CN114618390A - Fixed bed reactor for producing N-methylmorpholine by continuous method - Google Patents
Fixed bed reactor for producing N-methylmorpholine by continuous method Download PDFInfo
- Publication number
- CN114618390A CN114618390A CN202011445396.2A CN202011445396A CN114618390A CN 114618390 A CN114618390 A CN 114618390A CN 202011445396 A CN202011445396 A CN 202011445396A CN 114618390 A CN114618390 A CN 114618390A
- Authority
- CN
- China
- Prior art keywords
- bed reactor
- fixed bed
- fixedly connected
- main body
- reactor main
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
- SJRJJKPEHAURKC-UHFFFAOYSA-N N-Methylmorpholine Chemical compound CN1CCOCC1 SJRJJKPEHAURKC-UHFFFAOYSA-N 0.000 title claims abstract description 139
- 238000011437 continuous method Methods 0.000 title abstract description 14
- MTHSVFCYNBDYFN-UHFFFAOYSA-N diethylene glycol Chemical compound OCCOCCO MTHSVFCYNBDYFN-UHFFFAOYSA-N 0.000 claims abstract description 96
- BAVYZALUXZFZLV-UHFFFAOYSA-N Methylamine Chemical compound NC BAVYZALUXZFZLV-UHFFFAOYSA-N 0.000 claims abstract description 82
- 238000006243 chemical reaction Methods 0.000 claims abstract description 32
- 238000004519 manufacturing process Methods 0.000 claims abstract description 17
- 238000007789 sealing Methods 0.000 claims abstract description 13
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 claims description 30
- 238000009826 distribution Methods 0.000 claims description 29
- 239000003054 catalyst Substances 0.000 claims description 27
- 239000010949 copper Substances 0.000 claims description 22
- RYGMFSIKBFXOCR-UHFFFAOYSA-N Copper Chemical compound [Cu] RYGMFSIKBFXOCR-UHFFFAOYSA-N 0.000 claims description 21
- 229910052802 copper Inorganic materials 0.000 claims description 21
- 239000000377 silicon dioxide Substances 0.000 claims description 15
- 238000010924 continuous production Methods 0.000 claims description 14
- 235000012239 silicon dioxide Nutrition 0.000 claims description 14
- 239000002245 particle Substances 0.000 claims description 12
- 238000003756 stirring Methods 0.000 claims description 9
- 239000000706 filtrate Substances 0.000 claims description 6
- 239000010705 motor oil Substances 0.000 claims description 2
- 239000000853 adhesive Substances 0.000 claims 2
- 230000001070 adhesive effect Effects 0.000 claims 2
- 239000012716 precipitator Substances 0.000 claims 1
- 238000000034 method Methods 0.000 abstract description 24
- 230000008569 process Effects 0.000 abstract description 10
- 230000000694 effects Effects 0.000 abstract description 9
- 230000007246 mechanism Effects 0.000 abstract description 3
- 239000007789 gas Substances 0.000 description 16
- 239000012043 crude product Substances 0.000 description 15
- YNAVUWVOSKDBBP-UHFFFAOYSA-N Morpholine Chemical compound C1COCCN1 YNAVUWVOSKDBBP-UHFFFAOYSA-N 0.000 description 14
- 239000002994 raw material Substances 0.000 description 13
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 12
- 239000007788 liquid Substances 0.000 description 12
- 239000000463 material Substances 0.000 description 10
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 9
- 239000001257 hydrogen Substances 0.000 description 9
- 229910052739 hydrogen Inorganic materials 0.000 description 9
- 239000000047 product Substances 0.000 description 9
- 238000010586 diagram Methods 0.000 description 8
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 8
- 229910052757 nitrogen Inorganic materials 0.000 description 6
- 239000012495 reaction gas Substances 0.000 description 6
- 238000005086 pumping Methods 0.000 description 5
- 239000002002 slurry Substances 0.000 description 4
- 239000002904 solvent Substances 0.000 description 4
- 239000000126 substance Substances 0.000 description 4
- 230000009471 action Effects 0.000 description 3
- 238000001816 cooling Methods 0.000 description 3
- 238000007599 discharging Methods 0.000 description 3
