CN1840528A - Process for preparing N-formyl morpholine - Google Patents
Process for preparing N-formyl morpholine Download PDFInfo
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- CN1840528A CN1840528A CN 200510058892 CN200510058892A CN1840528A CN 1840528 A CN1840528 A CN 1840528A CN 200510058892 CN200510058892 CN 200510058892 CN 200510058892 A CN200510058892 A CN 200510058892A CN 1840528 A CN1840528 A CN 1840528A
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- morpholine
- reaction
- methyl
- formyl morpholine
- separation
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- LCEDQNDDFOCWGG-UHFFFAOYSA-N morpholine-4-carbaldehyde Chemical compound O=CN1CCOCC1 LCEDQNDDFOCWGG-UHFFFAOYSA-N 0.000 title abstract description 8
- 238000004519 manufacturing process Methods 0.000 title description 9
- YNAVUWVOSKDBBP-UHFFFAOYSA-N Morpholine Chemical compound C1COCCN1 YNAVUWVOSKDBBP-UHFFFAOYSA-N 0.000 claims abstract description 62
- 238000006243 chemical reaction Methods 0.000 claims abstract description 40
- 239000003054 catalyst Substances 0.000 claims abstract description 17
- 238000002360 preparation method Methods 0.000 claims abstract description 12
- 239000000463 material Substances 0.000 claims abstract description 5
- 239000000047 product Substances 0.000 claims description 32
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 claims description 30
- 238000000926 separation method Methods 0.000 claims description 24
- 238000005516 engineering process Methods 0.000 claims description 20
- 238000011084 recovery Methods 0.000 claims description 20
- 239000002994 raw material Substances 0.000 claims description 10
- 239000007791 liquid phase Substances 0.000 claims description 9
- 239000006200 vaporizer Substances 0.000 claims description 9
- WQDUMFSSJAZKTM-UHFFFAOYSA-N Sodium methoxide Chemical compound [Na+].[O-]C WQDUMFSSJAZKTM-UHFFFAOYSA-N 0.000 claims description 8
- 238000005809 transesterification reaction Methods 0.000 claims description 7
- 239000012071 phase Substances 0.000 claims description 6
- -1 sodium alkoxide Chemical class 0.000 claims description 6
- MFRIHAYPQRLWNB-UHFFFAOYSA-N sodium tert-butoxide Chemical compound [Na+].CC(C)(C)[O-] MFRIHAYPQRLWNB-UHFFFAOYSA-N 0.000 claims description 6
- 241000282326 Felis catus Species 0.000 claims description 5
- RTAQQCXQSZGOHL-UHFFFAOYSA-N Titanium Chemical compound [Ti] RTAQQCXQSZGOHL-UHFFFAOYSA-N 0.000 claims description 5
- 239000007795 chemical reaction product Substances 0.000 claims description 5
- 150000001875 compounds Chemical class 0.000 claims description 5
- JGFBRKRYDCGYKD-UHFFFAOYSA-N dibutyl(oxo)tin Chemical compound CCCC[Sn](=O)CCCC JGFBRKRYDCGYKD-UHFFFAOYSA-N 0.000 claims description 5
- LQRUPWUPINJLMU-UHFFFAOYSA-N dioctyl(oxo)tin Chemical compound CCCCCCCC[Sn](=O)CCCCCCCC LQRUPWUPINJLMU-UHFFFAOYSA-N 0.000 claims description 5
- 238000001914 filtration Methods 0.000 claims description 5
- 230000035484 reaction time Effects 0.000 claims description 5
- GHVZOJONCUEWAV-UHFFFAOYSA-N [K].CCO Chemical compound [K].CCO GHVZOJONCUEWAV-UHFFFAOYSA-N 0.000 claims description 4
- 238000009833 condensation Methods 0.000 claims description 4
- 230000005494 condensation Effects 0.000 claims description 4
- BDAWXSQJJCIFIK-UHFFFAOYSA-N potassium methoxide Chemical compound [K+].[O-]C BDAWXSQJJCIFIK-UHFFFAOYSA-N 0.000 claims description 4
- QDRKDTQENPPHOJ-UHFFFAOYSA-N sodium ethoxide Chemical compound [Na+].CC[O-] QDRKDTQENPPHOJ-UHFFFAOYSA-N 0.000 claims description 4
- 125000000484 butyl group Chemical group [H]C([*])([H])C([H])([H])C([H])([H])C([H])([H])[H] 0.000 claims description 3
- 238000007701 flash-distillation Methods 0.000 claims description 3
- 239000002032 methanolic fraction Substances 0.000 claims description 3
- LPNYRYFBWFDTMA-UHFFFAOYSA-N potassium tert-butoxide Chemical compound [K+].CC(C)(C)[O-] LPNYRYFBWFDTMA-UHFFFAOYSA-N 0.000 claims description 3
- 239000000126 substance Substances 0.000 claims description 3
