CN216629750U - System for separate pentaerythritol and calcium formate from pentaerythritol mother liquor - Google Patents
System for separate pentaerythritol and calcium formate from pentaerythritol mother liquor Download PDFInfo
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- CN216629750U CN216629750U CN202123428352.1U CN202123428352U CN216629750U CN 216629750 U CN216629750 U CN 216629750U CN 202123428352 U CN202123428352 U CN 202123428352U CN 216629750 U CN216629750 U CN 216629750U
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Abstract
A system for separating pentaerythritol and calcium formate from pentaerythritol mother liquor comprises an extraction tower, wherein a first feed inlet formed in the extraction tower is communicated with a mother liquor feed pipe through a mother liquor feed pump, and a second feed inlet formed in the extraction tower is communicated with an extractant storage tank; a first discharge port formed in the extraction tower is communicated with a first feed inlet formed in the back extraction tower through a pipeline, and a second discharge port formed in the extraction tower is communicated with a feed inlet formed in the raffinate tank through a pipeline; a second feed port formed in the back extraction tower is communicated with the desalted water feeding device through a pipeline, a first discharge port formed in the back extraction tower is communicated with a feed port formed in the extraction liquid tank through a pipeline, and a second discharge port formed in the back extraction tower is communicated with a feed port formed in the raffinate liquid tank through a pipeline; the pentaerythritol and calcium formate products separated by the system have high quality and high recovery rate, and the extracting agent can be separated, recovered and recycled, so that the treatment cost for separating pentaerythritol and calcium formate from pentaerythritol mother liquor is greatly reduced.
Description
Technical Field
The utility model belongs to the technical field of biochemical equipment manufacturing, and particularly relates to a system for separating pentaerythritol and calcium formate from pentaerythritol mother liquor.
Background
Pentaerythritol belongs to polyhydric alcohol organic matters, is white crystal or powder, is combustible, and is a key raw material for producing high-solid-content, water-soluble and general alkyd resin, rosin ester, synthetic lubricating oil and antioxidant. In the process of producing pentaerythritol, a large amount of mother liquor is produced, the mother liquor contains considerable pentaerythritol and calcium formate with industrial value, and if the mother liquor is not recycled, a large amount of industrial products of pentaerythritol and calcium formate are lost, and a serious environmental protection problem is caused. In the existing mother liquor recovery treatment process, the mother liquor is enriched and viscous in the concentration process, pentaerythritol crystals are difficult to separate from the mother liquor, a large amount of pentaerythritol is not effectively recovered, the recovery rates of pentaerythritol and calcium formate are low, the product quality is general, the consumption of an organic solvent is large, the separation cost is high, the content of organic matters in the treated waste liquor is high, and the serious environmental protection problem still exists.
Therefore, it is necessary to design a system for separating pentaerythritol and calcium formate from a pentaerythritol mother liquor to solve the above technical problems.
It should be noted that the above background description is only for the sake of clarity and complete description of the technical solutions of the present invention and for the understanding of those skilled in the art. Such solutions are not considered to be known to the person skilled in the art merely because they have been set forth in the background section of the utility model.
Disclosure of Invention
In order to overcome the defects in the prior art, the utility model aims to provide a system for separating pentaerythritol and calcium formate from a pentaerythritol mother liquor.
In order to achieve the above objects and other related objects, the present invention provides the following technical solutions: a system for separating pentaerythritol and calcium formate from pentaerythritol mother liquor comprises an extraction tower, wherein a first feed inlet formed in the extraction tower is communicated with a mother liquor feed pipe through a mother liquor feed pump, and a second feed inlet formed in the extraction tower is communicated with an extractant storage tank through an extractant feed pump; a first discharge port formed in the extraction tower is communicated with a first feed port formed in the back extraction tower through a pipeline, and a second discharge port formed in the extraction tower is communicated with a feed port formed in the raffinate tank through a pipeline; the second feed inlet of seting up on the stripping tower passes through pipeline intercommunication desalinized water feed arrangement, the first discharge gate of seting up on the stripping tower passes through the feed inlet of seting up on the pipeline intercommunication extraction liquid groove, the second discharge gate of seting up on the stripping tower passes through the feed inlet of seting up on the pipeline intercommunication raffinate groove, the discharge gate of seting up on the raffinate groove passes through weak solvent recovery charge pump intercommunication weak solvent recovery processing mechanism, simultaneously the discharge gate of seting up on the extraction liquid groove passes through solvent recovery charge pump intercommunication solvent recovery processing mechanism.
