CONVERSION OF PROPANE TO ACRYLIC ACID

Abstract: Propane is converted to acrylic acid in an integrated three-stage process. Propane is dehydrogenated in a first stage to propylene, hydrogen, and by-products. The reaction effluent is passed into a second stage where propylene is oxidized to acrolein without significant oxidation of the hydrogen and by-products. The effluent from the second stage may be passed as feed to a third stage for the oxidation of acrolein to acrylic acid. The acrylic acid is recovered as the primary product, while the unconverted propane may be separated and recycled to the first stage for dehydrogena­ tion.

Description: Conversion of Propane to Acrylic Acid The invention relates generally to the preparation of acrylic acid. More specifically the invention relates to the preparation of acrylic acid in a threestage process from propane. In typical processes of the prior art propylene is reacted in the vapor phase with molecular oxygen over a catalyst to produce acrolein. The reactor effluent containing acrolein is then passed to a second oxidation step where it is -reacted with molecular oxygen in the vapor phase over a different catalyst to form acrylic acid. Generally, the feed for this process has been the unsaturated olef in. Any saturated hydrocarbon present was considered to-be essentially an inert since little, if any, oxidation occurred. Known dehydrogenation processes could be used to prepare propylene from propane as a feedstock for the known methods of preparing acrylic acid. However, if propylene must be purified before oxidation, then this would be an uneconomic way of preparing acrolein and acrylic acid. Integrated processes are not generally used because the by-products of dehydrogenation cannot be present in the subsequent use of propylene, without causing contamination of the ultimate end product. The present process relates to an integrated process in which the dehydrogenation of propane is combined with the oxidation of the resulting propylene to acrylic acid without intermediate separation and purification of the propylene before the oxidation is carried out. In British Patent 1,340,891 propane and oxygen are reacted to prepare propylene, acrolein, and acrylic acid over a variety of base metal oxide catalysts, Since the conversion of propane is quite low, high concentrations of propane are used so that the net amount of propylene produced is sufficient to result in a practical process. U.S, Patent 4,260,822 also discloses a process for direct oxidation of propane to acrylic acid in a single step, again using large amounts of propane in order to overcome the relatively low conversion of propane to the product. The above one-step processes are not economic, since the conversions are quite low and require recycling of substantial amounts of unreacted feed in order to convert a high proportion of the propane fed. Also, the catalysts typically do not have the long useful life necessary for satisfactory commercial operations. A number of processes have been developed for converting propane-to propylene. In U.S. Patent 3,784,483 a cobalt, iron, and phosphorus catalyst is disclosed as useful for the oxidative dehydrogenation of propane to propylene. In a group¯of patents exemplified by U.S. 4,083,883 a precious metal combined with promoter metals on a support is used for- the dehydrogenation of paraffins, particularly normal paraffins. Another approach is taken in U.S. Patents 3,692,701, 4,005,985 and 4,041,099. In these processes large quantities of steam are used to dehydrogenate propane over a catalyst of platinum-tin on zinc aluminate. Dehydrogenation of propane is shown over zinc titanate catalysts in U.S. 4,144,277 and 4,176,140. Many patents have disclosed processes for oxida tin . of propylene to acrylic acid, such as EP 0000663 and U.S. 3,954,855. These processes are generally carried out in two steps in order to obtain the best yields of acrylic acid. In the first step propylene is oxidized to acrolein in the vapor-phase over a promoted molybdenum catalyst and the effluent from the reaction is passed with added oxygen over a second promoted molybdenum catalyst to produce acrylic acid. Based on the prior art discussed above, one might assemble a multi-step process wherein propane is dehydrogenated with or without the presence of oxygen to produce propylene, which would be separated and purified and fed to a conventional acrylic acid process. In this way, substantially all of the propane fed is converted to acrylic acid by merely combining known processes. Bow- ever, this may not be an economic way to produce acrylic acid. As will be seen, the present invention pertains to an integrated process by which propane may be converted to acrylic acid without first purifying an intermediate propylene product. Dehydrogenation of propane produces substantial amounts of hydrogen and small amounts of lower