CA1098857A - Apparatus for separating mixtures of materials - Google Patents
Apparatus for separating mixtures of materialsInfo
- Publication number
- CA1098857A CA1098857A CA279,666A CA279666A CA1098857A CA 1098857 A CA1098857 A CA 1098857A CA 279666 A CA279666 A CA 279666A CA 1098857 A CA1098857 A CA 1098857A
- Authority
- CA
- Canada
- Prior art keywords
- interior
- tube
- inner tube
- mass transfer
- outer tube
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Expired
Links
Classifications
-
- 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
- B01D3/04—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping pipe stills
Abstract
ABSTRACT OF THE DISCLOSURE
Apparatus for separating mixtures of substances by rectification in a separating column is described. The separating column contains individual parallel connected mass transfer pipes, each of which has its own reflux condenser and its own reflux evaporator.
Apparatus for separating mixtures of substances by rectification in a separating column is described. The separating column contains individual parallel connected mass transfer pipes, each of which has its own reflux condenser and its own reflux evaporator.
Description
~ his invention relates to appara-tus for separating mixtures o~ materials by means of rectification, particularly for separating such mixtures o~ ~aterials the boiling points of which lie ~ery close to one another.
Qften the differences~ iIl the properties of the ~aterials to be separated are so small that even using vacuum,excess pressure, ex~rac~ve distillation or reactive distillation, separation is extraordinarily difficult.
Rectification columns for separati~g such mixtures have a high ratio between the internal mass flo~r ~of the liquid or of the gas) and the mass flow of the mixture to be separated~ Often very many separation stages are necessary, which necessitates a large constructional height of the columns. Additionally, the separation must often be carried out under low pressure (vacuum) which makes the ratio of the volume flow of the gas to the volume flow of the liquid very large. ~or economicall~ carrying out the separation of materials the pressure drop in the column and the quantities of materials to be transported s~ould be as low as possible.
Various rectification columns for facilitating the separation of materials from mixtures of materials with very similar properties are known. In these previously known rectification columns it is dif~icult to g~aran-tee a substantially constant ratio of gas stream to liquid stream at each place of the horizontal cross section. Additionally costly fillings must be used in order to guarantee good wetting with the li~uid, which are easily fouled up.
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The object of the,pres,ent inyention consists in pro-viding a rectification column w'nich enables simple and economic separation of mixtures of materials with boiling points which lie very close to one another and which have very similar properties. This is achieved according to tlle invention by a rectification column which has individually parallel connected mass transfer pipes of which each has its own reflux condenser and its own reflux evaporator.
The expression mass transfer pipe is used to denote a vertically arranged tube in tne interior of which gas flows upwards while on the waIls the liquid flows downwards, by means of whicil mass transfer can take place between liquid and gas.
The feed of tlle mixture of the material to the individual mass transfer pipes and the removal of the at least partly separated materials from tlle mass transfer pipes takes place in the gas phase. By means of this the distribution over the in-dividual mass transfer pipes and ~he collection of the rectified products is facilitated.
~ t the upper or lower end respectively of -the mass trans-f,er pipes, the wall of the tube serves simultaneously as thesurface of the reflux condenser or of the evaporator, res-pectively.
According to a preferred embodiment the inner surface of the mass transfer pipe is so treated that substantially even wctting is achieved. This can be achieved especially by providing axial or helical grooves on the tube wall.
The :~eed of the mi~ure of materi.als to ~e separated and the removal of the rectiflcation products from the in-dividual mass trsnsfer pipes is effected. through opening~
and/or through tubes whiGh are arranged in t~e interior of the mass -transfer pipes and w~ich have openings at suitable places.
~ he invention is described by way o~ example with reference to an embodiment and to the accompanying dral~ings~
in which:
~ igure 1 is a longitudinal section through an individual mass transfer pipe;
~ igure 2 is a longitudinal section through the separating column, and . ~igure 3 i5 a c.ross-section through a part of the wall of a mass transfer pipe.
mass transfer pipe 1 consists of an outer tube
Qften the differences~ iIl the properties of the ~aterials to be separated are so small that even using vacuum,excess pressure, ex~rac~ve distillation or reactive distillation, separation is extraordinarily difficult.
