CN206447795U - The energy saver of dihydric alcohol aqueous solution dehydration by-product monohydric alcohol - Google Patents
The energy saver of dihydric alcohol aqueous solution dehydration by-product monohydric alcohol Download PDFInfo
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- CN206447795U CN206447795U CN201720120069.7U CN201720120069U CN206447795U CN 206447795 U CN206447795 U CN 206447795U CN 201720120069 U CN201720120069 U CN 201720120069U CN 206447795 U CN206447795 U CN 206447795U
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Abstract
The utility model is related to a kind of energy saver of dihydric alcohol aqueous solution dehydration by-product monohydric alcohol, the process and device of removing moisture and the monohydric alcohol in by-product binary alcohol solution during it is a kind of alcohol solution from binary.Whole device at least includes five towers and its corollary equipments such as the first dehydrating tower (T101), the second dehydrating tower (T102), the 3rd dehydrating tower (T103), methanol and ethanol tower (T104), methanol column (T105).The utility model employs multitower and is thermally integrated process, the operation energy consumption of whole device is reduced, while by-product monohydric alcohol product.With significant practicality and economic benefit, have a extensive future.
Description
Technical field
The utility model is related to a kind of energy saver of dihydric alcohol aqueous solution dehydration by-product monohydric alcohol, and it is a kind of from binary
Moisture is removed in alcohol solution and the process and device of monohydric alcohol in binary alcohol solution is reclaimed.
Background technology
Currently, in face of increasingly serious energy crisis, regenerated resources have turned into the most important thing of following survival and development.20 generation
Record since the nineties, due to the sharp increase of world's fiber product market comsupton, dihydric alcohol is very important organic as a class
Industrial chemicals is widely used by feat of many purposes and advantage, in the fields such as chemical fibre, polyester resin industrial production
With very high application value.
Ethylene glycol is most simple and most important aliphatic dihydroxy alcohol, and its purposes is widely.Current ethylene glycol maximum
Purposes is production polyester resin (fiber and film), and polyester resin is mainly used to make beverage industries PET bottle and textile industry at present
Terylene, is then to be used to produce various engineering plastics in addition.Another important use of ethylene glycol is do automobile radiators cold
But agent, because ethylene glycol can significantly reduce the freezing point of the aqueous solution, therefore available for antifreeze.In addition to above-mentioned two big purposes, second two
Alcohol is also its larger consuming point as organic intermediate, and ethylene glycol is just come from as the glyoxal of artificial silk anti-piping compound.Second two
The polymer that alcohol is generated with polyacid is referred to as alkyd resin, and they are main in the form of dryness resin and plasticizer after modified
Sell.
The viscosity and good hygroscopicity of propane diols, it is nontoxic, thus it is widely used as moisture absorption in food, medicine and cosmetics industry
Agent, antifreeze, lubricant and solvent.In addition, it is also production unsaturated polyester resin, epoxy resin, polyurethane resin and conjunction
Into the important intermediate of plasticizer etc., the extensive use in plastics industry.
1,4- butanediols are mainly for the manufacture of tetrahydrofuran, gamma-butyrolacton and polyurethane.1,4- butanediols and adipic acid etc.
The excellent polyurethane elastomer of low-temperature characteristics, fracture strength, tensile strength can be made in the polyester that polynary acid reaction is obtained, and can use
In synthetic leather, the raw material of shaping polyurethane elastomer.Another important use of 1,4- butanediols is to prepare engineering thermoplastic
Plastics PBT resin, as building and engineering plastics, it has excellent mechanical property and electric property, and its production development is rapid.
The monobasic acid ester of 1,3 butylene glycol is used as the plasticizer of cellulose and polyvinyl chloride.The polyester-type plasticising prepared by dicarboxylic esters
Agent, with good compatibility and resistance to migration, is with a wide range of applications, is favorably improved the stability for being plasticized thing.
1,3-BDO is also used for producing the terminator of oil-free alkyd resin, antifreezing agent, humidizer, coupling agent as aircraft etc..2,
3- butanediols are used to produce in special ebonite production industry as crosslinking agent, are the important intermediates of pharmaceuticals industry.
It can be used as humidizer, plasticizer, after being mixed with other compounds, antifreezing agent of good performance can be made.
In view of the above-mentioned extensive use of dihydric alcohol, the new technology such as synthesis gas preparing ethylene glycol, biomass preparing ethylene glycol in recent years
It is rapidly developed.And in the production process of dihydric alcohol, plant energy consumption be influence dihydric alcohol production cost key factor it
One.With increasingly serious the problems such as oil, coal, the in short supply of natural gas equal energy source resource, environmental pollution and greenhouse effects, two
The reduction production cost of the industries such as first alcohol has turned into Business survival and has improved the key of competitiveness, increasingly by the weight of each side
Depending on.
