CN115006863B - Rectification system and rectification process for separating wide boiling range binary mixture - Google Patents
Rectification system and rectification process for separating wide boiling range binary mixture Download PDFInfo
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- 238000000034 method Methods 0.000 title claims abstract description 32
- 238000009835 boiling Methods 0.000 title claims abstract description 21
- 239000000203 mixture Substances 0.000 title claims abstract description 18
- 238000010992 reflux Methods 0.000 claims abstract description 37
- 239000007791 liquid phase Substances 0.000 claims abstract description 25
- 229920006395 saturated elastomer Polymers 0.000 claims abstract description 15
- 238000007599 discharging Methods 0.000 claims abstract description 14
- 239000011555 saturated liquid Substances 0.000 claims abstract description 14
- 239000012071 phase Substances 0.000 claims abstract description 13
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 9
- 239000007788 liquid Substances 0.000 claims description 35
- 238000000926 separation method Methods 0.000 claims description 16
- 230000008016 vaporization Effects 0.000 claims description 6
- 238000010438 heat treatment Methods 0.000 claims description 4
- 239000000463 material Substances 0.000 claims description 3
- 238000001816 cooling Methods 0.000 abstract description 3
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 description 12
- 238000005265 energy consumption Methods 0.000 description 8
- 238000000605 extraction Methods 0.000 description 7
- KFZMGEQAYNKOFK-UHFFFAOYSA-N Isopropanol Chemical compound CC(C)O KFZMGEQAYNKOFK-UHFFFAOYSA-N 0.000 description 6
- IEJIGPNLZYLLBP-UHFFFAOYSA-N dimethyl carbonate Chemical compound COC(=O)OC IEJIGPNLZYLLBP-UHFFFAOYSA-N 0.000 description 6
- 238000004364 calculation method Methods 0.000 description 5
- MVPPADPHJFYWMZ-UHFFFAOYSA-N chlorobenzene Substances ClC1=CC=CC=C1 MVPPADPHJFYWMZ-UHFFFAOYSA-N 0.000 description 5
- 230000008901 benefit Effects 0.000 description 3
- PXQFMBNNNYOFRN-UHFFFAOYSA-N chlorobenzene;propan-2-ol Chemical compound CC(C)O.ClC1=CC=CC=C1 PXQFMBNNNYOFRN-UHFFFAOYSA-N 0.000 description 3
- 238000010586 diagram Methods 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- 238000004088 simulation Methods 0.000 description 3
- 238000009834 vaporization Methods 0.000 description 3
- GUNDKLAGHABJDI-UHFFFAOYSA-N dimethyl carbonate;methanol Chemical compound OC.COC(=O)OC GUNDKLAGHABJDI-UHFFFAOYSA-N 0.000 description 2
- 238000004134 energy conservation Methods 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 238000002309 gasification Methods 0.000 description 2
- 239000002994 raw material Substances 0.000 description 2
- 241000183024 Populus tremula Species 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 238000012824 chemical production Methods 0.000 description 1
- 230000006835 compression Effects 0.000 description 1
- 238000007906 compression Methods 0.000 description 1
- 230000005611 electricity Effects 0.000 description 1
- 125000001449 isopropyl group Chemical group [H]C([H])([H])C([H])(*)C([H])([H])[H] 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
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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
- B01D3/32—Other features of fractionating columns ; Constructional details of fractionating columns not provided for in groups B01D3/16 - B01D3/30
-
- 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
- B01D3/34—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping with one or more auxiliary substances
- B01D3/38—Steam distillation
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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
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
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- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
Abstract
A rectification system and rectification process for separating binary mixtures with wide boiling ranges. The rectification process comprises the following steps: introducing the binary mixture with wide boiling range into a rectifying tower, dividing light component saturated steam extracted from the tower top into two paths, introducing one path into a steam generator, boosting the temperature of the other path through a tower top gas compressor, introducing the other path into a side reboiler, performing heat exchange with saturated liquid extracted from the middle part of the rectifying tower as a heat source, reboiling the saturated liquid, returning the saturated liquid from the middle part of the tower into the tower, and discharging heavy components from a tower kettle; the compressed tower top gas is discharged through a side reboiler at a bubble point, throttled and then introduced into a flash tank, gas phase obtained from the flash tank is introduced into a tower top gas compressor or a steam generator as a heat source, the obtained liquid phase and liquid phase generated after heat exchange of the steam generator are introduced into a reflux buffer tank together, a part of condensate obtained from the reflux buffer tank flows back to the tower top, and the other part of condensate is extracted as a tower top product. The invention can reduce the consumption of the cooling circulating water at the top of the tower and the steam at the bottom of the tower in the rectification process, and is economical and energy-saving.
