CN206404352U - The device of the tower methanol distillation column by-product ethanol of dividing plate - Google Patents
The device of the tower methanol distillation column by-product ethanol of dividing plate Download PDFInfo
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- CN206404352U CN206404352U CN201720046673.XU CN201720046673U CN206404352U CN 206404352 U CN206404352 U CN 206404352U CN 201720046673 U CN201720046673 U CN 201720046673U CN 206404352 U CN206404352 U CN 206404352U
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- distillation column
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- ethanol
- dividing plate
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Abstract
The utility model is related to a kind of device of the tower methanol distillation column by-product ethanol of dividing plate, mainly includes methanol rectification pre-tower, methanol rectification unit, methanol distillation column, methanol distillation column condenser and connecting pipeline；Described methanol distillation column bottom sets dividing plate, and methanol distillation column bottom is separated into methanol stripping side and ethanol stripping side by dividing plate, and both sides are not connected；Methanol stripping side connects methanol rectification unit by feeding line；While it is that one kind completes Methanol Recovery process in partitioned column, realize the process and device of by-product ethanol, significantly reduce the methanol and ethanol content in fusel oil, it is remarkably improved the yield of methanol product, significantly reduce whole methanol fractionation system operation energy consumption, simultaneously can by-product alcohol product, with significant practicality and economic benefit.
Description
Technical field
The utility model is related to a kind of device of the tower methanol distillation column by-product ethanol of dividing plate.
Background technology
Methanol is a kind of important Organic Chemicals and novel energy fuel, in chemical industry, light industry and clean energy resource field
Tool has been widely used.In synthesizing methanol commercial process, the yield and plant energy consumption of methanol product are influence methanol
One of key factor of production cost.As oil, coal, the in short supply of natural gas equal energy source resource, environmental pollution and greenhouse are imitated
Should the problems such as it is increasingly serious, the reduction production cost of the industry such as methanol has turned into the key of Business survival and raising competitiveness,
Increasingly paid attention to by each side.
Chinese Industrial Standards (CIS)《Industrial methanol》Though ethanol content in regulation methanol product is not known in GB338-2011, typically
User requires that ethanol content is no more than 100ppm.Industrial methanol U.S. federal standard " AA " level（O-M-232K）To methanol product
Middle ethanol content proposes higher requirement, and ethanol content must not exceed 10ppm.
To ensure that the requisite quality of tower top methanol product and tower reactor waste discharge methanol content be not exceeded, the second in dilute methanol liquid
Alcohol is necessarily discharged from fusel oil side line, with the extraction of side line fusel oil, wherein will necessarily also lose a certain amount of methanol.When
Fusel oil ingredient in raw material（For example：Ethanol etc.）When content is higher, necessarily cause increasing for side line fusel oil produced quantity, so as to make
Loss amount into methanol increases, and reduces the yield of methanol product, influences the economic benefit of methyl alcohol product installation.Moreover, a large amount of
Methanol be present in the fusel oil of extraction, also increase the difficulty of follow-up fusel oil processing, add the expense of fusel oil processing
With improving production cost.
The content of the invention
The purpose of this utility model is the device for providing a kind of tower methanol distillation column by-product ethanol of dividing plate, and it is a kind of
While completing Methanol Recovery process in partitioned column, the process and device of by-product ethanol are realized.The utility model is notable
The methanol and ethanol content in fusel oil are reduced, the yield of methanol product is improved, while can by-product alcohol product；Moreover, should be every
The tower methanol distillation column of plate can be thermally integrated with methanol rectification pre-tower, reduce the operation energy consumption of whole methanol fractionation system.With aobvious
The practicality and economic benefit of work, have a extensive future.
A kind of process for the tower methanol distillation column by-product ethanol of dividing plate that the utility model is provided includes：
1）Methanol distillation column body lower part set dividing plate, dividing plate by methanol distillation column bottom be separated into methanol stripping side and
Ethanol stripping side, and both sides are not connected；Dilute methanol liquid from methanol rectification unit is fed by methanol stripping side.
