CN115006863A - 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
- Publication number
- CN115006863A CN115006863A CN202210701893.7A CN202210701893A CN115006863A CN 115006863 A CN115006863 A CN 115006863A CN 202210701893 A CN202210701893 A CN 202210701893A CN 115006863 A CN115006863 A CN 115006863A
- Authority
- CN
- China
- Prior art keywords
- tower
- rectification
- liquid
- inlet
- steam generator
- 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.)
- Granted
Links
- 238000000034 method Methods 0.000 title claims abstract description 32
- 238000009835 boiling Methods 0.000 title claims abstract description 22
- 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
- 238000007599 discharging Methods 0.000 claims abstract description 18
- 229920006395 saturated elastomer Polymers 0.000 claims abstract description 17
- 239000011555 saturated liquid Substances 0.000 claims abstract description 16
- 239000012071 phase Substances 0.000 claims abstract description 15
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 11
- 239000007788 liquid Substances 0.000 claims description 35
- 238000000926 separation method Methods 0.000 claims description 19
- 230000008016 vaporization Effects 0.000 claims description 7
- 239000000463 material Substances 0.000 claims description 5
- 238000010438 heat treatment Methods 0.000 claims description 2
- 238000011084 recovery Methods 0.000 claims description 2
- 238000001816 cooling Methods 0.000 abstract description 4
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 description 9
- 238000005265 energy consumption Methods 0.000 description 8
- 238000000605 extraction Methods 0.000 description 7
- 238000004364 calculation method Methods 0.000 description 5
- IEJIGPNLZYLLBP-UHFFFAOYSA-N dimethyl carbonate Chemical compound COC(=O)OC IEJIGPNLZYLLBP-UHFFFAOYSA-N 0.000 description 5
- KFZMGEQAYNKOFK-UHFFFAOYSA-N Isopropanol Chemical compound CC(C)O KFZMGEQAYNKOFK-UHFFFAOYSA-N 0.000 description 4
- MVPPADPHJFYWMZ-UHFFFAOYSA-N chlorobenzene Chemical compound ClC1=CC=CC=C1 MVPPADPHJFYWMZ-UHFFFAOYSA-N 0.000 description 4
- PXQFMBNNNYOFRN-UHFFFAOYSA-N chlorobenzene;propan-2-ol Chemical compound CC(C)O.ClC1=CC=CC=C1 PXQFMBNNNYOFRN-UHFFFAOYSA-N 0.000 description 4
- 230000008901 benefit Effects 0.000 description 3
- GUNDKLAGHABJDI-UHFFFAOYSA-N dimethyl carbonate;methanol Chemical compound OC.COC(=O)OC GUNDKLAGHABJDI-UHFFFAOYSA-N 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- 238000002309 gasification Methods 0.000 description 3
- 238000004088 simulation Methods 0.000 description 3
- 238000009834 vaporization Methods 0.000 description 3
- 238000010586 diagram Methods 0.000 description 2
- 238000004134 energy conservation Methods 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 239000002994 raw material Substances 0.000 description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- 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
- 238000004821 distillation Methods 0.000 description 1
Images
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
- B01D3/14—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
-
- 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
Landscapes
- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
Abstract
A rectification system and a rectification process for separating a wide boiling range binary mixture. The rectification process comprises the following steps: introducing the wide boiling range binary mixture into a rectifying tower, dividing light component saturated steam extracted from the top of the tower into two paths, introducing one path into a steam generator, introducing the other path into a side reboiler after the pressure and temperature of a top gas compressor are increased, 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 reboiled saturated liquid into the tower from the middle part of the tower, and discharging heavy components from a tower kettle; the compressed tower top gas is discharged at a bubble point after passing through a side reboiler, and is throttled and then introduced into a flash tank, the gas phase obtained from the flash tank is introduced into a tower top gas compressor or a steam generator to be used as a heat source, the obtained liquid phase and the liquid phase generated after heat exchange of the steam generator are introduced into a reflux buffer tank, part of condensate obtained from the reflux buffer tank flows back to the tower top, and the other part of condensate is taken as a tower top product to be extracted. The invention can reduce the consumption of tower top cooling circulating water and tower bottom steam in the rectification process, and is economical and energy-saving.