molecular weight hydrocarbons, which in the prior art processes would be removed from the product, but which in an integrated process must be accommodated in the oxidation of propylene to acrolein. The hydrogen and by-products should not have an adverse effect on the oxidation catalysts or their performance. For example, the exposure of the by-products to oxidizing conditions cannot produce contaminants which reduce the quality of the acrylic acid. Also, the presence of hydrogen should not create an explosive mixture in the oxidation reactors. Summary of the Invention Acrylic acid is prepared from propane in an integrated process in which dehydrogenation of propane to propylene in a first stage is followed immediately, that is, without separation and purification of the propylene from the dehydrogenation effluent, by addition of oxygen and oxidation of the propylene to acrolein in a second stage. Alternatively, the dehydrogenation effluent may be cooled and water condensed and separated before the effluent stream enters the oxidation stage. The oxidation stage may be followed by immediate oxidation of the acrolein in the second stage effluent to acrylic acid in a third stage. Alternatively, the acrolein may be recovered or concentrated in the second stage effluent before being fed to the third stage for oxidation. The acrylic acid product is recovered by scrubbing or quenching the third stage effluent which also contains unreacted propane, propylene, and oxygen, plus hydrogen, carbon oxides and miscellaneous light and heavy hydrocarbon by-products of the dehydrogenation and oxida tiort-reactions. -Acryli-c-acid may be absorbed in water to separate it from the lighter by-products and unreacted feed components. Thereafter, at least unreacted propane is recycled. Residual gases depleted in acrylic acid may be scrubbed to recover propane and propylene, which are recycled to the first stage for dehydrogenation. Alternatively, a selective oxidation may be employed to remove oxygen from the residual gases and carbon dioxide removed by scrubbing with a suitable solvent. The dehydrogenation of propane to propylene is carried out by a vapor-phase reaction over a suitable catalyst, which may be platinum with or without a promoter on a zinc aluminate support or other suitable noble and base metal catalysts. When the catalyst is platinum, with or without a promoter, on zinc aluminate the dehydrogenation will be carried -out at about 400 to 700"C and up to about 10 kg/cm2 gauge pressure, with a propane to steam ratio of about 1/0.5 to 1/10. The oxidation of propylene to acrolein and of acrolein to acrylic acid may be carried out over suitable catalysts, such as mixed base metal oxides, especially molybdenum oxide-based catalysts. Description of the Drawings , Figure 1 is a block diagram showing the process of the invention. Figure 2 is a simplified flowsheet showing one embodiment of the invention. Figure 3 is a simplified flowsheet showing an alternative embodiment of the invention. Description of the Preferred Embodiments In the principal aspect, the invention is an integrated process combining the dehydrogenation of propane to propylene with the oxidation of the propylene to acrylic acid in two steps. The product acrylic acid is separated from the by-products and the unreacted propane may be recovered and recycled to the dehydrogenation step if desired. A schematic view of such a complete process is shown in Figure 1. The process contrasts with those of the prior art particularly in that the effluent from the dehydrogenation reaction 10 may be fed directly to the oxidation reaction 12 for conversion of propylene to acrolein. One familiar with the prior art would expect that propylene would be separated from the effluent of the dehydrogenation step 10 before feeding it to the oxidation step 12. Since the dehydrogenation of propane involves the production of significant quantities of hydrogen, as well as small amounts of lower molecular weight hydrocarbons, the propylene must be oxidized in the presence of significant quantities of hydrogen, propane, and by-products, without markedly affecting the oxidation of propylene to acrolein or causing oxidation of the hydrogen. We have found that propylene may be oxidized to met'gacrolein in the presence of hydrogen, propane, and by-products of the dehydrogenation step, while not adversely affecting the oxidation process. After the propylene has been oxidized to acrolein, the entire effluent from the first oxidation step 12 may be sent directly to the second oxidation step 14 where the acrolein-is oxidized to acrylic acid. Thereafter, the effluent of oxidation step 14 is. partially condensed and separated at 16. Purified acrylic acid is the product while the lower-boiling components are separated at 18. Waste gases and heavy by-products are discharged while unreacted propane is recycled to step 10. Alternatively, oxygen