Continuous automatic temperature control device for dimethyl phosphite deacidification process
By designing a continuous automatic temperature control device in the dimethyl phosphite production process, and interlocking with the temperature monitoring device with the steam cut-off valve and the trap, the automatic control of the temperature of the deacid kettle is achieved, solving the problems of high labor intensity and large steam loss in the prior art, and improving production efficiency and product quality.
Patent Information
- Application Number
- CN202422566277.2
- Authority / Receiving Office
- CN · China
- Patent Type
- Utility models(China)
- Current Assignee / Owner
- Filing Date
- 2024-10-23
- Publication Date
- 2025-08-22
- Estimated Expiration
- 2034-10-23
AI Technical Summary
In the existing dimethyl phosphite production process, the deacidification process has a high labor intensity, unstable control, large steam loss, and poor control in terms of process indicators, which affects the reaction efficiency.
A continuous automatic temperature control device including a primary deacid kettle and a secondary deacid kettle is designed. By setting a steam cut-off valve and a trap at the primary deacid kettle jacket, it is interlocked with the temperature monitoring device of the secondary deacid kettle, and it is combined with the regulating valve on the steam main pipe to achieve automatic control to ensure the stability of the deacid kettle temperature.
Automatic temperature control of the deacidification process of dimethyl phosphite is realized, which improves production efficiency, reduces the number of workers, and improves the quality of dimethyl phosphite.
Smart Images
Figure CN223249285U_ABST
Abstract
Description
Technical Field
[0001] The utility model belongs to the field of dimethyl phosphite production, and particularly relates to a continuous automatic temperature control device for the deacidification process of dimethyl phosphite. Background Art
[0002] The existing dimethyl phosphite production process uses phosphorus trichloride and methanol as raw materials. After being metered in a specific molar ratio, they are continuously pumped into a reactor by a corresponding pumping mechanism, where dimethyl phosphite, hydrogen chloride, and methyl chloride are produced in a negative pressure system. This production process requires deacidification, which is carried out in two stages, each controlled by steam controlled by a manual valve. This operating mode is labor-intensive, unstable, and has high steam loss. The controllability of process indicators and other aspects is poor, affecting reaction efficiency. Utility Model Content
[0003] The utility model provides a continuous automatic temperature control device for the deacidification process of dimethyl phosphite, comprising a first-stage deacidification kettle, which is connected to a second-stage deacidification kettle via a discharge pipe; the second-stage deacidification kettle is connected to a first crude ester receiver and a second crude ester receiver via a discharge pipe; a jacket is provided on the outer side of the first-stage deacidification kettle, which is connected to a steam main pipe; and a jacket is provided on the outer side of the second-stage deacidification kettle, which is connected to a hot water collecting tank.
[0004] The first-stage deacidification kettle is provided with a temperature monitoring device. The steam outlet pipeline connected to the bottom of the jacket of the first-stage deacidification kettle is provided with a steam cut-off valve and a steam trap, and is connected to the jacket outside the second-stage deacidification kettle. The steam cut-off valve and the steam trap are interlocked with the temperature monitoring device of the second-stage deacidification kettle; the steam trap is provided with a bypass drainage switch valve.
[0005] A steam regulating valve is installed on the steam main pipe and is interlocked with the temperature monitoring device of the first-stage deacidification kettle.
[0006] The first-stage deacidification kettle is connected to the first-stage deacidification first-stage condenser, the first-stage deacidification first-stage condenser is connected to the first-stage deacidification second-stage condenser, the first-stage deacidification second-stage condenser is connected to the total separator, and discharge pipes are respectively provided at the bottom of the first-stage deacidification first-stage condenser, the first-stage deacidification second-stage condenser and the total separator to enter the esterification kettle, and the gas phase discharge pipe of the total separator is connected to the concentrated hydrochloric acid absorption tower.
[0007] The secondary deacidification kettle is connected to the secondary deacidification condenser, the secondary deacidification condenser is connected to the secondary deacidification separator, the secondary deacidification separator is connected to the main separator, the secondary deacidification condenser and the secondary deacidification separator are respectively provided with discharge pipes to enter the crude ester receiver 1 and the crude ester receiver 2, the crude ester receiver 1 and the crude ester receiver 2 are connected to the crude ester high-level tank via the crude ester transfer pump 1 or the crude ester transfer pump 2, the crude ester high-level tank is connected to the crude ester storage tank 1 and the crude ester storage tank 2, and the crude ester storage tank 1 and the crude ester storage tank 2 are connected to the crude ester tail gas absorption tower.