Preferably, dilute solvent recovery processing mechanism includes dilute solvent recovery tower, the feed inlet of seting up on the dilute solvent recovery tower passes through pipeline and dilute solvent recovery charge-in pump intercommunication, the first discharge gate of seting up on the dilute solvent recovery tower passes through the feed inlet of seting up on the pipeline intercommunication solvent recovery reboiler, the second discharge gate of seting up on the dilute solvent recovery tower passes through pipeline intercommunication dilute solvent recovery pump, the discharge gate of seting up on the solvent recovery reboiler passes through pipeline intercommunication dilute solvent recovery delayer.
Preferably, the solvent recovery processing mechanism comprises a solvent recovery tower, a first feed inlet formed in the solvent recovery tower is communicated with a solvent recovery feed pump through a pipeline, a first discharge outlet formed in the solvent recovery tower is communicated with a feed inlet formed in the solvent recovery condenser through a pipeline, a second discharge outlet formed in the solvent recovery tower is communicated with the solvent recovery pump through a pipeline, and a discharge outlet formed in the solvent recovery condenser is communicated with the solvent recovery reflux tank.
Preferably, a first discharge port formed in the dilute solvent recovery delayer is communicated with the extractant tank through a pipeline, and a second discharge port formed in the dilute solvent recovery delayer is communicated with the raffinate tank through a pipeline.
Preferably, a first discharge port formed in the solvent recovery reflux tank is communicated with the solvent recovery vacuum pump through a pipeline, and a second discharge port formed in the solvent recovery reflux tank is communicated with a second feed port formed in the solvent recovery tower through the solvent recovery reflux pump and the pipeline.
Due to the application of the technical scheme, compared with the prior art, the utility model has the following advantages:
the system for separating pentaerythritol and calcium formate from pentaerythritol mother liquor designed by the scheme can realize circulating continuous treatment on the pentaerythritol mother liquor, the pentaerythritol and calcium formate products obtained by the system through separation are high in quality and recovery rate, and the extracting agent can be separated, recovered and recycled, so that the treatment cost for separating pentaerythritol and calcium formate from the pentaerythritol mother liquor is greatly reduced, the discharged waste liquor is greatly reduced, and the pressure of environmental protection treatment is reduced. The system has the advantages of compact structure, simple operation, small occupied area and low investment, improves the treatment efficiency of pentaerythritol mother liquor, improves the recovery rate of pentaerythritol and calcium formate, reduces the consumption of organic solvent, saves energy, and has better application prospect and comprehensive economic benefit.
Drawings
Fig. 1 is a schematic diagram of the overall structure of the system.
In the above drawings, an extraction tower 1, a stripping tower 2, a dilute solvent recovery tower 3, a solvent recovery tower 4, a solvent recovery reboiler 5, a solvent recovery condenser 6, a mother liquor feed pump 7, an extractant feed pump 8, a dilute solvent recovery feed pump 9, a solvent recovery feed pump 10, a dilute solvent recovery pump 11, a solvent recovery pump 12, a solvent recovery reflux pump 13, a solvent recovery vacuum pump 14, an extractant tank 15, a raffinate tank 16, an extraction liquid tank 17, a dilute solvent recovery delaminator 18, and a solvent recovery reflux tank 19.
