CN115888158A - Coupling rectification separation system and coupling rectification separation method - Google Patents
Coupling rectification separation system and coupling rectification separation method Download PDFInfo
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- CN115888158A CN115888158A CN202211510386.1A CN202211510386A CN115888158A CN 115888158 A CN115888158 A CN 115888158A CN 202211510386 A CN202211510386 A CN 202211510386A CN 115888158 A CN115888158 A CN 115888158A
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- 238000000926 separation method Methods 0.000 title claims abstract description 55
- 230000008878 coupling Effects 0.000 title claims abstract description 30
- 238000010168 coupling process Methods 0.000 title claims abstract description 30
- 238000005859 coupling reaction Methods 0.000 title claims abstract description 30
- 238000010992 reflux Methods 0.000 claims abstract description 100
- 239000007789 gas Substances 0.000 claims description 59
- 239000012071 phase Substances 0.000 claims description 54
- 239000007791 liquid phase Substances 0.000 claims description 41
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 30
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims description 22
- 239000001257 hydrogen Substances 0.000 claims description 22
- 229910052739 hydrogen Inorganic materials 0.000 claims description 22
- 238000005194 fractionation Methods 0.000 claims description 13
- 229910052757 nitrogen Inorganic materials 0.000 claims description 11
- 238000004891 communication Methods 0.000 claims description 7
- 238000000034 method Methods 0.000 claims description 5
- 239000007788 liquid Substances 0.000 description 13
- 239000002994 raw material Substances 0.000 description 11
- 238000004821 distillation Methods 0.000 description 10
- 229910001873 dinitrogen Inorganic materials 0.000 description 8
- 239000000126 substance Substances 0.000 description 8
- 239000005046 Chlorosilane Substances 0.000 description 6
- KOPOQZFJUQMUML-UHFFFAOYSA-N chlorosilane Chemical compound Cl[SiH3] KOPOQZFJUQMUML-UHFFFAOYSA-N 0.000 description 6
- ZDHXKXAHOVTTAH-UHFFFAOYSA-N trichlorosilane Chemical compound Cl[SiH](Cl)Cl ZDHXKXAHOVTTAH-UHFFFAOYSA-N 0.000 description 5
- 239000005052 trichlorosilane Substances 0.000 description 5
- 239000007792 gaseous phase Substances 0.000 description 4
- 230000001276 controlling effect Effects 0.000 description 3
- 239000012043 crude product Substances 0.000 description 3
- 239000000203 mixture Substances 0.000 description 3
- 230000035945 sensitivity Effects 0.000 description 3
- 239000013589 supplement Substances 0.000 description 3
- 238000001514 detection method Methods 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- 239000000047 product Substances 0.000 description 2
- 230000001105 regulatory effect Effects 0.000 description 2
- VXEGSRKPIUDPQT-UHFFFAOYSA-N 4-[4-(4-methoxyphenyl)piperazin-1-yl]aniline Chemical compound C1=CC(OC)=CC=C1N1CCN(C=2C=CC(N)=CC=2)CC1 VXEGSRKPIUDPQT-UHFFFAOYSA-N 0.000 description 1
- BLRPTPMANUNPDV-UHFFFAOYSA-N Silane Chemical compound [SiH4] BLRPTPMANUNPDV-UHFFFAOYSA-N 0.000 description 1
- 238000012824 chemical production Methods 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- MROCJMGDEKINLD-UHFFFAOYSA-N dichlorosilane Chemical compound Cl[SiH2]Cl MROCJMGDEKINLD-UHFFFAOYSA-N 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 229910000077 silane Inorganic materials 0.000 description 1
- 239000005049 silicon tetrachloride Substances 0.000 description 1
- 238000003860 storage Methods 0.000 description 1
- 230000001629 suppression Effects 0.000 description 1
- 238000010408 sweeping Methods 0.000 description 1
- 238000012546 transfer 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
- B01D3/42—Regulation; Control
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- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
Abstract
The invention provides a coupling rectification separation system and a coupling rectification separation method. The coupling rectification separation system comprises a first rectification tower, a second rectification tower, a reflux tank, a tower top communicating pipe and a tower top control valve; the discharge hole of the first rectifying tower is communicated with the feed inlet of the second rectifying tower, the reflux tank is communicated with the top of the second rectifying tower through the top communicating pipe, and the top control valve is arranged on the top communicating pipe. The separation system can flexibly adjust the tower top pressure of the second rectifying tower.
