CN105646146A - Propyl alcohol-triethylamine azeotropic mixture extraction and rectification method - Google Patents
Propyl alcohol-triethylamine azeotropic mixture extraction and rectification method Download PDFInfo
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- CN105646146A CN105646146A CN201610026621.6A CN201610026621A CN105646146A CN 105646146 A CN105646146 A CN 105646146A CN 201610026621 A CN201610026621 A CN 201610026621A CN 105646146 A CN105646146 A CN 105646146A
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
- C07C29/74—Separation; Purification; Use of additives, e.g. for stabilisation
- C07C29/76—Separation; Purification; Use of additives, e.g. for stabilisation by physical treatment
- C07C29/80—Separation; Purification; Use of additives, e.g. for stabilisation by physical treatment by distillation
- C07C29/84—Separation; Purification; Use of additives, e.g. for stabilisation by physical treatment by distillation by extractive distillation
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C209/00—Preparation of compounds containing amino groups bound to a carbon skeleton
- C07C209/82—Purification; Separation; Stabilisation; Use of additives
- C07C209/86—Separation
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
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- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
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Abstract
The invention provides a propyl alcohol-triethylamine azeotropic mixture extraction and rectification method. The propyl alcohol-triethylamine azeotropic mixture extraction and rectification method comprises a normal-pressure continuous operation mode or a normal-pressure intermittent operation mode, various extraction agents are selected to obtain a high-purity propyl alcohol and triethylamine product, and the extraction agents can be recycled. The method is characterized in that traditional solvents are used in extraction, mixed extraction agents composed of the traditional solvents and ionic liquid are also adopted, advantages in the aspects of energy consumption, environment pressure and product purity are huge, the method is particularly suitable for large-scale industrial application, especially for separation of a propyl alcohol-triethylamine azeotropic system, and the method fills in existing technical gaps.
Description
Technical field
Separation method provided by the present invention is directed to propanol-triethylamine azeotropic system, it is respectively adopted the mixed solvent of ethylene glycol, N-METHYLFORMAMIDE and ethylene glycol and ionic liquid composition as extractant, belongs to the extraction rectifying method of propanol-triethylamine azeotropic system.
Background technology
The raw material related in the present invention is propanol and triethylamine, both common in chemical industry material. Propanol (C3H8O), it is important chemical products and raw material, as solvent and for pharmacy, paint and cosmetics etc. Also act as the antibacterial of fuel oil, pesticide and medical material, perfume base. Triethylamine (C6H15N), have another name called: N, N-diethyl ethanamine, triethylamine, organic synthesis industry can be used as solvent, catalyst and raw material. Triethylamine can be used to special solvent, enamel anti-hardening agent, acid binding agent, surfactant, preservative, antibacterial, ion exchange resin, dyestuff, spice, medicine, high-energy fuel and the liquid rocket propellant etc. of producing in the catalyst of phosgenation Merlon, the polymerization inhibitor of tetrafluoroethene, thiofide, paint stripper.
Propanol and triethylamine not only have important application at petrochemical industry, and also have inside other industry and quite use widely. But there is azeotropism in two kinds of materials so that the difficulty separating both is greatly increased. For the recovery of organic solvent, industrial widely used be the processing mode of distillation or rectification, but for azeotropic system, what domestic employing was more is azeotropic distillation method. But azeotropic distillation has the limitation of himself: in energy consumption, cost relatively additive method is higher, in equipment investment, also tends to relatively additive method bigger, and product purity is difficult to ensure that.
In the separation method that chemical industry is conventional, rectification becomes the selection of numerous enterprises with the advantage of himself, but rectification means that and needs energy consumption, and therefore energy consumption cost also becomes the problem that enterprise needs emphasis to consider. In conjunction with country " 13 " planning and presently relevant industrial policy, energy-conservation, reduction of discharging becomes the most important thing of the chemical enterprise coming years. The present invention adopts extraction rectification technique, compared with tradition azeotropic distillation, energy consumption problem significantly improves, and product purity is higher. The extractant adopted in the present invention, is no longer simple organic solvent, but selects the mixed extractant of organic solvent and ionic liquid composition, it is possible to substantially reduce the loss of extractant.