- 238000011049 filling Methods 0.000 description 3
- 238000010438 heat treatment Methods 0.000 description 3
- 239000007791 liquid phase Substances 0.000 description 3
- 239000000203 mixture Substances 0.000 description 3
- 239000012071 phase Substances 0.000 description 3
- 230000009467 reduction Effects 0.000 description 3
- 238000005070 sampling Methods 0.000 description 3
- 239000007787 solid Substances 0.000 description 3
- 239000000243 solution Substances 0.000 description 3
- 230000000087 stabilizing effect Effects 0.000 description 3
- 229920001651 Cyanoacrylate Polymers 0.000 description 2
- RTZKZFJDLAIYFH-UHFFFAOYSA-N Diethyl ether Chemical compound CCOCC RTZKZFJDLAIYFH-UHFFFAOYSA-N 0.000 description 2
- MHAJPDPJQMAIIY-UHFFFAOYSA-N Hydrogen peroxide Chemical compound OO MHAJPDPJQMAIIY-UHFFFAOYSA-N 0.000 description 2
- 229920000433 Lyocell Polymers 0.000 description 2
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 description 2
- 239000004830 Super Glue Substances 0.000 description 2
- 230000032683 aging Effects 0.000 description 2
- 238000004458 analytical method Methods 0.000 description 2
- 230000015572 biosynthetic process Effects 0.000 description 2
- 238000004140 cleaning Methods 0.000 description 2
- 238000001125 extrusion Methods 0.000 description 2
- 238000004817 gas chromatography Methods 0.000 description 2
- 239000003292 glue Substances 0.000 description 2
- 238000011835 investigation Methods 0.000 description 2
- 230000011987 methylation Effects 0.000 description 2
- 238000007069 methylation reaction Methods 0.000 description 2
- 229920002635 polyurethane Polymers 0.000 description 2
- 239000004814 polyurethane Substances 0.000 description 2
- 238000003786 synthesis reaction Methods 0.000 description 2
- 230000002194 synthesizing effect Effects 0.000 description 2
- ZNSMNVMLTJELDZ-UHFFFAOYSA-N Bis(2-chloroethyl)ether Chemical compound ClCCOCCCl ZNSMNVMLTJELDZ-UHFFFAOYSA-N 0.000 description 1
- 241000196324 Embryophyta Species 0.000 description 1
- 229910002651 NO3 Inorganic materials 0.000 description 1
- 229920000297 Rayon Polymers 0.000 description 1
- 244000275012 Sesbania cannabina Species 0.000 description 1
- 229920001800 Shellac Polymers 0.000 description 1
- 230000002411 adverse Effects 0.000 description 1
- 150000001412 amines Chemical class 0.000 description 1
- 239000007864 aqueous solution Substances 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 239000003153 chemical reaction reagent Substances 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- NEHMKBQYUWJMIP-UHFFFAOYSA-N chloromethane Chemical compound ClC NEHMKBQYUWJMIP-UHFFFAOYSA-N 0.000 description 1
- 150000001875 compounds Chemical class 0.000 description 1
- XTVVROIMIGLXTD-UHFFFAOYSA-N copper(II) nitrate Chemical compound [Cu+2].[O-][N+]([O-])=O.[O-][N+]([O-])=O XTVVROIMIGLXTD-UHFFFAOYSA-N 0.000 description 1
- 230000007797 corrosion Effects 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 230000018044 dehydration Effects 0.000 description 1
- 238000006297 dehydration reaction Methods 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 230000018109 developmental process Effects 0.000 description 1
- ZBCBWPMODOFKDW-UHFFFAOYSA-N diethanolamine Chemical compound OCCNCCO ZBCBWPMODOFKDW-UHFFFAOYSA-N 0.000 description 1
- 229940043237 diethanolamine Drugs 0.000 description 1
- 230000009977 dual effect Effects 0.000 description 1
- 229920001971 elastomer Polymers 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
- 238000012840 feeding operation Methods 0.000 description 1
- 239000000835 fiber Substances 0.000 description 1
- 239000012065 filter cake Substances 0.000 description 1
- 238000001914 filtration Methods 0.000 description 1
- 239000012847 fine chemical Substances 0.000 description 1
- 239000006260 foam Substances 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 239000010842 industrial wastewater Substances 0.000 description 1
