CN213466793U - Glycerol concentration device - Google Patents
Glycerol concentration device Download PDFInfo
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- CN213466793U CN213466793U CN202022013269.7U CN202022013269U CN213466793U CN 213466793 U CN213466793 U CN 213466793U CN 202022013269 U CN202022013269 U CN 202022013269U CN 213466793 U CN213466793 U CN 213466793U
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/50—Improvements relating to the production of bulk chemicals
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Abstract
The utility model discloses a glycerine enrichment facility, it includes one effect evaporimeter, two effect evaporimeters, three effect evaporimeter A, three effect evaporimeter B, one effect evaporimeter, two effect evaporimeters, three effect evaporimeter A, three effect evaporimeter B series connection in proper order, one of them effect evaporimeter, two effect evaporimeters, three effect evaporimeter A are climbing film evaporator, and three effect evaporimeter B is central circulation tubular evaporator. The utility model discloses a high-efficient steam that utilizes of multiple-effect evaporation to reach the energy saving, reduce the steam quantity, improve evaporation efficiency's purpose.
Description
Technical Field
The utility model relates to a glycerine evaporation purification device technical field, concretely relates to glycerine enrichment facility.
Background
The heat exchanger performing the evaporation operation is called an evaporator. The evaporator is commonly used for evaporation concentration, evaporation crystallization in the chemical wastewater treatment or chemical production process. The principle of the evaporator is that the materials in the evaporator exchange heat with a heat source (steam), and after the solution is heated, part of the solvent is vaporized and separated out, so that the concentration of the solution is increased, namely the solution is concentrated. Since most of the evaporated solution is aqueous solution, the evaporation process uses water vapor as a heat source to generate water vapor, and for the convenience of distinction, the water vapor as the heat source is called heating vapor or primary vapor, and the vapor evaporated from the solution is called secondary vapor.
The evaporator mainly comprises a heating chamber and a separating chamber. The heating chamber provides heat required for evaporation of the liquid to promote boiling and vaporization of the liquid, and the vapor generated in the heating chamber carries a large amount of liquid foam, and after reaching the separation chamber with a large space, the liquid is separated from the vapor by self-condensation.
In the existing glycerin concentration technology, a large amount of heating steam is consumed in the operation process of an evaporator, and a multi-effect evaporation device can be adopted for saving the heating steam.
SUMMERY OF THE UTILITY MODEL
In order to solve the problem, the utility model provides an energy saving reduces the steam quantity, improves evaporation efficiency's glycerine enrichment facility.
In order to achieve the above object, the utility model adopts the following technical scheme: the evaporator comprises a first-effect evaporator, a second-effect evaporator, a third-effect evaporator A and a third-effect evaporator B, wherein the first-effect evaporator, the second-effect evaporator, the third-effect evaporator A and the third-effect evaporator B are sequentially connected in series, the first-effect evaporator, the second-effect evaporator and the third-effect evaporator A are climbing film evaporators, and the third-effect evaporator B is a central circulating tube evaporator.