Description
Technical Field
The present invention relates to rectification technology, and is especially rectification technology for separating binary mixture in wide boiling range.
Background
According to statistics, in the chemical production process, the energy consumption required by the separation process accounts for more than 70% of the whole production process. The rectification is a main means of separation, the economic advantage of the traditional rectification in separation is seriously insufficient, the equipment cost and the operation cost are high, and the energy conservation and emission reduction design of the traditional rectification is imperative under the dual-carbon background.
In order to improve the energy-saving effect and the economic benefit of the traditional rectification, a common improvement mode is to embed a heat pump system into the rectification process and couple the heat of the tower top and the tower bottom, so that the total operation cost can be effectively reduced. Fig. 1 shows a schematic diagram of a conventional heat pump rectification system, and as shown in fig. 1, the heat pump rectification system comprises a rectification tower T5, a tower top gas compressor C5, a tower kettle reboiler E6, a liquid collecting tank V5, a reflux buffer tank V6, a throttle valve V7, a condenser V8, a feed pump P5, a tower kettle extraction pump P6, a reflux pump P7 and the like.
The improved rectification system is mostly used in a near-boiling system and an azeotropic system, and the grade of the rectification system is improved by compressing the gas at the top of the tower, so that the rectification system is used for reboiling and heating the tower bottom. Since in most cases the heat of the top and bottom of the column is not perfectly matched, a water cooler or auxiliary reboiler/preheater etc. needs to be provided, thus increasing the corresponding utility consumption. In addition, in some wide boiling range systems, the pressure ratio that the compressor needs to withstand in conventional heat pump rectification is too large to be suitable due to the excessive temperature difference between the top and bottom of the column.
Disclosure of Invention
The technical problem to be solved by the invention is to provide a rectification system and a rectification process for separating a wide-boiling-range binary mixture, which can reduce the consumption of tower top cooling circulating water and tower bottom steam in the rectification process of the wide-boiling-range binary mixture, reduce public engineering consumption and achieve the effect of economy and energy conservation.
According to one aspect of an embodiment of the present invention, there is provided a rectification process for the separation of a wide boiling range binary mixture comprising the steps of: introducing the binary mixture with wide boiling range into a rectifying tower from the middle part of the rectifying tower for rectifying, dividing light component saturated steam extracted from the tower top into two paths, introducing one path into a steam generator, vaporizing boiler feed water as a heat source, introducing the other path into a side reboiler after boosting and heating by a tower top gas compressor, performing heat exchange with saturated liquid extracted from the middle part of the rectifying tower as the heat source, returning the saturated liquid from the middle part of the rectifying tower to the rectifying tower after reboiling, and discharging heavy components from a tower kettle; the condensed liquid obtained from the side reboiler is introduced into a liquid collecting tank, non-condensable gas is discharged from the top of the liquid collecting tank and enters a steam generator, the liquid phase obtained from the liquid collecting tank is throttled and introduced into a flash tank for gas-liquid separation, the gas phase obtained from the flash tank is introduced into a tower top gas compressor or a steam generator as a heat source, the liquid phase obtained from the flash tank and the liquid phase generated after heat exchange by the steam generator are introduced into a reflux buffer tank together, a part of condensate obtained from the reflux buffer tank flows back to the top of the tower, and the other part of condensate is taken as a tower top product.
According to another aspect of an embodiment of the present invention, there is provided a rectification system for wide boiling range binary mixture separation, comprising a rectification column, an overhead gas compressor, a steam generator, a side reboiler, a bottoms reboiler, a liquid collection tank, a flash tank, a throttling element, and a reflux buffer tank; the gas phase outlet of the top of the rectifying tower is respectively communicated with the gas inlet of the top gas compressor and the hot side inlet of the steam generator, the gas outlet of the top gas compressor is communicated with the hot side inlet of the side reboiler, the hot side outlet of the side reboiler is communicated with the inlet of the liquid collecting tank, the gas phase outlet of the liquid collecting tank is communicated with the hot side inlet of the steam generator, and the liquid phase outlet of the liquid collecting tank is communicated with the material inlet of the flash tank through a throttling element; the cold side inlet and the cold side outlet of the side reboiler are respectively communicated with a collecting outlet and a reflux port which are arranged in the middle of the rectifying tower; the liquid phase outlet of the tower bottom of the rectifying tower is divided into two paths: one path is communicated with a cold side inlet of a tower kettle reboiler, and the other path is discharged by Yu Dafu; the cold side outlet of the tower kettle reboiler is communicated with the tower kettle steam inlet of the rectifying tower; the gas phase outlet of the flash tank is communicated with the gas inlet of the tower top gas compressor or the hot side inlet of the steam generator; the first inlet and the second inlet of the reflux buffer tank are respectively communicated with the liquid phase outlet of the flash tank and the hot side outlet of the steam generator, the outlet of the reflux buffer tank is divided into two paths, one path of reflux tower top and the other path of reflux tower top are used for discharging.
The invention has at least the following advantages and characteristics:
1. In the embodiment, a part of saturated liquid is extracted from the side line and exchanges heat with the compressed tower top gas, and the middle reboiling is realized by using less compression work, so that the heat load of a tower kettle reboiler is greatly reduced, the consumption of tower top cooling circulating water and tower kettle steam is saved, and the aim of saving energy is fulfilled;
2. Aiming at the problem that the heat of the top of the rectifying tower and the heat of the tower kettle cannot be completely matched, the embodiment uses the steam generator to replace an auxiliary heat exchanger which needs to consume cold and hot public engineering in the traditional heat pump rectifying process, the original top gas which needs to be water-cooled is used for generating steam through the steam generator, and the generated steam can be used as other heat exchange requirements after being upgraded by a heat pump, so that the energy consumption of a system is reduced.
Drawings
Fig. 1 shows a schematic diagram of a prior art heat pump rectification system.
FIG. 2 shows a schematic diagram of a rectification system for wide boiling range binary mixture separation in accordance with an embodiment of the present invention.
Detailed Description
The invention will now be described in detail with reference to the drawings and specific examples.
Please refer to fig. 2. The rectification system for separating the wide boiling range binary mixture according to the embodiment of the invention comprises a rectification column T1, an overhead gas compressor C1, a side reboiler E1, a column kettle reboiler E2, a steam generator E3, a liquid collecting tank V1, a flash tank V2, a reflux buffer tank V3, a throttling element V4, a feed pump P1, a column kettle extraction pump P2 and a reflux pump P3.
The broad boiling range of the present invention means that the boiling range is 20 ℃ or higher.
The gas phase outlet of the top of the rectifying tower T1 is respectively communicated with the gas inlet of the top gas compressor C1 and the hot side inlet of the steam generator E3, the gas outlet of the top gas compressor C1 is communicated with the hot side inlet of the side reboiler E1, the hot side outlet of the side reboiler E1 is communicated with the inlet of the liquid collecting tank V1, the gas phase outlet of the liquid collecting tank V1 is communicated with the hot side inlet of the steam generator E3, the liquid phase outlet of the liquid collecting tank V1 is communicated with the material inlet of the flash tank V2 through a throttling element V4, and the cold side inlet and the cold side outlet of the side reboiler E1 are respectively communicated with a collecting outlet and a reflux outlet which are arranged in the middle of the rectifying tower T1.
In the present embodiment, the throttle element V4 is a throttle valve V4. The rectifying tower T1 is a plate-type tower, the extraction outlet and the reflux outlet are arranged on the same column plate of the plate-type tower, and the column plate is selected from the position with smaller temperature difference (the temperature difference is 10-20 ℃) between the middle part of the tower and the top of the tower.
The liquid phase outlet of the tower kettle of the rectifying tower T1 is divided into two paths: one path is communicated with a cold side inlet of a tower kettle reboiler E2, and the other path is used for tower kettle discharging through a tower kettle extraction pump P2; the cold side outlet of the tower kettle reboiler E2 is communicated with the tower kettle steam inlet of the rectifying tower T1. The hot side inlet of the bottoms reboiler E2 is used to receive steam.
The gas phase outlet of the flash tank V2 is communicated with the gas inlet of the tower top gas compressor C1 or the hot side inlet of the steam generator E3; the first inlet and the second inlet of the reflux buffer tank V3 are respectively communicated with the liquid phase outlet of the flash tank V2 and the hot side outlet of the steam generator E3, the outlet of the reflux buffer tank V3 is divided into two paths, one path passes through the reflux pump P3 to reflux the top of the rectifying tower T1, and the other path is used for discharging.
