Cyclohexanone separation device

Abstract

The utility model discloses a cyclohexanone separation device. The cyclohexanone separation device comprises a light component removal tower, a partition plate tower, a first condenser and a first reboiler, the interior of the partition plate tower is sequentially divided into a rectifying section, a partition plate section and a stripping section from top to bottom, the partition plate section is provided with a vertical partition plate, and the partition plate section is divided into a pre-separation area and a main tower area by the partition plate; a tower kettle of the light component removal tower is communicated with the pre-separation area and is used for introducing crude cyclohexanone in the tower kettle of the light component removal tower into the pre-separation area; and the main tower area is provided with a first discharge port. According to the utility model, the cyclohexanol tower is integrated into the cyclohexanone tower, and cyclohexanol and heavy components are separated while a cyclohexanone product is obtained in the single cyclohexanone tower, so that not only can the investment of the device be reduced, but also the energy consumption is reduced, and meanwhile, the construction land of the device is also reduced, and good economic benefits are achieved. A cyclohexanone product is obtained by using a single cyclohexanone tower, and the separation of cyclohexanol and heavy components is realized at the same time.

Description

Technical Field

[0001] This utility model relates to a device for separating cyclohexanone. Background Technology

[0002] Cyclohexanone, an important chemical raw material, is a major intermediate in the production of caprolactam and also an important industrial solvent. Currently, the main method for producing cyclohexanone is the dehydrogenation of cyclohexanol in the presence of a catalyst, with a cyclohexanol conversion rate of 40%–50%. During the dehydrogenation process, some side reactions inevitably occur, generating light and heavy component impurities. To obtain the cyclohexanone product, the light components must first be removed, and then the unreacted cyclohexanol must be separated. The unreacted cyclohexanol needs to be removed from the heavy components and reused.

[0003] The typical separation and purification process for cyclohexanone is as follows: the crude ketone from the dehydrogenation of cyclohexanol is dehydrated in a dehydration tower, light component impurities are removed in a light component removal tower, cyclohexanone is purified in a cyclohexanone tower, and cyclohexanol and heavy component impurities are separated in a cyclohexanol tower, ultimately yielding the product cyclohexanone. Because the "cyclohexanone purification" and "cyclohexanol purification" processes overlap, the same material undergoes multiple evaporations and condensations, resulting in wasted energy. Utility Model Content

[0004] The technical problem this invention aims to solve is the high cost and energy consumption associated with existing cyclohexanone separation processes, which involve numerous and complex equipment. This invention provides a cyclohexanone separation device that utilizes the separation characteristics of a partitioned column to couple the cyclohexanol and cyclohexanone columns together. Only one reboiler and condenser are needed, allowing for the simultaneous separation of cyclohexanone and heavy components within a single column. Compared to traditional processes, this invention not only reduces equipment investment and energy consumption but also minimizes land use, resulting in significant economic benefits.

[0005] The present invention solves the above-mentioned technical problems through the following technical solution:

[0006] This invention proposes a cyclohexanone separation device, which includes a light-removal tower, a partition tower, a first condenser, and a first reboiler.

[0007] The partition column is divided into a rectification section, a partition section, and a stripping section from top to bottom. The partition section is equipped with vertical partitions, which divide the partition section into a pre-separation zone and a main column zone.

[0008] The bottom of the light-light removal tower is connected to the pre-separation zone, and is used to introduce the crude cyclohexanone from the bottom of the light-light removal tower into the pre-separation zone; the main tower zone is provided with a first discharge port;

[0009] The first condenser is communicated with the rectification section, and is used for returning the material flowed out from the top of the tower to the rectification section after condensation treatment.

[0010] The first reboiler is communicated with the stripping section, and is used for returning the material flowed out from the bottom of the tower to the stripping section after heating treatment.

[0011] In the utility model, the first discharge port is preferably arranged at a position lower than the central height of the baffle.

[0012] In the utility model, the rectification section is used for further purifying the light component. The light component is discharged from the top of the tower, and part of the light component is returned to the condenser to form liquid and return to the tower. The liquid is further mass transferred and heat exchanged with the light component to purify the cyclohexanone. The heat exchanged liquid enters the liquid distributor, and part of the liquid is distributed to the pre-separation zone and the main tower zone through the liquid distributor.

