CN114832417B - Titanium tetrachloride recovery system in refined low boiling point distillate - Google Patents
Titanium tetrachloride recovery system in refined low boiling point distillate Download PDFInfo
- Publication number
- CN114832417B CN114832417B CN202210420663.3A CN202210420663A CN114832417B CN 114832417 B CN114832417 B CN 114832417B CN 202210420663 A CN202210420663 A CN 202210420663A CN 114832417 B CN114832417 B CN 114832417B
- Authority
- CN
- China
- Prior art keywords
- tower
- low
- distillate
- boiling
- titanium tetrachloride
- 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
- 238000009835 boiling Methods 0.000 title claims abstract description 93
- XJDNKRIXUMDJCW-UHFFFAOYSA-J titanium tetrachloride Chemical compound Cl[Ti](Cl)(Cl)Cl XJDNKRIXUMDJCW-UHFFFAOYSA-J 0.000 title claims abstract description 50
- 238000011084 recovery Methods 0.000 title claims abstract description 12
- 239000000047 product Substances 0.000 claims abstract description 142
- 239000012535 impurity Substances 0.000 claims abstract description 29
- 239000006227 byproduct Substances 0.000 claims abstract description 27
- 238000010992 reflux Methods 0.000 claims abstract description 26
- 238000000926 separation method Methods 0.000 claims abstract description 20
- 238000000034 method Methods 0.000 claims abstract description 10
- 238000007670 refining Methods 0.000 claims abstract description 10
- 239000007788 liquid Substances 0.000 claims description 27
- 239000012071 phase Substances 0.000 claims description 8
- 239000007791 liquid phase Substances 0.000 claims description 4
- 238000012856 packing Methods 0.000 claims description 4
- 238000004519 manufacturing process Methods 0.000 description 11
- 239000007789 gas Substances 0.000 description 5
- 239000012141 concentrate Substances 0.000 description 2
- 238000009833 condensation Methods 0.000 description 2
- 230000005494 condensation Effects 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 238000004821 distillation Methods 0.000 description 2
- 238000010438 heat treatment Methods 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 238000012958 reprocessing Methods 0.000 description 2
- 239000002699 waste material Substances 0.000 description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- 229910003902 SiCl 4 Inorganic materials 0.000 description 1
- 229910021627 Tin(IV) chloride Inorganic materials 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 238000005660 chlorination reaction Methods 0.000 description 1
- 230000000295 complement effect Effects 0.000 description 1
- 238000001514 detection method Methods 0.000 description 1
- 230000006866 deterioration Effects 0.000 description 1
- 230000002542 deteriorative effect Effects 0.000 description 1
- 238000010790 dilution Methods 0.000 description 1
- 239000012895 dilution Substances 0.000 description 1
- 239000000428 dust Substances 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 239000007792 gaseous phase Substances 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 238000012544 monitoring process Methods 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 239000000243 solution Substances 0.000 description 1
- 239000013589 supplement Substances 0.000 description 1
- HPGGPRDJHPYFRM-UHFFFAOYSA-J tin(iv) chloride Chemical compound Cl[Sn](Cl)(Cl)Cl HPGGPRDJHPYFRM-UHFFFAOYSA-J 0.000 description 1
- 238000009834 vaporization Methods 0.000 description 1
- 230000008016 vaporization Effects 0.000 description 1
- 239000002918 waste heat Substances 0.000 description 1
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
- B01D3/322—Reboiler specifications
-
- 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
- B01D3/4205—Reflux ratio control splitter
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D5/00—Condensation of vapours; Recovering volatile solvents by condensation
- B01D5/0057—Condensation of vapours; Recovering volatile solvents by condensation in combination with other processes
- B01D5/006—Condensation of vapours; Recovering volatile solvents by condensation in combination with other processes with evaporation or distillation
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01G—COMPOUNDS CONTAINING METALS NOT COVERED BY SUBCLASSES C01D OR C01F
- C01G23/00—Compounds of titanium
- C01G23/02—Halides of titanium
- C01G23/022—Titanium tetrachloride
- C01G23/024—Purification of tetrachloride
-
- 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)
- Organic Chemistry (AREA)