- 239000003112 inhibitor Substances 0.000 description 1
- 210000000936 intestine Anatomy 0.000 description 1
- 239000002085 irritant Substances 0.000 description 1
- 231100000021 irritant Toxicity 0.000 description 1
- 238000011068 loading method Methods 0.000 description 1
- WSFSSNUMVMOOMR-NJFSPNSNSA-N methanone Chemical compound O=[14CH2] WSFSSNUMVMOOMR-NJFSPNSNSA-N 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000007935 neutral effect Effects 0.000 description 1
- 229910000510 noble metal Inorganic materials 0.000 description 1
- 239000003921 oil Substances 0.000 description 1
- 229920000728 polyester Polymers 0.000 description 1
- 239000000843 powder Substances 0.000 description 1
- 239000002964 rayon Substances 0.000 description 1
- 238000011160 research Methods 0.000 description 1
- 239000011265 semifinished product Substances 0.000 description 1
- 239000004208 shellac Substances 0.000 description 1
- ZLGIYFNHBLSMPS-ATJNOEHPSA-N shellac Chemical compound OCCCCCC(O)C(O)CCCCCCCC(O)=O.C1C23[C@H](C(O)=O)CCC2[C@](C)(CO)[C@@H]1C(C(O)=O)=C[C@@H]3O ZLGIYFNHBLSMPS-ATJNOEHPSA-N 0.000 description 1
- 229940113147 shellac Drugs 0.000 description 1
- 235000013874 shellac Nutrition 0.000 description 1
- XJKVPKYVPCWHFO-UHFFFAOYSA-N silicon;hydrate Chemical compound O.[Si] XJKVPKYVPCWHFO-UHFFFAOYSA-N 0.000 description 1
- 229910000029 sodium carbonate Inorganic materials 0.000 description 1
- 238000009987 spinning Methods 0.000 description 1
- 239000003381 stabilizer Substances 0.000 description 1
- QAOWNCQODCNURD-UHFFFAOYSA-N sulfuric acid Substances OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 1
- 239000004094 surface-active agent Substances 0.000 description 1
- 150000003512 tertiary amines Chemical class 0.000 description 1
- 238000012360 testing method Methods 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
Images
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
- B01J8/0278—Feeding reactive fluids
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07D—HETEROCYCLIC COMPOUNDS
- C07D295/00—Heterocyclic compounds containing polymethylene-imine rings with at least five ring members, 3-azabicyclo [3.2.2] nonane, piperazine, morpholine or thiomorpholine rings, having only hydrogen atoms directly attached to the ring carbon atoms
- C07D295/02—Heterocyclic compounds containing polymethylene-imine rings with at least five ring members, 3-azabicyclo [3.2.2] nonane, piperazine, morpholine or thiomorpholine rings, having only hydrogen atoms directly attached to the ring carbon atoms containing only hydrogen and carbon atoms in addition to the ring hetero elements
- C07D295/023—Preparation; Separation; Stabilisation; Use of additives
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07D—HETEROCYCLIC COMPOUNDS
- C07D295/00—Heterocyclic compounds containing polymethylene-imine rings with at least five ring members, 3-azabicyclo [3.2.2] nonane, piperazine, morpholine or thiomorpholine rings, having only hydrogen atoms directly attached to the ring carbon atoms
- C07D295/02—Heterocyclic compounds containing polymethylene-imine rings with at least five ring members, 3-azabicyclo [3.2.2] nonane, piperazine, morpholine or thiomorpholine rings, having only hydrogen atoms directly attached to the ring carbon atoms containing only hydrogen and carbon atoms in addition to the ring hetero elements
- C07D295/027—Heterocyclic compounds containing polymethylene-imine rings with at least five ring members, 3-azabicyclo [3.2.2] nonane, piperazine, morpholine or thiomorpholine rings, having only hydrogen atoms directly attached to the ring carbon atoms containing only hydrogen and carbon atoms in addition to the ring hetero elements containing only one hetero ring
- C07D295/03—Heterocyclic compounds containing polymethylene-imine rings with at least five ring members, 3-azabicyclo [3.2.2] nonane, piperazine, morpholine or thiomorpholine rings, having only hydrogen atoms directly attached to the ring carbon atoms containing only hydrogen and carbon atoms in addition to the ring hetero elements containing only one hetero ring with the ring nitrogen atoms directly attached to acyclic carbon atoms
