CN115253350A - Double-tower MVR continuous distillation recovery system and method - Google Patents
Double-tower MVR continuous distillation recovery system and method Download PDFInfo
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- 238000011084 recovery Methods 0.000 title claims abstract description 221
- 238000001944 continuous distillation Methods 0.000 title claims abstract description 25
- 238000000034 method Methods 0.000 title claims abstract description 14
- 239000002904 solvent Substances 0.000 claims abstract description 300
- 238000010992 reflux Methods 0.000 claims abstract description 62
- 238000004821 distillation Methods 0.000 claims abstract description 36
- 238000007906 compression Methods 0.000 claims abstract description 15
- 230000006835 compression Effects 0.000 claims abstract description 13
- 239000002351 wastewater Substances 0.000 claims description 37
- 238000000605 extraction Methods 0.000 claims description 12
- 239000007788 liquid Substances 0.000 claims description 12
- 239000000203 mixture Substances 0.000 claims description 12
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- 230000001105 regulatory effect Effects 0.000 claims description 8
- 238000001514 detection method Methods 0.000 claims description 4
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- 238000005516 engineering process Methods 0.000 description 4
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- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 description 3
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- 229960003160 hyaluronic acid Drugs 0.000 description 1
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- UHVMMEOXYDMDKI-JKYCWFKZSA-L zinc;1-(5-cyanopyridin-2-yl)-3-[(1s,2s)-2-(6-fluoro-2-hydroxy-3-propanoylphenyl)cyclopropyl]urea;diacetate Chemical compound [Zn+2].CC([O-])=O.CC([O-])=O.CCC(=O)C1=CC=C(F)C([C@H]2[C@H](C2)NC(=O)NC=2N=CC(=CC=2)C#N)=C1O UHVMMEOXYDMDKI-JKYCWFKZSA-L 0.000 description 1
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/14—Fractional distillation or use of a fractionation or rectification column
- B01D3/143—Fractional distillation or use of a fractionation or rectification column by two or more of a fractionation, separation or rectification step
- B01D3/146—Multiple effect distillation
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/42—Regulation; Control
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- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
Abstract
The invention belongs to the technical field of solvent distillation recovery, and particularly relates to a double-tower MVR continuous distillation recovery system and a method, wherein the system comprises two connected MVR evaporator systems which are respectively a first MVR evaporator system and a second MVR evaporator system; the first MVR evaporator system comprises a solvent recovery tower I, a compressor I, a reboiler of the recovery tower I, a reflux flash tank of the recovery tower I and a reflux pump of the recovery tower I; compared with the prior art, (1) compared with double-effect distillation recovery and triple-effect distillation recovery processes, the distillation process of the invention does not need primary steam, solvent steam at the top of a compressor compression tower driven by a motor is used as a heat source, and the energy-saving effect is very obvious; (2) The compressor I corresponding to the solvent recovery tower I adopts a smaller compression ratio; and a compressor II of the solvent recovery tower II adopts a larger compression ratio, so that the power consumption in the compression process can be effectively reduced.
Description
Technical Field
The invention relates to the technical field of solvent distillation recovery, in particular to a double-tower MVR continuous distillation recovery system and method.
Background
The solvent recovery mainly relates to various industries such as pharmacy, chemical industry, cellulose, xanthan gum, carrageenan, gellan gum, curdlan, hyaluronic acid and the like. The related solvents mainly comprise ethanol, isopropanol, methanol, acetone and the like. Ten years ago, solvent recovery equipment mostly adopts single-tower distillation plant, adds steam at the bottom of the tower, and top of the tower solvent steam directly passes through the condenser condensation, and the heat is taken away through the circulating water, has caused thermal huge waste.
In the last decade, in order to save energy and reduce consumption, double-effect and triple-effect solvent distillation recovery equipment is adopted in related industries in succession, single-tower distillation recovery equipment is gradually replaced, and the equipment is particularly widely applied to large-scale distillation recovery devices.