Rectification columns for separati~g such mixtures have a high ratio between the internal mass flo~r ~of the liquid or of the gas) and the mass flow of the mixture to be separated~ Often very many separation stages are necessary, which necessitates a large constructional height of the columns. Additionally, the separation must often be carried out under low pressure (vacuum) which makes the ratio of the volume flow of the gas to the volume flow of the liquid very large. ~or economicall~ carrying out the separation of materials the pressure drop in the column and the quantities of materials to be transported s~ould be as low as possible.
Various rectification columns for facilitating the separation of materials from mixtures of materials with very similar properties are known. In these previously known rectification columns it is dif~icult to g~aran-tee a substantially constant ratio of gas stream to liquid stream at each place of the horizontal cross section. Additionally costly fillings must be used in order to guarantee good wetting with the li~uid, which are easily fouled up.
.
; .
''" .
The object of the,pres,ent inyention consists in pro-viding a rectification column w'nich enables simple and economic separation of mixtures of materials with boiling points which lie very close to one another and which have very similar properties. This is achieved according to tlle invention by a rectification column which has individually parallel connected mass transfer pipes of which each has its own reflux condenser and its own reflux evaporator.
The expression mass transfer pipe is used to denote a vertically arranged tube in tne interior of which gas flows upwards while on the waIls the liquid flows downwards, by means of whicil mass transfer can take place between liquid and gas.
The feed of tlle mixture of the material to the individual mass transfer pipes and the removal of the at least partly separated materials from tlle mass transfer pipes takes place in the gas phase. By means of this the distribution over the in-dividual mass transfer pipes and ~he collection of the rectified products is facilitated.
~ t the upper or lower end respectively of -the mass trans-f,er pipes, the wall of the tube serves simultaneously as thesurface of the reflux condenser or of the evaporator, res-pectively.
According to a preferred embodiment the inner surface of the mass transfer pipe is so treated that substantially even wctting is achieved. This can be achieved especially by providing axial or helical grooves on the tube wall.
The :~eed of the mi~ure of materi.als to ~e separated and the removal of the rectiflcation products from the in-dividual mass trsnsfer pipes is effected. through opening~
and/or through tubes whiGh are arranged in t~e interior of the mass -transfer pipes and w~ich have openings at suitable places.
~ he invention is described by way o~ example with reference to an embodiment and to the accompanying dral~ings~
in which:
~ igure 1 is a longitudinal section through an individual mass transfer pipe;
~ igure 2 is a longitudinal section through the separating column, and . ~igure 3 i5 a c.ross-section through a part of the wall of a mass transfer pipe.
mass transfer pipe 1 consists of an outer tube
2 and an innex tube 3 arranged concentrically theretoO
~ube 3 is provided with two openings 4, 5. Concentric tube sections 6 and 7 of smaller diameter than tube 3 are located at both ends of the mass transfer pipe 1. A further concentric tube section 8 is arranged at the bottom between the tube 2 or 3 and the tube sections 7. ~he sealing of various spaces is effected b~ means of bungs,9 to 13. ~he bungs 10 and 13 are pro~ided with labyrinth throttling sections 14, 15. On the inner tube 3 there are affixed centering pins 16.
. .
.
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The interior spaces of all interior tubes 3 debouch upwardly into a first collector 17 with a pipe 18 and downwardly into a second collector 1~ with a pipe 20. The intermedia-te spaces between the outer tubes 2 and the inner tubes 3 debouch upwardly into a collector 21 with a pipe 22 and below into a collector 23 with a pipe 24. Below the collector 21 there is located the jacket space 25 of the condenser which is divided by means of a baffle 26 and whicll is provided with a cooling water inlet pipe 27 as well as a cooling water outlet pipe 28.
Above the collector 23 there is located the jacket space 29 of an evaporator which is provided with a steam pipe 30 and a con~
densate pipe 31.
