CN216170035U - Rectifying device - Google Patents
Rectifying device Download PDFInfo
- Publication number
- CN216170035U CN216170035U CN202122497320.0U CN202122497320U CN216170035U CN 216170035 U CN216170035 U CN 216170035U CN 202122497320 U CN202122497320 U CN 202122497320U CN 216170035 U CN216170035 U CN 216170035U
- Authority
- CN
- China
- Prior art keywords
- tower
- preheater
- outlet
- pressure
- kettle
- 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.)
- Active
Links
Images
Landscapes
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
Abstract
The utility model discloses a rectifying device. The structure of the rectifying device is as follows: the raw material feeding port is sequentially connected with the first preheater and the first feeding port; the outlet of the first tower top is connected with a second preheater, a third preheater and a second feed inlet in sequence; the outlet of the first tower kettle is connected with a second preheater, a first preheater and a first heavy component outlet in sequence; the outlet of the second tower top is sequentially connected with the first tower kettle reboiler and the first reflux port; the outlet of the second tower kettle is connected with a third preheater and a second heavy component outlet in sequence. The rectifying device combines the heat exchange network optimization, fully recovers system waste heat, realizes that the heat exchange network has no pinch point phenomenon, reduces operation energy consumption, reduces carbon emission, and meets the production requirement of the rectifying process.
Description
Technical Field
The utility model relates to a rectifying device.
Background
For azeotropic systems, conventional fractionation methods are difficult to separate. Although both extractive distillation and azeotropic distillation can separate an azeotropic system, an extracting agent or an entrainer is additionally introduced, which affects secondary use, and secondary pollution is caused if the using amount is large.
For the pressure sensitive azeotropic system, the separation can be carried out by adopting a pressure swing rectification mode. The main energy consumption of pressure swing distillation is steam or hot oil in a reboiler at the bottom of a tower, particularly a high-pressure tower, and the grade and the using amount of energy are high due to high temperature and a product tower, and a patent (CN 108704330A) discloses a low-energy-consumption pressure swing distillation device which is only used for conventional waste heat utilization, does not perform pinch point optimization on the distillation device, does not recycle heat to the maximum extent, and is unreasonable in the heat exchange process in the prior art, so that part of heat is lost in the heat transfer process, and the energy consumption of public engineering is increased finally.
SUMMERY OF THE UTILITY MODEL
The utility model aims to solve the technical problems that the optimization of pinch points is not considered and the heat exchange flow is unreasonable in the prior art, and provides a rectifying device which is combined with the optimization of a heat exchange network, fully recovers the waste heat of a system, realizes that the heat exchange network has no cross pinch point phenomenon, realizes the maximization of heat recovery utilization, reduces the energy consumption of public works and the energy consumption of operation, reduces carbon emission and meets the production requirement of a rectifying process.
The utility model solves the technical problems through the following technical scheme:
the utility model provides a rectification device, comprising: the system comprises a raw material feeding port, a first heavy component outlet, a low-pressure tower, a high-pressure tower, a first preheater, a second preheater, a third preheater and a second heavy component outlet.
The low-pressure tower is provided with a first feed inlet, a first tower kettle reboiler, a first reflux opening, a first tower top outlet and a first tower kettle outlet;
the high-pressure tower is provided with a second feed inlet, a second tower top outlet and a second tower kettle outlet;
the raw material feeding hole is sequentially connected with the first preheater and the first feeding hole; the outlet of the first tower top is sequentially connected with the second preheater, the third preheater and the second feed inlet; the outlet of the first tower kettle is sequentially connected with the second preheater, the first preheater and the first heavy component outlet;
the second tower top outlet is connected with the first tower kettle reboiler and the first reflux port in sequence; and the outlet of the second tower kettle is sequentially connected with the third preheater and the second heavy component outlet.