Detailed Description
The following description of the embodiments of the present invention is provided for illustrative purposes, and other advantages and effects of the present invention will become apparent to those skilled in the art from the present disclosure.
Please refer to fig. 1. It should be understood that in the description of the present invention, it should be noted that the terms "center", "upper", "lower", "left", "right", "vertical", "horizontal", "inner", "outer", etc. indicate the orientation or positional relationship based on the orientation or positional relationship shown in the drawings, or the orientation or positional relationship which the products of the present invention are usually placed in when used, which is only for the convenience of describing the present invention and simplifying the description, but does not indicate or imply that the device or element referred to must have a specific orientation, be constructed in a specific orientation, and be operated, and therefore, should not be construed as limiting the present invention. Furthermore, the terms "first," "second," "third," and the like are used solely to distinguish one from another and are not to be construed as indicating or implying relative importance. The terms "horizontal", "vertical", "overhang" and the like do not imply that the components are required to be absolutely horizontal or overhang, but may be slightly inclined. For example, "horizontal" merely means that the direction is more horizontal than "vertical" and does not mean that the structure must be perfectly horizontal, but may be slightly inclined.
In the description of the present invention, it should be further noted that, unless otherwise specifically stated or limited, the terms "disposed," "mounted," "connected," and "connected" are to be construed broadly and may include, for example, a fixed connection, a detachable connection, an integral connection, a mechanical connection, an electrical connection, a direct connection, an indirect connection via an intermediate medium, and a communication between two elements. The specific meanings of the above terms in the present invention can be understood in specific cases to those skilled in the art.
Example (b): as shown in fig. 1, a system for separating pentaerythritol and calcium formate from pentaerythritol mother liquor comprises an extraction tower 1, wherein a first feed inlet formed in the extraction tower 1 is communicated with a mother liquor feed pipe through a mother liquor feed pump 7, and a second feed inlet formed in the extraction tower 1 is communicated with an extractant storage tank 15 through an extractant feed pump 8; a first discharge port formed in the extraction tower 1 is communicated with a first feed port formed in the back extraction tower 2 through a pipeline, and a second discharge port formed in the extraction tower 1 is communicated with a feed port formed in the raffinate tank 16 through a pipeline; the second feed inlet of seting up on the stripping tower 2 passes through pipeline intercommunication desalinized water feed arrangement, the first discharge gate of seting up on the stripping tower 2 passes through the feed inlet of seting up on pipeline intercommunication extraction liquid groove 17, the second discharge gate of seting up on the stripping tower 2 passes through the feed inlet of seting up on pipeline intercommunication raffinate cistern 16, the discharge gate of seting up on the raffinate cistern 16 passes through thin solvent recovery charge pump 10 intercommunication thin solvent recovery processing mechanism, simultaneously the discharge gate of seting up on the extraction liquid groove 17 passes through solvent recovery charge pump 10 intercommunication solvent recovery processing mechanism.
The preferred embodiment is as follows:
dilute solvent recovery processing mechanism includes dilute solvent recovery tower 3, the feed inlet of seting up on the dilute solvent recovery tower 3 passes through pipeline and dilute solvent recovery charge-in pump 10 intercommunication, the first discharge gate of seting up on the dilute solvent recovery tower 3 passes through the feed inlet of seting up on pipeline intercommunication solvent recovery reboiler 5, the second discharge gate of seting up on the dilute solvent recovery tower 3 passes through pipeline intercommunication dilute solvent recovery pump 11, the discharge gate of seting up on the solvent recovery reboiler 5 passes through pipeline intercommunication dilute solvent recovery delayer 18.
The solvent recovery processing mechanism comprises a solvent recovery tower 4, a first feed inlet formed in the solvent recovery tower 4 is communicated with a solvent recovery feed pump 10 through a pipeline, a first discharge outlet formed in the solvent recovery tower 4 is communicated with a feed inlet formed in a solvent recovery condenser 6 through a pipeline, a second discharge outlet formed in the solvent recovery tower 4 is communicated with a solvent recovery pump 12 through a pipeline, and a discharge outlet formed in the solvent recovery condenser 6 is communicated with a solvent recovery reflux tank 19.
