CN105503501A - Butanol-cyclohexane azeotropic mixture extractive distillation method - Google Patents
Butanol-cyclohexane azeotropic mixture extractive distillation method Download PDFInfo
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- CN105503501A CN105503501A CN201610026620.1A CN201610026620A CN105503501A CN 105503501 A CN105503501 A CN 105503501A CN 201610026620 A CN201610026620 A CN 201610026620A CN 105503501 A CN105503501 A CN 105503501A
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
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- C07C7/00—Purification; Separation; Use of additives
- C07C7/04—Purification; Separation; Use of additives by distillation
- C07C7/05—Purification; Separation; Use of additives by distillation with the aid of auxiliary compounds
- C07C7/08—Purification; Separation; Use of additives by distillation with the aid of auxiliary compounds by extractive distillation
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- 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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Abstract
Provided is a butanol-cyclohexane azeotropic mixture extractive distillation method. The butanol-cyclohexane azeotropic mixture extractive distillation method comprises a pressure-reduction continuous operating mode or a pressure-reduction intermittent operating mode, by means of selecting multiple extraction agents, high-purity butanol and cyclohexane products are obtained, and the extraction agents can be recycled. The butanol-cyclohexane azeotropic mixture extractive distillation method has the advantages that in the extraction process, not only is traditional solvent adopted, but also a mixed extraction agent which is composed of the traditional solvent and ionic liquid is adopted, the huge advantages in the aspects of energy consumption, environment stress and product purity are achieved, the method is specially suitable for large scale industrial application and particularly aims at separation of a butanol-cyclohexane azeotropic system, and the current technical gap is filled up.
Description
Technical field
Separation method provided by the present invention for be butanols-hexanaphthene azeotropic system, adopt mixed solvent that ethylene glycol, ethylene glycol and ionic liquid form as extraction agent respectively, belong to the extraction rectifying method of butanols-hexanaphthene azeotropic system.
Background technology
The raw material related in the present invention is butanols and hexanaphthene, both common in chemical industry material.Butanols (C
4h
10o), have another name called tyrosol, the third carbinol, the solvent of multiple coating and the raw material of plasticizer phthalic acid dibutylester (see phthalic ester) processed, also for the manufacture of butyl acrylate, N-BUTYL ACETATE, butyl glycol ether and the extraction agent as organic synthesis intermediate and biochemical medicine, also for the manufacture of tensio-active agent.Hexanaphthene (C
6h
12), be mainly used as the solvent of rubber, coating, varnish, the thinner of tackiness agent, oil extraction agent.Because the toxicity of hexanaphthene is little, therefore the normal benzene that replaces is used for de-oiling fat, de-lubricating grease and depainting.Also be usually used in the monomer hexanodioic acid of manufacture nylon, hexanediamine and hexanolactam, be also used as the raw material manufacturing hexalin, pimelinketone.
Butanols and hexanaphthene not only have important application at petrochemical industry, and also have inside other industry and use quite widely.But two kinds of materials but exist azeotropism, the difficulty both being separated is increased greatly.For the recovery of organic solvent, industrial extensive employing be distillation or the processing mode of rectifying, 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 comparatively additive method is higher, and in facility investment, also often comparatively additive method is larger, and product purity is difficult to ensure.
In the separation method that chemical industry is conventional, rectifying becomes the selection of numerous enterprises with the advantage of himself, but rectifying just means 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 current related industries policy, energy-conservation, reduction of discharging becomes the most important thing of the chemical enterprise coming years.Adopt extraction rectification technique in the present invention, compared with traditional azeotropic distillation, energy consumption problem has obvious improvement, and product purity is higher.The extraction agent adopted in the present invention is no longer simple organic solvent, but the mixed extractant selecting organic solvent and ionic liquid to form, obviously can reduce the loss of extraction agent.
