CN106083526A - Ethanol reclaims the system and method for Automated condtrol - Google Patents
Ethanol reclaims the system and method for Automated condtrol Download PDFInfo
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- CN106083526A CN106083526A CN201610387066.XA CN201610387066A CN106083526A CN 106083526 A CN106083526 A CN 106083526A CN 201610387066 A CN201610387066 A CN 201610387066A CN 106083526 A CN106083526 A CN 106083526A
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
- C07C29/74—Separation; Purification; Use of additives, e.g. for stabilisation
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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
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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
- B01D3/42—Regulation; Control
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
- C07C29/74—Separation; Purification; Use of additives, e.g. for stabilisation
- C07C29/76—Separation; Purification; Use of additives, e.g. for stabilisation by physical treatment
- C07C29/80—Separation; Purification; Use of additives, e.g. for stabilisation by physical treatment by distillation
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- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
Abstract
The invention discloses ethanol and reclaim the system and method for Automated condtrol, the outlet of ethanol waste liquid pretreatment system is connected with the entrance of ethanol recovery system, connect and on pipeline, effusion meter is set, preheater arranges pneumatic control valve on the connection pipeline of ethanol distillation tower, ethanol distillation tower bottom arranges ethanol outlet, a part of ethanol enters reboiler and returns ethanol distillation tower, a part enters vapour liquid separator by blowdown pneumatic operated valve, after entering vapor-liquid separation, gas returns to ethanol distillation tower, liquid is discharged, ethanol distillation tower steam out enters back into condenser system after entering preheater hot exchange and condenses, the qualified alcohol liquid discharged is collected after finished product cooler.The ethanol of the present invention reclaim the method for Automated condtrol for by waste ethanol coarse-grain mother solution and after after screen plate frame filter out sediment, enter recovery system again carry out Distillation recovery.Present invention optimizes the apparatus and method of alcohol recycle Automated condtrol, energy-saving and cost-reducing, reduce sewage discharge, improve distillation yield.
Description
Technical field
The invention belongs to ethanol and reclaim field, relate to ethanol and reclaim the system and method for Automated condtrol.
Background technology
Ethanol recovery tower operation principle: utilize ethyl alcohol boiling point to be less than the principle of other solution boiling point, boils with a little higher than ethanol
The temperature of point, carries out heating volatilization by the Diluted Alcohol solution that need to reclaim, and after tower body rectification, separates out straight alcohol gas, improves second
The concentration of alcoholic solution, reaches to reclaim the purpose of ethanol.
Along with energy cost, the lifting of cost of labor, the increase of environmental protection pressure, save energy and reduce the cost, cut payroll to improve efficiency, improve product
Yield, reduction production cost are the themes of each interprise's intensive management.It is the production that energy resource consumption is big, blowdown flow rate is many that ethanol reclaims
Unit, it is therefore necessary to do technological innovation and process optimization in terms of ethanol recovery.
CN201310265012.2 " a kind of alcohol steam recovery device " discloses a kind of alcohol recovering device, including reclaiming
Unit.Described recovery unit includes a recovery tower being provided with charging aperture, waste liquid outlet and steam (vapor) outlet and is provided with discharging opening
Condenser, the steam (vapor) outlet of described recovery tower is connected with condenser, including at least 2 grades of recovery units, Qi Zhongshang by recovery tube
The waste liquid outlet of level recovery tower is connected with the charging aperture of subordinate's recovery tower；It is equipped with ethanol on the waste liquid outlet of each recovery tower to pass
Sensor；The input of ethanol sensor and a controller connects, the waste liquid outlet of each recovery tower is also equipped with electromagnetic valve,
Electromagnetic valve is connected with the outfan of described controller, and alcohol vapour condensed water, through the heating of at least 2 grades of recovery towers, makes in waste liquid
Ethanol content is less than 2%, decreases the waste of ethanol.The shortcoming of this invention is at least 2 grades of recovery tower heating, and the equipment of input becomes
This height, energy-output ratio is big, has the ethanol of 2% simultaneously, do not accomplish zero-emission in waste liquid, and ethanol recovery is low.
