CN206986063U - A kind of system that refined methanol and absolute ethyl alcohol are extracted from crude carbinol - Google Patents
A kind of system that refined methanol and absolute ethyl alcohol are extracted from crude carbinol Download PDFInfo
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- CN206986063U CN206986063U CN201720739850.2U CN201720739850U CN206986063U CN 206986063 U CN206986063 U CN 206986063U CN 201720739850 U CN201720739850 U CN 201720739850U CN 206986063 U CN206986063 U CN 206986063U
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Abstract
A kind of system that refined methanol and absolute ethyl alcohol are extracted from crude carbinol is the utility model is related to, periodic off-gases scrubbing tower, pre-rectifying tower, compression rectification tower, atmospheric distillation tower, recovery tower, fusel oil rectifier, membrane filtration dewatering system, methanol distillation column and Ethanol rectification column are sequentially connected in system.The utility model has the characteristics of energy-conservation, efficient, and the utility model can improve the added value of ammonia from coal device to greatest extent, have significant economic benefit and social benefit.
Description
Technical field
A kind of system that refined methanol and absolute ethyl alcohol are extracted from crude carbinol is the utility model is related to, belongs to ammonia from coal
Technical field.
Background technology
It is general that refined methanol is obtained using the rectification process of crude carbinol during ammonia from coal.Typically adopted in conventional apparatus
Crude carbinol rectifying is carried out with three towers or four towers, so in addition to refined methanol is obtained, also obtains the very high rectifying accessory substance of water content,
The accessory substance contains a certain amount of methanol simultaneously.The very high rectifying accessory substance poor quality of water content, can not directly be applied, if directly
Run in put and will result in environmental pollution, cost of sewage disposal can be increased again by being discharged to sewage disposal process, and content of organics is high
Deal with and difficult.
The content of the invention
The utility model provides a kind of system that refined methanol and absolute ethyl alcohol are extracted from crude carbinol, the utility model,
Fusel oil can be made to get utilization, reduced environmental pollution, the utility model significantly improves the warp of ammonia from coal device
Help benefit and social benefit, solving the higher rectifying accessory substance of water content that traditional rectification process obtains can not recycling
Problem.The technical solution of the utility model is as follows：
A kind of technique that refined methanol and absolute ethyl alcohol are extracted from crude carbinol, is comprised the following steps that：
（1）Crude carbinol enters pre-rectifying tower after heat exchanger A heat exchange, and the overhead components of pre-rectifying tower exchange heat through heat exchanger B
Afterwards, gas phase portion enters periodic off-gases scrubbing tower, and gas phase portion contains substantial amounts of methanol, into periodic off-gases scrubbing tower recovery gas phase portion
Methanol in point, liquid phase part enter backflash A, the separation of aqueous phase and fusel oil, periodic off-gases scrubbing tower are realized in backflash A
Tower top for fuel gas, bottom of towe component and backflash A bottom component mixing after enter pre-rectifying tower, backflash A top is light
Component is fusel oil, can individually be reclaimed；
The pre-rectifying tower tower top pressure is 139 kPaA, and temperature is 74.8 DEG C；Tower bottom pressure is that 147 kPaA temperature are
77.5 DEG C, reflux ratio 0.92；The temperature of the pressure normal pressure of periodic off-gases scrubbing tower, tower top and bottom of towe is normal temperature, and periodic off-gases wash
Desalination water spray system is provided with tower, positioned at gas phase entrance top, desalted water and gaseous component counter current contacting are to wash in gas phase
Methanol.
（2）The bottom of towe component of pre-rectifying tower enters compression rectification tower, pre-rectifying tower and compression rectification after heat exchanger C heat exchange
Tower shares a heat exchanger C；
The tower top pressure of the compression rectification tower is 800 kPaA, and temperature is 128 DEG C；Tower bottom pressure is 813 kPaA, temperature
Spend for 134 DEG C；Reflux ratio is 3.0.
（3）The overhead components of compression rectification tower are divided into two parts after backflash B, and a part exchanges heat laggard through heat exchanger D
Enter compression rectification tower to change through heat exchanger C as industrial methanol finished product, the bottom component of compression rectification tower as backflow, another part
Enter atmospheric distillation tower after heat；
The purpose of overhead reflux allows liquid flux more to absorb the solute in fog, reaches more preferable for more preferable stripping
Vapour-liquid rectification effect；Another part is extracted out and is used as industrial methanol finished product.
