CN103130633A - Method for producing p-methylacetophenone with fixed-bed reactor - Google Patents
Method for producing p-methylacetophenone with fixed-bed reactor Download PDFInfo
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- CN103130633A CN103130633A CN2013100861523A CN201310086152A CN103130633A CN 103130633 A CN103130633 A CN 103130633A CN 2013100861523 A CN2013100861523 A CN 2013100861523A CN 201310086152 A CN201310086152 A CN 201310086152A CN 103130633 A CN103130633 A CN 103130633A
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- bed reactor
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- toluene
- methylacetophenone
- methyl aceto
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- GNKZMNRKLCTJAY-UHFFFAOYSA-N 4'-Methylacetophenone Chemical compound CC(=O)C1=CC=C(C)C=C1 GNKZMNRKLCTJAY-UHFFFAOYSA-N 0.000 title claims abstract description 160
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 7
- YXFVVABEGXRONW-UHFFFAOYSA-N Toluene Chemical compound CC1=CC=CC=C1 YXFVVABEGXRONW-UHFFFAOYSA-N 0.000 claims abstract description 105
- 238000000034 method Methods 0.000 claims abstract description 30
- 238000006243 chemical reaction Methods 0.000 claims abstract description 28
- 238000007670 refining Methods 0.000 claims abstract description 22
- 239000003153 chemical reaction reagent Substances 0.000 claims abstract description 20
- 239000002994 raw material Substances 0.000 claims abstract description 18
- 239000003054 catalyst Substances 0.000 claims abstract description 6
- 239000012043 crude product Substances 0.000 claims description 36
- QTBSBXVTEAMEQO-UHFFFAOYSA-N Acetic acid Chemical compound CC(O)=O QTBSBXVTEAMEQO-UHFFFAOYSA-N 0.000 claims description 21
- XEKOWRVHYACXOJ-UHFFFAOYSA-N Ethyl acetate Chemical compound CCOC(C)=O XEKOWRVHYACXOJ-UHFFFAOYSA-N 0.000 claims description 12
- ZMXDDKWLCZADIW-UHFFFAOYSA-N N,N-Dimethylformamide Chemical compound CN(C)C=O ZMXDDKWLCZADIW-UHFFFAOYSA-N 0.000 claims description 12
- 238000005917 acylation reaction Methods 0.000 claims description 11
- WFDIJRYMOXRFFG-UHFFFAOYSA-N Acetic anhydride Chemical compound CC(=O)OC(C)=O WFDIJRYMOXRFFG-UHFFFAOYSA-N 0.000 claims description 8
- UHOVQNZJYSORNB-UHFFFAOYSA-N monobenzene Natural products C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 claims description 7
- MVPPADPHJFYWMZ-UHFFFAOYSA-N chlorobenzene Chemical compound ClC1=CC=CC=C1 MVPPADPHJFYWMZ-UHFFFAOYSA-N 0.000 claims description 6
- SECXISVLQFMRJM-UHFFFAOYSA-N N-Methylpyrrolidone Chemical compound CN1CCCC1=O SECXISVLQFMRJM-UHFFFAOYSA-N 0.000 claims description 5
- WETWJCDKMRHUPV-UHFFFAOYSA-N acetyl chloride Chemical group CC(Cl)=O WETWJCDKMRHUPV-UHFFFAOYSA-N 0.000 claims description 4
- 239000012346 acetyl chloride Substances 0.000 claims description 4
- LQNUZADURLCDLV-UHFFFAOYSA-N nitrobenzene Chemical compound [O-][N+](=O)C1=CC=CC=C1 LQNUZADURLCDLV-UHFFFAOYSA-N 0.000 claims description 4
- 239000003960 organic solvent Substances 0.000 claims description 4
- 238000000746 purification Methods 0.000 claims description 4
- HXJUTPCZVOIRIF-UHFFFAOYSA-N sulfolane Chemical compound O=S1(=O)CCCC1 HXJUTPCZVOIRIF-UHFFFAOYSA-N 0.000 claims description 4
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical group O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 claims description 3
- 239000011347 resin Substances 0.000 claims description 3
- 229920005989 resin Polymers 0.000 claims description 3
- WSLDOOZREJYCGB-UHFFFAOYSA-N 1,2-Dichloroethane Chemical compound ClCCCl WSLDOOZREJYCGB-UHFFFAOYSA-N 0.000 claims description 2
- 125000001997 phenyl group Chemical group [H]C1=C([H])C([H])=C(*)C([H])=C1[H] 0.000 claims description 2
- 239000003795 chemical substances by application Substances 0.000 claims 5
