CN107213665B - Concurrent fractionating device - Google Patents
Concurrent fractionating device Download PDFInfo
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- CN107213665B CN107213665B CN201710576405.3A CN201710576405A CN107213665B CN 107213665 B CN107213665 B CN 107213665B CN 201710576405 A CN201710576405 A CN 201710576405A CN 107213665 B CN107213665 B CN 107213665B
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- reboiler
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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
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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
- B01D3/143—Fractional distillation or use of a fractionation or rectification column by two or more of a fractionation, separation or rectification step
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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
- B01D3/32—Other features of fractionating columns ; Constructional details of fractionating columns not provided for in groups B01D3/16 - B01D3/30
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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
- B01D3/32—Other features of fractionating columns ; Constructional details of fractionating columns not provided for in groups B01D3/16 - B01D3/30
- B01D3/322—Reboiler specifications
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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
- B01D3/42—Regulation; Control
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P70/00—Climate change mitigation technologies in the production process for final industrial or consumer products
- Y02P70/10—Greenhouse gas [GHG] capture, material saving, heat recovery or other energy efficient measures, e.g. motor control, characterised by manufacturing processes, e.g. for rolling metal or metal working
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- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
Abstract
The invention discloses a concurrent fractionating device, which comprises a raw material preheating tank, an evaporator, a reboiler, a temperature control heat exchanger, a heat recoverer, a low-temperature fraction cooler and a high-temperature fraction cooler, the bottom of the raw material preheating tank is provided with three liquid outlets, the raw material preheating tank is connected with a raw material liquid inlet at the bottom of the temperature control heat exchanger through a temperature control pump, the raw material preheating tank is connected with a raw material liquid inlet at the bottom of the heat recoverer through a heat recovery pump, the raw material preheating tank is connected with the evaporator through a feeding pump, an air outlet of the evaporator at the top of the evaporator is connected with an air inlet of the temperature-controlled heat exchanger on one side of the temperature-controlled heat exchanger, a liquid-gas outlet of the temperature-controlled heat exchanger is connected with a liquid-gas inlet of a reboiler of the reboiler, a high-temperature fraction outlet of the reboiler is connected with a liquid inlet of the heat recoverer on one side of the heat recoverer, and a heater is wrapped on the outer surface of the evaporator. The invention has simple process, small occupied area and low equipment cost, and can recycle the heat in the device.
Description
Technical Field
The invention relates to the field of chemical industry, in particular to a concurrent fractionating device.
Background
In chemical production, fractionation plays an important role as a separation means, most of traditional fractionation devices are countercurrent fractionation, traditional fractionation towers are provided with bubble caps, packing types, float valves and the like, the height of the fractionation towers is higher, the manufacturing cost is high, meanwhile, the occupied area is large, components in the towers of the traditional fractionation towers are complex, the operation requirement is higher, and the energy consumption of the fractionation towers is high.
Disclosure of Invention
The present invention aims at providing one kind of cocurrent fractionating apparatus to solve the technological problems.
In order to achieve the purpose, the invention adopts the following technical scheme:
a concurrent fractionating device comprises a raw material preheating tank, an evaporator, a reboiler, a temperature-controlled heat exchanger, a heat recoverer, a low-temperature fraction cooler and a high-temperature fraction cooler, wherein three liquid outlets are formed in the bottom of the raw material preheating tank, the raw material preheating tank is connected with a raw material inlet in the bottom of the temperature-controlled heat exchanger through a temperature-controlled pump, the raw material preheating tank is connected with a raw material inlet of the heat recoverer in the bottom of the heat recoverer through a heat recovery pump, the raw material preheating tank is connected with the evaporator through a feeding pump, an evaporator gas outlet in the top of the evaporator is connected with a gas inlet on one side of the temperature-controlled heat exchanger, a liquid-gas outlet of the temperature-controlled heat exchanger is connected with a liquid-gas inlet of the reboiler, a high-temperature distillation outlet of the reboiler is connected with a heat recoverer inlet on one side of the heat recoverer, and a heat recoverer outlet on one side of the heat recoverer is connected with a high-temperature fraction cooler inlet on the top of the high-temperature fraction cooler, the bottom of the high-temperature fraction cooler is provided with a high-temperature fraction product outlet, the gas outlet of the reboiler at the top of the reboiler is connected with the inlet of the top low-temperature fraction cooler of the low-temperature fraction cooler, the bottom of the low-temperature fraction cooler is provided with a low-temperature fraction product outlet, the outer surface of the evaporator is wrapped with a heater, the burner is connected with the heater through a pipeline, and one side of the top of the heater is provided with a flue gas outlet.