Chinese patent CN1765860A discloses one kind concentrating lower polyol process from dilute aqueous solution, by dilute water
Solution concentration process is divided into the upgrading unit of 2~8 series connection to complete inside whole concentration process, each upgrading unit again by 2
~6 concentration tower serial operations, after the segmentation concentration of such 2~8 upgrading units, obtain polyalcohol concentrate.Though
So whole concentration process can be carried out in the range of vacuum to normal pressure, and required heat source all can be by internal system low-grade heat
Source is provided, but monohydric alcohol removal process is not carried out while dehydration to be thermally integrated operation, subsequently also to be expended steam and be completed unitary
The purification of alcohol, overall energy consumption is higher.
The content of the invention
The purpose of this utility model is to provide a kind of energy saver of dihydric alcohol aqueous solution dehydration by-product monohydric alcohol, and it is
Moisture is removed in a kind of alcohol solution from binary and the process and device of monohydric alcohol in binary alcohol solution is reclaimed.
Whole device at least include five towers such as the first dehydrating tower, the second dehydrating tower, the 3rd dehydrating tower, methanol and ethanol tower, methanol column and its
Corollary equipment.The utility model employs multitower and is thermally integrated process, the operation energy consumption of whole device is reduced, in the same of dehydration
When, can by-product monohydric alcohol product.With significant practicality and economic benefit, have a extensive future.
A kind of energy-saving process method for dihydric alcohol aqueous solution dehydration by-product monohydric alcohol that the utility model is provided includes as follows
Step：
1) five towers such as the first dehydrating tower, the second dehydrating tower, the 3rd dehydrating tower, methanol and ethanol tower, methanol column are at least included.
2) the second dehydrating tower is by being thermally integrated operation between the first dehydration column reboiler and the first dehydrating tower.
3) operation is directly thermally integrated between the second dehydrating tower and methanol and ethanol tower, the second dehydration column overhead vapor is directly drawn
Enter methanol and ethanol tower tower reactor, separation institute calorific requirement is provided for methanol and ethanol tower.
4) the second dehydrating tower is by being thermally integrated operation between methanol column reboiler and methanol column.
5) waste water is discharged respectively from the second dehydration column overhead, the 3rd dehydration column overhead, methanol and ethanol tower tower reactor.
6) from methanol column overhead or top side take-off methanol.
7) ethanol water for being substantially free of methanol is obtained from methanol column tower reactor.
8) the dehydration diol mixture for being substantially free of moisture is obtained from the 3rd dehydrating tower tower reactor.
The process provided by the utility model, includes following any one or they for the thermal source to raw material preheating
Any combination mode：First dehydration column overhead gas phase, the 3rd dehydration column overhead gas phase, methanol and ethanol column overhead gas phase, methanol column
Top gaseous phase, the second dehydration column reboiler heating vapour-condensing liquid, the 3rd dehydration column reboiler heating vapour-condensing liquid, the second dehydrating tower
Overhead extraction waste water, the 3rd dehydration column overhead extracted waste water, the dehydration diol mixture of the 3rd dehydrating tower tower reactor extraction, first and second
Alcohol tower tower reactor extracted waste water, methanol column reboiler heating gas phase lime set, waste water, methanol, ethanol water.
Second dehydrating tower is thermally integrated operation (Fig. 1) with methanol and ethanol tower, and its mode can be the second dehydration column overhead water
Steam is introduced directly into methanol and ethanol tower tower reactor, and separation institute calorific requirement is provided for methanol and ethanol tower.
Second dehydrating tower is thermally integrated operation (Fig. 2) with methanol and ethanol tower, and its mode can also be the second dehydrating tower and first
Operation is thermally integrated by methanol and ethanol tower reboiler indirectly between ethanol tower.
The process provided by the utility model, the economic benefits and social benefits heat collection between described the first dehydrating tower, the second dehydrating tower
It is split as being thermally integrated operation between 2~6 dehydrating towers the need for being thermally integrated according to internal system into operation.Such as Fig. 3 institutes
Show, can increase the 4th dehydrating tower, the first dehydrating tower (T101) tower reactor discharging pipeline is connected with the 4th dehydrating tower (T106),
4th dehydrating tower (T106) tower reactor discharging pipeline is connected with the second dehydrating tower (T102), the second dehydrating tower (T102) top gaseous phase pipe
Line is connected with the 4th dehydration column reboiler (E112) shell side inlet, the 4th dehydrating tower (T106) top gaseous phase pipeline and first is dehydrated
Tower reboiler (E101) shell side inlet is connected, and triple effect is formed between the first dehydrating tower, the 4th dehydrating tower, the second dehydrating tower and is thermally integrated
Operation, the 4th dehydration column overhead steam provides thermal source to the first dehydrating tower tower reactor, and the second dehydration column overhead steam is to the 4th dehydration
Tower tower reactor provides thermal source, and the second dehydrating tower is the first effect, and the 4th dehydrating tower is the second effect, and the first dehydrating tower is triple effect.