（4）The overhead components of atmospheric distillation tower enter backflash C after heat exchanger E heat exchange, the component come out from backflash C
Be divided into three strands, one enter atmospheric distillation tower as overhead reflux, a stock-traders' know-how heat exchanger F heat exchange after be used as industrial methanol finished product,
One enters recovery tower and is discharged into waste water after heat exchanger G heat exchange as overhead reflux, the bottom of towe component of atmospheric distillation tower for waste water
System；
The tower top pressure of the atmospheric distillation tower is 113 kPaA, and temperature is 67.5 DEG C；Tower bottom pressure is 143 kPaA, temperature
Spend for 110 DEG C；Reflux ratio is 1.85.
（5）Enter recovery tower lower end from the component that atmospheric distillation tower comes out through feeder trough, the overhead components of recovery tower enter
Atmospheric distillation tower, bottom of towe component are that waste water is discharged into waste water system after heat exchanger H heat exchange, and the lower end component of recovery tower is through heat exchanger
Enter fusel oil rectifying column after I heat exchange；
The tower top pressure of the recovery tower is 133 kPaA, and temperature is 72 DEG C；Tower bottom pressure is 153 kPaA, and temperature is
111.5℃；Capacity of returns 3100kg/h.
（6）The overhead components of fusel oil rectifier enter backflash D after heat exchanger J heat exchange, go out backflash D component point
For two strands, one returns again to fusel oil rectifier and taken off as aqueous 10% fusel of being less than of overhead reflux, another stock into membrane filtration
Water system, the bottom of towe component of fusel oil rectifier enter waste water system after heat exchanger K heat exchange, and tower lower end another part is through heat exchange
Fusel oil rectifier is returned after device L heat exchange；
The tower top pressure of the fusel oil rectifier is 23 kPaA, and temperature is 99.45 DEG C；Tower bottom pressure is 30 kPaA,
Temperature is 100 DEG C；Reflux ratio is 12-13；Preferably, reflux ratio 12.5.
（7）Most of waste water in membrane filtration dewatering system removing fusel, aqueous 0.5% fusel of being no more than return into methanol
Receive tower；
（8）The overhead components of methanol distillation column are divided into two strands after heat exchanger M and backflash E, and one enters Methanol Recovery
Tower enters atmospheric distillation tower, the bottom of towe group of methanol distillation column together as overhead reflux, the overhead product of another stock and recovery tower
Divide a part to return to methanol distillation column after heat exchanger N heat exchange to flow back as bottom of towe, be partly into Ethanol rectification column as second
The charging of alcohol rectifying column；
The pressure of the methanol distillation column is normal pressure, and tower top temperature is 69 DEG C, and column bottom temperature is 79 DEG C.
（9）The overhead components of Ethanol rectification column enter backflash F after heat exchanger O heat exchange, and the component for going out backflash F is divided into
Two strands, one enters Ethanol rectification column and obtains the absolute ethyl alcohol of high-purity after exchanging heat as overhead reflux, a stock-traders' know-how heat exchanger P,
A bottom of towe component part for Ethanol rectification column returns to Ethanol rectification column after heat exchanger Q heat exchange and flowed back as bottom of towe, another part
Anhydrous C4 fusels are obtained after heat exchanger R heat exchange；
The pressure of the Ethanol rectification column is normal pressure, and tower top temperature is 78.5 DEG C, and column bottom temperature is 83 DEG C.
Pre-rectifying tower described in the utility model, compression rectification tower, atmospheric distillation tower, recovery tower, fusel oil rectifier, first
Alcohol recovery tower and Ethanol rectification column can use plate column or structured packing to add the combination tower of column plate, and preferably structured packing adds tower
The combination tower of plate.