- Life Sciences & Earth Sciences (AREA)
- Environmental & Geological Engineering (AREA)
- General Life Sciences & Earth Sciences (AREA)
- Geology (AREA)
- Inorganic Chemistry (AREA)
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
Abstract
A titanium tetrachloride recovery system in refined low-boiling-point distillate comprises a low-boiling-point distillate separating tower, wherein a tower body of the low-boiling-point distillate separating tower is connected with a refined low-boiling-point distillate feeding pipeline, the tower bottom is communicated with the lower part of a reboiler, the top of the reboiler is communicated with the low-boiling-point distillate separating tower in a gas phase manner, an overflow discharge port at the upper part of the reboiler is connected with a tower kettle product tank, and an outlet pipeline of the tower kettle product tank is connected with a low-boiling-point impurity separating system in a titanium tetrachloride refining process; the top of the low boiling point distillate separating tower is connected with a tower top product tank through a pipeline and a tower top product condenser, and an outlet pipeline of the tower top product tank is connected with two branches which are respectively connected with a reflux port and a byproduct storage tank at the upper part of the low boiling point distillate separating tower. The invention carries out high-efficiency separation on the refined low-boiling point distillate to obtain high-concentration low-boiling point byproducts and recovered titanium tetrachloride, thereby reducing the product loss of the titanium tetrachloride.
Description
Technical Field
The invention belongs to the technical field of titanium tetrachloride production processes, and particularly relates to a titanium tetrachloride recovery system in refined low-boiling-point distillate.
Background
The production of titanium tetrachloride is required to be subjected to chlorination, dust removal, condensation and refining procedures, the refining procedures comprise a high-boiling-point impurity separation system and a low-boiling-point impurity separation system, wherein the low-boiling-point impurity separation system consists of a plate-type distillation tower, a reboiler, a condenser, a reflux tank, a reflux pump, a product tank and the like, distillation separation is carried out according to the difference of boiling points of impurities, impurities with boiling points lower than that of titanium tetrachloride are mainly separated, and qualified refined titanium tetrachloride is obtained through separation of the low-boiling-point impurity separation systemThe product, the low-boiling impurities are enriched and concentrated at the top of the tower, and the incomplete separation of the low-boiling impurities can lead to the abrupt deterioration of the quality of the titanium tetrachloride product. However, a large amount of low boiling point distillate is produced as a byproduct after the low boiling point impurity separation system is separated, the refined low boiling point distillate accounts for more than 5 percent of the feeding amount of the low boiling point impurity separation system, and the refined low boiling point distillate contains a large amount of low boiling point impurities, mainly SnCl 4 、SiCl 4 And other impurities containing oxygen and carbon below the boiling point of titanium tetrachloride, cannot be directly used as products, however, the content of titanium tetrachloride in the refined low-boiling-point distillate still reaches more than 92%, so that the refined low-boiling-point distillate needs to be treated again to separate the titanium tetrachloride and the low-boiling-point impurities.
The conventional process method for reprocessing the refined low-boiling point distillate is to return the refined low-boiling point distillate to be mixed with crude titanium tetrachloride for dilution, then to refine, enrich and concentrate again or to temporarily store and then to feed the mixture to a low-boiling point impurity separation system for refining, enriching and concentrating again independently, so as to obtain a low-boiling point byproduct with higher concentration of low-boiling point impurities. However, the reprocessing method has the risk of deteriorating the product quality, and the production operation stability is affected by the need of stopping the production line to perform enrichment and concentration again.