and carbon oxides may be removed selectively and the remaining gases recycled. Although acrolein will normally be converted to acrylic acid and by-products, if the conversion is kept at a lower level so that a significant amount of acrolein remains, then acrolein optionally may be recovered and recycled to the oxidation stage 14 as shown. In another aspect, the effluent from the first oxidation step 12 may be separated to concentrate the acrolein, which is then fed, along with air or oxygen to the second oxidation step 14. Recovery may be made by absorption -in suitable liquids, such as water and the lower carboxylic acids. Unreacted propane will be returned to the dehydrogenation step 10 as shown. Example 1 Dehydrogenation of - Propane A catalyst composed of 0.4 wt % Pt and 1 wt % In on a zinc aluminate support was prepared. A catalyst sample of 50 cc as 3 mm extrudate was charged to a tubular reactor having a 25.4 mm i.d. An additional 250 ce of the zinc aluminate support was added to the reactor above the catalyst bed. A gas stream containing 1 mol of propane for each 2 mols of steam was fed to the reactor at a gas hourly space velocity of 4000 hr1 under a pressure of 3.5 kgZcm2 gauge. The inlet to the catalyst bed was held at a predetermined temperature, with the outlet temperature reflecting the endothermic nature of the dehydrogenation reaction. The results are given below in Table A. Table A Inlet Conversion Selectivity to Test Temp.'C. of Propane,% Propylene,% 1 548 23.6 95.8 2 523 29.7 96.5 The dehydrogenation of propane produces one mol of hydrogen for each mol of propylene and additional hydrogen from the formation of some lower molecular weight by-products. When propylene is not separated before subsequent oxidation the hydrogen and other by-products are carried into the subsequent oxidation reaction. Oxidation of the by-products to compounds which contaminate acrolein must be avoided. Oxidizing the hydrogen along with.propylene would be undesirable since it would consume oxygen and interfere with the oxidation of propylene. Also, oxidation of hydrogen would generate undesirable heat and could create hot-spots in the catalyst and lower the production of acrolein. However, it has been found that oxidation of propylene can be carried out in the presence of hydrogen with substantially no consumption of hydrogen, as will be seen in the following example. The presence of propane which has not been dehydrogenated also appears to have no significant effect on the oxidation of propylene. Example 2 Oxidation of Propylene to Acrolein A catalyst was prepared according to the method described in EP 0000663 and corresponding to Reference Catalyst A and having composition of 80% K0.lNi2.5Co4.5Fe3BtIPO.5Mo12Oxand 20% SiO2. A charge of 220 cc of catalyst as 4.7 mm pellets was placed in a single-tube reactor having an i.d. of 12.7 mm. A feed gas containing 5 vol% propylene, 20 vol % steam and 12% oxygen was passed at a volume hourly space velocity of 1000-1200 hr-l over the catalyst. The pressure in the catalyst was about 1.76 kg/cm2 gauge. Analysis by gas chromatography of the effluent gases gave the results designated in Tests 3-6 of Table A. Table A Test Time, Temp. Conversion of Selectivity to Acrolein No. hrs. 'C Propylene, % and Acrylic Acid, * 3 78.0 310 91.1 87.4 4 81.0 310 90.6 86.3 5 93.5 310 90.5 87.7 6 99.5 310 90.1 89.7 7 102 310 94.2 86.6 8 115 309-- 92.6 88.7 9 124 309 92.5 87.9 10 139 309 89.3 87.2 11 147 309 91.4 85.6 12 156 310 93.7 86.7 13 180 309 92.9 86.9 After the performance of the catalyst had been established with only propylene feed, hydrogen was added to the feed gas to simulate in part the conditions which would pertain to the oxidation reaction when supplied with propylene produced by dehydrogenation of propane. An additional 4 vol % of hydrogen was included with the mixture previously fed. The results are shown as Tests 7-10 in Table A. it-will be seen that substantially the same results were achieved as in Tests 3-6. It was concluded that essentially no hydrogen was being oxidized, judging from the operating conditions in the reactor. The hydrogen was discontinued and the oxidation reaction continued with 4 vol * propane added. The results are shown as tests 11-13 in Table A. Again substantially the same results were obtained as in Tests 3-6, indicating that propane was not affecting the oxidation of propylene and was not itself being oxidized. These results show that propylene can be oxidized in the presence of hydrogen and propane, the two principal components of the dehydrogenation of propane to propylene. It may be concluded that the integration of the denydrogenation and oxidation reactions is feasible. Example 3 Oxidation of Acrolein to Acrylic Acid To illustrate the oxidation of acrolein to acrylic acid and the effect of hydrogen and propane additions to the feed gas, experiments were carried out which parallel those of Example 2. A catalyst was prepared corresponding to the composition of Example 1 of U.S. 3,954,855 and according to the procedure described there. The catalyst composition was Mo12V4.8SrO.5W2.4Cu2.2Ox. A 73 cc sample of the catalyst as 4.7 mm pellets was placed in a tubular reactor having 12.7 mm i.d. The reactor was surrounded by a bath thermostatically providing a uniform predetermined temperature. The feed to the reactor was initially 6-8 vol % acrolein, 51 vol % air, and 45 vol % steam. The volumetric space velocity was 3000 hr'l and the average reactor pressure slightly above atmospheric. The results are shown in Table B. Table B Test Time, Temp. Conversion of Selectivity to No. hrs. 