In the utility model, the system of extraction refined methanol and absolute ethyl alcohol from crude carbinol, system includes periodic off-gases and washed
Tower, pre-rectifying tower, compression rectification tower, atmospheric distillation tower, recovery tower, fusel oil rectifier, membrane filtration dewatering system, Methanol Recovery
Tower and Ethanol rectification column；Heat exchanger A is connected by pipeline with pre-rectifying tower, and the tower top of pre-rectifying tower passes through pipeline and heat exchanger B
Connection, heat exchanger B are connected with periodic off-gases scrubbing tower and backflash A respectively by pipeline, the bottom of towe of periodic off-gases scrubbing tower and backflow
Groove A bottom is connected by pipeline with pre-rectifying tower, and pre-rectifying tower bottom of towe is by pipeline through heat exchanger C and compression rectification tower phase
Even, compression rectification tower bottom of towe is connected by pipeline through heat exchanger C with atmospheric distillation tower, and compression rectification column overhead is by pipeline with returning
Chute B connections, backflash B are connected with industrial methanol accumulator tank and heat exchanger D respectively by pipeline, heat exchanger D by pipeline with
Compression rectification tower is connected, and atmospheric distillation column overhead is connected by pipeline with heat exchanger E, and heat exchanger E passes through pipeline and backflash C phases
Even, backflash C is connected with atmospheric distillation tower, recovery tower and heat exchanger F respectively by pipeline, and heat exchanger F passes through pipeline and industry
Methanol accumulator tank is connected, and atmospheric distillation tower bottom of towe is connected by pipeline with heat exchanger G, and atmospheric distillation tower is by pipeline through feeder trough
It is connected with recovery tower, recovery column overhead is connected by pipeline with atmospheric distillation tower, and recovery tower bottom of towe passes through pipeline and heat exchanger H phases
Even, recovery tower is connected by pipeline through heat exchanger I with fusel oil rectifier, and the bottom of towe of fusel oil rectifier passes through pipeline and heat exchange
Device K is connected, and fusel oil rectifier lower end is connected by pipeline with heat exchanger L, and heat exchanger L passes through pipeline and fusel oil rectifier phase
Even, fusel oil rectifying column tower top is connected by pipeline through heat exchanger J with backflash D, backflash D by pipeline respectively with fusel oil
Rectifying column is connected with membrane filtration dewatering system, and membrane filtration dewatering system is connected by pipeline with methanol distillation column, methanol distillation column
Top be connected by pipeline through heat exchanger M with backflash E, backflash E by pipeline respectively with methanol distillation column and atmospheric distillation tower
It is connected, methanol distillation column bottom of towe is connected with heat exchanger N and Ethanol rectification column respectively by pipeline, and heat exchanger N passes through pipeline and first
Alcohol recovery tower is connected, and Ethanol rectification column tower top is connected by pipeline through heat exchanger O with backflash F, and backflash F is distinguished by pipeline
It is connected with Ethanol rectification column and heat exchanger P, heat exchanger P is connected by pipeline with absolute ethyl alcohol accumulator tank, Ethanol rectification column bottom of towe
It is connected respectively with heat exchanger Q and heat exchanger R by pipeline, heat exchanger Q is connected by pipeline with Ethanol rectification column, and heat exchanger R leads to
Piping is connected with anhydrous C4 fusels accumulator tank, and heat exchanger G, heat exchanger H, the bottom of heat exchanger K and membrane filtration dewatering system are equal
It is connected with waste water system.
Further, the membrane filtration dewatering system include feeder trough A, superheater, membrane module, vavuum pump, water storage tank and
Pan tank, the feeder trough A are connected by pipeline through heat exchanger one with superheater, and superheater is connected by pipeline with membrane module,
Membrane module is connected by pipeline through heat exchanger two with water storage tank, and membrane module is connected by pipeline through heat exchanger three with pan tank, water
Storage tank is connected by pipeline with vavuum pump；Preferably, mixed between the membrane module using series, parallel or series and parallel
Mode；The vavuum pump is water-ring vacuum pump；The membrane module is inorganic infiltrating and vaporizing membrane.
The utility model has advantages below compared with prior art：
（1）The multiple products such as refined methanol, absolute ethyl alcohol, fusel oil, anhydrous C4 fusels can be obtained using the utility model,
And fusel oil and anhydrous C4 fusels can be as the blend components of gasoline；
（2）The utility model can make fusel oil get utilization, and reduce environmental pollution, while significantly improve coal
The economic benefit and social benefit of methanol device processed；
（3）The utility model can reclaim the methanol escaped from pre-rectifying tower tower top to greatest extent, and recyclable fusel
Oil.
Brief description of the drawings
Fig. 1 is the utility model process chart；
Fig. 2 is membrane filtration dewatering system flow chart.
Symbol description：
1. periodic off-gases scrubbing tower, 2. pre-rectifying towers, 3. compression rectification towers, 4. atmospheric distillation towers, 5. recovery towers, 6. fusel oil
Rectifying column, 7. membrane filtration dewatering systems, 8. methanol distillation columns, 9. Ethanol rectification columns, 10-27. heat exchangers A-R, 28-33. backflow
Groove A-F, 34. feeder troughs, 35. industrial methanol accumulator tanks, 36. absolute ethyl alcohol accumulator tanks, 37. anhydrous C4 fusels accumulator tanks, 701.