CN201110379162.7 " automatic alcohol recycling system " discloses as solving what existing ethanol recovery system existed
The manually manual operation of whole process, labor intensity is high, workload is big, and a kind of ethanol of the problems such as working cycle length reclaims automatically
System, is set up in parallel by multiple waste ethanol storage tanks, and the outlet of each waste ethanol storage tank is connected with preheater, connects and arranges on pipeline
First feed pump and charging regulation valve, the outlet of preheater is connected with the waste ethanol entrance of ethanol recovery tower；At the bottom of ethanol recovery tower
Portion is provided with between Diluted Alcohol outlet, and Diluted Alcohol outlet and entrance series connection reboiler, and preheater is provided with waste water and discharges
Mouthful；The tower top of ethanol recovery tower is provided with alcohol vapour outlet, the first overhead condenser of connecting in chilled(cooling) water return (CWR), and condenser is arranged
The ethanol part gone out refluxes blowback ethanol recovery tower through return tank first, and another part is through going cost ethanol regulation valve finished product cold
Condenser enters finished product ethanol storage tank.The advantage of this invention is the reduction of manual operation, and shortcoming is not solve energy resource consumption greatly, steams
Evaporate the problem that yield is low.
Summary of the invention
In view of this, it is an object of the invention to provide a kind of ethanol and reclaim the system and method for Automated condtrol, optimize
Ethanol reclaims Automated condtrol technique, energy-saving and cost-reducing, reduces sewage discharge, improves distillation yield.In order to realize foregoing invention mesh
, the present invention by the following technical solutions:
Ethanol reclaims the system of Automated condtrol, including ethanol waste liquid pretreatment system and ethanol recovery system, described second
The outlet of alcohol waste liquid pretreatment system is connected with the entrance of ethanol recovery system.
Further, described ethanol recovery system includes reboiler, ethanol distillation tower, preheater, vapour liquid separator, condensed system
System, finished product cooler；The liquid outlet of described preheater is connected with the liquid inlet of ethanol distillation tower by pipeline, described ethanol
The steam (vapor) outlet of distillation column is connected with the steam inlet of preheater, the steam inlet phase of the steam (vapor) outlet of preheater and condenser system
Even, described preheater is connected with the entrance of finished product cooler with the condensate outlet of condenser system；Described ethanol distillation tower bottom
Arranging ethanol outlet A and outlet B, described outlet A is connected with the liquid inlet of reboiler, the outlet of reboiler and ethanol
The boiling ethanol entrance port of distillation column is connected, and described outlet B is connected with the liquid inlet of vapour liquid separator, described vapour liquid separator
Gas outlet be connected with the gas entrance of ethanol distillation tower.
Further, described condenser system includes the first condenser, the second condenser, the 3rd condenser, described first condensation
The steam (vapor) outlet of device and the steam inlet of the second condenser are connected, the steam (vapor) outlet of the second condenser and the steam of the 3rd condenser
Entrance is connected.
Further, the ethanol liquid conveyance conduit being connected with preheater is provided with effusion meter, connects preheater and ethanol steams
The liquid conducting pipes evaporating tower is provided with charging pneumatic operated valve, and the jet chimney that enters of reboiler is provided with steam and enters vapour pneumatic operated valve, row
Outlet B is provided with blowdown pneumatic operated valve with the connection pipeline of vapour liquid separator.
Further, described ethanol waste liquid pretreatment system includes neutralizing tank, liquid caustic soda measuring tank, filters sheet frame, waste ethanol storage
Tank, the described discharging opening of liquid caustic soda measuring tank is connected with the feeding mouth of neutralizing tank, the discharging opening of described neutralizing tank and filtration sheet frame
Feeding mouth is connected, and the discharging opening of described filtration sheet frame is connected with the feed liquid refluxing opening of neutralizing tank, connects and arranges reflux inlet on pipeline,
Described screen plate frame discharging opening is also connected with waste ethanol reservoir inlet.