2）Methanol distillation column institute's calorific requirement is by being connected to the methanol stripping side reboiler of methanol stripping side bottom and being connected to
The ethanol stripping side reboiler of ethanol stripping side bottom is provided respectively.
3）Liquid header is set above dividing plate, and liquid cyclone is connected with liquid header；Liquid cyclone is by dividing plate
Upper liquid is assigned to dividing plate both sides.
4）Recovery methanol product is obtained from Methanol Recovery column overhead, recovery alcohol product is obtained from ethanol stripping side bottom,
Waste water is discharged from methanol stripping side bottom, it is very low miscellaneous from side take-off methanol and ethanol content near the charging aperture of methanol stripping side
Alcohol oil.
A kind of process for the tower methanol distillation column by-product ethanol of dividing plate that the utility model is provided, its concrete technology mistake
Cheng Wei：Methanol distillation column bottom sets dividing plate, and methanol distillation column bottom is separated into methanol stripping side and ethanol stripping side by dividing plate,
And both sides are not connected.Dilute methanol liquid from methanol rectification unit is fed by methanol stripping side, and methanol stripping side reboiler is
Methanol stripping side tower reactor provides heat, and the methanol in the dropping liq of methanol stripping side, ethanol are stripped out, drops to methanol and carries
The liquid for evaporating side tower reactor is the waste water without methanol, ethanol, from methanol stripping side tower reactor discharging bottom discharge waste water；Methanol Recovery
Column overhead ascending vapor is condensed through methanol distillation column condenser, and condensate is divided into two parts, and a part is returned as methanol distillation column
Flow liquid enters Methanol Recovery column overhead, and another part is produced as methanol is reclaimed；Phegma by the ethanol in uprising gas in tower and
Moisture is progressively cleaned, and methanol stripping side, which is risen in the gas phase of partition position, is substantially free of moisture, rises in the gas phase of tower top
Without ethanol and moisture；Liquid header is set to collect dropping liq above dividing plate and import liquid cyclone above dividing plate,
Dividing plate upper liquid is assigned to dividing plate both sides by liquid cyclone；Into methanol stripping side liquid by methanol stripping side rise gas
Moisture in body is cleaned substantially so that methanol stripping side, which is risen in the gas of dividing plate tip position, is substantially free of moisture；Into
The ethanol of ethanol stripping side is progressively enriched with by the liquid of ethanol stripping side to ethanol stripping side tower reactor；Ethanol stripping side reboiler is
Ethanol stripping side provides heat, and the methanol in the dropping liq of ethanol stripping side is stripped out, drops to ethanol stripping side tower reactor
Liquid be the recovery alcohol product for being substantially free of first alcohol and water；Fusel oil is from side take-off near the charging aperture of methanol stripping side.
The tower methanol distillation column of described dividing plate can be thermally integrated with methanol rectification pre-tower, and methanol distillation column top gaseous phase is used for
Heat is provided to methanol rectification pre-tower tower reactor reboiler, the operation energy consumption of whole methanol fractionation system is reduced.
The tower methanol distillation column dividing plate both sides liquid measure relations of distribution of described dividing plate are：Methanol stripping side liquid measure is carried with ethanol
The ratio for evaporating side liquid measure is 1:0.3~5.
The methanol stripping side bottom of the tower methanol distillation column of described dividing plate can without reboiler, using live (open) steam plus
Heat.
The process for the tower methanol distillation column by-product ethanol of dividing plate that the utility model is provided, the tower first of described dividing plate
Alcohol recovery tower can be thermally integrated operation with the miscellaneous equipment in methanol rectification unit, for example to the tower in methanol rectification unit again
Device heating is boiled, or to patterns such as crude carbinol raw material preheatings, reduces the operation energy consumption of whole methanol fractionation system.
The device for the tower methanol distillation column by-product ethanol of dividing plate that the utility model is provided mainly includes：Methanol rectification is pre-
Tower, methanol rectification unit, methanol distillation column, methanol distillation column condenser and connecting pipeline (road).