Feeder trough A, 702. superheaters, 703. membrane modules, 704. vavuum pumps, 705. water storage tanks, 706. pan tanks, 707. heat exchangers one,
708. heat exchangers two, 709. heat exchangers three.
Embodiment
The utility model is further described with reference to specific embodiment, and the advantages of the utility model and feature will be with
Description and it is apparent.But embodiment is only exemplary, does not form any restrictions to the scope of the utility model.Ability
Field technique personnel should be understood that can be to the utility model technical side under without departing from spirit and scope of the present utility model
The details and form of case are modified or replaced, but these modifications and replacement are each fallen within the scope of protection of the utility model.
In the utility model, pre-rectifying tower, compression rectification tower, atmospheric distillation tower, recovery tower, fusel oil rectifier, methanol
Recovery tower and Ethanol rectification column are the combination tower that structured packing adds column plate.
A kind of technique that refined methanol and absolute ethyl alcohol are extracted from crude carbinol of embodiment 1
Comprise the following steps that：
（1）Crude carbinol enters pre-rectifying tower 2 after the heat exchange of heat exchanger A 10, and the overhead components of pre-rectifying tower 2 are through heat exchanger B
After 11 heat exchange, gas phase portion enters periodic off-gases scrubbing tower 1, and gas phase portion contains substantial amounts of methanol, returned into periodic off-gases scrubbing tower 1
The methanol in gas phase portion is received, liquid phase part enters backflash A 28, and point of aqueous phase and fusel oil is realized in backflash A 28
From the tower top of, periodic off-gases scrubbing tower 1 to enter pre- rectifying after the bottom component mixing of fuel gas, bottom of towe component and backflash A 28
Tower 2, backflash A 28 top light component is fusel oil, can individually be reclaimed；
（2）The bottom of towe component of pre-rectifying tower 2 enters compression rectification tower 3 after the heat exchange of heat exchanger C 12, pre-rectifying tower 2 and adds
Rectifying column 3 is pressed to share a heat exchanger C 12；
（3）The overhead components of compression rectification tower 3 are divided into two parts after backflash B 29, and a part is changed through heat exchanger D 13
Enter compression rectification tower 3 after heat to pass through as industrial methanol finished product, the bottom component of compression rectification tower 3 as backflow, another part
Heat exchanger C 12 enters atmospheric distillation tower 4 after exchanging heat；
（4）The overhead components of atmospheric distillation tower 4 enter backflash C 30 after the heat exchange of heat exchanger E 14, from backflash C 30
Component out is divided into three strands, and one enters atmospheric distillation tower 4 as conduct after overhead reflux, a stock-traders' know-how heat exchanger F 15 heat exchange
Industrial methanol finished product, one be used as overhead reflux into recovery tower 5, the bottom of towe component of atmospheric distillation tower 4 is waste water through heat exchanger G
Waste water system is discharged into after 16 heat exchange；
（5）Enter the lower end of recovery tower 5, the overhead components of recovery tower 5 from the component that atmospheric distillation tower 4 comes out through feeder trough 34
It is that waste water is discharged into waste water system, the lower end group of recovery tower 5 after the heat exchange of heat exchanger H 17 into atmospheric distillation tower 4, bottom of towe component
Lease making heat exchanger I 18 enters fusel oil rectifying column 6 after exchanging heat；
（6）The overhead components of fusel oil rectifier 6 enter backflash D 31 after the heat exchange of heat exchanger J 19, go out backflash D
31 component is divided into two strands, one return again to fusel oil rectifier 6 as overhead reflux, another stock it is aqueous be less than 10% fusel
Into membrane filtration dewatering system 7, the bottom of towe component of fusel oil rectifier 6 enters waste water system, tower after the heat exchange of heat exchanger K 20
Lower end another part returns to fusel oil rectifier 6 after the heat exchange of heat exchanger L 21；
（7）Membrane filtration dewatering system 7 removes most of waste water in fusel, and aqueous 0.5% fusel of being no more than returns into methanol
Receive tower 8；
（8）The overhead components of methanol distillation column 8 are divided into two strands after heat exchanger M 22 and backflash E 32, and one enters first
Alcohol recovery tower 8 is used as overhead reflux, and the overhead product of another stock and recovery tower 5 enters atmospheric distillation tower 4, methanol distillation column together
A 8 bottom of towe component part returns to methanol distillation column 8 after the heat exchange of heat exchanger N 23 and flowed back as bottom of towe, is partly into ethanol
Charging of the rectifying column 9 as Ethanol rectification column；
（9）The overhead components of Ethanol rectification column 9 enter backflash F 33 after the heat exchange of heat exchanger O 24, go out backflash F 33
Component be divided into two strands, one is used as overhead reflux into Ethanol rectification column 9, is obtained after a stock-traders' know-how heat exchanger P 25 heat exchange high-purity
The absolute ethyl alcohol of degree, a bottom of towe component part for Ethanol rectification column 9 return to the conduct of Ethanol rectification column 9 after the heat exchange of heat exchanger Q 26
Bottom of towe flows back, and another part obtains anhydrous C4 fusels after the heat exchange of heat exchanger R 27.
