CN212174853U - Catalyst system for PBT production - Google Patents
Catalyst system for PBT production Download PDFInfo
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- CN212174853U CN212174853U CN202020372128.1U CN202020372128U CN212174853U CN 212174853 U CN212174853 U CN 212174853U CN 202020372128 U CN202020372128 U CN 202020372128U CN 212174853 U CN212174853 U CN 212174853U
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Abstract
The utility model relates to a catalyst system is used in PBT production, the bucket pump export of catalyst bucket links to each other with the feed inlet of catalyst jar, the air inlet at catalyst tank top links to each other with the nitrogen gas pipe, the gas vent links to each other with the blow-down pipe, the middle part entry that catalyst bleeder valve and metering pipe were passed through to the bottom of catalyst jar links to each other, the level gauge is installed to one side of metering pipe, catalyst reflux valve and catalyst back flow and catalyst jar's top backward flow mouth are passed through at the top of metering pipe and are linked to each other, the sight glass with catalyst jar lower part parallel and level is installed to catalyst reflux valve top, catalyst baiting valve and catalyst metering pump's entry is passed through in the bottom export of metering pipe and is linked to each other, catalyst heater's material export links to each other through catalyst bottom notes pipe and catalyst bottom notes entry of valve. The catalyst injection of the system is not easy to hydrolyze or block the pipeline, and the feeding condition of the catalyst can be accurately mastered.
Description
Technical Field
The utility model relates to a PBT production system especially relates to a catalyst system is used in PBT production, belongs to polyester production facility technical field.
Background
Polybutylene terephthalate (PBT) belongs to polyester series and is prepared by polycondensation of 1, 4-Butanediol (BDO) and terephthalic acid (PTA) or terephthalate (DMT). The catalyst for PBT polymerization production is tetrabutyl titanate which is easy to hydrolyze in water and lose activity, and simultaneously generates titanium hydrate, so that a pipeline is easy to block, and the addition of the catalyst is influenced. Tetrabutyl titanate is both an esterification catalyst and a polycondensation catalyst, and is generally added from the esterification reaction stage, but the esterification reaction generates a large amount of water.
The current catalyst preparation methods are two: one method is that a certain amount of catalyst and fresh 1, 4-Butanediol (BDO) are mixed and prepared in a preparation tank, the prepared mixture is transferred to a finished product tank, and then the mixture is conveyed by a pump and mixed with high-temperature BDO recycled by a process tower and then added into an esterification kettle. The method can prevent the prepared catalyst solution from entering the esterification kettle at normal temperature and being vaporized at high temperature suddenly, but the fresh BDO and the high-temperature recycled BDO contain water, so that the catalyst is easy to hydrolyze after long service time, blocks pipelines and influences production.
The other is as follows: the mixture is not mixed and prepared, and is directly pumped into a tank by a barrel pump and then is conveyed to an esterification kettle by a metering pump. Because the usage amount of the catalyst is calculated by PPM, the usage amount is very small, and the liquid level in the preparation tank is basically unchanged after each addition. Once the metering pump is out of order, such as gear slippage, or the catalyst is not added successfully due to other reasons, the catalyst cannot be found, and the instability of the production line is often caused, so that the product quality is influenced.
SUMMERY OF THE UTILITY MODEL
An object of the utility model is to overcome the problem that exists among the prior art, provide a catalyst system for PBT production, the catalyst need not mix with 1, 4-butanediol and prepares, is difficult to hydrolyze or block up the pipeline, and can ensure that the catalyst adds successfully, guarantees the continuous stable production of production line.
In order to solve the technical problem, the utility model discloses a catalyst system for PBT production, including catalyst bucket, catalyst jar and esterification reaction cauldron, the built-in barrel pump that has in the catalyst bucket, the export of barrel pump through barrel pump output tube with the feed inlet of catalyst jar links to each other, the air inlet at catalyst jar top is passed through nitrogen gas admission valve and is linked to each other with the export of nitrogen gas pipe, the gas vent at catalyst jar top passes through the atmospheric valve and links to each other with the blow-down pipe, esterification reaction cauldron's bottom is installed and is annotated the valve with the catalyst, the bottom of catalyst jar is installed and is had the catalyst bleeder valve, and the export of catalyst bleeder valve links to each other with the middle part entry of metering tube, and one side of metering tube is installed the metering tube level gauge, and the top export of metering tube links to each other with the top backward flow mouth of catalyst jar through catalyst backward flow valve and catalyst, and the height of the sight glass is flush with the lower part of the catalyst tank, the outlet at the bottom of the metering pipe is connected with the inlet of the catalyst metering pump through a catalyst discharge valve, the outlet of the catalyst metering pump is connected with the inlet of the catalyst filter, the outlet of the catalyst filter is connected with the material inlet of the catalyst heater, and the material outlet of the catalyst heater is connected with the inlet of the catalyst bottom injection valve through a catalyst bottom injection pipe.
