CN209940875U - Monomer separation economizer system - Google Patents
Monomer separation economizer system Download PDFInfo
- Publication number
- CN209940875U CN209940875U CN201920479899.8U CN201920479899U CN209940875U CN 209940875 U CN209940875 U CN 209940875U CN 201920479899 U CN201920479899 U CN 201920479899U CN 209940875 U CN209940875 U CN 209940875U
- Authority
- CN
- China
- Prior art keywords
- rectifying tower
- tower
- rectifying
- reflux
- reboiler
- 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
Classifications
-
- 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
-
- 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
- Y02P20/50—Improvements relating to the production of bulk chemicals
Abstract
The utility model relates to a monomer separation energy-saving system, the top of a rectifying tower is connected with a thermal coupling reboiler through a pipeline, the thermal coupling reboiler is connected with a reflux groove of the rectifying tower through a coupling reflux pump, and the bottom of the rectifying tower is connected to a discharged product area; and one part of a reflux groove of the rectifying tower passes through a reflux pump of the rectifying tower, is connected with the first rectifying tower, the other part of the reflux groove is connected with the second rectifying tower, and the bottom of the second rectifying tower is connected to a discharged product area. The utility model discloses fully adopt thermal coupling rectification technology, with the whole heat sources as rectifying column two tower cauldron thermal coupling reboilers of rectifying column top gas phase material, rational utilization the latent heat of rectifying column top gas phase steam material, reduce steam consumption 30% on year by year, reduce circulating water quantity 40%.
Description
Technical Field
The utility model relates to a monomer separation economizer system belongs to organosilicon production technical field.
Background
The methyl chlorosilane mixed monomer comprises dimethyl dichlorosilane (dimethyl for short), methyl trichlorosilane (methyl for short), trimethyl monochlorosilane (trimethyl for short), methyl dichlorosilane (methyl for short contains hydrogen), high boiling point substances and low boiling point substances. As is well known, the synthesis of methyl chlorosilane monomers at home and abroad generally adopts a direct method synthesis process, silicon powder and chloromethane are used as raw materials, a methyl chlorosilane mixed monomer is directly synthesized under the action of a copper catalyst system, the methyl chlorosilane mixed monomer is rectified and separated to obtain a main target product dimethyl, and byproducts, namely methyl, methyl contain hydrogen, trimethyl, high-boiling residues and low-boiling residues. Dimethyl is hydrolyzed and cracked to produce various organosilicon intermediates, namely oligomeric methyl siloxane or alkoxy silane, and the oligomeric methyl siloxane or alkoxy silane is further processed into various organosilicon downstream products.
The purity requirement of dimethyl as a raw material is quite high when silicone oil and silicone rubber are prepared, and particularly, the purity of the dimethyl as a key raw material is required to reach more than 99.95 percent when high-temperature vulcanized silicone rubber is prepared. However, the crude monomer components are complex, the boiling point difference is small, and the dimethyl product rectified by the domestic organic silicon manufacturers at present has low purity and large energy consumption compared with the foreign advanced level, so that the market competitiveness of the product is low. The energy consumption for separating the methyl chlorosilane mixed monomer accounts for more than 80 percent of the whole organic silicon device, so that the related technical research on the separation and purification process of the methyl chlorosilane mixed monomer is necessary, and the energy consumption is reduced as much as possible under the condition of ensuring the product quality.
Disclosure of Invention
The utility model provides an energy-conserving technology of monomer separation and system solves prior art difficult the carrying, overcomes among the monomer separation rectifying column one and rectifying column two steam and the circulating water quantity great, the energy consumption is higher gets the problem.