Ionic liquid refers to the salt compounds being at room temperature in a liquid state being made up of organic cation and anion, have that steam forces down, fusing point is low, liquid journey width, easily operation, solubility is good and stablizes advantages of higher, although ionic liquid has numerous advantages, but owing to existing market is expensive, and the large usage quantity of extractant, causing that production cost is very high, therefore utilization rate is relatively low. Research worker finds, ionic liquid can form new ionic liquid with complexant, can effectively reduce the cost of industrial applications, and the advantage simultaneously having both concurrently, conventional complexant has ethylene glycol, glycerol etc., the complexant that the present invention selects is ethylene glycol, forms mixed solvent with ionic liquid.
Advantage based on ionic liquid, rectification process can use the conventional organic solvents mixed liquor with ionic liquid as extractant, (ionic liquid is non-volatile, loss rate is extremely low can to effectively reduce the loss of conventional solvent, and recycle), reduce production cost, product quality can be improved simultaneously.
Existing azeotropic system separation means is divided into two classes substantially: azeotropic distillation and extracting rectifying. Extracting rectifying in product purity, energy consumption relatively azeotropic distillation there is advantage. And at present in the selection of extractant, substantially adopt conventional solvent as extractant in other words directly adopt ion liquid abstraction agent, CN103193590A continuous extraction separation mixed alcohol-method of water, CN102627556A separation of extractive distillation Ethyl formate-alcohol-water technique all adopt ethylene glycol to make extractant; The method of CN103193590A ion liquid abstraction rectification separation Acetic Acid-Water uses ionic liquid as extractant. The former is low on extraction efficiency, and the latter is then much bigger in cost of investment. Sum it up, how to reduce loss of extractant and production cost, raising product purity are the problems that current rectification process needs solution badly.
Currently, with respect to the separation of propanol-triethylamine azeotropic system, not relevant document is delivered or reports.
Summary of the invention
The invention aims to overcome the deficiency existed in existing technique, and for propanol-triethylamine azeotropic system, it is proposed to a kind of good separating effect, product purity are high, energy consumption is low, and extractant easily reclaims, is prone to industrialized separation method. By T-x-y phasor, it can be seen that propanol-triethylamine exists azeotropism (it can be seen that propanol-triethylamine exists azeotropic point in accompanying drawing 1).
For solving above-mentioned technical problem, the technical solution used in the present invention is: a kind of propanol-triethylamine azeotropic mixture extraction rectifying method, and the method adopts seriality operation or intermittent operation.
Extractant described in the invention respectively ethylene glycol, N-METHYLFORMAMIDE, ethylene glycol and ionic liquid (40wt% ~ 50wt%) form mixed extractant, it is possible to be effectively improved product purity and extraction efficiency, reduce production cost. The ionic liquid respectively N-ethylpyridine dimethyl phosphate salt ([epy] [DMP]) of invention employing, N-picoline dimethyl phosphate salt ([mpy] [DMP]), N-butyl-pyridinium dimethyl phosphate salt ([bpy] [DMP]).
A kind of propanol-triethylamine azeotropic mixture extraction rectifying method seriality operating procedure of the present invention is as follows:
1) propanol and triethylamine mixture are continuously added to by feed system by T101 middle and lower part, and extractant adds from tower top, and feeding temperature is all room temperature, and it is normal pressure that T101 operates pressure;
2) T101 tower top can obtain product purity more than 99.9% triethylamine product, is propanol and extractant at the bottom of tower;
3) T101 tower base stream enters the middle part of T102, obtains the propanol product of purity more than 99.9% at T102 tower top, remains triethylamine and the isopropanol of extractant and trace at the bottom of tower, and it is normal pressure that T102 operates pressure;
4) T102 tower base stream is incorporated to extractant feed pipeline, supplements as extractant.
