture of vinyltoluene.

Vinyltoluene is commonly prepared by the catalytic dehydrogenation of ethyltoluene, cooling of the gaseous materials to condense the same and fractionally distilling the liquid product to obtain vinyltoluene. In the manufacture of vinyltoluene by the catalytic dehydrogenation of ethyltoluene, considerable difficulty has been experienced prior to and during the distillation of the crude vinyltoluene product to obtain purified vinyltoluene, because of the production of thermal polymers. This problem manifests itself in a plugging of the equipment used for the manufacture of the vinyltoluene.

In order to prevent the formation of the thermal polymer during distillation of vinyltoluene, various types of known polymerization inhibitors have been employed in connection with prior art distillation processes. These inhibitors have been only partially effective in preventing the formation of the undesirable thermal polymer in the distillation apparatus. However, since this normal addition of an inhibitor to the crude vinyltolueiie product takes place in or just prior to the distillation apparatus, the inhibitor does not prevent the formation of the undesirable thermal polymers in the equipment upstream of the distillation unit, such as in the condensers and in the crude vinyltoluene drum. The occurrence of fouling in the condensers and drum due to polymer formation represents a serious problem in the production of vinyltoluene.

It is an object of the present invention to provide an improved process for the production of vinyltoluene.

According to the present invention there is provided a process for the production of vinyltoluene comprising the steps of passing ethyltoluene through a dehydrogenation zone to form vaporous crude vinyltoluene; adding a first portion of polymerisation inhibitor to the vaporous crude vinyltoluene; condensing the vaporous crude vinyltoluene; maintaining the pH of the aqueous phase of the condensed crude vinyltoluene at a value sufficient to maintain the inhibitor in the organic phase of the condensed crude vinyltoluene; adding a second portion of polymerisation inhibitor to the condensed crude vinyltoluene; and distilling the condensed crude vinyltoluene under distillation conditions to recover pure vinyltoluene. The condensed crude vinyltoluene may advantageously be filtered before distillation to remove polymer which may otherwise serve as "seed" polymer in the distillation train.The polymerisation inhibitor may comprise a nitrated phenol, preferably dinitropara-cresol (hereinafter referred to as DNPC).

In accordance with a further aspect of the invention, the pH of the aqueous phase is adjusted to a level of from 5.5 to 6.5. Additionally, the process may further comprise the step of recycling the aqueous phase back to the dehydrogenation step.

In accordance with a still further aspect of the invention, the first portion of polymerisation inhibitor is added when the vaporous crude vinyltoluene temperature is from 2000C to 3000C. Also, the first portion of polymerisation inhibitor is advantageously added in amounts of 50 to 100 parts per million by weight relative to the vinyltoluene present, and the total of the first and second portions of the inhibitor added is preferably sufficient to bring the inhibitor concentration to a level of about 500 parts per million during the distillation step.

In accordance with still another aspect of the present invention, there is provided an apparatus for manufacturing vinyltoluene, comprising means for dehydrogenating ethyltoluene to form vaporous vinyltoluene; first means for introducing a polymerisation inhibitor into the vaporous vinyltoluene after the vaporous vinyltoluene leaves the dehydrogenation means; means for condensing the vaporous vinyltoluene; means for collecting the condensed vinyltoluene; a second means for introducing a polymerisation inhibitor into the collected vinyltoluene; and means for purifying the vinyltoluene, preferably a distillation apparatus. Additionally, a filter for filtering the vinyltoluene may be included prior to the purification thereof.

In the process according to the invention, a portion of the inhibitor is introduced directly into the stream of vaporous vinyltoluene as it leaves the dehydrogenation apparatus but immediately prior to its condensation. The pH required to maintain the inhibitor in the organic phase of the vinyltoluene feed stock will vary depending upon the pKa of the inhibitor selected. It has been found that the pH required for DNPC is less than about 6.5 and typically from 5.5 to 6.5. However if inhibitors other than DNPC are used during the processes, the pH required to maintain the inhibitor in the organic phase will depend on the acidic character of the inhibitor employed during the process. Any conventional filter may be utilised to filter the crude vinyltoluene feed stock prior to distillation.It has been found that a filter with passages of less than about 50 microns is the most efficient size in removing any undesirable thermal polymer.