- ZLMJMSJWJFRBEC-UHFFFAOYSA-N Potassium Chemical compound [K] ZLMJMSJWJFRBEC-UHFFFAOYSA-N 0.000 claims description 2
- 229910052700 potassium Inorganic materials 0.000 claims description 2
- 239000011591 potassium Substances 0.000 claims description 2
- 229910052708 sodium Inorganic materials 0.000 claims description 2
- 239000011734 sodium Substances 0.000 claims description 2
- 230000001020 rhythmical effect Effects 0.000 claims 2
- 238000011175 product filtration Methods 0.000 claims 1
- TZIHFWKZFHZASV-UHFFFAOYSA-N methyl formate Chemical compound COC=O TZIHFWKZFHZASV-UHFFFAOYSA-N 0.000 abstract 2
- 150000002148 esters Chemical class 0.000 abstract 1
- 238000000034 method Methods 0.000 description 37
- 230000015572 biosynthetic process Effects 0.000 description 10
- BDAGIHXWWSANSR-UHFFFAOYSA-N methanoic acid Natural products OC=O BDAGIHXWWSANSR-UHFFFAOYSA-N 0.000 description 10
- 238000003786 synthesis reaction Methods 0.000 description 10
- 239000007789 gas Substances 0.000 description 8
- 230000009466 transformation Effects 0.000 description 8
- ZWEHNKRNPOVVGH-UHFFFAOYSA-N 2-Butanone Chemical compound CCC(C)=O ZWEHNKRNPOVVGH-UHFFFAOYSA-N 0.000 description 6
- OSWFIVFLDKOXQC-UHFFFAOYSA-N 4-(3-methoxyphenyl)aniline Chemical compound COC1=CC=CC(C=2C=CC(N)=CC=2)=C1 OSWFIVFLDKOXQC-UHFFFAOYSA-N 0.000 description 5
- 239000003795 chemical substances by application Substances 0.000 description 5
- 238000000605 extraction Methods 0.000 description 5
- 235000019253 formic acid Nutrition 0.000 description 5
- 239000002904 solvent Substances 0.000 description 4
- 239000002253 acid Substances 0.000 description 3
- 238000010923 batch production Methods 0.000 description 3
- 238000010992 reflux Methods 0.000 description 3
- 230000003068 static effect Effects 0.000 description 3
- 238000003756 stirring Methods 0.000 description 3
- 125000003118 aryl group Chemical group 0.000 description 2
- 238000010924 continuous production Methods 0.000 description 2
- 238000005260 corrosion Methods 0.000 description 2
- 230000007797 corrosion Effects 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 2
- 125000004108 n-butyl group Chemical group [H]C([H])([H])C([H])([H])C([H])([H])C([H])([H])* 0.000 description 2
- 125000000383 tetramethylene group Chemical group [H]C([H])([*:1])C([H])([H])C([H])([H])C([H])([H])[*:2] 0.000 description 2
- 239000010409 thin film Substances 0.000 description 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 2
- BKHJHGONWLDYCV-UHFFFAOYSA-N [C]=O.[C] Chemical compound [C]=O.[C] BKHJHGONWLDYCV-UHFFFAOYSA-N 0.000 description 1
- 230000002378 acidificating effect Effects 0.000 description 1
- 238000009835 boiling Methods 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 229910002091 carbon monoxide Inorganic materials 0.000 description 1
- 235000009508 confectionery Nutrition 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 235000019628 coolness Nutrition 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 239000012847 fine chemical Substances 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 239000002815 homogeneous catalyst Substances 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 239000003345 natural gas Substances 0.000 description 1
- 230000001376 precipitating effect Effects 0.000 description 1
- 239000000376 reactant Substances 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 238000007086 side reaction Methods 0.000 description 1
- 238000001308 synthesis method Methods 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
- 239000002351 wastewater Substances 0.000 description 1
Abstract
The preparation method for N-formyl morpholine comprises: in batch or continual reactor, with 0.5-5wt% ester interchange catalyst, selecting methyl formate and morpholine by mass ratio as 1:1.30~1.74 as material, reacting for 2-6h on condition of normal pressure-0.6Mpa and 30-120Deg; separating and recovering the product. With this invention, the conversion ratio of morpholine can achieve 98%, total yield up to 95%, and purity more than 99.5%.