The process provided by the utility model, described the second dehydration column reboiler, the 3rd dehydration column reboiler,
Reboiler in three dehydrating tower feed preheaters, the 3rd dehydrating tower tower, thermal source used in the 4th dehydration column reboiler can be fresh steamings
Vapour, conduction oil, or the material steam that internal system is produced.
In the process provided by the utility model, the 3rd described dehydrating tower feed preheater and the 3rd dehydrating tower tower
Reboiler is the heat exchanger in order to be set using internal system thermal source, and two can all omit without that can also omit and wherein appoint
What one.
The process provided by the utility model, described each tower typical operation conditions are：
First dehydration column overhead operating pressure scope is 5~150kpa；
Second dehydration column overhead operating pressure scope is 50~300kpa；
3rd dehydration column overhead operating pressure scope is 5~200kpa；
Methanol and ethanol column overhead operating pressure scope is 5~200kpa；
Methanol column overhead operating pressure scope is 10~300kpa.
Unless otherwise specified, all pressure refer both to absolute pressure in the utility model.
The process provided by the utility model, described each tower preferred operations condition is：
First dehydration column overhead operating pressure is 40kpa, 75 DEG C of tower top, 86 DEG C of tower reactor；
Second dehydration column overhead operating pressure is 170kpa, 107 DEG C of tower top, 117 DEG C of tower reactor；
3rd dehydration column overhead operating pressure is 15kpa, 56 DEG C of tower top, 142 DEG C of tower reactor；
Methanol and ethanol column overhead operating pressure is 105kpa, 73.8 DEG C of tower top, 104 DEG C of tower reactor；
Methanol column overhead operating pressure is 105kpa, 64 DEG C of tower top, 80 DEG C of tower reactor.
The energy saver for the dihydric alcohol aqueous solution dehydration by-product monohydric alcohol that the utility model is provided：Including the first dehydrating tower,
Five towers and the connecting pipelines such as the second dehydrating tower, the 3rd dehydrating tower, methanol and ethanol tower, methanol column.
Described feed preheater is connected in the middle part of the first dehydrating tower；First dehydration column overhead and the first dehydrating tower condenser
Connection, the first dehydrating tower condensator outlet is connected with the middle part of the first dehydration column overhead and methanol and ethanol tower respectively；First dehydrating tower bottom
Portion is connected with the first dehydration column reboiler tube-side inlet and the second dehydrating tower respectively, the first dehydration column reboiler tube side outlet connection
To the first dehydrating tower tower reactor；
Second dehydration column overhead is boiled again with the first dehydration column reboiler shell side inlet, methanol and ethanol tower tower reactor, methanol column respectively
Device shell side inlet is connected；First dehydration column reboiler shell-side outlet is connected to the second dehydration column overhead and waste water discharging pipeline；The
Two dehydration tower bottoms are connected with the second dehydration column reboiler tube-side inlet and the 3rd dehydrating tower feed preheater respectively, the second dehydration
The outlet of tower reboiler tube side is connected to the second dehydrating tower tower reactor；
3rd dehydrating tower feed preheater is exported with being connected in the middle part of the 3rd dehydrating tower；3rd dehydration column overhead and the 3rd dehydration
Tower condenser is connected, and the 3rd dehydrating tower condensator outlet is connected with the 3rd dehydration column overhead with waste water discharging pipeline respectively；3rd
Reboiler is connected in the middle part of the 3rd dehydrating tower in dehydrating tower tower；3rd dehydration tower bottom respectively with the 3rd dehydration column reboiler tube side
Entrance is connected with dehydration diol mixture discharging pipeline, and the outlet of the 3rd dehydration column reboiler tube side is connected to the 3rd dehydrating tower tower
Kettle；
Methanol and ethanol column overhead is connected with methanol and ethanol tower condenser, methanol and ethanol tower condensator outlet respectively with methanol and ethanol column overhead
It is connected with methanol column middle part；Methanol and ethanol tower tower reactor is connected with waste water discharging pipeline；
Methanol column overhead is connected with methanol column condenser, and methanol column condensator outlet goes out with methanol column overhead and methanol respectively
Expects pipe line is connected；Methanol tower bottom is connected with methanol column reboiler tube-side inlet and ethanol water discharging pipeline respectively；Methanol
The outlet of tower reboiler tube side is connected to methanol column tower reactor；Methanol column reboiler shell-side outlet is connected with waste water discharging pipeline.
The utility model is related to a kind of energy-saving process method and device of dihydric alcohol aqueous solution dehydration by-product monohydric alcohol, and it is
The process and device of moisture and the monohydric alcohol in by-product binary alcohol solution are removed in a kind of alcohol solution from binary.