Compared with the prior art, the utility model discloses following beneficial effect has been obtained: the catalyst tetrabutyl titanate is in a liquid state and is easy to convey, and by utilizing the characteristic, tetrabutyl titanate in the catalyst barrel is pumped out by a barrel pump and enters the catalyst tank for storage through an output pipe of the barrel pump, and the gas phase space of the catalyst tank is filled with nitrogen from a nitrogen pipe to protect the catalyst. Firstly opening a nitrogen gas inlet valve and a vent valve, discharging air in a catalyst tank through a vent pipe by using nitrogen, then setting the pressure of the catalyst tank to be automatic, wherein the set pressure of the catalyst tank is 2kPa, when the pressure in the catalyst tank is lower than 1 kPa, the nitrogen gas inlet valve is automatically opened, and when the pressure in the catalyst tank is higher than 3 kPa, the nitrogen gas inlet valve is automatically closed; when the pressure in the catalyst tank is higher than 5 kPa, the vent valve automatically opens and closes to the set pressure. When the catalyst is added, a catalyst discharge valve and a catalyst reflux valve are opened, the catalyst in a catalyst tank enters a metering pipe by virtue of liquid level difference and flows upwards, when the material is displayed in a viewing mirror, the catalyst discharge valve is closed, then a catalyst discharge valve is opened, a catalyst metering pump is started, the catalyst in the metering pipe is pumped out and metered, the preparation by BDO is not needed, and meanwhile, in order to prevent the catalyst from being vaporized at high temperature, the catalyst sent out by the catalyst metering pump is preheated to 120-170 ℃ by a catalyst heater and is sent into an esterification reaction kettle. Because the esterification reaction can generate a large amount of water in the esterification reaction kettle, the density of the water is less than that of the PBT; fresh catalyst is injected from the bottom of the esterification reaction kettle through a catalyst bottom injection pipe and a catalyst bottom injection valve, so that the contact of the catalyst and water can be avoided. Because the filling amount of the catalyst is too small, the catalyst tank cannot observe the micro fluctuation of the liquid level, the system converts the micro fluctuation of the liquid level which cannot be observed by the catalyst tank into the obvious liquid level fluctuation in the metering pipe, accurately masters the feeding condition of the catalyst, finds the problem of the catalyst metering pump in time and processes the problem in time so as to confirm that the catalyst is injected into the esterification reaction kettle, and ensures the stability of the production line.
As an improvement of the utility model, a steam regulating valve is installed at a heat medium inlet of the catalyst heater, an inlet of the steam regulating valve is connected with a steam pipe, a material outlet of the catalyst heater is provided with a temperature sensor, and the opening degree of the steam regulating valve is controlled by the temperature of the catalyst measured by the temperature sensor; and a heating medium outlet of the catalyst heater is connected with a condensed water discharge pipe. When the catalyst temperature at the outlet of the catalyst heater measured by the temperature sensor is higher than a set upper limit value, the opening degree of the steam regulating valve is reduced; when the catalyst temperature at the outlet of the catalyst heater measured by the temperature sensor is lower than the set lower limit value, the opening of the steam regulating valve is increased, and the stability of the catalyst temperature can be automatically kept.
As a further improvement, the catalyst bucket is arranged on the conveying trolley, the outlet of the barrel pump is connected with the output pipe of the barrel pump through a soft joint, the feed inlet of the catalyst tank is provided with a feed valve of the catalyst tank, and the inlet of the feed valve of the catalyst tank is connected with the output pipe of the barrel pump. The conveying trolley carries the catalyst barrel to reach the inlet of the output pipe of the barrel pump, after the catalyst barrel is connected by the soft joint, the feeding valve of the catalyst tank is opened, the barrel pump can be started, and the catalyst is injected into the catalyst tank.
Drawings
The invention will be described in further detail with reference to the drawings and the detailed description, which are provided for reference and illustration purposes only and are not intended to limit the invention.
FIG. 1 is a flow chart of the catalyst system for PBT production according to the present invention.
In the figure: 1. a catalyst barrel; 2. a catalyst tank; 3. a catalyst metering pump; 4. a catalyst filter; 5. a catalyst heater; 6. an esterification reaction kettle; 7. a conveying trolley; 8. a metering tube; 9. a sight glass; LT. a metering tube level gauge; G1. a barrel pump output pipe; G2. a nitrogen gas pipe; G3. a catalyst return pipe; G4. an emptying pipe; G5. a catalyst bottom injection pipe; G6. a steam pipe; G7. a condensed water discharge pipe; v1. catalyst pot feed valve; v2, a nitrogen gas inlet valve; v3. blow-off valve; v4. a catalyst discharge valve; v5. a catalyst return valve; v6. catalyst discharge valve; v7. catalyst bottom injection valve; v8. steam control valve; t1, a temperature sensor.