Further, described ethanol recovery system also includes return tank, described preheater and the liquid outlet of the first condenser
Being connected with the entrance of return tank, the outlet of return tank is connected with the alcohol reflux mouth of ethanol distillation tower by pipeline.
Ethanol reclaims the method for Automated condtrol: enter back into second after first waste ethanol being carried out pretreatment in pretreatment system
Alcohol recovery system carries out Distillation recovery.
Further, after described pretreatment is for being neutralized waste ethanol coarse-grain mother solution, then sediment is filtered out through screen plate frame；
In described N-process, waste liquid temperature controls at 40～50 DEG C, and wine degree controls 0%～50%vol, and the waste liquor PH after neutralization is
6.7～7.2.
Further, described Distillation recovery process is: steam enters ethanol distillation tower by reboiler and carries out tower body preheating, with
Time control steam pressure, treat tower body preheating after, open condenser system, waste ethanol liquid after pretreatment passes through preheater
Enter ethanol distillation tower after preheating to distill, control fluid flow simultaneously, and regulate temperature and the ethanol controlling condenser system
Each section of temperature of distillation column, the preheated device of gas distilled out from ethanol distillation tower carries out heat exchange, colder by condenser system
Solidifying, finally carry out finished product cooling and recovery, an ethanol liquid part for ethanol distillation tower bottom returns to ethanol by after reboiler
Distillation column, a part is by returning to ethanol distillation tower with gas form after vapour liquid separator.
Further, in described still-process, Steam pressure control is 0.04～0.05Mpa, and the voltage-controlled system of distillation column is 0.02
～0.05MPa, waste ethanol flow-control is 3.5～5.0m3/ h, distillation column column bottom temperature controls at 104～110 DEG C, the middle temperature of tower
Degree controls at 80～95 DEG C, and tower top temperature controls at 75～77 DEG C, and the first condenser temperature controls at 65～75 DEG C, the second condensation
Device temperature controls at 40～60 DEG C, and the 3rd condenser temperature controls below 34 DEG C, the voltage-controlled system of distillation column 0.02～
0.05MPa。
The beneficial effects of the present invention is:
(1) from distillation column top, steam out be introduced into preheater to enter back into condenser (is not to be directly entered condensation
Device): the temperature of recovery tower top alcohol vapour is 75-77 DEG C, carries out through the light ethanol that preheater and temperature are 40-50 DEG C
Heat exchange, improves light ethanol and enters the temperature of recovery tower, can be with steam saving.
(2) distillation column bottom arranges reboiler: makes the steam of boiler directly not contact with waste liquid at the bottom of tower, the most indirectly heats
Mode, the most i.e. decrease the discharge of waste water, Boiler Steam can be made again to become the profit of the high-temperature water recycling boiler after condensed water
With, save coal.
(3) the preprocessed system of ethanol waste liquid process up to standard after, enter back into Distallation systm: by acid-alkali accommodation pH value in
Property, such ethanol waste liquid will not corrode distillation column after entering distillation column, filters out sediment by filter press, can avoid blocking up
Plug delivery pump and column plate, keep the temperature of ethanol waste liquid and wine degree constant, it is ensured that still-process does not fluctuates, and can improve steaming
Evaporate yield, reduce energy resource consumption.
(4) blowoff valve uses pneumatic control valve, automatically controls: can be automatically switched off when temperature is less than 104 DEG C, make in soiling solution
Ethanol content is zero, substantially increases distillation yield.
(5) steam inlet valve uses pneumatic control valve, automatically controls: the steam pressure that can make entrance distillation column is stable, steams
Evaporating process steady, the process of ethanol distillation is steady, can improve, with the consumption of steam saving, the yield that ethanol reclaims.
(6) charging regulation valve uses pneumatic control valve, automatically controls: purpose is that control charging is uniform and stable, still-process
Steadily without fluctuation, distillation yield can be improved and reduce steam mono-consumption.
(7) on feed pipe, effusion meter is set, carries out flow-control: purpose is that control charging is uniform and stable, effusion meter
The numerical value that numerical value automatically controls with pneumatic control valve in computer is proofreaded, it is ensured that the accuracy automatically controlled.
Accompanying drawing explanation
In order to make the purpose of the present invention, technical scheme and beneficial effect clearer, the present invention provides drawings described below to carry out
Illustrate:
Fig. 1 is ethanol waste liquid pretreatment system schematic diagram.
Fig. 2 is ethanol recovery system schematic diagram.
In figure: 1 neutralizing tank, 2 liquid caustic soda measuring tanks, 3 filter sheet frames, 4 waste ethanol storage tanks, 5 sample taps, 6
Air admission valve, 7 reflux inlets, 8 reboilers, 9 ethanol distillation towers, 10 preheaters, 11 first condensers, 12 second
Condenser, 13 the 3rd condensers, 14 vapour liquid separators, 15 finished product coolers, 16 effusion meters, 17 steam enter vapour gas
Dynamic valve, 18 charging pneumatic operated valve, 19 blowdown pneumatic operated valves, 20 outlets A, 21 outlets B, 22 return tanks.
Detailed description of the invention
Below in conjunction with accompanying drawing, the preferred embodiments of the present invention are described in detail.
Embodiment 1
As shown in Figure 1, 2, ethanol reclaims the system of Automated condtrol, reclaims including ethanol waste liquid pretreatment system and ethanol
System, the outlet of ethanol waste liquid pretreatment system is connected with the entrance of ethanol recovery system.
Ethanol recovery system includes reboiler 8, ethanol distillation tower 9, preheater 10, vapour liquid separator 14, condenser system, becomes
Product cooler 15；The liquid outlet of preheater 10 is connected with the liquid inlet of ethanol distillation tower 9 by pipeline, ethanol distillation tower 9
Steam (vapor) outlet be connected with the steam inlet of preheater 10, the steam inlet phase of the steam (vapor) outlet of preheater 10 and condenser system
Even, preheater 10 is connected with the entrance of finished product cooler 15 with the condensate outlet of condenser system；Arrange bottom ethanol distillation tower 9
Ethanol outlet A20 and outlet B21, outlet A20 is connected with the liquid inlet of reboiler 8, the outlet of reboiler 8 and ethanol
The boiling ethanol entrance port of distillation column 9 is connected, and outlet B21 is connected with the liquid inlet of vapour liquid separator 14, vapour liquid separator 14
Gas outlet be connected with the gas entrance of ethanol distillation tower 9.
Condenser system includes first condenser the 11, second condenser the 12, the 3rd condenser 13, the steam of the first condenser 11
Outlet is connected with the steam inlet of the second condenser 12, the steam of the steam (vapor) outlet of the second condenser 12 and the 3rd condenser 13 enters
Mouth is connected.
The ethanol liquid conveyance conduit being connected with preheater 10 is provided with effusion meter 16, connects preheater 10 and ethanol distillation
The liquid conducting pipes of tower 9 is provided with charging pneumatic operated valve 18, and the jet chimney that enters of reboiler 8 is provided with steam and enters vapour pneumatic operated valve
17, outlet B21 is provided with blowdown pneumatic operated valve 19 with the connection pipeline of vapour liquid separator 14.
Ethanol waste liquid pretreatment system includes neutralizing tank 1, liquid caustic soda measuring tank 2, filters sheet frame 3, waste ethanol storage tank 4, described
The discharging opening of liquid caustic soda measuring tank 2 is connected with the feeding mouth of neutralizing tank 1, the discharging opening of neutralizing tank 1 and the feeding mouth phase of filtration sheet frame 3
Even, the discharging opening filtering sheet frame 3 is connected with the feed liquid refluxing opening of neutralizing tank 1, connects and arranges reflux inlet 7 on pipeline, filters sheet frame 3
Discharging opening is also connected with waste ethanol storage tank 4 entrance.
Ethanol described in present embodiment reclaims the system of Automated condtrol and includes following four part:
1, waste ethanol pretreatment controls loop: realize to corrode distillation column after ethanol waste liquid enters distillation column and avoiding blocking up
Plug delivery pump and column plate, waste ethanol is the most neutral by carrying out acid-alkali accommodation pH value in neutralizing tank 1, then filters through screen plate frame 3
Fall sediment, can avoid blocking delivery pump and column plate, keep the temperature of ethanol waste liquid and wine degree constant, keep the temperature of ethanol waste liquid
Constant with wine degree, it is ensured that still-process does not fluctuates, distillation yield can be improved, reduce energy resource consumption.
2, automatic feed controls loop: realize the continuous automatic feed of ethanol recovery system, and ethanol is by warp after preheater
Pipeline enters ethanol distillation tower 9, and evaporation capacity and discharge capacity according to ethanol distillation tower 9 adjust feed rate automatically.
3, automatic computer heating control loop: realize the automatic heating evaporation of ethanol recovery tower, the ethanol in ethanol distillation tower 9 one
Lease making is crossed vapour liquid separator 14 and is discharged, and a part returns to ethanol distillation tower 9 through reboiler 8 and heats, and is automatically adjusted steam
Amount size, it is ensured that tower reactor heating quantity of steam.
4, automatic-discharging controls loop: realize ethanol distillation tower 9 waste ethanol automatic-discharging, ethanol bottom ethanol distillation tower 9
Being discharged by vapour liquid separator 14, this loop adjusts removal waste fluid flow automatically according to temperature in ethanol distillation tower 9, it is ensured that second
Alcohol distillation column 9 continuous high-efficient evaporates, and can be automatically switched off when temperature is less than 104 DEG C, and making the ethanol content in soiling solution is zero, significantly
Improve distillation yield.
Embodiment 2
Embodiment 1 is described further by this enforcement, and ethanol recovery system also includes return tank 22, preheater 10 and first
The liquid outlet of condenser 11 is connected with the entrance of return tank 22, and the outlet of return tank 22 is by pipeline and ethanol distillation tower 9
Alcohol reflux mouth is connected.
Embodiment 3
Ethanol reclaims the method for Automated condtrol: enter back into second after first waste ethanol being carried out pretreatment in pretreatment system
Alcohol reclaims Distallation systm and distills.After pretreatment is for being neutralized waste ethanol coarse-grain mother solution, then filter out through screen plate frame
Sediment；In N-process, waste liquid temperature controls at 40～50 DEG C, and wine degree controls 0%～50%vol, the waste liquor PH after neutralization
It is 6.7～7.2.
Still-process is: steam enters ethanol distillation tower by reboiler and carries out tower body preheating, controls steam pressure simultaneously,
Steam pressure control, 0.04～0.05Mpa, after treating tower body preheating, opens condenser system, waste ethanol after pretreatment
Liquid is entered ethanol distillation tower after being preheated by preheater and distills, and controls fluid flow simultaneously, and waste ethanol flow-control exists
3.5～5.0m3/ h, and regulate temperature and each section of temperature of ethanol distillation tower controlling condenser system, waste ethanol flow-control is 3.5
～5.0m3/ h, distillation column column bottom temperature controls at 104～110 DEG C, and in tower, temperature controls at 80～95 DEG C, and tower top temperature controls
At 75～77 DEG C, the first condenser temperature controls at 65～75 DEG C, and the second condenser temperature controls at 40～60 DEG C, the 3rd condensation
Device temperature controls below 34 DEG C.The preheated device of gas distilled out from ethanol distillation tower carries out heat exchange, then by condensation
System condensing, finally carries out finished product cooling and recovery, and an ethanol liquid part for ethanol distillation tower bottom is by returning after reboiler
To ethanol distillation tower, a part is by returning to ethanol distillation tower with gas form after vapour liquid separator.
Ethanol waste liquid preprocessing process concretely comprises the following steps:
1, waste ethanol coarse-grain mother solution is neutralized
1) in neutralizing tank 1, coarse-grain mother solution and top washing liquid are put into, based on 1.0～2.0% (kg/L) of coarse-grain mother solution volume
Calculate calcium carbonate consumption.