A kind of technique that refined methanol and absolute ethyl alcohol are extracted from crude carbinol of embodiment 2
Comprise the following steps that：
（1）Crude carbinol enters pre-rectifying tower 2 after the heat exchange of heat exchanger A 10, and the overhead components of pre-rectifying tower 2 are through heat exchanger B
After 11 heat exchange, gas phase portion enters periodic off-gases scrubbing tower 1, and gas phase portion contains substantial amounts of methanol, returned into periodic off-gases scrubbing tower 1
The methanol in gas phase portion is received, liquid phase part enters backflash A 28, and point of aqueous phase and fusel oil is realized in backflash A 28
From the tower top of, periodic off-gases scrubbing tower 1 to enter pre- rectifying after the bottom component mixing of fuel gas, bottom of towe component and backflash A 28
Tower 2, backflash A 28 top light component is fusel oil, can individually be reclaimed；
The tower top pressure of pre-rectifying tower 2 is 139 kPaA, and temperature is 74.8 DEG C；Tower bottom pressure is that 147 kPaA temperature are
77.5 DEG C, reflux ratio 0.92；The temperature of the pressure normal pressure of periodic off-gases scrubbing tower 1, tower top and bottom of towe is normal temperature, and periodic off-gases wash
Desalination water spray system is provided with tower 1, positioned at gas phase entrance top；
（2）The bottom of towe component of pre-rectifying tower 2 enters compression rectification tower 3 after the heat exchange of heat exchanger C 12, pre-rectifying tower 2 and adds
Rectifying column 3 is pressed to share a heat exchanger C 12；
The tower top pressure of the compression rectification tower 3 is 800 kPaA, and temperature is 128 DEG C；Tower bottom pressure is 813 kPaA, temperature
Spend for 134 DEG C；Reflux ratio is 3.0；
（3）The overhead components of compression rectification tower 3 are divided into two parts after backflash B 29, and a part is changed through heat exchanger D 13
Enter compression rectification tower 3 after heat to pass through as industrial methanol finished product, the bottom component of compression rectification tower 3 as backflow, another part
Heat exchanger C 12 enters atmospheric distillation tower 4 after exchanging heat；
（4）The overhead components of atmospheric distillation tower 4 enter backflash C 30 after the heat exchange of heat exchanger E 14, from backflash C 30
Component out is divided into three strands, and one enters atmospheric distillation tower 4 as conduct after overhead reflux, a stock-traders' know-how heat exchanger F 15 heat exchange
Industrial methanol finished product, one be used as overhead reflux into recovery tower 5, the bottom of towe component of atmospheric distillation tower 4 is waste water through heat exchanger G
Waste water system is discharged into after 16 heat exchange；
The tower top pressure of the atmospheric distillation tower 4 is 113 kPaA, and temperature is 67.5 DEG C；Tower bottom pressure is 143 kPaA,
Temperature is 110 DEG C；Reflux ratio is 1.85；
（5）Enter the lower end of recovery tower 5, the overhead components of recovery tower 5 from the component that atmospheric distillation tower 4 comes out through feeder trough 34
It is that waste water is discharged into waste water system, the lower end group of recovery tower 5 after the heat exchange of heat exchanger H 17 into atmospheric distillation tower 4, bottom of towe component
Lease making heat exchanger I 18 enters fusel oil rectifying column 6 after exchanging heat；
The tower top pressure of the recovery tower 5 is 133 kPaA, and temperature is 72 DEG C；Tower bottom pressure is 153 kPaA, and temperature is
111.5℃；Capacity of returns 3100kg/h；
（6）The overhead components of fusel oil rectifier 6 enter backflash D 31 after the heat exchange of heat exchanger J 19, go out backflash D
31 component is divided into two strands, one return again to fusel oil rectifier 6 as overhead reflux, another stock it is aqueous be less than 10% fusel
Into membrane filtration dewatering system 7, the bottom of towe component of fusel oil rectifier 6 enters waste water system, tower after the heat exchange of heat exchanger K 20
Lower end another part returns to fusel oil rectifier 6 after the heat exchange of heat exchanger L 21；
The tower top pressure of the fusel oil rectifier 6 is 23 kPaA, and temperature is 99.45 DEG C；Tower bottom pressure is 30 kPaA,
Temperature is 100 DEG C；Reflux ratio is 12.5；
（7）Membrane filtration dewatering system 7 removes most of waste water in fusel, and aqueous 0.5% fusel of being no more than returns into methanol
Receive tower 8；