The double-effect solvent distillation recovery device saves energy by 30% -40% compared with single-tower distillation recovery equipment, the triple-effect solvent distillation recovery device saves energy by 50% -60% compared with the single-tower distillation recovery equipment, the energy-saving effect is obvious, and the triple-effect solvent distillation recovery device is well received by wide users. But also has the defects of material foaming, coking, equipment blockage and the like caused by the rising of the operation temperature. Meanwhile, with the increasing price of energy, even if a triple-effect solvent distillation recovery device is adopted, the energy cost is still higher, and the energy cost still has a larger reduction space compared with the advanced foreign level.
The MVR technology is widely applied to the fields of wastewater evaporation, seawater desalination and the like at present, and is short for mechanical vapor recompression (mechanical vapor recompression) technology. The method is characterized in that low-grade secondary steam (low in temperature and low in pressure and cannot be utilized) in the evaporation process is compressed by a compressor, the temperature and the pressure of the secondary steam are increased, and the secondary steam is used as a heat source to heat materials to be evaporated again, so that the purpose of recycling the steam is achieved, and no additional steam is needed in the evaporation process; namely, a high-efficiency energy-saving technology which obtains more heat energy by using a small amount of electric energy so as to reduce the requirement of the system on external energy. Except for starting, the whole evaporation process does not need raw steam.
Disclosure of Invention
In order to overcome the defects of the conventional solvent distillation recovery process, the invention provides a double-tower MVR continuous distillation recovery system and a double-tower MVR continuous distillation recovery method.
The invention provides a double-tower MVR continuous distillation recovery system, which comprises two connected MVR evaporator systems, wherein the two MVR evaporator systems are respectively a first MVR evaporator system and a second MVR evaporator system;
the first MVR evaporator system comprises a solvent recovery tower I, a compressor I, a recovery tower I reboiler, a recovery tower I reflux flash tank and a recovery tower I reflux pump;
the second MVR evaporator system comprises a solvent recovery tower II, a compressor II, a reboiler of the recovery tower II, a reflux flash tank of the recovery tower II, a reflux pump of the recovery tower II and a wastewater pump;
and a feeding pump of the recovery tower II is arranged between the output end of the tower kettle of the solvent recovery tower I and the solvent input end of the middle part of the solvent recovery tower II.
Preferably, the compressor I is a low compression ratio compressor, and the compressor II is a high compression ratio compressor.
Preferably, the solvent recovery tower II discharges waste water, and the waste water is conveyed to a sewage treatment section through a waste water pump.
Preferably, the solvent recovery tower I comprises a dilute solvent inlet, the dilute solvent inlet is externally connected with a dilute solvent conveying pipeline, and a primary preheater and a secondary preheater are mounted on the dilute solvent conveying pipeline.
Preferably, the heat source of the primary preheater is the heat of the solvent recovered by the first MVR evaporator system and the second MVR evaporator system; the heat source of the secondary preheater is the heat of the waste water discharged from the tower bottom of the solvent recovery tower II.
A double-tower MVR continuous distillation recovery method is characterized in that a first MVR evaporator system and a second MVR evaporator system in the double-tower MVR continuous distillation recovery system are utilized to sequentially carry out first-stage solvent distillation recovery and second-stage solvent distillation recovery;
the solvent discharged from the tower bottom of the solvent recovery tower I in the first MVR evaporator system is a raw material for the second-stage solvent distillation recovery of the second MVR evaporator system;
and the solvent recovery tower II in the second MVR evaporator system discharges wastewater, and the wastewater is conveyed to a sewage treatment working section through a wastewater pump for subsequent treatment.