Based on above-mentioned a kind of propanol-triethylamine azeotropic mixture extraction rectifying method seriality operation, this seriality operation important technological parameters is:
1) T101 technical parameter: theoretical cam curve=30 ~ 60; Reflux ratio=1:1 ~ 5:1, operates pressure=normal pressure; Charge ratio=2:1 ~ the 6:1 of extractant and raw material, feeding temperature=30 DEG C ~ 40 DEG C, pressure=0.11MPa, raw material is propanol (14wt%) and the nearly azeotropic of triethylamine (86wt%) forms, feeding temperature=30 DEG C ~ 40 DEG C, pressure=0.11MPa; Extracted feed position is 3 ~ 5 blocks of column plates, 20 ~ 45 blocks, feedstock position column plate;
2) T102 technical parameter: theoretical cam curve=20 ~ 60; Reflux ratio=1:1 ~ 6:1, operates pressure=normal pressure; Feed entrance point is 12 ~ 32 blocks of column plates.
A kind of propanol-triethylamine azeotropic mixture extraction rectifying method intermittent operation step of the present invention is as follows:
1) propanol and triethylamine mixture are by the disposable tower bottom of rectifying tower E1 that squeezes into of raw material pump P2, open heating;
2) when condensed fluid, total reflux operation occurs in tower top, and extractant is continuously added in tower by pump P1, and continues total reflux operation;
3) when tower top temperature reaches 88 DEG C, detection, tower top triethylamine content is more than 99%, with reflux ratio (1 ~ 7): 1 extraction triethylamine product is to V3(along with the rising of tower top temperature, and reflux ratio is increased to 7:1 accordingly);
4) when tower top temperature is more than 93 DEG C, and detect that triethylamine content starts to reduce, close extraction, carry out total reflux operation 0.5h, start with reflux ratio (2 ~ 4) afterwards: 1 extraction triethylamine-propanol changeover portion is to V2(along with the rising of tower top temperature, and reflux ratio is increased to 4:1 accordingly);
5) when tower top temperature reaches 96 DEG C, detection, tower top alcohol content is more than 99%, with reflux ratio (1 ~ 6): 1 extraction propanol product is to V5(along with the rising of tower top temperature, and reflux ratio is increased to 6:1 accordingly; )
6) when tower top temperature is more than 103 DEG C, and detect that alcohol content starts to reduce, stop adding extractant and also close extraction that infinite reflux 0.2h starts with (2 ~ 4) afterwards: 1 extraction propanol-extractant changeover portion is to V4;
7) when tower top temperature is more than 120 DEG C, stop heating, after the cooling of tower reactor extractant, be discarded to V1 standby.
Based on above-mentioned a kind of propanol-triethylamine azeotropic mixture extraction rectifying method intermittent operation step, the main important technological parameters of this operating procedure is
1) extractive distillation column theoretical cam curve N=30 ~ 60; Full tower operation pressure is normal pressure;
2) extractant and charge ratio R=(2 ~ 6): the 1 of raw material.
Beneficial effects of the present invention: the present invention is by adding extractant, it is possible to make propanol-triethylamine azeotropism disappear (in accompanying drawing 2, azeotropic point disappears).
The novelty of the present invention and advantage are in that:
1) the separating of propanol and triethylamine azeotropic system, there is no separating technology report at present or delivers;
3) adopting multiple extractant, selectivity is various;
3) extractant with the addition of ionic liquid, it is possible to increase the service efficiency of extractant, reduce cost;
4) technique is simple, adopts double tower continuous rectification mode (T101 tower is extractive distillation column, and T102 tower is solvent recovery tower) or single column batch fractionating mode, it is possible to requires to select according to product yield, flexible operation, effectively reduces cost simultaneously.
Accompanying drawing explanation
Fig. 1 is propanol-triethylamine T-x-y phasor.
Fig. 2 is the T-x-y phasor after propanol-triethylamine adds extractant.