[0008] The esterification kettle is connected to the first-level deacidification kettle via a discharge pipe, the gas phase pipe on the top of the esterification kettle is connected to the first-level esterification condenser, the first-level esterification condenser is connected to the second-level esterification condenser, the second-level esterification condenser is connected to the total separator, and the bottoms of the first-level esterification condenser and the second-level esterification condenser are respectively provided with discharge pipes entering the esterification kettle.
[0009] The front feed port of the esterification kettle is connected to a methanol storage tank and a phosphorus trichloride storage tank via a pipeline.
[0010] The beneficial effects of the utility model are as follows:
[0011] The utility model studies the process of continuous automatic temperature control in the deacidification process of producing dimethyl phosphite. By transforming the deacidification system, a steam shut-off valve and a steam regulating valve are added to the steam inlet of the first-stage deacidification kettle, and the steam shut-off valve and the steam regulating valve are interlocked with the temperature of the second-stage deacidification kettle. The control system is automatically operated throughout the process, thereby achieving the purpose of automatic temperature control of the deacidification kettle, improving work efficiency, reducing the number of workers, and improving the quality of dimethyl phosphite. BRIEF DESCRIPTION OF THE DRAWINGS
[0012] Figure 1 Schematic diagram of the device of the present utility model.
[0013] Description of the markings in the figure: methanol storage tank 1, phosphorus trichloride storage tank 2, methanol feeding pump 1 3, methanol feeding pump 2 4, phosphorus trichloride feeding pump 1 5, phosphorus trichloride feeding pump 2 6, methanol mass flow meter 7, phosphorus trichloride mass flow meter 8, esterification kettle 9, first-stage deacidification kettle 10, second-stage deacidification kettle 11, crude ester receiver 1 12, crude ester receiver 2 13, crude ester transfer pump 1 14, crude ester transfer pump 2 15, esterification first-stage condenser 16, esterification second First-stage condenser 17, first-stage deacidification first-stage condenser 18, first-stage deacidification second-stage condenser 19, total gas-liquid separator 20, crude ester high-level tank 21, second-stage deacidification condenser 22, second-stage deacidification separator 23, crude ester storage tank 1 24, crude ester storage tank 2 25, hot water collection tank 26, crude ester tail gas absorption tower 27, concentrated hydrochloric acid absorption tower 28, steam main pipe 29, steam shut-off valve 101, steam trap 102, bypass drainage switch valve 103. DETAILED DESCRIPTION
[0014] The embodiments of the present invention will be described in detail below with reference to the examples. The following examples are only used to illustrate the present invention and should not be considered as limiting the scope of the present invention.
[0015] Example 1
[0016] A continuous automatic temperature control device for the deacidification process of dimethyl phosphite, such as Figure 1As shown, it includes a first-level deacidification kettle 10, which is connected to a second-level deacidification kettle 11 via a discharge pipe; the second-level deacidification kettle 11 is connected to a crude ester receiver 12 and a crude ester receiver 2 13 via a discharge pipe; a jacket is provided on the outside of the first-level deacidification kettle 10, which is connected to a steam main pipe 29; a jacket is provided on the outside of the second-level deacidification kettle 11, which is connected to a hot water collection tank 26.
[0017] The first-stage deacidification kettle 10 is provided with a temperature monitoring device. The steam outlet pipeline connected to the bottom of the jacket of the first-stage deacidification kettle 10 is provided with a steam shut-off valve 101 and a steam trap 102, and is connected to the jacket outside the second-stage deacidification kettle 11. The steam shut-off valve 101 and the steam trap 102 are interlocked with the temperature monitoring device of the second-stage deacidification kettle 11; the steam trap 102 is provided with a bypass drainage switch valve 103.
[0018] A steam regulating valve is provided on the steam main pipe 29 and is interlocked with the temperature monitoring device of the first-stage deacidification kettle 10.
[0019] The first-stage deacidification kettle 10 is connected to the first-stage deacidification first-stage condenser 18, the first-stage deacidification first-stage condenser 18 is connected to the first-stage deacidification second-stage condenser 19, the first-stage deacidification second-stage condenser 19 is connected to the total separator 20, and the first-stage deacidification first-stage condenser 18, the first-stage deacidification second-stage condenser 19 and the total separator 20 are respectively provided with discharge pipes at the bottom to enter the esterification kettle 9, and the gas phase discharge pipe of the total separator 20 is connected to the concentrated hydrochloric acid absorption tower 28.