Ionic liquid refers to the salt compounds be at room temperature in a liquid state be made up of organic cation and negatively charged ion, has that steam forces down, fusing point is low, liquid journey is wide, easy to operate, solubility is good and stable advantages of higher.Although ionic liquid has numerous advantages, because existing market is expensive, and the large usage quantity of extraction agent, cause production cost very high, therefore rate of utilization is lower.Researchist finds, ionic liquid can form new ionic liquid with coordination agent, effectively can reduce the cost of industrial applications, and have both advantages concurrently simultaneously, conventional coordination agent has ethylene glycol, glycerine etc., the coordination agent that the present invention selects is ethylene glycol, forms mixed solvent with ionic liquid.
Based on the advantage of ionic liquid, the mixed solution of conventional organic solvents and ionic liquid can be used in rectification process as extraction agent, (ionic liquid is non-volatile, rate of loss is extremely low can to effectively reduce the loss of conventional solvent, and recycle), reduce production cost, can improve the quality of products simultaneously.
Existing azeotropic system separation means is divided into two classes substantially: azeotropic distillation and extracting rectifying.Extracting rectifying in product purity, energy consumption comparatively azeotropic distillation there is advantage.And at present in the selection of extraction agent, substantially adopt conventional solvent directly to adopt ion liquid abstraction agent in other words as extraction agent, CN103193590A a continuous extraction separation method for alcohol mixture-water, the technique of CN102627556A separation of extractive distillation ethyl formate-alcohol-water all adopt ethylene glycol to make extraction agent; The method of CN103193590A ion liquid abstraction rectifying separation Acetic Acid-Water adopts ionic liquid as extraction agent.The former is low on extraction efficiency, and the latter is then much bigger in cost of investment.Generally speaking, loss of extractant how is reduced and production cost, raising product purity are the problems that current rectification process needs solution badly.
At present, about the separation of butanols-hexanaphthene azeotropic system, not relevant document or report.
Summary of the invention
The object of the invention is to overcome the deficiency existed in existing technique, and for butanols-hexanaphthene azeotropic system, propose a kind of good separating effect, product purity is high, energy consumption is low, and extraction agent easily reclaims, is easy to industrialized separation method.By T-x-y phasor, can see that butanols-hexanaphthene exists azeotropism (can see in accompanying drawing 1 that butanols-hexanaphthene exists azeotropic point).
For solving the problems of the technologies described above, the technical solution used in the present invention is: a kind of butanols-hexanaphthene azeotropic mixture extraction rectifying method, and the method adopts continuity operation or intermittent operation.
Extraction agent described in the invention is respectively ethylene glycol, ethylene glycol and ionic liquid (40wt% ~ 50wt%) and forms mixed extractant, can effectively improve product purity and extraction efficiency, reduces production cost.The ionic liquid that invention adopts is respectively N-ethylpyridine dimethyl phosphate salt ([epy] [DMP]), N-picoline dimethyl phosphate salt ([mpy] [DMP]), N-butyl-pyridinium dimethyl phosphate salt ([bpy] [DMP]).
A kind of butanols of the present invention-hexanaphthene azeotropic mixture extraction rectifying method continuity operation steps is as follows:
1) butanols and cyclohexane mixtures are added by feed system continuously by T101 middle and lower part, and extraction agent adds from tower top, and feeding temperature is all normal temperature, and T101 working pressure is 0.3atm(absolute pressure);
2) T101 tower top can obtain product purity more than 99.9% hexanaphthene product, is butanols and extraction agent at the bottom of tower;
3) T101 tower base stream enters the middle part of T102, obtains the butanols product of purity more than 99.9% at T102 tower top, and remain extraction agent and micro-butanols and hexanaphthene at the bottom of tower, T102 working pressure is 0.3atm(absolute pressure);
4) T102 tower base stream is incorporated to extractant feed pipeline, supplements as extraction agent.