（8）The overhead components of methanol distillation column 8 are divided into two strands after heat exchanger M 22 and backflash E 32, and one enters first
Alcohol recovery tower 8 is used as overhead reflux, and the overhead product of another stock and recovery tower 5 enters atmospheric distillation tower 4, methanol distillation column together
A 8 bottom of towe component part returns to methanol distillation column 8 after the heat exchange of heat exchanger N 23 and flowed back as bottom of towe, is partly into ethanol
Charging of the rectifying column 9 as Ethanol rectification column；
The pressure of the methanol distillation column 8 is normal pressure, and tower top temperature is 69 DEG C, and column bottom temperature is 79 DEG C；
（9）The overhead components of Ethanol rectification column 9 enter backflash F 33 after the heat exchange of heat exchanger O 24, go out backflash F 33
Component be divided into two strands, one is used as overhead reflux into Ethanol rectification column 9, is obtained after a stock-traders' know-how heat exchanger P 25 heat exchange high-purity
The absolute ethyl alcohol of degree, a bottom of towe component part for Ethanol rectification column 9 return to the conduct of Ethanol rectification column 9 after the heat exchange of heat exchanger Q 26
Bottom of towe flows back, and another part obtains anhydrous C4 fusels after the heat exchange of heat exchanger R 27；
The pressure of the Ethanol rectification column 9 is normal pressure, and tower top temperature is 78.5 DEG C, and column bottom temperature is 83 DEG C.
A kind of system that refined methanol and absolute ethyl alcohol are extracted from crude carbinol of embodiment 3
As illustrated in fig. 1 and 2, system include periodic off-gases scrubbing tower 1, pre-rectifying tower 2, compression rectification tower 3, atmospheric distillation tower 4,
Recovery tower 5, fusel oil rectifier 6, membrane filtration dewatering system 7, methanol distillation column 8 and Ethanol rectification column 9；Heat exchanger A 10 passes through
Pipeline is connected with pre-rectifying tower 2, and the tower top of pre-rectifying tower 2 is connected by pipeline with heat exchanger B 11, and heat exchanger B 11 passes through pipe
Road is connected with periodic off-gases scrubbing tower 1 and backflash A 28 respectively, and the bottom of towe of periodic off-gases scrubbing tower 1 and backflash A 28 bottom lead to
Piping is connected with pre-rectifying tower 2, and the bottom of towe of pre-rectifying tower 2 is connected by pipeline through heat exchanger C 12 with compression rectification tower 3, pressurization
The bottom of towe of rectifying column 3 is connected by pipeline through heat exchanger C12 with atmospheric distillation tower 4, and the tower top of compression rectification tower 4 passes through pipeline and backflow
Groove B 29 is connected, and backflash B 29 is connected with industrial methanol accumulator tank 35 and heat exchanger D 13 respectively by pipeline, heat exchanger D
13 are connected by pipeline with compression rectification tower 3, and the tower top of atmospheric distillation tower 4 is connected by pipeline with heat exchanger E 14, heat exchanger E
14 are connected by pipeline with backflash C 30, backflash C 30 by pipeline respectively with atmospheric distillation tower 4, recovery tower 5 and heat exchange
Device F 15 is connected, and heat exchanger F 15 is connected by pipeline with industrial methanol accumulator tank 35, the bottom of towe of atmospheric distillation tower 4 by pipeline and
Heat exchanger G 16 is connected, and atmospheric distillation tower 4 is connected by pipeline through feeder trough 34 with recovery tower 5, and the tower top of recovery tower 5 passes through pipeline
It is connected with atmospheric distillation tower 4, the bottom of towe of recovery tower 5 is connected by pipeline with heat exchanger H 17, and recovery tower 5 is by pipeline through heat exchanger
I 18 is connected with fusel oil rectifier 6, and the bottom of towe of fusel oil rectifier 6 is connected by pipeline with heat exchanger K 20, fusel olein
Evaporate the lower end of tower 6 by pipeline with heat exchanger L 21 to be connected, heat exchanger L 21 is connected by pipeline with fusel oil rectifier 6, fusel
The tower top of oil rectifier 6 is connected by pipeline through heat exchanger J 19 with backflash D 31, backflash D 31 by pipeline respectively with it is miscellaneous
Alcohol oil rectifier 6 is connected with membrane filtration dewatering system 7, and membrane filtration dewatering system 7 is connected by pipeline with methanol distillation column 8, first