'C Acrolein, % Acrylic Acid, % 14 126 254 92.8 89.1 15 126 251 84.5 89.2 16 41 252 86.8 88.4 17 36 251 80.7 87 As was done in Example 2, first 4 vol * hydrogen was added and then the hydrogen was replaced with propane. The results are shown in Table B as Test 16 (H2) and 17 (propane). Although some difference in the conversion of acrolein appears, it is clear from Tests 14 and 15 that conversion is very sensitive to temperature and the differences among Tests 15, 16, and 17 are not considered significant. The selectivity to acrylic acid is substantially the same. Again, it may be concluded that an integrated process is feasible. Separation of acrylic acid (16) may be done by methods known to the prior art. See for example, U.S. 3,926,744. The acrylic acid reactor effluent may be quenched with water or a high-boiling point solvent. Acrylic acid can be removed from the aqueous solution by solvent extraction with a suitable liquid, e.g. ethyl acetate. The resulting acrylic acid-solvent solutions may be separated and purified by distillation to produce acrylic acid. In its broadest form, the invention includes the integration of dehydrogenation and two oxidation stages whereby the propane is converted to acrylic acid, after which-unreacted propane is recycled. Such a combination process without an intermediate separation of propylene has been shown to be possible. If the resulting by-product stream containing significant quantities of propylene and propane can be used for other purposes, then recycling of the gas is not required. In many cases, it will be desirable to recycle unreacted propylene and propane so that the integrated process substantially converts propane to acrylic acid with only minor amounts of by-products and without ever producing a substantially pure propylene stream. In order to recycle gas containing large amounts of propane, it will be necessary to remove hydrogen produced in the dehydrogenation step, excess oxygen from the oxidation step, and carbon oxides formed in all three steps. In addition, a purge of light and heavy by-products and feed impurities will be taken. Removal of carbon dioxide typically would be done by scrubbing all or a portion of the recycle stream with a carbonate or amine solution as is known in the art in order to maintain the desired level of carbon dioxide. Carbon monoxide will be converted to carbon dioxide in the dehydrogenation reactor. Since the presence of these materials is not critical to either the dehydrogenation or oxidation steps, they may be economically permitted to build up in the recycle stream to a level in which they may be conveniently and economically removed. Since the light and heavy hydrocarbon by-products, such as methane,.. ethane, ethylene, butane, and butenes boil at temperatures significantly different from those of acrolein or. the C3 hydrocarbons, they may be separated by distillation. Alternatively, streams containing the by-products in concentrated amounts may be purged. Separation of the hydrogen formed by the dehydrogenation of propane might be done by various methods such as catalytic oxidation, liquid phase absorption or gas phase adsorption. Fiaure 2 is a simplified flowsheet showing a preferred embodiment of-the invention with a complete process whereby propane is converted substantially to acrylic acid. Fresh propane feed 20 is combined with recycle stream 24 containing principally propane and vaporized in exchanger 22. The combined stream 26 is then heated in exchanger 28 to a temperature such that when combined with the required amount of steam (30) the temperature obtained wilL be that suited for the dehydrogenation of propane to propylene. The amount of steam used preferably is suitable for the subsequent oxidation of the propylene to acrolein. As shown here, steam is supplied as a fresh feed stream. If this is done, then water produced in the reactions is eventually purged from the system from the bottom of the stripper 56. A feed stream containing propane and steam in molar ratios between 1/0.5 and 1/10, preferably 1/1 to 1/5, is fed at temperatures between about 400-700iC, particularly about 600so, and at pressures up to about 0-10 kg/cm2 gauge, preferably