Preferably, the first-stage solvent distillation recovery process comprises the following steps: the dilute solvent in the previous working section is conveyed to a solvent recovery tower I through a dilute solvent conveying pipeline; in the conveying process, the dilute solvent enters a solvent recovery tower I after being preheated by a primary preheater and a secondary preheater in sequence;
the dilute solvent descends in the solvent recovery tower I and is heated by steam at the tower bottom, part of the solvent in the dilute solvent becomes steam and ascends, the rest of the solvent is discharged from the tower bottom of the solvent recovery tower I, the solvent is sent to the solvent recovery tower II by a feed pump of the solvent recovery tower II, and finally the wastewater is discharged from the tower bottom of the solvent recovery tower II;
the solvent steam and the tower top reflux liquid are subjected to sufficient heat transfer exchange and mass transfer exchange while ascending in the solvent recovery tower I, are gradually concentrated and then enter a low-compression-ratio compressor, and enter a reboiler of the solvent recovery tower I after being pressurized and heated;
after a reboiler of the recovery tower I heats the solvent steam, the solvent steam enters a tower kettle of the solvent recovery tower I to heat the dilute solvent, and partial solvent steam is condensed to obtain a mixture of solvent condensate and the solvent steam; the mixture of the solvent condensate and the solvent steam enters a reflux flash tank of a recovery tower I, and the solvent condensate and the solvent steam are separated in the reflux flash tank of the recovery tower I;
the solvent steam in the reflux flash tank of the recovery tower I enters a low-compression-ratio compressor again; conveying the solvent condensate in the reflux flash tank of the recovery tower I through a reflux pump of the recovery tower I, taking out part of the solvent condensate as a finished product solvent after the solvent condensate is detected to be qualified, and taking the rest of the solvent condensate as the reflux of the solvent recovery tower I; the liquid level in the reflux flash tank of the recovery tower I is controlled by a regulating valve, and the extraction amount of the finished product solvent is controlled by the temperature in the solvent recovery tower I and the extraction flow in a linkage manner.
Preferably, the second-stage solvent distillation recovery process comprises the following steps: preheating the dilute solvent from the tower kettle of the solvent recovery tower I, then entering the middle part of a solvent recovery tower II, and heating the dilute solvent by tower kettle steam to be solvent steam while descending in the solvent recovery tower II; the solvent steam and the tower top reflux liquid are subjected to sufficient heat transfer exchange and mass transfer exchange while going up in the recovery tower II, are gradually concentrated and then enter a high compression ratio compressor, and enter a reboiler of the solvent recovery tower II after being pressurized and heated;
after the reboiler of the recovery tower II heats the solvent steam, the solvent steam enters the tower kettle of the solvent recovery tower II to heat the dilute solvent, and partial solvent steam is condensed to obtain a mixture of solvent condensate and the solvent steam; the mixture of the solvent condensate and the solvent steam enters a recovery tower II reflux flash tank, and the solvent condensate and the solvent steam are separated in the recovery tower II reflux flash tank;
the solvent steam in the reflux flash tank of the recovery tower II enters the high-compression-ratio compressor again; conveying the solvent condensate of the reflux flash tank of the recovery tower II through a reflux pump of the recovery tower II, taking out the part of the solvent condensate as a finished product solvent after the detection is qualified, and taking the rest of the solvent condensate as the reflux of the solvent recovery tower II; the liquid level of the reflux flash tank of the recovery tower II is controlled by a regulating valve, and the extraction amount of the finished product solvent is controlled by the temperature in the solvent recovery tower II and the extraction flow in a linkage manner; and the tower kettle wastewater of the solvent recovery tower II is conveyed by a wastewater pump, preheated by a secondary preheater and conveyed to a sewage treatment working section.
Preferably, the dilute solvent conveying pipeline is provided with a feed regulating valve, and the flow of the dilute solvent in the dilute solvent conveying pipeline is controlled by the feed regulating valve.
In summary, the invention has the following beneficial technical effects:
(1) The MVR technology is transplanted to the field of solvent distillation, low-grade tower top solvent vapor (low in temperature and low in pressure and cannot be utilized) in the distillation process is compressed by a compressor, the temperature and the pressure of the tower top solvent vapor are increased, and the tower top solvent vapor is used as a heating source of a tower bottom reboiler again, so that the aim of recycling the solvent vapor is fulfilled;
compared with double-effect distillation recovery and triple-effect distillation recovery processes, the distillation process does not need primary steam, solvent steam at the top of a compression tower of a compressor driven by a motor is used as a heat source, and the energy-saving effect is very obvious;
(2) The two compressors are arranged in the double-tower MVR continuous distillation recovery system, and because the tower bottom of the solvent recovery tower I contains a solvent with a certain concentration and the temperature of the tower bottom is lower, the compressor I corresponding to the solvent recovery tower I adopts a smaller compression ratio;
the tower bottom of the solvent recovery tower II is wastewater with higher temperature, a compressor II of the solvent recovery tower II adopts a larger compression ratio, and the single-tower MVR continuous distillation recovery process needs a larger compression ratio due to the fact that the tower bottom is wastewater with higher temperature; therefore, the power consumption in the compression process can be effectively reduced by adopting a double-tower MVR continuous distillation recovery process.