The technical terms used in the utility model explain:
coarse high-boiling residues: a component having a boiling point of greater than 70.2 ℃ under standard conditions;
a first rectifying tower: a column for removing high boilers;
and (2) rectifying tower II: a tower for removing the component with the boiling point lower than that of the dimethyldichlorosilane;
crude dimethyldichlorosilane: a crude product of a dimethyldichlorosilane product;
crude monomer: the main components of the methyl chlorosilane mixed monomer are methyl trichlorosilane, dimethyl dichlorosilane, trimethyl monochlorosilane, methyl dichlorosilane, silicon tetrachloride and the like;
the utility model discloses technical scheme as follows:
a monomer separation energy-saving process and a system thereof are disclosed, wherein a crude monomer enters a first rectifying tower, a first rectifying tower kettle extracts crude high-boiling materials, high-boiling gas phase materials removed from the tower top completely enter a second rectifying tower kettle thermal coupling reboiler as a heat source, the materials are conveyed out of the thermal coupling reboiler and then enter a reflux groove of the rectifying tower through a pump, one part of the materials in the reflux groove are conveyed through the pump to return to the top of the first rectifying tower as tower reflux, and the other part of the materials are used as second rectifying tower feed; and the second tower kettle of the rectifying tower adopts a second reboiler steam reboiler as a supplementary heat source, the gas phase at the tower top is condensed by a condenser and enters a reflux tank, and the material in the reflux tank is conveyed by a pump to partially return to the tower top as tower reflux, and the other part of the material enters a subsequent rectifying tower for separation.
The temperature of the top of the rectifying tower is controlled at 110-125 ℃, and the pressure of the top of the rectifying tower is controlled at 0.20-0.35 MPa.
The temperature of the second tower kettle of the rectifying tower is controlled to be 85-100 ℃, and the pressure of the tower kettle is controlled to be 0.05-0.18 MPa.
And the gas phase material at the top of the first rectifying tower is completely used as a heat source of a thermal coupling reboiler at the tower bottom of the second rectifying tower 2, and the insufficient gas phase material is supplemented by a second steam reboiler of the second reboiler rectifying tower.
The gas phase temperature at the top of the first rectifying tower is 20-25 ℃ higher than the temperature of the bottom of the second rectifying tower.
The first rectifying tower is a pressurized rectifying tower, and the second rectifying tower is a low-pressure rectifying tower.
The first rectifying section of the rectifying tower is a packed tower or a plate tower, and the stripping section is a plate tower; and the second rectifying tower is a packed tower.
On the basis of the process, the utility model provides a monomer separation energy-saving system, the top of a rectifying tower is connected with a thermal coupling reboiler through a pipeline, the thermal coupling reboiler is connected with a reflux groove of the rectifying tower through a coupling reflux pump, and the bottom of the rectifying tower is connected to a discharged product area;
and one part of a reflux groove of the rectifying tower passes through a reflux pump of the rectifying tower, is connected with the first rectifying tower, the other part of the reflux groove is connected with the second rectifying tower, and the bottom of the second rectifying tower is connected to a discharged product area.
The top of the rectifying tower is also connected with a condenser of the rectifying tower through a pipeline, and the condenser of the rectifying tower is connected with a reflux groove of the rectifying tower.
The top of the second rectifying tower is connected with a second condenser of the rectifying tower, the second condenser of the rectifying tower is connected with a second reflux groove of the rectifying tower, and the second reflux groove of the rectifying tower is connected to the second rectifying tower through a second reflux pump of the rectifying tower.
The bottoms of the first rectifying tower and the second rectifying tower are respectively provided with a reboiler of the rectifying tower and a steam reboiler of the second rectifying tower.
The utility model discloses simple process technology, control condition are rigorous, have good application prospect and using value, compare its good effect with prior art and lie in: in the conventional process, the reboilers of the first rectifying tower and the second rectifying tower are heated by steam, and the tower top is condensed by circulating water; the utility model discloses make full use of material component and characteristic adopt thermal coupling rectification technology, with a rectifying column pressurization operation, improve rectifying column one top of the tower temperature, with the whole heat sources as rectifying column two tower cauldron thermal coupling reboilers of top of the tower high temperature gaseous phase material, the latent heat of rational utilization rectifying column one top of the tower gaseous phase steam material has both reduced the steam consumption of rectifying column two, has reduced the quantity of rectifying column circulating water again.
Drawings
FIG. 1 is a monomer separation energy-saving system, wherein 1, a first rectifying tower; 2, a second rectifying tower; 3, a reboiler of the rectifying tower; 4, a condenser of the rectifying tower; 5, a reflux groove of the rectifying tower; 6 thermally coupled reboiler; 7, a second condenser of the rectifying tower; 8, a second reflux groove of the rectifying tower; 9, a second steam reboiler of the rectifying tower; 10 a reflux pump of the rectifying tower; 11 a second reflux pump of the rectifying tower; 12 a crude monomer feed pipe; 13 a coarse high-boiling-point substance discharge pipe; 14 a discharge pipe of methyltrichlorosilane and a component having a lower boiling point than that of methyltrichlorosilane; 15 a coarse dimethyldichlorosilane discharge pipe; a reflux pump is coupled to 16.
