CN205730432U - A kind of mechanical steam recompression Distallation systm - Google Patents
A kind of mechanical steam recompression Distallation systm Download PDFInfo
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- CN205730432U CN205730432U CN201521123009.8U CN201521123009U CN205730432U CN 205730432 U CN205730432 U CN 205730432U CN 201521123009 U CN201521123009 U CN 201521123009U CN 205730432 U CN205730432 U CN 205730432U
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Abstract
The utility model discloses a kind of mechanical steam recompression Distallation systm, including distillation unit, vapour compression machine, indirect steam condensation and vacuum pump set, raw material preheating unit and water vapour drainer；Distillation unit includes distillating still and the distillation column being positioned above；Vapour compression machine import is connected with distillation tower top, and vapour compression machine outlet is connected with indirect steam condensation and vacuum pump set；Indirect steam condensation and vacuum pump set include interconnective indirect steam first-stage condenser, indirect steam secondary condenser, B-grade condensation gas-liquid separator, three grades of condensers of indirect steam, three grades of condensing gas liquid/gas separators and vacuum pump；Raw material preheating unit includes one-level preheater, two grades of preheaters, three grades of preheaters, level Four preheater and Pyatyi preheater, one-level preheater and two grades of preheaters are connected with water vapor condensate tank by feed pump, and Pyatyi preheater is by feed pump and water vapor condensate tank.This utility model simple in construction, energy consumption is low, reduces material unaccounted-for (MUF).
Description
Technical field
This utility model relates to steam distillation technology, particularly relates to a kind of mechanical steam recompression Distallation systm.
Background technology
Traditional distillation equipment many employings single distillation column, invests low but automaticity is low, production efficiency is low, steam consumption is high, in terms of distilled spirit, about needs steam 1t/t finished product ethanol.Existing continuous multitower pressure reduction Distallation systm or evaporation with distillation association system, energy consumption reduces to the half of single distillation column, but cost of investment is significantly increased.
CN 203677978U discloses a kind of steam compression type alcohol distillation column, distillation column top is connected with vapour compression machine import, vapour compression machine outlet is connected with vaporizer thermal medium inlet in distillating still, and vaporizer thermal medium outlet is connected with condensate drum, and condensate drum is connected with vacuum mechanism.This system make use of the latent heat of compression indirect steam, relatively single effect evaporation energy consumption is lower, but have a disadvantage in that (1) distillation tower top i.e. alcohol steam is about 78 DEG C, and distill temperature in the kettle higher than 100 DEG C, in view of the heat transfer temperature difference of vaporizer, after indirect steam compression, temperature should be more than 108 DEG C, and both vapor compression is bigger, power consumption of compressor is higher, becomes apparent from especially for the lower methanol of boiling point, acetone, oxolane etc.；(2) basic and organic solvent the latent heat of the sensible heat of residual liquid is suitable, and residual liquid directly discharges and causes serious heat loss；(3) distillation drainer is directly connected with vacuum pump, causes the ethanol of volatilization in the indirect steam having not enough time to heat exchange and condensate drum to be directly entered vacuum pump, causes the loss of ethanol.
Utility model content
The purpose of this utility model is to overcome the deficiencies in the prior art, it is provided that a kind of mechanical steam recompression Distallation systm, simple in construction, and energy consumption is low, reduces material unaccounted-for (MUF).
In order to achieve the above object, the technical solution adopted in the utility model is:
A kind of mechanical steam recompression Distallation systm, including distillation unit, vapour compression machine, indirect steam condensation and vacuum pump set, raw material preheating unit and water vapour drainer；Distillation unit includes distillating still and the distillation column being positioned above；
Vapour compression machine import is connected with distillation column, and vapour compression machine outlet is connected with indirect steam condensation and vacuum pump set；
Indirect steam condensation and vacuum pump set include interconnective indirect steam first-stage condenser, indirect steam secondary condenser, B-grade condensation gas-liquid separator, three grades of condensers of indirect steam, three grades of condensing gas liquid/gas separators and vacuum pump；
Raw material preheating unit includes one-level preheater, two grades of preheaters, three grades of preheaters, level Four preheater and Pyatyi preheater, three grades of preheaters share with indirect steam secondary condenser shared composition indirect steam secondary condenser and three grades of preheaters of raw material, level Four preheater and indirect steam first-stage condenser and constitute indirect steam first-stage condenser and raw material level Four preheater, one-level preheater and two grades of preheaters are connected with water vapor condensate tank by feed pump, and Pyatyi preheater is by condensate pump and water vapour drainer.