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The invention discloses a fixed bed reactor for producing N-methylmorpholine by a continuous method, which comprises a fixed bed reactor main body, wherein the upper end of the fixed bed reactor main body is fixedly connected with an upper cover, the upper end of the upper cover is fixedly connected with a lifting ring and a feeding port, an inlet distributor is arranged in the feeding port, an online oil inlet is fixed on the outer side of the upper cover, and a diethylene glycol feeding pump and a monomethylamine feeding pump are fixedly connected to one side of the fixed bed reactor main body. The fixed bed reactor for producing the N-methylmorpholine by the continuous method can realize continuous feeding, has high reaction selectivity, obviously improves the production capacity of the device, has stable process and more stable product quality compared with a kettle type reactor adopted in the prior art, can be disassembled and assembled at the bottom through the lifting mechanism, is convenient to clean the inside, increases the reaction effect, has excellent sealing performance, and brings better use prospect.
Description
Technical Field
The invention relates to the field of organic synthesis, in particular to a fixed bed reactor for producing N-methylmorpholine by a continuous method.
Background
N-methylmorpholine is an important organic chemical intermediate, is a colorless to yellow liquid compound with amine taste, has a chemical formula of C5H11NO, a CAS number of 109-02-4 and a molecular weight of 101.15, has dual properties of tertiary amine and ether, is widely used as a chemical intermediate, an extracting agent, a corrosion inhibitor, a surfactant and the like, is used as a catalyst of polyester polyurethane flexible block foam in the polyurethane industry, is used as a solvent (an excellent solvent of dye, casomo, wax, shellac and the like), is used as a stabilizer and an analytical reagent of chlorocarbon, is also used for synthesizing a rubber accelerator and other fine chemicals, can be oxidized by hydrogen peroxide to synthesize N-methylmorpholine, is a spinning solvent of Lyocell (commonly known as tencel) and Newcel rayon filament which are currently called green fibers, and can also be used as a solvent for producing plant intestines, with the continuous development of science and technology, people have higher and higher requirements on the manufacturing process of N-methylmorpholine.
The existing N-methylmorpholine has certain disadvantages when in use, firstly, the synthesis process of the N-methylmorpholine is multiple, according to the raw materials, the morpholine method, the N-methyl diethanol method, the diethanol amine method, the diethylene glycol method and the dichloroethyl ether method are available, wherein the research on methylation by taking morpholine as the raw material is the most, and the method is also an important method for synthesizing the N-methylmorpholine, the morpholine methylation method has high price of the raw material morpholine, needs a noble metal catalyst, has high production cost, simultaneously produces a large amount of industrial wastewater containing formaldehyde, is difficult to treat, other methods basically adopt concentrated sulfuric acid for dehydration, has high three wastes and low yield, brings certain adverse effects to the use process of people, in addition, the interior of the device can not be cleaned conveniently, the scale formation condition is easy to occur during the use time, and the reaction effect is reduced, for this purpose, we propose a fixed bed reactor for the continuous process for the production of N-methylmorpholine.