Detailed Description
The present invention will be further described with reference to the accompanying drawings and examples, but the following examples are only preferred embodiments of the present invention, and not all of them. Based on the embodiments in the implementation, other embodiments obtained by those skilled in the art without any creative work belong to the protection scope of the present invention.
The first embodiment is as follows:
the method comprises the following steps of (1) enabling an organosilicon crude monomer 12 to enter a first rectifying tower 1 at a flow rate of 25.5t/h, extracting crude high boiling 13 from a first tower kettle of the rectifying tower, extracting dimethyl and components with a boiling point lower than that of dimethyl from the top of the rectifying tower, enabling all gas phase materials at the top of the rectifying tower to enter a thermally coupled kettle reboiler 6 of a second tower of the rectifying tower to serve as a heat source, conveying the gas phase materials at the top of the rectifying tower to enter a reflux groove 5 of the rectifying tower through a coupled reflux pump 16 after coming out of the thermally coupled reboiler 6, conveying one part of the materials in the reflux groove 5 of the rectifying tower to serve as tower reflux to return to the top of the first rectifying tower; the temperature of the top of the rectifying tower is controlled at 120 ℃, and the pressure of the top of the rectifying tower is controlled at 0.30 MPa.
The top of the second rectifying tower 2 is used for extracting monomethyl trichlorosilane and components 14 with boiling points lower than that of the monomethyl trichlorosilane, the bottom of the second rectifying tower 2 is used for extracting crude dimethyldichlorosilane products 15, the bottom of the second rectifying tower 2 is used for adopting a second reboiler, a second steam reboiler 9 of the rectifying tower as a supplementary heat source, the gas phase at the top of the second rectifying tower is condensed by a second rectifying tower condenser 7 and enters a second rectifying tower reflux groove 8, materials in the second rectifying tower reflux groove 8 are conveyed by a second rectifying tower reflux pump 11, one part of the materials are used as tower reflux and return to the top of the second rectifying tower 2, the other part of the materials are used for entering a subsequent rectifying tower for separation, the temperature of the second rectifying tower is controlled at 97 ℃, and the pressure of the bottom of the second.
Under the same throughput and product quality circumstances, conventional technology with the utility model discloses the energy consumption contrast data of technology and system as follows:
through the comparison of the data, the heat consumption is only 67.68% of that of the conventional process and the load of the condenser is 59.62% of that of the conventional process under the condition of the same treatment capacity and product quality by adopting the thermal coupling process and the thermal coupling system, so that the consumption of energy and circulating water is greatly reduced.
Example two:
the method comprises the following steps of (1) enabling an organosilicon crude monomer 12 to enter a first rectifying tower 1 at a flow rate of 18t/h, extracting crude high boiling 13 from a first tower kettle of the rectifying tower, extracting dimethyl and components with a boiling point lower than that of dimethyl from the top of the rectifying tower, enabling all gas phase materials at the top of the rectifying tower to enter a second tower kettle thermal coupling reboiler 6 of the rectifying tower to serve as a heat source, conveying the gas phase materials at the top of the rectifying tower to enter a reflux groove 5 of the rectifying tower through a coupling reflux pump 16 after coming out of the thermal coupling reboiler 6, conveying one part of the materials in the reflux groove 5 of the rectifying tower to serve as tower reflux to return to the top of the first rectifying tower 1; the temperature of the top of the rectifying tower is controlled at 115 ℃, and the pressure of the top of the rectifying tower is controlled at 0.25 MPa.
The top of the second rectifying tower 2 is used for extracting monomethyl trichlorosilane and components 14 with boiling points lower than that of the monomethyl trichlorosilane, the bottom of the second rectifying tower 2 is used for extracting crude dimethyldichlorosilane products 15, the bottom of the second rectifying tower 2 is used for adopting a second reboiler, a second steam reboiler 9 of the rectifying tower as a supplementary heat source, the gas phase at the top of the second rectifying tower is condensed by a second rectifying tower condenser 7 and enters a second rectifying tower reflux groove 8, materials in the second rectifying tower reflux groove 8 are conveyed by a second rectifying tower reflux pump 11, one part of the materials are used as tower reflux and return to the top of the second rectifying tower 2, the other part of the materials are used for entering a subsequent rectifying tower for separation, the temperature of the second rectifying tower is controlled at 95 ℃, and the pressure of the bottom of the second.