The most representative low boiling impurities in the refined low boiling distillate are SnCl 4 The detection is most accurate, the boiling point of tin tetrachloride (114 ℃) is close to that of titanium tetrachloride (137 ℃), and SnCl is often used 4 The concentration of the low boiling impurities is determined. In general, snCl in low boiling point distillate is purified 4 If the method is adopted to concentrate the refined low-boiling point distillate for multiple times, the SnCl in the concentrated low-boiling point distillate is generally about 2 percent 4 Still not exceeding 5%, wherein the unseparated titanium tetrachloride still has a very high content. The concentrated low boiling distillate is sold at a price far lower than the production cost of titanium tetrachloride, resulting in a great deal of titanium tetrachloride waste. As the production of titanium tetrachloride increases, the amount of low boiling point distillate increases and the normal production system cannot diluteOr refining and concentrating again, so that the treatment of the low-boiling point distillate becomes a key factor influencing the production cost of the titanium tetrachloride.
Disclosure of Invention
The invention aims to provide a titanium tetrachloride recovery system in refined low-boiling point distillate, which is used for efficiently separating the refined low-boiling point distillate to obtain high-concentration low-boiling point byproducts, efficiently recovering titanium tetrachloride and greatly reducing the product loss of titanium tetrachloride.
In order to achieve the above purpose, the technical scheme adopted by the invention is as follows: a titanium tetrachloride recovery system in refined low-boiling point distillate comprises a low-boiling point distillate separating tower, a reboiler, a tower kettle product tank, a tower top product condenser and a tower top product tank; the tower body of the low boiling point distillate separating tower is connected with a refined low boiling point distillate feeding pipeline, the tower bottom is communicated with the lower part of the reboiler so that a liquid phase product at the tower bottom automatically flows into the reboiler, the top of the reboiler is communicated with the gas phase of the low boiling point distillate separating tower, an overflow discharge port at the upper part of the reboiler is connected with a tower kettle product tank, and an outlet pipeline of the tower kettle product tank is connected with a low boiling point impurity separating system in the titanium tetrachloride refining process; the top of the low boiling point distillate separating tower is connected with the top product tank through a pipeline and the top product condenser so as to separate and collect gas phase products at the top of the tower, and an outlet pipeline of the top product tank is connected with two branches which are respectively connected with a reflux port and a byproduct storage tank at the upper part of the low boiling point distillate separating tower.
And the outlet pipeline of the tower kettle product tank and the low-boiling-point distillate feeding pipeline are intersected in a feeding product preheater, and the tower kettle product conveyed by the outlet pipeline of the tower kettle product tank preheats the low-boiling-point distillate in the low-boiling-point distillate feeding pipeline.
And a feeding product control valve and a feeding flowmeter which are controlled in an interlocking manner are arranged on the low-boiling-point distillate feeding pipeline.
The tower kettle product tank is provided with a tower kettle product tank liquid level meter, and an outlet pipeline of the tower kettle product tank is provided with a tower kettle product control valve which is in linkage control with the tower kettle product tank liquid level meter.
And a tower kettle product conveying pump is arranged on an outlet pipeline of the tower kettle product tank.
The tower top product tank is provided with a tower top product tank liquid level meter, and an outlet pipeline of the tower top product tank is provided with a tower top product reflux pump which is controlled by the tower top product tank liquid level meter in an interlocking way.
The outlet of the tower top product reflux pump is respectively connected with a first branch provided with a tower top product reflux control valve and a second branch provided with a high-concentration low-boiling-point byproduct control valve, the first branch is connected with a reflux port at the upper part of the low-boiling-point distillate separation tower, and the second branch is connected with a byproduct storage tank.
The low boiling point distillate separating tower is a packed tower with a packing height of more than 20 meters.
The beneficial effects of the invention are as follows: the invention solves the problems of high titanium tetrachloride content in low boiling point distillate, large byproduct amount and great production cost waste caused by insufficient concentration degree of low boiling point impurities in the existing low boiling point impurity separation system. The recovery system provided by the invention can be used as the complement and perfection of the existing refining system, the separation of low-boiling impurities is more thorough, and the reduction of low-boiling distillate byproducts can be realized. SnCl in low boiling distillate 4 The concentration is improved by 10 times, and the amount of by-products of the low-boiling point distillate is reduced by 80 percent.