2) open stirring, charge door be slowly added to the calcium carbonate of amount of calculation；Now, substantial amounts of carbon dioxide gas can be produced
Body, so should be slowly added into, in order to avoid feed liquid is overflowed.Add calcium carbonate, continue stirring 20 minutes.
3) liquid caustic soda in liquid caustic soda measuring tank 2 adds neutralizing tank 1, adjusts pH to 6.7～7.2 (test of pH reagent paper), N-process
Middle holding waste liquid temperature 40～50 DEG C；Waste liquid wine degree 30%～50%vol.
2, filter pressing top is washed
1) pressure filter number of units determines: every 70m2Frame holds 1.2m3Pressure filter, should enter neutralizer 20～35m3。
2), after neutralizing, the inlet valve on the bottom valve of neutralizing tank 1, turnover pump valve, filter press, reflux inlet 7 are driven,
Opening dnockout pump 7, feed liquid passes back into former neutralizing tank 1, return time 10～20 minutes through filter press, goes out at filter press
Material mouth sampling is observed, after filtrate clarification, and closing volume valve 7, open filter press outlet valve, feed to waste ethanol storage tank 4.
3) standby top washing liquid: put into enough water in empty neutralizing tank 1.
4) by top washing liquid, come out in the waste ethanol liquid top of remaining in filtration sheet frame 3.
5) open air admission valve 10, blow more than 1 hour, close air admission valve, tear sheet frame discharging open.
Waste ethanol Distillation recovery process concretely comprises the following steps:
1) close the tower bottom valve of ethanol distillation tower 9, open tower top exhaust-valve, open and enter vapour pneumatic operated valve 17, steam into steam
Stress control, 0.04～0.05Mpa, carries out tower body preheating, when tower top just emerges steam, closes tower top exhaust-valve immediately, opens
Open preheater turnover valve and the inlet/outlet valve of each condenser cooling water.
2) open charging pneumatic operated valve 18 and blowdown pneumatic operated valve 19, start feed pump, observe and regulate the feed liquor of effusion meter 16
Valve, makes flow-control 3.5～5.0m3/h。
3) regulation steam enters vapour pneumatic operated valve 17 and each condenser water intaking valve and the outlet valve of correspondence, makes column bottom temperature control
104～110 DEG C, in tower, temperature controls between 80～95 DEG C, and tower top temperature controls at 75～77 DEG C, the first condenser temperature control
System is at 65～75 DEG C, and the second condenser temperature controls at 40～60 DEG C, and the 3rd condenser temperature controls below 34 DEG C.Distilled
Cheng Zhong, the voltage-controlled system of tower is 0.02～0.05MPa.
4) qualified recovery ethanol (>=90%L/L, 20 DEG C) enters finished product basin, and underproof recovery ethanol flows into useless second
Alcohol basin, re-starts distillation.
Embodiment 4
The device before transformation is used to carry out ethanol recovery: the steam in embodiment 3 enters vapour pneumatic operated valve 17, charging pneumatic operated valve
18, blowdown pneumatic operated valve 19 all replaces with hand-operated valve, and other devices and connected mode thereof are with embodiment 3.Ethanol before transformation returns
Receipts concrete operation step is as follows:
First, ethanol waste liquid is carried out pretreatment, concretely comprises the following steps:
1, waste ethanol coarse-grain mother solution is neutralized
1) in neutralizing tank, put into coarse-grain mother solution and top washing liquid, calculate by 1.0～2.0% (kg/L) of coarse-grain mother solution volume
Calcium carbonate consumption.
2) open stirring, charge door be slowly added to the calcium carbonate of amount of calculation；Now, substantial amounts of carbon dioxide gas can be produced
Body, so should be slowly added into, in order to avoid feed liquid is overflowed.Add calcium carbonate, continue stirring 20 minutes.
3) liquid caustic soda in liquid caustic soda measuring tank adds neutralizing tank, adjusts pH to 6.5～8.0 (test of pH reagent paper), in N-process
Do not control waste liquid wine degree and waste liquid temperature.