The present method prevents the formation of soluble and insoluble (cross-linked) thermal polymers during the processing and subsequent distillation of vinyltoluene feed stock prepared by the catalytic dehydrogenation of ethyltoluene.

Thus, fouling of the crude vinyltoluene condensers and drums used prior to distillation with undesirable thermal polymers is prevented.

Furthermore the apparatus of the present invention is less prone to fouling with thermal polymers during the manufacture of vinyltoluene.

Through the use of the process according to the present invention, the amount of polymerisation occuring before and during the distillation of vinyltoluene is significantly reduced in comparison to conventionally employed methods. In addition, the amount of desired distillation product is increased in proportion to the decrease in the amount of polymer formation. Still further, since the inhibitor is maintained in the organic phase of the vinyltoluene, the water can be reused, e.g., in the generation of dilution steam for dehydrogenating ethyltoluene.

Vinyltoluene is typically manufactured by reacting toluene with ethylene in the presence of an activated Friedei-Crafts catalyst, such as aluminium chloride, or a zeolite catalyst, dehydrogenating the ethyltoluene by passing it together with steam through a dehydrogenation zone at a sufficient reaction temperature, and separating the dehydrogenated product by means of fractional distillation.

The present invention provides a process and apparatus for the production of vinyltoluene whereby the formation of the undesirable thermal polymer can be greatly inhibited or entirely prevanted prior to and during distillation of vinyltoluene feed stock prepared by the catalytic dehydrogenation of ethyltoluene. This is accomplished by adding an inhibitor immediately prior to the step of condensing the dehydrogenated vinyltoluene feed stock, adjusting the pH of the aqueous phase of the condensed feed stock to maintain the inhibitor substantially in the organic phase and optionally filtering the feed stock prior to fractional distillation.

Toluene is alkylated to form ethyltoluene by any suitable method known to those of skill in the art.

The ethyltoluenes formed are dehydrogenated by vaporising the hydrocarbons by means of heat exchangers, passing a stream of the vapour into admixture with steam to form a vapor mixture comprising from 1 to 10, advantageously from 2 to 3 parts by weight of steam per part of hydrocarbons, and passing the vapor mixture into a reactor containing a solid, granular dehydrogenation catalyst at a reaction temperature of from 5500 to 7000 C, preferably from 5600 to 6500 C. Any of the known catalysts which are suitable for use in dehydrogenating ethyltoluene may be used. A considerable number and variety of such catalysts are known and are commercially available. Catalysts of the self regenerative type are preferably used.

A vapor mixture containing steam and vinyltoluene then leaves the dehydrogenation reactor and passes through one or more heat exchangers. A polymerisation inhibitor is then injected into the vaporous mixture. Any of the inhibitors which are suitable for use in preventing the formation of undesirable thermal polymers in vinyltoluene and are soluble in the organic phase of the mixture may be utilised. Nitrated phenols are preferred, for example, dinitro-ortho-cresol, dinitro-para-cresol (DNPC), meta-nitro-paracresol, dinitro phenol, N-nitroso diphenyl amine, 4-halo-3,5-dinitro toluene, 3-nitro-2,5-cresotic acid and the like. The temperture of the vaporous mixture, at the time of the injection of the inhibitor, is preferably from 2000C to 3000C in order to prevent rapid decomposition of the inhibitor and to assure maximum effectiveness of the inhibitor.If DNPC is utilised as an inhibitor, it is preferably added to the vaporous stream of crude vinyltoluene in amounts of from 50 to 100 parts per million by weight relative to the vinyltoluene in the stream. The mixture is then cooled to condense the product, and the pH of the aqueous phase is adjusted, if necessary, to maintain the inhibitor in the organic phase. The pH needed to maintain the inhibitor in the organic phase will depend on the pKa of the inhibitor used. For instance, if DNPC is used as an inhibitor, a pH of 5.5-6.5 is sufficient to prevent the formation of the enolate anion, which is water soluble, and thus to maintain the DNPC substantially in the organic phass. Of course, if an inhibitor is selected which has a pKa different from that of DNPC, a different pH will be required to maintain the inhibitor in the organic phase of the vinyltoluene.The water collected may be recycled for use in future dehydrogenation reactions.