Alcohol recovery tower 8 top is connected by pipeline through heat exchanger M 22 with backflash E 32, backflash E 32 by pipeline respectively with methanol
Recovery tower 8 and atmospheric distillation tower 4 are connected, the bottom of towe of methanol distillation column 8 by pipeline respectively with heat exchanger N 23 and Ethanol rectification column 9
It is connected, heat exchanger N 23 is connected by pipeline with methanol distillation column 8, and the tower top of Ethanol rectification column 9 is by pipeline through heat exchanger O 24
It is connected with backflash F 33, backflash F 33 is connected with Ethanol rectification column 9 and heat exchanger P 25 respectively by pipeline, heat exchanger P
25 are connected by pipeline with absolute ethyl alcohol accumulator tank 36, and the bottom of towe of Ethanol rectification column 9 is by pipeline respectively with heat exchanger Q 26 and changing
Hot device R 27 is connected, and heat exchanger Q 26 is connected by pipeline with Ethanol rectification column 9, and heat exchanger R 27 is miscellaneous by pipeline and anhydrous C4
Alcohol accumulator tank 37 connects, heat exchanger G 16, heat exchanger H 17, heat exchanger K 20 and membrane filtration dewatering system 7 bottom with it is useless
Water system is connected.
A kind of system that refined methanol and absolute ethyl alcohol are extracted from crude carbinol of embodiment 4
On the basis of embodiment 3, as depicted in figs. 1 and 2, the membrane filtration dewatering system 7 includes feeder trough A701, mistake
Hot device 702, membrane module 703, water-ring vacuum pump 704, water storage tank 705 and pan tank 706, the feeder trough A 701 pass through pipe
Road is connected through heat exchanger 1 with superheater 702, and superheater 702 is connected by pipeline with membrane module 703, and membrane module 703 passes through
Pipeline is connected through heat exchanger 2 708 with water storage tank 705, and membrane module 703 is by pipeline through heat exchanger 3 709 and the phase of pan tank 706
Even, water storage tank 705 is connected by pipeline with water-ring vacuum pump 704, and parallel way is used between the membrane module 703；It is described
Membrane module 703 is inorganic infiltrating and vaporizing membrane.
Claims (7)
1. a kind of system that refined methanol and absolute ethyl alcohol are extracted from crude carbinol, it is characterised in that system is washed including periodic off-gases
Tower, pre-rectifying tower, compression rectification tower, atmospheric distillation tower, recovery tower, fusel oil rectifier, membrane filtration dewatering system, Methanol Recovery
Tower and Ethanol rectification column；Heat exchanger A is connected by pipeline with pre-rectifying tower, and the tower top of pre-rectifying tower passes through pipeline and heat exchanger B
Connection, heat exchanger B are connected with periodic off-gases scrubbing tower and backflash A respectively by pipeline, the bottom of towe of periodic off-gases scrubbing tower and backflow
Groove A bottom is connected by pipeline with pre-rectifying tower, and pre-rectifying tower bottom of towe is by pipeline through heat exchanger C and compression rectification tower phase
Even, compression rectification tower bottom of towe is connected by pipeline through heat exchanger C with atmospheric distillation tower, and compression rectification column overhead is by pipeline with returning
Chute B connections, backflash B are connected with industrial methanol accumulator tank and heat exchanger D respectively by pipeline, heat exchanger D by pipeline with
Compression rectification tower is connected, and atmospheric distillation column overhead is connected by pipeline with heat exchanger E, and heat exchanger E passes through pipeline and backflash C phases
Even, backflash C is connected with atmospheric distillation tower, recovery tower and heat exchanger F respectively by pipeline, and heat exchanger F passes through pipeline and industry
Methanol accumulator tank is connected, and atmospheric distillation tower bottom of towe is connected by pipeline with heat exchanger G, and atmospheric distillation tower is by pipeline through feeder trough
It is connected with recovery tower, recovery column overhead is connected by pipeline with atmospheric distillation tower, and recovery tower bottom of towe passes through pipeline and heat exchanger H phases
Even, recovery tower is connected by pipeline through heat exchanger I with fusel oil rectifier, and the bottom of towe of fusel oil rectifier passes through pipeline and heat exchange
Device K is connected, and fusel oil rectifier lower end is connected by pipeline with heat exchanger L, and heat exchanger L passes through pipeline and fusel oil rectifier phase