Based on above-mentioned a kind of butanols-hexanaphthene azeotropic mixture extraction rectifying method continuity operation, this continuity operation main technical details is:
1) T101 technical parameter: tower theoretical plate number=35 ~ 60; Reflux ratio=2:1 ~ 4:1, working pressure=0.3atm; Extraction agent is respectively the mixed extractant (wherein ionic liquid is N-ethylpyridine dimethyl phosphate salt ([epy] [DMP]), N-picoline dimethyl phosphate salt ([mpy] [DMP]), the N-butyl-pyridinium dimethyl phosphate salt ([bpy] [DMP]) of content at 40wt% ~ 50wt%) that ethylene glycol, ethylene glycol and ionic liquid form; Charge ratio=1.5:1 ~ the 5:1 of extraction agent and raw material, feeding temperature=30 DEG C ~ 40 DEG C, pressure=0.11MPa, raw material is that butanols (93wt%) forms with the nearly azeotropic of hexanaphthene (7wt%), feeding temperature=30 DEG C ~ 40 DEG C, pressure=0.11MPa; Bottom temperature=125 DEG C ~ 131 DEG C, tower top temperature=44 DEG C ~ 49 DEG C.Feed solution position is 3 ~ 9 blocks of column plates, 28 ~ 45 blocks, feedstock position column plate;
2) T102 technical parameter: theoretical plate number=30 ~ 45; Reflux ratio=1:1 ~ 4:1, working pressure=0.3atm; Bottom temperature=161 DEG C ~ 167 DEG C, tower top temperature=85 DEG C ~ 90 DEG C, feed entrance point is 23 ~ 36 blocks of column plates.
A kind of butanols of the present invention-hexanaphthene azeotropic mixture extraction rectifying method intermittent operation step is as follows:
1) butanols and cyclohexane mixtures squeeze into tower bottom of rectifying tower E1 by feedstock pump P2 is disposable, open heating;
2) when phlegma appears in tower top, total reflux operation, and extraction agent is added in tower continuously by pump P1, and continue total reflux operation;
3) when tower top temperature reaches 43 DEG C, detect, tower top cyclohexane content is greater than 99%, with reflux ratio (2 ~ 4): 1 extraction hexanaphthene product is to the rising of V3(along with tower top temperature, and reflux ratio is corresponding is increased to 4:1);
4) when tower top temperature is more than 50 DEG C, and detect that cyclohexane content starts to reduce, close extraction, carry out total reflux operation 0.5h, start with reflux ratio (2 ~ 5) afterwards: 1 extraction hexanaphthene-butanols transition section is to the rising of V2(along with tower top temperature, and reflux ratio is corresponding is increased to 5:1);
5) when tower top temperature reaches 82 DEG C, detect, tower top butanol content is greater than 99%, with reflux ratio (1 ~ 4): 1 extraction butanols product is to the rising of V5(along with tower top temperature, and reflux ratio is corresponding is increased to 4:1);
6) when tower top temperature is more than 90 DEG C, and detect that butanol content starts to reduce, stop adding extraction agent and closing extraction, total reflux 0.2h, start with (2 ~ 4) afterwards: 1 extraction butanols-ethylene glycol transition section is to V4;
7) when tower top temperature is more than 120 DEG C, stop heating, after the cooling of tower reactor extraction agent, be discarded to V1 for subsequent use.
Based on above-mentioned a kind of butanols-hexanaphthene azeotropic mixture extraction rectifying method intermittent operation step, the main main technical details of this operation steps is
1) extractive distillation column theoretical plate number=38 ~ 55, working pressure is 0.3atm;
2) charge ratio=(1.5 ~ 5) of extraction agent and raw material: 1.
Beneficial effect of the present invention: the present invention, by adding extraction agent, can make butanols-hexanaphthene azeotropism disappear (in accompanying drawing 2, azeotropic point disappears).
Novelty of the present invention and advantage are:
1) being separated of butanols and hexanaphthene azeotropic system, there is no separating technology report at present or delivers;
2) adopt multiple extraction agent, selectivity is various;
3) adopting rectification under vacuum, effectively can reduce energy consumption, by improving the relative volatility of raw material to improve product purity, and by adopting rectification under vacuum, production cost can be reduced by the grade reducing heating agent;
4) with the addition of ionic liquid in extraction agent, the service efficiency of extraction agent can improved, reduce costs;
5) technique is simple, adopts double tower continuous rectification mode (T101 tower is extractive distillation column, and T102 tower is solvent recovery tower) or single tower batch fractionating mode, and can require to select according to product production, flexible operation, effectively reduces costs simultaneously.