Description
Technical field:
The present invention relates to a kind of synthetic aromatic device extraction solvent, methyl ethyl ketone plant butylene and put forward the preparation method of dense extraction solvent and synthetic gas acid gas removal agent N-N-formyl morpholine N-.
Background technology
The N-N-formyl morpholine N-is that the good extraction solvent and the methyl ethyl ketone plant butylene of aromatic device carried dense extraction solvent.And N-N-formyl morpholine N-and composition thereof is good Sweet natural gas and the agent of synthetic gas acid gas removal, is used for the external Morphysorb novel process of exploitation in recent years.
The synthesis technique of N-N-formyl morpholine N-mainly contains formic acid method (CN1345723, CN1356324 and 1482121), carbon monoxide oxo synthesis and methyl-formiate method.
It is acylating agent that formic acid method synthetic route adopts formic acid, synthetic N-N-formyl morpholine N-under the effect of an acidic catalyst and band aqua.Because reaction system acidity is very strong, seriously corroded needs to adopt expensive corrosion resistant apparatus, has waste water to produce simultaneously in the production process, easy residual formic acid in the product and have corrodibility.
Carbon monoxide carbon back synthesis method adopts CO to make acylating agent, and abundant raw material is cheap, but needs could realize under high temperature, highly compressed condition, and needs to adopt expensive catalysts, and complex process to the equipment requirements height, is invested bigger.
The methyl-formiate method adopts methyl-formiate to make acylating agent, in the presence of transesterification catalyst, with the synthetic N-N-formyl morpholine N-of morpholine reaction.
The process characteristic of methyl-formiate method is, the process side reaction is few, the little and anhydrous generation of corrosion, and technology is simple, and morpholine and methyl-formiate transformation efficiency, product yield and quality are all than higher, and especially free acid content is much smaller than the formic acid method.
Summary of the invention
The present invention is a raw material with methyl-formiate and morpholine, adds transesterification catalyst, in batch reactor or the flow reactor internal reaction, reaction product through intermittently or continuous separation technology obtain product N-N-formyl morpholine N-.Adopt intermittently (employing stirred-tank reactor) or (employing shell and tube or tower reactor) production technique continuously, main processes is as follows:
One, batch production process
(1) building-up process
With methyl-formiate and morpholine is raw material, adds morpholine and transesterification catalyst earlier in reactor, under violent stirring, slowly adds methyl-formiate, and reaction obtains thick product.Wherein the mass ratio of morpholine and methyl-formiate is 1.30～1.74: 1; Reaction pressure is normal pressure～0.6Mpa; Temperature of reaction is 30～120 ℃; Reaction times is 2～6 hours; Catalyst levels is 0.5～5% of a raw material gross weight.
The catalyzer that adopts is the compound of sodium methylate, potassium methylate, sodium ethylate, potassium ethylate, sodium tert-butoxide, potassium tert.-butoxide, Dibutyltin oxide, dioctyl tin oxide, titanic acid ester or above-mentioned substance.
(2) sepn process
Intermittently the separating technology operation comprises:
1. the Separation and Recovery of methyl-formiate: the rectifying separation reaction product, rectifier unit is made up of reactor and batch fractionating tower, rectifying pressure 0.1～0.2Mpa, 68～82 ℃ of temperature of reaction kettle, rectifying tower top is collected the methyl-formiate cut;
2. the Separation and Recovery of methyl alcohol: rectifying pressure is become normal pressure, 68～130 ℃ of temperature of reaction kettle, rectifying tower top is collected methanol fraction;
3. the Separation and Recovery of morpholine: will operate the 2 thick products that obtain and filter, and carry out rectification under vacuum behind the filtration catalizer, vacuum tightness is 0.09～0.099MPa, 130～155 ℃ of temperature of reaction kettle, overhead collection morpholine cut;
4.N-the acquisition of N-formyl morpholine N-: it is constant to operate 3 vacuum tightnesss, and temperature of reaction kettle becomes 155～165 ℃, overhead collection N-N-formyl morpholine N-;
The advance of this technology is: one, simple, reasonable, the no three wastes of raw material route.Two, simple to operation, facility investment is few.Three, adopt high-efficient homogeneous catalyst, shorten the reaction times greatly, improve transformation efficiency.The transformation efficiency of this technology building-up process reaches as high as 98% (in methyl-formiate), and process total recovery yield reaches more than 93% (in methyl-formiate, to be counted more than 96% with morpholine).