Fig. 3 is seriality of the present invention operation device and flow chart.
Fig. 4 is intermittent operation device of the present invention and flow chart.
1. extractant enters tower stream stock; 2. raw material enters tower stream stock; 3. extractive distillation column backflow stream stock; 4. extractive distillation column extraction stream stock; 5. solvent recovery tower incoming flow stock; 6. solvent recovery tower backflow stream stock; 7. solvent recovery tower extraction stream stock; 8. extractant extraction stream stock.
Fig. 3 capital equipment illustrates: T101 extractive distillation column; T102 solvent recovery tower; E101, E103 condenser; E102, E103 reboiler; P101 expects pump.
Fig. 4 symbol description: P1 extractant feed pump; P2 feedstock pump; E1 tower reactor; E2 condenser (containing catcher); V1 ~ V5 respectively extractant recycling can, interim fraction tank 1., products pot 1., interim fraction tank 2., products pot 2..
Detailed description of the invention
The invention will be further described to be below embodied as case for combination, but does not limit the scope of protection of the invention.
Embodiment one
The implementation case is continuous extraction distillation operation mode, and as shown in Figure 3, extractant selects ethylene glycol and N-ethylpyridine dimethyl phosphate salt ([epy] [DMP]), and consumption is 500kg/h; Feed throughput is 100kg/h, and raw material consists of propanol (14wt%) and triethylamine (86wt%). The T101 number of plates is 40, and extractant feed position is at the 5th block of column plate, and feedstock position is at 32 blocks of column plates. Reflux ratio is set as 4:1, and overhead extraction speed is 86kg/h, and the triethylamine purity obtained is 99.9%. The T102 number of plates is 30, and stream stock 5. feed entrance point is the 20th block of column plate, and reflux ratio is 2:1, and overhead extraction speed is 14kg/h, and the propanol purity obtained is 99.9%, extractant backflow at the bottom of tower, supplementing as solvent.
Embodiment two
Extractant select ethylene glycol, consumption is 600kg/hr, and the reflux ratio that the reflux ratio of T101 is set to 3:1, T102 is set to 1:1, other conditions such as embodiment one, the propanol obtained with triethylamine product purity all more than 99.9%.
Embodiment three
Extractant select N-METHYLFORMAMIDE, other conditions such as embodiment one, the propanol obtained with triethylamine product purity all more than 99.9%.
Embodiment four
The implementation case is batch extracting rectified mode of operation, and as shown in Figure 4, extractant selects ethylene glycol and N-picoline dimethyl phosphate salt ([mpy] [DMP]), and consumption is 500kg; Feed throughput is 100kg, and raw material consists of propanol (14wt%) and triethylamine (86wt%). Theoretical cam curve is 40, and extractant feed position is at the 5th block of column plate. Propanol and triethylamine mixture, by the disposable tower bottom of rectifying tower E1 that squeezes into of raw material pump P2, open heating; When condensed fluid, total reflux operation occurs in tower top, and extractant is continuously added in tower by pump P1, and continues total reflux operation; When tower top temperature reaches 88 DEG C, detection, tower top triethylamine content is more than 99%, with reflux ratio (1 ~ 7): 1 extraction triethylamine product is to V3(along with the rising of tower top temperature, and reflux ratio is increased to 7:1 accordingly); When tower top temperature is more than 93 DEG C, and detect that triethylamine content starts to reduce, close extraction, carry out total reflux operation 0.5h, start with reflux ratio (2 ~ 4) afterwards: 1 extraction triethylamine-propanol changeover portion is to V2(along with the rising of tower top temperature, and reflux ratio is increased to 4:1 accordingly);When tower top temperature reaches 96 DEG C, detection, tower top alcohol content is more than 99%, with reflux ratio (1 ~ 6): 1 extraction propanol product is to V5(along with the rising of tower top temperature, and reflux ratio is increased to 6:1 accordingly); When tower top temperature is more than 103 DEG C, and detect that alcohol content starts to reduce, stop adding extractant and also close extraction that infinite reflux 0.2h starts with (2 ~ 4) afterwards: 1 extraction propanol-extractant changeover portion is to V4; When tower top temperature is more than 120 DEG C, stop heating, after the cooling of tower reactor extractant, be discarded to V1 standby.