Further, the rectification system of the embodiment of the invention comprises a vapor compressor C2, wherein an air inlet of the vapor compressor C2 is communicated with a cold side outlet of the vapor generator E3, and is used for compressing vapor generated by the vapor generator to realize pressure rise and temperature rise so as to improve the grade of the vapor and be used as other heat exchange requirements.
A rectification process for the separation of wide boiling range binary mixtures according to an embodiment of the present invention comprises the steps of:
Introducing the binary mixture with wide boiling range into a rectifying tower T1 from the middle part of the rectifying tower T1 through a feed pump P1 for rectification, dividing light component saturated steam extracted from the tower top into two paths, introducing one path into a steam generator E3 as a heat source to vaporize boiler feed water, introducing the other path into a side reboiler E1 after boosting and heating through a tower top gas compressor C1 as a heat source to exchange heat with saturated liquid extracted from the middle part of the tower, returning the saturated liquid from the same position of the middle part of the tower into the rectifying tower T1 after reboiling, and discharging the heavy component from the tower bottom after reboiling and concentrating;
the condensed liquid obtained from the side reboiler E1 is introduced into a liquid collecting tank V1, noncondensable gas is discharged from the top of the liquid collecting tank V1 and enters a steam generator E3, condensate in the liquid collecting tank V1 is throttled and introduced into a flash tank V2 for gas-liquid separation, gas phase obtained from the flash tank V2 is introduced into an overhead gas compressor C1 or the steam generator E3 as a heat source, liquid phase obtained from the flash tank V2 and liquid phase generated after heat exchange by the steam generator E3 are introduced into a reflux buffer tank V3 together, a part of condensate obtained from the reflux buffer tank V3 is refluxed to the top of the tower according to a certain reflux ratio, and the other part of condensate is taken as an overhead product.
In this embodiment, the temperature difference between the light component saturated steam after the pressure and temperature rise by the overhead gas compressor and the saturated liquid extracted from the middle part of the rectifying tower is 10-20 ℃. The compressed tower top gas is discharged through a side reboiler E1 and then is introduced into a liquid collecting tank V1 at a bubble point, the liquid phase obtained from the liquid collecting tank V1 is decompressed to the tower top pressure through a throttle valve V4, gas-liquid separation is carried out in a flash tank V2 after partial vaporization, steam returns to an air inlet of a tower top gas compressor C1 (only when compressed tower top gas is insufficient for supplying heat to the side reboiler) or is vaporized by a steam generator E3, and the produced saturated steam is used as other heat exchange requirements through a steam heat pump to improve the grade, so that the whole process energy saving effect is remarkable, and the consumption of tower bottom heat public engineering and tower top cold public engineering is greatly reduced. The above-described vapor heat pump employs a vapor compressor C2 in the present embodiment.
The technical scheme of the invention is further explained by taking the rectification process of the isopropanol-chlorobenzene and methanol-dimethyl carbonate system as an example, and the superiority of the lateral line heat pump rectification process of the embodiment of the invention is explained by comparing the energy consumption and the operation cost of the traditional direct rectification and the traditional heat pump rectification process.
Application example 1
Referring to fig. 2, a calculation simulation result of a side-stream heat pump rectification process flow of isopropanol-chlorobenzene separation is taken as an example to describe, and specific conditions are shown in table 1.
TABLE 1 isopropanol-chlorobenzene separation process conditions
Description of the process flow:
1-1, as shown in fig. 2, feeding an isopropyl alcohol-chlorobenzene mixed raw material into a rectifying tower T1 through a feed pump P1 at a feed rate of 5000kg/h, taking isopropyl alcohol as a light component from the top of the tower (82 ℃,1500kg/h, isopropyl alcohol concentration of 99.9 wt.%), and discharging chlorobenzene as a heavy component from the bottom of the tower (130 ℃,3500kg/h, chlorobenzene concentration of 99.9 wt.%);
1-2, compressing the tower top saturated steam to 510kPa through a tower top gas compressor C1, then taking the compressed steam as a hot stream, exchanging heat with saturated liquid (with the temperature difference of 20 ℃ at the tower top) extracted from the middle side line of a rectifying tower T1 in a side line reboiler E1, discharging cold stream from an extraction tower plate at a gasification rate of 20%, returning the cold stream into the tower, discharging the hot stream after heat exchange at a bubble point, entering a liquid collection tank V1, decompressing to 101.325kPa through a throttle valve V4, separating gas from liquid in a flash tank V2 after partial vaporization, returning the steam to an air inlet of the tower top gas compressor C1, and providing enough heat for side line reboiling after recompression;
1-3, the surplus small amount of tower top gas is vaporized by a steam generator E3, and the produced saturated steam (40 kPa,76 ℃) is upgraded by a steam compressor C2 (300 kPa,150 ℃) and is used as other heat exchange requirements; the condensed liquid phase was collected in a reflux buffer tank V3 together with the liquid phase separated from the flash tank V2, and was subjected to overhead reflux and withdrawn at a reflux ratio of 2.78.