The dehydrogenation mixture may optionally and preferably be filtered to prevent transfer of any undesirable insoluble polymers into the distillation apparatus. Such polymers, unless removed, serve as seed polymers for the formation of large quantities of insoluble polymer in the distillation columns.

Additional polymerisation inhibitor is added to the crude vinyltoluene prior to entry into the distillation apparatus in order to prevent any undesirable polymer formation during distillation of the vinyltoluene. Typically, an amount of inhibitor is added which is sufficient to raise the total concentration of the inhibitor to a level of about 500 parts per million by weight relative to the vinyltoluene. This has been found to be sufficient to prevent the formation of undesirable insoluble polymers during the distillation process.

The dehydrogenation mixture is fractionally distilled in a series of fractionating columns. The distillation is preferably conducted under reduced pressure to further reduce the tendency of the vinyltoluene to polymerise. Lower boiling portions are separated from the vinyltoluene. The vinyltoluene is then removed from the heavier boiling fractions. Typical operating conditions for the distillation process include a temperature from 650C to 1 380C, and a subatmospheric pressure from 10 to 200 mm Hg absolute. The specific operating conditions produce a final product of commercial grade vinyltoluene which satisfies industry standards for quality and purity.

The present invention will now be described, by way of example only, with reference to the accompanying drawings, in which: Figure 1 is a schematic diagram of a preferred embodiment of the apparatus employed in practicing the present invention; and Figure 2 shows a schematic diagram of another apparatus which may be employed in practicing the invention.

Referring to the drawings, Figure 1 illustrates one embodiment for carrying out the process of the present invention. An ethyltoluene feed stock is introduced into a dehydrogenation apparatus 10 to form vinyltoluene. The vinyltoluene feed stock is injected with a polymerization inhibitor 12 immediately prior to condensing the vinyltoluene.

The vinyltotuene feed stock is condensed in a condenser 1 4, then transferred via line 1 6 to a crude vinyltoluene drum 18. The condenser 14 may comprise a condenser using a fan or water for cooling. Alternatively, any condenser suitable for condensing vaporous crude vinyltoluene may be utilized. The inhibitor 12 is preferably added as close to the quench nozzle of the condensing apparatus as possible in order to prevent decomposition of the inhibitor and to prevent the formation of undesirable polymers in the condenser 14 or the drum 1 8.The pH of the aqueous phase is adjusted to a pH which is sufficiently acidic to substantially maintain the inhibitor in the organic phase of the vinyltoluene feed stock A convenient means of controlling the pH of the aqueous phase in the crude drum comprises the following arrangement. Preferably, a partial stream of quench water is recycled from the crude drum to the condensing apparatus. A pH probe 1 9 is located in this recycle line, and downstream of the probe an inlet nozzle is provided for selectively injecting a pH control agent 20 when necessary. In order to maintain the aqueous phase slightly acidic, it is preferred to selectively add an inorganic mineral acid to the recycle stream, most preferably hydrochloric or sulfuric acid.

The aqueous phase of the feed stock is withdrawn from the crude vinyltoluene drum through line 21 and is recycled for water treatment end use in the boilers used in the dehydrogenation of ethyltoluene.

The product remaining in the vinyltoluene drum 18 is pumped through line 22 via pump 24 through filter 26 into a conventional vinyltoluene distillation train. Additional inhibitor 28 is injected into the vinyltoluene feed stock in line 30 in order to ensure the presence of a sufficient amount of inhibitor during the distillation process.

In this embodiment, the vinyltoluene feed stock is introduced into the intermediate portion of recycle column 32 which is preferably of the parallel distillation path design. Reboiler 34 provides the necessary heat for distillation in column 32.

An overhead product comprising toluene and ethyltoluene is withdrawn through line 35 for subsequent fractionation in distillation column 36.

In column 36, toluene and other light distillates are withdrawn through line 38. An ethyltoluene bottoms product is withdrawn through line 40 and is recycled for use in the ethyltoluene dehydrogenation reactor 1 0. Reboiler 42 provides the bottoms with the necessary heat for the distillation.