Described methanol distillation column body lower part sets dividing plate, and methanol distillation column bottom is separated into methanol stripping side by dividing plate
With ethanol stripping side, and both sides are not connected；Methanol stripping side connects methanol rectification unit by feeding line；Methanol stripping side
Reboiler is connected to methanol stripping side bottom, and ethanol stripping side reboiler is connected to ethanol stripping side bottom；Liquid header is set
Put above dividing plate, liquid header and liquid cyclone connection, liquid cyclone connection methanol stripping side and ethanol stripping side；
Fusel oil draws pipeline and is connected to methanol stripping side.
Methanol distillation column top gaseous phase pipeline is connected to methanol rectification pre-tower tower reactor reboiler shell side gas phase entrance, methanol essence
Pre-tower tower reactor reboiler shell side liquid-phase outlet is evaporated to be connected to methanol distillation column overhead reflux mouthful and reclaim methanol product discharging pipeline.
The utility model provides a kind of device of the tower methanol distillation column by-product ethanol of dividing plate, and it is one kind in partitioned column
While interior completion Methanol Recovery process, the process and device of by-product ethanol are realized, the methanol in fusel oil is significantly reduced
And ethanol content, the yield of methanol product is improved, while can by-product alcohol product；Moreover, the tower methanol distillation column of the dividing plate can
It is thermally integrated with methanol rectification pre-tower, reduces the operation energy consumption of whole methanol fractionation system.With significant practicality and economic effect
Benefit, has a extensive future.
Brief description of the drawings
Fig. 1 is a kind of structurally and operationally pattern sketch of methanol distillation column widely used at present.
Fig. 2 is a kind of device sketch for typical tower methanol distillation column by-product ethanol of dividing plate that the utility model is provided.
Fig. 3 is that a kind of of Fig. 2 develops process, and the tower methanol distillation column of dividing plate and pre-tower are thermally integrated operation, and methanol is returned
Receive the tower top methanol steam of tower and provide heat for pre-tower tower reactor reboiler, pre-tower is heated without live steam, be greatly reduced whole
The operation energy consumption of methanol rectification.
Fig. 4 is that a kind of of Fig. 3 develops process, and the methanol stripping side bottom of the tower methanol distillation column of dividing plate without boiling again
Device, using direct steam heating.
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.
Fig. 1 is the widely used typical structure of methanol distillation column and operator scheme in a kind of current methanol rectifying system, slightly
Methanol feedstock 1 is introduced into methanol rectification pre-tower T101, by tower top discharge fixed gas 3 and removing light component 6, the prognosis that tower reactor is obtained
（Methanol industry universal term, refers to after being handled by pre-tower）Crude carbinol 10 enters methanol rectification unit, through methanol rectification list
After member extraction refined methanol product, the essence of methanol rectification unit discharge（Methanol industry universal term, refers to by methanol rectification unit
After reason）Dilute methanol liquid 11 enters in the middle part of methanol distillation column T102, and top gaseous phase 12 is by methanol distillation column condenser E104
Condensed 13 points of lime set is two strands, and one is that phegma 14 is directly returned at the top of methanol distillation column T102；Another burst of conduct is adopted
Go out to be recycled methanol 15.Lateral line withdrawal function fusel oil 16 near methanol distillation column T102 feed entrance points.Tower reactor discharges waste water 20.
A kind of process for the tower methanol distillation column by-product ethanol of dividing plate that the utility model is provided includes：
1）Dividing plate W101 is set in methanol distillation column T103 body lower parts, dividing plate W101 is by part under methanol distillation column T103
Methanol stripping side S101 and ethanol stripping side S102 are divided into, and both sides are not connected；Dilute methanol liquid from methanol rectification unit
Fed by methanol stripping side S101.
2）Methanol distillation column T103 institute's calorific requirements are by being connected to the methanol stripping side reboilers of methanol stripping side S101 bottoms
E103 is provided respectively with the ethanol stripping side reboiler E105 for being connected to ethanol stripping side S102 bottoms.
3）Liquid header C101, liquid cyclone SP101 is set to be connected with liquid header C101 above dividing plate W101,
Dividing plate W101 upper liquids are assigned to dividing plate W101 both sides by liquid cyclone SP101.