In the present invention, preferably, the low pressure column is further provided with a first loop which sequentially flows back to the column bottom of the low pressure column through the first column bottom outlet and the first column bottom reboiler; the low-pressure tower is also provided with a second loop which sequentially flows back to the tower kettle of the low-pressure tower through the outlet of the first tower kettle and a reboiler of a second tower kettle.
Wherein, more preferably, the raw material feeding port is respectively merged and connected with the first preheater through a fourth preheater and a fifth preheater; the fourth preheater, an overhead condenser and a booster pump are also arranged between the first overhead outlet and the second preheater; and the fifth preheater is arranged between the first preheater and the first heavy component outlet.
Wherein, further preferably, the low-pressure tower is further provided with a third loop which sequentially passes through the first tower top outlet, the fourth preheater and the tower top condenser and then flows back to the tower top of the low-pressure tower.
In the present invention, preferably, the high pressure column is further provided with a fourth loop which flows back to the top of the high pressure column through the second top outlet and the first kettle reboiler; the high pressure tower is also provided with a fifth loop which flows back to the low pressure tower through the second tower top outlet and the first tower kettle reboiler.
In the present invention, preferably, the high pressure column is further provided with a sixth loop which flows back to the column bottom of the high pressure column through the outlet of the second column bottom and a reboiler of a third column bottom.
In the present invention, it is preferable that the theoretical plate number of the low pressure column is 10 to 40, and it is more preferable that the theoretical plate number of the low pressure column is 15.
In the present invention, the theoretical plate number of the high pressure column is preferably 10 to 40, and more preferably 10.
The positive progress effects of the utility model are as follows:
1) when the rectifying device is adopted, the temperature of the top of the high-pressure tower rises by improving the pressure of the high-pressure tower, so that the heat transfer driving force of the heated material at the bottom of the low-pressure tower is increased, the heat exchange area of a reboiler at the bottom of the tower is reduced, the retention time can be reduced for a thermosensitive system, the pressure drop can be reduced, the gasification temperature after heating is reduced, and the problems of coking, polymerization, denaturation and the like are avoided.
2) The heat exchange network is optimized through a pinch point technology, the waste heat of the system is fully utilized, and meanwhile, the heat loss is reduced, the heat utilization rate is improved, the heat is recycled to the maximum extent, the energy consumption of the rectifying device is reduced, and the carbon emission is reduced.
3) The heat exchange system is reasonable in design, and energy consumption of public works and operation energy consumption are reduced.
Drawings
Fig. 1 is a schematic view of a rectifying apparatus in example 1 of the present application.
The reference numerals are explained below:
low-pressure column 1
Fourth preheater 3
First preheater 5
Reboiler 6 of second tower kettle
First column reboiler 7
Overhead condenser 8
Pressure pump 9
Third preheater 11
A first heavy fraction outlet 13
Feed inlet 14
Second heavy fraction outlet 15
Detailed Description
The utility model is further illustrated by the following examples, which are not intended to limit the scope of the utility model. The experimental methods without specifying specific conditions in the following examples were selected according to the conventional methods and conditions, or according to the commercial instructions.
Example 1
As shown in fig. 1, the rectifying apparatus includes: a raw material inlet 14, a first heavy component outlet 13, a low-pressure tower 1, a high-pressure tower 2, a first preheater 5, a second preheater 10, a third preheater 11 and a second heavy component outlet 15; the low-pressure tower 1 is provided with a first feed inlet, a first tower kettle reboiler 7, a first reflux opening, a first tower top outlet and a first tower kettle outlet; the high pressure tower 2 is provided with a second feed inlet, a second tower top outlet and a second tower kettle outlet.