Description
Technical Field
The invention relates to a rectification technology, in particular to a rectification technology for separating a wide boiling range binary mixture.
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. Rectification is a main separation means, the economic advantages of traditional rectification in separation are seriously insufficient, the equipment cost and the operation cost are high, and the design of energy conservation and emission reduction is imperative under the background of double carbon.
In order to improve the energy-saving effect and 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 includes a rectification column T5, an overhead gas compressor C5, a column reboiler E5, a column reboiler E6, a liquid collection tank V5, a reflux buffer tank V6, a throttle valve V7, a condenser V8, a feed pump P5, a column withdrawal pump P6, a reflux pump P7, and the like.
The improved rectifying system is mainly used in a near-boiling system and an azeotropic system, the grade of the rectifying system is improved by compressing the top gas of the tower, and the rectifying system is used for reboiling and supplying heat to the tower kettle. Since the heat of the top of the tower and the heat of the bottom of the tower cannot be completely matched in most cases, a water cooler or an auxiliary reboiler/preheater or the like needs to be configured, so that the corresponding utility consumption is increased. In addition, in some wide boiling range systems, the pressure ratio which the compressor needs to bear in the traditional heat pump rectification is too large due to the overlarge temperature difference between the tower top and the tower bottom, so that the wide boiling range system is not suitable.
Disclosure of Invention
The invention aims to provide a rectification system and a rectification process for separating a wide boiling range binary mixture, which can reduce the consumption of cooling circulating water at the top of a tower and steam at the bottom of the tower in the rectification process of the wide boiling range binary mixture, reduce the consumption of public works and achieve the effects of economy and energy conservation.
According to an 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 a wide boiling range binary mixture into a rectifying tower from the middle part of the rectifying tower for rectification, dividing light component saturated steam extracted from the top of the tower into two paths, introducing one path of the light component saturated steam into a steam generator to be used as a heat source for vaporizing boiler feed water, introducing the other path of the light component saturated steam into a side reboiler after boosting and heating by a top gas compressor to be used as a heat source for carrying out heat exchange with saturated liquid extracted from the middle part of the rectifying tower, reboiling the saturated liquid and returning the saturated liquid into the rectifying tower from the middle part of the rectifying tower, 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 then introduced into a flash tank for gas-liquid separation, the gas phase obtained from the flash tank is introduced into a gas compressor at the top of the tower or introduced into the steam generator as a heat source, the liquid phase obtained from the flash tank and the liquid phase generated after heat exchange of the steam generator are introduced into a reflux buffer tank together, one part of condensate obtained from the reflux buffer tank flows to the top of the tower, and the other part of condensate is taken as a product at the top of the tower.
According to another aspect of the embodiments of the present invention, a rectification system for separating a wide boiling range binary mixture is provided, which comprises a rectification tower, an overhead gas compressor, a steam generator, a side reboiler, a kettle reboiler, a liquid collecting tank, a flash tank, a throttling element and a reflux buffer tank; the top gas phase outlet of the rectifying tower is respectively communicated with the gas inlet of a top gas compressor and the hot side inlet of a steam generator, the exhaust port of the top gas compressor is communicated with the hot side inlet of a side reboiler, the hot side outlet of the side reboiler is communicated with the inlet of a 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; a cold side inlet and a cold side outlet of the side reboiler are respectively communicated with a recovery port 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 a reboiler of the tower kettle, and the other path is used for discharging materials from the tower kettle; a cold side outlet of the tower kettle reboiler is communicated with a tower kettle steam inlet of the rectifying tower; the gas phase outlet of the flash tank is communicated with the gas inlet of the overhead 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 to exchange heat with the compressed tower top gas, intermediate reboiling is realized by using less compression work, the heat load of a reboiler at the tower bottom is greatly reduced, and the consumption of cooling circulating water at the tower top and steam at the tower bottom is saved, so that the aim of saving energy is fulfilled;
2. to the problem that the heat of rectifying column top and tower cauldron can not match completely, this embodiment replaces the auxiliary heat exchanger that needs to consume cold and hot public works among the traditional heat pump rectification flow with steam generator, passes through steam generator with the tower overhead gas that originally needs water-cooling and produces steam, and the steam that produces can be used as other heat transfer demands after the heat pump promotes the grade, reduces system energy consumption.