Whole device at least include five towers such as the first dehydrating tower, the second dehydrating tower, the 3rd dehydrating tower, methanol and ethanol tower, methanol column and its
Corollary equipment.The utility model employs multitower and is thermally integrated process, the operation energy consumption of whole device is reduced, while by-product one
First alcohol product.With significant practicality and economic benefit, have a extensive future.
Brief description of the drawings
Fig. 1 is a kind of energy-saving process method flow of typical dihydric alcohol aqueous solution dehydration by-product monohydric alcohol of the utility model
Figure.
Fig. 2 is that a kind of of Fig. 1 develops process, and the second dehydration column overhead water vapour shown in Fig. 1 is not introduced directly into first
Ethanol tower tower reactor, but enter methanol and ethanol tower reboiler shell side, realize that the second dehydrating tower is thermally integrated operation indirectly with methanol and ethanol tower.
The thermal source that reboiler is used in the 3rd dehydrating tower tower shown in Fig. 1 is not live steam, heating vapour-condensing liquid or conduction oil, and
It is to use the second dehydration column overhead water vapour.
Fig. 3 is Fig. 1 another differentiation process, the economic benefits and social benefits between the first dehydrating tower, the second dehydrating tower shown in Fig. 1
It is thermally integrated operation and is split as triple effect and is thermally integrated operation.Increase the 4th dehydrating tower, the first dehydrating tower, the 4th dehydrating tower, second
Triple effect is formed between dehydrating tower and is thermally integrated operation, the 4th dehydration column overhead steam provides thermal source, second to the first dehydrating tower tower reactor
Dehydration column overhead steam provides thermal source to the 4th dehydrating tower tower reactor, and the second dehydrating tower is the first effect, and the 4th dehydrating tower is the second effect,
First dehydrating tower is triple effect.
Embodiment
Specific embodiment of the present utility model is explained in detail with reference to the accompanying drawings as follows, but for illustrative purposes only rather than limits this reality
With new.
Unless otherwise specified, the composition of the process equipment such as unreceipted specifically used tower part, structure, material in embodiment
(being used to connect connecting pipeline between each tower part etc.), reagent etc., commercially obtain, or this area ordinary skill
Personnel's method known to is obtained.Involved specific experiment method, operating condition, generally according to common process condition and hand
Condition described in volume, or according to the condition proposed by manufacturer.
A kind of energy-saving process method for dihydric alcohol aqueous solution dehydration by-product monohydric alcohol that the utility model is provided includes as follows
Step：
1) the first dehydrating tower (T101), the second dehydrating tower (T102), the 3rd dehydrating tower (T103), methanol and ethanol tower are at least included
(T104), five towers such as methanol column (T105)；
2) the second dehydrating tower (T102) passes through hot between the first dehydration column reboiler (E101) and the first dehydrating tower (T101)
Integrated operation；
3) operation is directly thermally integrated between the second dehydrating tower (T102) and methanol and ethanol tower (T104), by the second dehydrating tower
(T102) tower top vapor is introduced directly into methanol and ethanol tower (T104) tower reactor, is that methanol and ethanol tower (T104) provides separation institute calorific requirement；
4) the second dehydrating tower (T102) between methanol column reboiler (E107) and methanol column (T105) by being thermally integrated operation；
5) from the second dehydrating tower (T102) tower top, the 3rd dehydrating tower (T103) tower top, methanol and ethanol tower (T104) tower reactor difference
Discharge waste water；
6) from methanol column (T105) tower top or top side take-off methanol (38)；
7) ethanol water (42) for being substantially free of methanol is obtained from methanol column (T105) tower reactor；
8) the dehydration diol mixture (29) for being substantially free of moisture is obtained from the 3rd dehydrating tower (T103) tower reactor.
The process provided by the utility model, is comprised the concrete steps that：Dihydric alcohol aqueous feed solution (1) is through feed preheater
(E100) laggard first dehydrating tower (T101) is preheated.Overhead vapours (2) is condensed solidifying through the first dehydrating tower condenser (E102)
Liquid (3) is divided into two strands, and one directly returns to the first dehydrating tower (T101) tower top as phegma (4), and another burst of material (5) enters
In the middle part of methanol and ethanol tower (T104).First dehydrating tower (T101) kettle material (9) enters the second dehydrating tower (T102).
Second dehydrating tower (T102) is thermally integrated operation, the second dehydrating tower (T102) tower top with the first dehydrating tower (T101)
Water vapour (10) is divided into three strands, and first burst of water vapour (11) enters the first dehydration column reboiler (E101) shell side, vapor
(11) condensed lime set (14) is divided into two strands, and one is directly returned as phegma (15) at the top of the second dehydrating tower (T102),
Another burst of lime set (16) enters waste discharge (44) as extraction.Second dehydrating tower (T102) kettle material (20) is through the 3rd dehydration
Enter after tower feed preheater (E109) heating in the middle part of the 3rd dehydrating tower (T103).