The first-effect evaporator comprises a first heating chamber and a first separation chamber, the second-effect evaporator comprises a second heating chamber and a second separation chamber, the third-effect evaporator A comprises a third heating chamber and a third separation chamber, and the third-effect evaporator B comprises a fourth heating chamber;
the lower ends of the tube side of the first heating chamber, the second heating chamber, the third heating chamber and the fourth heating chamber are provided with feed inlets; the shell side upper ends of the first heating chamber, the second heating chamber, the third heating chamber and the fourth heating chamber are all heat source ports;
the air outlet of the first heating chamber is connected with the air inlet of the first separation chamber, the air outlet of the second heating chamber is connected with the air inlet of the second separation chamber, and the air outlets of the third heating chamber and the fourth heating chamber are connected with the air inlet of the third separation chamber;
the air outlet of the first separation chamber is connected with the heat source ports of the second heating chamber and the fourth heating chamber, the air outlet of the second separation chamber is connected with the heat source port of the third heating chamber, and the pipeline of the air outlet of the third separation chamber is connected with a vacuumizing unit;
the discharge hole of the first separation chamber is connected with the feed inlet of the second heating chamber, the discharge hole of the second separation chamber is connected with the feed inlet of the third heating chamber, the upper end of the tube pass of the third heating chamber is provided with a discharge hole, the discharge hole is connected with the feed inlet of the fourth heating chamber, and the discharge hole of the fourth heating chamber is arranged at the lower end of the tube pass;
and the lower end circulating liquid discharge port of the first separation chamber is connected with the lower end circulating liquid feed inlet of the first heating chamber tube side, the lower end circulating liquid discharge port of the second separation chamber is connected with the lower end circulating liquid feed inlet of the second heating chamber tube side, and the lower end circulating liquid discharge port of the third separation chamber is connected with the lower end circulating liquid feed inlet of the third heating chamber tube side.
The lower ends of the first heating chamber, the second heating chamber, the third heating chamber and the fourth heating chamber are respectively provided with a condensed water outlet, wherein the condensed water outlets of the second heating chamber and the fourth heating chamber are respectively connected to the lower end of the third heating chamber and are uniformly discharged from the condensed water outlet of the third heating chamber.
Pneumatic valves are arranged on the first heating chamber, the second heating chamber, the third heating chamber feeding pipelines and the first heating chamber heat source pipeline, and a flowmeter is arranged on the first heating chamber feeding port pipeline.
The first separation chamber, the second separation chamber and the third separation chamber are all provided with thermometers, and the upper end of the third separation chamber is also provided with a pressure gauge.
Use the utility model discloses a beneficial effect is: the evaporator carries out multi-effect evaporation, improves the utilization rate of steam, and achieves the purposes of saving energy and improving the evaporation efficiency. The principle of the efficient utilization of steam by the evaporator is that after steam (primary steam) is subjected to one-effect heat exchange, steam (secondary steam) evaporated from materials enters the next effect to provide a heat source for the next effect, the operating pressure and the boiling point of the next effect are lower than those of the previous effect, and the like, so that the efficient utilization is achieved. The more the evaporator is used, the better the energy-saving effect is, but the more the effect is, the larger the temperature difference loss is, so the effect is limited to a certain extent.
Drawings
Fig. 1 is a schematic structural diagram of the present invention.
The reference numerals include:
1 is a one-effect evaporator, 1-1 is a first heating chamber, 1-2 is a first separation chamber,
2 is a double-effect evaporator, 2-1 is a second heating chamber, 2-2 is a second separation chamber,
3 is a triple-effect evaporator A, 3-1 is a third heating chamber, 3-2 is a third separation chamber,
4 is a triple-effect evaporator B, 4-1 is a fourth heating chamber,
5 is pneumatic valve, 6 is thermometer, 7 is manometer, 8 is vacuum pumping unit, and 9 is flowmeter.
Detailed Description
In order to make the purpose, technical solution and advantages of the present technical solution more clear, the present technical solution is further described in detail below with reference to specific embodiments. It should be understood that the description is intended to be exemplary only, and is not intended to limit the scope of the present teachings.
The utility model discloses a glycerine enrichment facility.
It includes one effect evaporimeter (1), two effect evaporimeter (2), three effect evaporimeter A (3), three effect evaporimeter B (4), one effect evaporimeter (1), two effect evaporimeter (2), three effect evaporimeter A (3), three effect evaporimeter B (4) series connection in proper order, one of them effect evaporimeter (1), two effect evaporimeter (2), three effect evaporimeter A (3) are climbing film evaporator, and three effect evaporimeter B (4) are central authorities' circulation tubular evaporator.