[0013] The pre-separation zone is used for preliminarily separating the crude cyclohexanone. The light component rising from below the pre-separation zone is mass transferred and heat exchanged with the liquid descending from above the pre-separation zone, so that the heavy component and the light component in the crude cyclohexanone are separated. The obtained light component goes upwards into the rectification section, and the heavy component goes downwards into the stripping section.

[0014] The main tower zone is used for further separating the preliminarily separated material. The light component rising from below the main tower zone is mass transferred and heat exchanged with the liquid descending from above the main tower zone to obtain liquid phase cyclohexanol, which is collected from the first discharge port.

[0015] The stripping section is used for gradually evaporating the light component in the liquid phase by using the rising vapor, and condensing the heavy component in the rising vapor to gradually descend. The heavy component is discharged from the bottom of the tower, part of which enters the reboiler to be heated and gasified and then returned to the stripping section to form the rising vapor.

[0016] In some specific embodiments of the utility model, the cyclohexanone separation device further comprises a liquid distributor and a liquid collecting tray. The liquid collecting tray is arranged at the lower part of the rectification section. The liquid distributor is communicated with the top of the bottom plate of the liquid collecting tray, the pre-separation zone and the main tower zone, and is used for distributing the liquid collected from the top of the liquid collecting tray and inputting the liquid into the pre-separation zone and the main tower zone.

[0017] Preferably, the cyclohexanone separation device further comprises an outlet pipe and two inlet pipes. One end of the outlet pipe is connected to a position above the bottom plate of the liquid collecting tray, and the other end of the outlet pipe is connected to the liquid distributor. One end of each of the two inlet pipes is connected to the liquid distributor, and the other end of each of the two inlet pipes is located at a position higher than the top of the baffle on the two sides of the baffle.

[0018] The liquid collecting tray is a conventional structure in the art, and in some embodiments of the present application, the liquid collecting tray comprises a bottom plate, a hollow pipe column and a cover plate, the baffle plate is provided with a hole, the bottom of the hollow pipe column is communicated with the hole, the top of the hollow pipe column is connected with the cover plate, and a gap for gas flow is arranged between the top of the hollow pipe column and the cover plate.

[0019] In the present application, the partitioned column is a conventional structure in the art, such as a structured packing column or a random packing column.

[0020] In some specific embodiments of the present application, the ratio of the cross sections of the pre-separation zone and the main column zone is (1:9)~(9:1), preferably 0.5~3, such as 0.8, 1.28, 1.33, 1.70 or 1.86.

[0021] In some specific embodiments of the present application, the total number of theoretical plates of the partitioned column is 15~150, such as 42, 50, 58, 60 or 65, and the total number of theoretical plates refers to the total number of theoretical plates of the rectification section, the pre-separation zone and the stripping section or the total number of theoretical plates of the rectification section, the main column zone and the stripping section.

[0022] In some specific embodiments of the present application, the number of theoretical plates of the rectification section is 5~50.

[0023] In some specific embodiments of the present application, the number of theoretical plates of the pre-separation zone is 5~50.

[0024] In some specific embodiments of the present application, the number of theoretical plates of the main column zone is 5~50.

[0025] In some specific embodiments of the present application, the number of theoretical plates of the stripping section is 5~50.

[0026] In the present application, the diameter and height of the partitioned column are determined according to the actual processing scale and are conventional in the art. In some specific embodiments of the present application, the diameter of the partitioned column is 50~15000mm, such as 2200mm, 3800mm, 6400mm, 9000mm or 13000mm, and the height of the partitioned column is 1000~50000mm, such as 25300mm, 26000mm, 29700mm, 30150mm or 32000mm.

[0027] In the present application, too few theoretical plates will increase the reflux ratio and increase the operating cost, and too many theoretical plates will increase the investment of the rectification column system.

[0028] In some embodiments of the present application, the pre-separation zone is provided with a feed inlet, the tower kettle of the light-removing column is provided with a coarse cyclohexanone outlet, the feed inlet is communicated with the coarse cyclohexanone outlet, and the coarse cyclohexanone in the tower kettle of the light-removing column is fed into the pre-separation zone.