The raw material feeding port is respectively combined and connected with the first preheater 5 through the fourth preheater 3 and the fifth preheater 4, and then is connected with the first feeding port; the outlet of the first tower top is connected with a fourth preheater 3, a tower top condenser 8, a booster pump 9, a second preheater 10, a third preheater 11 and a second feed inlet in sequence; the outlet of the first tower kettle is connected with a second preheater 10, a first preheater 5, a fifth preheater 4 and a first heavy component outlet 13 in sequence; the outlet of the second tower top is connected with a first tower kettle reboiler 7 and a first reflux port in sequence; the outlet of the second tower kettle is connected with a third preheater 11 and a second heavy component outlet 15 in sequence.
The low-pressure tower 1 is provided with a first loop which sequentially flows back to the tower kettle of the low-pressure tower 1 through a first tower kettle outlet and a first tower kettle reboiler 7; the low-pressure tower 1 is also provided with a second loop which sequentially flows back to the tower kettle of the low-pressure tower 1 through the outlet of the first tower kettle and a reboiler 6 of the second tower kettle; the low-pressure tower 1 is also provided with a third loop which sequentially flows back to the top of the low-pressure tower 1 through a first top outlet, a fourth preheater 3 and a top condenser 8.
The high pressure tower 2 is provided with a fourth loop which flows back to the top of the high pressure tower 2 through a second tower top outlet and a first tower kettle reboiler 7; the high pressure tower 2 is also provided with a fifth loop which flows back to the low pressure tower 1 through a second tower top outlet and a first tower kettle reboiler 7; the high pressure tower 2 is also provided with a sixth loop which flows back to the tower kettle of the high pressure tower 2 through the outlet of the second tower kettle and a reboiler 12 of the third tower kettle.
The ascending vapor phase at the top of the low-pressure tower 1 and the material at the bottom of the low-pressure tower 1 are used as heat sources for heating the feeding of the low-pressure tower 1, so that the heat is recovered, and the energy consumption of rectification is reduced. The gas phase at the top of the high-pressure tower 2 is used as a heat source of a reboiler of the low-pressure tower 1, and the material at the bottom of the high-pressure tower 2 is used for heating the feed material of the high-pressure tower 2.
In this example 1, the tetrahydrofuran-water containing feedstock was: the tetrahydrofuran content is 6 percent, and the balance is water, and the materials are fed at normal pressure and normal temperature.
Tetrahydrofuran-water is divided into two feed streams, one feed stream enters a fourth preheater 3, the other feed stream enters a fifth preheater 4, after primary preheating, the two feed streams coming out of the fourth preheater 3 and the fifth preheater 4 enter a first preheater 5, the preheated feed stream enters a 5 th theoretical plate of a low-pressure tower 1 and enters the tower for rectification, the operating reflux ratio of the top of the low-pressure tower 1 is 1, the number of theoretical plates is 15, the operating pressure of the tower is 101kPa, the temperature of a tower kettle is 102 ℃, and the temperature of the top of the tower is 63 ℃. One strand of tower bottom liquid of the low-pressure tower 1 enters a first tower bottom reboiler 7 to reflux, and the other strand of tower bottom liquid sequentially passes through a second preheater 10, a first preheater 5, a fifth preheater 4 and a first heavy component outlet 13 to obtain a first heavy component product, namely water. The overhead gas of the low-pressure tower 1 sequentially passes through a fourth preheater 3 and a tower top condenser 8; one part of the condensed material enters the top of the low-pressure tower 1, the other part of the condensed material passes through a second preheater 10 and a third preheater 11 in sequence through a pressure pump 9, the material exchanges heat with the tower kettle material of the low-pressure tower 1 and the tower kettle material of the high-pressure tower 2 to 130 ℃, then enters a 10 th theoretical plate of the high-pressure tower 2 and enters the tower for rectification, the operating reflux ratio of the top of the high-pressure tower 2 is 1, the number of the theoretical plates is 30, the operating pressure of the tower is 700kPa, the temperature of the tower kettle is 141 ℃, and the temperature of the top of the tower is 129 ℃. A part of the tower bottom liquid of the high-pressure tower 2 enters a third tower bottom reboiler 12, and the other part of the tower bottom liquid passes through a third preheater 11 and a second heavy component outlet 15 to obtain a second heavy component product, namely tetrahydrofuran; the overhead gas of the high pressure tower 2 enters a first reboiler, one part of the heat-exchanged material enters the low pressure tower 1, and the other part of the heat-exchanged material enters the top of the high pressure tower 2.