- XYIBRDXRRQCHLP-UHFFFAOYSA-N ethyl acetoacetate Chemical compound CCOC(=O)CC(C)=O XYIBRDXRRQCHLP-UHFFFAOYSA-N 0.000 claims 1
- 238000005516 engineering process Methods 0.000 abstract description 4
- 238000010924 continuous production Methods 0.000 abstract 1
- 238000011031 large-scale manufacturing process Methods 0.000 abstract 1
- 239000000047 product Substances 0.000 description 19
- 239000007788 liquid Substances 0.000 description 15
- 238000003860 storage Methods 0.000 description 9
- 238000011084 recovery Methods 0.000 description 8
- 239000006227 byproduct Substances 0.000 description 6
- 230000009466 transformation Effects 0.000 description 6
- 239000006200 vaporizer Substances 0.000 description 6
- 238000000605 extraction Methods 0.000 description 5
- 239000000463 material Substances 0.000 description 5
- 239000000126 substance Substances 0.000 description 4
- 230000007812 deficiency Effects 0.000 description 3
- 238000010586 diagram Methods 0.000 description 3
- 238000002474 experimental method Methods 0.000 description 3
- 239000003205 fragrance Substances 0.000 description 3
- 238000010438 heat treatment Methods 0.000 description 3
- 239000002841 Lewis acid Substances 0.000 description 2
- WRQNANDWMGAFTP-UHFFFAOYSA-N Methylacetoacetic acid Chemical compound COC(=O)CC(C)=O WRQNANDWMGAFTP-UHFFFAOYSA-N 0.000 description 2
- 238000009833 condensation Methods 0.000 description 2
- 230000005494 condensation Effects 0.000 description 2
- 235000013305 food Nutrition 0.000 description 2
- 238000010992 reflux Methods 0.000 description 2
- 238000011160 research Methods 0.000 description 2
- JGRDPVUWSFRGMI-UHFFFAOYSA-N 2-[4-(4-fluorophenyl)-4-oxobutyl]guanidine Chemical compound NC(N)=NCCCC(=O)C1=CC=C(F)C=C1 JGRDPVUWSFRGMI-UHFFFAOYSA-N 0.000 description 1
- 239000005995 Aluminium silicate Substances 0.000 description 1
- 241000196324 Embryophyta Species 0.000 description 1
- 235000016623 Fragaria vesca Nutrition 0.000 description 1
- 240000009088 Fragaria x ananassa Species 0.000 description 1
- 235000011363 Fragaria x ananassa Nutrition 0.000 description 1
- -1 Lewis acid ion Chemical class 0.000 description 1
- 235000005087 Malus prunifolia Nutrition 0.000 description 1
- 244000070406 Malus silvestris Species 0.000 description 1
- 244000086363 Pterocarpus indicus Species 0.000 description 1
- 235000009984 Pterocarpus indicus Nutrition 0.000 description 1
- 239000002253 acid Substances 0.000 description 1
- 239000000654 additive Substances 0.000 description 1
- 230000000996 additive effect Effects 0.000 description 1
- 235000012211 aluminium silicate Nutrition 0.000 description 1
- 235000009508 confectionery Nutrition 0.000 description 1
- 230000007797 corrosion Effects 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 230000002950 deficient Effects 0.000 description 1
- 238000013461 design Methods 0.000 description 1
- 235000013399 edible fruits Nutrition 0.000 description 1
- 239000012847 fine chemical Substances 0.000 description 1
- 230000002363 herbicidal effect Effects 0.000 description 1
- 239000004009 herbicide Substances 0.000 description 1
- 239000011964 heteropoly acid Substances 0.000 description 1
- 235000012907 honey Nutrition 0.000 description 1
- 239000002608 ionic liquid Substances 0.000 description 1
- NLYAJNPCOHFWQQ-UHFFFAOYSA-N kaolin Chemical compound O.O.O=[Al]O[Si](=O)O[Si](=O)O[Al]=O NLYAJNPCOHFWQQ-UHFFFAOYSA-N 0.000 description 1
- 150000007517 lewis acids Chemical class 0.000 description 1
- 239000007791 liquid phase Substances 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 239000002808 molecular sieve Substances 0.000 description 1
- 238000012544 monitoring process Methods 0.000 description 1
- 229910052680 mordenite Inorganic materials 0.000 description 1
- 229930014626 natural product Natural products 0.000 description 1