[0020] The secondary deacidification kettle 11 is connected to the secondary deacidification condenser 22, the secondary deacidification condenser 22 is connected to the secondary deacidification separator 23, the secondary deacidification separator 23 is connected to the main separator 20, the secondary deacidification condenser 22 and the secondary deacidification separator 23 are respectively provided with discharge pipes to enter the crude ester receiver 12 and the crude ester receiver 2 13, the crude ester receiver 12 and the crude ester receiver 2 13 are connected to the crude ester high-level tank 21 via the crude ester transfer pump 14 or the crude ester transfer pump 2 15, the crude ester high-level tank 21 is connected to the crude ester storage tank 1 24 and the crude ester storage tank 2 25, and the crude ester storage tank 1 24 and the crude ester storage tank 2 25 are connected to the crude ester tail gas absorption tower 27.
[0021] The esterification kettle 9 is connected to the first-level deacidification kettle 10 via a discharge pipe, the gas phase pipe at the top of the esterification kettle 9 is connected to the first-level esterification condenser 16, the first-level esterification condenser 16 is connected to the second-level esterification condenser 17, the second-level esterification condenser 17 is connected to the total separator 20, and the bottoms of the first-level esterification condenser 16 and the second-level esterification condenser 17 are respectively provided with discharge pipes entering the esterification kettle 9.
[0022] The front feed port of the esterification kettle 9 is connected to the methanol storage tank 1 and the phosphorus trichloride storage tank 2 via a pipeline.
[0023] Example 2
[0024] As shown in the figure, the deacidification process is as follows:
[0025] During operation, methanol is fed through methanol feed pump 1 3 or methanol feed pump 2 4, and phosphorus trichloride is fed through phosphorus trichloride feed pump 1 5 or phosphorus trichloride feed pump 6 according to the set molar ratio and converted into a mass ratio. The feed amount is controlled by methanol mass flow meter 7 and phosphorus trichloride mass flow meter 8 respectively, and then enters the esterification kettle 9 for reaction. After the reaction reaches a certain stage, the materials enter the first deacidification kettle 10 and the second deacidification kettle 11 in turn. The steam from the steam main pipe 29 enters the first deacidification kettle 10 through the steam regulating valve. The steam and hot water in the jacket of the first deacidification kettle 10 The steam condensate enters the jacket of the secondary deacidification kettle 11 through the steam shut-off valve 101 and the steam trap 102 respectively. The steam trap 102 is provided with a bypass drainage switch valve 103. When the steam trap 102 is abnormal and cannot drain water in time, the bypass drainage switch valve 103 automatically opens to drain water. The secondary deacidification kettle 11 discharges the steam condensate to the hot water collection tank 26 through its bottom steam trap for collection. The crude ester inside the secondary deacidification kettle 11 passes through the crude ester receiver 1 12 or the crude ester receiver 2 13, and then enters the crude ester storage tank 24 or the crude ester storage tank 25 through the crude ester high-level tank 21, thereby completing the deacidification process.
[0026] The gas phase in the esterification kettle 9 enters the esterification primary condenser 16, the esterification secondary condenser 17, and the total separator 20 in sequence through the top pipe, and finally the gas phase is absorbed by the concentrated hydrochloric acid absorption tower 28; the liquid phases in the esterification primary condenser 16, the esterification secondary condenser 17, and the total separator 20 enter the esterification kettle 9 through the bottom discharge pipes of each for reuse. The gas phase in the first-stage deacidification kettle 10 enters the first-stage deacidification primary condenser 18, the first-stage deacidification secondary condenser 19, and the total separator 20 in sequence through the top pipe, and finally the gas phase is absorbed by the concentrated hydrochloric acid absorption tower 28; the liquid phases in the first-stage deacidification primary condenser 18, the first-stage deacidification secondary condenser 19, and the total separator 20 enter the esterification kettle 9 through the bottom discharge pipes of each for reuse. The gas phase of the secondary deacidification kettle 11 enters the secondary deacidification condenser 22, the secondary deacidification separator 23 and the main separator 20 in sequence through the top pipeline, and finally the gas phase is absorbed by the concentrated hydrochloric acid absorption tower 28; the liquid phase in the secondary deacidification condenser 22 and the secondary deacidification separator 23 enters the crude ester receiver 1 12 or the crude ester receiver 2 13 through the pipelines at the bottom of each.
[0027] During the deacidification process, the steam is automatically regulated: a steam regulating valve is provided on the steam main pipe 29, which is interlocked with the temperature monitoring device of the first-stage deacidification kettle 10; the steam shut-off valve 101 and the steam trap 102 are interlocked with the temperature monitoring device of the second-stage deacidification kettle 11, thereby achieving the purpose of automatic control of the deacidification temperature.
[0028] Preferably, the temperature of the secondary deacidification kettle 11 is preferably 75-85°C. By setting the temperatures of the secondary deacidification kettle 11 and the primary deacidification kettle 10, the openings of the steam regulating valve, steam shut-off valve 101 and steam trap 102 on the steam main 29 are controlled, thereby controlling the temperatures of the primary deacidification kettle 10 and the secondary deacidification kettle 11 to be maintained at the set values.