Detailed Description
As shown in figure 1, the catalyst system for PBT production of the utility model comprises a catalyst barrel 1, a catalyst tank 2 and an esterification reaction kettle 6, a barrel pump is arranged in the catalyst barrel 1, the outlet of the barrel pump is connected with the feed inlet of the catalyst tank 2 through a barrel pump output pipe G1, the air inlet at the top of the catalyst tank 2 is connected with the outlet of a nitrogen pipe G2 through a nitrogen inlet valve V2, the exhaust port at the top of the catalyst tank 2 is connected with an emptying pipe G4 through an emptying valve V3, a catalyst bottom injection valve V7 is arranged at the bottom of the esterification reaction kettle 6, a catalyst discharge valve V4 is arranged at the bottom of the catalyst tank 2, the outlet of the catalyst discharge valve V4 is connected with the middle inlet of a metering pipe 8, a metering pipe liquid level meter is arranged at one side of the metering pipe 8, the top outlet of the LT metering pipe 8 is connected with the top return port of the catalyst tank 2 through a catalyst return valve V5 and a catalyst return pipe G3, and the height of the sight glass 9 is flush with the lower part of the catalyst tank 2, the outlet at the bottom of the metering pipe 8 is connected with the inlet of the catalyst metering pump 3 through a catalyst discharge valve V6, the outlet of the catalyst metering pump 3 is connected with the inlet of the catalyst filter 4, the outlet of the catalyst filter 4 is connected with the material inlet of the catalyst heater 5, and the material outlet of the catalyst heater 5 is connected with the inlet of a catalyst bottom injection valve V7 through a catalyst bottom injection pipe G5.
The catalyst tetrabutyl titanate is in a liquid state and is easy to convey, and by utilizing the characteristic, tetrabutyl titanate in the catalyst barrel 1 is pumped out by a barrel pump and enters the catalyst tank 2 for storage through a barrel pump output pipe G1, and the gas phase space of the catalyst tank 2 is filled with nitrogen from a nitrogen pipe G2 to protect the catalyst. Firstly opening a nitrogen gas inlet valve V2 and a vent valve V3, discharging air in the catalyst tank 2 through a vent pipe G4 by using nitrogen, then setting the pressure of the catalyst tank 2 to be automatic, automatically opening the nitrogen gas inlet valve V2 when the pressure in the tank is lower than 1 kPa, and automatically closing the nitrogen gas inlet valve V2 when the pressure in the tank is higher than 3 kPa; when the pressure in the catalyst tank 2 is higher than 5 kPa, the blow valve V3 is automatically opened to close to the set pressure.
When adding the catalyst, firstly opening a catalyst discharge valve V4 and a catalyst reflux valve V5, enabling the catalyst in a catalyst tank 2 to enter a metering pipe 8 by virtue of liquid level difference and flow upwards, when material is displayed in a viewing mirror 9, closing a catalyst discharge valve V4, then opening a catalyst discharge valve V6, starting a catalyst metering pump 3, pumping out and metering the catalyst in the metering pipe 8, preparing the catalyst by BDO (boron-containing organic compound), and simultaneously preheating the catalyst sent out by the catalyst metering pump 3 to 120-170 ℃ by a catalyst heater 5 and sending the catalyst into an esterification reaction kettle 6 in order to prevent the catalyst from being vaporized at high temperature. Because the esterification reaction can generate a large amount of water in the esterification reaction kettle 6, the density of the water is less than that of the PBT; fresh catalyst is injected from the bottom of the esterification reaction kettle 6 through a catalyst bottom injection pipe G5 and a catalyst bottom injection valve V7, so that the catalyst can be prevented from contacting water. Because the filling amount of the catalyst is too small, the catalyst tank 2 cannot observe the micro fluctuation of the liquid level, the system converts the micro fluctuation of the liquid level which cannot be observed by the catalyst tank 2 into the obvious liquid level fluctuation in the metering pipe 8, accurately masters the feeding condition of the catalyst, finds the problem of the catalyst metering pump 3 in time and processes the problem in time so as to confirm that the catalyst is injected into the esterification reaction kettle 6 and ensure the stability of the production line.
A steam regulating valve V8 is installed at a heat medium inlet of the catalyst heater 5, an inlet of a steam regulating valve V8 is connected with a steam pipe G6, a material outlet of the catalyst heater 5 is provided with a temperature sensor T1, and the opening degree of the steam regulating valve V8 is controlled by the catalyst temperature measured by a temperature sensor T1; the heat medium outlet of the catalyst heater 5 is connected to a condensed water discharge pipe G7. When the catalyst temperature at the outlet of the catalyst heater 5 measured by the temperature sensor T1 is higher than the set upper limit value, the opening degree of the steam adjusting valve V8 becomes smaller; when the catalyst temperature at the outlet of the catalyst heater 5 measured by the temperature sensor T1 is lower than the set lower limit value, the opening degree of the steam adjusting valve V8 is increased, and the catalyst temperature can be automatically kept stable.