[0029] In some embodiments of the present application, the feed inlet is arranged at a position higher than the center of the baffle, and in some embodiments, the feed inlet is arranged at a position where the number of theoretical plates of the baffle column is 10-30 from top to bottom.

[0030] In some embodiments of the present application, the top of the baffle column is provided with a second outlet, the rectification section is provided with a first reflux port, and the first condenser is connected between the second outlet and the first reflux port; further, the first reflux port is arranged on the side of the baffle column; further, the second outlet is provided with a first outlet pipe and a first reflux pipe in parallel, and the first condenser is arranged on the first reflux pipe.

[0031] In some embodiments of the present application, the bottom of the baffle column is provided with a third outlet, the stripping section is provided with a second reflux port, and the first reboiler is connected between the third outlet and the second reflux port, so that the material flowing out of the bottom is returned to the stripping section after being heated; further, the second reflux port is arranged on the side of the baffle column; further, the third outlet is provided with a third outlet pipe and a second reflux pipe in parallel, and the reboiler is arranged on the second reflux pipe.

[0032] In the present application, the light-removing column is conventional in the art.

[0033] In some embodiments of the present application, the top of the light-removing column is provided with a fourth outlet and a third reflux port, the fourth outlet is used for discharging light components, and a second condenser is arranged between the fourth outlet and the third reflux port.

[0034] In some embodiments of the present application, the tower kettle of the light-removing column is provided with a coarse cyclohexanone outlet and a fourth reflux port, and a second reboiler is arranged between the coarse cyclohexanone outlet and the fourth reflux port.

[0035] In the present application, the total number of theoretical plates of the light-removing column is conventional in the art, and is determined according to the actual processing scale and the size of the light-removing column.

[0036] In some embodiments of the present application, the total number of theoretical plates of the light-removing column is 15-150, for example, 32.

[0037] In some embodiments of the present application, the diameter of the light-removing column is 100-10000 mm, such as 1300 mm, 2400 mm, 3800 mm, 5800 mm, or 8200 mm.

[0038] In some embodiments of the present application, the height of the light-removing column is 1000-30000 mm, such as 25000 mm.

[0039] When the liquid of cyclohexanol dehydrogenation is separated by the aforementioned separation device of cyclohexanone, the separation method comprises the following steps:

[0040] The liquid of cyclohexanol dehydrogenation is introduced into the light-removing column for light-removing treatment, and the crude cyclohexanone is obtained; the crude cyclohexanone is introduced into the partition column for separation treatment, and the cyclohexanone, cyclohexanol and heavy components are obtained.

[0041] In the present application, the pressure, temperature and reflux ratio of the partition column are conventional in the art.

[0042] In some embodiments of the present application, the pressure at the top of the partition column is 1-20 kPa, such as 4 kPa, 5 kPa or 10 kPa.

[0043] In some embodiments of the present application, the temperature at the top of the partition column is 45-100℃, such as 61.5℃, 66.5℃ or 83.2℃.

[0044] In some embodiments of the present application, the temperature at the bottom of the partition column is 120-200℃, such as 147.3℃, 147.6℃, 152.5℃, 154.4℃ or 162.7℃.

[0045] In some embodiments of the present application, the reflux ratio at the top of the partition column is 1.8-20, preferably 1.8-10, such as 2.23, 2.26, 2.53, 3.46 or 3.79.

[0046] In some embodiments of the present application, when the aforementioned liquid distributor is provided, the mass ratio of the liquid entering the pre-separation zone and the main column zone through the liquid distributor after distribution is 0.1-1.5, such as 0.23, 0.33, 0.40 or 0.46.

[0047] In the present application, the pressure, temperature and reflux ratio of the light-removing column are conventional in the art.

[0048] In some embodiments of the present application, the pressure at the top of the light-removing column is 50-150 kPa, for example 56 kPa.

[0049] In some embodiments of the present application, the temperature at the top of the light-removing column is 100-150 DEG C, for example 110.4 DEG C.

[0050] In some embodiments of the present application, the temperature at the bottom of the light-removing column is 135-175 DEG C, for example 141 DEG C.

[0051] In some embodiments of the present application, the operating reflux ratio of the light-removing column is 100-300 DEG C, for example 120 DEG C.