Disclosure of Invention
Technical problem to be solved
Aiming at the defects of the prior art, the invention provides a fixed bed reactor for producing N-methylmorpholine by a continuous method, which can realize continuous feeding, and compared with a kettle type reactor adopted in the prior art, the production capacity of the device is obviously improved, and the product content is high (more than 99.5%); in addition, the process route of the raw materials of diethylene glycol and monomethylamine is adopted, the raw material cost is low, the selectivity of N-methylmorpholine is more than 92%, the bottom of the N-methylmorpholine can be disassembled and assembled through a lifting mechanism, the inside of the N-methylmorpholine can be conveniently cleaned, the reaction effect is improved, the sealing performance is excellent, and the problems in the background art can be effectively solved.
(II) technical scheme
In order to achieve the purpose, the invention adopts the technical scheme that: a fixed bed reactor for producing N-methylmorpholine by a continuous method comprises a fixed bed reactor main body, wherein the upper end of the fixed bed reactor main body is fixedly connected with an upper cover, the upper end of the upper cover is fixedly connected with a lifting ring and a feeding port, an inlet distributor is arranged inside the feeding port, an online oil inlet is fixed on the outer side of the upper cover, a diethylene glycol feeding pump and a monomethylamine feeding pump are fixedly connected to one side of the fixed bed reactor main body, an upper passage port and a lower passage port are fixedly connected to the other side of the fixed bed reactor main body, a reaction tank is arranged inside the fixed bed reactor main body, a first supporting base and a second supporting base are fixedly connected to the outer wall of the lower end of the fixed bed reactor main body, a detachable bottom cover is arranged at the lower end of the fixed bed reactor main body, and a positioning support and a discharge port are fixedly connected to the lower end of the detachable bottom cover, an outlet collector is arranged inside the discharge port, and a lifting support is fixedly connected to the lower end of the positioning support.
As a preferred technical scheme, the inside fixedly connected with location chassis of removable bottom, the upper end fixedly connected with location outer lane and the location inner circle of removable bottom, the location outer lane is located the outer lane of location inner circle, the outer wall fixedly connected with of location inner circle is sealed to fill up, the upper end swing joint on location chassis has the puddler, the outer wall fixedly connected with stirring vane of puddler.
As a preferred technical scheme, the inner wall of the upper end of the fixed bed reactor main body is fixedly connected with a multifunctional distribution disc, the inner part of the multifunctional distribution disc is fixedly connected with a distribution frame, the outer wall of the multifunctional distribution disc is fixedly connected with a fixed frame, the lower end of the multifunctional distribution disc is provided with a depositor, threads and a clamping ring are arranged between the multifunctional distribution disc and the depositor, and the outer wall of the depositor is provided with a filtrate port.
As an optimal technical scheme, a first fixing frame is arranged between the fixed bed reactor main body and the diglycol feeding pump and the monomethylamine feeding pump, one side of the fixed bed reactor main body is fixedly connected with one end of the diglycol feeding pump and one end of the monomethylamine feeding pump through the first fixing frame, a second fixing frame is arranged between the fixed bed reactor main body and the upper-layer channel opening and between the fixed bed reactor main body and the lower-layer channel opening, and the other side of the fixed bed reactor main body is fixedly connected with one end of the lower-layer channel opening through the second fixing frame.
As a preferred technical scheme, positioning seats are arranged between the detachable bottom cover and the positioning inner ring and between the detachable bottom cover and the positioning outer ring, the upper end of the detachable bottom cover is fixedly connected with the lower ends of the positioning inner ring and the positioning outer ring through the positioning seats, a strong glue is arranged between the positioning inner ring and the sealing gasket, and the outer surface of the positioning inner ring is fixedly connected with the inner surface of the sealing gasket through the strong glue.
As a preferred technical scheme, the lower end of the multifunctional distribution disc is detachably connected with the upper end of the depositor through threads and a clamping ring, a positioning piece is arranged between the multifunctional distribution disc and the distribution frame, and the interior of the multifunctional distribution disc is fixedly connected with the outer wall of the distribution frame through the positioning piece.
In a preferred embodiment, the fixed-bed reactor main body is formed by stacking silica-supported copper catalyst particles having a particle diameter of Φ 5 × (4 to 5) mm, and the silica-supported copper catalyst is composed of the following components in parts by weight: 20-60% of copper and 30-80% of silicon dioxide.