The catalyst barrel 1 is arranged on the conveying trolley 7, the outlet of the barrel pump is connected with a barrel pump output pipe G1 through a soft joint, the feed inlet of the catalyst tank 2 is provided with a catalyst tank feed valve V1, and the inlet of the catalyst tank feed valve V1 is connected with a barrel pump output pipe G1. The conveying trolley 7 carries the catalyst barrel 1 to reach the inlet of the output pipe G1 of the barrel pump, after the catalyst barrel 1 is connected by a soft joint, the catalyst tank feeding valve V1 is opened, the barrel pump can be started, and the catalyst is injected into the catalyst tank 2.
The above description is only a preferred embodiment of the present invention, and not intended to limit the scope of the present invention. In addition to the above embodiments, the present invention can also have other embodiments, and all technical solutions formed by equivalent replacement or equivalent transformation fall within the protection scope of the present invention. The undescribed technical features of the present invention can be realized by or using the prior art, and are not described herein again.
Claims (3)
1. The utility model provides a catalyst system is used in PBT production, includes catalyst bucket, catalyst jar and esterification reaction cauldron, it has the bucket pump to embed in the catalyst bucket, the export of bucket pump through bucket pump output tube with the feed inlet of catalyst jar links to each other, the air inlet at catalyst tank deck portion passes through the nitrogen gas admission valve and links to each other with the export of nitrogen gas pipe, the gas vent at catalyst tank deck portion passes through the atmospheric valve and links to each other with the blow-down pipe, the catalyst bottom injection valve, its characterized in that are installed to esterification reaction cauldron's bottom: catalyst bleeder valve is installed to the bottom of catalyst jar, and the export of catalyst bleeder valve links to each other with the middle part entry of metering tube, and metering tube level gauge is installed to one side of metering tube, and the top export of metering tube links to each other through the top backward flow mouth of catalyst reflux valve and catalyst back flow with the catalyst jar, and the sight glass is installed to the top of catalyst reflux valve, and the height of sight glass and the lower part parallel and level of catalyst jar, and the bottom export of metering tube links to each other through the entry of catalyst baiting valve with the catalyst measuring pump, the export of catalyst metering pump links to each other with the entry of catalyst filter, the export of catalyst filter links to each other with the material entry of catalyst heater, the material export of catalyst heater through catalyst end annotate the pipe with the entry of catalyst end notes valve.
2. The catalyst system for PBT production according to claim 1, wherein: a steam regulating valve is installed at a heat medium inlet of the catalyst heater, an inlet of the steam regulating valve is connected with a steam pipe, a material outlet of the catalyst heater is provided with a temperature sensor, and the opening degree of the steam regulating valve is controlled by the temperature of the catalyst measured by the temperature sensor; and a heating medium outlet of the catalyst heater is connected with a condensed water discharge pipe.
3. Catalyst system for the production of PBT according to claim 1 or 2, characterized in that: the catalyst barrel is arranged on the conveying trolley, the outlet of the barrel pump is connected with the output pipe of the barrel pump through a soft joint, the feed port of the catalyst tank is provided with a catalyst tank feed valve, and the inlet of the catalyst tank feed valve is connected with the output pipe of the barrel pump.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202020372128.1U CN212174853U (en) | 2020-03-23 | 2020-03-23 | Catalyst system for PBT production |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202020372128.1U CN212174853U (en) | 2020-03-23 | 2020-03-23 | Catalyst system for PBT production |
Publications (1)
| Publication Number | Publication Date |
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| CN212174853U true CN212174853U (en) | 2020-12-18 |
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| Application Number | Title | Priority Date | Filing Date |
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| CN202020372128.1U Active CN212174853U (en) | 2020-03-23 | 2020-03-23 | Catalyst system for PBT production |
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| CN (1) | CN212174853U (en) |
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- 2020-03-23 CN CN202020372128.1U patent/CN212174853U/en active Active
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Address after: No. 301, Wangjiang Road, economic and Technological Development Zone, Yangzhou City, Jiangsu Province Patentee after: Yangzhou Huitong Technology Co.,Ltd. Address before: No. 301, Wangjiang Road, economic and Technological Development Zone, Yangzhou City, Jiangsu Province Patentee before: YANGZHOU HUITONG CHEMICAL TECHNOLOGY Co.,Ltd. |
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| CP01 | Change in the name or title of a patent holder |