[0052] In the present application, the reflux ratio refers to the ratio of the flow rate of the reflux liquid returned to the column to the flow rate of the product at the top of the column.

[0053] In the present application, compared to combining the light-removing column and the cyclohexanone column into a partitioned column, the present application integrates the cyclohexanol column into the cyclohexanone column, which has the advantages of lower equipment investment, lower energy consumption, lower operating cost, no need for a complicated condensing system, and lower operating pressure.

[0054] In the present application, the pressure at the top of the column and the temperature at the top of the column refer to the pressure and temperature at the uppermost part of the rectifying section; and the temperature at the bottom of the column refers to the pressure and temperature at the bottommost part of the stripping section.

[0055] In the present application, the cyclohexanol dehydrogenation liquid refers to the product obtained by dehydrogenation of cyclohexanol under the action of a catalyst, and in the art, the cyclohexanol dehydrogenation liquid generally includes cyclohexanone, cyclohexanol, heavy components, and light components.

[0056] The positive progress effect of the present application is that:

[0057] The present application integrates the cyclohexanol column into the cyclohexanone column, and in a single cyclohexanone column, the separation of cyclohexanol and heavy components is achieved while obtaining the cyclohexanone product, which not only reduces the device investment and energy consumption, but also reduces the land used for device construction, and has good economic benefits.

[0058] The present application fully utilizes the separation characteristics of the partitioned column, and only one reboiler and condenser are provided, which not only reduces the device investment, but also saves more than 40% of energy compared to the traditional process, and greatly reduces the operating cost. BRIEF DESCRIPTION OF DRAWINGS

[0059] Figure 1 Figure 1 is a schematic diagram of a cyclohexanone separation device according to Embodiment 1 of the present application.

[0060] Figure 2 A schematic view of the separation device for cyclohexanone according to the present application comparative example 1.

[0061] Explanation of reference signs:

[0062] 1 - dividing wall column, 2 - dividing wall, 3 - light removal column, 4 - first condenser, 5 - first reboiler, 6 - second condenser, 7 - second reboiler, 8 - liquid distributor, 9 - collecting tray;

[0063] A - rectifying section, B1 - pre-separation zone, B2 - main column zone, C - stripping section;

[0064] 101 - second discharge port, 102 - first reflux port, 103 - feed port, 104 - first discharge port, 105 - third discharge port, 106 - second reflux port;

[0065] 301 - fourth discharge port, 302 - third reflux port, 303 - crude cyclohexanone discharge port, 304 - fourth reflux port;

[0066] 901 - bottom plate, 902 - hollow pipe column, 903 - cover plate. DETAILED DESCRIPTION

[0067] The present application will be further illustrated by way of examples below, but the present application is not limited to the scope of the examples.

[0068] Example 1

[0069] The present example discloses a separation device for cyclohexanone, which comprises a dividing wall column 1, a light removal column 3, a first condenser 4, a first reboiler 5, a second condenser 6 and a second reboiler 7.

[0070] The dividing wall column 1 is sequentially divided into a rectifying section A, a dividing wall section and a stripping section C from top to bottom, the dividing wall section is provided with a vertical dividing wall 2, the dividing wall 2 divides the dividing wall section into a pre-separation zone B1 and a main column zone B2, the cross-sectional ratio of the pre-separation zone B1 to the main column zone B2 is 1.28.

[0071] The dividing wall column 1 is provided with a second discharge port 101 at the top, the rectifying section is provided with a first reflux port 102, the first reflux port 102 is arranged at the side of the dividing wall column 1. The first condenser 4 is connected between the second discharge port 101 and the first reflux port 102, specifically, the second discharge port 101 is provided with a first discharge pipe and a first reflux pipe in parallel, the first condenser 4 is arranged on the first reflux pipe, the pre-separation zone B1 is provided with a feed port 103, the feed port 103 is arranged at a position with a theoretical plate number of 10-30 from top to bottom of the dividing wall column; the main column zone B2 is provided with a first discharge port 104, the first discharge port 104 is arranged at a position lower than the center height of the dividing wall.