- 239000012071 phase Substances 0.000 description 1
- QCDYQQDYXPDABM-UHFFFAOYSA-N phloroglucinol Chemical compound OC1=CC(O)=CC(O)=C1 QCDYQQDYXPDABM-UHFFFAOYSA-N 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 description 1
- 239000002904 solvent Substances 0.000 description 1
- 239000012808 vapor phase Substances 0.000 description 1
- 238000009834 vaporization Methods 0.000 description 1
- 230000008016 vaporization Effects 0.000 description 1
- 239000000341 volatile oil Substances 0.000 description 1
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- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
本发明公开了一种以固定床反应器生产对甲基苯乙酮的方法，包括如下步骤：（1）反应工段：固定床反应器中装有催化剂床层，在温度为60～300℃，压力为0.05～30MPa的条件下，将甲苯和酰化试剂混合均匀后经原料送料泵送入固定床反应器中进行酰化反应，得到对甲基苯乙酮粗品；（2）精制工段：将所述的对甲基苯乙酮粗品应用精馏技术进行精馏提纯，得到高纯度的对甲基苯乙酮产品。与传统的工艺流程相比，本发明工艺流程操作简单，投资成本低，产品纯度高等优点；同时，反应器具备结构简单，操作稳定，便于控制，易于实现规模化和连续化生产。
The invention discloses a method for producing p-methylacetophenone with a fixed-bed reactor, which includes the following steps: (1) Reaction section: a catalyst bed is installed in the fixed-bed reactor, and the temperature is 60-300°C. Under the condition of pressure of 0.05-30MPa, mix toluene and acylating reagent evenly, and then send them into the fixed bed reactor through raw material feeding pump for acylating reaction to obtain crude p-methylacetophenone; (2) Refining section: The crude p-methylacetophenone is purified by rectification technology to obtain high-purity p-methylacetophenone product. Compared with the traditional process flow, the process flow of the present invention has the advantages of simple operation, low investment cost and high product purity; at the same time, the reactor has simple structure, stable operation, easy control, and easy realization of large-scale and continuous production.
Description
Technical field
The present invention relates to a kind of method with the synthetic p-methyl aceto phenone of fixed-bed reactor production, belong to food and chemical technology field.
Background technology
As everyone knows, p-methyl aceto phenone is the important fine chemicals intermediate of food and chemical field, fragrance with similar crab apple flower, and the fragrance that looks like honey, strawberry is arranged, flowers and fruits fragrance sharply is with sweet, is widely used in the various essence of preparation, herbicide intermediate etc., also can make foodstuff additive, be also simultaneously the intermediate of producing other high value added product, and its natural product are present in rosewood essential oil and Touch-me-notAction Plant caul-fat.
Both at home and abroad phase of basic research synthetic p-methyl aceto phenone in laboratory only is confined to the batch experiment process, and is less about the continuous experimental study of its production, uses fixed bed to do the acylation reaction that reactor carries out toluene and not yet reports.
The reaction process of traditional synthetic p-methyl aceto phenone, take simple intermittence tank reactor as main, itself have the deficiencies such as the reaction treatment amount is little, reaction is insufficient and the reaction investment consumption is large, deficiency in economic performance.At present; the method of domestic synthetic p-methyl aceto phenone is mainly to be obtained through acylation reaction under the katalysis of Lewis acid or protonic acid etc. by toluene and diacetyl oxide; catalyzer itself also exists and can not recycle, the defective such as serious and aftertreatment is seriously polluted to equipment corrosion.
Summary of the invention
The objective of the invention is to overcome the deficiencies in the prior art, a kind of method with fixed-bed reactor production p-methyl aceto phenone that makes the reaction process mass-producing is provided.