After rectification treatment, the concentration of the water extracted from the first heavy component outlet and the concentration of the tetrahydrofuran product extracted from the second heavy component outlet are both over 99.9 percent, and the recovery rate of the tetrahydrofuran is close to 100 percent.
According to the rectifying apparatus of the present embodiment 1, data of the target amount of each utility is obtained without considering the pinch point and the system
The prior art of waste heat utilization separates azeotropes to obtain data on actual quantities of various utilities, as shown in table 1 below:
TABLE 1 Utility energy usage and carbon emissions
| General public works | Heating utilities | Cooling utilities | Carbon emissions | |
| Actual quantity | 14688kW | 5457kW | 9231kW | 1292kW |
| Target volume | 7382kW | 1804kW | 5578kW | 427kW |
| Reduction of | 7306kW | 3653kW | 3653kW | 865kW |
| Rate of reduction | 49.74％ | 66.94％ | 39.58％ | 66.95％ |
As can be seen from the table, the total public engineering energy of 7306kW can be reduced by adopting the rectifying device; wherein heating utility energy can be reduced by 66.94% (3653kW) and cooling utility energy can be reduced by 39.58% (3653 kW). Accordingly, carbon emissions may also be reduced by 66.95% (865 kW).
The statements in this specification merely set forth a list of implementations of the inventive concepts, and the scope of the present disclosure should not be construed as limited to the particular forms set forth in the examples.
Claims (8)
1. A rectification apparatus, comprising: the system comprises a raw material feeding port, a first heavy component outlet, a low-pressure tower, a high-pressure tower, a first preheater, a second preheater, a third preheater and a second heavy component outlet;
the low-pressure tower is provided with a first feed inlet, a first tower kettle reboiler, a first reflux opening, a first tower top outlet and a first tower kettle outlet;
the high-pressure tower is provided with a second feed inlet, a second tower top outlet and a second tower kettle outlet;
the raw material feeding hole is sequentially connected with the first preheater and the first feeding hole; the outlet of the first tower top is sequentially connected with the second preheater, the third preheater and the second feed inlet; the outlet of the first tower kettle is sequentially connected with the second preheater, the first preheater and the first heavy component outlet;
the second tower top outlet is connected with the first tower kettle reboiler and the first reflux port in sequence; and the outlet of the second tower kettle is sequentially connected with the third preheater and the second heavy component outlet.
2. Rectification apparatus as claimed in claim 1,
the low-pressure tower is also provided with a first loop which sequentially flows back to the tower kettle of the low-pressure tower through the outlet of the first tower kettle and the reboiler of the first tower kettle;
the low-pressure tower is also provided with a second loop which sequentially flows back to the tower kettle of the low-pressure tower through the outlet of the first tower kettle and a reboiler of a second tower kettle.
3. Rectification unit as claimed in claim 2,
the raw material feeding port is combined and connected with the first preheater through a fourth preheater and a fifth preheater respectively;
the fourth preheater, an overhead condenser and a booster pump are also arranged between the first overhead outlet and the second preheater;
and the fifth preheater is arranged between the first preheater and the first heavy component outlet.
4. Rectification apparatus as claimed in claim 3,
the low-pressure tower is also provided with a third loop which sequentially passes through the first tower top outlet, the fourth preheater and the tower top condenser and flows back to the tower top of the low-pressure tower.
5. Rectification apparatus as claimed in claim 1,
the high-pressure tower is also provided with a fourth loop which flows back to the top of the high-pressure tower through the second tower top outlet and the first tower kettle reboiler;
the high-pressure tower is also provided with a fifth loop which flows back to the middle part of the low-pressure tower through the second tower top outlet and the first tower kettle reboiler.