Description
Technical Field
The invention relates to a coupling rectification separation system and a coupling rectification separation method, and belongs to the technical field of chemical separation.
Background
In chemical production, a plurality of rectifying towers are generally connected in series to separate a multi-component mixture, or a plurality of rectifying towers are connected in series to improve the separation precision of products. Fig. 1 shows a coupled rectification separation system in the prior art. As shown in fig. 1, taking any two interconnected rectifying towers as an example, a coupled rectifying and separating system in the prior art includes a first rectifying tower 1, a second rectifying tower 2, a reboiler 3, a reflux tank 7, a pressure release unit, a lower liquid valve 4, a pressurization unit, a liquid phase delivery pipe 10 and a gas phase delivery pipe 8; wherein, the tower bottom liquid phase outlet of the first rectifying tower 1 is communicated with the liquid phase inlet of the reboiler 3, the tower top gas phase outlet of the second rectifying tower 2 is communicated with the gas phase inlet of the reboiler 3, the first liquid phase outlet of the reboiler 3 is communicated with the liquid phase inlet of the reflux tank 7 through a liquid phase delivery pipe 10, the liquid discharge valve 4 is arranged on the liquid phase delivery pipe 10, the reboiler 3 and the reflux tank 7 are further communicated through a gas phase delivery pipe 8, the pressure release unit and the pressurization unit are respectively communicated with the reflux tank 7, the communicating pipeline of the pressure release unit and the reflux tank 7 is provided with the vent valve 5, and the communicating pipeline of the pressurization unit and the reflux tank 7 is provided with the hydrogen valve 6. In the actual operation process, on one hand, the heat exchange area of the reboiler 3 is controlled by controlling the opening and closing conditions of the lower liquid valve 4 so as to adjust the top pressure of the second rectifying tower 2; on the other hand, the opening and closing conditions of the lower liquid valve 4, the emptying valve 5 and the hydrogen valve 6 are respectively controlled, so that the top pressure of the second rectifying tower 2 is adjusted.
However, in practical application, the pressure at the top of the second rectification column 2 is adjusted through the emptying valve 5, the lower liquid valve 4 and the hydrogen valve 6, so that the delay and the interference are caused, the adjustment sensitivity is low, the improper operation easily causes that the pressure at the top of the second rectification column 2 is difficult to adjust or the pressure at the top of the second rectification column 2 fluctuates greatly, the raw material separation is not facilitated, and the safety problem is caused.
Disclosure of Invention
The invention provides a coupling rectification separation system which can flexibly adjust the tower top pressure of a second rectification tower.
The invention provides a coupling rectification separation method which is carried out by using the coupling rectification separation system and can flexibly adjust the tower top pressure of a second rectification tower.
The invention provides a coupling rectification separation system, which comprises a first rectification tower, a second rectification tower, a reflux tank, a tower top communicating pipe and a tower top control valve, wherein the first rectification tower is connected with the reflux tank through the first rectification tower;
the discharge port of the first rectifying tower is communicated with the feed inlet of the second rectifying tower, the reflux tank is communicated with the top of the second rectifying tower through the top of the tower communicating pipe, and the top of the tower control valve is arranged on the top of the tower communicating pipe.
The coupled rectification separation system further comprises a pressurization unit, and the pressurization unit is communicated with the reflux tank.
The coupled rectification separation system as described above, wherein the pressurization unit comprises a hydrogen pressurization unit and/or a nitrogen pressurization unit.
The coupled rectification separation system further comprises a pressure relief unit, and the pressure relief unit is communicated with the reflux tank.
The coupled rectification separation system further comprises a reboiler arranged at the tower bottom of the first rectification tower.
The coupled rectification separation system further comprises a liquid phase conveying pipe;
the tower kettle of the first rectifying tower is communicated with the liquid phase inlet of the reboiler, the tower top of the second rectifying tower is communicated with the gas phase inlet of the reboiler, and the liquid phase outlet of the reboiler is communicated with the reflux tank through the liquid phase conveying pipe.