The first-effect evaporator (1) comprises a first heating chamber (1-1) and a first separation chamber (1-2), the second-effect evaporator (2) comprises a second heating chamber (2-1) and a second separation chamber (2-2), the third-effect evaporator A (3) comprises a third heating chamber (3-1) and a third separation chamber (3-2), and the third-effect evaporator B (4) comprises a fourth heating chamber (4-1);
the lower end of the tube side of the first heating chamber (1-1), the second heating chamber (2-1), the third heating chamber (3-1) and the fourth heating chamber (4-1) is provided with a feed inlet; the upper ends of the first heating chamber (1-1), the second heating chamber (2-1), the third heating chamber (3-1) and the fourth heating chamber (4-1) are all heat source ports;
the air outlet of the first heating chamber (1-1) is connected with the air inlet of the first separation chamber (1-2), the air outlet of the second heating chamber (2-1) is connected with the air inlet of the second separation chamber (2-2), and the air outlets of the third heating chamber (3-1) and the fourth heating chamber (4-1) are connected with the air inlet of the third separation chamber (3-2);
the air outlet of the first separation chamber (1-2) is connected with the heat source ports of the second heating chamber (2-1) and the fourth heating chamber (4-1), the air outlet of the second separation chamber (2-2) is connected with the heat source port of the third heating chamber (3-1), and the air outlet pipeline of the third separation chamber (3-2) is connected with a vacuumizing unit (8);
the discharge hole of the first separation chamber (1-2) is connected with the feed hole of the second heating chamber (2-1), the discharge hole of the second separation chamber (2-2) is connected with the feed hole of the third heating chamber (3-1), the upper end of the tube side of the third heating chamber (3-1) is provided with a discharge hole, the discharge hole is connected with the feed hole of the fourth heating chamber (4-1), and the discharge hole of the fourth heating chamber (4-1) is arranged at the lower end of the tube side;
a circulating liquid discharge port at the lower end of the first separation chamber (1-2) is connected with a circulating liquid feed port at the lower end of a tube side of the first heating chamber (1-1), a circulating liquid discharge port at the lower end of the second separation chamber (2-2) is connected with a circulating liquid feed port at the lower end of a tube side of the second heating chamber (2-1), and a circulating liquid discharge port at the lower end of the third separation chamber (3-2) is connected with a circulating liquid feed port at the lower end of a tube side of the third heating chamber (3-1);
the lower ends of the first heating chamber (1-1), the second heating chamber (2-1), the third heating chamber (3-1) and the fourth heating chamber (4-1) are respectively provided with a condensed water outlet, wherein the condensed water outlets of the second heating chamber (2-1) and the fourth heating chamber (4-1) are respectively connected to the lower end of the third heating chamber (3-1), and are uniformly discharged through the condensed water outlet of the third heating chamber (3-1).
The first heating chamber (1-1), the second heating chamber (2-1), the third heating chamber (3-1) and the heat source pipeline of the first heating chamber (1-1) are respectively provided with a pneumatic valve (5), and a flow meter (9) is arranged on the feed inlet pipeline of the first heating chamber (1-1).
The device is characterized in that the upper ends of the first separation chamber (1-2), the second separation chamber (2-2) and the third separation chamber (3-2) are respectively provided with a thermometer (6), and the upper end of the third separation chamber (3-2) is also provided with a pressure gauge (7).
When the evaporator is actually used, the first-effect evaporator, the second-effect evaporator and the third-effect evaporator A are climbing film evaporators, and the third-effect evaporator B is a central circulating tube evaporator. The glycerin evaporation is usually triple effect evaporation, and the unit steam consumption of the triple effect is 0.4 by considering various temperature difference losses and heat loss of the evaporator. And the utility model discloses increase a triple effect evaporimeter B (central circulating tube evaporator) behind triple effect evaporimeter A, make the utility model discloses be close the effect of four-effect evaporation (the unit steam consumption of four-effect evaporation is 0.3), triple effect evaporimeter B's heating medium is the secondary steam that one-effect evaporimeter separating chamber produced, does not additionally increase the quantity of steam, and triple effect evaporimeter B's addition has further reduced the steam quantity on the contrary (the unit steam consumption is less than 0.4), has improved evaporation efficiency simultaneously.