Accompanying drawing explanation
Fig. 1 is the T-x-y phasor of butanols-hexanaphthene.
Fig. 2 is the T-x-y phasor after butanols-hexanaphthene adds extraction agent.
Fig. 3 is continuity operating gear of the present invention and schema.
Fig. 4 is intermittent operation device of the present invention and schema.
Fig. 3 mainly flows stock and illustrates: 1.-extraction agent 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.-extraction agent extraction stream stock.
Fig. 3 major equipment illustrates: T101-extractive distillation column; T102-solvent recovery tower; E101, E103-condenser; E102, E103-reboiler; P101-material pump.
Fig. 4 is intermittent operation device of the present invention and schematic flow sheet.
Fig. 4 nomenclature: P1-extractant feed pump; P2-feedstock pump; E1-tower reactor; E2-condenser (containing trap); V1 ~ V5 be respectively extraction agent withdrawing can, interim fraction tank 1., products pot 1., interim fraction tank 2., products pot 2..
Embodiment
Below for the invention will be further described in conjunction with concrete case study on implementation, but do 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, extraction agent selects ethylene glycol and N-picoline dimethyl phosphate salt ([mpy] [DMP]), and consumption is 150kg/h; Feed throughput is 100kg/h, and raw material consists of butanols (93wt%) and hexanaphthene (7wt%).T101 stage number is 55, and extractant feed position is at the 5th block of column plate, and feedstock position is at 45 blocks of column plates.Reflux ratio is set as 4:1, and overhead extraction speed is 93kg/h, and the cyclohexane purity obtained is 99.7%.T102 stage number is 35, and stream stock 5. feed entrance point is the 7th block of column plate, and reflux ratio is 2:1, and overhead extraction speed is 7kg/h, and the butanols purity obtained is 99.6%.Extraction agent backflow at the bottom of tower, supplementing as solvent.
Embodiment two
Ethylene glycol selected by extraction agent, and consumption is 400kg/hr, and the reflux ratio of T101 is set to 3:1, and the reflux ratio of T102 is set to 4:1, and other conditions are as embodiment one.The butanols obtained follows hexanaphthene product purity all more than 99.9%.
Embodiment three
The implementation case is batch extracting rectified operating method, and as shown in Figure 4, extraction agent selects ethylene glycol and N-picoline dimethyl phosphate salt ([mpy] [DMP]), and consumption is 500kg; Feed throughput is 100kg, and raw material consists of butanols (93wt%) and hexanaphthene (7wt%).Extracting rectifying column plate number is 55, and extractant feed position is at the 5th block of column plate; Butanols and cyclohexane mixtures squeeze into tower bottom of rectifying tower E1 by feedstock pump P2 is disposable, open heating; When phlegma appears in tower top, total reflux operation, and extraction agent is added in tower continuously by pump P1, and continue total reflux operation; When tower top temperature reaches 43 DEG C, detect, tower top cyclohexane content is greater than 99%, with reflux ratio (2 ~ 4): 1 extraction hexanaphthene product is to the rising of V3(along with tower top temperature, and reflux ratio is corresponding is increased to 4:1); When tower top temperature is more than 50 DEG C, and detect that cyclohexane content starts to reduce, close extraction, carry out total reflux operation 0.5h, start with reflux ratio (2 ~ 5) afterwards: 1 extraction hexanaphthene-butanols transition section is to the rising of V2(along with tower top temperature, and reflux ratio is corresponding is increased to 5:1); When tower top temperature reaches 82 DEG C, detect, tower top butanol content is greater than 99%, with reflux ratio (1 ~ 4): 1 extraction butanols product is to the rising of V5(along with tower top temperature, and reflux ratio is corresponding is increased to 4:1); When tower top temperature is more than 90 DEG C, and detect that butanol content starts to reduce, stop adding extraction agent and closing extraction, total reflux 0.2h, start with (2 ~ 4) afterwards: 1 extraction butanols-ethylene glycol transition section is to V4; When tower top temperature is more than 120 DEG C, stop heating, after the cooling of tower reactor extraction agent, be discarded to V1 for subsequent use.