Preferably, the inside upper portion of reboiler is equipped with the mist eliminator of support mounting, and mist eliminator hand hole has been seted up to mist eliminator one side, and the middle part is equipped with liquid temperature buffer zone in the reboiler, and liquid temperature buffer zone lower part is equipped with heating device, and the import of high temperature fraction export in the reboiler extends downwards and runs through liquid temperature buffer zone.
Preferably, the temperature-adjusting raw material liquid outlet at the top of the temperature-controlling heat exchanger and the heat recoverer raw material liquid outlet at the top of the heat recoverer are both connected with the raw material preheating tank through pipelines.
Preferably, temperature thermocouples are arranged at the front end of the liquid-gas inlet of the reboiler and at the lower part of the liquid temperature buffer zone of the reboiler.
Preferably, the shell side of the temperature-controlled heat exchanger is used for transporting mixed distillate gas, and the raw material liquid for adjusting the temperature is transported through the tube side.
Preferably, the heat recoverer is of a heat exchanger structure, and high-temperature fraction liquid passes through a shell pass.
Compared with the prior art, the invention has the following advantages: the invention has simple process, changes the traditional counter-flow fractionation into the concurrent fractionation, and ensures that the temperature control heat exchanger and the reboiler of the fractionating tower replace the prior fractionation to reduce the occupied area; the design of the evaporator, the reboiler, the temperature control heat exchanger, the heat recoverer, the low-temperature fraction cooler and the high-temperature fraction cooler reduces the operation difficulty and has low operation cost; the heat recoverer can recover and reuse heat in the device; the raw material liquid can be recovered through the temperature-adjusting raw material liquid outlet and the heat recoverer raw material liquid outlet.
Drawings
FIG. 1 is a schematic view of a forward fractionation apparatus according to the present invention.
In the figure: 1. a burner, 2, a heater, 3, an evaporator, 4, an evaporator gas outlet, 5, a temperature-controlled heat exchanger gas inlet, 6, a temperature-controlled feedstock liquid outlet, 7, a temperature-controlled heat exchanger, 8, a temperature-controlled heat exchanger liquid-gas outlet, 9, a feedstock liquid inlet, 10, a heat recoverer feedstock liquid outlet, 11, a heat recoverer liquid inlet, 12, a heat recoverer liquid outlet, 13, a heat recoverer, 14, a heat recoverer feedstock liquid inlet, 15, a temperature-controlled pump, 16, a heat recovery pump, 17, a feed pump, 18, a feedstock preheating tank, 19, a high-temperature fraction cooler, 20, a high-temperature fraction cooler inlet, 21, a low-temperature fraction cooler, 22, a low-temperature fraction cooler inlet, 23, a reboiler gas outlet, 24, a mist eliminator, 25, a reboiler, 26, a high-temperature fraction outlet, 27, a heating device, 28, a reboiler liquid-gas inlet, 29, a liquid temperature buffer zone, 30. and a flue gas outlet.
Detailed Description
The invention is explained in further detail below with reference to the figures and the specific embodiments.