The coupled rectification separation system further comprises a gas phase conveying pipe;
and the gas phase outlet of the reboiler is communicated with the reflux tank through the gas phase conveying pipe.
The coupled rectification separation system further comprises a gas phase valve; the gas phase valve is arranged above the gas phase conveying pipe.
The coupled fractionation system as described above, wherein the reboiler and the reflux drum are located on the same plane.
The invention also provides a coupled rectification separation method, wherein the coupled rectification separation system is used for carrying out the coupled rectification separation method.
The invention provides a coupling rectification separation system, which utilizes a tower top communicating pipe to communicate a reflux tank with the tower top of a second rectification tower, and is provided with a tower top control valve, and the tower top pressure of the second rectification tower is controlled in real time by utilizing the tower top control valve, so that the delay in the control process is eliminated, and the control sensitivity is improved.
The invention provides a coupling rectification separation method, which is carried out by using the coupling rectification separation system, so that the tower top pressure of a second rectification tower can be controlled in real time, and the coupling rectification separation method is simple to operate and suitable for wide popularization and application.
Drawings
In order to more clearly illustrate the embodiments of the present invention or the technical solutions in the related art, the drawings used in the description of the embodiments of the present invention or the related art are briefly introduced below. It is obvious that the drawings in the following description are only some embodiments of the invention, and that for a person skilled in the art, other drawings can be derived from them without inventive effort.
FIG. 1 is a prior art coupled rectification separation system;
fig. 2 is a coupled rectification separation system in some embodiments of the present invention.
Description of reference numerals:
1: a first rectification column;
2: a second rectification column;
3: a reboiler;
4: a liquid discharge valve;
5: an atmospheric valve;
6: a hydrogen valve;
7: a reflux tank;
8, a gas phase conveying pipe;
9, a pressure detection unit;
10: a liquid phase delivery pipe;
11: a nitrogen gas valve;
12: a gas phase valve;
13: a tower top communicating pipe;
14: a control valve at the top of the tower.
Detailed Description
The technical solutions in the embodiments of the present invention will be clearly and completely described below with reference to the drawings in the embodiments of the present invention, and it is obvious that the described embodiments are only a part of the embodiments of the present invention, and not all of the embodiments. All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the protection scope of the present invention.
Fig. 2 is a coupled rectification separation system in some embodiments of the present invention. As shown in fig. 2, the present invention provides a coupling rectification separation system, which includes a first rectification tower 1, a second rectification tower 2, a reflux tank 7, a tower top communicating pipe 13 and a tower top control valve 14;
the discharge hole of the first rectifying tower 1 is communicated with the feed hole of the second rectifying tower 2, the reflux tank 7 is communicated with the top of the second rectifying tower 2 through a tower top communicating pipe 13, and the tower top control valve 14 is arranged on the tower top communicating pipe 13.
In a specific embodiment, a raw material enters a first rectifying tower 1 through a feed inlet of the first rectifying tower 1 to be subjected to a first rectifying treatment, in the first rectifying treatment, a light component (a first component) in the raw material is output from the top of the first rectifying tower 1, a heavy component (a second component) in the raw material is output from a tower kettle of the first rectifying tower, and an intermediate component in the raw material is output from a discharge outlet of the first rectifying tower 1 and enters a second rectifying tower 2 through a feed inlet of a second rectifying tower 2; and (3) carrying out second rectification treatment on the intermediate component in the second rectification tower 2, wherein in the second rectification treatment, a part of light components in the intermediate component is output from the top of the second rectification tower 2 and is condensed and converted into a liquid phase by an external cold source, the liquid phase enters a reflux tank 7 for storage, a part of the liquid phase is output from the reflux tank 7 to obtain a third component, the other part of the liquid phase is output from the reflux tank 7 and enters the second rectification tower 2 from the top of the second rectification tower 2 for reflux, a heavy component in the intermediate component is extracted from a tower kettle of the second rectification tower 2 to obtain a fourth component, and the obtained product is output from a discharge hole of the second rectification tower 2.