The invention is used for recovering the titanium tetrachloride for refining the low-boiling point distillate, and SnCl in the high-concentration low-boiling point byproducts obtained in the treatment process 4 Concentration enrichment and concentration to 20 percent, realizes that the recovery rate of titanium tetrachloride in refined low-boiling point distillate reaches 80 percent, and the recovered SnCl in the titanium tetrachloride 4 A content of SnCl of less than 0.2% and a material entering the low boiling point impurity separation system 4 The content is basically consistent, and the low-boiling impurities can be directly returned to the low-boiling impurities separation system.
Through trial of certain titanium tetrachloride production enterprises, the byproduct amount of low-boiling-point distillate is reduced by more than 2000 tons in year, and the production cost is saved by 600 ten thousand yuan according to the market price difference of 3000 yuan/ton of the titanium tetrachloride and byproducts.
Drawings
FIG. 1 is a schematic diagram of a titanium tetrachloride recovery system in the refined low boiling distillate of the invention described in example 1;
FIG. 2 is a schematic diagram of a titanium tetrachloride recovery system in the refined low boiling distillate of the invention according to example 2;
the marks in the figure: 1. the device comprises a feeding product control valve, a low-boiling-point distillate separating tower, a reboiler, a tower kettle product tank, a tower kettle product conveying pump, a tower kettle product control valve, a feeding product preheater, a tower top product condenser, a tower top product tank, a tower top product reflux pump, a tower top product reflux control valve, a high-concentration low-boiling-point byproduct control valve, a tower top product tank liquid level meter, a tower kettle product tank liquid level meter, a feeding flowmeter, a byproduct storage tank and a low-boiling-point impurity separating system.
Detailed Description
The invention is described in further detail below with reference to the drawings and examples, which are not intended to be limiting.
Example 1: as shown in fig. 1, a titanium tetrachloride recovery system in refined low boiling point distillate comprises a feed product control valve 1, a low boiling point distillate separating column 2, a reboiler 3, a column bottom product tank 4, a column bottom product delivery pump 5, a column bottom product control valve 6, a column top product condenser 8, a column top product tank 9, a column top product reflux pump 10, a column top product reflux control valve 11, a high concentration low boiling point byproduct control valve 12, a column top product tank level gauge 13, a column bottom product tank level gauge 14 and a feed flow meter 15.
The low boiling point distillate separating tower 2 is a packed tower, high-efficiency regular corrugated packing is arranged in the packed tower, the packing height requirement reaches more than 20 meters, the theoretical plate number reaches more than 70, and the high-efficiency separation of the feeding products is ensured.
The middle part of the tower body of the low boiling point distillate separating tower 2 is a separating tower feed inlet, a feed pipeline is connected, a feed product control valve 1 and a feed flowmeter 15 are sequentially arranged on the feed pipeline, refined low boiling point distillate generated by the low boiling point impurity separating system enters the low boiling point distillate separating tower 2 through the feed product control valve 1, the feed flowmeter 15 detects the feed amount in real time, and the feed product control valve 1 and the feed flowmeter 15 can realize linkage control, so that the feed amount of the low boiling point distillate separating tower 2 is strictly controlled.
The bottom of the low-boiling-point distillate separating tower 2 is communicated with the lower part of the reboiler 3, so that a liquid-phase product (liquid titanium tetrachloride) at the bottom of the tower can automatically flow into the reboiler 3, the top of the reboiler 3 is communicated with the low-boiling-point distillate separating tower 2 in a gas phase manner, and the supply of the gas-phase product in the tower is ensured.
The reboiler 3 adopts vertical electrical heating cauldron, heats the vaporization to liquid titanium tetrachloride material, in order to guarantee gaseous phase component in the low boiling point distillate knockout tower 2, reboiler 3's heating zone is located the liquid level all the time below, reboiler 3's bottom is provided with the drain, regularly carries out the blowdown, reboiler 3's upper portion overflow discharge gate with tower cauldron product tank 4 links to each other, thereby need not to control the liquid level in the reboiler 3, simple easy operation.