The recycle bottoms product, containing vinyltoluene inhibitor and polyvinyltoluene is withdrawn from the recycle column 32 through 44 using pump 46 and is charged into the middle portion of finishing column 48. A reboiler circuit comprising a reboiler 50 and an air feed line 52 is attached to the finishing column 48 for supplying the necessary heat and for establishing a counterflow of air within the column. The purified vinyltoluene (VT) overhead product is withdrawn through iine 54.

The finishing column bottoms product is directed to flash pot 56 via line 58 and pump 60.

The flash pot 56 has a reboiler 62 to facilitate the fractionation of the bottoms. The tar produced during the distillation process is withdrawn through line 64 by pump 66 for proper disposal.

Figure 2 illustrates the application of the process of the present invention to another distillation train for vinyltoluene. An ethyltoluene feed stock is introduced into a dehydrogenation apparatus 110 to form vinyltoluene. The vinyltoluene feed stock is injected with a polymerization inhibitor 11 2 prior to the condensation of the vinylto;uene as explained in connection with Figure 1. The vinyltoluene feed stock is then condensed in condenser 11 4, and the condensed vinyltoluene flows via line 11 6 to a crude vinyltoluene drum 118. The pH of the aqueous phase is regulated by means of pH probe 11 9 and acid 120 as explained in connection with Figure 1.The aqueous phase of the feed stock is withdrawn through line 1 21 and is recycled back to the dehydrogenation apparatus 110. The product remaining in the crude vinyltoluene drum 118 is pumped through line 122 via pump 124 through filter 126 into the vinyltoluene distillation train. Additional inhibitor 128 is added through line 122 into the vinyltoluene feed stock as explained in connection with Figure The vinyltoluene feed stock is introduced into the intermediate portion of column 130 through feed line 122. The co!umn 130 may be of any suitable design known to those skilled in the art and may contain any suitable number of vaporliquid contracting devices, such as a sufficient number of bubble cap trays, perforated trays, valve trays, etc., to separate lower boiling fractions from vinyltoluene.Alternatively, a packed column may be utilized to effect the separation. Column 1 30 is also equipped with a suitable reboiler 132 for supplying heat thereto.

Under the distillation conditions imposed in column 130, an overhead stream of low-boiliny hydrocarbons comprising mainly toluene is removed from column 130 via line 134. These low-boiling hydrocarbons are subsequently condensed and passed into storage for further use.

The bottoms product of the column 130 is then introduced into the recycle column 136 by means for line 138 and pump 140.

The recycle column 1 36 may be of any suitable design known to those skilled in the art. In one embodiment, the recycle column is of the parallel path design, i.e., two parallel distillation paths descending through the column. In this embodiment, it is necessary that the recycle column contain a sufficiently large number of trays to permit a proper separation between the similar boiling vinyltoluene and ethyltoluene.

Alternatively, the recycle column 136 may comprise a packed column. The recycle column 136 is equipped with a suitable reboiler 142.

The ethyltoluene overhead product of the recycle column 1 36 is withdrawn through line 144 and is subsequently condensed for reuse in the ethyltoluene dehydrogenation apparatus 110.

The recycle bottoms is withdrawn from the recycle column 136 through line 146. The recycle bottoms product is fed by pump 148 into finishing column 1 50 via line 146. The finishing column 1 50 is equipped with a reboiler 1 52. Inhibitor protection is adequately provided in this column and the recycle column 136 because of the prior additional of the polymerization inhibitor.

The purified vinyltoluene overhead product is withdrawn through line 1 54 from the finishing column. The purified vinyltoluene product will comprise commercial quality vinyltoluene. The finishing column bottoms product is withdrawn through line 1 56 via pump 1 58 into flash pot 160.

The flash pot 1 60 has a reboiler 162 to facilitate the fractionation of the bottoms. The tar produced during the distillation process is withdrawn through line 164 by pump 166 for proper disposal.

However, recycling these inhibitor-bearing tars into the recycle column is also contemplated as an optional step.

The use of the process of the present invention enables an apparatus for the production of vinyltoluene to operate at an increased rate and significantly reduces the amount of unwanted thermal polymerization normally occurring during the production of vinyltoluene.

