Acetone recovery and purification

Abstract

Disclosed are methods and systems for producing acetone from cumene hydroperoxide (CHP). The disclosed methods involve cleaving CHP to form a cleavage product stream. In some embodiments, the cleavage product stream is separated into an overhead stream and a bottoms stream. The bottoms stream is neutralized, washed, and then processed in a crude acetone column to produce a crude acetone stream. The cleavage product overhead stream is flashed forward in the process, bypassing the neutralization, wash, and crude acetone columns, and then combined with the crude acetone stream. The combined acetone stream is fed to an acetone product column. According to some embodiments, the acetone product column has a side draw for obtaining a recycled acetone stream that is recycled to the cleavage reactor. The recycled acetone side draw may be located on the acetone product column below the point where the acetone product is obtained. The disclosed methods improve process efficiency.

Description

Detailed Description of the Invention

[0001] [Field of the Invention] This application relates to methods and systems for producing acetone from cumene. More particularly, embodiments relate to improving the efficiency of acetone recovery.

[0002] [introduction] Phenol and acetone are produced by a variety of processes, the most common of which is variously known as the Hock process, the Hock-Lang process, or the cumene-phenol process. This process begins with the oxidation of cumene (isopropylbenzene) to produce cumene hydroperoxide (CHP). CHP is then cleaved in the presence of an acid catalyst to produce a mixture of phenol, acetone, and / or alpha-methylstyrene ("AMS"). This mixture is subsequently neutralized and fractionated to recover the final products: phenol, acetone, and / or AMS.

[0003] While such processes have been used for decades, there is a continuing need to optimize the efficiency of product recovery in such processes.

[0004] [overview] Disclosed herein is a method for producing acetone, the method including: (i) cleaving cumene hydroperoxide (CHP) in at least one cleavage reactor to form a cleavage product stream; (ii) separating the cleavage product stream into an overhead stream and a bottoms stream; (iii) separating the bottoms stream in a crude acetone column to provide a phenol-rich stream and an acetone-rich stream; (iv) feeding both the overhead stream from step (ii) and the acetone-rich stream from step (iii) to an acetone product column; and (v) obtaining product acetone from the acetone product column. According to some embodiments, the at least one cleavage reactor comprises a first-stage cleavage reactor and a second-stage cleavage reactor, and cleaving the CHP comprises supplying the CHP to the first-stage cleavage reactor, contacting the CHP with an acid catalyst, recycled acetone, and water to produce a first-stage cleavage reactor product, supplying the first-stage cleavage reactor product to the second-stage cleavage reactor, and obtaining a cleavage product stream as an effluent from the second-stage cleavage reactor. According to some embodiments, separating the cleavage product stream into an overhead stream and a bottoms stream comprises flashing the cleavage product stream in a flash drum and supplying the overhead stream from the flash drum. According to some embodiments, the flash drum operates at a pressure of about 90 kPa to about 190 kPa. According to some embodiments, the overhead stream from the flash drum comprises about 60% to about 75% acetone by volume. According to some embodiments, the method further comprises cooling the bottoms stream of step (ii). According to some embodiments, the method further comprises neutralizing the bottoms stream of step (ii). According to some embodiments, feeding both the overhead stream of step (ii) and the acetone-rich stream of step (iii) to the acetone product column comprises combining the overhead stream of step (ii) with the acetone-rich stream of step (iii) to form a combined stream, and feeding the combined stream to the acetone product column. According to some embodiments, the crude acetone column comprises a condenser, and combining the overhead stream of step (ii) with the acetone-rich stream of step (iii) comprises feeding the overhead stream of step (ii) to the condenser.According to some embodiments, the method further includes recycling recycled acetone from the acetone product column to the cleavage reactor used to carry out step (i). According to some embodiments, the acetone product column has a first side draw from which product acetone is obtained and a second side draw from which recycled acetone is obtained. According to some embodiments, the second side draw is located below the first side draw.