Embodiment five
Extractant select ethylene glycol, consumption is 400kg, other conditions such as embodiment four, the propanol obtained with triethylamine product purity all more than 99%.
The above is effect preferably case in the present invention, but described content is only presently preferred embodiments of the present invention, it is impossible to be used to be defined the practical range of the present invention.
Claims (6)
1. propanol-triethylamine azeotropic mixture extraction rectifying method, it is characterized in that: the method is divided into seriality operation or intermittent operation, wherein seriality operation comprises extractive distillation column (T101) and solvent recovery tower (T102), the mixture of raw material propanol and triethylamine adds in T101 middle and lower part, extractant adds from T101 top, triethylamine is at T101 overhead extraction, extractant and propanol mixture are by entering in the middle part of T102 after extraction at the bottom of T101 tower, propanol is from T102 overhead extraction, and extractant extraction Posterior circle at the bottom of tower utilizes; Intermittent operation includes propanol and squeezes into tower bottom of rectifying tower E1 with triethylamine mixture material is disposable, extractant is continuously added to by tower top, first overhead extraction is triethylamine, different according to temperature afterwards, successively extraction triethylamine-propanol interim fraction, propanol, propanol-extractant interim fraction, tower reactor extraction extractant recycle.
2. by the method described in claim 1, it is characterised in that: seriality or interval row operation extractant are ethylene glycol or the mixed extractant of N-METHYLFORMAMIDE or ethylene glycol and ionic liquid composition.
3. by the method described in claim 2, it is characterised in that: mixed extractant intermediate ion liquid respectively N-picoline dimethyl phosphate salt, N-ethylpyridine dimethyl phosphate salt, N-butyl-pyridinium dimethyl phosphate salt.
4. by the method described in claim 2, it is characterised in that: ethylene glycol is with the mixed extractant of ionic liquid composition, and ionic liquid mass fraction is 40wt% ~ 50wt%.
5. by the method described in claim 1, it is characterised in that: under seriality mode of operation, important technological parameters is:
1) T101 technical parameter: theoretical cam curve is 30 ~ 60; Reflux ratio is 1:1 ~ 5:1, and full tower operation pressure is normal pressure; Charge ratio 2:1 ~ 6:1, the pressure 0.11MPa of extractant and raw material; Raw material is propanol and triethylamine, feeding temperature 30 DEG C ~ 40 DEG C, pressure 0.11MPa; Extracted feed position is 3 ~ 5 blocks of column plates, 20 ~ 45 blocks, feedstock position column plate;
2) T102 technical parameter: theoretical cam curve is 20 ~ 60; Reflux ratio 1:1 ~ 6:1, full tower operation pressure is normal pressure; Feed entrance point is 12 ~ 32 blocks of column plates.
6. by the method described in claim 1, it is characterised in that: under intermittent operation mode, important technological parameters is:
Extractive distillation column theoretical cam curve is 30 ~ 60; The charge ratio of extractant and raw material is 2 ~ 6:1; Full tower operation pressure is normal pressure.
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Cited By (3)
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| CN107382743A (en) * | 2017-07-31 | 2017-11-24 | 湖北江汉石化装备有限公司 | A kind of method of extracting rectifying purification triethylamine |
| CN109134198A (en) * | 2018-11-08 | 2019-01-04 | 山东科技大学 | A kind of method of separation of extractive distillation tetrafluoropropanol and water azeotropic mixture |
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| CN109134198A (en) * | 2018-11-08 | 2019-01-04 | 山东科技大学 | A kind of method of separation of extractive distillation tetrafluoropropanol and water azeotropic mixture |
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