Two, continuous building-up process
(1) building-up process
To contain the methyl-formiate of catalyzer and morpholine respectively with volume pump by metering than squeezing in the static mixer, enter shell and tube reactor or tower reactor then and react and obtain thick product.The mass ratio of morpholine and methyl-formiate is 1.30～1.74: 1; Reaction pressure 0.2～0.6Mpa; Temperature of reaction is 30～120 ℃; The reaction solution residence time is 2～6 hours; Catalyst levels is 0.5～5% of a raw material gross weight.The catalyzer that adopts can comprise the compound of sodium methylate, potassium methylate, sodium ethylate, potassium ethylate, sodium tert-butoxide, potassium tert.-butoxide, Dibutyltin oxide, dioctyl tin oxide, titanic acid ester or above-mentioned substance.
(2) sepn process
1. the Separation and Recovery of methyl-formiate: enter flash tank after effusive reaction solution drops to normal pressure～0.2MPa through throttling valve with pressure in the reactor, the gas phase part that flash distillation obtains obtains methyl-formiate after condensation, and liquid phase enters vaporizer;
2. methyl alcohol Separation and Recovery: vaporizer liquid phase temperature out is controlled at 160～165 ℃, and the gas phase part in the vaporizer is as methanol product, and liquid phase part enters lights column after removing catalyzer after filtration;
3. morpholine Separation and Recovery: lights column vacuum tightness is 0.08～0.09Mpa, and tower still temperature is 158～162 ℃, and cat head obtains the morpholine component, and leftover materials enter vacuum product tower;
4.N-the acquisition of N-formyl morpholine N-: vacuum product tower vacuum tightness is 0.09～0.099Mpa, 164～168 ℃ of tower still temperature, and cat head obtains the N-N-formyl morpholine N-.
The advance of this technology is: one, operate continuously, be convenient to automatization control.Two, production energy consumption is few, and running expense is low.Three, little, the compact construction of synthesis device volume.The transformation efficiency of this technology building-up process reaches as high as 98% (in methyl-formiate), and process total recovery yield reaches more than 95% (in methyl-formiate, to be counted more than 98% with morpholine).
Three, the combination of different process
The production of N-N-formyl morpholine N-also can be adopted intermittently synthesis technique [(1)] and continuous separation technology [two (2)] combination, perhaps adopts continuous synthesis technique [two (1)] and intermittently separates [one (2)] process combination.
(" fine-chemical intermediate " 2003.8.Vol.33 No.4) compares with prior art, the preparation method of N-N-formyl morpholine N-provided by the invention, realized the industrialized mass of N-N-formyl morpholine N-, transformation efficiency height (having reached 98%) in the production process in methyl-formiate, process total recovery yield reaches more than 93%, the product N-N-formyl morpholine N-purity height that obtains.The production technique of N-N-formyl morpholine N-comprises intermittently synthesis technique and continuous separation technology combination, continuous synthesis technique and intermittently separating technology combination, full continuous processing combination or batch technology combination entirely in the invention.The separation of reactant is purified and is had intermittently and continuous two kinds of technologies, and the separation of reaction product is complete, and refuse is few, and reaction by-product is recycling substantially all.Catalyzer comprises sodium alkoxide, potassium alcoholate, organotin, titanic acid ester or their compound in the invention, can select flexibly to use according to practical situation in process of production.Below will the present invention will be further described by embodiment, among the embodiment:
Total recovery=synthesis yield * rectifying yield/100
If there is not specified otherwise, transformation efficiency and yield are the building-up process index, and all are to calculate benchmark with the morpholine, and pressure is absolute pressure.
