CN113398625A - Control system and control method for discharging oil and water in long-chain dicarboxylic acid extraction and refining - Google Patents
Control system and control method for discharging oil and water in long-chain dicarboxylic acid extraction and refining Download PDFInfo
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- CN113398625A CN113398625A CN202110738394.0A CN202110738394A CN113398625A CN 113398625 A CN113398625 A CN 113398625A CN 202110738394 A CN202110738394 A CN 202110738394A CN 113398625 A CN113398625 A CN 113398625A
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D11/00—Solvent extraction
- B01D11/04—Solvent extraction of solutions which are liquid
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D11/00—Solvent extraction
- B01D11/04—Solvent extraction of solutions which are liquid
- B01D11/0484—Controlling means
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D17/00—Separation of liquids, not provided for elsewhere, e.g. by thermal diffusion
- B01D17/02—Separation of non-miscible liquids
- B01D17/0208—Separation of non-miscible liquids by sedimentation
- B01D17/0214—Separation of non-miscible liquids by sedimentation with removal of one of the phases
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B67—OPENING, CLOSING OR CLEANING BOTTLES, JARS OR SIMILAR CONTAINERS; LIQUID HANDLING
- B67D—DISPENSING, DELIVERING OR TRANSFERRING LIQUIDS, NOT OTHERWISE PROVIDED FOR
- B67D7/00—Apparatus or devices for transferring liquids from bulk storage containers or reservoirs into vehicles or into portable containers, e.g. for retail sale purposes
- B67D7/02—Apparatus or devices for transferring liquids from bulk storage containers or reservoirs into vehicles or into portable containers, e.g. for retail sale purposes for transferring liquids other than fuel or lubricants
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B67—OPENING, CLOSING OR CLEANING BOTTLES, JARS OR SIMILAR CONTAINERS; LIQUID HANDLING
- B67D—DISPENSING, DELIVERING OR TRANSFERRING LIQUIDS, NOT OTHERWISE PROVIDED FOR
- B67D7/00—Apparatus or devices for transferring liquids from bulk storage containers or reservoirs into vehicles or into portable containers, e.g. for retail sale purposes
- B67D7/06—Details or accessories
- B67D7/08—Arrangements of devices for controlling, indicating, metering or registering quantity or price of liquid transferred
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- G—PHYSICS
- G05—CONTROLLING; REGULATING
- G05D—SYSTEMS FOR CONTROLLING OR REGULATING NON-ELECTRIC VARIABLES
- G05D27/00—Simultaneous control of variables covered by two or more of main groups G05D1/00 - G05D25/00
- G05D27/02—Simultaneous control of variables covered by two or more of main groups G05D1/00 - G05D25/00 characterised by the use of electric means
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Abstract
The invention discloses a control system and a control method for discharging oil and water in long-chain binary acid extraction and refining, wherein the control system comprises an extraction kettle, a differential pressure liquid level meter, a capacitance instrument, a middle layer discharge valve, a water phase discharge valve, an oil phase discharge valve and a controller, the controller is connected with the differential pressure liquid level meter, the capacitance instrument, the middle layer discharge control valve, the water phase discharge control valve and the oil phase discharge control valve, and the differential pressure liquid level meter and the capacitance instrument are used for monitoring an oil-water interface in the extraction kettle. The differential pressure liquid level meter and the capacitance instrument simultaneously monitor an oil-water interface, when any one of the instruments monitors an oil phase, a signal is transmitted to the controller, the controller closes the water phase discharge valve, and the water phase discharge is finished; then opening an oil phase discharge valve to discharge the oil phase; when the middle layer is accumulated to a certain volume, the middle layer is discharged. Therefore, complete discharge of oil and water phases is realized, the utilization rate of the reaction kettle is increased, and materials are not mixed with each other.
Description
Technical Field
The invention relates to a control system and a control method for oil-water discharging in extraction refining, in particular to a control system and a control method for oil-water discharging in long-chain dicarboxylic acid extraction refining.