In the invention, light components output from the top of the second rectifying tower 2 also enter the reflux tank 7 through the tower top communicating pipe 13, and the amount of the light components entering the reflux tank 7 from the top of the second rectifying tower 2 is regulated and controlled by the tower top control valve 14 arranged on the tower top communicating pipe 13, so that the tower top pressure of the second rectifying tower 2 can be regulated. If the pressure at the top of the second rectifying tower 2 is too high, opening a top control valve 14 to enable more light components at the top of the second rectifying tower 2 to enter a reflux tank 7, and gradually reducing the pressure at the top of the second rectifying tower 2 along with the output of the light components at the top of the second rectifying tower 2; if the pressure at the top of the second rectifying tower 2 is low, the top control valve 14 is closed, so that the pressure at the top of the second rectifying tower 2 is suppressed, and thus the top pressure of the second rectifying tower 2 is increased, and if the pressure at the top of the second rectifying tower 2 still cannot meet the operation requirement due to the pressure suppression, the gas phase in the reflux tank 7 can be returned to the top of the second rectifying tower 2, so that the top of the second rectifying tower 2 is pressurized.
According to the coupled rectification separation system, the reflux tank 7 is communicated with the top of the second rectification tower 2 through the tower top communicating pipe 13, the tower top communicating pipe 13 is further provided with the tower top control valve 14, the tower top pressure of the second rectification tower 2 can be controlled in real time through the tower top control valve 14, the delay in the control process is eliminated, and the control sensitivity is improved.
It can be understood that in the coupled rectification separation system, the rectification tower for outputting the materials is the first rectification tower 1, and the rectification tower for inputting the materials is the second rectification tower 2. In the present invention, the first distillation column 1 and the second distillation column 2 may be any distillation column commonly used in the art, for example, the first distillation column 1 and the second distillation column 2 are each independently selected from a dividing wall column or a packed column. The coupling rectification separation system can be suitable for two-stage and above coupling rectification, for example, two-stage coupling rectification, three-stage coupling rectification or four-stage coupling rectification.
In some embodiments of the present invention, the coupled fractionation system may further include a pressurizing unit, which is in communication with the reflux drum 7.
In a specific embodiment, if it is difficult to make the top pressure of the second rectification column 2 meet the operation requirement through the pressure-holding, the reflux tank 7 may be pressurized by using a pressurization unit, and the top pressure of the second rectification column 2 may be increased through the top communicating pipe 13.
In some embodiments, the pressurizing unit comprises a hydrogen pressurizing unit and/or a nitrogen pressurizing unit.
When the pressurizing unit comprises a hydrogen pressurizing unit, a pipeline for communicating the hydrogen pressurizing unit with the reflux tank 7 is provided with a hydrogen valve 6, if the pressure at the top of the second rectifying tower 2 is too low, the hydrogen valve 6 can be opened to supplement pressure to the reflux tank 7, so that the pressure at the top of the second rectifying tower 2 is increased; when the pressure boost unit includes the nitrogen gas pressure boost unit, be provided with nitrogen gas valve 11 on the pipeline of nitrogen gas pressure boost unit and reflux drum 7 intercommunications, when the top of the tower pressure of second rectifying column 2 crossed low, can open nitrogen gas valve 11, for 7 pressure compensations of reflux drum, and then improve the top of the tower pressure of second rectifying column 2, when the pressure boost unit included the nitrogen gas pressure boost unit, nitrogen gas can also be used for sweeping the replacement to the gas in the reflux drum 7.
In some embodiments of the present invention, the coupled rectification separation system further comprises a pressure relief unit, which is in communication with the reflux drum 7.
In a specific embodiment, a vent valve 5 is further arranged on a pipeline of the pressure relief unit communicated with the return tank 7, and if the pressure in the return tank 7 is too high, the pressure in the return tank 7 can be reduced through the pressure relief unit, so that the operation safety is improved.
In some embodiments of the present invention, the coupled fractionation system further comprises a reboiler 3 disposed at the bottom of the first distillation column 1.
In the invention, a reboiler 3 can be arranged at the tower bottom of the first rectifying tower 1, and part of the third component output from the tower bottom of the first rectifying tower 1 enters the reboiler 3 to provide energy for the tower bottom of the first rectifying tower 1.