near 0 kg/cm2 gauge, to reactor 32 where about 50% of the propane is converted to propylene, witha selectivity of 75% or more. A number of catalysts have been disclosed in the prior art for use in this process and the conditions under which the reaction is carried out will depend on the catalyst selected. Of particular usefulness is a platinum-based catalyst of the type shown in U.S. 4,005,985. Although platinum and tin disposed on a zinc aluminate support provides good performance, other catalysts which have been found effective include platinum and other promoters, such as rhenium and indium supported on zinc aluminate. Other Group VIII noble metals, alone or in combination on various supports known to the art may have application in the dehydrogenation of propane to propylene. Other potential supports would include alumina, other alkaline earth metal aluminates, and rare earth aluminates including lanthanum. Promoters such as tin, lead, antimony, and thallium may be used. Base metal catalysts such as the chromium, zirconium, titanium, magnesium and vanadium oxides as shown in U.S. 3,479,416 and 3,784,483 or the zinc titanate of U.S. 4,176,140 and 4,144,277 also might be used. The invention is not considered to be limited to specific catalyst formulations. It will be understood by those skilled in the art that in this process the catalyst rapidly deactivates and must be regenerated frequently. Typically, the process will be operated with multiple reactors so that frequent regeneration is possible. The details of such operations are, however, not considered part of the invention. The dehydrogenation reaction is endothermic and the temperature leaving the reactor 32 will be on;the order of 50-200µC lower than the inlet temperature. This will be affected by the amount of steam employed, the condition of the catalyst, and the severity of the reaction conditions chosen. -The dehydrogenation reactor effluent is cooled in exchanger 34 to a suitable temperature for inlet to the oxidation reactor 38 and joined with an oxygen-containing stream 36 to provide a suitable feed for the oxidation of propylene to acrolein. Air enriched in oxygen or air alone might be used, if economic to do so. Although not shown in this flowsheet, it is also possible to cool the effluent from reactor 32 until water is condensed from the gases. Removal of the water would permit adjustment of the steam to propylene ratio used in oxidation reactor 38. The reaction would be carried out under conditions typical of the art, that is, temperatures in the range of about 200-600"C, usually about 300-3500C, pressures of about 0-5 kg/cm2 gauge, and gas hourly space velocities on the order of 2000 hrs¯1. A suitable oxidation catalyst will be used, typically a mixture of base metal oxides, especially those which are molybdenum-based. The reactor typically will be of the tubular type where the pelleted catalyst is placed inside tubes which are surrounded by a heat transfer fluid for the removal of the heat of reaction. Typically, 90-95% of the propylene feed to the reactor will be converted to acrolein, along with minor amounts of acrylic acid, acetic acid, and less significant quantities of lighter and heavier by-products. Some of the propylene is burned to carbon oxides and water. The effluent from reactor 38 is fed with or without intermediate heat exchange and adjustment of the gas composition to reactor 40, where the acrolein is converted to acrylic acid. The reaction would be carried out under conditions typical of the art, that is, temperatures in the range of about 200-600"C,. usually about 250 3000C, pressures of about 0-5 kg/cm2 gauge, and gas hourly space velocities on the order of 2000 hrs¯1. A suitable oxidation catalyst will be used, typically a mixture of base metal oxides, especially those which are molybdenum-based. The reactor configuration will be similar tQ--that of reactor 38. Typically 90-98% of the acrolein fed to the reactor 40 will be converted to acrylic acid, and minor amounts of acetic acid, carbon oxides, and other by-products. Overall, the selectivity of propylene to acrylic acid would be about 75-808. The resulting gaseous mixture may be cooled and fed to an quench. tower 42 where an acrylic acid-water mixture is condensed in a recirculating aqueous stream 44 at temperatures in the range of about 30-50"C. Substantially all of the acrylic acid is recovered in a solution containing up to about 35 mol % acrylic acid. This solution is sent to an extraction column 46 where the acrylic acid is selectively extracted by a recirculating stream of a suitable solvent, such as ethyl acetate. The solvent rich with acrylic acid is passed to a stripper 48 to recover the solvent for recycle via line 50. Acrylic acid is passed via line 51 to two additional columns 52 and 54 for separation of the lighter and heavier impurities. Water produced in the process is removed