As shown in fig. 1, a concurrent fractionating apparatus includes a raw material preheating tank 18, an evaporator 3, a reboiler 25, a temperature-controlled heat exchanger 7, a heat recovery device 13, a low-temperature fraction cooler 21, and a high-temperature fraction cooler 19, wherein three liquid outlets are formed at the bottom of the raw material preheating tank 18, the raw material preheating tank 18 is connected with a raw material liquid inlet 9 at the bottom of the temperature-controlled heat exchanger 7 through a temperature-controlled pump 15, a shell side of the temperature-controlled heat exchanger 7 removes mixed fraction gas, a raw material liquid at an adjusted temperature passes through a tube side, the amount of the raw material entering the temperature-controlled heat exchanger is controlled by controlling the rotation speed of the temperature-controlled pump or the opening of a valve, so as to adjust the temperature, the temperature of the temperature-controlled heat exchanger can be adjusted by air cooling or other media, the raw material preheating tank 18 is connected with a raw material liquid inlet 14 of the heat recovery device 13 at the bottom of the heat recovery device 13 through a heat recovery pump 16, the heat recovery device 13 is of a heat exchanger structure, the shell pass of the high-temperature distillate liquid is removed, a raw material preheating tank 18 is connected with an evaporator 3 through a feed pump 17, an evaporator air outlet 4 at the top of the evaporator 3 is connected with an air inlet 5 at one side of a temperature-controlled heat exchanger 7, a liquid-gas outlet 8 of the temperature-controlled heat exchanger 7 is connected with a reboiler liquid-gas inlet 28 of a reboiler 25, a high-temperature distillate outlet 26 of the reboiler 25 is connected with a heat recoverer inlet 11 at one side of a heat recoverer 13, a foam catcher 24 mounted on a support is arranged at the upper inner part of the reboiler 25, a foam catcher hand hole is formed at one side of the foam catcher 24, a liquid temperature buffer area 29 is arranged at the middle part in the reboiler 25, a heating device 27 is arranged at the lower part of the liquid temperature buffer area 29 and used for maintaining the temperature of the liquid temperature buffer area to be relatively stable, an inlet of the high-temperature distillate outlet 26 in the reboiler 25 extends downwards to penetrate through the liquid temperature buffer area 29, and the separation of high-low distillate is realized by the design of the liquid temperature buffer area 29, the low-temperature fraction component overflows from the liquid temperature buffer area and upwards passes through the foam catcher and a gas outlet of the reboiler, enters the low-temperature fraction cooler and is cooled to obtain a low-temperature fraction product from the low-temperature fraction cooler, the high-temperature fraction liquid enters the heat recoverer and is cooled to obtain a high-temperature fraction product from the high-temperature fraction cooler after being subjected to heat recovery, temperature measuring thermocouples are respectively installed at the front end of a liquid-gas inlet 28 of the reboiler and the lower part of a liquid temperature buffer area 29 of the reboiler 25, an outlet 12 of the heat recoverer at one side of the heat recoverer 13 is connected with an inlet 20 of the high-temperature fraction cooler at the top of the high-temperature fraction cooler 19, a high-temperature fraction product outlet is formed at the bottom of the high-temperature fraction cooler 19, an air outlet 23 of the reboiler at the top of the reboiler 25 is connected with an inlet 22 of the low-temperature fraction cooler at the top of the low-temperature fraction cooler 21, and a low-temperature fraction product outlet is formed at the bottom of the low-temperature fraction cooler 21, a temperature-adjusting raw material liquid outlet 6 at the top of the temperature-controlling heat exchanger 7 and a heat recoverer raw material liquid outlet 10 at the top of the heat recoverer 13 are both connected with a raw material preheating tank 18 through pipelines, a heater 2 is wrapped on the outer surface of the evaporator 3, the combustor 1 is connected with the heater 2 through a pipeline, a flue gas outlet 30 is formed in one side of the top of the heater 2, and the evaporator 3 can also utilize evaporators in various forms; if multi-stage fractionation is needed, the gas outlet of the reboiler is connected with the next temperature-controlled heat exchanger and another reboiler downwards, and the processes are repeated.
The foregoing is a preferred embodiment of the present invention, and it will be apparent to those skilled in the art that variations, modifications, substitutions and alterations can be made in the embodiment without departing from the principles and spirit of the invention.