A first discharge port formed in the dilute solvent recovery delayer 18 is communicated with the extractant tank 15 through a pipeline, and a second discharge port formed in the dilute solvent recovery delayer 18 is communicated with the raffinate tank 16 through a pipeline.
A first discharge port formed in the solvent recovery reflux tank 19 is communicated with the solvent recovery vacuum pump 14 through a pipeline, and a second discharge port formed in the solvent recovery reflux tank 19 is communicated with a second feed port formed in the solvent recovery tower 4 through the solvent recovery reflux pump 13 and the pipeline.
The specific process comprises the following steps:
the first step is as follows: conveying pentaerythritol mother liquor into a mother liquor tank through a pipeline for storage, conveying the pentaerythritol mother liquor into the upper part of an extraction tower through a mother liquor feeding pump (the pentaerythritol mother liquor enters a mother liquor heater after being pressurized, the pentaerythritol mother liquor enters the upper part of the extraction tower at the temperature of 50-70 ℃, conveying liquid in an extractant tank into an extractant heater after being pressurized by a pump, and conveying the liquid at the temperature of 50-70 ℃ into the lower part of the extraction tower;
the second step is that: and enabling the desalted water to enter a desalted water heater, and controlling the temperature to be 50-70 ℃ to enter the upper part of the stripping tower. The liquid at the top of the back extraction tower enters an extraction liquid tank, and the liquid at the bottom of the back extraction tower enters an extraction raffinate tank;
the third step: the liquid in the raffinate tank is pressurized by a dilute solvent recovery feed pump and then is sent to the upper part of a dilute solvent recovery tower, steam at the top of the dilute solvent recovery tower enters a dilute solvent recovery condenser, condensate enters a dilute solvent recovery delayer, an oil layer returns to an extractant tank for recycling, and a water layer returns to the extractant tank to continuously recover the solvent in the extractant tank. A dilute solvent recovery reboiler at the lower part of the dilute solvent recovery tower uses water vapor as a heat source for heating, and wastewater with less solvent at the tower bottom is pressurized by a bottom pump of the solvent recovery tower and then is sent out;
the fourth step: the extraction liquid tank is provided with low-level water diversion, and the separated water layer is sent to the raffinate tank. The oil layer in the extracting liquid tank is pressurized by a solvent recovery feed pump and then is sent to the middle part of a solvent recovery tower, the steam at the top of the solvent recovery tower enters a solvent recovery condenser and a solvent recovery tail cooler, the condensate enters a reflux tank of the solvent recovery tower, a part of the condensate flows back into the solvent recovery tower after being pressurized by a solvent recovery reflux pump, and a part of the condensate is sent to an extracting agent tank for recycling. The liquid at the bottom of the solvent recovery tower is pressurized by a solvent recovery circulating pump and then sent into a solvent recovery reboiler, the solvent recovery reboiler is heated by using water vapor as a heat source, the heated gas-liquid phase enters the bottom of the solvent recovery tower, and high-boiling-point substances are extracted from the lower end socket of the solvent recovery reboiler and sent out by a solvent recovery discharge pump. The solvent recovery tower is operated in vacuum, and is vacuumized by using a solvent recovery vacuum pump.
The foregoing embodiments are merely illustrative of the principles and utilities of the present invention and are not intended to limit the utility model. Those skilled in the art can modify or change the above-described embodiments without departing from the spirit and scope of the present invention. Accordingly, it is intended that all equivalent modifications or changes which may be made by those skilled in the art without departing from the spirit and scope of the present invention as defined in the appended claims.