Drawings
FIG. 1 is a schematic diagram of the overall configuration of the two-column MVR continuous distillation recovery system of the present invention.
Detailed Description
The invention is described in further detail below with reference to fig. 1.
Example 1
The invention discloses a double-tower MVR continuous distillation recovery system, which comprises two connected MVR evaporator systems as shown in figure 1, wherein the two MVR evaporator systems are respectively a first MVR evaporator system and a second MVR evaporator system.
As shown in FIG. 1, the first MVR evaporator system comprises a solvent recovery tower I, a compressor I, a reboiler of the recovery tower I, a reflux flash tank of the recovery tower I and a reflux pump of the recovery tower I.
As shown in fig. 1, the second MVR evaporator system comprises a solvent recovery column ii, a compressor ii, a recovery column ii reboiler, a recovery column ii reflux flash tank, a recovery column ii reflux pump, and a waste water pump.
As shown in figure 1, a feed pump of a recovery tower II is arranged between the output end of the tower kettle of the solvent recovery tower I and the solvent input end of the middle part of the solvent recovery tower II.
As shown in fig. 1, the compressor i is a low compression ratio compressor, and the compressor ii is a high compression ratio compressor.
As shown in figure 1, the tower kettle of the solvent recovery tower II discharges waste water, and the waste water is conveyed to a sewage treatment section through a waste water pump.
As shown in figure 1, the solvent recovery tower I comprises a dilute solvent inlet, a dilute solvent conveying pipeline is externally connected with the dilute solvent inlet, and a first-stage preheater and a second-stage preheater are installed on the dilute solvent conveying pipeline.
As shown in fig. 1, the heat source of the primary preheater is the heat of the solvent recovered by the first MVR evaporator system and the second MVR evaporator system. The heat source of the secondary preheater is the heat of the waste water discharged from the tower bottom of the solvent recovery tower II.
A first MVR evaporator system and a second MVR evaporator system in the double-tower MVR continuous distillation recovery system are utilized to sequentially carry out first-stage solvent distillation recovery and second-stage solvent distillation recovery.
The solid line in FIG. 1 represents the flow of the dilute solvent or solvent condensate and the single-dashed line represents the flow of the solvent vapor; the flow of wastewater is indicated by the chain double-dashed line.
The solvent discharged from the first tower kettle of the solvent recovery tower in the first MVR evaporator system is a raw material for the second-stage solvent distillation recovery of the second MVR evaporator system.
And (4) discharging wastewater from a tower kettle of a solvent recovery tower II in the second MVR evaporator system, and conveying the wastewater to a sewage treatment workshop section through a wastewater pump for subsequent treatment.
The first-stage solvent distillation recovery process comprises the following steps: and the dilute solvent in the front working section is conveyed to the solvent recovery tower I through a dilute solvent conveying pipeline. In the conveying process, the dilute solvent enters a solvent recovery tower I after being preheated by a first-stage preheater and a second-stage preheater in sequence.
The dilute solvent descends in the solvent recovery tower I and is heated by the steam in the tower kettle at the same time, part of the solvent in the dilute solvent becomes steam and ascends, the rest of the solvent is discharged from the tower kettle of the solvent recovery tower I, the solvent is sent to the solvent recovery tower II by the feeding pump of the recovery tower II, and finally the wastewater is discharged from the tower kettle of the solvent recovery tower II.
The solvent steam and the tower top reflux liquid are subjected to sufficient heat transfer exchange and mass transfer exchange while ascending in the solvent recovery tower I, are gradually concentrated and then enter a low-compression-ratio compressor, and enter a reboiler of the solvent recovery tower I after being pressurized and heated.