Description of drawings:
Fig. 1 is a N-N-formyl morpholine N-batch production process schematic representation;
Fig. 2 is a N-N-formyl morpholine N-continuous production processes synoptic diagram.
Embodiment:
Embodiment 1～5
As shown in Figure 1,1 stirred autoclave; 2 reaction reflux exchangers; 3 catalyst filters; 4 medial launders; 5 batch fractionating towers; 6 condensers of returning; 7 return tanks; Scale tank in the middle of 8; 9 ganging of products grooves; 10 vacuum buffer tanks; 11 vacuum pumps.Referring to N-N-formyl morpholine N-batch production process schematic representation (Fig. 1), answer morpholine and the transesterification catalyst that adds metering in the still 1 to stirring to send out, under violent stirring, the methyl-formiate that slowly adds metering, control reaction temperature and pressure reach necessary requirement, the reaction regular hour, obtain thick product.
Reactor utilizes the heating coil of reactor inside to heat, in conjunction with utilizing a batch fractionating tower 5 (theoretical plate number 35) to carry out product separation as rectifying still this moment.
The working pressure of methyl-formiate Separation and Recovery process is 0.2Mpa, and reactor 1 temperature is at 68～82 ℃, and rectifying tower 5 overhead collection temperature are 60～72 ℃ methyl-formiate cut; Subsequently working pressure is become normal pressure, tower still temperature is at 68～130 ℃, and the overhead collection temperature is 63～65 ℃ a methanol fraction; After Methanol Recovery finishes, thick product is filtered, leach the catalyzer (catalyzer is insoluble to the N-N-formyl morpholine N-) that precipitating is got off, carry out rectification under vacuum then, vacuum tightness is 0.095MPa, tower still 1 temperature is at 130～155 ℃, and rectifying tower 5 overhead collection temperature are 70～145 ℃ morpholine cut (containing small amount of methanol, water, N-N-formyl morpholine N-); Keep the vacuum constant, tower still 1 temperature is increased to 155～165 ℃, the cut of gathering 148～150 ℃ of rectifying tower 5 tower top temperatures is as product,
The concrete reaction conditions of each embodiment sees Table 1, and reaction result sees Table 2.
Table 1
| Raw material weight is than (morpholine: methyl-formiate) | Catalyzer | Catalyst levels (%) | Reaction pressure (Mpa) | Temperature of reaction (℃) | Reaction times (h) | |
| Embodiment 1 | 1.30∶1 | Sodium methylate | 0.5 | Normal pressure | 72～74 | 2 |
| Embodiment 2 | 1.74∶1 | Potassium ethylate | 5 | 0.6 | 120 | 6 |
| Embodiment 3 | 1.45∶1 | Dibutyltin oxide | 1.5 | 0.29～0.31 | 87～90 | 2 |
| Embodiment 4 | 1.45∶1 | Butyl (tetra) titanate | 5.0 | Normal pressure | 30 | 6 |
| Embodiment 5 | 1.45∶1 | Dibutyltin oxide: butyl (tetra) titanate=1: 1 | 1.5 | 0.29～0.31 | 87～90 | 4 |
Table 2
| The morpholine transformation efficiency, % | Synthesis yield, % | Total recovery, % | Product purity, wt% | |
| Embodiment 1 | 85.6 | 85.1 | 80.9 | 99.58 |
| Embodiment 2 | 81.6 | 81.3 | 78.9 | 99.67 |
| Embodiment 3 | 93.4 | 92.9 | 88.5 | 99.54 |
| Embodiment 4 | 98.4 | 98.0 | 93.7 | 99.63 |
| Embodiment 5 | 98.7 | 98.2 | 94.5 | 99.74 |
Embodiment 6～10
21 static mixers among Fig. 2; 22 reactors; 23 flash tanks; 24 methyl-formiate condensers; 25 thin-film evaporators; 26 methanol condensers; 27 catalyst settlers (or strainer); 28 lights column; 29 light tower condensers; 210 light tower reboilers; 211 vacuum product towers; 212 product tower condensers; 213 product tower reboilers.Referring to N-N-formyl morpholine N-continuous production processes synoptic diagram (Fig. 2) will contain the methyl-formiate of specified amount catalyzer and morpholine respectively with volume pump by metering than squeezing in the static mixer 21, enter shell and tube reactor 22 (embodiment 6-7) or tower reactor 22 (embodiment 8-10) then and react and obtain thick product.
