CN104945213B - Negative pressure drying process for drying tower - Google Patents
Negative pressure drying process for drying tower Download PDFInfo
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- CN104945213B CN104945213B CN201410318094.7A CN201410318094A CN104945213B CN 104945213 B CN104945213 B CN 104945213B CN 201410318094 A CN201410318094 A CN 201410318094A CN 104945213 B CN104945213 B CN 104945213B
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- drying tower
- tower
- drying
- negative pressure
- hexamethylene
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Abstract
The invention belongs to the technical field of cyclohexanone production process in chemical industry and in particular relates to a negative pressure drying process for a drying tower. The negative pressure drying process for the drying tower has the advantages that evaporation, condensation and reflux are carried out, so that water content of cyclohexane is reduced, and recovery rate of cyclohexane is also increased; technological operation is simple, technological indexes can be easily controlled, safety and reliability are realized, recovery rate of cyclohexane in the drying tower is increased and water removal effect is improved after the negative pressure drying process for the drying tower is adopted, especially the condition that a large amount of low-pressure steam is discharged out is avoided, medium pressure steam with high thermal energy is saved, and steam resource is effectively recycled.
Description
(1) technical field
The present invention relates to a kind of drying tower negative pressure drying technique, belong to chemical industry and produce cyclohexanone production process technology neck
Territory.
(2) background technology
Existing chemical enterprise needs mostly to have built a lot of chemical industry equipment to produce, and such as CFBB, follows
Circulation fluidized bed boiler all can produce a certain amount of steam due to synthesis ammonia, dust technology, concentrated nitric acid etc. in chemical process, for
Effectively utilizing heat energy, increase flue gas waste heat recovery project, this project also can produce a certain amount of low-pressure steam, but existing
Device and new device cannot be fully utilized, have some residual steam to need directly and empty air, cause substantial amounts of energy waste,
The low-pressure steam power & light company that Chemical Manufacture needs simultaneously can not directly feed, and needs again to increase reducing-and-cooling plant and pipe
Line, one-time investment is bigger, and the loss of heat energy conversion simultaneously is the biggest, does not meets the principle of economical production.
(3) summary of the invention
The present invention is in order to make up the defect of prior art, it is provided that one makes up the thermally equilibrated deficiency of existing production, reduces
The tower pressure of drying tower, tower temperature, improve the yield of hexamethylene and reduce the drying tower negative pressure drying work of the problems such as hexamethylene water content
Skill.
The present invention is achieved through the following technical solutions:
A kind of drying tower negative pressure drying technique, with low-pressure steam as processing object, it is characterised in that: produced by extraction tower top
Product are entered drying tower by middle and upper part, and the thick ketone containing 1% moisture that dehydrogenation unit is come is entered drying tower in the middle part of extraction tower,
This condition of negative pressure by the hexamethylene in extraction tower overhead product, residual moisture and dehydrogenation come thick ketone in containing 1% moisture by doing
Remove at dry column overhead；Through drying tower condenser, drying tower cooler, the vapor condensation of drying tower tower top is become liquid, then warp
Swirl separator separation moisture content, anhydrous hexamethylene by swirl separator top exit deliver to be dried tower top return stream, its flow
Being 2～5m*3/h, FPV regulate, the aqueous hexamethylene of last swirl separator outlet at bottom returns through FR2 effusion meter, drying tower
After the regulation of chute Liquid level adjusting valve, it is sent to hexamethylene condensation liquid bath.
Wherein:
Described low-pressure steam introduces drying tower vacuum equipment by valve A, makes drying tower form negative pressure.
Described low-pressure steam introduces drying tower reboiler by valve B, it is provided that the temperature required for drying tower.
The present invention through pervaporation, condense, refluxing not only reduces hexamethylene water amount, also improves the recovery of hexamethylene
Rate, per hour can steam saving 9 tons, by 150 yuan per ton, 8000 hours calculate, economic benefit 10,800,000 yuan can be increased every year.
The invention has the beneficial effects as follows: technological operation is simple, and technic index is easy to control, safe and reliable, after using this technique
Improve the response rate and the water removal effect of drying tower hexamethylene, particularly solve the situation of low-pressure steam outer row in a large number, save
The middle pressure steam of high heat energy, efficient recovery steam resource.
(4) accompanying drawing explanation
The present invention is further illustrated below in conjunction with the accompanying drawings.
Accompanying drawing 1 is present invention process schematic flow sheet；
Accompanying drawing 2 is valve A position partial enlarged drawing；
Accompanying drawing 3 is valve B position partial enlarged drawing.
In figure: 1, drying tower；2, drying tower condenser；3, drying tower cooler；4, drying tower backflash；5, drying tower is true
Empty device；6, drying tower reboiler；7, drying tower reflux pump；8, valve A；9, valve B.
Detailed description of the invention
Accompanying drawing is the specific embodiment of the present invention.