In some embodiments of the present invention, the coupled fractionation system further comprises a liquid phase transport pipe 10;
the tower kettle of the first rectifying tower 1 is communicated with the liquid phase inlet of the reboiler 3, the tower top of the second rectifying tower 2 is communicated with the gas phase inlet of the reboiler 3, and the liquid phase outlet of the reboiler 3 is communicated with the reflux tank 7 through a liquid phase conveying pipe 10.
In a specific embodiment, a part of the third component generated at the tower bottom of the first rectifying tower 1 enters the reboiler 3 through the liquid phase inlet of the reboiler 3, a part of the light component generated at the tower top of the second rectifying tower 2 enters the reboiler 3 through the gas phase inlet of the reboiler 3, and in the reboiler 3, the third component at the tower bottom of the first rectifying tower 1 and the light component generated at the tower top of the second rectifying tower 2 are subjected to heat exchange treatment, on one hand, the third component at the tower bottom of the first rectifying tower 1 condenses the light component generated at the tower top of the second rectifying tower 2 into a liquid phase, and the liquid phase is output through the liquid phase outlet of the reboiler 3 and enters the reflux tank 7 through the liquid phase conveying pipe 10; on the other hand, the gas phase at the top of the second rectifying tower 2 provides energy for the third component at the bottom of the first rectifying tower 1, and further provides energy for the bottom of the first rectifying tower 1.
According to the invention, the condensation reflux of the gas phase at the top of the second rectifying tower 2 can be realized under the condition that no condensing equipment or external cold source is used, and the heat of the gas phase at the top of the second rectifying tower 2 is utilized to supplement heat for the tower kettle of the first rectifying tower 1, so that the equipment cost and the energy consumption are saved.
The application system of the coupled rectification separation system is not particularly limited, and can be used for separating chlorosilane mixtures. When the method is used for separating a silane mixture, a crude chlorosilane raw material containing dichlorosilane, trichlorosilane, silicon tetrachloride and impurities can enter a first rectifying tower 1 through a feed inlet of the first rectifying tower 1 for first rectifying treatment, after the first rectifying treatment, part of high-boiling-point substances (second components) in the crude chlorosilane raw material is extracted from a tower kettle of the first rectifying tower 1 and enters a downstream unit, low-boiling-point substances (first components) in the crude chlorosilane raw material is extracted from a tower top of the first rectifying tower 1, and a trichlorosilane crude product (intermediate components) in the crude chlorosilane raw material is extracted from a discharge port of the first rectifying tower 1 and enters a second rectifying tower 2 through a feed inlet of the second rectifying tower 2; extracting low-boiling-point substances in the trichlorosilane crude product through the top of the second rectifying tower 2 to enter a reflux tank, extracting the other part of high-boiling-point substances (second components) in the crude chlorosilane raw material through the bottom of the first rectifying tower 1 to enter a reboiler 3, performing heat exchange between the low-boiling-point substances from the second rectifying tower 2 and the second components from the first rectifying tower 1 in the reboiler 3, gasifying the second components of the first rectifying tower 1 by using light components at the top of the second rectifying tower 2 to generate heat, outputting the generated light components through the reboiler 3 to enter the bottom of the first rectifying tower 1, condensing the low-boiling-point substances from the second rectifying tower 2 into a liquid phase by using the second components in the reboiler 3 to obtain third components, outputting the third components through a liquid phase outlet of the reboiler 3 to enter the reflux tank 7, outputting the part of the third components from the reflux tank 7 to a downstream unit, using the other part of the third components as reflux liquid of the second rectifying tower 2, extracting the high-boiling-point substances (second components) in the trichlorosilane crude product through the top of the second rectifying tower 2 to exit of the reflux tank 2, and extracting the high-point of the trichlorosilane raw material through the discharge port of the reboiler 2.
In some embodiments of the invention, the coupled fractionation system further comprises a gas phase transfer line 8;
the gas phase outlet of the reboiler 3 is communicated with a reflux drum 7 through a gas phase delivery pipe 8.
In the invention, after the tower top gas phase of the second rectifying tower 2 and the tower bottom third component of the first rectifying tower 1 exchange heat in the reboiler 3, the tower bottom third component of the first rectifying tower 1 is converted into the gas phase, the gas phase comprises a part of non-condensable gas, and the non-condensable gas is output through a gas phase outlet of the reboiler 3 and enters the reflux tank 7 through a gas phase conveying pipe 8.