As this utility model preferred embodiment, being provided with steam heating component inside distillation column described in the utility model, distillation column outlet is connected with water vapour drainer, and water vapour drainer is connected with Pyatyi preheater and two grades of preheaters successively by condensate pump.
As this utility model preferred embodiment, vapour compression machine import described in the utility model is connected with distillation tower top, and vapour compression machine outlet is connected with indirect steam first-stage condenser and raw material level Four preheater.
As this utility model preferred embodiment, Distallation systm described in the utility model includes at least six heat exchanger, wherein indirect steam first-stage condenser and raw material level Four preheater are tube side formula heat exchanger, and one-level preheater, two grades of preheaters, indirect steam secondary condenser and three grades of preheaters of raw material, Pyatyi preheater and three grades of condensers of indirect steam are plate type heat exchanger.
As this utility model preferred embodiment, the thermal source of one-level preheater described in the utility model, two grades of preheaters, three grades of preheaters, level Four preheater and Pyatyi preheater is water vapor condensate/residual liquid, incoagulable gas, compression indirect steam, water vapor condensate after indirect steam condensed fluid, heat exchange successively.
As this utility model preferred embodiment, the thermal source of indirect steam first-stage condenser described in the utility model, indirect steam secondary condenser and three grades of condensers of indirect steam be successively three grades preheating after feed liquid, two grades preheating after feed liquid, industrial cooling water.
As this utility model preferred embodiment, the outlet at bottom of B-grade condensation gas-liquid separator described in the utility model and three grades of condensing gas liquid/gas separators is connected with water vapor condensate tank.
As this utility model preferred embodiment, water vapour drainer described in the utility model is connected with distillation column top by condensate pump, forms the partial reflux loop of condensed fluid.
As this utility model preferred embodiment, water vapour drainer described in the utility model is connected with the thermal medium inlet of one-level preheater by condensate pump.
As this utility model preferred embodiment, water vapour drainer described in the utility model is that water vapor condensate tank shares with residual liquid tank, and described condensate pump is that water vapor condensation liquid pump shares with tail pump.
Operation principle of the present utility model is: during use, and material liquid passes sequentially through preheater at different levels and enters distillating still, and the liquid level in still to be distilled reaches to set after requiring, is then turned on steam heating；Observing working condition, feed liquid explosive evaporation to distillating still, the indirect steam being evaporated is again through distillation column vapor-liquid separation, and the indirect steam separated is delivered to the heating chamber of level Four preheater after compressor supercharging heats up and used as adding vapours；Solid-liquid separation is carried out in condensed fluid after heat exchange and indirect steam more than needed (containing incoagulable gas) drainer again, indirect steam more than needed reclaims heat and condensed fluid again after B-grade condensation and three grades of condensations, and condensed fluid finally also self is lowered the temperature as finished product through raw material one-level preheater preheating material；Entering water vapor condensate tank after the condensed water condensation of heater in evaporating kettle, residual liquid enters water vapour drainer simultaneously, and the two finally pumps into secondary raw materials preheater and reclaims sensible heat.
Compared with prior art, the beneficial effects of the utility model are:
Compared with single column or multi-tower distillation, there is the advantage that energy consumption is low；
Compared with existing machinery formula vapor recompression Distallation systm, compression indirect steam and feed liquid are carried out heat exchange at tube side formula heat exchanger, compression indirect steam temperature is higher or lower than azeotropic point, when leaving steam heating component in distillating still for compressing vapor (steam) temperature less than azeotropic point, therefore, compressor power consumption acting and water vapour consumption can adjust, and also it is ensured that compressor electricity consumption and initial steam total energy consumption are minimum, are particularly well-suited to the feed liquid distillation that azeotropic point differs bigger with residual liquid boiling point；
Compared with existing machinery formula vapor recompression Distallation systm, the outlet of distillating still residual liquid is connected with raw material level Four preheater, two grades of preheaters of raw material successively, takes full advantage of the sensible heat of residual liquid；
Compared with existing machinery formula vapor recompression Distallation systm, water vapor condensate tank is connected with vacuum pump by after two-stage heat exchange again, have collected the indirect steam condensed fluid of vacuum, decreases the loss of distillate, take full advantage of the latent heat of indirect steam simultaneously.