4）Recovery methanol product is obtained from methanol distillation column T103 tower tops, recovery second is obtained from ethanol stripping side S102 bottoms
Alcohol product, waste water is discharged from methanol stripping side S101 bottoms, from side take-off methanol near the S101 charging apertures of methanol stripping side and
Ethanol content very low fusel oil.
A kind of process for the tower methanol distillation column by-product ethanol of dividing plate that the utility model is provided, its concrete technology mistake
Cheng Wei：Methanol distillation column T103 bottoms set dividing plate W101, dividing plate W101 that methanol distillation column T103 bottoms are separated into methanol and carried
Side S101 and ethanol stripping side S102 are evaporated, and both sides are not connected.Dilute methanol liquid 11 from methanol rectification unit is carried by methanol
Side S101 chargings are evaporated, methanol stripping side reboiler E103 provides heat for methanol stripping side S101 tower reactors, by methanol stripping side
Methanol, ethanol in S101 dropping liqs are stripped out, and the liquid for dropping to methanol stripping side S101 tower reactors is without methanol, second
The waste water of alcohol, from methanol stripping side tower reactor discharging bottom discharge waste water 20；Methanol distillation column T103 tower tops ascending vapor 12 is through first
Alcohol recovery tower condenser E104 is condensed, and 13 points of condensate is two parts, and a part enters methanol as methanol distillation column phegma 14
Column overhead is reclaimed, another part is produced as methanol 15 is reclaimed；Phegma 14 by the ethanol and moisture in uprising gas in tower by
Step is cleaned, and methanol stripping side S101, which is risen in the gas phase of partition position, is substantially free of moisture, rises in the gas phase 12 of tower top
Without ethanol and moisture；Liquid header C101 is set to collect dropping liq above dividing plate and import liquid above dividing plate W101
Dividing plate W101 upper liquids are assigned to dividing plate W101 both sides by current divider SP101, liquid cyclone SP101；Into methanol stripping
Side S101 liquid 22 cleans the moisture in the S101 uprising gas of methanol stripping side substantially so that methanol stripping side S101 rises
Moisture is substantially free of into the gas of dividing plate W101 tip positions；Liquid 23 into ethanol stripping side S102 is by ethanol stripping side
S102 ethanol is progressively enriched with to ethanol stripping side S102 tower reactors；Ethanol stripping side reboiler E105 is that ethanol stripping side S102 is carried
Heating load, the methanol in the S102 dropping liqs of ethanol stripping side is stripped out, drops to the liquid of ethanol stripping side S102 tower reactors
Body is the recovery alcohol product 27 for being substantially free of first alcohol and water；Fusel oil is adopted from side line near the S101 charging apertures of methanol stripping side
Go out.
The tower methanol distillation column T103 of described dividing plate can be thermally integrated with methanol rectification pre-tower T101, methanol distillation column T103
Top gaseous phase is used to provide heat to methanol rectification pre-tower tower reactor reboiler E101, reduces the operation energy of whole methanol fractionation system
Consumption.
The tower methanol distillation column dividing plate both sides liquid measure relations of distribution of described dividing plate are：Methanol stripping side S101 liquid measures and second
The ratio of alcohol stripping side S102 liquid measures is 1:0.3~5.
The methanol stripping side S101 bottoms of the tower methanol distillation column of described dividing plate can be without reboiler, using directly steaming
Vapour is heated.
The process for the tower methanol distillation column by-product ethanol of dividing plate that the utility model is provided, the tower first of described dividing plate
Alcohol recovery tower T103 can be thermally integrated operation with the miscellaneous equipment in methanol rectification unit, such as to the tower in methanol rectification unit
Reboiler heating, or to patterns such as crude carbinol raw material preheatings, reduce the operation energy consumption of whole methanol fractionation system.
The device for the tower methanol distillation column by-product ethanol of dividing plate that the utility model is provided mainly includes：Methanol rectification pre-tower
T101, methanol rectification unit, methanol distillation column T103, methanol distillation column condenser E104 and connecting pipeline (road).