[0005] Also disclosed herein is a method for producing acetone, the method including: (i) cleaving cumene hydroperoxide (CHP) in at least one cleavage reactor to form a cleavage product stream; (ii) treating at least a first portion of the cleavage product stream to wash and neutralize the first portion of the cleavage product stream; (iii) separating the first portion of the cleavage product stream in a crude acetone column to provide a phenol-rich stream and an acetone-rich stream; (iv) feeding the acetone-rich stream of step (iii) to an acetone product column; and (v) obtaining product acetone from a first side draw of the acetone product column and recycled acetone from a second side draw of the acetone product column. According to some embodiments, the second side draw is below the first side draw. According to some embodiments, the at least one cleavage reactor comprises a first cleavage reactor and a second cleavage reactor. According to some embodiments, the method further includes recycling recycled acetone to the second cleavage reactor. According to some embodiments, recycling the recycled acetone to the second cleavage reactor comprises recycling acetone in an amount that provides a weight ratio of acetone to CHP of about 0.05 to about 0.25, based on the CHP fed to the at least one cleavage reactor. According to some embodiments, the method further comprises, prior to step (ii), flashing the cleavage product in a flash drum, providing a first portion of the cleavage product stream as a bottoms stream from the flash drum, and providing an overhead stream. According to some embodiments, the method further comprises flashing the overhead stream forward downstream of the crude acetone column. [Brief explanation of the drawings]

[0006] [Figure 1] 1 illustrates an embodiment of a system for producing acetone and phenol from cumene hydroperoxide (CHP). [Figure 2] 1 illustrates an embodiment of an improved system for producing acetone and phenol from cumene hydroperoxide (CHP). DETAILED DESCRIPTION OF THE INVENTION

[0007] [Detailed explanation] FIG. 1 shows a system 100 for producing acetone and phenol from cumene hydroperoxide (CHP). Concentrated CHP enters the system via line 102. The concentration of CHP in line 102 may be about 65-90 wt. %, more typically about 80-85 wt. %, e.g., about 82 wt. %. CHP may be produced by the oxidation of cumene, as described, for example, in U.S. Pat. No. 8,697,917, the entire contents of which are incorporated herein by reference. Oxidation products (not shown) from the oxidation of cumene include CHP and may also include one or more of alpha-methylstyrene (AMS), dimethylbenzyl alcohol (DMBA), and / or acetophenone (ACP).

[0008] The concentrated CHP is sequentially fed to one or two cleavage reactors, as described, for example, in U.S. Patent No. 5,371,305. In the illustrated system 100, two cleavage reactors in series are shown. The CHP is fed to the first cleavage reactor 104, where it is cleaved by an acid catalyst. The acid catalyst may be, for example, sulfuric acid (H2SO4). In the illustrated embodiment, the first cleavage reactor may be a backmix reactor and may operate, for example, between 50°C and 80°C. In the first cleavage reactor, the CHP is partially reacted in two reactions: i) the CHP is cleaved to produce phenol and acetone; and ii) the CHP partially reacts with DMBA in an equilibrium reaction to produce the intermediate product dicumyl peroxide (DCP) and water. DMBA is partially dehydrated to AMS, which reacts with phenol in a sequential reaction to produce high-boiling cumylphenol. AMS may also form high-boiling dimers. Additional by-products, such as hydroxyacetone (HA), 2-methylbenzofuran (2-MBF), and mesityl oxide (MO), may also be produced. Because the cleavage reaction is highly exothermic, recycled acetone may be fed to the cleavage reactor to maintain adequate dilution, thereby minimizing the formation of undesirable by-products. In the illustrated embodiment, recycled purified acetone is fed to the first cleavage reactor via line 106. Water may be added for optimal cleavage yields.

[0009] In the illustrated embodiment, the product of the first cleavage reactor 104 is fed to the second cleavage reactor 108, where three main reactions take place: i) cleavage of residual CHP from the first cleavage reactor to phenol and acetone, ii) dehydration of residual DMBA from the first cleavage reactor to AMS, and iii) conversion of DCP to AMS, phenol, and acetone. The second stage cleavage reactor may be a plug flow reactor and may be steam heated, for example, at a temperature of about 105° C. to 145° C.