Background
The solvent extraction method is a common method for refining long-chain dicarboxylic acid, and mainly utilizes the characteristics that the solubility of the long-chain dicarboxylic acid in a solvent phase is higher than that in water, and impurities are basically insoluble in the solvent phase to refine and purify the long-chain dicarboxylic acid. After extraction, the mixture is usually kept still for a period of time for oil-water separation, and then oil phases and water phases are respectively sent to different subsequent working sections. During discharging, oil and water are completely discharged, the utilization rate of the reaction kettle can be increased, and materials are not mixed with each other, so that the key of discharging process control is realized. This not only relates to the smooth proceeding of the subsequent process, but also affects the quality and yield of the final product. Patent application No. 201220516050.1 of the prior art describes a water cutting device for an oil storage tank: a sensor is arranged on the water outlet pipeline, and when the requirement of water drainage in the oil storage tank is met, the water cutting executing mechanism is started through the controller to start water drainage; when the oil content in water reaches a certain value set by the sensor and is monitored, the controller closes the water cutting actuating mechanism after receiving the signal. The oil pipe is established on the upper portion of separator staving for patent application number 201310618034.2, and the oil pipe below is equipped with detection device, and the outlet pipe is established to the staving lower part, is equipped with the control valve on oil pipe and the outlet pipe respectively, and detection device and the input connection of controller, the control end of control valve and the output connection of controller, the controller is according to detection device's testing result, and the corresponding control valve of control valve is opened or is closed. Patent application number is 201721092008.0 sets up a baffle in the water oil separating incasement, divide into water oil separating groove and guiding gutter with the box, the feed inlet sets up in water oil separating groove top, the discharge gate sets up in the guiding gutter below, be equipped with the hydrometer on the discharging pipe way, water pipeline, oil pipeline, the opening and close of the solenoid valve on water pipeline and the oil pipeline is controlled through hydrometer testing result, and establish air intake and fan at the top of guiding gutter, the fan is established to the end of discharge gate, after the water phase separation, dry ejection of compact house steward, mix with remaining water once more when avoiding the oil phase ejection of compact.
In the prior art, the device is mainly suitable for water cutting of a storage tank, less for oil-water separation of a long-chain dibasic acid reaction kettle, more complex in material components of the reaction kettle compared with the storage tank, more frequent and complex in operation, and easy to cause misoperation if only one detection control means is adopted. In particular, after the extraction is completed, there is an intermediate layer which is distinguished from the oil layer and the water layer, and the removal of the intermediate layer to the oil layer or the water layer is disadvantageous for the subsequent production. Secondly, modern chemical industry device arrangements tend to be more and more compact, and installation of a water cut-off device on a tank outlet pipeline is often limited in space, and has the conditions of regular maintenance, high cost and the like.
Disclosure of Invention
The purpose of the invention is as follows: the invention aims to provide a control system for oil-water discharging process in extraction and refining of long-chain dibasic acid, which realizes complete discharging of oil and water phases, increases the utilization rate of a reaction kettle, does not mix materials, and ensures that materials in a middle layer do not go out of an oil layer or a water layer.
The technical scheme is as follows: the invention discloses a control system for an oil-water discharging process in long-chain dibasic acid extraction refining, which comprises an extraction kettle, a differential pressure type liquid level meter, a capacitance instrument, a middle layer discharging control valve, a water phase discharging control valve, an oil phase discharging control valve and a controller, wherein the controller is connected with the differential pressure type liquid level meter, the capacitance instrument, the middle layer discharging control valve, the water phase discharging control valve and the oil phase discharging control valve, and the differential pressure type liquid level meter and the capacitance instrument are used for monitoring an oil-water interface in the extraction kettle.
The extraction kettle is mainly used for extracting long-chain dicarboxylic acid from a water phase by using an organic solvent; the middle layer discharge control valve is used for opening or cutting off the middle layer discharge; the water phase discharging control valve is used for opening or cutting off the water phase discharging; the oil phase discharging control valve is used for opening or cutting off oil phase discharging; and the controller is used for receiving the signal of the detecting instrument and outputting an opening and closing signal of the control valve.
Furthermore, the extraction kettle is provided with a middle layer discharge port, a water phase discharge port, an oil phase discharge port, a capacitance instrument port, a first differential pressure type liquid level meter port and a second differential pressure type liquid level meter port, and the relative position heights of the pipe ports are respectively that the second differential pressure type liquid level meter port, the oil phase discharge port, the first differential pressure type liquid level meter port, the capacitance instrument port, the water phase discharge port and the extraction kettle are provided with the middle layer discharge port.