[0072] The bottom of the partition column 1 is provided with a third discharge port 105, and the stripping section C is provided with a second reflux port 106. The first reboiler 5 is connected between the third discharge port 105 and the second reflux port 106, and is used to return the material flowing out of the bottom to the stripping section C after being heated. Specifically, the second reflux port 106 is arranged on the side of the partition column 1. The third discharge port 105 is provided with a third discharge pipe and a second reflux pipe in parallel. The first reboiler 5 is arranged on the second reflux pipe.

[0073] In the embodiment, the separation device of cyclohexanone further comprises a liquid distributor 8 and a liquid collecting tray 9. The liquid collecting tray 9 comprises a bottom plate 901, a hollow pipe column 902 and a cover plate 903. The bottom plate 901 is provided with a hole. The bottom of the hollow pipe column 902 is communicated with the hole. The top of the hollow pipe column 902 is connected with the cover plate 903. A gap for gas flow is arranged between the top of the hollow pipe column 902 and the cover plate 903. The cross section of the cover plate 903 is inverted V-shaped.

[0074] The liquid collecting tray 9 is arranged at the lower part of the rectifying section A. The feed port of the liquid distributor 8 is communicated with the upper part of the bottom plate 901. Two discharge ports of the liquid distributor 8 are respectively communicated with the pre-separation zone B1 and the main column zone B2, and are used to distribute the liquid collected from the upper part of the liquid collecting tray 9 and input into the pre-separation zone B1 and the main column zone B2.

[0075] The diameter, height and total theoretical plate number of the partition column 1 of the embodiment are shown in Table 3. The theoretical plate number of the rectifying section A is 27. The theoretical plate number of the pre-separation zone B1 is 9. The theoretical plate number of the main column zone B2 is 7. The theoretical plate number of the stripping section C is 6.

[0076] The top of the light-removing column 3 is provided with a fourth discharge port 301 and a third reflux port 302. The second condenser 6 is arranged between the fourth discharge port 301 and the third reflux port 302. The bottom of the light-removing column 3 is provided with a crude cyclohexanone discharge port 303 and a fourth reflux port 304. The second reboiler 7 is arranged between the crude cyclohexanone discharge port 303 and the fourth reflux port 304.

[0077] The crude cyclohexanone discharge port 303 of the light-removing column 3 is communicated with the feed port 103 of the partition column 1. The crude cyclohexanone in the bottom of the light-removing column is input into the pre-separation zone B1.

[0078] The diameter, height, total theoretical plate number, top temperature and pressure, bottom temperature, feed mass flow and other parameters of the light-removing column 3 are the same as those of the comparative example 1. See Table 3 for details.

[0079] The cyclohexanol dehydrogenation liquid is separated and treated by using the separation device of cyclohexanone of the embodiment. The specific steps include the following steps:

[0080] The cyclohexanol dehydrogenation liquid is introduced into the light component removal column 3 for light component removal treatment, light components are collected from the top of the light component removal column 3, and crude cyclohexanone is collected from the bottom of the light component removal column 3; the crude cyclohexanone is introduced into the partition column 1 for separation treatment, to obtain cyclohexanone, cyclohexanol and heavy components.

[0081] The cyclohexanol dehydrogenation liquid includes light components, heavy components, cyclohexanone and cyclohexanol. The feed parameters of the partition column 1 and the obtained cyclohexanone, cyclohexanol and heavy components are shown in Table 1, and the top temperature, top pressure, bottom temperature, top pressure and reflux ratio of the partition column 1 are shown in Table 3.

[0082] The processing scale of the embodiment is 30,000 tons.

[0083] Table 1

[0084]

[0085] Comparative Example 1

[0086] The cyclohexanone separation device of the comparative example is a three-column structure, as shown in Figure 2 The cyclohexanol dehydrogenation liquid is introduced into the light component removal column 3 for light component removal treatment, light components are collected from the top of the light component removal column 3, and crude cyclohexanone is collected from the bottom of the light component removal column 3; the crude cyclohexanone is introduced into the partition column 1 for separation treatment, to obtain cyclohexanone, cyclohexanol and heavy components.

