DISTILLATION SYSTEM AND DISTILLATION METHOD THEREOF

Abstract

The present disclosure relates to a distillation system for separating a mixed material existing in feedstock into a high volatile component and a low volatile component using difference of boiling point, the system comprising: an evaporation-separator which evaporates the high volatile component to discharge the high volatile component as an overhead vapor; a first compressor which receives the discharged overhead vapor and adiabatically compresses the received discharged overhead vapor; an evaporator which receives the adiabatically compressed overhead vapor, exchanges heat between water supplied from a water supply source and the compressed overhead vapor and evaporates the water into water vapor; and a second compressor which receives the evaporated water vapor and compresses the received evaporated water vapor. Accordingly, provided herein is a distillation system and distillating method thereof, capable of compressing the overhead vapor before the overhead vapor is introduced into the evaporator, and then increasing the amount of saturated water vapor in the method of generating the saturated water vapor using the condensed latent heat of the compressed overhead vapor, thereby reducing distillation cost.

Claims

1. A distillation system for separating a mixed material existing in feedstock into a high volatile component and a low volatile component using difference of boiling point, the system comprising: an evaporation-separator which evaporates the high volatile component to discharge the high volatile component as an overhead vapor; a first compressor which receives the discharged overhead vapor and adiabatically compresses the received discharged overhead vapor; an evaporator which receives the adiabatically compressed overhead vapor, exchanges heat between water supplied from a water supply source and the compressed overhead vapor, and evaporates the water into water vapor; and a second compressor which receives the evaporated water vapor and compresses the received evaporated water vapor.

2. The system according to claim 1, wherein heat of the water vapor compressed at the second compressor is supplied as a heat source for separating the mixed material in the distillation system.

3. The system according to claim 1, wherein the first compressor adiabatically compresses the overhead vapor using Mechanical Vapor Recompression (MVR) method.

4. A distillating method at a distillation system for separating a mixed material existing in feedstock into a high volatile component and a low volatile component using difference of boiling point, the method comprising following steps: (a) applying heat to an evaporation-separator containing the mixed material and evaporating the high volatile component to discharge the high volatile component as an overhead vapor; (b) adiabatically compressing the discharged overhead vapor by means of a first compressor which receives the discharged overhead vapor; (c) evaporating the water into water vapor by exchanging heat between water and the adiabatically compressed overhead vapor by means of an evaporator which receives the adiabatically compressed overhead vapor; and (d) compressing the water vapor by means of a second compressor which receives the evaporated water vapor.

5. The method according to claim 4, further comprising, after the step (d), (e) supplying heat of the compressed water vapor as a heat source for separating the mixed material in the distillation system.

Description

BRIEF DESCRIPTION OF THE DRAWINGS

[0016] Example embodiments will now be described more fully hereinafter with reference to the accompanying drawings; however, they may be embodied in different forms and should not be construed as limited to the embodiments set forth herein. Rather, these embodiments are provided so that this disclosure will be thorough and complete, and will fully convey the scope of the example embodiments to those skilled in the art.

[0017] In the drawing figures, dimensions may be exaggerated for clarity of illustration. It will be understood that when an element is referred to as being between two elements, it can be the only element between the two elements, or one or more intervening elements may also be present between two elements. Like reference numerals refer to like elements throughout.

[0018] FIG. 1 is a view schematically illustrating a conventional distillation system.

[0019] FIG. 2 is a view schematically illustrating a distillation system according to an embodiment of the present disclosure.

[0020] FIG. 3 is a view schematically illustrating a conventional distillation system illustrating data acquisition points regarding Table 1 and Table 3.

[0021] FIG. 4 is a view schematically illustrating a distillation system according to an embodiment of the present disclosure illustrating data acquisition points regarding Table 2 and Table 4.

[0022] FIG. 5 is a flowchart of a distillation method according to an embodiment of the present disclosure.

DETAILED DESCRIPTION

[0023] Hereinbelow, for explaining configurative elements having the same features, the explanation will be made in a first embodiment as a representative using the same reference numerals, and in the rest of the embodiments, explanation will be made on features that are different from the first embodiment.

[0024] Hereinafter, explanation will be made on a distillation system and distillation method thereof according to the first embodiment of the present disclosure with reference to the drawings attached.

[0025] FIG. 2 is a view schematically illustrating a distillation system according to an embodiment of the present disclosure.

[0026] The distillation system according to the embodiment of the present disclosure may be configured to include an evaporation-separator 110, a first compressor 120, an evaporator 130 and a second compressor 140.