The control method of the control system comprises the following steps:
(a) the control system adopts a differential pressure liquid level meter and a capacitance instrument to monitor an oil-water interface simultaneously, when any one of the instruments monitors an oil phase, a signal is transmitted to the controller, the controller closes the water phase discharging control valve, and the water phase discharging is finished;
(b) opening an oil phase discharging control valve (H3) to start oil phase discharging;
(c) after the oil phase is discharged, the middle layer material is still in the extraction kettle (V1), and after the next batch of material enters the extraction kettle (V1), mixing and extracting are carried out.
Further, in the step (c), when the intermediate layer is accumulated to a certain volume, the intermediate layer discharging control valve (H1) is opened to discharge the intermediate layer from the intermediate layer discharging port (N1) to a specified place. The operation pressure of the extraction kettle is 100-300kPaA, and the operation temperature is 75-98 ℃. The density of the oil phase material is 750-900kg/m3The density of the water phase material is 950-1050kg/m3. Oil layer material in the material entering the extraction kettle44-50 wt%, 10-14 wt% of middle layer material and 36-46 wt% of water layer material.
Has the advantages that: compared with the prior art, the invention has the following remarkable advantages: according to the invention, the detection instrument is only required to be arranged on the extraction kettle, the common stop valve is arranged on the outlet pipeline, the relative positions of the upper discharge hole of the reaction kettle and the detection instrument are adjusted, and the measuring instrument on the reaction kettle is interlocked with the stop valve, so that complete discharge of oil and water phases is realized, the utilization rate of the reaction kettle is increased, materials are not mixed mutually, and the materials in the middle layer are prevented from being removed from an oil layer or a water layer.
Drawings
FIG. 1 is a diagram of a control system for discharging oil and water in the refining of long-chain dicarboxylic acid.
Detailed Description
The technical solution of the present invention is further illustrated by the following examples.
Example 1
As shown in fig. 1, after the crude dibasic acid solution and the extractant are subjected to extraction reaction in an extraction kettle V1, standing for a period of time to form an oil layer, a water layer and a middle layer, at this time, the reading of a differential pressure type liquid level meter a1 shows 100%, a capacitance meter a2 shows that information is in a boundary position, and a water phase discharge control valve H2 is opened to start water phase discharge. Along with the discharging of the water phase, the oil-water interface in the reaction kettle continuously drops. When the oil-water interface in the reaction kettle is lowered to the position of the upper meter port N6 of the differential pressure type liquid level meter A1, the reading of the differential pressure type liquid level meter A1 begins to fall along with the continuous lowering of the oil-water interface, and at the moment, the display information of the capacitance meter A2 is still a boundary level. When the oil-water interface is lowered to the position of the lower meter port N5 of the differential pressure type liquid level meter A1, the reading of the differential pressure type liquid level meter A1 is 0%, or the capacitance meter A2 detects the oil phase, and the capacitance meter A2 displays no-boundary position information. When the two satisfy one of the two, the signal is transmitted to the controller C1, and the controller C1 outputs a signal to close the water phase discharging control valve H2 to finish the water phase discharging. At this time, the oil phase discharge control valve H3 is opened to start oil phase discharge. After the oil phase is discharged, the middle layer material is still in the extraction kettle V1. In daily production, the quantity of the middle layer materials is less, the middle layer materials are kept in the extraction kettle V1, and the next batch of materials are mixed and extracted after entering the extraction kettle V1. When the middle layer is accumulated to a certain volume, the middle layer discharge control valve H1 is opened, so that the middle layer is discharged from the middle layer discharge port N1 to a designated place.