Described methanol distillation column T103 body lower parts set dividing plate W101, and dividing plate W101 is by methanol distillation column T103 bottoms
Methanol stripping side S101 and ethanol stripping side S102 are separated into, and both sides are not connected；Methanol stripping side S101 passes through feed pipe
Line connects methanol rectification unit；Methanol stripping side reboiler E101 is connected to methanol stripping side S101 bottoms, and ethanol stripping side is again
Boiling device E105 is connected to ethanol stripping side S102 bottoms；Liquid header C101 is arranged on above dividing plate W101, liquid header
C101 and liquid cyclone SP101 connections, liquid cyclone SP101 connection methanol stripping side S101 and ethanol stripping side S102；
Fusel oil draws pipeline and is connected to methanol stripping side S101.
Methanol distillation column T103 top gaseous phase pipelines are connected to methanol rectification pre-tower T101 tower reactor reboiler E101 shell side gas
Phase entrance, methanol rectification pre-tower T101 tower reactor reboiler E101 shell side liquid-phase outlets are connected to methanol distillation column T103 overhead refluxes
Mouth and recovery methanol product discharging pipeline.
Embodiment 1：
As shown in Fig. 2 crude carbinol raw material 1 is introduced into methanol rectification pre-tower T101, it is light by tower top discharge fixed gas 3 and removing
Component 6, the prognosis crude carbinol 10 that tower reactor is obtained enters methanol rectification unit, and refined methanol product, first are produced through methanol rectification unit
Dilute methanol liquid 11 enters methanol distillation column T103 after the essence of alcohol rectification cell discharge.
Methanol distillation column T103 bottoms set dividing plate W101, dividing plate W101 that methanol distillation column T103 bottoms are separated into methanol
Stripping side S101 and ethanol stripping side S102, and both sides are not connected.
Dilute methanol liquid 11 from methanol rectification unit is fed by methanol stripping side S101, methanol stripping side reboiler E103
Heat is provided for methanol stripping side S101 tower reactors, the methanol in the S101 dropping liqs of methanol stripping side, ethanol are stripped out, under
The liquid for dropping to methanol stripping side S101 tower reactors is the waste water without methanol, ethanol, from methanol stripping side tower reactor discharging bottom row
Go out waste water 20；Methanol distillation column T103 tower tops ascending vapor 12 is condensed through methanol distillation column condenser E104, and 13 points of condensate is
Two parts a, part enters Methanol Recovery column overhead as methanol distillation column phegma 14, and another part is adopted as methanol 15 is reclaimed
Go out；Phegma 14 progressively cleans the ethanol and moisture in uprising gas in tower, and methanol stripping side S101 rises to partition position
Gas phase in be substantially free of moisture, rise in the gas phase 12 of tower top be free of ethanol and moisture；Liquid is set above dividing plate W101
Dropping liq above dividing plate is collected and imports liquid cyclone SP101 by collector C101, and liquid cyclone SP101 is by dividing plate
W101 upper liquids are assigned to dividing plate W101 both sides；Liquid 22 into methanol stripping side S101 rises methanol stripping side S101
Moisture in gas is cleaned substantially so that methanol stripping side S101, which is risen in the gas of dividing plate W101 tip positions, to be substantially free of
Moisture；Into ethanol stripping side S102 liquid 23 by ethanol stripping side S102 ethanol progressively to ethanol stripping side S102 tower reactors
Enrichment；Ethanol stripping side reboiler E105 provides heat for ethanol stripping side S102, by the S102 dropping liqs of ethanol stripping side
Methanol be stripped out, the liquid for dropping to ethanol stripping side S102 tower reactors is the recovery alcohol product for being substantially free of first alcohol and water
27；Fusel oil is from side take-off near the S101 charging apertures of methanol stripping side.
The ratio of methanol distillation column T103 methanol strippings side S101 liquid measures and ethanol stripping side S102 liquid measures is 1:0.3~5.
By taking 1,000,000 tons/year of natural gas U.S. federal standard " AA " level methanol devices as an example（Operation hour is small by 8000
When/count in year）, the process and device of the tower methanol distillation column by-product ethanol of dividing plate provided by the utility model（Such as Fig. 2 institutes
Show）With widely used at present Methanol Recovery tower process and device（As shown in Figure 1）, operation energy consumption, product quality, product yield
Contrast as follows Deng major parameter（As shown in table 1）：
Table 1：Process contrast shown in Fig. 1, Fig. 2
As it can be seen from table 1 the technique side of the tower methanol distillation column by-product ethanol of the dividing plate provided using the utility model
Method and device（As shown in Figure 2）In contrast to widely used at present Methanol Recovery tower process and device（As shown in Figure 1）, can be notable
The yield of methanol product is improved, whole methanol fractionation system operation energy consumption is suitable, while can by-product alcohol product.
Relatively current widely used Methanol Recovery tower process and device, the tower methanol of dividing plate that the utility model is provided are returned
The process and device methanol yield for receiving tower by-product ethanol improve 99.3% -98.6%=0.7%.
100 × 10000 × 0.7%=7000 tons relative to annual methanol product output increased.
By 0.3 ten thousand yuan/ton of calculating of methanol product, the increased economic benefit of only this item is：
0.3 × 7000=21,000,000 yuan/year
0.2 ten thousand yuan/ton of calculating of alcohol product are reclaimed, increased economic benefit is：
0.2 × 6400=12,800,000 yuan/year
Three economic benefits of the above add up to yuan/year of 2100+1280=33,800,000.
The process and device of the tower methanol distillation column by-product ethanol of dividing plate provided using the utility model have aobvious
The economic benefit of work.
Embodiment 2：
As shown in figure 3, it, which is a kind of of Fig. 2, develops process, with respect to the process difference shown in Fig. 2 such as
Under：
Dividing plate tower methanol distillation column T103 and pre-tower T101 is thermally integrated operation, the tower top methanol steam 12 of methanol distillation column
Heat is provided for pre-tower tower reactor reboiler E101,13 points of the condensate of methanol steam 12 is two parts, and one is used as Methanol Recovery
Tower T103 phegmas 14 return to methanol distillation column T103 tower tops, and another strand produces as recovery methanol 15.Pre-tower tower reactor is again
Boil device E101 to heat without live steam, the operation energy consumption of whole methanol rectification is greatly reduced.
By taking 1,000,000 tons/year of natural gas U.S. federal standard " AA " level methanol devices as an example（Operation hour is small by 8000
When/count in year）, the process and device of the tower methanol distillation column by-product ethanol of dividing plate provided by the utility model（Such as Fig. 3 institutes
Show）With widely used at present Methanol Recovery tower process and device（As shown in Figure 1）, operation energy consumption, product quality, product yield
Contrast as follows Deng major parameter（As shown in table 2）：
Table 2：Process contrast shown in Fig. 1, Fig. 3
The process and device of the tower methanol distillation column by-product ethanol of dividing plate provided using the utility model（Such as Fig. 2
It is shown）In contrast to widely used at present Methanol Recovery tower process and device（As shown in Figure 1）, it is remarkably improved methanol product
Yield, significantly reduces whole methanol fractionation system operation energy consumption, while can by-product alcohol product.
Relatively current widely used Methanol Recovery tower process and device, the tower methanol of dividing plate that the utility model is provided are returned
The process and device methanol yield for receiving tower by-product ethanol improve 99.3% -98.6%=0.7%.
100 × 10000 × 0.7%=7000 tons relative to annual methanol product output increased.
By 0.3 ten thousand yuan/ton of calculating of methanol product, the increased economic benefit of only this item is:
0.3 × 7000=21,000,000 yuan/year
Save steam consumption（71.2 - 36.9）× 8000/10000=27.44 ten thousand tons/year.
By 150 yuan of calculating of steam per ton, steam expense can be saved every year：Yuan/year of 27.44 × 15,0=4,116 ten thousand.
It is 0.8 × 8000=6400 tons/year to reclaim ethanol production
0.2 ten thousand yuan/ton of calculating of alcohol product are reclaimed, increased economic benefit is：
0.2 × 6400=12,800,000 yuan/year.
Three economic benefits of the above add up to yuan/year of 2100+4116+1280=74,960,000.