Under the same throughput and product quality circumstances, conventional technology with the utility model discloses the energy consumption contrast data of technology and system as follows:
through the comparison of the data, the heat consumption is only 66.57 percent of that of the conventional process and the load of the condenser is 59.65 percent of that of the conventional process under the condition of the same treatment capacity and product quality by adopting the thermal coupling process and the thermal coupling system, so that the consumption of energy and circulating water is greatly reduced.
Example three:
the method comprises the following steps of (1) enabling an organosilicon crude monomer 12 to enter a first rectifying tower 1 at a flow rate of 30t/h, extracting crude high boiling 13 from a first tower kettle of the rectifying tower, extracting dimethyl and components with a boiling point lower than that of dimethyl from the top of the rectifying tower, enabling all gas phase materials at the top of the rectifying tower to enter a second tower kettle thermal coupling reboiler 6 of the rectifying tower to serve as a heat source, conveying the gas phase materials at the top of the rectifying tower to enter a reflux groove 5 of the rectifying tower through a coupling reflux pump 16 after coming out of the thermal coupling reboiler 6, conveying one part of the materials in the reflux groove 5 of the rectifying tower to serve as tower reflux to return to the top of the first rectifying tower 1; the temperature of the top of the rectifying tower is controlled at 122 ℃, and the pressure of the top of the rectifying tower is controlled at 0.32 MPa.
The top of the second rectifying tower 2 is used for extracting monomethyl trichlorosilane and components 14 with boiling points lower than that of the monomethyl trichlorosilane, the bottom of the second rectifying tower 2 is used for extracting crude dimethyldichlorosilane products 15, the bottom of the second rectifying tower 2 is used for adopting a second reboiler, a second steam reboiler 9 of the rectifying tower as a supplementary heat source, the gas phase at the top of the second rectifying tower is condensed by a second rectifying tower condenser 7 and enters a second rectifying tower reflux groove 8, materials in the second rectifying tower reflux groove 8 are conveyed by a second rectifying tower reflux pump 11, one part of the materials are used as tower reflux and return to the top of the second rectifying tower 2, the other part of the materials are used for entering a subsequent rectifying tower for separation, the temperature of the second rectifying tower is controlled at 99 ℃, and the pressure of the bottom of the second.
Under the same throughput and product quality circumstances, conventional technology with the utility model discloses the energy consumption contrast data of technology and system as follows:
through the comparison of the data, the thermal coupling process and the thermal coupling system have the advantages that under the condition of the same treatment capacity and product quality, the heat consumption is only 66.09% of that of the conventional process, the load of a condenser is 60.13% of that of the conventional process, and the consumption of energy and circulating water is greatly reduced.
Example four:
a monomer separation energy-saving system, the top of a rectifying tower 1 is connected with a thermal coupling reboiler 6 through a pipeline, the thermal coupling reboiler 6 is connected with a reflux groove 5 of the rectifying tower through a coupling reflux pump 16, and the bottom of the rectifying tower 1 is connected with a discharged product area;
and the reflux groove 5 of the rectifying tower is connected with the first rectifying tower 1 through a reflux pump 10 of the rectifying tower, one way is connected with the second rectifying tower 2, and the bottom of the second rectifying tower 2 is connected to a discharged product area.
The top of the first rectifying tower 1 is also connected with a first rectifying tower condenser 4 through a pipeline, and the first rectifying tower condenser 4 is connected with a reflux groove 5 of the rectifying tower.
The top of the second rectifying tower 2 is connected with a second rectifying tower condenser 7, the second rectifying tower condenser 7 is connected with a second rectifying tower reflux groove 8, and the second rectifying tower reflux groove 8 is connected to the second rectifying tower 2 through a second rectifying tower reflux pump 11.
And the bottoms of the first rectifying tower 1 and the second rectifying tower 2 are respectively provided with a reboiler 3 of the rectifying tower and a reboiler 9 of the second steam of the rectifying tower.