Drawings
Fig. 1 shows a schematic diagram of a prior art heat pump rectification system.
FIG. 2 shows a schematic of a rectification system for the separation of wide boiling range binary mixtures in accordance with an embodiment of the present invention.
Detailed Description
The invention is described in detail below with reference to the figures and specific embodiments.
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 tower T1, an overhead gas compressor C1, a side reboiler E1, a tower 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 tower extraction pump P2 and a reflux pump P3.
The wide boiling range described in the examples herein means a boiling range of 20 ℃ or higher.
The top gas phase outlet of the rectifying tower T1 is respectively communicated with a gas inlet of a top gas compressor C1 and a hot side inlet of a steam generator E3, a gas outlet of the top gas compressor C1 is communicated with the hot side inlet of a side reboiler E1, the hot side outlet of the side reboiler E1 is communicated with an inlet of a 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 port and a return port which are arranged in the middle of the rectifying tower T1.
In the present embodiment, the throttling element V4 is a throttle valve V4. The rectifying tower T1 is a plate tower, the extraction opening and the return opening are arranged on the same tower plate of the plate tower, and the tower plate is selected from a position where the temperature difference between the middle part of the tower and the top of the tower is small (the temperature difference is 10-20 ℃).
The liquid phase outlet of the tower bottom 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 discharging from the tower kettle through a tower kettle extraction pump P2; the cold side outlet of the tower reboiler E2 is communicated with the tower steam inlet of the rectifying tower T1. The hot side inlet of the column reboiler E2 is for receiving steam.
The gas phase outlet of the flash tank V2 is communicated with the gas inlet of an overhead gas compressor C1 or the hot side inlet of a 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 of the two paths flows through the reflux pump P3 to reflux the top of the rectifying tower T1, and the other path of the two paths is used for discharging.
Further, the rectification system of the embodiment of the invention comprises a steam compressor C2, wherein an air inlet of the steam compressor C2 is communicated with a cold side outlet of a steam generator E3, and the rectification system is used for compressing steam generated by the steam generator to realize pressure rise and temperature rise so as to improve the grade of the steam and serve as other heat exchange requirements.
A rectification process for the separation of a wide boiling range binary mixture according to an embodiment of the invention comprises the following steps:
introducing the wide boiling range binary mixture 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 top of the tower into two paths, introducing one path into a steam generator E3 to serve as a heat source to vaporize boiler feed water, introducing the other path into a side reboiler E1 after being subjected to pressure rise and temperature rise through a top gas compressor C1, performing heat exchange with saturated liquid extracted from the middle part of the tower as the heat source, returning the saturated liquid into the rectifying tower T1 from the same position of the middle part of the tower after being reboiled, and discharging the recombined component from the bottom of the tower after being reboiled and concentrated;
introducing condensed liquid obtained from a side reboiler E1 into a liquid collecting tank V1, discharging non-condensable gas from the top of a liquid collecting tank V1 into a steam generator E3, throttling the condensate in the liquid collecting tank V1 and then introducing the condensate into a flash tank V2 for gas-liquid separation, introducing a gas phase obtained from a flash tank V2 into a tower top gas compressor C1 or introducing the gas phase into the steam generator E3 as a heat source, introducing a liquid phase obtained from a flash tank V2 and a liquid phase generated after heat exchange of the steam generator E3 into a reflux buffer tank V3, and refluxing a part of the condensate obtained from the reflux buffer tank V3 to the tower top according to a certain reflux ratio, and extracting the other part of the condensate as a tower top product.