The process and device of the tower methanol distillation column by-product ethanol of dividing plate provided using the utility model have pole
Its significant economic benefit.
Embodiment 3：
As shown in figure 4, it, which is a kind of of Fig. 3, develops process, with respect to the process difference shown in Fig. 2 such as
Under：
The methanol stripping side S101 bottoms of the tower methanol distillation column of dividing plate are added without using reboiler using live (open) steam 28
Heat.
The utility model provides the process and device of a kind of tower methanol distillation column by-product ethanol of dividing plate, and it is one
While planting the completion Methanol Recovery process in partitioned column, the process and device of by-product ethanol are realized, fusel is significantly reduced
Methanol and ethanol content in oil, are remarkably improved the yield of methanol product, significantly reduce whole methanol fractionation system operation energy
Consumption, at the same can by-product alcohol product, with significant practicality and economic benefit.Illustrated in conjunction with the embodiments, it is related
The method that the personnel in field can provide according to the utility model completely suitably change or change with combining, to realize the skill
Art.It should be strongly noted that it is all these by the technological process that provides the utility model carry out similar changes or
Change and reconfigure, it is apparent to those skilled in the art, it is considered as in spirit of the present utility model, model
Enclose with content.
Claims (1)
1. a kind of device of the tower methanol distillation column by-product ethanol of dividing plate, mainly includes methanol rectification pre-tower（T101）, methanol essence
Evaporate unit, methanol distillation column（T103）, methanol distillation column condenser（E104）And connecting pipeline；It is characterized in that：
Described methanol distillation column（T103）Body lower part sets dividing plate（W101）, dividing plate（W101）By methanol distillation column（T103）
Bottom is separated into methanol stripping side（S101）With ethanol stripping side（S102）, and both sides are not connected；Methanol stripping side（S101）
Methanol rectification unit is connected by feeding line；Methanol stripping side reboiler（E101）It is connected to methanol stripping side（S101）Bottom
Portion, ethanol stripping side reboiler（E105）It is connected to ethanol stripping side（S102）Bottom；Liquid header（C101）Be arranged on every
Plate（W101）Top, liquid header（C101）And liquid cyclone（SP101）Connection, liquid cyclone（SP101）Connect first
Alcohol stripping side（S101）With ethanol stripping side（S102）；Fusel oil draws pipeline and is connected to methanol stripping side（S101）；
Methanol distillation column（T103）Top gaseous phase pipeline is connected to methanol rectification pre-tower（T101）Tower reactor reboiler（E101）Shell side
Gas phase entrance, methanol rectification pre-tower（T101）Tower reactor reboiler（E101）Shell side liquid-phase outlet is connected to methanol distillation column（T103）
Overhead reflux mouthful and recovery methanol product discharging pipeline.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201720046673.XU CN206404352U (en) | 2017-01-16 | 2017-01-16 | The device of the tower methanol distillation column by-product ethanol of dividing plate |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201720046673.XU CN206404352U (en) | 2017-01-16 | 2017-01-16 | The device of the tower methanol distillation column by-product ethanol of dividing plate |
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| Publication Number | Publication Date |
|---|---|
| CN206404352U true CN206404352U (en) | 2017-08-15 |
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| CN201720046673.XU Expired - Fee Related CN206404352U (en) | 2017-01-16 | 2017-01-16 | The device of the tower methanol distillation column by-product ethanol of dividing plate |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106582053A (en) * | 2017-01-16 | 2017-04-26 | 天津市新天进科技开发有限公司 | Ethanol by-production process method and apparatus for partition plate tower type methanol recovery tower |
-
2017
- 2017-01-16 CN CN201720046673.XU patent/CN206404352U/en not_active Expired - Fee Related
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106582053A (en) * | 2017-01-16 | 2017-04-26 | 天津市新天进科技开发有限公司 | Ethanol by-production process method and apparatus for partition plate tower type methanol recovery tower |
| CN106582053B (en) * | 2017-01-16 | 2019-06-14 | 天津市新天进科技开发有限公司 | The process and device of the tower methanol distillation column by-product ethyl alcohol of partition |
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