In order to compare the design energy consumption of the conventional direct rectification and the conventional heat pump rectification (as shown in fig. 1) with the heat pump rectification flow of the present invention, the feeding and separation indexes adopted in each flow calculation are identical, ASPEN PLUS is adopted to perform process simulation, the efficiency of the compressor is calculated according to 80%, the public engineering specification is referred to table 2, and the calculation result of each flow energy consumption is referred to table 3.
TABLE 2 Utility Specification
Table 3 energy consumption and utility consumption for each process versus (unit time: hours)
Comparison results: the operation cost of each process year is calculated by combining the table 2 and the table 3, the same separation requirement is achieved under the same feeding condition, the side stream heat pump rectification energy-saving process (110 ten thousand yuan/year) of the application example 1 saves 58.8% of the operation cost per year compared with the traditional direct rectification (267 ten thousand yuan/year), and saves 35.7% of the operation cost per year compared with the traditional heat pump rectification (171 ten thousand yuan/year).
Application example 2
Referring to fig. 2, a calculation simulation result of a side-stream heat pump rectification process flow for separating methanol from dimethyl carbonate is taken as an example for description, and the specific process flow is described as follows:
2-1, feeding a methanol-dimethyl carbonate mixed raw material (1350 kPa, bubble point feed, composition of 50wt.%, 50 wt.%) into a rectifying tower T1 through a feed pump P1 at a feed rate of 5000kg/h, taking methanol and dimethyl carbonate azeotrope (147.27 ℃,1300kPa, methanol: dimethyl carbonate=90.9 wt.: 9.1 wt.%) as light components from the top of the tower (147.27 ℃,1300kPa,2813.6kg/h, methanol: 88.8 wt.%) and dimethyl carbonate: 11.2 wt.%) and taking dimethyl carbonate as heavy components from the bottom of the tower (199.4 ℃,1350kPa,2186.4kg/h, and dimethyl carbonate concentration 99.99 wt.%);
2-2, compressing the saturated steam at the top of the tower to 3000kPa through a compressor C1, taking the compressed saturated steam as a hot stream, exchanging heat with saturated liquid (with the temperature difference of 20 ℃ at the top of the tower) extracted from the middle side line of a rectifying tower T1 in a side line reboiler E1, discharging cold stream from an extraction tower plate at a gasification rate of 20%, returning the cold stream into the tower, discharging the hot stream after heat exchange at a bubble point, entering a liquid collection tank V1, decompressing the hot stream to 1300kPa through a throttle valve V4, separating gas from liquid in a flash tank V2 after partial vaporization, and converging the separated steam and a small amount of surplus overhead gas into one stream to enter a steam generator E3;
2-3, vaporizing boiler feed water in the steam generator E3 by utilizing the latent heat of saturated steam at the top of the tower, and using the generated saturated steam (400 kPa,144 ℃) as other heat exchange requirements after the grade of the saturated steam is improved (2500 kPa,220 ℃) by the steam compressor C2; the condensed liquid phase and the liquid phase separated from the flash tank V2 are fed together into a reflux buffer tank V3, and are subjected to overhead reflux and extraction at a reflux ratio of 5.1.
The calculation results of the energy consumption of each flow in this embodiment are shown in table 4.
Table 4 comparison of Process energy consumption and Utility consumption (unit time: hours)
Comparison results: the operation cost of each process year is calculated by combining the table 2 and the table 4, the same separation requirement is achieved under the same feeding condition, the lateral line heat pump rectification energy-saving process (273 ten thousand yuan/year) saves 75.8% of the operation cost per year compared with the traditional direct rectification (1126 ten thousand yuan/year), and saves 60.4% of the operation cost per year compared with the traditional heat pump rectification (690 ten thousand yuan/year).