[0087] The cyclohexanol dehydrogenation liquid is introduced into the light component removal column 3 for light component removal treatment, light components are collected from the top of the light component removal column 3, and crude cyclohexanone is collected from the bottom of the light component removal column 3; the crude cyclohexanone is introduced into the partition column 1 for separation treatment, to obtain cyclohexanone, cyclohexanol and heavy components.

[0088] The cyclohexanol dehydrogenation liquid is introduced into the light component removal column 3 for light component removal treatment, light components are collected from the top of the light component removal column 3, and crude cyclohexanone is collected from the bottom of the light component removal column 3; the crude cyclohexanone is introduced into the partition column 1 for separation treatment, to obtain cyclohexanone, cyclohexanol and heavy components.

[0089] The parameters of the light component removal column of the comparative example are the same as those of Example 1.

[0090] Table 2

[0091]

[0092] Table 3

[0093]

[0094] As can be seen, compared with Comparative Example 1, the total energy consumption of the reboiler in Example 1 was reduced by 51.77%.

[0095] Example 2

[0096] The cyclohexanone separation apparatus in this embodiment is basically the same as that in Embodiment 1, except that the size parameters of the partition column 1 and the light component removal column 3 are different from those in Embodiment 1, as shown in Table 6. Specifically, the theoretical number of plates in the rectification section A is 31, the theoretical number of plates in the pre-separation zone B1 is 12, the theoretical number of plates in the main column zone B2 is 9, and the theoretical number of plates in the stripping section C is 7.

[0097] The processing capacity of this embodiment is 100,000 tons.

[0098] The separation method in this embodiment is basically the same as that in embodiment 1, except that the feed parameters, discharge parameters, top temperature and pressure of the partition column, and bottom temperature and pressure are different. The feed parameters of the partition column 1 in this embodiment and the obtained cyclohexanone, cyclohexanol and heavy components are shown in Table 4. The top temperature, top pressure, bottom temperature, top pressure and reflux ratio of the partition column 1 are shown in Table 6.

[0099] Table 4

[0100]

[0101] Comparative Example 2

[0102] The separation apparatus for cyclohexanone in this comparative example is the same as that in Comparative Example 1.

[0103] The separation method of this comparative example is basically the same as that of comparative example 1. The difference is that the feed parameters, discharge parameters, top temperature and pressure of the baffle column, and bottom temperature and pressure are different. The feed parameters of this comparative example and the obtained cyclohexanone, cyclohexanol and heavy components are shown in Table 5. The top temperature and pressure of cyclohexanone column 10 and cyclohexanol column 11, the bottom temperature and pressure, and the reflux ratio are shown in Table 6.

[0104] Table 5

[0105]

[0106] Table 6

[0107]

[0108] As can be seen, in Example 2, the total energy consumption of the reboiler was reduced by 44.48% compared to Comparative Example 2.

[0109] Example 3

[0110] The cyclohexanone separation apparatus in this embodiment is basically the same as that in Embodiment 1, except that the size parameters of the partition column 1 and the light component removal column 3 are different from those in Embodiment 1, as shown in Table 9. Specifically, the theoretical plate number of the rectification section A in this embodiment is 39, the theoretical plate number of the pre-separation zone B1 is 15, the theoretical plate number of the main column zone B2 is 12, and the theoretical plate number of the stripping section C is 11.

[0111] The processing capacity of this embodiment is 250,000 tons.

[0112] The separation method in this embodiment is basically the same as that in embodiment 1, except that the feed parameters, discharge parameters, top temperature and pressure of the partition column, and bottom temperature and pressure are different. The feed parameters of the partition column 1 in this embodiment and the obtained cyclohexanone, cyclohexanol and heavy components are shown in Table 7. The top temperature, top pressure, bottom temperature, top pressure and reflux ratio of the partition column 1 are shown in Table 9.

[0113] Table 7

[0114]

[0115] Comparative Example 3

[0116] The separation apparatus for cyclohexanone in this comparative example is the same as that in Comparative Example 1.

[0117] The separation method of this comparative example is basically the same as that of comparative example 1, except that the feed parameters, discharge parameters, top temperature and pressure of the baffle column, and bottom temperature and pressure are different. The feed parameters of this comparative example and the obtained cyclohexanone, cyclohexanol and heavy components are shown in Table 8. The top temperature, top pressure, bottom temperature and top pressure and reflux ratio of cyclohexanone column 10 and cyclohexanol column 11 are shown in Table 9.