2, (with embodiment 3) is washed on filter pressing top
Then, waste ethanol is carried out Distillation recovery, concretely comprises the following steps:
1) close the tower bottom valve of ethanol distillation tower, open tower top exhaust-valve, open into steam hand-operated valve, Steam pressure control
0.04～0.06Mpa, carry out tower body preheating, when tower top just emerges steam, close tower top exhaust-valve immediately, open preheater
Turnover valve and the inlet/outlet valve of each condenser cooling water.
2) open inlet valve and blowoff valve, start feed pump, observe and regulate the liquid feed valve of effusion meter, make flow-control exist
3.5～5.0m3/h。
3) regulation steam inlet valve and each condenser water intaking valve and the outlet valve of correspondence, make column bottom temperature control 104～
110 DEG C, in tower, temperature controls between 80～95 DEG C, and tower top temperature controls at 75～77 DEG C, and the first condenser temperature controls
65～75 DEG C, the second condenser temperature controls at 40～60 DEG C, and the 3rd condenser temperature controls below 34 DEG C.Still-process
In, the voltage-controlled system of tower is 0.02～0.05MPa.
4) qualified recovery ethanol (>=90%L/L, 20 DEG C) enters finished product basin, and underproof recovery ethanol flows into useless second
Alcohol basin, re-starts distillation.
Embodiment 5
Embodiment 3 and the energy resource consumption of embodiment 4 and alcohol yield contrast, and refer to table 1.
Table 1 energy resource consumption contrasts with alcohol yield
| Project | Embodiment 4 | Embodiment 3 |
| Ethanol unit consumption | 1.86 tons/ton | 1.45 tons/ton |
| Steam mono-consumption | 1.16 tons/ton | 1.03 tons/ton |
| Alcohol recycle rate | 95% | 97% |
As can be seen here, use apparatus and method of the present invention, the skill before ethanol unit consumption and steam mono-consumption are both less than transformed
Art, alcohol recycle rate is higher than the technology before transformation.Therefore the technical method of the present invention achieves energy-saving and cost-reducing, improves ethanol and steams
Evaporate yield.
Finally illustrate, preferred embodiment above only in order to technical scheme to be described and unrestricted, although logical
Cross above preferred embodiment the present invention to be described in detail, it is to be understood by those skilled in the art that can be
In form and it is made various change, without departing from claims of the present invention limited range in details.
Claims (10)
1. ethanol reclaims the system of Automated condtrol, it is characterised in that: include that ethanol waste liquid pretreatment system and ethanol reclaim system
System, the described outlet of ethanol waste liquid pretreatment system is connected with the entrance of ethanol recovery system.
Ethanol the most according to claim 1 reclaims the system of Automated condtrol, it is characterised in that: described ethanol recovery system
Including reboiler (8), ethanol distillation tower (9), preheater (10), vapour liquid separator (14), condenser system and finished product cooler
(15)；The liquid outlet of described preheater (10) is connected with the liquid inlet of ethanol distillation tower (9) by pipeline, and described ethanol steams
The steam inlet of the steam (vapor) outlet and preheater (10) that evaporate tower (9) is connected, the steam (vapor) outlet of preheater (10) and condenser system
Steam inlet is connected, and described preheater (10) is connected with the entrance of finished product cooler (15) with the condensate outlet of condenser system；
Described ethanol distillation tower (9) bottom arranges ethanol outlet A (20) and outlet B (21), described outlet A (20) and reboiler
(8) liquid inlet is connected, and the outlet of reboiler (8) is connected with the boiling ethanol entrance port of ethanol distillation tower (9), described outlet
B (21) is connected with the liquid inlet of vapour liquid separator (14), gas outlet and the ethanol distillation tower of described vapour liquid separator (14)
(9) gas entrance is connected.