The tower kettle product tank 4 is provided with a tower kettle product tank liquid level meter 14 for monitoring the liquid level of titanium tetrachloride liquid in the tower kettle product tank 4 in real time, an outlet pipeline at the bottom of the tower kettle product tank 4 is provided with a tower kettle product conveying pump 5 for conveying tower kettle products in the tower kettle product tank 4, further, a downstream pipeline of the tower kettle product conveying pump 5 is provided with a tower kettle product control valve 6, the tower kettle product control valve 6 and the tower kettle product tank liquid level meter 14 are in linkage control, and the controller controls the opening and closing of the tower kettle product control valve 6 according to a liquid level signal of the tower kettle product tank liquid level meter 14, so that titanium tetrachloride in the tower kettle product tank 4 is stably conveyed and returned to the low-boiling-point impurity separation system 17.
The top of the low-boiling-point distillate separating tower 2 is provided with a gas phase pipeline connected with a top product condenser 8, a liquid outlet of the top product condenser 8 is connected with an inlet of a top product tank 9, and gas phase products in the low-boiling-point distillate separating tower 2 enter the top product tank 9 for storage after condensation.
The overhead product tank 9 is provided with an overhead product tank liquid level gauge 13 and an overhead product reflux pump 10, the overhead product tank liquid level gauge 13 is used for detecting the liquid level of overhead products (namely high-concentration low-boiling byproducts) in the overhead product tank 9 in real time, the overhead product reflux pump 10 and the overhead product tank liquid level gauge 13 are controlled in a linkage manner, and a controller controls the on-off of the overhead product reflux pump 10 according to the liquid level signal of the overhead product tank liquid level gauge 13, so that continuous and stable conveying of overhead products is ensured. The downstream pipeline of the overhead product reflux pump 10 is divided into two branches, namely a first branch connected with the upper reflux port of the low-boiling-point distillate separating tower 2 and a second branch connected with the byproduct storage tank 16, wherein the first branch is provided with an overhead product reflux control valve 11, the second branch is provided with a high-concentration low-boiling-point byproduct control valve 12, the overhead product reflux pump 10 continuously reflux part of overhead product in the overhead product tank 9 to the low-boiling-point distillate separating tower 2 through the overhead product reflux control valve 11 as the liquid phase supplement of the low-boiling-point distillate separating tower 2, and the other part of overhead product is sent to the byproduct storage tank 16 for storage through the high-concentration low-boiling-point byproduct control valve 12.
Example 2: the difference between this embodiment and embodiment 1 is that the feed line of the low boiling point distillate separating column 2 and the outlet line at the bottom of the bottom product tank 4 meet at the feed product preheater 7 downstream of the bottom product control valve 6, and the heat of the bottom product is used to preheat the refined low boiling point distillate entering the separating column, so as to fully utilize the system waste heat and reduce the power consumption of the whole system. The refined low boiling point distillate and the tower kettle product are subjected to countercurrent heat exchange in the feed product preheater 7 so as to achieve the optimal heat exchange effect. In general, the temperature of the tower kettle product is more than 160 ℃, the feeding temperature of the refined low-boiling point distillate can be raised to more than 120 ℃, and the system saves 20% of power cost. Other structures and connection relations of this embodiment are the same as those of embodiment 1.
The above embodiments are only for illustrating the technical solution of the present invention and not for limiting it, and it should be understood by those skilled in the art that modifications and equivalents may be made to the specific embodiments of the present invention with reference to the above embodiments, and any modifications and equivalents not departing from the spirit and scope of the present invention are within the scope of the claims appended hereto.