If too much gas phase or too much pressure is present in the reflux drum 7, the blow valve 5 can be opened to allow the non-condensable gases to escape through the blow valve 5.
Taking the example of controlling the top pressure temperature of the second rectification column 2 to be about 0.52MPaG as an example to exemplarily illustrate the scheme of the present invention, when the top pressure of the second rectification column 2 is higher than 0.54MPaG, the vent valve 5 is opened to release a part of gas, so that the pressure of the reflux tank 7 is reduced, and further, the top pressure of the second rectification column 2 communicated with the reflux tank 7 through the top connecting pipe 13 is reduced until the top pressure of the second rectification column 2 is 0.52MPaG, the vent valve 5 is closed; when the top pressure of the second distillation column 2 is lower than 0.5MPaG, a hydrogen valve 6 may be opened to supplement the pressure to the reflux drum 7, so that the top pressure of the second distillation column 2 communicated with the reflux drum 7 through the top connecting pipe 13 is also increased, and the hydrogen valve 6 is closed until the top pressure of the second distillation column 2 is 0.52 MPaG.
In some embodiments of the invention, the coupled fractionation system further comprises a gas phase valve 12; the gas phase valve 12 is disposed above the gas phase transport pipe 8.
The invention controls the condition that the gas phase in the reboiler 3 enters the reflux tank 7 by arranging a gas phase valve 12 on the gas phase conveying pipe 8 and utilizing the gas phase valve 12.
In the prior art, since the second rectifying tower 2, the reboiler 3 and the reflux tank 7 are communicated with each other, the pressure at the top of the second rectifying tower 2 is equal to the pressure in the reflux tank 7, and the pressure of the liquid phase in the reboiler 3 is lower than the pressure in the reflux tank 7, so that the liquid phase in the reboiler 3 can enter the reflux tank 7, and a liquid bag is prevented from being present in the liquid phase delivery pipe 10 of the reboiler 3 and the reflux tank 7, it is usually necessary to install the reboiler 3 and the reflux tank 7 on different floors (for example, the reboiler 3 is installed on the second floor, and the reflux tank 7 is installed on the first floor).
In some embodiments of the invention, the reboiler 3 may be co-planar with the reflux drum 7.
In the invention, the gas phase valve 12 can control whether the gas phase in the reboiler 3 enters the reflux tank 7 (the gas phase valve 12 can realize the communication between the reboiler 3 and the reflux tank 7 or not), when the reflux tank 7 is not communicated with the reboiler 3, the pressure of the reflux tank 7 and the pressure of the top of the second rectifying tower 2 can be respectively controlled, therefore, the pressure in the reflux tank 7 can be lower than the pressure of the top of the second rectifying tower 2, and when the reboiler 3 and the reflux tank 7 are positioned on the same plane, the liquid phase in the reboiler 3 can be pressed into the reflux tank 7 by utilizing the pressure difference between the top pressure of the second rectifying tower 2 and the pressure in the reflux tank 7 according to the principle of a communicating vessel.
Through the arrangement, the reboiler 3 and the reflux tank 7 can be positioned on the same plane, so that the pipeline cost and the civil engineering cost are saved.
For example, in the existing coupled rectification system, if the reflux tank 7 and the reboiler 3 of the same size are placed on the same plane (two levels), the liquid level in the reflux tank 7 will be 4.5 meters higher than the liquid level of the shell of the reboiler 3 (the base height of the reflux tank at the two levels is 1.1 meters), and therefore, the liquid phase in the shell of the reboiler 3 will be difficult to flow into the reflux tank 7. To overcome this drawback, as shown in fig. 1, the prior art usually locates the reboiler 3 in two layers, the reflux drum 7 in one layer (the height of the reflux drum is 2.4 meters on the basis of one layer), the height of the two layers is usually 9 meters, and the liquid level position of the inner shell of the reboiler 3 is 3 meters higher than the liquid level position of the reflux drum 7, so that the liquid phase in the shell of the reboiler 3 can flow into the reflux drum 7. The scheme of the invention reduces the pressure of the reflux tank 7 by 0.1MPaG, and can ensure that the liquid in the reboiler 3 enters the reflux tank 7 in a self-pressurized flow state, so that the reboiler 3 and the reflux tank 7 can be arranged in the same layer, the structural cost is saved by about 5-10%, the space of one floor is greatly saved, and the operation and the maintenance of equipment by personnel are facilitated. Meanwhile, the reboiler 3 and the reflux tank 7 are arranged in the same layer, so that the inlet pressure of the reflux pump is increased, the cavitation allowance of the pump is increased, corresponding cost can be saved, and the operation of the pump is safer and more stable.