Claims (4)
1. A concurrent fractionating device comprises a raw material preheating tank (18), an evaporator (3), a reboiler (25), a temperature control heat exchanger (7), a heat recoverer (13), a low-temperature fraction cooler (21) and a high-temperature fraction cooler (19), and is characterized in that three liquid outlets are formed in the bottom of the raw material preheating tank (18), the raw material preheating tank (18) is connected with a raw material liquid inlet (9) in the bottom of the temperature control heat exchanger (7) through a temperature control pump (15), the raw material preheating tank (18) is connected with a raw material liquid inlet (14) of the heat recoverer in the bottom of the heat recoverer (13) through a heat recovery pump (16), the raw material preheating tank (18) is connected with the evaporator (3) through a feeding pump (17), an evaporator gas outlet (4) in the top of the evaporator (3) is connected with a gas inlet (5) on one side of the temperature control heat exchanger (7), and a liquid-gas outlet (8) of the temperature control heat exchanger (7) is connected with a reboiler liquid outlet (25) of the reboiler (25) A gas inlet (28) is connected, a high-temperature fraction outlet (26) of a reboiler (25) is connected with a heat recoverer inlet (11) at one side of a heat recoverer (13), a heat recoverer outlet (12) at one side of the heat recoverer (13) is connected with a high-temperature fraction cooler inlet (20) at the top of a high-temperature fraction cooler (19), a high-temperature fraction product outlet is arranged at the bottom of the high-temperature fraction cooler (19), a reboiler air outlet (23) at the top of the reboiler (25) is connected with a top low-temperature fraction cooler inlet (22) of the low-temperature fraction cooler (21), a low-temperature fraction product outlet is formed in the bottom of the low-temperature fraction cooler (21), the outer surface of the evaporator (3) is wrapped with a heater (2), the burner (1) is connected with the heater (2) through a pipeline, and one side of the top of the heater (2) is provided with a flue gas outlet (30);
a foam catcher (24) installed by a support is arranged at the inner upper part of the reboiler (25), a foam catcher hand hole is formed in one side of the foam catcher (24), a liquid temperature buffer zone (29) is arranged at the inner middle part of the reboiler (25), a heating device (27) is arranged at the lower part of the liquid temperature buffer zone (29), and an inlet of a high-temperature fraction outlet (26) in the reboiler (25) extends downwards to penetrate through the liquid temperature buffer zone (29);
and a temperature-adjusting raw material liquid outlet (6) at the top of the temperature-controlling heat exchanger (7) and a heat recoverer raw material liquid outlet (10) at the top of the heat recoverer (13) are connected with a raw material preheating tank (18) through pipelines.
2. A forward fractionation apparatus according to claim 1 wherein thermocouples are provided at the front end of the reboiler inlet (28) and below the liquid temperature buffer (29) of the reboiler (25).
3. A forward flow fractionation apparatus according to claim 1 wherein the shell side of said temperature controlled heat exchanger (7) passes mixed distillate gases and the temperature conditioned feed liquid passes the tube side.
4. A co-current fractionator according to claim 1 wherein said recuperator (13) is a heat exchanger structure and high temperature distillate liquid travels the shell side.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201710576405.3A CN107213665B (en) | 2017-07-14 | 2017-07-14 | Concurrent fractionating device |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201710576405.3A CN107213665B (en) | 2017-07-14 | 2017-07-14 | Concurrent fractionating device |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN107213665A CN107213665A (en) | 2017-09-29 |
| CN107213665B true CN107213665B (en) | 2022-06-14 |
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| CN201710576405.3A Active CN107213665B (en) | 2017-07-14 | 2017-07-14 | Concurrent fractionating device |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN102604665B (en) * | 2012-03-23 | 2014-11-12 | 浙江工业大学 | Multilayer-evaporation-based bio-diesel continuous rectification system and process |
| CN105126374B (en) * | 2015-06-29 | 2017-03-29 | 天津市天地创智科技发展有限公司 | A kind of tert-butyl alcohol water ring hexanone oxime differential pressure distillation system |
| CN205115337U (en) * | 2015-10-10 | 2016-03-30 | 河北冀春化工有限公司 | Low power consuming is by device of methyl alcohol preparation aerosol dimethyl ether |
| CN106730967B (en) * | 2017-01-11 | 2019-10-25 | 河北美邦工程科技股份有限公司 | A kind of system and method using the condensation thermal rectification of top gaseous phase fraction |
| CN206934785U (en) * | 2017-07-14 | 2018-01-30 | 王举才 | A kind of downflow type fractionating device |
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| CN107213665A (en) | 2017-09-29 |
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