As a preferable technical scheme, the reaction temperature in the fixed bed reactor main body is 200-260 ℃, the reaction pressure in the fixed bed reactor main body is 0.5-1.0Mpa, and the circulating gas quantity of the circulating pump in the fixed bed reactor main body is 30-60L/h.
(III) advantageous effects
Compared with the prior art, the invention provides a fixed bed reactor for producing N-methylmorpholine by a continuous method, which has the following beneficial effects: the fixed bed reactor for producing the N-methylmorpholine by the continuous method has the advantages that the bottom can be disassembled and assembled through the lifting mechanism, the inside can be conveniently cleaned, the reaction effect is improved, the sealing performance is excellent, the continuous feeding can be realized, the reaction selectivity is high compared with a kettle type reactor adopted in the prior art, the production capacity of the device is obviously improved, the process is stable, the product quality is more stable, in addition, a process route of raw materials of diethylene glycol and monomethylamine is adopted, the raw material cost is low, the obtained crude product is directly used for a rectification step to obtain a product, the excessive monomethylamine can be circularly applied, the operation is simple, no corrosive or irritant substances are generated in the production process, only a small amount of water is generated, the production equipment cannot be corroded, the environmental pollution cannot be generated, the fixed bed reactor belongs to clean production, the continuous feeding can be realized, compared with the kettle type reactor adopted in the prior art, the production capacity of the device is obviously improved, and the product content is high (more than 99.5%); in addition, the process route of the raw materials of diethylene glycol and monomethylamine is adopted, the raw material cost is low, the selectivity of N-methylmorpholine is more than 92%, the fixed bed reactor provided by the invention can be used for continuously producing N-methylmorpholine, the purity of a crude product reaches more than 95.9%, the yield is more than 95%, the crude product is a semi-finished product, the conversion rate of a target product represented by the crude product is high, the conversion rate is high, the yield is high, the whole N-methylmorpholine has a simple structure, the operation is convenient, and the using effect is better than that of a traditional mode.
Drawings
FIG. 1 is a schematic diagram of the overall structure of a fixed bed reactor for producing N-methylmorpholine by a continuous method.
FIG. 2 is a schematic diagram of a detachable base of a fixed bed reactor for producing N-methylmorpholine by a continuous method.
FIG. 3 is a schematic view of a multifunctional distribution plate of a fixed bed reactor for producing N-methylmorpholine by a continuous method.
FIG. 4 is a schematic diagram of a depositor of a fixed bed reactor for the continuous production of N-methylmorpholine according to the present invention.
FIG. 5 is a schematic diagram of the overall structure of a fixed bed reactor for producing N-methylmorpholine by a continuous process according to the present invention.
FIG. 6 is a structural diagram of a structural formula of a target product N-methylmorpholine in a fixed bed reactor for producing N-methylmorpholine by a continuous method.
FIG. 7 is a schematic diagram of the structure for examining the copper loading in a fixed bed reactor for the continuous process for producing N-methylmorpholine according to the present invention.
FIG. 8 is a schematic structural diagram of an analysis table of investigation results in a fixed bed reactor for producing N-methylmorpholine by a continuous process.
FIG. 9 is a schematic structural diagram of an analysis table of crude product investigation results in a fixed bed reactor for continuous production of N-methylmorpholine according to the present invention.
In the figure: 1. a fixed bed reactor main body; 2. a hoisting ring; 3. a liquid inlet; 4. a diethylene glycol feed pump; 5. a monomethylamine feed pump; 6. a first support base; 7. an outlet collector; 8. a discharge port; 9. a feeding port; 10. an inlet distributor; 11. an upper cover; 12. a dispensing shelf; 13. an upper layer channel port; 14. a reaction tank; 15. a lower layer channel port; 16. a removable bottom cover; 17. a second support base; 18. a lifting support; 19. a stirring sheet; 20. positioning the inner ring; 21. positioning the outer ring; 22. positioning the bracket; 23. a stirring rod; 24. a gasket; 25. positioning the chassis; 26. a fixed mount; 27. a multifunctional distribution tray; 28. a depositor; 29. a filtrate port; 30. a thread; 31. and a collar.