The inner surface of the outer tube 2 is provided over its entire periphery and over the entire length of the tube with axial or helically shaped grooves 32 (see Figure 3). The vapour arising condenses above on these surfaces and the conden-sate flows downwards at the base of the groove. In the region of the evaporator this liquid is wholly evaporated and the vapour arising then flows upwards in the annular space between the outer tube 2 and the inner tube 3 in the opposite direction to the liquid. By means of this mass transfer takes place between the liquid and the gaseous phases.
In the example described herein two feed streams are illustrated. The higher introduced feed stream flows through the pipe 18, collector 17, tube section 6, the interior of the inner tube 3 and opening 4 into the annular space between the outer tube 2 and the inner tube 3, where it mixes with the ~ - 5 -ii7 previously mentioned upwardl~ flowing vapour. The lower introduced feed stream flow through the pipe 20 7 collector 19, pipe section 7, the interior of inner tube 3 and opening 5 likewise to -the annular space between the outer tube 2 s and the inner tube 3, wh.ere it likewise mixes with the pre~iousl~ mentioned upwardly flowing vapour~
~ he removal of the head product takes place via the labyrinth throttl.ing section 14, the Gollector Zl and the pipe 22. ~he bottoms product is removed via the baffle which is constituted by the tube section 8 for holding back any liquid which comes to be collected there and fur-ther via the labyri~th throttling section 15, the collector 23 and the pipe 24.
~ he cooling water is fed through the pipe 27 and the jacket space 25 of the condenser and flows, cooling the upper part o.~ the outer tube 2, in the direction shown by the arrow to the outlet .through the pipe 2~. ~he heati~g steam is fed throu~h the pipe 30 to the jacket space 2~
of the evaporator and condenser on the outer surface of the lower part of the outer tube 2~ '~he condensate is fed ~way by the pipe 31~ -. _ .
.- ~:. ~ ;
.-~ . .: , ~ ' ~
~ube 3 is provided with two openings 4, 5. Concentric tube sections 6 and 7 of smaller diameter than tube 3 are located at both ends of the mass transfer pipe 1. A further concentric tube section 8 is arranged at the bottom between the tube 2 or 3 and the tube sections 7. ~he sealing of various spaces is effected b~ means of bungs,9 to 13. ~he bungs 10 and 13 are pro~ided with labyrinth throttling sections 14, 15. On the inner tube 3 there are affixed centering pins 16.
. .
.
.
The interior spaces of all interior tubes 3 debouch upwardly into a first collector 17 with a pipe 18 and downwardly into a second collector 1~ with a pipe 20. The intermedia-te spaces between the outer tubes 2 and the inner tubes 3 debouch upwardly into a collector 21 with a pipe 22 and below into a collector 23 with a pipe 24. Below the collector 21 there is located the jacket space 25 of the condenser which is divided by means of a baffle 26 and whicll is provided with a cooling water inlet pipe 27 as well as a cooling water outlet pipe 28.
Above the collector 23 there is located the jacket space 29 of an evaporator which is provided with a steam pipe 30 and a con~
densate pipe 31.
The inner surface of the outer tube 2 is provided over its entire periphery and over the entire length of the tube with axial or helically shaped grooves 32 (see Figure 3). The vapour arising condenses above on these surfaces and the conden-sate flows downwards at the base of the groove. In the region of the evaporator this liquid is wholly evaporated and the vapour arising then flows upwards in the annular space between the outer tube 2 and the inner tube 3 in the opposite direction to the liquid. By means of this mass transfer takes place between the liquid and the gaseous phases.
In the example described herein two feed streams are illustrated. The higher introduced feed stream flows through the pipe 18, collector 17, tube section 6, the interior of the inner tube 3 and opening 4 into the annular space between the outer tube 2 and the inner tube 3, where it mixes with the ~ - 5 -ii7 previously mentioned upwardl~ flowing vapour. The lower introduced feed stream flow through the pipe 20 7 collector 19, pipe section 7, the interior of inner tube 3 and opening 5 likewise to -the annular space between the outer tube 2 s and the inner tube 3, wh.ere it likewise mixes with the pre~iousl~ mentioned upwardly flowing vapour~
~ he removal of the head product takes place via the labyrinth throttl.ing section 14, the Gollector Zl and the pipe 22. ~he bottoms product is removed via the baffle which is constituted by the tube section 8 for holding back any liquid which comes to be collected there and fur-ther via the labyri~th throttling section 15, the collector 23 and the pipe 24.