Technical scheme of the present invention is summarized as follows:
A kind of method of producing p-methyl aceto phenone with fixed-bed reactor comprises following process:
(1) react workshop section: beds is housed in fixed-bed reactor, it is 60～300 ℃ in temperature, pressure is under the condition of 0.05～30MPa, with the raw material take away pump, toluene and acylating reagent is sent into and is carried out acylation reaction in described fixed-bed reactor, obtains the p-methyl aceto phenone crude product;
(2) refining workshop section: the p-methyl aceto phenone crude product is carried out rectification and purification, obtain p-methyl aceto phenone.
The mol ratio of toluene and acylating reagent can be 1:0.1～30, and toluene and acylating reagent can be sent into respectively fixed-bed reactor, sends into fixed-bed reactor after also can mixing.
In step (1), also can send into organic solvent sending into toluene and acylating reagent in fixed-bed reactor when.
In step (1), the beds type of feed is loose heap type or regular type.
Temperature is preferably 80～220 ℃, preferably 160 ℃; Pressure is preferably 0.3～20MPa, preferably 0.5MPa.
The mol ratio of toluene and acylating reagent is for being better 1:2～20, preferably 1:15.
The preferred Acetyl Chloride 98Min. of acylating reagent, diacetyl oxide, acetic acid, methyl aceto acetate or ethyl acetate, preferably diacetyl oxide or Acetyl Chloride 98Min. can also adopt other acylating reagent.
Organic solvent is preferably benzene, toluene, acetic acid, 1,2-ethylene dichloride, tetramethylene sulfone, chlorobenzene, oil of mirbane, dimethyl formamide or N-Methyl pyrrolidone, preferably tetramethylene sulfone.
The rectification and purification mode is continuous rectification or batch fractionating.
Described catalyzer is MCM-41, HZSM-5, Mont-K10, CT-175 resin, HY or load Zn
2+HY.
Advantage of the present invention:
The present invention has that technical process is simple to operate, and cost of investment is low, the product purity advantages of higher; Simultaneously, fixed-bed reactor are simple in structure, and stable operation is convenient to control, and the cost design cost is low, is easy to realize mass-producing and serialization production.
Description of drawings
Fig. 1 is the process flow diagram that reacts workshop section of the present invention, and 1a in figure, 1b are the reaction solution storage tank, 2a, 2b is the raw material take away pump, and 3 is the vaporizer of fixed-bed reactor, and 4 is fixed-bed reactor, 5 is computer on-line Control instrument, and 6 for reacting workshop section's condenser, and 7 is the crude product storage tank;
Fig. 2 is the treating tower schematic diagram at intermittence of refining workshop section, and wherein 25 are the rectifying tower reactor, and 26 is heating jacket, and 27 is thermopair, and 28 is the treating tower at intermittence, and 29 is condenser, and 30 is reflux ratio controller, and 31 is overhead product extraction mouth, and 32 is vacuum pump system.
Fig. 3 is a kind of process flow diagram of producing p-methyl aceto phenone with fixed-bed reactor, 1a in figure, 1b is the reaction solution storage tank, 2a, 2b is the raw material take away pump, 3 is the vaporizer of fixed-bed reactor, 4 is fixed-bed reactor, 5 is computer on-line Control instrument, 6 for reacting workshop section's condenser, 7 is the crude product storage tank, 8 is the first take away pump, 9 is the second take away pump, 10 is the first container for storing liquid, 11 is the toluene recovery tower, 12, 13, 20, 21 are pipeline, 14 is the byproduct treating tower, 15 is the second container for storing liquid, 16 is the 3rd take away pump, 17 is the 4th take away pump, 18 is the 3rd container for storing liquid, 19 is the acylating reagent recovery tower, 22 is p-methyl aceto phenone continuous treating tower, 23 is the 4th container for storing liquid, and 24 is the 5th take away pump.
Embodiment
The present invention is further illustrated below in conjunction with the drawings and specific embodiments.
Embodiments of the invention are in order to make those skilled in the art understand better the present invention, but the present invention are not imposed any restrictions.