3rd dehydrating tower (T103) overhead vapours (22) is through the 3rd dehydrating tower condenser (E104) condensed lime set (23)
It is divided into two strands, one directly returns to the 3rd dehydrating tower (T103) tower top as phegma (24), and another burst of lime set (25), which is used as, adopts
Go out to enter waste discharge (44).Reboiler (E110) in 3rd dehydrating tower tower is set in the middle part of the 3rd dehydrating tower (T103).3rd takes off
Water tower (T103) tower reactor extraction material is the dehydration diol mixture (29) for being substantially free of moisture.
Second dehydrating tower (T102) is thermally integrated operation, the second dehydrating tower (T102) overhead water with methanol and ethanol tower (T104)
Steam (10) is divided into three strands, and second burst of steam (12) is introduced directly into methanol and ethanol tower (T104) tower reactor, is methanol and ethanol tower (T104)
Separation institute calorific requirement is provided.Methanol and ethanol tower (T104) overhead vapours (30) is through methanol and ethanol tower condenser (E106) condensed lime set
(31) it is divided into two strands, one directly returns to methanol and ethanol tower (T104) tower top as phegma (32), and another burst of lime set (33) enters
In the middle part of methanol column (T105).Methanol and ethanol tower (T104) kettle material (34) enters waste discharge (44) as extraction.
Second dehydrating tower (T102) is thermally integrated operation with methanol column (T105), and the second dehydrating tower (T102) overhead water is steamed
Vapour (10) is divided into three strands, and the 3rd burst of water vapour (13) enters methanol column reboiler (E107) shell side, after vapor (13) condensation
Lime set (43) as extraction enter waste discharge (44).Methanol column (T105) overhead vapours (35) is through methanol column condenser
(E108) condensed lime set (36) is divided into two strands, and one is directly returned as phegma (37) at the top of methanol column (T105), separately
One lime set (38) is produced as methanol product.Methanol column (T105) also can tower top carry out total reflux operation, by tower top side line
Produce methanol (38).Methanol column (T105) kettle material (42) produces the ethanol water (42) for being substantially free of methanol.
The process provided by the utility model, its typical raw material, which is constituted, is：
Above-mentioned raw materials compositing range is not constituted to any limitation of the present utility model, and the utility model can be used for various compositions
Binary alcohol solution separation.In the utility model unless otherwise specified, described propane diols refers both to 1,2-PD.
Embodiment 1：
As shown in figure 1, dihydric alcohol aqueous feed solution (1) preheats laggard first dehydrating tower through feed preheater (E100)
(T101).Overhead vapours (2) is divided into two strands through the first dehydrating tower condenser (E102) condensed lime set (3), one as return
Flow liquid (4) directly returns to the first dehydrating tower (T101) tower top, and another burst of material (5) enters in the middle part of methanol and ethanol tower (T104).First
Dehydrating tower (T101) kettle material (9) enters in the middle part of the second dehydrating tower (T102).
Second dehydrating tower (T102) is thermally integrated operation with the first dehydrating tower (T101), and the second dehydrating tower (T102) overhead water is steamed
Vapour (10) is divided into three strands, and first strand (11) enter the first dehydration column reboiler (E101) shell side, and vapor (11) is condensed
Lime set (14) is divided into two strands, and one is directly returned as phegma (15) at the top of the second dehydrating tower (T102), and another stock (16) is made
Enter waste discharge (44) for extraction.Second dehydrating tower (T102) kettle material (20) is through the 3rd dehydrating tower feed preheater
(E109) enter after heating in the middle part of the 3rd dehydrating tower (T103).
3rd dehydrating tower (T103) overhead vapours (22) is through the 3rd dehydrating tower condenser (E104) condensed lime set (23)
Be divided into two strands, one directly returns to the 3rd dehydrating tower (T103) tower top as phegma (24), another stock (25) as produce into
Enter waste discharge (44).Reboiler (E110) in 3rd dehydrating tower tower is set in the middle part of the 3rd dehydrating tower (T103).3rd dehydrating tower
(T103) tower reactor extraction material is the dehydration diol mixture (29) for being substantially free of moisture.
Second dehydrating tower (T102) is thermally integrated operation, the second dehydrating tower (T102) overhead vapor stream with methanol and ethanol tower (T104)
(10) three strands are divided into, second strand (12) are introduced directly into methanol and ethanol tower (T104) tower reactor, are that methanol and ethanol tower (T104) provides separation
Institute's calorific requirement.Methanol and ethanol tower (T104) overhead vapours (30) is divided into through methanol and ethanol tower condenser (E106) condensed lime set (31)
Two strands, one directly returns to methanol and ethanol tower (T104) tower top as phegma (32), and another stock (33) enters methanol column (T105)
Middle part.Methanol and ethanol tower (T104) kettle material (34) enters waste discharge (44) as extraction.