After the reboiler of the recovery tower I heats up the solvent steam, the solvent steam enters the tower kettle of the solvent recovery tower I to heat the dilute solvent, and then partial solvent steam is condensed to obtain a mixture of solvent condensate and the solvent steam. And (3) the mixture of the solvent condensate and the solvent steam enters a reflux flash tank of a recovery tower I, and the solvent condensate and the solvent steam are separated in the reflux flash tank of the recovery tower I.
And the solvent steam in the reflux flash tank of the recovery tower I reenters the low-compression-ratio compressor. And conveying the solvent condensate in the reflux flash tank of the recovery tower I through a reflux pump of the recovery tower I, taking out part of the solvent condensate as a finished solvent after the solvent condensate is qualified through detection, and taking the rest of the solvent condensate as the reflux of the solvent recovery tower I. The liquid level in the reflux flash tank of the recovery tower I is controlled by a regulating valve, and the extraction amount of the finished product solvent is controlled by the temperature in the solvent recovery tower I and the extraction flow in a linkage manner.
The second-stage solvent distillation recovery process comprises the following steps: the dilute solvent from the tower kettle of the solvent recovery tower I enters the middle part of the solvent recovery tower II after being preheated, and the dilute solvent descends in the solvent recovery tower II and is heated by the steam of the tower kettle to be changed into the solvent steam. And the solvent steam and the tower top reflux liquid are subjected to sufficient heat transfer exchange and mass transfer exchange while moving upwards in the recovery tower II, are gradually concentrated and then enter a high-compression-ratio compressor, and enter a reboiler of the solvent recovery tower II after being pressurized and heated.
And after the reboiler of the recovery tower II heats the solvent steam, the solvent steam enters the tower kettle of the solvent recovery tower II to heat the dilute solvent, and then partial solvent steam is condensed to obtain a mixture of the solvent condensate and the solvent steam. And the mixture of the solvent condensate and the solvent steam enters a recovery tower II reflux flash tank, and the solvent condensate and the solvent steam are separated in the recovery tower II reflux flash tank.
And the solvent steam in the reflux flash tank of the recovery tower II enters the high-compression-ratio compressor again. And conveying the solvent condensate of the reflux flash tank of the recovery tower II through a reflux pump of the recovery tower II, taking out the part of the solvent condensate after the detection is qualified as a finished product solvent, and taking the rest of the solvent condensate as the reflux of the solvent recovery tower II. The liquid level of the reflux flash tank of the recovery tower II is controlled by a regulating valve, and the extraction amount of the finished product solvent is controlled by the temperature in the solvent recovery tower II and the extraction flow in a linkage manner. And the tower kettle wastewater of the solvent recovery tower II is conveyed by a wastewater pump, preheated by a secondary preheater and conveyed to a sewage treatment working section.
And a feeding adjusting valve is arranged on the dilute solvent conveying pipeline, and the flow of the dilute solvent in the dilute solvent conveying pipeline is controlled by the feeding adjusting valve.
The above are the preferred embodiments of the present invention, and the protection scope of the present invention is not limited thereby, so: equivalent changes made according to the structure, shape and principle of the invention shall be covered by the protection scope of the invention.
Claims (9)
1. A continuous distillation recovery system of two tower MVR, its characterized in that: the system comprises two connected MVR evaporator systems, wherein the two MVR evaporator systems are a first MVR evaporator system and a second MVR evaporator system respectively;
the first MVR evaporator system comprises a solvent recovery tower I, a compressor I, a recovery tower I reboiler, a recovery tower I reflux flash tank and a recovery tower I reflux pump;
the second MVR evaporator system comprises a solvent recovery tower II, a compressor II, a reboiler of the recovery tower II, a reflux flash tank of the recovery tower II, a reflux pump of the recovery tower II and a wastewater pump;
and a feeding pump of the recovery tower II is arranged between the output end of the tower kettle of the solvent recovery tower I and the solvent input end of the middle part of the solvent recovery tower II.
2. The continuous distillation recovery system of a two-column MVR as claimed in claim 1, wherein: the compressor I is a low-compression-ratio compressor, and the compressor II is a high-compression-ratio compressor.