The first is produced the method for p-methyl aceto phenone (refining workshop section adopts batch fractionating) with fixed-bed reactor.(seeing Fig. 1 and Fig. 2)
(1) react workshop section's (see figure 1): in fixed-bed reactor 4, beds is housed, under the condition of certain temperature and pressure, be standby with raw material take away pump 2a(2b) will to be stored in reaction solution storage tank 1a(1b be standby) in the toluene that mixes and acylating reagent send into and carry out acylation reaction in fixed-bed reactor, obtain the p-methyl aceto phenone crude product, after reacting workshop section's condenser 6 condensations, enter in crude product storage tank 7; Vaporizer 3 can be arranged between raw material take away pump and fixed-bed reactor, and the raw material of liquid towards is vaporized as required.If adopt the situation of vapor phase toluene and acylating reagent; can use 3 pairs of raw materials of vaporizer to vaporize, if adopt the situation of liquid phase toluene and acylating reagent, not need to use vaporizer 3; directly by raw material take away pump 2a or 2b, raw material is sent in fixed-bed reactor 4.
Computer on-line Control instrument 5 is controlled the flow of raw material take away pump 2a, 2b, the temperature of reaction of the vaporization temperature of vaporizer 3 and fixed-bed reactor 4.
(2) refining workshop section: the p-methyl aceto phenone crude product is carried out the batch fractionating separating-purifying, obtain highly purified p-methyl aceto phenone product.
The flow process of batch fractionating is:
The p-methyl aceto phenone crude product in crude product storage tank 7 of being stored in that reaction workshop section obtains is packed in rectifying tower reactor 25, through heating jacket 26 heating, material is through treating tower 28 separation at intermittence, under the control of reflux ratio controller 30, through condenser 29 condensations, at overhead product extraction mouth 31 places extraction product p-methyl aceto phenone; Tower head is connected with vacuum pump system 32, the temperature of thermopair 27 monitoring rectifying tower reactor 25 interior p-methyl aceto phenone crude products,
The following examples 1-6 adopts the first to produce the method for p-methyl aceto phenone (refining workshop section adopts batch fractionating) with fixed-bed reactor.
Embodiment 1
Reaction workshop section: the MCM-41 beds is housed in fixed-bed reactor, and the beds type of feed is loose heap type; It is 60 ℃ in temperature, pressure is under the condition of 0.05MPa, the toluene and the diacetyl oxide that are 1:0.1 with mol ratio are pre-mixed evenly, send into the raw material take away pump and carry out acylation reaction in fixed-bed reactor and obtain the p-methyl aceto phenone crude product, the transformation efficiency of diacetyl oxide is 35.7%, and the yield of p-methyl aceto phenone is 95%;
Refining workshop section: the p-methyl aceto phenone crude product is carried out batch fractionating purify, obtain purity and be 99% p-methyl aceto phenone product.
Reaction workshop section: the HZSM-5 beds is housed in fixed-bed reactor, and the beds type of feed is loose heap type; It is 80 ℃ in temperature, pressure is under the condition of 0.3MPa, the toluene and the Acetyl Chloride 98Min. that are 1:2 with mol ratio are pre-mixed evenly, send into the raw material take away pump and carry out acylation reaction in fixed-bed reactor and obtain the p-methyl aceto phenone crude product, the transformation efficiency of toluene is 52%, and the yield of p-methyl aceto phenone is 96%;
Refining workshop section: the p-methyl aceto phenone crude product is carried out batch fractionating purify, obtain purity and be 99.5% p-methyl aceto phenone product.
Reaction workshop section: the Mont-K10 beds is housed in fixed-bed reactor, and the beds type of feed is loose heap type; It is 160 ℃ in temperature, pressure is under the condition of 0.5MPa, to be the toluene of 1:15 and acetic acid send into respectively with the raw material take away pump carries out acylation reaction in fixed-bed reactor and obtain the p-methyl aceto phenone crude product with mol ratio, and the transformation efficiency of toluene is 65%, and the yield of p-methyl aceto phenone is 96%;
Refining workshop section: the p-methyl aceto phenone crude product is carried out batch fractionating purify, obtain purity and be 99.1% p-methyl aceto phenone product.