The crude glycerin water preheated to be close to the boiling point is pumped from the lower pipe stroke of the one-effect evaporator under the control of the flow meter and the pneumatic valve, the crude glycerin water is driven by secondary steam which rises at a high speed, evaporation is carried out while flowing like a film along the wall surface, the required concentration can be achieved at the top of the first heating chamber, and the concentrated glycerin water is discharged from the bottom of the first separation chamber. The discharged liquid flows into the lower part of the tube pass of the double-effect evaporator under the control of the pneumatic valve, the glycerin water is driven by secondary steam which rises at a high speed, evaporation is carried out while the glycerin water flows like a film along the wall surface, the required concentration can be achieved at the top of the second heating chamber, and the condensed glycerin water is discharged from the bottom of the second separation chamber. The discharged liquid flows into the lower part of the tube pass A of the triple-effect evaporator under the control of the pneumatic valve, the glycerol water is driven by secondary steam which rises at a high speed and flows like a film along the wall surface to evaporate, the required concentration can be achieved at the top of the third heating chamber, the concentrated glycerol water flows into the lower part of the tube pass B of the triple-effect evaporator from the upper part of the tube pass A of the triple-effect evaporator, the triple-effect evaporator B has the advantages of good solution circulation and high heat transfer efficiency, the glycerol water can be quickly separated to achieve the concentration of the finished glycerol, and the finished glycerol meeting the concentration requirement flows out from the lower part of the tube pass B of the triple-effect evaporator.
The vacuum in the third separation chamber reduces the operating pressure of the second effect evaporator, the third effect evaporator A, B and the boiling point of the solution, so that the secondary steam of the front effect can be introduced as the heating medium of the back effect. The utility model discloses in, steam lets in one effect evaporator shell side under pneumatic valve control, the steam condensate water is discharged from one effect evaporator shell side bottom, the steam in the one effect evaporator disengagement chamber gives the heating of two effect evaporator and three effect evaporator B, the steam of two effect evaporator disengagement chamber production gives the heating of three effect evaporator A, the condensate that two effect evaporator and three effect evaporator B produced is discharged into three effect evaporator A shell side to the condensate that produces with three effect evaporator A is discharged from three effect evaporator A's shell side below.
The foregoing is only a preferred embodiment of the present invention, and many variations can be made in the specific embodiments and applications of the present invention by those skilled in the art without departing from the spirit of the present invention.
Claims (5)
1. A glycerine enrichment facility which characterized in that: the evaporator comprises a first-effect evaporator, a second-effect evaporator, a third-effect evaporator A and a third-effect evaporator B, wherein the first-effect evaporator, the second-effect evaporator, the third-effect evaporator A and the third-effect evaporator B are sequentially connected in series, the first-effect evaporator, the second-effect evaporator and the third-effect evaporator A are climbing film evaporators, and the third-effect evaporator B is a central circulating tube evaporator.