Effusive thick product drops to pressure through throttling valve and enters flash tank 23 behind the 0.15MPa and carry out flash distillation in the reactor, and the gas phase part is methyl-formiate after condensation, and liquid phase enters rotating thin film scraper-type vaporizer 25; Vaporizer liquid phase temperature out is controlled at 160～165 ℃, the gas phase part that the vaporizer top obtains, and as methanol product, the thick product of liquid phase is introduced lights column 28 after removing catalyzer after filtration after condensation; Lights column 28 (theoretical plate number 35, rectifying section/stripping section=19/16) tower still temperature is 158～162 ℃, and vacuum tightness is 0.088～0.090Mpa, and reflux ratio is 4～5, the morpholine cut that the overhead collection temperature is 97～100 ℃, leftover materials enter vacuum product tower 211; Vacuum product tower 211 (theoretical plate numbers 22, rectifying section/stripping section=10/12) tower still temperature is 164～168 ℃, and reflux ratio is 0.4～0.6, and vacuum tightness is 0.092～0.095MPa, the cut that cat head extraction temperature is 155～158 ℃ obtains N-N-formyl morpholine N-product after water cooler 212 coolings.Tower still high boiling material is (about 35kg/t product) seldom, is interrupted and discharges the oil production that acts as a fuel.The concrete reaction conditions of each embodiment sees Table 3, and reaction result sees Table 4.
Table 3
| Raw material weight is than (morpholine: methyl-formiate) | Catalyzer | Catalyst levels (%) | Reaction pressure (Mpa) | Temperature of reaction (℃) | Reaction time (h) | |
| Embodiment 6 | 1.30∶1 | Potassium methylate | 0.5 | Normal pressure | 72～74 | 2 |
| Embodiment 7 | 1.74∶1 | Sodium ethylate | 5 | 0.6 | 120 | 6 |
| Embodiment 8 | 1.45∶1 | Dioctyl tin oxide | 1.5 | 0.29～0.31 | 87～90 | 2 |
| Embodiment 9 | 1.45∶1 | Butyl (tetra) titanate | 3.0 | 0.29～0.31 | 87～90 | 4 |
| Embodiment 10 | 1.50∶1 | Dioctyl tin oxide: butyl (tetra) titanate=1: 1 | 1.5 | 0.29～0.31 | 87～90 | 4 |
Table 4
| The morpholine transformation efficiency, % | Synthesis yield, % | Total recovery, % | Product purity, wt% | |
| Embodiment 6 | 89.7 | 89.2 | 85.1 | 99.62 |
| Embodiment 7 | 80.7 | 80.4 | 77.3 | 99.56 |
| Embodiment 8 | 95.9 | 95.3 | 92.1 | 99.61 |
| Embodiment 9 | 97.6 | 97.2 | 94.7 | 99.58 |
| Embodiment 10 | 99.1 | 98.7 | 95.9 | 99.60 |
Claims (7)
1. the preparation method of a N-N-formyl morpholine N-, it is characterized in that: with methyl-formiate and morpholine is raw material, add transesterification catalyst, successive reaction in rhythmic reaction or the flow reactor in batch reactor, reaction product through intermittence separating technology or continuous separation technology obtain product N-N-formyl morpholine N-, wherein
Reaction conditions is:
The mass ratio of morpholine and methyl-formiate is 1.30～1.74: 1;
Catalyst levels accounts for 0.5～5% of raw material gross weight;
Reaction pressure is normal pressure～0.6Mpa;
Temperature of reaction is 30～120 ℃;
Reaction times is 2～6 hours;
Intermittently the separating technology operation comprises:
(1) Separation and Recovery of methyl-formiate: the rectifying separation reaction product, rectifier unit is made up of reactor and batch fractionating tower, rectifying pressure 0.1～0.2Mpa, 68～82 ℃ of temperature of reaction kettle, rectifying tower top is collected the methyl-formiate cut;
(2) Separation and Recovery of methyl alcohol: rectifying pressure is become normal pressure, 68～130 ℃ of temperature of reaction kettle, rectifying tower top is collected methanol fraction;
(3) Separation and Recovery of morpholine: will operate the thick product filtration that (2) obtain, and carry out rectification under vacuum behind the filtration catalizer, vacuum tightness is 0.09～0.099MPa, 130～155 ℃ of temperature of reaction kettle, overhead collection morpholine cut;
(4) acquisition of N-N-formyl morpholine N-: operation (3) vacuum tightness is constant, and temperature of reaction kettle becomes 155～165 ℃, overhead collection N-N-formyl morpholine N-;