[0010] In the illustrated system 100, the cleavage product from the second cleavage reactor 108 is cooled using a cooler 110 and sent to one or more neutralization and wash units 112. The cleavage effluent contains sulfuric acid, which is used as a catalyst for the cleavage reaction. To avoid corrosion problems in downstream equipment, the acid must be extracted and neutralized using one or more bases, such as sodium hydroxide, and / or one or more salt solutions. For example, the salt solutions may be or include sodium phenate. The salt solutions may reduce or stop any ongoing cleavage reactions in the cleavage product. Thus, the neutralization and wash unit 112 may produce a neutralized cleavage product. However, in improved embodiments described below, the cleavage product undergoes different processing, as described below.

[0011] The step following cleavage and neutralization (i.e., acetone fractionation) is primarily aimed at purifying the products (acetone and phenol) and recovering by-products and reusable cumene. The acetone fractionation system serves the following purposes: (1) crude separation of the fractionation feed into light and heavy components, and (2) purification of the acetone product. The organic effluent from the neutralization unit 112 flows to a first distillation column, referred to herein as the crude acetone column (CAC) 114. The function of the CAC is to separate the neutralization product into a phenol fraction and an acetone fraction. Aspects of the CAC are described in U.S. Pat. No. 8,889,915, the entire contents of which are incorporated herein by reference. The vapor fraction (line 120) contains acetone, water, cumene, AMS, small amounts of phenol, and other light materials in the feed. The CAC may include a CAC reboiler 116 and a CAC condenser 118. The CAC reboiler 116 may be a forced circulation exchanger heated, for example, by high-pressure steam. The phenol-rich bottoms (line 122) may be sent to a phenol fractionation unit (not shown). The overhead vapor (line 120) is partially condensed in the CAC condenser 118. The condensed liquid is returned to the CAC 114, while the vapor fraction is sent via line 126 to a second distillation column, referred to herein as the acetone product column (APC) 124.

[0012] The purpose of the APC 124 is to remove light ends (primarily acetaldehyde via line 128) from the acetone product and to separate the acetone from water, cumene, AMS, and other heavy organics. Aspects of the APC are described in U.S. Pat. No. 4,340,447, the contents of which are incorporated by reference. The APC includes an APC reboiler 130 and an APC condenser 131. The APC reboiler 130 may be fed from a liquid trap outside the bottom tray of the APC 124, from a recycle stream from the column bottom, or may be heated by low-pressure steam.

[0013] The interior volume 140 of the APC 124 may be empty or may be partially or completely filled with one or more fill materials (not shown). Exemplary fill materials may include, but are not limited to, trays, packing, or a combination thereof. As used herein, the term "tray" may include, but is not limited to, one or more tray types that may improve contact between the gas and liquid phases within the APC 124. Exemplary trays may include, but are not limited to, perforated trays, sieve trays, bubble cap trays, floating valve trays, fixed valve trays, cartridge trays, dual flow trays, baffle trays, shower deck trays, chimney trays, slit trays, or any combination thereof. As used herein, the terms "packing material" or "packing" may include, but are not limited to, one or more regularly and / or irregularly shaped materials disposed within the APC 124. The packing material can increase the effective surface area within the APC 124, thereby improving mass transfer between the liquid and gas phases within the APC 124. The packing material can be made of any suitable material, such as, for example, metal, non-metal, polymer, ceramic, glass, or any combination thereof. Examples of random packing materials include, but are not limited to, Raschig rings, NeXRings, and the like. TM , Nutter Rings TM , I-Rings TM , C-Rings TM , P-Rings TM , R-Rings TM and S-Rings TM , Intalox® ULTRA, IMTP®, HY-PAK®, CASCADE MINI RINGS®, FLEXIRING®, AHPP saddle rings, pawl rings, SuperBlend TMThe packing may include, but is not limited to, structured packing, corrugated sheets, crimped sheets, gauze, grids, wire mesh, or any combination thereof. The packing may enhance mass transfer and / or separation of multi-component fluids. The packing material and / or packing pattern within the interior volume 140 may include one or more structured packings and / or random packings. Two or more types of packing materials may be disposed within the interior volume 126. The APC 124 may be made of one or more metallic materials that are physically and chemically compatible with the temperature, pressure, and contents of the APC 124. Suitable metallic materials may include, but are not limited to, iron alloys, including carbon and stainless steel, such as clad carbon steel, 304 stainless steel, 316 stainless steel, duplex stainless steel, and combinations of these metallic materials. Additionally, the APC 124 can be operated at pressures and temperatures ranging from a minimum of about 40 kPa, about 50 kPa, or about 60 kPa to a maximum of about 80 kPa, about 90 kPa, or about 100 kPa.