from the bottom of column 46 via stream 47 and sent to stripper 56 for removal of hydrocarbons and then disposed of or recirculated as steam to the dehydrogenation step. The light gases leaving the top of the quench tower 42 contain large quantities of propane along with lesser amounts of propylene, carbon oxides, hydrogen, oxygen, nitrogen, and light impurities. These gases are passed to absorber 58 for recovery of the C3 content if they are to be returned for further conversion to acrylic acid. Suitable solvents which may be employed include paraffin or aromatic hydrocarbons. Light gases are vented from the process from the top of tower 58. The solvent rich in C3 's is passed to column 60 where they are stripped out and returned to reactor 20 via line 24. In an alternative embodiment, the gases from absorber 42 could be passed to a reactor where the oxygen content is consumed by reaction with the hydrogen present. This selective oxidation may be carried out over suitable catalysts, such as platinum on alumina, which can carry out the oxidation at a sufficiently low temperature that the valuable C3 hydrocarbons are not oxidized and lost. Once the oxygen has been consumed the gas may be returned to the dehydrogenation reactor, preferably after a slip stream having been scrubbed to remove the carbon dioxide produced by the oxidation steps and to separate C31s from light by-products, which are purged. An example of the practical operation of the flow sheet shown in Figure 2 is as follows: Example 4 One hundred mols/hr of a feed stream 20 containing 99% propane is vaporized in exchanger 22 and fed to the dehydrogenation reactor 32, along with 240 mols/hr of a recycle propane stream 24. The combined streams 26 are heated to about 675it (28) and mixed with 560 mol/hr of steam (30) which may be provided by recycling and vaporizing stream 49 from the stripper 56. The combined stream 29 is fed to the dehydrogenation reactor 32, where about 29% of the propane fed is converted with 80% selectivity to propylene over a promoted platinum catalyst. Leaving the reactor 32 at about 630iC, the effluent stream is cooled to about 1250C in exchanger 34 and mixed with 152 mol/hr of oxygen (36) before being supplied to the oxidation reactor 38, where about 93% of the propylene is converted with 88% selectivity to acrolein over a promoted molybdenum catalyst. Leaving the reactor 38 at about 325"C and 1.4 kg/cm2 gauge the effluent gases are passed to the second oxidation reactor 40 for conversion of acrolein to acrylic acid. Leaving the reactor (40) at about 270'C and 1.0 kg/cm2 gauge the effluent steam is cooled to about 1400C and enters quench tower 42 where water, acrolein, and acrylic acid are condensed and absorbed in a recirculating stream 44, cooled to about 35-C in exchanger 43. The crude recycle gas leaving the top of the absorber 42 is passed to absorber 58 where it is contacted with a recirculating stream of 250 mol/hr containing C8 paraffins to recover substantially all of the C3 content. The waste gases, i.e. 250 mol/hr of hydrogen, oxygen, nitrogen, and light by-products, are vented from the top of column 58. The enriched liquid is stripped in column 60 and 240 mol/hr of propane is recovered and recycled via line 24 to dehydrogenation reactor 32. An aqueous. stream of 550 mol/hr containing 12 mol % acrylic acid, along with acrolein and miscellaneous by-products such as acetic acid, maleic acid, formic acidr and other oxygenated compounds is passed to extractor 46 where it passes countercurrently versus 190 mol/hr lean solvent (ethyl acetate) entering the base of the tower via line 50. Substantially all of the acrylic acid is absorbed. Water raffinate is withdrawn from the bottom of column 46 and passed via line 47 to column 56 where light by-products are distilled overhead and withdrawn as a waste stream. Stripped water is withdrawn (49) from the bottom of the column for reuse or disposal. The enriched solvent passes overhead from column 46 and is distilled in column 48 to separate the solvent which is recovered overhead and recirculated to column 46 via line 50. The crude acrylic acid leaves the bottom of column 48 and is sent to column 52 via line 51. The crude acrylic acid stream of 70 mol/hr comprises 90 mol % acrylic acid, with the remainder.acetic acid, ethyl acetate and heavy by-products. Light impurities and any residual water are distilled overhead and passed via line 53 to column 56. Partially purified acrylic acid is sent to column 54 via line 55 where it is distilled away from the heavy by-products and withdrawn as a sidestream. High boiling waste materials such as maleic acid are withdrawn from the bottom of column 54 for disposal. Any residual light materials are sent to column 56. Figure 3 is a simplified flow sheet showing an alternative embodiment of the invention where acrolein is recovered -and purified from the effluent of