Embodiment four
Ethylene glycol selected by extraction agent, and consumption is 400kg, and other conditions are as embodiment three.The butanols obtained follows hexanaphthene product purity all more than 99%.
The above is effect preferably case in the present invention, but described content is only preferred embodiment of the present invention, can not be used to be defined practical range of the present invention.
Claims (6)
1. butanols-hexanaphthene azeotropic mixture extraction rectifying method, it is characterized in that: the method is divided into continuity to operate or intermittent operation, wherein continuity operation comprises extractive distillation column (T101) and solvent recovery tower (T102), the mixture of raw material butanol and hexanaphthene adds in T101 middle and lower part, extraction agent adds from T101 top, hexanaphthene is at T101 overhead extraction, extraction agent and butanol mixture enter in the middle part of T102 by after extraction at the bottom of T101 tower, butanols is from T102 overhead extraction, and extraction agent extraction Posterior circle at the bottom of tower utilizes; Intermittent operation comprises butanols and cyclohexane mixtures raw material is disposable squeezes into tower bottom of rectifying tower E1, extraction agent is added continuously by tower top, first overhead extraction is hexanaphthene, different according to temperature afterwards, extraction hexanaphthene-butanols interim fraction, butanols, butanols-extraction agent interim fraction successively, tower reactor extraction extraction agent is recycled.
2. by the said method of claim 1, it is characterized in that: continuity or interval line operate extraction agent are the mixed extractant that ethylene glycol or ethylene glycol and ionic liquid form.
3., by the said method of claim 2, it is characterized in that: mixed extractant intermediate ion liquid is respectively N-picoline dimethyl phosphate salt, N-ethylpyridine dimethyl phosphate salt, N-butyl-pyridinium dimethyl phosphate salt.
4., by the said method of claim 2, it is characterized in that: in the mixed extractant that ethylene glycol and ionic liquid form, ionic liquid massfraction is 40wt% ~ 50wt%.
5., by the said method of claim 1, it is characterized in that: under continuity operating method, main technical details is:
1) T101 technical parameter: tower theoretical plate number=35 ~ 60; Reflux ratio=2:1 ~ 4:1, working pressure=0.3atm; Charge ratio=1.5:1 ~ the 5:1 of extraction agent and raw material, feeding temperature=30 DEG C ~ 40 DEG C, pressure=0.11MPa, raw material is butanols and hexanaphthene, feeding temperature=30 DEG C ~ 40 DEG C, pressure=0.11MPa; Feed solution position is 3 ~ 9 blocks of column plates, 28 ~ 45 blocks, feedstock position column plate;
2) T102 technical parameter: theoretical plate number=30 ~ 45; Reflux ratio=1:1 ~ 4:1, working pressure=0.3atm; Feed entrance point is 23 ~ 36 blocks of column plates.
6., by the said method of claim 1, it is characterized in that: under intermittent operation mode, main technical details is:
Extractive distillation column theoretical plate number=38 ~ 55; The charge ratio of extraction agent and raw material is 1.5:1 ~ 5:1; Full tower working pressure is 0.3atm.
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105906479A (en) * | 2016-05-24 | 2016-08-31 | 济南大学 | Method for separating butanol-butyronitrile mixture |
| CN106008159A (en) * | 2016-05-24 | 2016-10-12 | 济南大学 | Method for separating isopropyl alcohol-propionitrile mixture |
| CN110052052A (en) * | 2019-05-29 | 2019-07-26 | 天津赫普菲乐新材料有限公司 | Multicomponent batch fractionating intelligence control system and control method |
| CN114805025A (en) * | 2022-05-27 | 2022-07-29 | 辽宁石油化工大学 | Separation and purification method of cyclohexanol and butyl cyclohexyl ether |
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