Detailed Description
In order to make the technical means, the creation characteristics, the achievement purposes and the effects of the invention easy to understand, the invention is further explained by combining the specific embodiments.
As shown in figures 1-9, a fixed bed reactor for producing N-methylmorpholine by a continuous method comprises a fixed bed reactor main body 1, an upper cover 11 is fixedly connected to the upper end of the fixed bed reactor main body 1, a hanging ring 2 and a feeding port 9 are fixedly connected to the upper end of the upper cover 11, an inlet distributor 10 is arranged inside the feeding port 9, an engine oil inlet 3 is fixedly connected to the outer side of the upper cover 11, a diethylene glycol feeding pump 4 and a methylamine feeding pump 5 are fixedly connected to one side of the fixed bed reactor main body 1, an upper passage port 13 and a lower passage port 15 are fixedly connected to the other side of the fixed bed reactor main body 1, a reaction tank 14 is arranged inside the fixed bed reactor main body 1, a first support base 6 and a second support base 17 are fixedly connected to the outer wall of the lower end of the fixed bed reactor main body 1, a detachable bottom cover 16 is arranged at the lower end of the fixed bed reactor main body 1, the lower end of the detachable bottom cover 16 is fixedly connected with a positioning support 22 and a discharge hole 8, an outlet collector 7 is arranged inside the discharge hole 8, and the lower end of the positioning support 22 is fixedly connected with a lifting support 18.
Further, the inside fixedly connected with location chassis 25 of removable bottom 16, the upper end fixedly connected with location outer lane 21 and the location inner circle 20 of removable bottom 16, location outer lane 21 is located the outer lane of location inner circle 20, and the outer wall fixedly connected with that fixes a position inner circle 20 fills up 24, and the upper end swing joint on location chassis 25 has puddler 23, and the outer wall fixedly connected with stirring vane 19 of puddler 23 is convenient for carry out dismouting cleaning operation.
Further, the upper end inner wall fixedly connected with of fixed bed reactor main part 1 has multi-functional plate 27 of distributor, and the inside fixedly connected with of multi-functional plate 27 distributes frame 12, and the outer wall fixedly connected with mount 26 of multi-functional plate 27 of distributor, the lower extreme of multi-functional plate 27 of distributor are provided with depositor 28, are provided with screw thread 30 and rand 31 between multi-functional plate 27 of distributor and the depositor 28, and filtrate mouth 29 has been seted up to the outer wall of depositor 28, and the convenient better filters the material.
Further, a fixing frame is arranged between the fixed bed reactor main body 1 and the diglycol feeding pump 4 and between the monomethylamine feeding pump 5, one side of the fixed bed reactor main body 1 is fixedly connected with one end of the diglycol feeding pump 4 and one end of the monomethylamine feeding pump 5 through the fixing frame, a fixing frame is arranged between the fixed bed reactor main body 1 and the upper-layer channel opening 13 and between the fixed bed reactor main body 1 and the lower-layer channel opening 15, and the other side of the fixed bed reactor main body 1 is fixedly connected with one end of the lower-layer channel opening 15 through the fixing frame, so that material feeding operation is facilitated.
Furthermore, positioning seats are arranged between the detachable bottom cover 16 and the positioning inner ring 20 and between the detachable bottom cover 16 and the positioning outer ring 21, the upper end of the detachable bottom cover 16 is fixedly connected with the lower ends of the positioning inner ring 20 and the positioning outer ring 21 through the positioning seats, a super glue is arranged between the positioning inner ring 20 and the sealing gasket 24, the outer surface of the positioning inner ring 20 is fixedly connected with the inner surface of the sealing gasket 24 through the super glue, and sealing and dismounting are facilitated.
Further, the lower end of the multifunctional distribution tray 27 is detachably connected with the upper end of the depositor 28 through threads 30 and a clamping ring 31, a positioning member is arranged between the multifunctional distribution tray 27 and the distribution frame 12, and the interior of the multifunctional distribution tray 27 is fixedly connected with the outer wall of the distribution frame 12 through the positioning member, so that the distribution operation is facilitated.