Drying tower negative pressure drying technique of the present invention as shown in Figure 1, Figure 2 and Figure 3, utilizes remaining low-pressure steam to lead to respectively
Cross valve A8, valve B9 is introduced directly into drying tower vacuum equipment 5 and drying tower reboiler 6, by controlling valve A8 and drying tower
Vacuum equipment 5 reaches the negative pressure pressure required for drying tower 1 and tower temperature, and extraction overhead product is entered drying tower 1 by middle and upper part,
The thick ketone containing 1% moisture that dehydrogenation unit is come enters drying tower 1 from extraction tower center, at this condition of negative pressure by extraction tower tower
In the thick ketone that hexamethylene, residual moisture and dehydrogenation in the product of top comes, the moisture containing 1% is removed by drying tower 1 tower top, through dry
The vapor condensation of drying tower 1 tower top is become liquid, condensed fluid to converge after being cooled with circulating water by dry tower condenser 2, drying tower cooler 3
Collection is to drying tower backflash 4, and drying tower reflux pump 7 is delivered to swirl separator, through swirl separator separation moisture content, anhydrous
Hexamethylene is delivered to drying tower 1 top by swirl separator top exit and is returned stream, flow 2～5m*3/h, FPV regulate, and whirlpool divides
From the aqueous hexamethylene of device outlet at bottom after FR2 effusion meter, the regulation of drying tower backflash 4 Liquid level adjusting valve, it is sent to hexamethylene
Condensation liquid bath, this not only reduces hexamethylene water amount through evaporating, condense, reflux, and also improves the response rate of hexamethylene.
Claims (1)
1. a drying tower negative pressure drying technique, with low-pressure steam as processing object, it is characterised in that: described low-pressure steam leads to
Cross valve A(8) introduce drying tower vacuum equipment (5), make drying tower (1) form negative pressure, by valve B(9) introduce drying tower again
Boiling device (6), it is provided that the temperature required for drying tower (1), by the extraction tower overhead product in cyclohexanone production process by middle and upper part
Place enters drying tower (1), and the thick ketone containing 1% moisture that dehydrogenation unit is come enters drying tower (1), at this condition of negative pressure from middle part
By the hexamethylene in extraction tower overhead product, residual moisture and dehydrogenation come thick ketone in containing 1% moisture by drying tower (1) tower
Remove at top；Through drying tower condenser (2), drying tower cooler (3), the vapor condensation of drying tower (1) tower top is become liquid,
Again through swirl separator separation moisture content, anhydrous hexamethylene is delivered to drying tower (1) tower top by swirl separator top exit and is returned
Stream, its flow is 2～5m3/ h, is regulated by voltage transmitter, and the aqueous hexamethylene of last swirl separator outlet at bottom is through FR2
After the regulation of effusion meter, drying tower backflash (4) Liquid level adjusting valve, it is sent to hexamethylene condensation liquid bath.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201410318094.7A CN104945213B (en) | 2014-07-07 | 2014-07-07 | Negative pressure drying process for drying tower |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201410318094.7A CN104945213B (en) | 2014-07-07 | 2014-07-07 | Negative pressure drying process for drying tower |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN104945213A CN104945213A (en) | 2015-09-30 |
| CN104945213B true CN104945213B (en) | 2017-01-11 |
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ID=54160351
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201410318094.7A Active CN104945213B (en) | 2014-07-07 | 2014-07-07 | Negative pressure drying process for drying tower |
Country Status (1)
| Country | Link |
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| CN (1) | CN104945213B (en) |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1681759A (en) * | 2002-09-12 | 2005-10-12 | 因维斯塔技术有限公司 | Process for oxidation of cyclohexane |
| CN101465070A (en) * | 2009-01-05 | 2009-06-24 | 南京化工职业技术学院 | Synthetic real training device for chemical industry operation |
| CN103055660A (en) * | 2013-01-15 | 2013-04-24 | 山东吉安化工有限公司 | Method and system for treating cyclohexane oxidation tail gas |
-
2014
- 2014-07-07 CN CN201410318094.7A patent/CN104945213B/en active Active
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1681759A (en) * | 2002-09-12 | 2005-10-12 | 因维斯塔技术有限公司 | Process for oxidation of cyclohexane |
| CN101465070A (en) * | 2009-01-05 | 2009-06-24 | 南京化工职业技术学院 | Synthetic real training device for chemical industry operation |
| CN103055660A (en) * | 2013-01-15 | 2013-04-24 | 山东吉安化工有限公司 | Method and system for treating cyclohexane oxidation tail gas |
Non-Patent Citations (1)
| Title |
|---|
| "环己酮装置废碱液分离技术的工业应用";周萍 等;《石油炼制与化工》;20080630;第39卷(第6期);18-21 * |
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| Publication number | Publication date |
|---|---|
| CN104945213A (en) | 2015-09-30 |
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Effective date of registration: 20161011 Address after: 274700 coalification Industrial Zone, Yuncheng, Shandong, Heze Applicant after: Shandong Yong Chi Chemical Co., Ltd. Address before: 274700 coalification Industrial Zone, Yuncheng County, Heze, Shandong Province Applicant before: Shandong Hongda Chemical Co., Ltd. |
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