Reaction workshop section: CT-175 resin catalyst bed is housed in fixed-bed reactor, and the beds type of feed is regular type; It is 220 ℃ in temperature, pressure is under the condition of 10MPa, after being pre-mixed mol ratio be 1:30:5 toluene, methyl aceto acetate and solvent sulfolane evenly, send into the raw material take away pump and carry out acylation reaction in fixed-bed reactor and obtain the p-methyl aceto phenone crude product, the transformation efficiency of toluene is 97%, and the yield of p-methyl aceto phenone is 96%;
Refining workshop section: the p-methyl aceto phenone crude product is carried out batch fractionating purify, obtain purity and be 99% p-methyl aceto phenone product.
Reaction workshop section: the HY beds is housed in fixed-bed reactor, and the beds type of feed is regular type; It is 300 ℃ in temperature, pressure is under the condition of 20MPa, be toluene, the ethyl acetate and 1 of 1:20:5 with mol ratio, the 2-ethylene dichloride is pre-mixed evenly, deliver to the raw material take away pump and carry out acylation reaction in fixed-bed reactor and obtain the p-methyl aceto phenone crude product, the transformation efficiency of toluene is 92%, and the yield of p-methyl aceto phenone is 96.2%;
Refining workshop section: the p-methyl aceto phenone crude product is carried out batch fractionating purify, obtain purity and be 99.8% p-methyl aceto phenone product.
Reaction workshop section: load Zn is housed in fixed-bed reactor
2+The HY beds, the beds type of feed is regular type; It is 300 ℃ in temperature, pressure is under the condition of 30MPa, toluene, ethyl acetate and the N-Methyl pyrrolidone (NMP) that are 1:15:5 with mol ratio are pre-mixed evenly, deliver to the raw material take away pump and carry out acylation reaction in fixed-bed reactor and obtain the p-methyl aceto phenone crude product, the transformation efficiency of toluene is 92%, and the yield of p-methyl aceto phenone is 96.2%;
Refining workshop section: the p-methyl aceto phenone crude product is carried out batch fractionating purify, obtain purity and be 99.8% p-methyl aceto phenone product.
Experiment showed, that the N-Methyl pyrrolidone that substitutes in the present embodiment with benzene, acetic acid, chlorobenzene, oil of mirbane or dimethyl formamide (DMF) can obtain the p-methyl aceto phenone crude product.
The second is produced the method for p-methyl aceto phenone (refining workshop section adopts continuous rectification) with fixed-bed reactor.(see figure 3)
(1) react workshop section:
Reaction workshop section with first method;
(2) refining workshop section: the p-methyl aceto phenone crude product is carried out continuous rectification purify, obtain highly purified p-methyl aceto phenone product.(see figure 3)
The flow process of continuous rectification is:
The p-methyl aceto phenone crude product that is stored in crude product storage tank 7 that obtains of reaction workshop section is delivered in toluene recovery tower 11 through the first take away pump 8, and the azeotrope of the toluene that rectifying obtains and a small amount of acetic acid is delivered to the 4th container for storing liquid 23 through pipeline 12 from the tower top of toluene recovery tower 11; The acylating reagent that the tower reactor of toluene recovery tower 11 obtains and by product and p-methyl aceto phenone crude product enter in the first container for storing liquid 10.
The material of storing at the first container for storing liquid 10 in the second take away pump 9 is delivered to byproduct treating tower 14, the by product that rectifying obtains from the tower top of byproduct treating tower 14 through pipeline 13 extraction; The acylating reagent that the tower reactor of byproduct treating tower obtains and p-methyl aceto phenone crude product enter in the second container for storing liquid 15.
The material of storing at the second container for storing liquid 15 is in the 3rd take away pump 16 is delivered to acylating reagent recovery tower 19, and the acylating reagent that rectifying obtains is delivered to the 4th container for storing liquid 23 through pipeline 20 from the tower top of acylating reagent recovery tower 19; The p-methyl aceto phenone crude product that the tower reactor of acylating reagent recovery tower obtains enters in the 3rd container for storing liquid 18.
Deliver in p-methyl aceto phenone continuous treating tower 22 through the 4th take away pump 17 at the material that the 3rd container for storing liquid 18 is stored, the p-methyl aceto phenone that rectifying obtains from the tower top of p-methyl aceto phenone continuous treating tower through pipeline 21 extraction.