The continuous separation technology operation comprises:
(1) Separation and Recovery of methyl-formiate: effusive reaction solution enters flash tank after through throttling valve pressure being dropped to normal pressure～0.2MPa in the reactor, and the gas phase part that flash distillation obtains obtains methyl-formiate after condensation, and liquid phase enters vaporizer;
(2) methyl alcohol Separation and Recovery: vaporizer liquid phase temperature out is controlled at 160～165 ℃, and the gas phase part in the vaporizer is as methanol product, and liquid phase part enters lights column after removing catalyzer after filtration;
(3) morpholine Separation and Recovery: lights column vacuum tightness is 0.08～0.09Mpa, and tower still temperature is 158～162 ℃, and cat head obtains the morpholine component, and leftover materials enter vacuum product tower;
(4) acquisition of N-N-formyl morpholine N-: vacuum product tower vacuum tightness is 0.09～0.099Mpa, 164～168 ℃ of tower still temperature, and cat head obtains the N-N-formyl morpholine N-.
2. the preparation method of N-N-formyl morpholine N-according to claim 1 is characterized in that: transesterification catalyst is sodium alkoxide, potassium alcoholate, organotin, titanic acid ester or their compound.
3. the preparation method of N-N-formyl morpholine N-according to claim 2 is characterized in that: transesterification catalyst is the compound of sodium methylate, potassium methylate, sodium ethylate, potassium ethylate, sodium tert-butoxide, potassium tert.-butoxide, Dibutyltin oxide, dioctyl tin oxide, butyl (tetra) titanate or above-mentioned substance.
4. the preparation method of N-N-formyl morpholine N-according to claim 1 is characterized in that: batch reactor is a stirred autoclave.
5. the preparation method of N-N-formyl morpholine N-according to claim 1 is characterized in that: flow reactor is to have the tubular type or the shell and tube reactor of hot-swap feature or have inner colded tower reactor.
6. the preparation method of N-N-formyl morpholine N-according to claim 1 is characterized in that: flow reactor internal reaction pressure is 0.2～0.6Mpa.
7. the preparation method of N-N-formyl morpholine N-according to claim 1 is characterized in that: the preparation method of N-N-formyl morpholine N-comprises rhythmic reaction and continuous separation technology combination, successive reaction and intermittently separating technology combination, full continuous processing combination or full batch technology combination.
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103641797A (en) * | 2013-09-11 | 2014-03-19 | 西南化工研究设计院有限公司 | Preparation method for N-acetyl morpholine |
| CN104513234A (en) * | 2014-12-28 | 2015-04-15 | 江苏天容集团股份有限公司 | Synthesis method for high-quality quizalofop-P-tefuryl |
| CN112619395A (en) * | 2020-12-22 | 2021-04-09 | 李通 | Tail gas absorption process for producing chloromethyl ethyl ether by high-purity hydrogen chloride method |
-
2005
- 2005-04-01 CN CNB2005100588921A patent/CN100548999C/en not_active Expired - Fee Related
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103641797A (en) * | 2013-09-11 | 2014-03-19 | 西南化工研究设计院有限公司 | Preparation method for N-acetyl morpholine |
| CN103641797B (en) * | 2013-09-11 | 2015-07-08 | 西南化工研究设计院有限公司 | Preparation method for N-acetyl morpholine |
| CN104513234A (en) * | 2014-12-28 | 2015-04-15 | 江苏天容集团股份有限公司 | Synthesis method for high-quality quizalofop-P-tefuryl |
| CN104513234B (en) * | 2014-12-28 | 2017-07-14 | 江苏天容集团股份有限公司 | A kind of method for synthesizing high-quality quizalofopPtefuryl |
| CN112619395A (en) * | 2020-12-22 | 2021-04-09 | 李通 | Tail gas absorption process for producing chloromethyl ethyl ether by high-purity hydrogen chloride method |
Also Published As
| Publication number | Publication date |
|---|---|
| CN100548999C (en) | 2009-10-14 |
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