Accompanying drawing explanation
Fig. 1 is unit construction system schematic diagram of the present utility model.
Detailed description of the invention
Purport of the present utility model is to overcome the deficiencies in the prior art, it is provided that a kind of mechanical steam recompression Distallation systm, compared with single column or multi-tower distillation, has the advantage that energy consumption is low, efficiency is high.It is described in detail referring to the drawings below in conjunction with embodiment, in order to technical characteristic of the present utility model and advantage are interpretated more in-depth.
Embodiment 1
Overall structure schematic diagram of the present utility model, as it is shown in figure 1, a kind of mechanical steam recompression Distallation systm, condenses and vacuum pump set, raw material preheating unit and water vapour drainer 3 including distillation unit, vapour compression machine 5, indirect steam；Distillation unit includes distillating still 1 and the distillation column 2 being positioned above；Vapour compression machine 5 import is connected with distillation column 2, and vapour compression machine 5 outlet is connected with indirect steam condensation and vacuum pump set.
Preferably, indirect steam condensation and vacuum pump set include three condensers of indirect steam, two gas-liquid separators and a vacuum pump.As it is shown in figure 1, indirect steam condensation and vacuum pump set include interconnective indirect steam first-stage condenser, indirect steam secondary condenser, B-grade condensation gas-liquid separator 6,16, three grades of condensing gas liquid/gas separators 7 of three grades of condensers of indirect steam and vacuum pump 8.
This utility model raw material preheating unit includes five preheaters.As shown in Figure 1, raw material preheating unit includes one-level preheater 12, three grades of preheaters of 11, two grades of preheaters, level Four preheater and Pyatyi preheater 15, three grades of preheaters share with indirect steam secondary condenser shared composition indirect steam secondary condenser and three grades of preheaters 13 of raw material, level Four preheater and indirect steam first-stage condenser and constitute indirect steam first-stage condenser and raw material level Four preheater 14, one-level preheater 11 and two grades of preheaters 12 are connected with water vapor condensate tank 9 by feed pump 10, and Pyatyi preheater 15 is by condensate pump 4 and water vapour drainer 3.
Distillation column 2 described in the utility model is internal is provided with steam heating component, and distillation column 2 exports and is connected with water vapour drainer 3, and water vapour drainer 3 is connected with Pyatyi preheater 15 and two grades of preheaters 12 successively by condensate pump 4.Vapour compression machine 5 described in the utility model import is connected with distillation column 2 top, and vapour compression machine 5 outlet is connected with indirect steam first-stage condenser and raw material level Four preheater 14.
Preferably, Distallation systm described in the utility model includes at least six heat exchanger, wherein indirect steam first-stage condenser and raw material level Four preheater 14 are preferably tube side formula heat exchanger, and 11, two grades of preheaters 12 of one-level preheater, indirect steam secondary condenser and three grades of preheaters 13 of raw material, Pyatyi preheater 15 and three grades of condensers of indirect steam 16 are preferably plate type heat exchanger.But being not limited to both heat exchangers in this utility model, other can realize the heat exchanger of said function all in this utility model protection domain.The thermal source of indirect steam first-stage condenser described in the utility model, indirect steam secondary condenser and three grades of condensers 16 of indirect steam be successively three grades preheating after feed liquid, two grades preheating after feed liquid, industrial cooling water.The outlet at bottom of described B-grade condensation gas-liquid separator 6 and three grades of condensing gas liquid/gas separators 7 is connected with water vapor condensate tank 9, is finished product after lowering the temperature with raw material heat exchange.
As it is shown in figure 1, the thermal source of one-level preheater described in the utility model 12, three grades of preheaters of 11, two grades of preheaters, level Four preheater and Pyatyi preheater 15 is water vapor condensate/residual liquid, incoagulable gas, compression indirect steam, water vapor condensate after indirect steam condensed fluid, heat exchange successively.
Water vapour drainer 3 described in the utility model is connected with distillation column 2 top by condensate pump 4, forms the partial reflux loop of condensed fluid.Described water vapour drainer 3 is connected with the thermal medium inlet of one-level preheater 11 by condensate pump 4.Preferably, described water vapour drainer 3 is that water vapor condensate tank shares with residual liquid tank, and described condensate pump 4 is that water vapor condensation liquid pump shares with tail pump.
The raw material of the present embodiment is faints waste liquid, and still-process is: faints waste liquid passes sequentially through preheater at different levels and enters distillating still, and the liquid level in still to be distilled reaches to set after requiring, is then turned on steam heating；Observing working condition, feed liquid explosive evaporation to distillating still, gas phase separates with backflow further through distillation column again, and the alcohol steam separated is delivered to the heating chamber of level Four preheater after compressor supercharging heats up and used as adding vapours；Solid-liquid separation is carried out in condensed fluid after heat exchange and indirect steam more than needed (containing incoagulable gas) drainer again, indirect steam more than needed reclaims heat and condensed fluid again after B-grade condensation and three grades of condensations, and condensed fluid finally also self is lowered the temperature as industrial alcohol through raw material one-level preheater preheating material；Entering water vapor condensate tank after the condensed water condensation of heater in evaporating kettle, residual liquid enters water vapour drainer simultaneously, and the two finally pumps into secondary raw materials preheater and reclaims sensible heat.
Embodiment 2
Embodiment 2 is substantially the same manner as Example 1, difference is in distillating still that the outlet of heater is connected with water vapor condensate tank, this system can be used for the dehydration distillation of the organic solvent (such as dioxanes, pyridine, glycol monomethyl ether, morpholine, ethylene glycol monoethyl ether, 1,2-PD, dimethyl sulfoxide, ethylene glycol, diethylene glycol, glycerol, ionic liquid etc.) higher than water boiling point.
The explanation of value, experiments verify that, the sulfate of Ni, Cu, Zn, Mn, Fe, Mg etc., phosphate etc. all can use solventing-out process to prepare, and also belong to protection scope of the present invention.
By the technical scheme in above example, this utility model is carried out clear, complete description, it is clear that described embodiment is the embodiment of this utility model part rather than whole embodiments.Based on the embodiment in this utility model, the every other embodiment that those of ordinary skill in the art are obtained under not making creative work premise, broadly fall into the scope of this utility model protection.
Claims (10)
1. a mechanical steam recompression Distallation systm, it is characterised in that: include distilling unit, vapour compression machine (5), indirect steam condensation and vacuum pump set, raw material preheating unit and water vapour drainer (3)；Distillation unit includes distillating still (1) and the distillation column (2) being positioned above；
Vapour compression machine (5) import is connected with distillation column (2), and vapour compression machine (5) outlet is connected with indirect steam condensation and vacuum pump set；
Indirect steam condensation and vacuum pump set include interconnective indirect steam first-stage condenser, indirect steam secondary condenser, B-grade condensation gas-liquid separator (6), three grades of condensers (16) of indirect steam, three grades of condensing gas liquid/gas separators (7) and vacuum pump (8)；
Raw material preheating unit includes one-level preheater (11), two grades of preheaters (12), three grades of preheaters, level Four preheater and Pyatyi preheater (15), three grades of preheaters share with indirect steam secondary condenser and constitute indirect steam secondary condenser and three grades of preheaters (13) of raw material, level Four preheater shares with indirect steam first-stage condenser and constitutes indirect steam first-stage condenser and raw material level Four preheater (14), one-level preheater (11) and two grades of preheaters (12) are connected with water vapor condensate tank (9) by feed pump (10), Pyatyi preheater (15) is by condensate pump (4) and water vapour drainer (3).
Mechanical steam recompression Distallation systm the most according to claim 1, it is characterized in that: described distillation column (2) is internal is provided with steam heating component, distillation column (2) outlet is connected with water vapour drainer (3), and water vapour drainer (3) is connected with Pyatyi preheater (15) and two grades of preheaters (12) successively by condensate pump (4).