The recovered material (toluene and acylating reagent) of storing in the 4th container for storing liquid 23 recycles in the 5th take away pump 24 is delivered to reaction solution storage tank 1a or 1b.
The following examples 7-12 is that the second that adopts is produced the method for p-methyl aceto phenone (refining workshop section adopts continuous rectification) with fixed-bed reactor.Equipment connection such as Fig. 3.
Reaction workshop section: with embodiment 1
Refining workshop section: described p-methyl aceto phenone crude product is carried out the continuous rectification separating-purifying, obtain purity and be 99% p-methyl aceto phenone product.
Embodiment 8
Reaction workshop section: with embodiment 2
Refining workshop section: described p-methyl aceto phenone crude product is carried out the continuous rectification separating-purifying, obtain purity and be 99.5% p-methyl aceto phenone product.
Embodiment 9
Reaction workshop section: with embodiment 3
Refining workshop section: described p-methyl aceto phenone crude product is carried out the continuous rectification separating-purifying, obtain purity and be 99.3% p-methyl aceto phenone product.
Embodiment 10
Reaction workshop section: with embodiment 4
Refining workshop section: described p-methyl aceto phenone crude product is carried out the continuous rectification separating-purifying, obtain purity and be 99% p-methyl aceto phenone product.
Embodiment 11
Reaction workshop section: with embodiment 5
Refining workshop section: described p-methyl aceto phenone crude product is carried out the continuous rectification separating-purifying, obtain purity and be 99% p-methyl aceto phenone product.
Embodiment 12
Reaction workshop section: with embodiment 6
Refining workshop section: described p-methyl aceto phenone crude product is carried out the continuous rectification separating-purifying, obtain purity and be 99% p-methyl aceto phenone product.
The experiment proved that, the catalyzer that the kind of catalyzer is not limited only to use in the various embodiments described above is as mordenite molecular sieve, kaolin, 13X, USY, NaY, SBA-15, heteropolyacid or ionic liquid etc.
Reference
[1] Jia Pengfei, Tang Hengdan, Wang Jihong, Ceng Aiwu, the research of rectification under vacuum technology purification p-methyl aceto phenone, Chemical Industry in Guangzhou, 2012,40(19): 61-63
[2] Shi Jinhui, Xiang Bin, Wang Min, Lewis acid ion liquid catalyst synthesizes the 4-methyl acetophenone, the Zhejiang chemical industry, 2011,42(2): 16-18.
Claims (10)
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106380386A (en) * | 2016-08-30 | 2017-02-08 | 枣阳市先飞高科农药有限公司 | Method for preparing p-methylacetophenone |
| CN107011134A (en) * | 2017-04-28 | 2017-08-04 | 浙江中欣氟材股份有限公司 | A kind of synthetic method of the bromoacetophenone of 2 fluorine 5 |
| CN110590518A (en) * | 2019-09-04 | 2019-12-20 | 宿迁科思化学有限公司 | Green new process for preparing p-methoxyacetophenone |
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2013
- 2013-03-18 CN CN2013100861523A patent/CN103130633A/en active Pending
Non-Patent Citations (3)
| Title |
|---|
| T. JAIMOL ET AL.: "Selective acetylation of toluene to 4-methylacetophenone over zeolite catalysts", 《JOURNAL OF MOLECULAR CATALYSIS A: CHEMICAL》 * |
| 徐新等: "固体酸催化合成2-乙酰噻吩", 《精细石油化工》 * |
| 贾鹏飞等: "真空精馏技术提纯对甲基苯乙酮的研究", 《广州化工》 * |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106380386A (en) * | 2016-08-30 | 2017-02-08 | 枣阳市先飞高科农药有限公司 | Method for preparing p-methylacetophenone |
| CN107011134A (en) * | 2017-04-28 | 2017-08-04 | 浙江中欣氟材股份有限公司 | A kind of synthetic method of the bromoacetophenone of 2 fluorine 5 |
| CN110590518A (en) * | 2019-09-04 | 2019-12-20 | 宿迁科思化学有限公司 | Green new process for preparing p-methoxyacetophenone |
| CN110590518B (en) * | 2019-09-04 | 2022-10-14 | 宿迁科思化学有限公司 | Novel green process for preparing p-methoxyacetophenone |
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