The invention will now be further illustrated by the following non-limiting Examples.

EXAMPLE I Following several vinyltoluene production runs during which insoluble popcorn-type polymer accumulated regularly (i.e., every 1 to 3 weeks) in the primary condenser system and the crude vinyltoluene drum, a mechanism for injecting a solution of DNPC just upstream of the quench nozzle was installed. It was found that 100 ppm DNPC relative to the vinyltoluene present was effective in controlling the fouling problem caused by polymer accumulation. Utilizing the DNPC injection just prior to the quench nozzle, as described, the system has operated more than sixty days without the occurrence of significant fouling.

EXAMPLE II Because of the ability of even vary small amounts of popcorn (insoluble) polymer to serve as seed for accumulations of additional insoluble polymer, a filter system was installed between the crude vinyltoluene drum and the distillation train of the system of Example I to prvent the forward transfer of solids. The filter system has been found to successfully accumulate the limited amounts of popcorn which remain notwithstanding the injection of the inhibitor just prior to the quench nozzle. As a consequence, the transfer of seed polymer into the distillation train has been precluded, resulting in a significant decrease in the rate of accumulation of insoluble polymer therein.

Claims (14)

1. A process for the preparation of vinyltoluene, comprising the steps of passing ethyltoluene through a dehydrogenation zone to form vaporous crude vinyltoluene; adding a first portion of polymerisation inhibitor to said vaporous crude vinyltoluene; condensing said vaporous crude vinyltoluene; maintaining the pH of the aqueous phase of said condensed crude vinyltoluene to a value sufficient to maintain said inhibitor in the organic phase of said condensed crude vinyltoluene; adding a second portion of polymerisation inhibitor to said condensed crude vinyltoluene; and distilling said condensed crude vinyltoluene under distillation conditions to recover pure vinyltoluene.

2. A process according to Claim 1, further comprising the step of filtering said condensed crude vinyltoluene before distillation thereof.

3. A process according to Claim 1 or 2, wherein the polymerisation inhibitor comprises a nitrated phenol.

4. A process according to Claim 3, wherein the polymerisation inhibitor comprises dinitro-paracresol.

5. A process according to any one of the preceding claims, wherein the pH of the aqueous phase is adjusted to a level of from 5.5 to 6.5.

6. A process according to any one of the preceding claims, further comprising the step of recycling the aqueous phase back to the dehydrogenation step.

7. A process according to any one of the preceding claims, wherein the first portion of polymerisation inhibitor is added when the vaporous crude vinyltoluene temperature is at from 2000C to 3000 C.

8. A process according to any one of the preceding claims, wherein the first portion of polymerisation inhibitor is added in an amount of from 50 to 1 OQ parts per million by weight relative to the vinyltoluene content of said crude vinyltoluene.

9. A process according to any one of the preceding claims, wherein the first portion of polymerisation inhibitor and the second portion of polymerisation inhibitor total about 500 parts per million by weight relative to the vinyltoluene content of said crude vinyltoluene.

10. A process according to Claim 1 substantially as hereinbefore described with reference to the accompanying drawings.

11. A process according to Claim 1 substantially as hereinbefore described in Example lorll.

1 2. Vinyltoluene when prepared by a process as claimed in any one of the preceding claims.

13. An apparatus for manufacturing vinyltoluene comprising means for dehydrogenating ethyltoluene to form vaporous vinyltoluene; first means for introducing a polymerisation inhibitor into said vaporous vinyltoluene after said vaporous vinyltoluene leaves said dehydrogenation means; means for condensing said vaporous vinyltoluene to produce an aqueous crude vinyltoluene feed stock; means for adjusting the pH of the aqueous phase of the condensed crude vinyltoluene feed stock; means for collecting said condensed crude vinyltoluene feed stock; a second means for introducing a polymerisation inhibitor into said collected crude vinyltoluene feed stock; and means for purifying said vinyltoluene.

14. An apparatus according to Claim 13, further comprising means for filtering the vinyltoluene prior to the purification thereof.

1 5. An apparatus according to Claim 13 or 14, wherein the purifying means is a distillation apparatus.

1 6. An apparatus according to Claim 13 substantially as hereinbefore described with reference to the accompanying drawings.