In this embodiment, the temperature difference between the light component saturated vapor after being boosted in pressure and heated by the overhead gas compressor and the saturated liquid extracted from the middle of the rectifying tower is 10 ℃ to 20 ℃. According to the gasification rate of 20 percent, compressed tower top gas passes through a side reboiler E1 and then is discharged into a liquid collecting tank V1 in a bubble point mode, liquid phase obtained from the liquid collecting tank V1 is decompressed to the pressure of the tower top 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 (when the compressed tower top gas is not enough to supply heat to the side reboiler) or boiler water is vaporized through a steam generator E3, the grade of the generated saturated steam is improved through a steam heat pump to be used as other heat exchange requirements, the whole flow energy-saving effect is remarkable, and the consumption of a tower kettle heat utility project and a tower top cold utility project is greatly reduced. The vapor heat pump described above employs a vapor compressor C2 in this embodiment.
The following takes the rectification process of the isopropanol-chlorobenzene and methanol-dimethyl carbonate system as an example to further explain the technical scheme of the invention, and the superiority of the side-line heat pump rectification process of the embodiment of the invention is illustrated by comparing the energy consumption and the operation cost of the traditional direct rectification and traditional heat pump rectification processes.
Application example 1
The following description will be made by taking the calculation simulation result of the side-stream heat pump distillation process flow of isopropanol-chlorobenzene separation as an example, referring to fig. 2, and the specific conditions are shown in table 1.
TABLE 1 Isopropanol-chlorobenzene separation Process conditions
The process flow is described as follows:
1-1, as shown in fig. 2, feeding an isopropanol-chlorobenzene mixed raw material into a rectifying tower T1 through a feed pump P1 at a feeding rate of 5000kg/h, extracting isopropanol (82 ℃, 1500kg/h, and the concentration of isopropanol is 99.9 wt.%) as a light component from the top of the tower, and discharging chlorobenzene (130 ℃, 3500kg/h, and the concentration of chlorobenzene is 99.9 wt.%) as a heavy component from the bottom of the tower;
1-2, compressing tower top saturated steam to 510kPa by a tower top gas compressor C1 to be used as hot stream, exchanging heat with saturated liquid (with the temperature difference of 20 ℃) extracted from the middle side line of a rectifying tower T1 in a side reboiler E1, discharging cold stream from an extraction tower plate to return to the tower at a gasification rate of 20%, discharging hot stream after heat exchange at a bubble point to enter a liquid collection tank V1, then decompressing to 101.325kPa by a throttle valve V4, performing gas-liquid separation in a flash tank V2 after partial vaporization, returning the steam to an air inlet of a tower top gas compressor C1, and providing enough heat for side line reboiling after recompression;
1-3, vaporizing boiler feed water by a small amount of residual overhead gas through a steam generator E3, and increasing the grade (300kPa, 150 ℃) of the generated saturated steam (40kPa, 76 ℃) through a steam compressor C2 to be used as other heat exchange requirements; the condensed liquid phase and the liquid phase separated from the flash tank V2 are merged into a reflux buffer tank V3, and overhead reflux and extraction are carried out according to the reflux ratio of 2.78.
In order to compare the design energy consumption of the traditional direct rectification, the traditional heat pump rectification (as shown in figure 1) and the heat pump rectification process, the feeding and separation indexes adopted in the calculation of each process are completely the same, ASPEN PLUS is adopted for process simulation, the efficiency of a compressor is calculated according to 80%, the public engineering specification is shown in table 2, and the energy consumption calculation result of each process is shown in table 3.