[0027] The evaporation-separator 110 is an apparatus for receiving feedstock or raw materials composed of mixed materials and for separating the received feedstock into high volatile component and low volatile component. The evaporation-separator 110 may receive heat from a reboiler 150. Here, by the quantity of heat retained by the low volatile component in the lower portion, that has been heated and evaporated by the reboiler 150, the high volatile component of the mixed material is evaporated and discharged as overhead vapor.

[0028] In the drawings, there is only one evaporation-separator 110 illustrated, but configurations using a plurality of evaporation-separators are also known, and thus features of the technical concept of the present disclosure may of course be applied thereto as well.

[0029] The first compressor 120 performs an adiabatic compression of the overhead vapor discharged from the evaporation-separator 110 before introducing the overhead vapor into the evaporator 130. Here, as the pressure of the overhead vapor rises, its temperature rises accordingly. In the present disclosure, the first compressor 120 may be configured to adiabatically compress the overhead vapor using Mechanical Vapor Recompression (MVR) method.

[0030] The evaporator 130 generates saturated water vapor by heat exchange of water with the condensation latent heat of the overhead vapor adiabatically compressed at the first compressor 120. Specifically, from a separate water supply source (not illustrated), water is supplied to the evaporator 130, and the supplied water is evaporated according to the required temperature and pressure, and by the second compressor 140, the saturated water vapor is compressed to reach the temperature and pressure required by evaporation-separator 110. Uncondensed overhead vapor is re-circulated and supplied to the evaporator 130, while the condensed overhead vapor is discharged to outside from the evaporator 130. Further, the saturated water vapor evaporated from the evaporator 130 passes through the second compressor 140.

[0031] The second compressor 140 compresses the saturated water vapor generated in the evaporator 130 until the temperature and pressure reach temperature and pressure required by the evaporation-separator 110. The second compressor 140 may be configured to perform multi-stage compression using a plurality of Mechanical Vapor Recompression (MVR).

[0032] Meanwhile, a high speed turbo compressor or a low speed blower type compressor and the like may be used as the apparatus using the Mechanical Vapor Recompression (MVR) method. In the case of using the blower type compressor, it is a blower type compressor having a low speed of 10000 rpm or below, and since it operates at low speed, there is an advantage of safe operation without any damage to the compressor even during long term operations. However, the blower type compressor is a low speed compressor of 10000 rpm or below, and preferably between 4000 and 7000 rpm, that is, the compression ratio is lower than the high speed turbo compressor. Therefore, in order to compensate for the low compression ratio, the blower type compressor may be composed of a plurality of blower type compressors. That is, the saturated water vapor saturated in the condensation-evaporator 130 is compressed at multi-stages in the plurality of blower type compressors according to a predetermined compression ratio.

[0033] In FIG. 2, the second compressor 140 was explained as a low speed blower type compressor having multi-stages as an example, but as long as the second compressor 140 can compress the saturated water vapor generated in the evaporator 130 to reach the temperature and pressure required by the evaporation-separator 110 or required by other processes, the second compressor is not limited to the low speed blower type compressor.

[0034] The saturated water vapor evaporated from the evaporator 130 is adiabatically compressed with multi-stages by each compressor 140 sequentially according to a predetermined compression ratio (for example, compression ratio of 1.34.4). Normally, at each stage, the temperature is raised by about 843 C., and in the case of four stages, the temperature may be raised up to about 4050 C.

[0035] Further, when the saturated water vapor is being compressed in each compressor 140, the compressed saturated water vapor is superheated, and thus a desuper-heating which removes the overheat by supplying certain condensate to each compressor 140 is necessary. Therefore, additional saturated water vapor will be obtained in every stage and the amount of saturated water vapor may slightly increase at each stage.

[0036] The water vapor compressed in the second compressor 140 is supplied to the reboiler 150 to be used as heat source of the evaporation-separator 110 or heat source of other processes.

[0037] As mentioned above, the evaporation-separator 110 includes a distillation column, a rectification column, a stripping column, and a stripping vessel or a stripper, etc. Generally, overhead vapor of the rectification column is composed of various kinds of hydrocarbons, and overhead vapor of the stripping column and stripping vessel or stripper is composed of various kinds of hydrocarbons and moisture.

[0038] According to the Dalton's Law regarding mixed gas, each gas has a partial pressure in proportion to the mole fraction that it accounts for in the Molar mass of the mixed gas, and the partial pressure of each gas is determined according to the definition that the sum of each partial pressure is identical to the total pressure of the mixed gas.