[0029] This embodiment can realize the automated operation of the control system of the entire process, thereby achieving the purpose of automatic control of the deacidification temperature, enabling continuous production of dimethyl phosphite, and improving work efficiency, reducing the number of workers, and improving the quality of dimethyl phosphite.
[0030] The above embodiments are merely preferred technical solutions of the present invention and should not be construed as limiting the present invention. The scope of protection of the present invention shall be the technical solutions set forth in the claims, including equivalent alternatives to the technical features of the technical solutions set forth in the claims. Equivalent alternatives and improvements within this scope are also within the scope of protection of the present invention.
Claims
1. A continuous automatic temperature control device for the deacidification process of dimethyl phosphite, characterized in that: The first deacidification kettle (10) is connected to the second deacidification kettle (11) via a discharge pipe; the second deacidification kettle (11) is connected to the first crude ester receiver (12) and the second crude ester receiver (13) via a discharge pipe; the first deacidification kettle (10) is provided with a jacket on the outside, and the jacket is connected to the steam main pipe (29); the second deacidification kettle (11) is provided with a jacket on the outside, and the jacket is connected to the hot water collection tank (26).
2. A continuous automatic temperature control device for dimethyl phosphite deacidification process according to claim 1, characterized in that: The first-stage deacidification kettle (10) is provided with a temperature monitoring device. The steam outlet pipeline connected to the bottom of the jacket of the first-stage deacidification kettle (10) is provided with a steam shut-off valve (101) and a steam trap (102), and is connected to the jacket outside the second-stage deacidification kettle (11). The steam shut-off valve (101) and the steam trap (102) are interlocked with the temperature monitoring device of the second-stage deacidification kettle (11); and the steam trap (102) is provided with a bypass drainage switch valve (103).
3. A continuous automatic temperature control device for dimethyl phosphite deacidification process according to claim 1, characterized in that: The steam main pipe (29) is provided with a steam regulating valve, and is interlocked with the temperature monitoring device of the first-stage deacidification kettle (10).
4. A continuous automatic temperature control device for dimethyl phosphite deacidification process according to claim 1, characterized in that: The first-stage deacidification kettle (10) is connected to the first-stage deacidification primary condenser (18), the first-stage deacidification primary condenser (18) is connected to the first-stage deacidification secondary condenser (19), the first-stage deacidification secondary condenser (19) is connected to the main separator (20), and the bottoms of the first-stage deacidification primary condenser (18), the first-stage deacidification secondary condenser (19) and the main separator (20) are respectively provided with discharge pipes to enter the esterification kettle (9), and the gas phase discharge pipe of the main separator (20) is connected to the concentrated hydrochloric acid absorption tower (28).
5. A continuous automatic temperature control device for dimethyl phosphite deacidification process according to claim 1, characterized in that: The secondary deacidification kettle (11) is connected to the secondary deacidification condenser (22), the secondary deacidification condenser (22) is connected to the secondary deacidification separator (23), the secondary deacidification separator (23) is connected to the main separator (20), the secondary deacidification condenser (22) and the secondary deacidification separator (23) are respectively provided with discharge pipes to enter the crude ester receiver 1 (12) and the crude ester receiver 2 (13), the crude ester receiver 1 (12) and the crude ester receiver 2 (13) are connected to the crude ester high-level tank (21) via the crude ester transfer pump 1 (14) or the crude ester transfer pump 2 (15), the crude ester high-level tank (21) is connected to the crude ester storage tank 1 (24) and the crude ester storage tank 2 (25), and the crude ester storage tank 1 (24) and the crude ester storage tank 2 (25) are connected to the crude ester tail gas absorption tower (27).
6. A continuous automatic temperature control device for dimethyl phosphite deacidification process according to claim 4, characterized in that: The esterification kettle (9) is connected to the first-stage deacidification kettle (10) via a discharge pipe. The gas phase pipe at the top of the esterification kettle (9) is connected to the first-stage esterification condenser (16). The first-stage esterification condenser (16) is connected to the second-stage esterification condenser (17). The second-stage esterification condenser (17) is connected to the main separator (20). The bottoms of the first-stage esterification condenser (16) and the second-stage esterification condenser (17) are respectively provided with discharge pipes to enter the esterification kettle (9).
7. A continuous automatic temperature control device for dimethyl phosphite deacidification process according to claim 6, characterized in that: The front feed port of the esterification kettle (9) is connected to the methanol storage tank (1) and the phosphorus trichloride storage tank (2) via a pipeline.