Claims (8)
1. A recovery system for refining titanium tetrachloride in a low boiling distillate, characterized by: the refined low-boiling point distillate is subjected to high-efficiency separation to obtain high-concentration low-boiling point byproducts, and the loss of titanium tetrachloride is reduced, wherein the high-concentration low-boiling point byproducts comprise a low-boiling point distillate separating tower, a reboiler, a tower bottom product tank, a tower top product condenser and a tower top product tank; the tower body of the low boiling point distillate separating tower is connected with a refined low boiling point distillate feeding pipeline, the tower bottom is communicated with the lower part of the reboiler so that a liquid phase product at the tower bottom automatically flows into the reboiler, the top of the reboiler is communicated with the gas phase of the low boiling point distillate separating tower, an overflow discharge port at the upper part of the reboiler is connected with a tower kettle product tank, and an outlet pipeline of the tower kettle product tank is connected with a low boiling point impurity separating system in the titanium tetrachloride refining process; the top of the low boiling point distillate separating tower is connected with the top product tank through a pipeline and the top product condenser so as to separate and collect gas phase products at the top of the tower, and an outlet pipeline of the top product tank is connected with two branches which are respectively connected with a reflux port and a byproduct storage tank at the upper part of the low boiling point distillate separating tower.
2. A system for recovering titanium tetrachloride from a refined low boiling distillate as claimed in claim 1, wherein: and the outlet pipeline of the tower kettle product tank and the low-boiling-point distillate feeding pipeline are intersected in a feeding product preheater, and the tower kettle product conveyed by the outlet pipeline of the tower kettle product tank preheats the low-boiling-point distillate in the low-boiling-point distillate feeding pipeline.
3. A system for recovering titanium tetrachloride from a refined low boiling distillate as claimed in claim 1, wherein: and a feeding product control valve and a feeding flowmeter which are controlled in an interlocking manner are arranged on the low-boiling-point distillate feeding pipeline.
4. A system for recovering titanium tetrachloride from a refined low boiling distillate as claimed in claim 1, wherein: the tower kettle product tank is provided with a tower kettle product tank liquid level meter, and an outlet pipeline of the tower kettle product tank is provided with a tower kettle product control valve which is in linkage control with the tower kettle product tank liquid level meter.
5. A system for recovering titanium tetrachloride from a refined low boiling distillate as defined in claim 4, wherein: and a tower kettle product conveying pump is arranged on an outlet pipeline of the tower kettle product tank.
6. A system for recovering titanium tetrachloride from a refined low boiling distillate as claimed in claim 1, wherein: the tower top product tank is provided with a tower top product tank liquid level meter, and an outlet pipeline of the tower top product tank is provided with a tower top product reflux pump which is controlled by the tower top product tank liquid level meter in an interlocking way.
7. A system for recovering titanium tetrachloride from a refined low boiling distillate as defined in claim 6, wherein: the outlet of the tower top product reflux pump is respectively connected with a first branch provided with a tower top product reflux control valve and a second branch provided with a high-concentration low-boiling-point byproduct control valve, the first branch is connected with a reflux port at the upper part of the low-boiling-point distillate separation tower, and the second branch is connected with a byproduct storage tank.
8. A system for recovering titanium tetrachloride from a purified low boiling distillate according to any one of claims 1 to 6, wherein: the low boiling point distillate separating tower is a packed tower with a packing height of more than 20 meters.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202210420663.3A CN114832417B (en) | 2022-04-21 | 2022-04-21 | Titanium tetrachloride recovery system in refined low boiling point distillate |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202210420663.3A CN114832417B (en) | 2022-04-21 | 2022-04-21 | Titanium tetrachloride recovery system in refined low boiling point distillate |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN114832417A CN114832417A (en) | 2022-08-02 |