Claims (5)
1. A system for separating pentaerythritol and calcium formate from pentaerythritol mother liquor is characterized in that: the extraction tower is provided with a first feed inlet which is communicated with a mother liquor feed pipe through a mother liquor feed pump, and a second feed inlet which is communicated with an extractant storage tank through an extractant feed pump; a first discharge port formed in the extraction tower is communicated with a first feed port formed in the back extraction tower through a pipeline, and a second discharge port formed in the extraction tower is communicated with a feed port formed in the raffinate tank through a pipeline; the second feed inlet of seting up on the stripping tower passes through pipeline intercommunication desalinized water feed arrangement, the first discharge gate of seting up on the stripping tower passes through the feed inlet of seting up on the pipeline intercommunication extraction liquid groove, the second discharge gate of seting up on the stripping tower passes through the feed inlet of seting up on the pipeline intercommunication raffinate groove, the discharge gate of seting up on the raffinate groove passes through weak solvent recovery charge pump intercommunication weak solvent recovery processing mechanism, simultaneously the discharge gate of seting up on the extraction liquid groove passes through solvent recovery charge pump intercommunication solvent recovery processing mechanism.
2. The system for separating pentaerythritol and calcium formate from pentaerythritol mother liquor as claimed in claim 1, wherein: dilute solvent recovery processing mechanism includes the dilute solvent recovery tower, the feed inlet of seting up on the dilute solvent recovery tower passes through pipeline and dilute solvent recovery charge-in pump intercommunication, the first discharge gate of seting up on the dilute solvent recovery tower passes through the feed inlet of seting up on the pipeline intercommunication solvent recovery reboiler, the second discharge gate of seting up on the dilute solvent recovery tower passes through pipeline intercommunication dilute solvent recovery pump, the discharge gate of seting up on the solvent recovery reboiler passes through pipeline intercommunication dilute solvent recovery delayer.
3. The system for separating pentaerythritol and calcium formate from pentaerythritol mother liquor as claimed in claim 1, wherein: the solvent recovery processing mechanism comprises a solvent recovery tower, a first feed inlet formed in the solvent recovery tower is communicated with a solvent recovery feed pump through a pipeline, a first discharge outlet formed in the solvent recovery tower is communicated with a feed inlet formed in a solvent recovery condenser through a pipeline, a second discharge outlet formed in the solvent recovery tower is communicated with the solvent recovery pump through a pipeline, and a discharge outlet formed in the solvent recovery condenser is communicated with a solvent recovery reflux tank.
4. The system for separating pentaerythritol and calcium formate from pentaerythritol mother liquor as claimed in claim 2, wherein: a first discharge port formed in the dilute solvent recovery delayer is communicated with the extractant tank through a pipeline, and a second discharge port formed in the dilute solvent recovery delayer is communicated with the raffinate tank through a pipeline.
5. The system for separating pentaerythritol and calcium formate from pentaerythritol mother liquor as claimed in claim 3, wherein: a first discharge port formed in the solvent recovery reflux tank is communicated with a solvent recovery vacuum pump through a pipeline, and a second discharge port formed in the solvent recovery reflux tank is communicated with a second feed port formed in the solvent recovery tower through the solvent recovery reflux pump and the pipeline.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202123428352.1U CN216629750U (en) | 2021-12-31 | 2021-12-31 | System for separate pentaerythritol and calcium formate from pentaerythritol mother liquor |
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| Application Number | Priority Date | Filing Date | Title |
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| CN202123428352.1U CN216629750U (en) | 2021-12-31 | 2021-12-31 | System for separate pentaerythritol and calcium formate from pentaerythritol mother liquor |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114534307A (en) * | 2021-12-31 | 2022-05-27 | 无锡荣丰生物工程有限公司 | System and method for separating pentaerythritol and calcium formate from pentaerythritol mother liquor |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114534307A (en) * | 2021-12-31 | 2022-05-27 | 无锡荣丰生物工程有限公司 | System and method for separating pentaerythritol and calcium formate from pentaerythritol mother liquor |
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