[0118] Table 8

[0119]

[0120] Table 9

[0121]

[0122] As can be seen, the total energy consumption of the reboiler in Example 3 was reduced by 51.04% compared to Comparative Example 3.

[0123] Example 4

[0124] The separation device of cyclohexanone in this example is basically the same as that in Example 1, with the exception that the size parameters of the partition tower 1 and the size parameters of the light-removing tower 3 in this example are different from those in Example 1, as shown in Table 12. Among them, the number of theoretical plates of the rectification section A in this example is 36, the number of theoretical plates of the pre-separation zone B1 is 13, the number of theoretical plates of the main tower zone B2 is 11, and the number of theoretical plates of the stripping section C is 9.

[0125] The processing scale of this example is 600,000 tons.

[0126] The separation method of this example is basically the same as that in Example 1, with the exception that the feed parameters, the discharge parameters, the tower top temperature and pressure of the partition tower, and the tower bottom temperature and pressure are different. The feed parameters of the partition tower 1 in this example and the obtained cyclohexanone, cyclohexanol and heavy components are shown in Table 10, and the tower top temperature, tower top pressure, tower bottom temperature, tower top pressure and reflux ratio of the partition tower 1 are shown in Table 12.

[0127] Table 10

[0128]

[0129] Comparative Example 4

[0130] The separation device of cyclohexanone in this example is the same as that in Comparative Example 1.

[0131] The separation method of this example is basically the same as that in Comparative Example 1, with the exception that the feed parameters, the discharge parameters, the tower top temperature and pressure of the partition tower, and the tower bottom temperature and pressure are different. The feed parameters of this example and the obtained cyclohexanone, cyclohexanol and heavy components are shown in Table 11, and the tower top temperature, tower top pressure, tower bottom temperature, tower top pressure and reflux ratio of the cyclohexanone tower 10 and the cyclohexanol tower 11 are shown in Table 12.

[0132] Table 11

[0133]

[0134] Table 12

[0135]

[0136] It can be seen that, compared with Comparative Example 4, the total energy consumption of the reboiler in Example 4 is reduced by 45.95%.

[0137] Example 5

[0138] The cyclohexanone separation apparatus in this embodiment is basically the same as that in Embodiment 1, except that the size parameters of the partition column 1 and the light component removal column 3 are different from those in Embodiment 1, as shown in Table 15. Specifically, the theoretical plate number of the rectification section A in this embodiment is 40, the theoretical plate number of the pre-separation zone B1 is 11, the theoretical plate number of the main column zone B2 is 9, and the theoretical plate number of the stripping section C is 9.

[0139] The processing capacity of this embodiment is 1.2 million tons.

[0140] The separation method in this embodiment is basically the same as that in Example 1, except that the feed parameters, discharge parameters, top temperature and pressure of the partition column, and bottom temperature and pressure are different. The feed parameters of the partition column 1 in this embodiment and the obtained cyclohexanone, cyclohexanol and heavy components are shown in Table 13. The top temperature, top pressure, bottom temperature, top pressure and reflux ratio of the partition column 1 are shown in Table 15.

[0141] Table 13

[0142]

[0143] Comparative Example 5

[0144] The separation apparatus for cyclohexanone in this comparative example is the same as that in Comparative Example 1.

[0145] The separation method of this comparative example is basically the same as that of comparative example 1, except that the feed parameters, discharge parameters, top temperature and pressure of the baffle column, and bottom temperature and pressure are different. The feed parameters of this comparative example and the obtained cyclohexanone, cyclohexanol and heavy components are shown in Table 11. The top temperature and pressure of cyclohexanone column 10 and cyclohexanol column 14, the bottom temperature and pressure, and the reflux ratio are shown in Table 15.

[0146] Table 14

[0147]

[0148] Table 15

[0149]

[0150] As can be seen, in Example 5, the total energy consumption of the reboiler was reduced by 32.73% compared to Comparative Example 5.