Mechanical steam recompression Distallation systm the most according to claim 2, it is characterized in that: described vapour compression machine (5) import is connected with distillation column (2) top, vapour compression machine (5) outlet is connected with indirect steam first-stage condenser and raw material level Four preheater (14).
Mechanical steam recompression Distallation systm the most according to claim 1, it is characterized in that: described Distallation systm includes at least 6 heat exchangers, wherein indirect steam first-stage condenser and raw material level Four preheater (14) are tube side formula heat exchanger, and one-level preheater (11), two grades of preheaters (12), indirect steam secondary condenser and three grades of preheaters (13) of raw material, Pyatyi preheater (15) and three grades of condensers (16) of indirect steam are plate type heat exchanger.
Mechanical steam recompression Distallation systm the most according to claim 4, it is characterised in that: the thermal source of described one-level preheater (11), two grades of preheaters (12), three grades of preheaters, level Four preheater and Pyatyi preheater (15) is water vapor condensate/residual liquid, incoagulable gas, compression indirect steam, water vapor condensate after indirect steam condensed fluid, heat exchange successively.
Mechanical steam recompression Distallation systm the most according to claim 4, it is characterised in that: the thermal source of described indirect steam first-stage condenser, indirect steam secondary condenser and three grades of condensers (16) of indirect steam be successively three grades preheating after feed liquid, two grades preheating after feed liquid, industrial cooling water.
Mechanical steam recompression Distallation systm the most according to claim 6, it is characterised in that: the outlet at bottom of described B-grade condensation gas-liquid separator (6) and three grades of condensing gas liquid/gas separators (7) is connected with water vapor condensate tank (9).
Mechanical steam recompression Distallation systm the most according to claim 1, it is characterized in that: described water vapour drainer (3) is connected with distillation column (2) top by condensate pump (4), form the partial reflux loop of condensed fluid.
Mechanical steam recompression Distallation systm the most according to claim 8, it is characterised in that: described water vapour drainer (3) is connected with the thermal medium inlet of one-level preheater (11) by condensate pump (4).
Mechanical steam recompression Distallation systm the most according to claim 8 or claim 9, it is characterized in that: described water vapour drainer (3) is that water vapor condensate tank shares with residual liquid tank, described condensate pump (4) is that water vapor condensation liquid pump shares with tail pump.
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN107619078A (en) * | 2017-10-31 | 2018-01-23 | 云南省环境科学研究院(中国昆明高原湖泊国际研究中心) | A kind of device of method treatment of acidic wastewater using concentration stripping |
| CN107982943A (en) * | 2017-12-14 | 2018-05-04 | 清远佳致新材料研究院有限公司 | A kind of cobalt sulfate solution vapo(u)rization system and its technique |
| CN110452125A (en) * | 2019-09-03 | 2019-11-15 | 天津科技大学 | A kind of toluenediamine dewatering and device based on mechanical steam recompression MVR |
| CN112870746A (en) * | 2019-11-29 | 2021-06-01 | 中国科学院理化技术研究所 | MVR heat pump system for realizing integration of concentration, steam stripping and rectification |
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2015
- 2015-12-31 CN CN201521123009.8U patent/CN205730432U/en active Active
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107619078A (en) * | 2017-10-31 | 2018-01-23 | 云南省环境科学研究院(中国昆明高原湖泊国际研究中心) | A kind of device of method treatment of acidic wastewater using concentration stripping |
| CN107619078B (en) * | 2017-10-31 | 2024-01-05 | 云南省生态环境科学研究院 | Device for treating acidic wastewater by adopting concentration stripping method |
| CN107982943A (en) * | 2017-12-14 | 2018-05-04 | 清远佳致新材料研究院有限公司 | A kind of cobalt sulfate solution vapo(u)rization system and its technique |
| CN110452125A (en) * | 2019-09-03 | 2019-11-15 | 天津科技大学 | A kind of toluenediamine dewatering and device based on mechanical steam recompression MVR |
| CN112870746A (en) * | 2019-11-29 | 2021-06-01 | 中国科学院理化技术研究所 | MVR heat pump system for realizing integration of concentration, steam stripping and rectification |
| CN112870746B (en) * | 2019-11-29 | 2022-07-22 | 中国科学院理化技术研究所 | MVR heat pump system for realizing integration of concentration, steam stripping and rectification |
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