Even, fusel oil rectifying column tower top is connected by pipeline through heat exchanger J with backflash D, backflash D by pipeline respectively with fusel oil
Rectifying column is connected with membrane filtration dewatering system, and membrane filtration dewatering system is connected by pipeline with methanol distillation column, methanol distillation column
Top be connected by pipeline through heat exchanger M with backflash E, backflash E by pipeline respectively with methanol distillation column and atmospheric distillation tower
It is connected, methanol distillation column bottom of towe is connected with heat exchanger N and Ethanol rectification column respectively by pipeline, and heat exchanger N passes through pipeline and first
Alcohol recovery tower is connected, and Ethanol rectification column tower top is connected by pipeline through heat exchanger O with backflash F, and backflash F is distinguished by pipeline
It is connected with Ethanol rectification column and heat exchanger P, heat exchanger P is connected by pipeline with absolute ethyl alcohol accumulator tank, Ethanol rectification column bottom of towe
It is connected respectively with heat exchanger Q and heat exchanger R by pipeline, heat exchanger Q is connected by pipeline with Ethanol rectification column, and heat exchanger R leads to
Piping is connected with anhydrous C4 fusels accumulator tank, and heat exchanger G, heat exchanger H, the bottom of heat exchanger K and membrane filtration dewatering system are equal
It is connected with waste water system.
2. system according to claim 1, it is characterised in that the membrane filtration dewatering system includes feeder trough A, overheat
Device, membrane module, vavuum pump, water storage tank and pan tank, the feeder trough A are connected by pipeline through heat exchanger one with superheater, mistake
Hot device is connected by pipeline with membrane module, and membrane module is connected by pipeline through heat exchanger two with water storage tank, and membrane module passes through pipeline
It is connected through heat exchanger three with pan tank, water storage tank is connected by pipeline with vavuum pump.
3. system according to claim 2, it is characterised in that series, parallel or series connection are used between the membrane module
The mode of parallel connection mixing.
4. system according to claim 2, it is characterised in that the vavuum pump is water-ring vacuum pump.
5. system according to claim 2, it is characterised in that the membrane module is inorganic infiltrating and vaporizing membrane.
6. system according to claim 1, it is characterised in that the pre-rectifying tower, compression rectification tower, atmospheric distillation tower,
Recovery tower, fusel oil rectifier, methanol distillation column and Ethanol rectification column add the compound of column plate using plate column or structured packing
Tower.
7. system according to claim 6, it is characterised in that the pre-rectifying tower, compression rectification tower, atmospheric distillation tower,
Recovery tower, fusel oil rectifier, methanol distillation column and Ethanol rectification column are the combination tower that structured packing adds column plate.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201720739850.2U CN206986063U (en) | 2017-06-23 | 2017-06-23 | A kind of system that refined methanol and absolute ethyl alcohol are extracted from crude carbinol |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201720739850.2U CN206986063U (en) | 2017-06-23 | 2017-06-23 | A kind of system that refined methanol and absolute ethyl alcohol are extracted from crude carbinol |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN206986063U true CN206986063U (en) | 2018-02-09 |
Family
ID=61398928
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201720739850.2U Active CN206986063U (en) | 2017-06-23 | 2017-06-23 | A kind of system that refined methanol and absolute ethyl alcohol are extracted from crude carbinol |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN206986063U (en) |
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2017
- 2017-06-23 CN CN201720739850.2U patent/CN206986063U/en active Active
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Address after: 010321 Dalu New District, Zhungeer banner, Ordos City, Inner Mongolia Autonomous Region Patentee after: Inner Mongolia Jiutai New Material Technology Co.,Ltd. Address before: 010321 Dalu New District, Ordos City, Inner Mongolia Autonomous Region Patentee before: JIUTAI ENERGY INNER MONGOLIA Co.,Ltd. |
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