| CN114832417B true CN114832417B (en) | 2024-02-02 |
Family
ID=82565924
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202210420663.3A Active CN114832417B (en) | 2022-04-21 | 2022-04-21 | Titanium tetrachloride recovery system in refined low boiling point distillate |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN114832417B (en) |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2007302522A (en) * | 2006-05-12 | 2007-11-22 | Toho Titanium Co Ltd | Method of refining titanium tetrachloride and refiner used for the same |
| CN201596372U (en) * | 2009-11-20 | 2010-10-06 | 天津渤天化工有限责任公司 | Rectifying tower for industrial test of removing vanadium with aluminum powder |
| CN110280037A (en) * | 2019-08-08 | 2019-09-27 | 中国恩菲工程技术有限公司 | Titanium tetrachloride rectifier unit |
| CN211215494U (en) * | 2019-08-08 | 2020-08-11 | 中国恩菲工程技术有限公司 | Titanium tetrachloride rectifying device |
| CN212467172U (en) * | 2020-04-21 | 2021-02-05 | 河南佰利联新材料有限公司 | System for separating silicon tetrachloride in crude titanium tetrachloride |
-
2022
- 2022-04-21 CN CN202210420663.3A patent/CN114832417B/en active Active
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2007302522A (en) * | 2006-05-12 | 2007-11-22 | Toho Titanium Co Ltd | Method of refining titanium tetrachloride and refiner used for the same |
| CN201596372U (en) * | 2009-11-20 | 2010-10-06 | 天津渤天化工有限责任公司 | Rectifying tower for industrial test of removing vanadium with aluminum powder |
| CN110280037A (en) * | 2019-08-08 | 2019-09-27 | 中国恩菲工程技术有限公司 | Titanium tetrachloride rectifier unit |
| CN211215494U (en) * | 2019-08-08 | 2020-08-11 | 中国恩菲工程技术有限公司 | Titanium tetrachloride rectifying device |
| CN212467172U (en) * | 2020-04-21 | 2021-02-05 | 河南佰利联新材料有限公司 | System for separating silicon tetrachloride in crude titanium tetrachloride |
Also Published As
| Publication number | Publication date |
|---|---|
| CN114832417A (en) | 2022-08-02 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN101748037B (en) | Special grade edible alcohol six-tower difference pressure distilling device and process thereof | |
| CN101153257B (en) | Five-tower two-grade difference pressure distillation equipment for senior edible ethanol and technique thereof | |
| CN114832417B (en) | Titanium tetrachloride recovery system in refined low boiling point distillate | |
| CN105502409B (en) | The method and device of infinite reflux rectification and purification optical fiber level silicon tetrachloride | |
| CN107837556B (en) | Operation control method of dividing wall rectifying tower | |
| CN210495287U (en) | Novel distillation tower without extracting industrial alcohol | |
| CN216777948U (en) | Intermittent purification device for propylene glycol methyl ether | |
| CN115140791A (en) | Device and process for recovering and extracting furfural from process wastewater | |
| CN107141199A (en) | Methanol mother liquor is without refluxed cryogenic rectificating method and equipment | |
| CN111018021B (en) | Hydrogen sulfide acidic water purification method based on side line and tower kettle reflux ratio control | |
| CN213680463U (en) | VCM high-boiling-point substance purification device | |
| CN215440045U (en) | High-concentration phenol-ammonia wastewater double-tower energy-saving treatment system | |
| CN114671405A (en) | Process for preparing high-purity hydrogen chloride from by-product hydrochloric acid in methane chloride process | |
| CN211645081U (en) | Novel EG is retrieved in succession device | |
| CN205933695U (en) | Methyl alcohol mother liquor does not have backward flow low temperature rectification plant | |
| CN210030511U (en) | Production device of dimethyl sulfone | |
| CN113975845A (en) | Extractive distillation device for dehydrating low-concentration acetonitrile solution and control method | |
| CN218665471U (en) | Waste hydrochloric acid treatment device | |
| CN112933638A (en) | 8N electronic grade high-purity ammonia rectification system and quality control method thereof | |
| CN110393938A (en) | A kind of novel destilling tower for being not required to extract industrial alcohol | |
| CN105693754A (en) | Organosilicone high-boiling-component removing and low-boiling-component removing tower pressure-variable thermal coupling distillation method and equipment | |
| CN220283634U (en) | Material comprehensive treatment system for polysilicon rectification process | |
| CN113372297A (en) | Method for treating mixed liquid containing ethanol, piperazine, n-hexanol and water | |
| CN1091414A (en) | The extraction rectification technique that ethanol concentrates and reclaims | |
| CN218357427U (en) | High-purity octafluorocyclobutane rectification system |
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 | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant |