WO2006022208A1 - 多重構造型内部熱交換型蒸留塔 - Google Patents
多重構造型内部熱交換型蒸留塔 Download PDFInfo
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- WO2006022208A1 WO2006022208A1 PCT/JP2005/015175 JP2005015175W WO2006022208A1 WO 2006022208 A1 WO2006022208 A1 WO 2006022208A1 JP 2005015175 W JP2005015175 W JP 2005015175W WO 2006022208 A1 WO2006022208 A1 WO 2006022208A1
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- heat exchange
- section
- outermost
- steam
- innermost
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Classifications
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/14—Fractional distillation or use of a fractionation or rectification column
- B01D3/16—Fractionating columns in which vapour bubbles through liquid
- B01D3/166—Heating and/or cooling of plates
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/14—Fractional distillation or use of a fractionation or rectification column
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/14—Fractional distillation or use of a fractionation or rectification column
- B01D3/26—Fractionating columns in which vapour and liquid flow past each other, or in which the fluid is sprayed into the vapour, or in which a two-phase mixture is passed in one direction
Definitions
- the present invention relates to a multi-structure internal heat exchange distillation column.
- Distillation operations are carried out in many fields including the petrochemical field.
- a multi-stage distillation column is used for more accurate distillation.
- energy loss is large.
- an internal heat exchange type distillation column has been proposed.
- Japanese Patent Application Laid-Open No. 8-133 17 04 a single tube is inserted into a cylindrical main body, a concentric double structure with a concentrating portion inside the single tube and a collecting portion outside.
- An internal heat exchange distillation column is disclosed.
- a single pipe is divided into a plurality of blocks, and a multistage structure is formed in which a plurality of blocks are stacked in the vertical direction.
- the recovery part of one block is connected to the recovery part of the adjacent block by a communication pipe, and the heat of the concentrating part is transferred to the recovery part through the wall of the single pipe and the wall of the communication pipe.
- An object of the present invention is to provide an internal heat exchange type distillation column which is further excellent in energy utilization rate (heat transfer efficiency).
- the present invention has a multiple structure composed of at least an outermost heat exchange part, an intermediate part, and an innermost heat exchange part; the innermost heat exchange part is isolated from the intermediate part; the outermost heat exchange part The outermost heat exchanging portion and the innermost heat exchanging portion communicate with each other through at least two communicating ports; and at least one of the communicating ports from the innermost heat exchanging portion.
- the steam is an inlet to the outermost heat exchange section and the other communication port is an outlet of the steam from the outermost heat exchange section to the innermost heat exchange section, the steam passes from the inlet to the outlet.
- a flow path configured to move only in one direction toward the outer surface is formed in the outermost heat exchange section; and the outermost heat exchange section and the innermost heat exchange section, and the intermediate section One of these is a concentrating part and the other is a recovery part.
- the outermost heat exchange section is composed of a plurality of outermost heat exchange chambers that are mutually independent and arranged one above the other; each of the plurality of outermost heat exchange chambers is The flow path is formed in each of the plurality of outermost heat exchange chambers.
- the outermost heat exchange part and the innermost heat exchange part are concentration parts, and the intermediate part is a recovery part.
- the multi-structure internal heat exchange distillation column of the present invention has a multi-cylindrical structure, a serpentine structure, or a plate structure.
- the innermost heat exchange part and the intermediate part are filled with a filler.
- the innermost heat exchange part and the intermediate part are Ray is provided.
- a tray is provided in the innermost heat exchange part, and the intermediate part is filled with a filler.
- the innermost heat exchange part is filled with a filler, and a tray is provided in the intermediate part.
- the outermost heat exchange section and the innermost heat exchange section communicate with each other, so that heat is transferred from both the side surface of the intermediate portion and the outer surface. . Furthermore, since the steam can flow in one direction from the inlet to the outlet along the flow path formed in the outermost heat exchange section, the steam surely flows toward the outlet without stagnating. Therefore, energy loss is reduced by setting either the outermost heat exchange part, the innermost heat exchange part, or the intermediate part as the high pressure side (high temperature side) and the other as the low pressure side (low temperature side). Is provided with an internal heat exchange distillation column with good heat transfer efficiency.
- FIG. 1 is a schematic top sectional view of a multi-cylindrical internal heat exchange distillation column of the present invention.
- FIG. 2 is a partial cross-sectional view showing an example of the shape of the flow path in the outermost heat exchange section.
- FIG. 3 is a schematic cross-sectional view showing the structure of the outermost heat exchange chamber.
- FIG. 4 is a front sectional view of a triple structure type internal heat exchange distillation column of one embodiment of the present invention.
- FIG. 5 is a front sectional view of a triple structure type internal heat exchange distillation column of another embodiment of the present invention.
- FIG. 6 is a diagram showing an example of an operating state in which toluene and benzene are separated using the triple structure type internal heat exchange distillation column of the present invention.
- BEST MODE FOR CARRYING OUT THE INVENTION The multi-structure internal heat exchange distillation column of the present invention has a multi-structure composed of at least an outermost heat exchange section, an intermediate section, and an innermost heat exchange section.
- the innermost heat exchanging part is separated from the intermediate part and the outermost heat exchanging part is also separated from the intermediate part.
- the innermost heat exchanging part and the outermost heat exchanging part are separated from each other by at least two. It has a structure that communicates with the communication port.
- At least one of the communication ports serves as a steam inlet from the innermost heat exchange unit to the outermost heat exchange unit, and the other communication port serves as a steam outlet from the outermost heat exchange unit to the innermost heat exchange unit.
- a flow path configured to allow steam to move in only one direction from the inlet to the outlet is formed in the outermost heat exchange section. Then, any one of the outermost heat exchange part, the innermost heat exchange part, and the intermediate part is a concentrating part, and the other is a recovery part.
- FIG. 1A is a top sectional view of an internal heat exchange distillation column 1 having a triple cylindrical structure according to an embodiment of the present invention.
- This triple-structured internal heat exchange distillation column 1 is composed of an innermost heat exchange part 2, an intermediate part 3, an outermost heat exchange part 4 and an outer jacket 6, and an innermost heat exchange part 2 and an intermediate part 3, and The intermediate part 3 and the outermost heat exchange part 4 are isolated from each other.
- the innermost heat exchange unit 2 and the outermost heat exchange unit 4 communicate with each other through at least two communication ports 7.
- FIG. 1A is a top sectional view of an internal heat exchange distillation column 1 having a triple cylindrical structure according to an embodiment of the present invention.
- This triple-structured internal heat exchange distillation column 1 is composed of an innermost heat exchange part 2, an intermediate part 3, an outermost heat exchange part 4 and an outer jacket 6, and an innermost heat exchange part 2 and an intermediate part 3, and
- the intermediate part 3 and the outermost heat exchange part 4 are isolated from each other.
- FIG. 1B is a top cross-sectional view of a quadruple cylindrical internal heat exchange distillation column 10 according to another embodiment of the present invention.
- This distillation column 10 has an outermost part 5 between the outermost heat exchange part 4 and the mantle 6 of the triple cylindrical structure type inner heat exchange type distillation tower 1 of FIG. 1A.
- This outermost part 5 is isolated from the outermost heat exchange part 4.
- a part such as a second intermediate part and a second heat exchange part may be provided between the intermediate part 3 and the outermost heat exchange part 4 shown in FIG. ,.
- FIG. 1C is a top sectional view of an internal heat exchange distillation column 110 having a plate structure according to another embodiment of the present invention.
- the outermost heat exchange section of this distillation column 1 1 0 4 Is arranged inside the intermediate part 3 and has a plate structure.
- the innermost heat exchange part 2 and the outermost heat exchange part 4 communicate with each other through at least two communication ports 7.
- the plate structure is installed radially. The arrangement direction and number of plates may be determined according to the operating conditions.
- FIG. 1D is a top cross-sectional view of an internal heat exchange distillation tower having a serpentine tube structure according to another embodiment of the present invention.
- the outermost heat exchange section 4 of the distillation column 120 is disposed inside the intermediate section 3 and has a serpentine structure.
- the innermost heat exchange unit 2 and the outermost heat exchange unit 4 are connected via at least two communication ports 7.
- the serpentine tube structure is arranged concentrically with the innermost heat exchange section 2. The direction and length of the serpentine tube may be determined according to the operating conditions.
- a flow path configured so that steam can move in only one direction from the inlet to the outlet is formed.
- the steam is introduced into the outermost heat exchange part 4 from at least one communication port 7 which is an inlet of the steam, It is configured to return to the innermost heat exchanging unit 2 from another communication port 7 which is an outlet of steam through a flow path provided in the outermost heat exchanging unit 4.
- the communication ports 7 may be provided close to each other or may be provided apart from each other, but are preferably provided apart from each other.
- the steam flow path in the outermost heat exchange section 4 is configured so that the steam always flows and there is no stagnation part. That is, the steam enters from the steam inlet 71 and flows only in the direction of the steam outlet 72.
- a specific example of the flow path of the outermost heat exchange section 4 of the multi-structure distillation column will be described.
- the flow path of the outermost heat exchanging section 4 having the structure of FIG. 1A is formed in a circumferential shape with a baffle plate, arranged in close contact with the inner wall and the outer wall, and partitioned by a partition plate 73.
- FIG. 2A to 2C are schematic partial cross-sectional views showing the flow path configured as described above.
- FIG. 2A and FIG. 2B are the i-i cross-sectional view and the i i — ii cross-sectional view of FIG. 1A when the communication port 7 is arranged close to each other.
- the steam enters the steam inlet 71, and flows to the near side, hits the partition plate 73, returns along the flow path immediately above, and again the partition plate. 7 It is configured to move to the next flow path upon hitting 3.
- FIG. 2B is a diagram showing that the steam hitting the partition plate 73 rises and flows to the upper channel. Then, as shown in FIGS. 2A and 2B, the steam finally descends from the uppermost flow path and returns to the innermost heat exchange section 2 from the steam outlet 72.
- FIG. 2C is a cross-sectional view taken along the line ii-ii of FIG. 1A when the communication port 7 is arranged separately.
- 2A and 2B above differ in that the steam flows out from the steam outlet 72 provided at the top of the outermost heat exchange section 4, and the steam flow is as shown in FIG. 2A. And the same as in Figure 2B.
- FIG. 2D is a cross-sectional view of the multi-structure distillation column having the plate structure of FIG. 1C, and is a schematic diagram showing the flow path of the outermost heat exchange section 4.
- a flow path is formed in the plate by a baffle plate. This flow path is formed so that the steam moves in only one direction.
- FIG. 2E is a schematic diagram showing a steam flow path when a serpentine tube structure is used as the outermost heat exchange section 4.
- a pressure difference is generated by the tray 21 located between the steam inlet 7 1 and the steam outlet 7 2, and the steam enters from the steam inlet 7 1 and moves upward in one direction along the serpentine tube. It is configured to flow and exit from the steam outlet 7 2.
- the steam flow path of the outermost heat exchange section 4 is configured such that steam entering from the steam inlet 71 moves only in one direction toward the steam outlet 72. ing. When distilling, vapors of components (substances) with different boiling points of 2 or more flow in the distillation column.
- the shape of the flow path is not particularly limited.
- the flow path may be formed in a spiral shape using a baffle plate, a pipe having a semicircular cross section, or the like. By arranging such a spiral flow path, steam can move smoothly along the inner wall of the outermost heat exchange section 4.
- the condensing part is pressurized to a temperature higher than that of the recovery part.
- the amount of energy saved is the difference in the amount of heat obtained by subtracting the amount of heat used for pressurization from the amount of heat transferred from the concentration unit to the recovery unit.
- the outermost heat exchange section 4 is composed of a plurality of outermost heat exchangers that are independent of each other and arranged vertically.
- the partial heat exchange chamber 4a is preferably configured.
- Each of the plurality of outermost heat exchange chambers 4 a communicates with the innermost heat exchange section 2 through at least two communication ports 7.
- FIG. 3 is a schematic cross-sectional view showing the structure of the outermost heat exchange chamber 4a.