[0014] The final bottoms stream 132 from the APC 124 may be fed to a sectioned crude AMS (not shown). Acetone product may be obtained from a side draw 134. A portion of the APC 124 refluxed from the reflux condenser 131 may be recycled via line 106 to a cleavage reactor section, such as the first cleavage reactor 104 described above. It should be noted that recycled acetone (line 1016) may also be removed as part of the acetone product side draw 134. The amount of recycled acetone may be determined based on the rate of CHP fed to the cleavage reactor. For example, the amount of acetone recycled to the cleavage reactor is an amount of acetone to CHP weight ratio of about 0.05 to about 0.25, based on the rate of CHP fed to the cleavage reactor.

[0015] The APC 124 may be provided with one or more caustic addition points 136 for the addition of a caustic material, such as sodium hydroxide (NaOH). For example, the caustic addition points 136 may be between the feed stream 126 and the product side draw 134.

[0016] It should be understood that certain aspects and devices of system 100 that are not specifically relevant to the present disclosure but that are implemented in the actual operation of such a system are not mentioned herein, as such aspects and devices are well known in the art and may be described in the above-incorporated references.

[0017] The inventors have discovered that the efficiency of system 100 can be improved. FIG. 2 illustrates system 200 for producing acetone and / or phenol from CHP, which is similar in some respects to system 100 (FIG. 1) but includes several improved features. A first additional aspect of system 200 is flash drum 202, which is equipped to receive effluent from a cleavage reactor stage, for example, from second cleavage reactor 108. As discussed above, the second cleavage reactor operates at an elevated temperature, for example, within a range from a minimum of about 105°C, about 110°C, or about 115°C to a maximum of about 135°C, about 140°C, or about 145°C. In system 200, the effluent (including acetone vapor) is supplied to flash drum 202 via line 204. The flash drum may operate at a pressure within a range from a minimum of about 90 kPa or about 100 kPa to a maximum of about 180 kPa or about 190 kPa. Liquid bottoms contained within flash drum 202 are supplied to neutralization cooler 110 via line 206. Acetone-containing vapor from flash drum 202 is "forward flashed" in the process via line 208, bypassing neutralization unit 112 and CAC 114. This acetone-containing vapor has a temperature ranging from a minimum of about 85°C or about 90°C to a maximum of about 115°C or about 120°C. This forward flashed stream contains acetone and may also contain water, cumene, AMS, and phenol. Line 208 may contain from a minimum of about 60% or about 65% by volume to a maximum of about 70% or about 75% by volume acetone. Line 208 may contain from a minimum of about 3.5% or about 4.0% by volume to a maximum of about 5.0% or about 5.5% by volume cumene. Line 208 may contain from a minimum of about 21% or about 23% by volume to a maximum of about 27% or about 29% by volume of water. Line 208 may contain from a minimum of about 0.3% or about 0.32% by volume to a maximum of about 0.38% or about 0.40% by volume of AMS. Line 208 may contain from a minimum of about 0.8% or about 1.0% by volume to a maximum of about 1.3% or about 1.5% by volume of phenol. The forward flashed stream, i.e., vapor stream 208, may be combined with overhead stream 120 of CAC 114.For example, stream 208 may be added to the feed to APC 124 either upstream (208a) or downstream (208b) of CAC condenser 118. Feeding forward-flashed stream 208 upstream of CAC condenser 118 (via stream 208a) or using a separate partial condenser (not shown) may reduce the phenol content of the final vapor stream before sending the stream to APC 124. CAC condenser 118 may be cooled by air, cooling water, tempered water, or the cumene feed stream to the oxidant as described in U.S. Pat. No. 8,889,915.