In some embodiments, the coupling and separating system of the present invention may further include a pressure detecting unit 9, the pressure detecting unit 9 is disposed at the top of the second distillation tower 2, the vent valve 5, the hydrogen valve 6, the nitrogen valve 11, the gas phase valve 12, and the tower top control valve 14 are switching valves, and the opening and closing of the vent valve 5, the hydrogen valve 6, the nitrogen valve 11, the gas phase valve 12, and the tower top control valve 14 may be manually controlled according to data of the pressure detecting unit 9.
In some embodiments, the coupling and separating system of the present invention may further include a control unit, wherein the deflating valve 5, the hydrogen valve 6, the nitrogen valve 11, the gas phase valve 12, the tower top control valve 14 and the pressure detecting unit 9 may be electrically connected to the control unit, and the control unit controls the opening and closing of the deflating valve 5, the hydrogen valve 6, the nitrogen valve 11, the gas phase valve 12 and the tower top control valve 14 in real time according to the data fed back by the pressure detecting unit 9.
In some embodiments, the atmospheric valve 5, the hydrogen valve 6, the nitrogen gas valve 11, the tower top control valve 14, and the pressure detection unit 9 may be electrically connected to the control unit, and the gas phase valve 12 is an on-off valve. The open and close of the gas phase valve 12 can be manually adjusted by controlling the open and close of the vent valve 5, the hydrogen valve 6, the nitrogen valve 11 and the tower top control valve 14 by the control unit.
The second aspect of the invention provides a coupled rectification separation method, wherein the coupled rectification separation system is used for carrying out the coupled rectification separation method.
The coupling rectification separation method is carried out by using the coupling rectification separation system, so that the tower top pressure of the second rectification tower 2 can be controlled in real time, the operation is simple, and the coupling rectification separation method is suitable for wide popularization and application.
The present invention will be further described with reference to specific examples.
Example 1
As shown in fig. 2, the coupling and decoupling system of the present embodiment includes:
a first rectifying tower 1, a second rectifying tower 2, a reflux tank 7, a tower top communicating pipe 13, a tower top control valve 14, a pressurizing unit, a pressure releasing unit, a reboiler 3, a liquid phase conveying pipe 10, a gas phase conveying pipe 8 and a gas phase valve 12;
the discharge hole of the first rectifying tower 1 is communicated with the feed hole of the second rectifying tower 2, the reflux tank 7 is communicated with the top of the second rectifying tower 2 through a tower top communicating pipe 13, and a tower top control valve 14 is arranged on the tower top communicating pipe 13;
the pressurizing unit is communicated with the reflux tank 7 and comprises a hydrogen pressurizing unit and a nitrogen pressurizing unit, a hydrogen valve 6 is arranged on a communication pipeline of the hydrogen pressurizing unit and the reflux tank 7, and a nitrogen valve 11 is arranged on a communication pipeline of the nitrogen pressurizing unit and the reflux tank 7;
the pressure relief unit is communicated with the reflux tank 7, and a vent valve 5 is arranged on a communicating pipeline between the pressure relief unit and the reflux tank 7;
the tower kettle of first rectifying column 1 communicates with reboiler 3's liquid phase entry, the top of the tower of second rectifying column 2 communicates with reboiler 3's gaseous phase entry, reboiler 3's liquid phase export and reflux tank 7 pass through liquid phase conveyer pipe 10 and communicate, reboiler 3's gaseous phase export and reflux tank 7 pass through gaseous phase conveyer pipe 8 and communicate, gas phase valve 12 sets up on gaseous phase conveyer pipe 8, reboiler 3 and reflux tank 7 are located the coplanar.