TABLE 2 Utility Specifications
TABLE 3 comparison of Process energy consumption and Utility consumption (hourly unit time)
And (3) comparing the results: the annual operating cost of each process is calculated by combining the table 2 and the table 3, the same separation requirement is achieved under the same feeding condition, and the energy-saving process (110 ten thousand yuan/year) of the side-line heat pump rectification in the application example 1 saves the operating cost by 58.8 percent per year compared with the traditional direct rectification (267 ten thousand yuan/year) and saves the operating cost by 35.7 percent per year compared with the traditional heat pump rectification (171 ten thousand yuan/year).
Application example 2
Referring to fig. 2, a side-stream heat pump rectification process flow calculation simulation result of methanol-dimethyl carbonate separation 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 (1350kPa, bubble point feeding, with the composition of 50 wt.% and 50 wt.%, respectively) into a rectifying tower T1 through a feeding pump P1 at a feeding rate of 5000kg/h, collecting methanol and dimethyl carbonate azeotrope (147.27 ℃, 1300kPa, methanol: dimethyl carbonate: 90.9 wt.% and 9.1 wt.%) as a light component from the top of the tower (147.27 ℃, 1300kPa, 2813.6kg/h, methanol: 88.8 wt.%, dimethyl carbonate: 11.2 wt.%), and discharging dimethyl carbonate as a heavy component from the bottom of the tower (199.4 ℃, 1350kPa, 2186.4kg/h, and the concentration of dimethyl carbonate is 99.99 wt.%);
2-2, compressing tower top saturated steam to 3000kPa by a compressor C1 to serve as hot stream, exchanging heat with saturated liquid (20 ℃ of temperature difference with the tower top) extracted from the middle side line of a rectifying tower T1 in a side reboiler E1, discharging cold stream at a gasification rate of 20% from an extraction tower plate to return to the tower, discharging the heat stream after heat exchange at a bubble point to enter a liquid collection tank V1, then reducing the pressure to 1300kPa by a throttle valve V4, performing gas-liquid separation in a flash tank V2 after partial vaporization, and merging the separated steam and a small amount of residual tower top gas into one stream to enter a steam generator E3;
2-3, vaporizing boiler feed water by utilizing latent heat of tower top saturated steam in a steam generator E3, and using the generated saturated steam (400kPa, 144 ℃) as other heat exchange requirements after the grade (2500kPa, 220 ℃) is improved by a steam compressor C2; the condensed liquid phase and the liquid phase separated from the flash tank V2 are merged into a reflux buffer tank V3, and the overhead reflux and extraction are carried out according to the reflux ratio of 5.1.
The energy consumption calculation results of each process in this example are shown in table 4.
TABLE 4 comparison of energy consumption of the processes and of the utilities (hours per unit time)
And (3) comparing the results: the annual operation cost of each process is calculated by combining the tables 2 and 4, the same separation requirement is achieved under the same feeding condition, and the energy-saving process of the side-line heat pump rectification (273 ten thousand yuan/year) saves the operation cost by 75.8 percent every year compared with the traditional direct rectification (1126 ten thousand yuan/year) and saves the operation cost by 60.4 percent every year compared with the traditional heat pump rectification (690 ten thousand yuan/year).
The rectification system and the rectification process of the embodiment of the invention realize zero consumption of steam and circulating water and even rich steam production by using a small amount of power consumption.
Claims (7)
1. A rectification process for the separation of wide boiling range binary mixtures comprising the steps of:
introducing a wide boiling range binary mixture into a rectifying tower from the middle part of the rectifying tower for rectification, dividing light component saturated steam extracted from the top of the tower into two paths, introducing one path of the light component saturated steam into a steam generator to be used as a heat source for vaporizing boiler feed water, introducing the other path of the light component saturated steam into a side reboiler after boosting and heating by a top gas compressor to be used as a heat source for carrying out heat exchange with saturated liquid extracted from the middle part of the rectifying tower, reboiling the saturated liquid and returning the saturated liquid into the rectifying tower from the middle part of the rectifying tower, and discharging heavy components from a tower kettle;
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 liquid phase into a flash tank, performing gas-liquid separation, introducing a gas phase obtained from the flash tank into a gas compressor at the top of the tower or introducing the gas phase into the steam generator as a heat source, introducing a liquid phase obtained from the flash tank and a liquid phase generated after heat exchange of the steam generator into a reflux buffer tank, and refluxing a part of condensate obtained from the reflux buffer tank to the top of the tower while taking the other part of condensate as a product at the top of the tower.