[0039] Regarding the discharge temperature of the overhead vapor, the temperature of each gas is identical. However, the discharge pressure of the overhead vapor is different in each gas due to the partial pressure according to the mole fraction of each gas. When saturated water vapor is generated using the condensation latent heat of the overhead vapor in the evaporator 130, condensation starts from the gas such as water having a low saturation vapor pressure, that is, having a high condensation temperature. With the gas volume reduced due to the condensation decreases the partial pressure, partial pressure of other gases are raised by as much as the reduced partial pressure. Then, condensation of the other gases begins and finally, the gas with the highest saturation vapor pressure is condensed at the lowest temperature. In this way, the entirety of the overhead vapor is condensed.

[0040] In the present disclosure, by the first compressor 120, it is possible to raise the pressure of the overhead vapor, and thus, raise the final partial pressure of the overhead vapor which is condensed at the evaporator 130. Therefore, it is possible to condense an increased amount of overhead vapor at a higher temperature and to increase the temperature at which the water vapor is evaporated, whereby there is an advantage to reduce the number of stages of the second compressor and to optimize electricity consumption.

[0041] Hereinafter, a distillation system in which the overhead vapor is compressed by the first compressor 120 before it is introduced into the evaporator 130 as in the present disclosure, is compared with a conventional distillation system where overhead vapor is introduced directly into the evaporator 130 without being compressed, and the simulation results are analyzed.

[0042] FIG. 3 is a view schematically illustrating a conventional distillation system illustrating data acquisition points regarding Table 1 and Table 3, and FIG. 4 is a view schematically illustrating a distillation system according to an embodiment of the present disclosure illustrating data acquisition points regarding Table 2 and Table 4.

[0043] Each of Nos. 1, 2, 3, 4 and 5 indicated in the drawings represents a position from which the data value in the table below has been obtained.

[0044] 1. In the Case where Overhead Vapor is Composed of Water and Methanol

[0045] <Table 1> and <Table 2> represent distillation data at each point illustrated in the drawings, in the aforementioned conventional distillation system and the distillation system according to the present disclosure, respectively. In both cases, the overhead vapor is composed of water and methanol.

TABLE-US-00001 TABLE 1 <Conventional Technology> No. 1 No. 2 No. 3 No. 4 No. 5 Mass flow rate (kg/h) 20,000 20,000 4,400 4,940 Methanol (kg/h) 16,000 16,000 0 0 Water (kg/h) 4,000 4,000 4,400 4,940 Pressure (barA) 1.0 0.9377 0.3123 1.3385 Temperature ( C.) 76.6 70.3 70.0 108.0 Condensate fraction (wt %) 0.0 33.1 0.0 0.0 Log Mean Temperature 2.081 Difference (LMTD) ( C.) Heat exchange area (m.sup.2) 1,580.0 MVR power (KW) 450.0

TABLE-US-00002 TABLE 2 <Present Invention> No. 1 No. 2 No. 3 No. 4 No. 5 Mass flow rate (kg/h) 20,000 20,000 20,000 11,800 13,250 Methanol (kg/h) 16,000 16,000 16,000 0 0 Water (kg/h) 4,000 4,000 4,000 11,800 13,250 Pressure (barA) 1.0 1.25 1.25 0.3123 1.3385 Temperature ( C.) 76.6 99.4 71.1 70.0 108.0 Condensate fraction (wt %) 0.0 0.0 100.0 0.0 0.0 Log Mean Temperature 6.852 Difference (LMTD) ( C.) Heat exchange area (m.sup.2) 1,580.0 MVR power (KW) 175 1200

[0046] In <Table 1> and <Table 2>, No. 1 data is data of the overhead vapor discharged through the evaporation-separator 110, the overhead vapor composed of water and methanol. The water and methanol are discharged from the evaporation-separation in the amount of 16,000 (kg/h) and 4,000 (kg/h), respectively, the pressure and temperature conditions being identical. In <Table 2>, No. 2 data is data of overhead vapor that passed through the first compressor 120 according to an embodiment of the present disclosure, and it can be seen that the pressure rose from 1.0 barA to 1.25 barA, and that the temperature rose from 76.6 C. to 99.4 C., by the adiabatic compression of the first compressor 120. Therefore, the present disclosure is characterized in that the overhead vapor discharged from the evaporation-separator 110 is introduced into the evaporator 130 after it is compressed preliminarily by the first compressor 120.

[0047] In <Table 1> and <Table 2>, No. 4 data represents data of the saturated water vapor evaporated from water at the evaporator 130 using the condensation latent heat of the overhead vapor. As shown in the tables, it can be seen that under the same pressure and temperature, in the conventional method, 4,400 (kg/h) of saturated water vapor is generated at the evaporator 130, but in the present disclosure, a far more amount of 11,800 (kg/h) of saturated water vapor is generated. The amount of the saturated water vapor after final compression by the second compressor 140 is 4,940 (kg/h) and 13,250 (kg/h), respectively. Further, it can be seen that even though the conventional distillation system and the distillation system according to the present disclosure use the same evaporator 130 and thus have the same heat exchange area, their Log Mean Temperature Differences (LMTD) are significantly different from each other, due to the compression by the first compressor 120.