Second dehydrating tower (T102) is thermally integrated operation, the second dehydrating tower (T102) overhead vapor stream with methanol column (T105)
(10) three strands are divided into, the 3rd strand (13) enter methanol column reboiler (E107) shell side, vapor (13) condensed lime set
(43) waste discharge (44) is entered as extraction.Methanol column (T105) overhead vapours (35) is condensed through methanol column condenser (E108)
Lime set (36) afterwards is divided into two strands, and one is directly returned as phegma (37) at the top of methanol column (T105), and another stock (38) is made
Produced for methanol product.Methanol column (T105) also can tower top carry out total reflux operation, by tower top side take-off methanol (38).First
Alcohol tower (T105) kettle material (42) produces the ethanol water (42) for being substantially free of methanol.
A kind of typical operation conditions of each tower in embodiment 1 are following present, typical operation conditions and operation energy consumption are as follows：
First dehydrating tower (T101) tower top operating pressure is 40kpa, 75 DEG C of tower top, 86 DEG C of tower reactor；
Second dehydrating tower (T102) tower top operating pressure is 170kpa, 107 DEG C of tower top, 117 DEG C of tower reactor；
3rd dehydrating tower (T103) tower top operating pressure is 15kpa, 56 DEG C of tower top, 142 DEG C of tower reactor；
Methanol and ethanol tower (T104) tower top operating pressure is 105kpa, 73.8 DEG C of tower top, 104 DEG C of tower reactor；
Methanol column (T105) tower top operating pressure is 105kpa, 64 DEG C of tower top, 80 DEG C of tower reactor.
Whole concentration systems only the 3rd dehydrating tower (T103) tower bottom reboiler E-105 needs middle pressure steam to heat, by 100,000
Ton/year dihydric alcohol device, middle pressure steam consumption is 3 ton hours.Thermal source needed for remaining each reboiler, heat exchanger is using being
System internal heat resource or follow-up polyalcohol refined part tower top material steam or the follow-up polyalcohol refined part tower top material of use
The low-pressure steam heating of generation.And above-mentioned steam consumption quantity has been contained needed for methanol and ethanol tower (T104) and methanol column (T105)
The ton hour of heat 4 needed for by-product monohydric alcohol.
With dihydric alcohol aqueous solution dehydration and reclaim monohydric alcohol calculate, this patent provide dihydric alcohol aqueous solution dehydration by-product one
The energy-saving process method of first alcohol is compared with the process that CN1765860A is provided：
Steam 4.5-3+4=5.5 ton hours can be saved per hour.
Can save every year ton hour × 8000 hour of middle pressure steam 5.5/year=44000 tons/year.
By 150 yuan of calculating of steam per ton, steam expense can be saved every year：
44000 tons/year × 150 yuan/ton yuan/year of ÷ 100,00=,660 ten thousand.
The energy-saving process method and device for the dihydric alcohol aqueous solution dehydration by-product monohydric alcohol that the utility model is provided, with aobvious
Write economic benefit.
Embodiment 2：
As shown in Fig. 2 it, which is a kind of of Fig. 1, develops process, with respect to the process difference shown in Fig. 1 such as
Under：
The second dehydrating tower (T102) overhead vapor stream (12) shown in Fig. 1 is not introduced directly into methanol and ethanol tower (T104) tower reactor,
But enter methanol and ethanol tower reboiler (E111) shell side, realize the second dehydrating tower (T102) and methanol and ethanol tower (T104) indirect thermal collection
Into operation, the second dehydrating tower (T102) tower top vapor (12) condensed lime set (45) enters waste discharge as extraction
(44).The thermal source that reboiler (E110) is used in the 3rd dehydrating tower tower shown in Fig. 1 is not live steam, heating vapour-condensing liquid
Or conduction oil, but the second dehydrating tower (T102) overhead vapor stream (46) is used, condensed lime set (47) enters as extraction
Waste discharge (44).
Embodiment 3：
As shown in figure 3, it is Fig. 1 another differentiation process, with respect to the process difference shown in Fig. 1 such as
Under：
The economic benefits and social benefits between the first dehydrating tower (T101), the second dehydrating tower (T102) shown in Fig. 1 are thermally integrated operation and are split as
Triple effect is thermally integrated operation.Increase the 4th dehydrating tower (T106), the first dehydrating tower (T101), the 4th dehydrating tower (T106), the
Triple effect is formed between two dehydrating towers (T102) and is thermally integrated operation, the second dehydrating tower (T102) is the first effect, the 4th dehydrating tower
(T106) it is the second effect, the first dehydrating tower (T101) is triple effect.