[0018] Utilizing a flush-forward configuration, as illustrated in system 200, results in improved system efficiency. In particular, by bypassing the CAC 114, some of the work of the CAC reboiler 116 is offloaded. For example, this improved process may reduce the energy input to the CAC by 20% to 30%, e.g., 25%, depending on operational parameters.

[0019] A further improvement in system 200 relates to how much acetone is recycled from APC 124 back to the cleavage reactor. As discussed in system 100 (FIG. 1), a portion of the purified acetone was recycled to first-stage cleavage reactor 104 via line 106. In system 200 of FIG. 2, recycled acetone (line 210) is removed as a side draw below acetone product line 134. The inventors recognized that the energy used at the top of the APC is primarily consumed by separating acetone from water and other light impurities. The inventors also recognized that purified acetone recycled from reflux condenser 131 (as shown in FIG. 1) or from acetone product draw 134 provides recycled acetone of a higher purity than is required to drive the cleavage reaction. Therefore, lowering the point on the column from which recycled acetone is removed results in significant savings in the energy consumed by APC 124. The distance DH below the acetone product draw at which the recycled acetone is removed will be determined based on the particular implementation by balancing energy savings (the higher the DH, the greater the energy savings realized) with the required purity and / or dryness of the recycled acetone. Removing recycled acetone from too low a position on the column risks, for example, contaminating the recycled acetone with caustic. Determining the optimal location of the recycled acetone draw 210 for a particular implementation based on these considerations is within the ability of one skilled in the art. As noted above, the amount of acetone recycled to the cleavage reactor may be determined as a ratio based on the CHP feed rate to the cleavage reactor. For example, the ratio of recycled acetone to CHP feed rate may be about 0.1 to about 0.5 by weight.

[0020] As can be seen in the table below, two improvements are described herein: (1) flashing the acetone-rich portion of the cleavage product forward in the process, thereby bypassing the CAC; and (2) obtaining recycled acetone from a lower side draw on the APC, each resulting in higher efficiency. Flashing the acetone-rich portion of the cleavage product forward in the process (Embodiment 1) improves the efficiency of the process by reducing the energy that must be input to the CAC reboiler. Obtaining recycled acetone from a lower side draw on the APC (Embodiment 2) improves the efficiency by reducing the energy that must be input to the APC reboiler. It should be noted that while the illustrated system 200 includes both of these embodiments, each embodiment contributes individually to improving efficiency. Therefore, processes and systems including any of these embodiments, alone or in combination, are within the scope of this disclosure.

[0021] A comparative study between the system 100 and an embodiment of the improved system 200 was conducted by process simulation. The CHP stream 102 to the first cleavage reactor 104, containing approximately 82 wt. % CHP and 18 wt. % cumene, was used as the feed stream for the study. In both systems, the recycle acetone flow rate to the first cleavage reactor 104 was kept the same. The comparative results of this study are shown in Table 1. [Table 1] This study shows that using embodiment 1 reduces the energy to the CAC by 25%, while embodiment 2 reduces the energy to the APC 124 by 30%. When both embodiments are implemented, the total energy reduction for the entire acetone processing system is approximately 26%.

[0022] While particular embodiments of the present invention have been illustrated and described, it should be understood that the above discussion is not intended to limit the invention to those embodiments. It will be apparent to those skilled in the art that various changes and modifications can be made without departing from the spirit and scope of the invention. Accordingly, the present invention is intended to cover alternatives, modifications, and equivalents, which may be included within the spirit and scope of the invention as defined by the claims.