The rectification system and the rectification process provided by the embodiment of the invention realize zero consumption of steam and circulating water and even rich steam by using a small amount of electricity consumption.
Claims (7)
1. A rectification process for separating a binary mixture having a wide boiling range, wherein the wide boiling range is 20 ℃ or higher; the method is characterized by comprising the following steps of:
Introducing the binary mixture with wide boiling range into a rectifying tower from the middle part of the rectifying tower for rectifying, dividing light component saturated steam extracted from the tower top into two paths, introducing one path into a steam generator, vaporizing boiler feed water as a heat source, introducing the other path into a side reboiler after boosting and heating by a tower top gas compressor, performing heat exchange with saturated liquid extracted from the middle part of the rectifying tower as the heat source, returning the saturated liquid from the middle part of the rectifying tower to the rectifying tower after reboiling, and discharging heavy components from a tower kettle;
And (3) introducing condensed liquid obtained from a side reboiler into a liquid collecting tank, discharging non-condensable gas from the top of the liquid collecting tank into a steam generator, throttling liquid phase obtained from the liquid collecting tank, introducing the throttled liquid phase into a flash tank for gas-liquid separation, introducing gas phase obtained from the flash tank into a tower top gas compressor or into the steam generator as a heat source, introducing liquid phase obtained from the flash tank and liquid phase generated after heat exchange of the steam generator into a reflux buffer tank together, refluxing a part of condensate obtained from the reflux buffer tank into the top of the tower, and extracting the other part of condensate as a tower top product.
2. The rectification process according to claim 1, wherein the saturated steam produced by said steam generator is upgraded with a steam heat pump.
3. The rectification process according to claim 1, wherein the temperature difference between the saturated vapor of the light component, which has been raised in pressure and temperature by the gas compressor at the top of the column, and the saturated liquid withdrawn from the middle part of the rectification column is 10 ℃ to 20 ℃.
4. A rectification system for separating binary mixtures with a wide boiling range, wherein the boiling range is more than or equal to 20 ℃, and the rectification system is characterized by comprising a rectification column, an overhead gas compressor, a steam generator, a side reboiler, a tower kettle reboiler, a liquid collecting tank, a flash tank, a throttling element and a reflux buffer tank;
The gas phase outlet of the top of the rectifying tower is respectively communicated with the gas inlet of the top gas compressor and the hot side inlet of the steam generator, the gas outlet of the top gas compressor is communicated with the hot side inlet of the side reboiler, the hot side outlet of the side reboiler is communicated with the inlet of the liquid collecting tank, the gas phase outlet of the liquid collecting tank is communicated with the hot side inlet of the steam generator, and the liquid phase outlet of the liquid collecting tank is communicated with the material inlet of the flash tank through the throttling element; the cold side inlet and the cold side outlet of the side reboiler are respectively communicated with a collecting outlet and a reflux port which are arranged in the middle of the rectifying tower;
the liquid phase outlet of the tower kettle of the rectifying tower is divided into two paths: one path is communicated with a cold side inlet of the tower kettle reboiler, and the other path is discharged by Yu Dafu; the cold side outlet of the tower kettle reboiler is communicated with the tower kettle steam inlet of the rectifying tower;
The gas phase outlet of the flash tank is communicated with the gas inlet of the tower top gas compressor or the hot side inlet of the steam generator; the first inlet and the second inlet of the reflux buffer tank are respectively communicated with the liquid phase outlet of the flash tank and the hot side outlet of the steam generator, the outlet of the reflux buffer tank is divided into two paths, one path is used for refluxing the top of the tower, and the other path is used for discharging.
5. The rectification system of claim 4, comprising a vapor compressor having an inlet in communication with a cold side outlet of said vapor generator.
6. The rectification system of claim 4, wherein said rectification column is a tray column, said outlet and said return being disposed on a same tray of said tray column.
7. The rectification system of claim 4, wherein said throttling element is a throttle valve.
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| CN215756535U (en) * | 2021-10-11 | 2022-02-08 | 科富恺工艺设备(上海)有限公司 | Rectification system for recovering DMAC (dimethyl acetamide) from wastewater |
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| Publication number | Priority date | Publication date | Assignee | Title |
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