2. A glycerol concentrator as claimed in claim 1, wherein: the first-effect evaporator comprises a first heating chamber and a first separation chamber, the second-effect evaporator comprises a second heating chamber and a second separation chamber, the third-effect evaporator A comprises a third heating chamber and a third separation chamber, and the third-effect evaporator B comprises a fourth heating chamber;
the lower ends of the tube side of the first heating chamber, the second heating chamber, the third heating chamber and the fourth heating chamber are provided with feed inlets; the shell side upper ends of the first heating chamber, the second heating chamber, the third heating chamber and the fourth heating chamber are all heat source ports;
the air outlet of the first heating chamber is connected with the air inlet of the first separation chamber, the air outlet of the second heating chamber is connected with the air inlet of the second separation chamber, and the air outlets of the third heating chamber and the fourth heating chamber are connected with the air inlet of the third separation chamber;
the air outlet of the first separation chamber is connected with the heat source ports of the second heating chamber and the fourth heating chamber, the air outlet of the second separation chamber is connected with the heat source port of the third heating chamber, and the pipeline of the air outlet of the third separation chamber is connected with a vacuumizing unit;
the discharge hole of the first separation chamber is connected with the feed inlet of the second heating chamber, the discharge hole of the second separation chamber is connected with the feed inlet of the third heating chamber, the upper end of the tube pass of the third heating chamber is provided with a discharge hole, the discharge hole is connected with the feed inlet of the fourth heating chamber, and the discharge hole of the fourth heating chamber is arranged at the lower end of the tube pass;
and the lower end circulating liquid discharge port of the first separation chamber is connected with the lower end circulating liquid feed inlet of the first heating chamber tube side, the lower end circulating liquid discharge port of the second separation chamber is connected with the lower end circulating liquid feed inlet of the second heating chamber tube side, and the lower end circulating liquid discharge port of the third separation chamber is connected with the lower end circulating liquid feed inlet of the third heating chamber tube side.
3. A glycerol concentrator as claimed in claim 2, wherein: the lower ends of the first heating chamber, the second heating chamber, the third heating chamber and the fourth heating chamber are respectively provided with a condensed water outlet, wherein the condensed water outlets of the second heating chamber and the fourth heating chamber are respectively connected to the lower end of the third heating chamber and are uniformly discharged from the condensed water outlet of the third heating chamber.
4. A glycerol concentrator as claimed in claim 2, wherein: pneumatic valves are arranged on the first heating chamber, the second heating chamber, the third heating chamber feeding pipelines and the first heating chamber heat source pipeline, and a flowmeter is arranged on the first heating chamber feeding port pipeline.
5. A glycerol concentrator as claimed in claim 2, wherein: the first separation chamber, the second separation chamber and the third separation chamber are all provided with thermometers, and the upper end of the third separation chamber is also provided with a pressure gauge.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202022013269.7U CN213466793U (en) | 2020-09-15 | 2020-09-15 | Glycerol concentration device |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202022013269.7U CN213466793U (en) | 2020-09-15 | 2020-09-15 | Glycerol concentration device |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN213466793U true CN213466793U (en) | 2021-06-18 |
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ID=76419234
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202022013269.7U Active CN213466793U (en) | 2020-09-15 | 2020-09-15 | Glycerol concentration device |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN213466793U (en) |
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2020
- 2020-09-15 CN CN202022013269.7U patent/CN213466793U/en active Active
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| GR01 | Patent grant | ||
| GR01 | Patent grant | ||
| PE01 | Entry into force of the registration of the contract for pledge of patent right | ||
| PE01 | Entry into force of the registration of the contract for pledge of patent right |
Denomination of utility model: A glycerol concentration device Effective date of registration: 20220929 Granted publication date: 20210618 Pledgee: Shengjing Bank Co.,Ltd. Liaoyang Hongwei Sub branch Pledgor: Liaoning Shengde Huaxing Chemical Co.,Ltd. Registration number: Y2022210000155 |
|
| PC01 | Cancellation of the registration of the contract for pledge of patent right | ||
| PC01 | Cancellation of the registration of the contract for pledge of patent right |
Date of cancellation: 20230925 Granted publication date: 20210618 Pledgee: Shengjing Bank Co.,Ltd. Liaoyang Hongwei Sub branch Pledgor: Liaoning Shengde Huaxing Chemical Co.,Ltd. Registration number: Y2022210000155 |
|
| PE01 | Entry into force of the registration of the contract for pledge of patent right | ||
| PE01 | Entry into force of the registration of the contract for pledge of patent right |
Denomination of utility model: A glycerol concentration device Effective date of registration: 20230926 Granted publication date: 20210618 Pledgee: Shengjing Bank Co.,Ltd. Liaoyang Hongwei Sub branch Pledgor: Liaoning Shengde Huaxing Chemical Co.,Ltd. Registration number: Y2023210000247 |