reactor 38 before being oxidized to acrylic acid in reactor 40. The previous discussion of the dehydrogenation and first oxidation steps is still pertinent. In this embodiment, the effluent from reactor 38 is cooled and then led to a quench tower 39A where acrolein is scrubbed from the gases by a recirculating aqueous stream. Gases which are not absorbed may be purged or preferably, the C3 content of the gases is separated by absorption or the like and returned to reactor 32 via line 24. After being absorbed in tower 39A, the enriched absorbent is stripped in tower 39B to provide stream rich in acrolein to the second oxidation reactor 40 via line 39C. Air or oxygen is added and the oxidation to acrylic acid is carried out as previously described. Recovery of the acrylic acid from the reactor effluent proceeds as in Figure 2, as does the purification of acrylic acid. An example of the operation of the process shown in Figure 3 is as follows: Example 5 -One hundred molsXhr-of a feed stream. 20 containing 99% propane is dehydrogenated to propylene and then oxidized to acrolein under the conditions of Example 4 except that upon leaving reactor 38 the effluent is cooled to 1200C and fed to absorber 39A, where the acrolein is scrubbed out by countercurrent contact with water. The rich absorbent is stripped in column 39B by vapor supplied by the reboiler. The light gases are returned to the dehydrogenation reactor 32 while 64 nol/hr of acrolein, along with minor amounts of by-products are sent via line 39C to the second oxidation reactor 40. The remainder of the flow sheet is substantially the same as that shown in Figure 2. Although in its principal aspects the invention is directed to the preparation of acrylic acid from propane, it should be understood that acrolein can be recovered from the effluent of the first oxidation reactor, as shown in Figure 3 for example, and used as a product of the process where acrolein is needed for various end uses, such as preparation of allyl alcohol.

Claims: CLAIMS 1. A process for the preparation of acrylic acid from propane comprising: (a) in a first stage dehydrogenating propane to propylene, optionally in the presence of steam, over a dehydrogenation catalyst to form an effluent stream comprising propylene, hydrogen, carbon oxides and unreacted propane; (b) in a second stage mixing oxygen and optionally steam with- sa-id effluent stream of (a) and passing the mixture over a first oxidation catalyst at conditions selected to produce a second effluent stream comprising acrolein, unreacted propylene and propane, and oxygen, hydrogen and carbon oxides; ; (c) in a third stage passing the effluent stream of (b) optionally with additional oxygen over a second oxidation catalyst at conditions selected to produce a third effluent stream comprising acrylic acid, unreacted propylene, propane and acrolein, and oxygen, hydrogen, and 'carbon oxides; (d) recovering the acrylic acid from said effluent of (c) to produce an acrylic acid-depleted effluent; and (e) returning at least the unreacted propane from said acrylic acid-depleted effluent to step (a). 2. The process of claim 1 wherein said dehydrogenation stage (a) is fed with propane and steam in a ratio of about 1/0.5 to 1/10 and a temperature about 400-700-C and a pressure up to about 10 kg/cm2 gauge. 3. The processor claim38 or claim 2 wherein said dehydrogenation stage (a) employs a catalyst comprising a Group VIII noble metal or a base metal oxide one support. 4. A process as claimed in any one of claims 1 to 3 characterized in that the effluent stream of (a) is cooled and water is condensed and separated there from before said effluent stream enters the second stage of (b). 5. A process as claimed in any one of claims I to 4 characterized in that said effluent of (c) is cooled to condense water therefrom and acrylic acid is recovered as an aqueous solution, thereby forming a residual effluent gaseous stream comprising unreacted propylene, propane, and acrolein, and oxygen and carbon oxides. 6. A process as claimed in claim 5 characterized in that the propylene, propane, and acrolein of said residual gaseous stream are absorbed in a suitable solvent and thereafter recovered from said solvent and returned to step (a). 7. A process as claimed in claim 5 characterized in that said residual gaseous stream is passed over a suitable catalyst at selective oxidation conditions for removal of said oxygen by reaction with hydrogen and thereafter returned -to step (a). 8. A process as claimed in any one of claims 1 to 7 characterized in that the effluent stream of step (b) is contact with a solvent to increase the acrolein content of said effluent stream passing over said second oxidation catalyst.

Inventors: KHOOBIAR, SARGIS, PORCELLI, RICHARD V.
Applicants: THE HALCON SD GROUP, INC.
Application year: 1984
Main classification: C07C51
IPC codes: C07C45, C07C57, C07C51, C07C67