~ he cooling water is fed through the pipe 27 and the jacket space 25 of the condenser and flows, cooling the upper part o.~ the outer tube 2, in the direction shown by the arrow to the outlet .through the pipe 2~. ~he heati~g steam is fed throu~h the pipe 30 to the jacket space 2~
of the evaporator and condenser on the outer surface of the lower part of the outer tube 2~ '~he condensate is fed ~way by the pipe 31~ -. _ .
.- ~:. ~ ;
.-~ . .: , ~ ' ~
Claims (5)
PROPERTY OR PRIVILEGE IS CLAIMED ARE DEFINED AS FOLLOWS:
1. Apparatus for separating mixtures of substances by rectification comprising a plurality of parallel connected mass transfer pipes each comprising an outer tube and an inner tube arranged concentrically therein, the interior of the inner tube being in communication with the interior of the outer tube through one or more openings in the inner tube wall, means for feeding a vapour phase mixture to the interior of the inner tube, and means for removing a vapour phase rectification product from the space between the inner and outer tubes at the top and bottom of each mass transfer pipe, each mass transfer pipe having its own reflux condenser and its own reflux evaporator.
2. Apparatus according to claim 1, wherein the mass transfer pipes are connected below and above to collectors for the vapour phase rectification products.
3. Apparatus according to claim 2, wherein the inner wall surface of each outer tube at its two ends constitutes the surface of the reflux condenser or reflux evaporator.
4. Apparatus according to claim 1, 2 or 3 wherein the wall surface of each outer tube has axial or helically running grooves.
5. Apparatus according to claim 1, 2 or 3 wherein each inner tube is divided into two interior sections which are not in communication, each section being in communication with the interior of the outer tube through an opening in the inner tube wall and each having means for feeding a vapour phase mixture to the interior of the inner tube.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CH7158/76 | 1976-06-02 | ||
| CH715876A CH612356A5 (en) | 1976-06-02 | 1976-06-02 | Apparatus and process for separating mixtures of substances by means of rectification |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CA1098857A true CA1098857A (en) | 1981-04-07 |
Family
ID=4320820
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CA279,666A Expired CA1098857A (en) | 1976-06-02 | 1977-06-01 | Apparatus for separating mixtures of materials |
Country Status (4)
| Country | Link |
|---|---|
| CA (1) | CA1098857A (en) |
| CH (1) | CH612356A5 (en) |
| GB (1) | GB1553028A (en) |
| IT (1) | IT1085222B (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113521784A (en) * | 2021-07-05 | 2021-10-22 | 内蒙古工业大学 | Micro-rectification heat integration system |
Families Citing this family (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| FR2525911A1 (en) * | 1982-04-30 | 1983-11-04 | Centre Nat Rech Scient | NOVEL FRACTIONAL DISTILLATION METHOD AND APPLICATIONS FOR THE PRODUCTION OF THERMAL OR MECHANICAL ENERGY FROM TWO LOW LEVEL HEAT SOURCES |
| WO1996006665A1 (en) * | 1994-08-29 | 1996-03-07 | Kimura Chemical Plants Co., Ltd. | Internal heat exchange type distillation column |
-
1976
- 1976-06-02 CH CH715876A patent/CH612356A5/en not_active IP Right Cessation
-
1977
- 1977-05-27 IT IT2410177A patent/IT1085222B/en active
- 1977-05-27 GB GB2254377A patent/GB1553028A/en not_active Expired
- 1977-06-01 CA CA279,666A patent/CA1098857A/en not_active Expired
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113521784A (en) * | 2021-07-05 | 2021-10-22 | 内蒙古工业大学 | Micro-rectification heat integration system |
| CN113521784B (en) * | 2021-07-05 | 2023-01-06 | 内蒙古工业大学 | Micro-rectification heat integration system |
Also Published As
| Publication number | Publication date |
|---|---|
| GB1553028A (en) | 1979-09-19 |
| IT1085222B (en) | 1985-05-28 |
| CH612356A5 (en) | 1979-07-31 |
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| MKEX | Expiry |