As shown in figure 3, dihydric alcohol aqueous feed solution (1) preheats laggard first dehydrating tower through feed preheater (E100)
(T101).Overhead vapours (2) is divided into two strands through the first dehydrating tower condenser (E102) condensed lime set (3), one as return
Flow liquid (4) directly returns to the first dehydrating tower (T101) tower top, and another burst of material (5) enters in the middle part of methanol and ethanol tower (T104).First
Dehydrating tower (T101) kettle material (9) enters in the middle part of the 4th dehydrating tower (T106).
4th dehydrating tower (T106) is thermally integrated operation with the first dehydrating tower (T101), and the 4th dehydrating tower (T106) overhead water is steamed
Vapour (48) enters the first dehydration column reboiler (E101) shell side, and vapor (48) condensed lime set (49) is divided into two strands, one
Directly returned as phegma (50) at the top of the 4th dehydrating tower (T106), another stock (51) enters waste discharge as extraction
(44).4th dehydrating tower (T106) kettle material (52) enters in the middle part of the second dehydrating tower (T102).
Second dehydrating tower (T102) is thermally integrated operation with the 4th dehydrating tower (T106), and the second dehydrating tower (T102) overhead water is steamed
Vapour (10) is divided into three strands, and first strand (11) enter the 4th dehydration column reboiler (E112) shell side, and vapor (11) is condensed
Lime set (14) is divided into two strands, and one is directly returned as phegma (15) at the top of the second dehydrating tower (T102), and another stock (16) is made
Enter waste discharge (44) for extraction.Second dehydrating tower (T102) kettle material (20) is through the 3rd dehydrating tower feed preheater
(E109) enter after heating in the middle part of the 3rd dehydrating tower (T103).
It following present a kind of typical operation conditions of each tower in embodiment 3：
First dehydrating tower (T101) tower top operating pressure is 40kpa, 75 DEG C of tower top, 80 DEG C of tower reactor；
4th dehydrating tower (T106) tower top operating pressure is 86kpa, 95 DEG C of tower top, 100 DEG C of tower reactor；
Second dehydrating tower (T102) tower top operating pressure is 170kpa, 115 DEG C of tower top, 122 DEG C of tower reactor；
3rd dehydrating tower (T103) tower top operating pressure is 15kpa, 56 DEG C of tower top, 142 DEG C of tower reactor；
Methanol and ethanol tower (T104) tower top operating pressure is 105kpa, 73.8 DEG C of tower top, 104 DEG C of tower reactor；
Methanol column (T105) tower top operating pressure is 105kpa, 64 DEG C of tower top, 80 DEG C of tower reactor.
The utility model provides a kind of energy saver of dihydric alcohol aqueous solution dehydration by-product monohydric alcohol, and whole device is at least
Including the first dehydrating tower (T101), the second dehydrating tower (T102), the 3rd dehydrating tower (T103), methanol and ethanol tower (T104), methanol column
(T105) five towers and its corollary equipment such as.The utility model employs multitower and is thermally integrated process, reduction whole device
Operation energy consumption, while by-product monohydric alcohol product, with significant practicality and economic benefit.It is subject in conjunction with the embodiments specifically
Bright, the method that the personnel of association area can provide according to the utility model completely suitably change or change and combine, and is come
Realize the technology.It should be strongly noted that all these similar by the technological process progress provided the utility model
Change or change with reconfiguring, it is apparent to those skilled in the art, be considered as in the utility model
Spirit, scope and content in.
Claims (5)
1. a kind of energy saver of dihydric alcohol aqueous solution dehydration by-product monohydric alcohol, it is characterised in that：Including the first dehydrating tower
(T101), the second dehydrating tower (T102), the 3rd dehydrating tower (T103), methanol and ethanol tower (T104), five towers of methanol column (T105) with
And connecting pipeline；
Feed preheater (E100) is connected in the middle part of the first dehydrating tower (T101)；First dehydrating tower (T101) tower top and the first dehydration
Tower condenser (E102) connect, the first dehydrating tower condenser (E102) outlet respectively with the first dehydrating tower (T101) tower top and first and second
It is connected in the middle part of alcohol tower (T104)；First dehydrating tower (T101) bottom respectively with the first dehydration column reboiler (E101) tube-side inlet and
Second dehydrating tower (T102) is connected, and the outlet of the first dehydration column reboiler (E101) tube side is connected to the first dehydrating tower (T101) tower
Kettle；
Second dehydrating tower (T102) tower top respectively with the first dehydration column reboiler (E101) shell side inlet, methanol and ethanol tower (T104) tower
Kettle, methanol column reboiler (E107) shell side inlet are connected；First dehydration column reboiler (E101) shell-side outlet is connected to second and taken off
Water tower (T102) tower top and waste water discharging pipeline；Second dehydrating tower (T102) bottom respectively with the second dehydration column reboiler (E103)