Taking an industrial production device of long-chain dibasic acid with nominal capacity of 100 tons/year as an example, after finishing extraction reaction of a dibasic acid crude product liquid and an extractant in an extraction kettle V1, standing for a period of time to form an oil layer, a water layer and a middle layer, wherein the reading of a differential pressure type liquid level meter A1 shows that the oil layer, the water layer and the middle layer are 100 percent, a capacitance meter A2 shows that information is that a boundary exists, and a water phase discharging control valve H2 is opened to start water phase discharging. Along with the discharging of the water phase, the oil-water interface in the reaction kettle continuously drops. When the oil-water interface in the reaction kettle is lowered to the position of the upper meter port N6 of the differential pressure type liquid level meter A1, the reading of the differential pressure type liquid level meter A1 begins to fall along with the continuous lowering of the oil-water interface, and at the moment, the display information of the capacitance meter A2 is still a boundary level. When the oil-water interface is lowered to the position of the lower meter port N5 of the differential pressure type liquid level meter A1, the reading of the differential pressure type liquid level meter A1 is 0, or the capacitance meter A2 detects an oil phase, and the display information of the capacitance meter A2 is no boundary position. When the two satisfy one of the two, the signal is transmitted to the controller C1, and the controller C1 outputs a signal to close the water phase discharging control valve H2 to finish the water phase discharging. At this time, the oil phase discharge control valve H3 is opened to start oil phase discharge. After the oil phase discharge is completed, the middle layer material is still in the extraction kettle V1. In daily production, the middle layer is left in the extraction kettle V1, and after the next batch of materials enters the extraction kettle V1, mixing and extraction are carried out. When the middle layer is accumulated to a certain volume, the middle layer discharge control valve H1 can be opened to discharge the middle layer from the middle layer discharge hole N1 to a designated place. The operating pressure of the extraction kettle is 100kPaA, the operating temperature is 75 ℃, and the density of oil layer materials is 750kg/m3The density of the water layer material is 950kg/m3In the materials entering the extraction kettle, the oil layer material accounts for 44 wt%, the middle layer material accounts for 10 wt%, and the water layer material accounts for 36 wt%. Therefore, complete discharge of oil and water phases is realized, the utilization rate of the reaction kettle is increased, materials are not mixed, and the situation that the materials in the middle layer are not removed from an oil layer or a water layer is ensured.
Example 2
With a nominal capacity of 8000 tons/long chainThe technical method is the same as that of the embodiment 1, the operation pressure of an extraction kettle is 300kPaA, the operation temperature is 98 ℃, and the density of oil layer materials is 900kg/m3The density of the water layer material is 1050kg/m3In the materials entering the extraction kettle, 50 wt% of oil layer materials, 14 wt% of middle layer materials and 36 wt% of water layer materials are contained. Therefore, complete discharge of oil and water phases is realized, the utilization rate of the reaction kettle is increased, materials are not mixed, and the situation that the materials in the middle layer are not removed from an oil layer or a water layer is ensured.
Example 3
Taking an industrial production device of long-chain dicarboxylic acid with nominal capacity of 500 tons/year as an example, the technical method is the same as that of the example 1, the operating pressure of an extraction kettle is 110kPaA, the operating temperature is 89 ℃, and the density of oil layer materials is 790kg/m3The density of the water layer material is 980kg/m3In the materials entering the extraction kettle, the oil layer material accounts for 46 wt%, the middle layer material accounts for 11 wt%, and the water layer material accounts for 43 wt%. Therefore, complete discharge of oil and water phases is realized, the utilization rate of the reaction kettle is increased, materials are not mixed, and the situation that the materials in the middle layer are not removed from an oil layer or a water layer is ensured.
Example 4
Taking an industrial production device of long-chain dicarboxylic acid with nominal capacity of 1500 tons/year as an example, the technical method is the same as that of the example 1, the operating pressure of an extraction kettle is 135kPaA, the operating temperature is 90 ℃, and the density of oil layer materials is 800kg/m3The density of the water layer material is 990kg/m3In the materials entering the extraction kettle, the oil layer material accounts for 47 wt%, the middle layer material accounts for 12 wt%, and the water layer material accounts for 41 wt%. Therefore, complete discharge of oil and water phases is realized, the utilization rate of the reaction kettle is increased, materials are not mixed, and the situation that the materials in the middle layer are not removed from an oil layer or a water layer is ensured.
Example 5
Taking an industrial production device of long-chain dicarboxylic acid with a nominal capacity of 3000 tons/year as an example, the technical method is the same as that of the example 1, the operating pressure of an extraction kettle is 160kPaA, the operating temperature is 92 ℃, and the density of an oil layer material is 810kg/m3The density of the water layer material was 995kg/m3In the materials entering the extraction kettle, oil layer materials account for 48 wt%, middle layer materials account for 13 wt%, and water layer materials account for 39 wt%. Thereby realizingThe oil phase and the water phase are completely discharged, the utilization rate of the reaction kettle is increased, materials are not mixed, and the materials in the middle layer are prevented from being removed from an oil layer or a water layer.