Claims (4)
1. A monomer separation energy-saving system is characterized in that the top of a rectifying tower I (1) is connected with a thermal coupling reboiler (6) through a pipeline, the thermal coupling reboiler (6) is connected with a reflux groove (5) of the rectifying tower through a coupling reflux pump (16), and the bottom of the rectifying tower I (1) is connected to a discharged product area;
a reflux groove (5) of the rectifying tower is connected with a first rectifying tower (1) on the one way through a reflux pump (10) of the rectifying tower, and is connected with a second rectifying tower (2) on the other way, and the bottom of the second rectifying tower (2) is connected to a discharged product area.
2. The monomer separation energy-saving system according to claim 1, wherein the top of the rectifying tower I (1) is further connected with a rectifying tower-condenser (4) through a pipeline, and the rectifying tower-condenser (4) is connected with a reflux groove (5) of the rectifying tower.
3. The monomer separation energy-saving system according to claim 1, wherein the top of the second rectifying tower (2) is connected with a second rectifying tower condenser (7), the second rectifying tower condenser (7) is connected with a second rectifying tower reflux tank (8), and the second rectifying tower reflux tank (8) is connected to the second rectifying tower (2) through a second rectifying tower reflux pump (11).
4. The monomer separation energy-saving system according to claim 1, wherein a rectifying tower reboiler (3) and a rectifying tower secondary steam reboiler (9) are respectively arranged at the bottoms of the rectifying tower I (1) and the rectifying tower II (2).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201920479899.8U CN209940875U (en) | 2019-04-10 | 2019-04-10 | Monomer separation economizer system |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201920479899.8U CN209940875U (en) | 2019-04-10 | 2019-04-10 | Monomer separation economizer system |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN209940875U true CN209940875U (en) | 2020-01-14 |
Family
ID=69127258
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201920479899.8U Active CN209940875U (en) | 2019-04-10 | 2019-04-10 | Monomer separation economizer system |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN209940875U (en) |
-
2019
- 2019-04-10 CN CN201920479899.8U patent/CN209940875U/en active Active
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN101786630B (en) | Trichlorosilane three-tower differential pressure coupling energy-saving rectifying and purifying system and operating method | |
| CN217828930U (en) | Crude monomer rectification energy-saving device | |
| CN101704524B (en) | Production device and method of high purity trichlorosilane by using heat pump distillation | |
| CN101857606B (en) | Methyl chlorosilane parallel double-effect distillation method | |
| CN101130484B (en) | Pressure-reducing flow-reversing dual-purpose distillation method and apparatus for refining crude methanol | |
| CN101538045A (en) | Trichlorosilane differential pressure coupling rectification system and operation method thereof | |
| CN107032959A (en) | A kind of heat pump and the methanol rectification method of multiple-effect coupling | |
| CN217939189U (en) | Coarse monomer separation energy-saving device | |
| CN217828931U (en) | Coarse monomer separation device | |
| CN205616824U (en) | Organosilicon takes off highly and takes off low tower vary voltage thermal coupling rectification plant | |
| CN109224492A (en) | Organic silicon monomer is from backheat rectifier unit and method | |
| CN110041359A (en) | A kind of monomer separation energy saving technique and system | |
| CN209940875U (en) | Monomer separation economizer system | |
| CN115282625A (en) | Crude monomer separation method and device | |
| CN115228118A (en) | Energy-saving method and device for rectifying crude monomer | |
| CN209361889U (en) | Organic silicon monomer is from backheat rectifier unit | |
| CN205653378U (en) | Dimethyl dichlorosilane's purification system | |
| CN209940873U (en) | Separation and purification system of methyl chlorosilane mixed monomer | |
| CN110041358B (en) | Coarse monomer separation process and system | |
| CN109438500B (en) | Device and method for separating methyl chlorosilane by using internal thermally coupled rectifying tower | |
| CN111298470B (en) | Organic silicon monomer rectification heat integration method | |
| CN102134080B (en) | Heat-pump energy-saving separating device for extracting trichlorosilane by adopting static mixing booster and method | |
| CN209940874U (en) | Coarse monomer separation system | |
| CN209940872U (en) | Monomer rectification system | |
| CN115282626A (en) | Crude monomer separation method |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| GR01 | Patent grant | ||
| GR01 | Patent grant |