- the communication port 7 has steam inlets 7 1 (communication ports 7 1) and steam outlets 7 2 (communication ports 7 2) at the upper and lower portions of each outermost heat conversion chamber 4 a. Is provided.
- FIG. 3 shows an i_i cross-sectional view when the outermost heat exchange section 4 of FIG. 1A is divided into a plurality of outermost heat exchange chambers 4a.
- the flow path in FIG. 3 is formed circumferentially with a baffle plate as in FIG. 1A, arranged in close contact with the inner wall and the outer wall, and partitioned by a partition plate 73. As described in FIG.
- the steam enters from the steam inlet 71 (lower communication port), flows from the steam inlet 71 to the near side, and hits the partition plate 73.
- the steam hitting the partition plate 7 3 rises and flows along the upper channel, hits the partition plate 73 again, and moves to the next channel. While repeating this process, the steam exits from the steam outlet 7 2 to the innermost heat exchange section 2.
- a pipe with a semicircular cross section, a coil, and the like are appropriately arranged so that the steam moves spirally along the inner wall of the outermost heat exchange section 4. It may be.
- the condensate will return to the bottom of the concentrating section. Therefore, there is no reflux to each part, so the reflux ratio may be insufficient. In this case, distillation is possible if sufficient reflux is performed at the top of the concentrating section. However, energy is required for returning the liquid by external reflux.
- the steam introduced into the outermost heat exchange chamber 4a depends on the height direction of the concentrating section. Concentration distribution is formed and condensed by heat exchange. The condensed liquid returns from the communication port 7 1 to the innermost heat exchange section 2, This liquid becomes a reflux liquid having an appropriate concentration.
- the lowest temperature in the concentrating section is the highest, so if the outermost heat exchange section 4 is not separated, the temperature difference between the recovery section and concentrating section at the top of the tower is large. Therefore, operation is easier if the outermost heat exchanger 4 is not separated.
- the number of outermost heat exchange chambers 4a (the number of divisions of outermost heat exchange section 4) is not particularly limited. Increasing the number of divisions complicates the structure of the distillation tower, so the appropriate number should be determined in consideration of the degree of energy saving.
- FIG. 4 is a front sectional view of a triple structure type internal heat exchange distillation column (hereinafter simply referred to as a distillation column) 100.
- the distillation tower 100 is composed of an innermost heat exchange section 2, an intermediate section 3, and an outermost heat exchange section 4.
- the innermost heat exchange section 2 is an intermediate section 3, and the intermediate section 3 is an outermost section.
- Each of the intermediate parts 3 is in contact with the outermost heat exchange part 4 and its inner side is in contact with the innermost heat exchange part 2.
- the outermost heat exchange section 4 communicates with the innermost heat exchange section 2 through the lower communication port 71 and the upper communication port 72.
- the innermost heat exchange part 2 and the outermost heat exchange part 4 to the high pressure side (high temperature side) and the intermediate part 3 to the low pressure side (low temperature side), or the innermost heat exchange part 2 and the outermost heat exchange part
- the heat exchange part 4 By setting the heat exchange part 4 to the low pressure side (low temperature side) and the intermediate part 3 to the high pressure side (high temperature side), the side of the intermediate part 3 passes from the high pressure side (high temperature side) to the low pressure side (low temperature side). Heat transfer.
- the innermost heat exchanging part 2 and the outermost heat exchanging part 4 are set to the high pressure side (high temperature side, that is, the concentrating part), and the intermediate part 3 is set to the low pressure side (low temperature). Side, that is, the recovery unit).
- the arrows in Fig. 4 indicate the steam flow.
- the lower part of the innermost heat exchange section 2 of the distillation column 100 is provided with a condensing part steam inlet 81, and the upper part of the innermost heat exchange part 2 is provided with a condensing part steam outlet 82.
- a concentrating part liquid inlet 83 is provided near the top of the innermost heat exchanging part 2, and a concentrating part liquid outlet 84 is provided in the lower part of the innermost heat exchanging part 2.
- a recovery unit steam outlet 9 1 is provided at the lower part of the intermediate part 3, and a recovery part steam outlet 92 is provided at the upper part of the intermediate part 3.
- a recovery part liquid inlet 93 is provided slightly below the recovery part steam outlet 92, and in the lowermost part of the intermediate part 3, a recovery part liquid outlet 94 is provided.
- the steam supplied from the condensing unit steam inlet 8 1 moves upward in the innermost heat exchanging part 2 and transfers to the intermediate part 3 to become a liquid along the inner wall of the innermost heat exchanging part 2. Distillation is carried out while coming into contact with the vapor that descends and rises from below.
- the steam is recovered from the concentrating section steam outlet 82, while the liquid collects at the bottom of the innermost heat exchange section 2.
- a part of the steam enters the outermost heat exchange section 4 from the lower steam inlet 71, moves upward, and returns to the innermost heat exchange section 2 from the steam outlet 72.
- the steam flowing in the outermost heat exchanging section 4 also becomes liquid when transferring heat to the intermediate section 3, and descends along the inner wall of the outermost heat exchanging section 4 in gas-liquid contact with the rising steam and communicates with the lower part. It returns to the innermost heat exchanging part 2 from the port 7 1 and is collected in the lower part of the innermost heat exchanging part 2. Most The liquid collected in the lower part of the internal heat exchange part 2 is extracted from the concentrating part liquid outlet 84.
- the inner side surface of the intermediate part 3 is transferred from the innermost heat exchanging part 2 and the outer side face is transferred from the outermost heat exchanging part 4, so that the heat transfer efficiency is extremely high and distillation is performed efficiently.
- a flow path may be formed by providing a baffle plate as shown in FIG.
- a steam passage may be formed by welding a pipe having a semicircular cross section in a spiral shape.
- both the innermost heat exchange part 2 and the intermediate part 3 are preferably provided with packings or trays.
- packings or trays There is no particular restriction on the arrangement of the packing or tray.
- a tray is provided in the innermost heat exchanging part 2 and the filling is filled in the intermediate part 3, or the innermost heat exchanging part 2 is filled with a filling, It is also preferable to provide a tray in the intermediate part 3.
- packings usually used by those skilled in the art that is, regular packing and irregular packing are used.
- a tray usually used by those skilled in the art is used.
- the tray is porous throughout the tray, only a portion (eg, the sieve portion) is porous, or the entire tray Any of non-porous may be sufficient.
- the tray may be a tray without a weir or a tray with a weir. Or you may use combining these. Examples of such a tray include a lift tray, a pulp tray, a sheave tray, and a cap tray.
- FIG. 5 is a front sectional view of a triple structure type internal heat exchange distillation column (hereinafter simply referred to as a distillation column) 200.
- a distillation column In the distillation tower 200, the innermost heat exchange part 2 and the outermost heat exchange part 4 are used as a concentrating part, and the intermediate part 3 is used as a collecting part.
- the innermost heat exchanger 2 of the distillation column in Fig. 5 is provided with a tray 21.
- the same reference numerals as those in FIG. 4 mean structures having the same functions as those in FIG. As shown in FIG.
- the outermost heat exchange section 4 of the distillation column 200 is composed of a plurality of outermost heat exchange chambers 4a that are independent and divided into upper and lower parts.
- the outermost heat exchange chamber 4 a communicates with the innermost heat exchange section 2 through two communication ports 7 1 and 7 2, respectively. By this communication, the outermost heat exchange chamber 4a can function as a concentration section.
- the steam introduced into the innermost heat exchanging part 2 from the condensing part steam inlet 8 1 provided at the lower part of the innermost heat exchanging part 2 ascends the inner wall of the innermost heat exchanging part 2, Heat is transferred to the middle part 3.
- Steam is liquefied by heat transfer, descends along the inner wall of the innermost heat exchanger 2 and is distilled while making vapor-liquid contact with the steam rising from the bottom.
- the steam enters each outermost heat exchange section 4a from each of the steam inlets 71 provided below the plurality of outermost heat exchange sections 4a.
- the steam flows in one direction along the flow path formed in the outermost heat exchange part 4a, and the innermost heat exchange part from the steam outlet 72 provided above each outermost heat exchange part 4a. It is configured to return to 2.
- the steam liquefies while transferring heat to the intermediate part 3, and the liquid comes into contact with the steam while returning to the steam inlet 71 along the formed flow path, and distillation is performed.
- the steam that has returned from the outermost heat exchange section 4 a to the innermost heat exchange section 2 is finally recovered from the condensing section steam outlet 82 at the top of the innermost heat exchange section 2.
- the liquid returns from the communication port (steam inlet) 71 to the innermost heat exchange section 2 and is extracted from the concentrated section liquid outlet 84 provided at the lower part of the innermost heat exchange section 2.
- the steam introduced into the outermost heat exchange chamber 4a is higher than the concentration section.
- a density distribution corresponding to the vertical direction is formed.
- the liquid condensed in each section is returned to the concentration section of the section as a reflux liquid, so that the distillation is sufficiently performed.
- reflux is insufficient, distillation cannot be performed and concentration cannot be performed.
- the amount of reflux from the outside can be reduced, and energy corresponding to the reduced amount can be saved. That is, energy is saved by exchanging heat internally.
- the distillation column of the present invention is a distillation column that can approach an ideal operation in which the distillation column can be operated only by internal heat exchange.
- a tray 21 is provided in the innermost heat exchange section 2 and / or the intermediate section 3.
- tray 2 1 or packing
- steam inlet 7 1 and steam outlet A pressure difference is generated between the two and the steam, and the flow of steam into the outermost heat exchange section 4 (outermost heat exchange chamber 4a) becomes smoother, and the distillation efficiency is improved.
- the flow path forming member 85 may be provided near (slightly above) the steam inlet 71 in the innermost heat exchange section 2.
- a tray is arranged in the innermost heat exchange part 2, it may be installed between the steam inlet 71 and the steam outlet 72.
- the packing When the packing is arranged, it may be arranged at the position of the steam inlet 7 1 or the steam outlet 7 2. If a tray or packing is placed in such a position, the pressure near the steam inlet 7 1 of the outermost heat exchange section 4 a is higher than the pressure near the steam outlet 72 because of pressure loss. High, it is easy for steam to flow into the outermost heat exchange section 4a. However, in order to prevent the steam from drifting, the steam flow path in the outermost heat exchange section 4a is made one flow path, and the steam entering from the steam inlet 71 stays in the outermost heat exchange section 4a. Without leaving the steam outlet 7 2, the steam flows in one direction, so that there is no steam stagnation inside the outermost heat exchange section 4 (outermost heat exchange chamber 4 a).
- the outermost heat exchanging part 4a may be provided with a plate as shown in FIG. 2 to form a flow path, or the steam is spirally formed on the outermost part.
- a guide may be provided by a baffle plate or the like so as to go up in the heat exchange part 4a.
- the distillation column 200 shown in FIG. 6 includes an innermost heat exchange unit 2 and an outermost heat exchange unit 4a that are concentrating units, and an intermediate unit 3 that is a recovery unit.
- the innermost heat exchange unit 2 is provided with a tray 21.
- one flow path is formed in a spiral shape by a baffle plate from the steam inlet 71 to the steam outlet 72.
- the benzene / toluene mixture is supplied from the recovery section liquid inlet 93, which is the raw material inlet, to the intermediate section 3, which is the recovery section.
- the intermediate part 3 (recovery part) is set to a predetermined temperature and pressure, and the upper part of the intermediate part 3 (recovery part) is set to a temperature near the boiling point of benzene at this pressure, for example.
- the lower part of the intermediate part 3 (recovery part) is set to a temperature near the boiling point of toluene at this pressure.
- Part of the recovered toluene is heated by the reboiler 95 and introduced into the intermediate part 3 (recovery part) from the recovery part steam inlet 91 and becomes a heat source for the intermediate part 3 (recovery part).
- the vapor mainly composed of benzene in the intermediate part 3 (recovery part) is discharged from the recovery part steam outlet 92 and pressurized by the compressor 9 7, and the steam in the innermost heat exchange part 2 (concentration part). It enters the innermost heat exchanging section 2 (concentrating section) through the condensing section steam inlet 81 and becomes a heat source for the innermost heat exchanging section 2 and the outermost heat exchanging section 4a (concentrating section).
- Inner heat exchange part 2 and outermost heat exchange part 4 a are set at a higher temperature and pressure than in intermediate part 3 (collection part), and innermost heat exchange part 2 and outermost heat
- the upper part of the exchange part 4a is set, for example, to a temperature near the boiling point of benzene at this pressure, and the lower part is set to a temperature near the boiling point of toluene at this pressure.
- the benzene vapor is discharged from the condensing unit vapor outlet 82, cooled by the condenser 96, and partly collected.
- the remaining benzene (liquid) is refluxed from the concentrating section liquid inlet 83 to the innermost heat exchange section 2 (concentrating section).
- the mixed solvent of benzene and toluene in the innermost heat exchange section 2 accumulates in the lower part of the innermost heat exchange section 2 (concentration section), and is discharged from the concentrating section liquid outlet 8 4 to be collected in the recovery section. It is introduced into the intermediate part 3 (recovery part) through the inlet 93 together with the raw material benzene and toluene mixture. In this way, benzene and toluene are fractionated continuously.
- the inner side surface and the outer side surface of the intermediate part are in contact with the outermost heat exchange part, so that heat can be transferred very efficiently. It can be used as a distillation column that achieves energy saving and has excellent fractionation efficiency.
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Priority Applications (3)
Application Number | Priority Date | Filing Date | Title |
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JP2006531883A JP4966655B2 (ja) | 2004-08-24 | 2005-08-15 | 多重構造型内部熱交換型蒸留塔 |
EP05772551A EP1800726A4 (en) | 2004-08-24 | 2005-08-15 | INTERNAL THERMAL EXCHANGE TYPE DISTILLATION TOWER WITH MULTI-STRUCTURES |
US11/660,444 US7846303B2 (en) | 2004-08-24 | 2005-08-15 | Multi-structure internal heat exchange type distillation tower |
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JP2004243745 | 2004-08-24 | ||
JP2004-243745 | 2004-08-24 |
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WO2006022208A1 true WO2006022208A1 (ja) | 2006-03-02 |
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PCT/JP2005/015175 WO2006022208A1 (ja) | 2004-08-24 | 2005-08-15 | 多重構造型内部熱交換型蒸留塔 |
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US (1) | US7846303B2 (ja) |
EP (1) | EP1800726A4 (ja) |
JP (1) | JP4966655B2 (ja) |
WO (1) | WO2006022208A1 (ja) |
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WO2011043199A1 (ja) * | 2009-10-05 | 2011-04-14 | 独立行政法人産業技術総合研究所 | 熱交換型蒸留装置 |
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CN104524800B (zh) * | 2014-12-31 | 2016-06-22 | 石家庄工大化工设备有限公司 | 一种具有换热塔板的热耦合喷射并流塔 |
DE102017106177A1 (de) * | 2017-03-22 | 2018-09-27 | Thyssenkrupp Ag | Boden für eine Stoffaustauschkolonne |
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- 2005-08-15 WO PCT/JP2005/015175 patent/WO2006022208A1/ja active Application Filing
- 2005-08-15 EP EP05772551A patent/EP1800726A4/en not_active Withdrawn
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Cited By (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
WO2011043199A1 (ja) * | 2009-10-05 | 2011-04-14 | 独立行政法人産業技術総合研究所 | 熱交換型蒸留装置 |
KR101235388B1 (ko) | 2009-10-05 | 2013-02-20 | 토요엔지니어링 카부시키가이샤 | 열 통합 증류 장치 |
US8440056B2 (en) | 2009-10-05 | 2013-05-14 | National Institute Of Advanced Industrial Science And Technology | Heat integrated distillation apparatus |
Also Published As
Publication number | Publication date |
---|---|
JP4966655B2 (ja) | 2012-07-04 |
US7846303B2 (en) | 2010-12-07 |
US20070251679A1 (en) | 2007-11-01 |
JPWO2006022208A1 (ja) | 2008-05-08 |
EP1800726A1 (en) | 2007-06-27 |
EP1800726A4 (en) | 2010-07-14 |
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