2. The rectification process according to claim 1, wherein saturated steam generated by the steam generator is upgraded by a steam heat pump.
3. The rectification process according to claim 1, wherein the temperature difference between the light component saturated vapor after being boosted in pressure and heated by the overhead gas compressor and the saturated liquid extracted from the middle part of the rectification column is 10 ℃ to 20 ℃.
4. A rectification system for separating a wide boiling range binary mixture is characterized by comprising a rectification tower, a tower top 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 top gas phase outlet 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; a cold side inlet and a cold side outlet of the side reboiler are respectively communicated with a recovery port 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 used for discharging materials from the tower kettle; a cold side outlet of the tower kettle reboiler is communicated with a tower kettle steam inlet of the rectifying tower;
the gas phase outlet of the flash tank is communicated with the gas inlet of the overhead 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.
5. The rectification system of claim 4, comprising a vapor compressor having an inlet in communication with the cold side outlet of the vapor generator.
6. The rectification system of claim 4, wherein the rectification column is a tray column, and the withdrawal port and the return port are disposed on the same tray of the tray column.
7. The rectification system as claimed in claim 4, wherein said throttling element is a throttle valve.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202210701893.7A CN115006863B (en) | 2022-06-20 | Rectification system and rectification process for separating wide boiling range binary mixture |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202210701893.7A CN115006863B (en) | 2022-06-20 | Rectification system and rectification process for separating wide boiling range binary mixture |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN115006863A true CN115006863A (en) | 2022-09-06 |
| CN115006863B CN115006863B (en) | 2024-10-22 |
Family
ID=
Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4357153A (en) * | 1981-03-30 | 1982-11-02 | Erickson Donald C | Internally heat pumped single pressure distillative separations |
| CN101854988A (en) * | 2007-11-09 | 2010-10-06 | 环球油品有限责任公司 | Separator with multi-stage heat pump compressor and intermediate reboiler |
| CN102451572A (en) * | 2010-11-03 | 2012-05-16 | 中国石油化工股份有限公司 | Method for separating acetic acid from water by rectification of acetic acid dehydrating tower |
| CN107137949A (en) * | 2017-07-11 | 2017-09-08 | 河北工业大学 | A kind of extracting rectifying partitioned column device and method of low concentration aqueous isopropanol dehydration |
| CN111302922A (en) * | 2020-03-27 | 2020-06-19 | 北京诺维新材科技有限公司 | Rectification separation method and rectification system |
| CN111635293A (en) * | 2020-05-14 | 2020-09-08 | 天津市汇筑恒升科技有限公司 | Sodium methoxide production device and method |
| 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 |
Patent Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4357153A (en) * | 1981-03-30 | 1982-11-02 | Erickson Donald C | Internally heat pumped single pressure distillative separations |
| CN101854988A (en) * | 2007-11-09 | 2010-10-06 | 环球油品有限责任公司 | Separator with multi-stage heat pump compressor and intermediate reboiler |
| CN102451572A (en) * | 2010-11-03 | 2012-05-16 | 中国石油化工股份有限公司 | Method for separating acetic acid from water by rectification of acetic acid dehydrating tower |
| CN107137949A (en) * | 2017-07-11 | 2017-09-08 | 河北工业大学 | A kind of extracting rectifying partitioned column device and method of low concentration aqueous isopropanol dehydration |
| CN111302922A (en) * | 2020-03-27 | 2020-06-19 | 北京诺维新材科技有限公司 | Rectification separation method and rectification system |