Ethanol the most according to claim 2 reclaims the system of Automated condtrol, it is characterised in that: described condenser system includes
First condenser (11), the second condenser (12), the 3rd condenser (13), the steam (vapor) outlet of described first condenser (11) and
The steam inlet of two condensers (12) is connected, the steam (vapor) outlet of the second condenser (12) and the steam inlet of the 3rd condenser (13)
It is connected.
Ethanol the most according to claim 2 reclaims the system of Automated condtrol, it is characterised in that: it is connected with preheater (10)
Ethanol liquid conveyance conduit be provided with effusion meter (16), connect preheater (10) and the liquid delivery tube of ethanol distillation tower (9)
Road is provided with charging pneumatic operated valve (18), and the jet chimney that enters of reboiler (8) is provided with steam and enters vapour pneumatic operated valve (17), outlet B
(21) the connection pipeline with vapour liquid separator (14) is provided with blowdown pneumatic operated valve (19).
Ethanol the most according to claim 1 reclaims the system of Automated condtrol, it is characterised in that: described ethanol waste liquid is located in advance
Reason system includes neutralizing tank (1), liquid caustic soda measuring tank (2), filters sheet frame (3) and waste ethanol storage tank (4), described liquid caustic soda measuring tank
(2) discharging opening is connected with the feeding mouth of neutralizing tank (1), the discharging opening of described neutralizing tank (1) and the feeding mouth of filtration sheet frame (3)
Being connected, the discharging opening of described filtration sheet frame (3) is connected with the feed liquid refluxing opening of neutralizing tank (1), connects and arranges reflux inlet on pipeline
(7), described filtration sheet frame (3) discharging opening is also connected with waste ethanol storage tank (4) entrance.
Ethanol the most according to claim 2 reclaims the system of Automated condtrol, it is characterised in that: described ethanol recovery system
Also include return tank (22), the entrance phase of the liquid outlet of described preheater (10) and the first condenser (11) and return tank (22)
Even, the outlet of return tank (22) is connected by the alcohol reflux mouth of pipeline with ethanol distillation tower (9).
7. the method that ethanol reclaims Automated condtrol, it is characterised in that: first in pretreatment system, waste ethanol is carried out pretreatment
After enter back into ethanol recovery system and carry out Distillation recovery.
Ethanol the most according to claim 7 reclaims the method for Automated condtrol, it is characterised in that: described pretreatment will be for giving up
After ethanol coarse-grain mother solution is neutralized, then filter out sediment through screen plate frame；In described N-process, waste liquid temperature controls 40
～50 DEG C, wine degree controls 0%～50%vol, and the waste liquor PH after neutralization is 6.7～7.2.
Ethanol the most according to claim 7 reclaims the method for Automated condtrol, it is characterised in that described Distillation recovery process
For: steam enters ethanol distillation tower by reboiler and carries out tower body preheating, controls steam pressure simultaneously, treats that tower body preheating is complete
After, open condenser system, waste ethanol liquid after pretreatment is entered ethanol distillation tower after being preheated by preheater and distills,
Control fluid flow simultaneously, and regulate temperature and each section of temperature of ethanol distillation tower controlling condenser system, from ethanol distillation tower
The preheated device of gas distilled out carries out heat exchange, then is condensed by condenser system, finally carries out finished product cooling and recovery, ethanol
An ethanol liquid part bottom distillation column by returning to ethanol distillation tower after reboiler, a part by after vapour liquid separator with
Gas form returns to ethanol distillation tower.
Ethanol the most according to claim 9 reclaims the method for Automated condtrol, it is characterised in that: in described still-process,
Steam pressure control 0.04～0.05Mpa, the voltage-controlled system of distillation column 0.02～0.05MPa, waste ethanol flow-control 3.5～
5.0m3/ h, distillation column column bottom temperature controls at 104～110 DEG C, and in tower, temperature controls at 80～95 DEG C, and tower top temperature controls
75～77 DEG C, the first condenser temperature controls at 65～75 DEG C, and the second condenser temperature controls at 40～60 DEG C, the 3rd condenser
Temperature controls below 34 DEG C, and the voltage-controlled system of distillation column is 0.02～0.05MPa.
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