3. The continuous distillation recovery system of a two-column MVR as claimed in claim 2, wherein: and discharging wastewater from the tower kettle of the solvent recovery tower II, and conveying the wastewater to a sewage treatment working section through a wastewater pump.
4. The continuous distillation recovery system of claim 3, wherein: the solvent recovery tower I comprises a dilute solvent inlet, the dilute solvent inlet is externally connected with a dilute solvent conveying pipeline, and a primary preheater and a secondary preheater are installed on the dilute solvent conveying pipeline.
5. The continuous distillation recovery system of claim 4, wherein: the heat source of the primary preheater is the heat of the solvent recovered by the first MVR evaporator system and the second MVR evaporator system; the heat source of the secondary preheater is the heat of the waste water discharged from the tower bottom of the solvent recovery tower II.
6. A continuous distillation recovery method of double-tower MVR is characterized in that: sequentially performing a first stage solvent distillation recovery and a second stage solvent distillation recovery using the first MVR evaporator system and the second MVR evaporator system of the two-tower MVR continuous distillation recovery system of claim 5;
the solvent discharged from the tower kettle I of the solvent recovery tower in the first MVR evaporator system is a raw material for the second-stage solvent distillation recovery of the second MVR evaporator system;
and the solvent recovery tower II in the second MVR evaporator system discharges wastewater, and the wastewater is conveyed to a sewage treatment working section through a wastewater pump for subsequent treatment.
7. The continuous distillation recovery process of claim 6, wherein: the first-stage solvent distillation recovery process comprises the following steps: the dilute solvent in the front working section is conveyed to a solvent recovery tower I through a dilute solvent conveying pipeline; in the conveying process, the dilute solvent enters a solvent recovery tower I after being preheated by a primary preheater and a secondary preheater in sequence;
the dilute solvent descends in the solvent recovery tower I and is heated by the steam at the tower bottom, part of the solvent in the dilute solvent turns into steam and ascends, the rest of the solvent is discharged from the tower bottom of the solvent recovery tower I, the solvent is conveyed to the solvent recovery tower II by a feed pump of the recovery tower II, and finally the wastewater is discharged from the tower bottom of the solvent recovery tower II;
the solvent steam and the tower top reflux liquid are subjected to sufficient heat transfer exchange and mass transfer exchange while ascending in the solvent recovery tower I, are gradually concentrated and then enter a low-compression-ratio compressor, and enter a reboiler of the solvent recovery tower I after being pressurized and heated;
after a reboiler of the recovery tower I heats the solvent steam, the solvent steam enters a tower kettle of the solvent recovery tower I to heat the dilute solvent, and partial solvent steam is condensed to obtain a mixture of solvent condensate and the solvent steam; the mixture of the solvent condensate and the solvent steam enters a reflux flash tank of a recovery tower I, and the solvent condensate and the solvent steam are separated in the reflux flash tank of the recovery tower I;
the solvent steam in the reflux flash tank of the recovery tower I enters a low-compression-ratio compressor again; conveying the solvent condensate in the reflux flash tank of the recovery tower I through a reflux pump of the recovery tower I, taking out part of the solvent condensate as a finished product solvent after the solvent condensate is detected to be qualified, and taking the rest of the solvent condensate as the reflux of the solvent recovery tower I; the liquid level in the reflux flash tank of the recovery tower I is controlled by a regulating valve, and the extraction amount of the finished product solvent is controlled by the temperature in the solvent recovery tower I and the extraction flow in a linkage manner.