[0151] The specific embodiments described above, in conjunction with the accompanying drawings and one example of the present invention, are specific support for the technical concept of a composite hot water heat transfer isothermal reactor proposed by the present invention. They should not be construed as limiting the scope of protection of the present invention. Any equivalent changes or modifications made based on the technical concept proposed by the present invention shall still fall within the scope of protection of the technical solution of the present invention.

Claims

1. A cyclohexanone separation device, characterized in that, It includes a light-light-removal tower, a baffle tower, a first condenser, and a first reboiler; The partition column is divided into a rectification section, a partition section, and a stripping section from top to bottom. The partition section is equipped with vertical partitions, which divide the partition section into a pre-separation zone and a main column zone. The bottom of the light-light removal tower is connected to the pre-separation zone, and is used to introduce the crude cyclohexanone from the bottom of the light-light removal tower into the pre-separation zone; the main tower zone is provided with a first discharge port; The first condenser is connected to the rectification section and is used to return the material flowing out from the top of the column to the rectification section after condensation. The first reboiler is connected to the stripping section and is used to return the material flowing out of the bottom of the column to the stripping section after heat treatment.

2. The cyclohexanone separation apparatus as described in claim 1, characterized in that, The cyclohexanone separation device further includes a liquid distributor and a collection tray. The collection tray is located at the lower part of the rectification section. The liquid distributor is connected to the bottom plate of the collection tray, the pre-separation zone, and the main column zone. It is used to distribute the liquid collected from the top of the collection tray to the pre-separation zone and the main column zone.

3. The cyclohexanone separation apparatus as described in claim 1, characterized in that, The ratio of the cross-sections of the pre-separation zone and the main tower zone is (1:9) to (9:1).

4. The cyclohexanone separation apparatus as described in claim 1, characterized in that, The total theoretical number of plates in the partition column is 15 to 150. The total theoretical number of plates refers to the sum of the theoretical number of plates in the rectifying section, the pre-separation zone, and the stripping section, or the sum of the theoretical number of plates in the rectifying section, the main column zone, and the stripping section.

5. The cyclohexanone separation apparatus as described in claim 4, characterized in that, The theoretical plate number of the rectification section is 5 to 50; The theoretical plate number of the pre-separation zone is 5 to 50; The theoretical number of trays in the main tower area is 5 to 50; The theoretical plate number of the stripping section is 5 to 50; The diameter of the diaphragm tower is 50~15000mm; The height of the diaphragm tower is 1000~50000mm.

6. The cyclohexanone separation apparatus as described in claim 1, characterized in that, The pre-separation zone is provided with a feed inlet, and the bottom of the light-weight removal tower is provided with a crude cyclohexanone outlet, and the feed inlet is connected to the crude cyclohexanone outlet. The first discharge port is located at a position where the theoretical number of trays in the diaphragm tower is 10 to 30 from top to bottom.

7. The cyclohexanone separation apparatus as described in claim 1, characterized in that, The top of the partition tower is provided with a second discharge port, the rectification section is provided with a first reflux port, and the first condenser is connected between the second discharge port and the first reflux port. The first reflux port is located on the side of the diaphragm tower; The second discharge port is connected in parallel with a first discharge pipe and a first return pipe, and the first condenser is installed on the first return pipe.

8. The cyclohexanone separation apparatus as described in claim 1, characterized in that, The bottom of the partition tower is provided with a third discharge port, the stripping section is provided with a second reflux port, and the first reboiler is connected between the third discharge port and the second reflux port. The second reflux port is located on the side of the diaphragm tower; The third discharge port is connected in parallel with a third discharge pipe and a second reflux pipe, and the reboiler is installed on the second reflux pipe.

9. The cyclohexanone separation apparatus as described in claim 1, characterized in that, The top of the light-light-removal tower is provided with a fourth discharge port and a third reflux port, and a second condenser is provided between the fourth discharge port and the third reflux port; The reboiler of the light-removal tower is equipped with a crude cyclohexanone outlet and a fourth reflux outlet, and a second reboiler is provided between the crude cyclohexanone outlet and the fourth reflux outlet.

10. The cyclohexanone separation apparatus according to claim 1, characterized in that, The total theoretical number of plates in the light-weight removal tower is 15~150; The diameter of the light-weight removal tower is 100~10000mm; The height of the light-weight removal tower is 1000~30000mm.

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