6. Rectification apparatus as claimed in claim 1,
the high-pressure tower is also provided with a sixth loop which flows back to the tower kettle of the high-pressure tower through the outlet of the second tower kettle and a reboiler of a third tower kettle.
7. The rectification apparatus of claim 1 wherein the theoretical plate count of the lower pressure column is 10 to 40;
and/or the theoretical plate number of the high-pressure tower is 10-40.
8. The rectification apparatus of claim 7 wherein the theoretical plate count of the lower pressure column is 15;
and/or the theoretical plate number of the high-pressure tower is 10.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202122497320.0U CN216170035U (en) | 2021-10-15 | 2021-10-15 | Rectifying device |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202122497320.0U CN216170035U (en) | 2021-10-15 | 2021-10-15 | Rectifying device |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN216170035U true CN216170035U (en) | 2022-04-05 |
Family
ID=80883049
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202122497320.0U Active CN216170035U (en) | 2021-10-15 | 2021-10-15 | Rectifying device |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN216170035U (en) |
-
2021
- 2021-10-15 CN CN202122497320.0U patent/CN216170035U/en active Active
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN108101748B (en) | Four-tower three-effect methanol rectification energy-saving process method and device | |
| CN101874935B (en) | Rectifying section tower bottom reboiling internal heat-integrated energy-saving rectifying apparatus and method | |
| CN108558603B (en) | Three-tower three-effect crude methanol refining process method | |
| CN114031580B (en) | Refining device and refining method for low-energy PBAT byproduct tetrahydrofuran | |
| CN110327647A (en) | A kind of refining crude methanol process of three tower triple effect of modified | |
| CN110256202A (en) | A kind of refining crude methanol process of four towers quadruple effect | |
| CN101874934A (en) | Flash evaporation feed type internal heat integration energy-saving rectifying device and method | |
| CN113877227B (en) | Styrene refining method for providing heat source required by separation tower through combination of falling film reboiler and heat pump technology | |
| CN102675029A (en) | Method for separating methylcyclohexane and toluene through differential pressure thermal coupling extractive rectification | |
| CN116116030A (en) | Energy-saving and emission-reducing system for chemical separation and purification process | |
| CN109646980B (en) | Fusel-free oil dividing wall tower coupled methanol multi-effect rectification energy-saving device and method | |
| CN101966398A (en) | Energy-saving distillation method and device through differential pressure column section heat integration in rectification column sequences | |
| CN216170035U (en) | Rectifying device | |
| CN101966397B (en) | Energy-saving rectifying device for integrating energy in rectifying tower sequence and method | |
| CN109675332B (en) | Toluene column fractionation device and method driven by heat pump | |
| CN115970315A (en) | Rectification device and azeotrope separation method | |
| CN213760551U (en) | 1-butene refining energy-saving device with heat pump heat integration | |
| CN213760550U (en) | Two-tower double-heat-pump integrated 1-butene refining energy-saving device | |
| CN210314061U (en) | Rectification and purification device for synthesizing dimethyl oxalate by carbonylation of coal-made ethylene glycol | |
| CN203196360U (en) | Manufacturing device of acraldehyde | |
| CN208292896U (en) | The methanol recovery device of methyl tertiary butyl ether(MTBE) production | |
| CN101792679B (en) | Energy-saving method for vaporizing feed of propylene depolymerization oil tower by stepped utilization of low-temperature wastewater and device thereof | |
| CN217973033U (en) | Device for preparing cyclohexanol and coproducing cyclohexanone by cyclohexene method | |
| CN220194017U (en) | Crude methanol three-tower three-effect heat pump refining process device | |
| CN216536961U (en) | Thermal coupling methanol rectifying device of side line and bulkhead recovery tower |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| GR01 | Patent grant | ||
| GR01 | Patent grant |