Tube-side inlet and the 3rd dehydrating tower feed preheater (E109) are connected, and the outlet of the second dehydration column reboiler (E103) tube side is connected to
Second dehydrating tower (T102) tower reactor；
3rd dehydrating tower feed preheater (E109) is exported with being connected in the middle part of the 3rd dehydrating tower (T103)；3rd dehydrating tower (T103)
Tower top and the 3rd dehydrating tower condenser (E104) are connected, the outlet of the 3rd dehydrating tower condenser (E104) respectively with the 3rd dehydrating tower
(T103) tower top is connected with waste water discharging pipeline；Reboiler (E110) is connected to the 3rd dehydrating tower (T103) in 3rd dehydrating tower tower
Middle part；3rd dehydrating tower (T103) bottom is mixed with the 3rd dehydration column reboiler (E105) tube-side inlet and dehydration dihydric alcohol respectively
Thing (29) discharging pipeline is connected, and the outlet of the 3rd dehydration column reboiler (E105) tube side is connected to the 3rd dehydrating tower (T103) tower reactor；
Methanol and ethanol tower (T104) tower top is connected with methanol and ethanol tower condenser (E106), methanol and ethanol tower condenser (E106) outlet difference
It is connected with the middle part of methanol and ethanol tower (T104) tower top and methanol column (T105)；Methanol and ethanol tower (T104) tower reactor and waste water discharging pipeline phase
Even；
Methanol column (T105) tower top is connected with methanol column condenser (E108), methanol column condenser (E108) outlet respectively with methanol
Tower (T105) tower top is connected with methanol (38) discharging pipeline；Methanol column (T105) bottom respectively with methanol column reboiler (E107)
Tube-side inlet is connected with ethanol water (42) discharging pipeline；The outlet of methanol column reboiler (E107) tube side is connected to methanol column
(T105) tower reactor；Methanol column reboiler (E107) shell-side outlet is connected with waste water discharging pipeline.
2. according to the device described in claim 1, it is characterised in that one the 4th dehydrating tower (T106) of increase, the first dehydrating tower
(T101) tower reactor discharging pipeline is connected with the 4th dehydrating tower (T106), the 4th dehydrating tower (T106) tower reactor discharging pipeline and second takes off
Water tower (T102) is connected, the second dehydrating tower (T102) top gaseous phase pipeline and the 4th dehydration column reboiler (E112) shell side inlet phase
Even, the 4th dehydrating tower (T106) top gaseous phase pipeline is connected with the first dehydration column reboiler (E101) shell side inlet, to form three
Effect is thermally integrated operation.
3. according to the device described in claim 2, it is characterised in that described the second dehydration column reboiler (E103), the 3rd dehydration
Reboiler (E110), the 4th dehydration in tower reboiler (E105), the 3rd dehydrating tower feed preheater (E109), the 3rd dehydrating tower tower
Tower (T106) reboiler (E112) is passed through live steam, conduction oil, or the material steam that internal system is produced.
4. according to the device described in claim 1, it is characterised in that the 3rd described dehydrating tower feed preheater (E109) and
In three dehydrating tower towers reboiler (E110) all omit without, or omit any of which one.
5. according to the device described in claim 1, it is characterised in that described methanol and ethanol tower (T104) tower reactor connection methanol and ethanol tower
Reboiler (E111), the second dehydrating tower (T102) top gaseous phase pipeline is connected with methanol and ethanol tower reboiler (E111) shell side inlet,
It is thermally integrated indirectly by methanol and ethanol tower reboiler (E111) with realizing between the second dehydrating tower (T102) and methanol and ethanol tower (T104)
Operation.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201720120069.7U CN206447795U (en) | 2017-02-09 | 2017-02-09 | The energy saver of dihydric alcohol aqueous solution dehydration by-product monohydric alcohol |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201720120069.7U CN206447795U (en) | 2017-02-09 | 2017-02-09 | The energy saver of dihydric alcohol aqueous solution dehydration by-product monohydric alcohol |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN206447795U true CN206447795U (en) | 2017-08-29 |
Family
ID=59665522
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|---|---|---|---|
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106748653A (en) * | 2017-02-09 | 2017-05-31 | 天津市新天进科技开发有限公司 | The energy-saving process method and device of dihydroxylic alcohols aqueous solution dehydration by-product monohydric alcohol |
-
2017
- 2017-02-09 CN CN201720120069.7U patent/CN206447795U/en not_active Withdrawn - After Issue
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106748653A (en) * | 2017-02-09 | 2017-05-31 | 天津市新天进科技开发有限公司 | The energy-saving process method and device of dihydroxylic alcohols aqueous solution dehydration by-product monohydric alcohol |
| CN106748653B (en) * | 2017-02-09 | 2023-05-02 | 天津市新天进科技开发有限公司 | Energy-saving process method and device for by-product monohydric alcohol from dehydration of dihydric alcohol aqueous solution |
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