Claims

1. 1. A method for producing acetone, comprising: (i) cleaving cumene hydroperoxide (CHP) in at least one cleavage reactor to form a cleavage product stream; (ii) separating the cleavage product stream into an overhead stream and a bottoms stream; (iii) separating the bottoms stream in a crude acetone column to provide a phenol-rich stream and an acetone-rich stream; (iv) feeding both the overhead stream of step (ii) and the acetone-rich stream of step (iii) to an acetone product column; (v) obtaining product acetone from the product acetone column; and A method comprising:

2. the at least one cleavage reactor comprises a first stage cleavage reactor and a second stage cleavage reactor; Cleaving the CHP comprises: feeding the CHP to the first-stage cleavage reactor; contacting the CHP with an acid catalyst, recycled acetone, and water to produce a first-stage cleavage reactor product; feeding the first-stage cleavage reactor product to the second-stage cleavage reactor; obtaining the cleavage product stream as an effluent from the second-stage cleavage reactor; The method of claim 1 , comprising:

3. 2. The method of claim 1, wherein separating the cleavage product stream into the overhead stream and the bottoms stream comprises flashing the cleavage product stream in a flash drum and providing the overhead stream from the flash drum.

4. The method of claim 3 , wherein the flash drum operates at a pressure of from 90 kPa to 190 kPa.

5. The overhead stream from the flash drum is 60% to 75% by volume of acetone. The method of claim 3, comprising:

6. 10. The method of claim 1, further comprising cooling the bottoms stream of step (ii).

7. 10. The method of claim 1, further comprising neutralizing the bottoms stream of step (ii).

8. feeding both the overhead stream of step (ii) and the acetone-rich stream of step (iii) to the acetone product column comprises: combining the overhead stream of step (ii) with the acetone-rich stream of step (iii) to form a combined stream; feeding the combined stream to the acetone product column; The method of claim 1 , comprising:

9. the crude acetone column comprises a condenser; 9. The method of claim 8, wherein combining the overhead stream of step (ii) with the acetone-rich stream of step (iii) comprises feeding the overhead stream of step (ii) to the condenser.

10. 10. The process of claim 1, further comprising recycling recycled acetone from the acetone product column to the cleavage reactor used to carry out step (i).

11. 11. The method of claim 10, wherein the acetone product column has a first side draw from which the acetone product is taken and a second side draw from which the recycled acetone is taken.

12. 12. The method of claim 11, wherein the second side draw is located below the first side draw.

13. 1. A method for producing acetone, comprising: (i) cleaving cumene hydroperoxide (CHP) in at least one cleavage reactor to form a cleavage product stream; (ii) treating at least a first portion of the cleavage product stream to wash and neutralize the first portion of the cleavage product stream; (iii) separating the first portion of the cleavage product stream in a crude acetone column to provide a phenol-rich stream and an acetone-rich stream; (iv) feeding the acetone-rich stream of step (iii) to an acetone product column; (v) obtaining product acetone from a first side draw of the product acetone column and obtaining recycled acetone from a second side draw of the product acetone column; Including, The method further comprises, prior to step (ii), flashing the cleavage product in a flash drum, providing the first portion of the cleavage product stream from the flash drum as a bottoms stream and providing an overhead stream.

14. 14. The method of claim 13, wherein the second side draw is below the first side draw.

15. 14. The method of claim 13, wherein the at least one cleavage reactor comprises a first cleavage reactor and a second cleavage reactor.

16. 16. The method of claim 15, further comprising recycling the recycled acetone to the second cleavage reactor.

17. 17. The method of claim 16, wherein recycling the recycled acetone to the second cleavage reactor comprises recycling acetone in an amount that provides a weight ratio of acetone to CHP of from 0.05 to 0.25, based on the CHP supplied to the at least one cleavage reactor.

18. 14. The method of claim 13, further comprising feeding the overhead stream to the acetone product column.

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