All the embodiments in the present specification are described in a related manner, and the same and similar parts among the embodiments may be referred to each other, and each embodiment focuses on the differences from the other embodiments. The above description is only for the preferred embodiment of the present invention, and is not intended to limit the scope of the present invention. Any modification, equivalent replacement, or improvement made within the spirit and principle of the present invention shall fall within the protection scope of the present invention.
Claims (10)
1. A coupling rectification separation system is characterized by comprising a first rectification tower, a second rectification tower, a reflux tank, a tower top communicating pipe and a tower top control valve;
the discharge hole of the first rectifying tower is communicated with the feed inlet of the second rectifying tower, the reflux tank is communicated with the top of the second rectifying tower through the top communicating pipe, and the top control valve is arranged on the top communicating pipe.
2. The coupled fractionation separation system of claim 1, further comprising a pressurization unit in communication with the reflux drum.
3. The coupled fractionation separation system according to claim 2, wherein the pressurizing unit comprises a hydrogen pressurizing unit and/or a nitrogen pressurizing unit.
4. The coupled rectification separation system according to any one of claims 1 to 3, further comprising a pressure relief unit in communication with the reflux drum.
5. The coupled fractionation system of any of claims 1-4, further comprising a reboiler disposed at the bottom of the first fractionation column.
6. The coupled rectification separation system according to claim 5, further comprising a liquid phase transport pipe;
the tower kettle of the first rectifying tower is communicated with the liquid phase inlet of the reboiler, the tower top of the second rectifying tower is communicated with the gas phase inlet of the reboiler, and the liquid phase outlet of the reboiler is communicated with the reflux tank through the liquid phase conveying pipe.
7. The coupled rectification separation system of claim 6 further comprising a gas phase transport pipe;
and the gas phase outlet of the reboiler is communicated with the reflux tank through the gas phase conveying pipe.
8. The coupled rectification separation system of claim 7 further comprising a gas phase valve; the gas phase valve is arranged above the gas phase conveying pipe.
9. The coupled fractionation separation system of claim 7, wherein the reboiler is in the same plane as the reflux drum.
10. A coupled fractionation process, characterized by being carried out using the coupled fractionation system according to any one of claims 1 to 9.
Priority Applications (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202211510386.1A CN115888158A (en) | 2022-11-29 | 2022-11-29 | Coupling rectification separation system and coupling rectification separation method |
| PCT/CN2023/079670 WO2024113526A1 (en) | 2022-11-29 | 2023-03-03 | Coupled distillation separation system and coupled distillation separation method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
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| CN202211510386.1A CN115888158A (en) | 2022-11-29 | 2022-11-29 | Coupling rectification separation system and coupling rectification separation method |
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| CN202211510386.1A Pending CN115888158A (en) | 2022-11-29 | 2022-11-29 | Coupling rectification separation system and coupling rectification separation method |
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| WO (1) | WO2024113526A1 (en) |
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| JP5863734B2 (en) * | 2013-09-18 | 2016-02-17 | ラムス テクノロジー インク | Systems and processes for producing linear alpha olefins |
| CN104771926B (en) * | 2015-03-23 | 2017-01-04 | 烟台国邦化工机械科技有限公司 | The rectifier unit of a kind of recovery of acetic acid from aqueous acetic acid and process |
| US11207611B1 (en) * | 2018-07-03 | 2021-12-28 | Burns & Mcdonnell Engineering Company, Inc. | Process for separating hydrocarbons in a liquid feed utilizing an externally heated reboiler connected to a divided wall column as the primary source of heat energy |
| CN210419809U (en) * | 2019-06-12 | 2020-04-28 | 天津市汇筑恒升科技有限公司 | Esterification and rectification heat integration system in process of preparing ethylene glycol from coal |
| CN110327647B (en) * | 2019-07-19 | 2021-12-10 | 张兵 | Improved three-tower three-effect crude methanol refining process method |
| CN211863899U (en) * | 2019-07-19 | 2020-11-06 | 张兵 | Improved three-tower three-effect crude methanol refining process system |
| CN110280037B (en) * | 2019-08-08 | 2024-07-09 | 中国恩菲工程技术有限公司 | Titanium tetrachloride rectifying device |
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