Example 6
Taking an industrial production device of long-chain dicarboxylic acid with the nominal capacity of 6000 tons/year as an example, the technical method is the same as that of the example 1, the operating pressure of an extraction kettle is 240kPaA, the operating temperature is 95 ℃, and the density of an oil layer material is 830kg/m3The density of the water layer material is 1000kg/m3In the materials entering the extraction kettle, 49 wt% of oil layer materials, 11 wt% of middle layer materials and 40 wt% of water layer materials are contained. Therefore, complete discharge of oil and water phases is realized, the utilization rate of the reaction kettle is increased, materials are not mixed, and the situation that the materials in the middle layer are not removed from an oil layer or a water layer is ensured.
Claims (7)
1. A control system for oil-water discharging process in long-chain binary acid extraction refining is characterized in that: the device comprises an extraction kettle (V1), a differential pressure type liquid level meter (A1), a capacitance instrument (A2), an intermediate layer discharge control valve (H1), a water phase discharge control valve (H2), an oil phase discharge control valve (H3) and a controller (C1), wherein the controller (C1) is connected with the differential pressure type liquid level meter (A1), the capacitance instrument (A2), the intermediate layer discharge control valve (H1), the water phase discharge control valve (H2) and the oil phase discharge control valve (H3), and the differential pressure type liquid level meter (A1) and the capacitance instrument (A2) are used for monitoring an oil-water interface in the extraction kettle.
2. The control system for the oil-water discharging process in the extraction and refining of the long-chain dicarboxylic acid as claimed in claim 1, wherein: the extraction kettle is provided with a middle layer discharge hole (N1), a water phase discharge hole (N2), an oil phase discharge hole (N3), a capacitance instrument hole (N4), a first differential pressure type liquid level meter instrument hole (N5) and a second differential pressure type liquid level meter instrument hole (N6), and the relative position heights of the pipe holes are respectively second differential pressure type liquid level meter hole (N6) > oil phase discharge hole (N3) > first differential pressure type liquid level meter instrument hole (N5) > capacitance instrument hole (N4) > water phase discharge hole (N2) > extraction kettle is provided with a middle layer discharge hole (N1).
3. A control method of the control system according to claim 1, characterized by comprising the steps of:
(a) the control system adopts a differential pressure liquid level meter (A1) and a capacitance instrument (A2) to monitor an oil-water interface simultaneously, when any instrument monitors an oil phase, a signal is transmitted to a controller (C1), and the controller (C1) closes a water phase discharging control valve to finish water phase discharging;
(b) opening an oil phase discharging control valve (H3) to start oil phase discharging;
(c) after the oil phase is discharged, the middle layer material is still in the extraction kettle (V1), and after the next batch of material enters the extraction kettle (V1), mixing and extracting are carried out.
4. The control method according to claim 3, characterized in that: in the step (c), when the middle layer is accumulated to a certain volume, the middle layer discharging control valve (H1) is opened to discharge the middle layer from the middle layer discharging hole (N1) to a designated place.
5. The control method according to claim 3, characterized in that: the operation pressure of the extraction kettle is 100-300kPaA, and the operation temperature is 75-98 ℃.
6. The control method according to claim 3, characterized in that: the density of the oil phase material is 750-900kg/m3The density of the water phase material is 950-1050kg/m3。
7. The control method according to claim 3, characterized in that: the oil layer material accounts for 44-50 wt%, the middle layer material accounts for 10-14 wt% and the water layer material accounts for 36-46 wt% of the materials entering the extraction kettle.
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Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| AU1753000A (en) * | 1999-02-16 | 2000-08-17 | Solvents Australia Pty Ltd | Solvent extraction apparatus and process |
| CN204319839U (en) * | 2014-12-03 | 2015-05-13 | 武汉旭日华科技发展有限公司 | For the vacuum storage tank in vacuum desorption |
| CN207680089U (en) * | 2017-11-28 | 2018-08-03 | 浙江华亿工程设计股份有限公司 | The extraction equipment of emulsion layer is handled using emulsion layer conservation tank |
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2021
- 2021-06-30 CN CN202110738394.0A patent/CN113398625A/en active Pending
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| AU1753000A (en) * | 1999-02-16 | 2000-08-17 | Solvents Australia Pty Ltd | Solvent extraction apparatus and process |
| CN204319839U (en) * | 2014-12-03 | 2015-05-13 | 武汉旭日华科技发展有限公司 | For the vacuum storage tank in vacuum desorption |
| CN207680089U (en) * | 2017-11-28 | 2018-08-03 | 浙江华亿工程设计股份有限公司 | The extraction equipment of emulsion layer is handled using emulsion layer conservation tank |
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Application publication date: 20210917 |