[0048] 2. In the Case where the Overhead Vapor is Composed of Various Different Kinds of Material (Water, Alpha-Epichlorohydrin, Dichlorohydrin, Trichloropropane)

[0049] <Table 3> and <Table 4> represent distillation data in the conventional distillation system and the distillation system according to the present disclosure, respectively.

TABLE-US-00003 TABLE 3 <Conventional Technology> 1 2 4 5 Mass flow rate (kg/h) 26,137 10,000 11,000 Water (kg/h) 16,874 10,000 11,000 Alpha-epichlorohidrin (kg/h) 8,253 Dichlorohydrin (kg/h) 157 Trichloropropane (kg/h) 853 Pressure (barA) 0.406 0.200 1.080 Temperature ( C.) 74.0 60.0 104.0 MVR power (KW) 854.5

TABLE-US-00004 TABLE 4 <Present Invention> 1 2 4 5 Mass flow rate (kg/h) 26,137 26,137 16,250 18,000 Water (kg/h) 16,874 16,874 16,250 18,000 Alpha-epichlorohidrin (kg/h) 8,253 8,253 Dichlorohydrin (kg/h) 157 157 Trichloropropane (kg/h) 853 853 Pressure (barA) 0.406 0.50 0.262 1.080 Temperature ( C.) 74.0 94.6 66.0 104.0 MVR power (KW) 233 1,483

[0050] In <Table 3> and <Table 4>, No. 1 data is data of the overhead vapor discharged from the evaporation-separator 110, the overhead vapor being composed of water and aipha-epichlorohidrin, dichlorohydrin and trichloropropane, and all the value including the conditions of pressure and temperature being the same. In <Table 4>, No. 2 data is data of the overhead vapor that passed through the first compressor 120 of the present disclosure, and it can be seen that the pressure by compression of the first compressor 120 rose from 0.406 barA to 0.50 barA, and that the temperature rose from 74.0 t to 94.6 C.

[0051] In <Table 3> and <Table 4>, No. 4 data represents data of the saturated water vapor evaporated at the evaporator 130, and it can be seen that in the conventional distillation system, 10,000 (kg/h) of saturated water vapor was generated, but in the distillation system according to the present disclosure, a much more amount of 16,250 (kg/h) of saturated water vapor was generated. It can be seen that the amount of saturated water vapor after a final compression by the second compressor are 11,000 (kg/h) and 18,000 (kg/h), respectively.

[0052] As aforementioned with reference to <Table 1> to <Table 4>, it can be seen that, in the present disclosure, the overhead vapor is adiabatically compressed before being introduced into the evaporator, thereby the amount of saturated water vapor generated is increased significantly compared to the conventional technology.

[0053] Next, a distillation method of the distillation system according to an embodiment of the present disclosure will be explained.

[0054] FIG. 5 is a flowchart of the distillation method according to an embodiment of the present disclosure.

[0055] First of all, in the evaporation-separator 110, feedstock is heated using heat energy applied from a separate steam supply unit, so that a high volatile component is evaporated and discharged as overhead vapor (S210). Next, the first compressor 120 adiabatically compresses the overhead vapor discharged from the evaporation-separator 110 before the overhead vapor is introduced into the evaporator 130 (S220). Further, the overhead vapor adiabatically compressed by the first compressor 120 is introduced into the evaporator 130, and water supplied from a separate water supply source (not illustrated) is evaporated into water vapor by the heat exchange using condensation latent heat of the overhead vapor (S230). The saturated water vapor evaporated at the evaporator 130 is compressed at the second compressor 140 (S240), preferably being compressed at multi-stages by the compressor 140 using Mechanical Vapor Recompression (MVR) method. The water vapor compressed through the second compressor 140 may be supplied as a heat source for separating the mixed material in the distillation system (S250). For example, the compressed water vapor may be used as a heat source for heating the evaporation-separator 110 by means of the reboiler 150, or used in other processes that need compressed steam.

[0056] In the drawings and specification, there have been disclosed typical embodiments of the invention, and although specific terms are employed, they are used in a generic and descriptive sense only and not for purposes of limitation. It will be understood by those of ordinary skill in the art that various changes in form and details may be made therein without departing from the spirit and scope of the present invention as defined by the following claims.