| CN111635293A (en) * | 2020-05-14 | 2020-09-08 | 天津市汇筑恒升科技有限公司 | Sodium methoxide production device and method |
| 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 |
Non-Patent Citations (4)
| Title |
|---|
| 丁良辉 等: "基于中间再沸器的氯化苄热泵精馏工艺模拟", 化学工程, vol. 44, no. 01, 15 January 2016 (2016-01-15), pages 23 - 27 * |
| 李沐荣 等: "热泵精馏隔壁塔分离宽沸程物系的模拟", 化工学报, vol. 68, no. 05, 31 May 2017 (2017-05-31), pages 1906 - 1911 * |
| 杨德明 等: "带中间再沸器的大温差体系热泵精馏工艺", 化学工程, vol. 45, no. 01, 15 January 2017 (2017-01-15), pages 1 - 4 * |
| 高晓新 等: "中间再沸式MVR热泵精馏回收处理二甲基乙酰胺稀溶液", 现代化工, vol. 33, no. 08, 20 August 2013 (2013-08-20), pages 114 - 116 * |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN104105531B (en) | Adopt method and the complete set of equipments of the distillating carbinol of heat recovery | |
| CN104788289B (en) | A kind of pump coupled heat technique of ethylene glycol rectifying | |
| CN101874935B (en) | Rectifying section tower bottom reboiling internal heat-integrated energy-saving rectifying apparatus and method | |
| CN112266799B (en) | Delayed coking method for realizing energy consumption reduction of absorption stabilization system | |
| CN101195561B (en) | Method for producing dimethyl ether with methanol gas-phase dehydration | |
| CN111116317A (en) | Five-tower four-effect methanol rectification process and equipment | |
| CN115317945B (en) | Two-tower thermal coupling and heat pump combined separation process and separation device for alkylation reaction product | |
| CN112179048B (en) | Co-production system and method for recycling and extracting helium from light hydrocarbon of helium-poor natural gas | |
| CN110256202A (en) | A kind of refining crude methanol process of four towers quadruple effect | |
| CN105237370A (en) | Method for producing cyclohexanone by cyclohexanol dehydrogenation | |
| CN101874934A (en) | Flash evaporation feed type internal heat integration energy-saving rectifying device and method | |
| CN104093464A (en) | Process and plant for distillation of methanol with heat recovery | |
| CN111187140A (en) | Energy-saving method and device for deisobutanizer | |
| CN109646980B (en) | Fusel-free oil dividing wall tower coupled methanol multi-effect rectification energy-saving device and method | |
| CN103585777B (en) | Utilization method for waste heat and excess pressure of gas fractionation apparatus | |
| CN104593057B (en) | A kind of delayed coking unit of low energy consumption | |
| CN115006863B (en) | Rectification system and rectification process for separating wide boiling range binary mixture | |
| CN115006863A (en) | Rectification system and rectification process for separating wide boiling range binary mixture | |
| CN107488104B (en) | Energy-saving rectifying system and energy-saving rectifying method for purifying fusel oil | |
| CN107541235B (en) | Two-stage condensation and separation method and separation system for oil gas at tower top of crude oil atmospheric distillation tower | |
| CN212269940U (en) | Methanol heat pump rectifying device | |
| CN115430166B (en) | Process system and method for steam driven heat pump auxiliary bulkhead tower | |
| CN221412268U (en) | NMP waste liquid recovery system | |
| CN212076901U (en) | Cogeneration device of superior edible alcohol and absolute ethyl alcohol | |
| CN116059675B (en) | Method and device for desorbing carbon II from absorbent rich liquid by differential pressure type rectification |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| CB02 | Change of applicant information |
Country or region after: China Address after: 201108 Shanghai city Minhang District Huaning Road No. 3111 Applicant after: Shanghai Qiyao Energy saving Technology Co.,Ltd. Address before: 201108 Shanghai city Minhang District Huaning Road No. 3111 Applicant before: SHANGHAI QIYAO EXPANDER Co.,Ltd. Country or region before: China |
|
| CB02 | Change of applicant information | ||
| GR01 | Patent grant |