8. The continuous distillation recovery process of claim 6, wherein: the second-stage solvent distillation recovery process comprises the following steps: preheating the dilute solvent from the tower kettle of the solvent recovery tower I, then feeding the preheated dilute solvent into the middle part of a solvent recovery tower II, and heating the dilute solvent by tower kettle steam to form solvent steam while descending in the solvent recovery tower II; the solvent steam and the tower top reflux liquid are subjected to sufficient heat transfer exchange and mass transfer exchange while moving upwards in the recovery tower II, are gradually concentrated and then enter a high compression ratio compressor, and enter a reboiler of the solvent recovery tower II after being pressurized and heated;
after the reboiler of the recovery tower II heats the solvent steam, the solvent steam enters the tower kettle of the solvent recovery tower II to heat the dilute solvent, and partial solvent steam is condensed to obtain a mixture of solvent condensate and the solvent steam; the mixture of the solvent condensate and the solvent steam enters a recovery tower II reflux flash tank, and the solvent condensate and the solvent steam are separated in the recovery tower II reflux flash tank;
the solvent steam in the reflux flash tank of the recovery tower II enters a high-compression-ratio compressor again; conveying the solvent condensate of the reflux flash tank of the recovery tower II through a reflux pump of the recovery tower II, taking out the part of the solvent condensate as a finished product solvent after the detection is qualified, and taking the rest of the solvent condensate as the reflux of the solvent recovery tower II; the liquid level of the reflux flash tank of the recovery tower II is controlled by a regulating valve, and the extraction amount of the finished product solvent is controlled by the temperature in the solvent recovery tower II and the extraction flow in a linkage manner; and the tower kettle wastewater of the solvent recovery tower II is conveyed by a wastewater pump, preheated by a secondary preheater to dilute solvent raw material and then conveyed to a sewage treatment section.
9. The continuous distillation recovery process of double column MVR according to claim 7, characterized in that: and the dilute solvent conveying pipeline is provided with a feeding adjusting valve, and the flow of the dilute solvent in the dilute solvent conveying pipeline is controlled by the feeding adjusting valve.
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Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN201762130U (en) * | 2010-08-25 | 2011-03-16 | 任松保 | Dual-effect steam recompression thermal mass recovery system |
| CN103408086A (en) * | 2013-08-02 | 2013-11-27 | 天华化工机械及自动化研究设计院有限公司 | MVR (Mechanical Vapor Recompression) vapor-stripping deamination system and application method thereof |
| JP2016145161A (en) * | 2015-02-06 | 2016-08-12 | 国立大学法人名古屋大学 | Distillation apparatus of hydrous ethanol, and manufacturing method of absolute ethanol |
| CN105964005A (en) * | 2016-04-22 | 2016-09-28 | 常州博睿杰能环境技术有限公司 | Split type MVR heat pump rectification heat integration system |
| CN106748864A (en) * | 2016-12-27 | 2017-05-31 | 广东创源节能环保有限公司 | The technique that a kind of double heat pump distillation methods of low pressure economic benefits and social benefits process DMF waste water |
| CN110975315A (en) * | 2019-12-09 | 2020-04-10 | 天津科技大学 | Energy-saving rectification purification system for high-purity propylene oxide |
| CN113813625A (en) * | 2021-08-09 | 2021-12-21 | 肥城金塔机械科技有限公司 | Device and method for recovering light alcohol by combining MVR with recovery tower |
-
2022
- 2022-08-05 CN CN202210939578.8A patent/CN115253350A/en active Pending
Patent Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN201762130U (en) * | 2010-08-25 | 2011-03-16 | 任松保 | Dual-effect steam recompression thermal mass recovery system |
| CN103408086A (en) * | 2013-08-02 | 2013-11-27 | 天华化工机械及自动化研究设计院有限公司 | MVR (Mechanical Vapor Recompression) vapor-stripping deamination system and application method thereof |
| JP2016145161A (en) * | 2015-02-06 | 2016-08-12 | 国立大学法人名古屋大学 | Distillation apparatus of hydrous ethanol, and manufacturing method of absolute ethanol |
| CN105964005A (en) * | 2016-04-22 | 2016-09-28 | 常州博睿杰能环境技术有限公司 | Split type MVR heat pump rectification heat integration system |
| CN106748864A (en) * | 2016-12-27 | 2017-05-31 | 广东创源节能环保有限公司 | The technique that a kind of double heat pump distillation methods of low pressure economic benefits and social benefits process DMF waste water |
| CN110975315A (en) * | 2019-12-09 | 2020-04-10 | 天津科技大学 | Energy-saving rectification purification system for high-purity propylene oxide |
| CN113813625A (en) * | 2021-08-09 | 2021-12-21 | 肥城金塔机械科技有限公司 | Device and method for recovering light alcohol by combining MVR with recovery tower |
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