Further, the fixed bed reactor main body 1 is formed by stacking silicon dioxide supported copper catalyst particles with the particle size of phi 5 x 4-5 mm, and the silicon dioxide supported copper catalyst comprises the following components in parts by weight: 20-60% of copper and 30-80% of silicon dioxide.
Further, the reaction temperature in the fixed bed reactor main body 1 is 200-.
Example 1:
the fixed bed reactor main body 1 is formed by stacking silicon dioxide supported copper catalyst particles with the particle size of phi 5 x (4-5) mm, and the thickness of the silicon dioxide supported copper catalyst particles is 40 cm; composition of copper on silica catalyst (weight): 35% of copper and 65% of silicon dioxide.
Example 2:
the fixed bed reactor main body 1 is formed by stacking silicon dioxide supported copper catalyst particles with the particle size of phi 5 x (4-5) mm, and the thickness of the silicon dioxide supported copper catalyst particles is 60 cm; composition of silica-supported copper catalyst (by weight): 45% of copper and 55% of silicon dioxide.
Example 3: reduction and pretreatment of the catalyst: after the fixed bed reactor main body 1 is filled, pressure test is carried out under 1.8-2.0MPa, no obvious gas leakage exists, nitrogen and hydrogen are replaced, mixed gas with the volume ratio of 4:1 of nitrogen and hydrogen is used for passing through a catalyst bed layer, the catalyst bed layer is gradually heated to 280 ℃ and continuously aged for 72 hours, then the temperature is reduced to 220 ℃ for standby, and N-methylmorpholine is prepared: filling hydrogen into a fixed bed reactor to 0.4Mpa, stabilizing the temperature of a bed layer at about 220 ℃, continuously pumping monomethylamine (the pump speed is 4ml/min) by a metering pump, starting a circulating pump, circulating reaction gas, adjusting a frequency converter to ensure that the circulating gas amount is 30L/h, sampling after 2 hours, detecting that the concentration of the monomethylamine is more than 40%, starting to continuously pump raw material diethylene glycol into a tubular reactor of the fixed bed reactor containing a copper-filled catalyst bed layer by the metering pump, carrying out gas, liquid and solid three-phase reaction, simultaneously reducing the flow rate of the monomethylamine to 0.6ml/min, reducing the flow rate of the diethylene glycol to 1ml/min, wherein the molar ratio of the diethylene glycol to the monomethylamine is as follows: diethylene glycol is 1.24:1, the reaction temperature is 220 ℃, the reaction pressure is 0.8-0.9 MPa, a high-pressure circulating gas pump circulates reaction gas at 30L/h, the reaction is continuously carried out for 6 hours, materials are cooled by a condenser, a liquid-phase crude product is discharged, the crude product is heated to remove redundant monomethylamine (the monomethylamine is recycled), a small amount of generated water is removed, and 400g of liquid is obtained, and the GC analysis shows that the diethylene glycol is 2.3%, the methylmorpholine is 94.2%, and the morpholine is 2.2%. The crude product was rectified by a 80cm rectification column to obtain 358g of finished product (content: 99.5%) with a yield of 93.5%.
Example 4: reduction and pretreatment of the catalyst: after the fixed bed catalyst (prepared according to the method of example 1) was filled, the pressure was tested at 1.8-2.0MPa without significant gas leakage, nitrogen, after hydrogen replacement, with nitrogen: and (2) passing a mixed gas with hydrogen of 4:1 (volume ratio) through a catalyst bed, gradually heating the catalyst bed to 280 ℃ and continuously aging for 72 hours, and then cooling to 240 ℃ for later use to prepare N-methylmorpholine: filling hydrogen into a fixed bed reactor to 0.4Mpa, stabilizing the temperature of a bed layer at about 220 ℃, continuously pumping monomethylamine (the pump speed is 4ml/min) by a metering pump, starting a circulating pump, circulating reaction gas, adjusting a frequency converter to enable the circulating gas flow to be 50L/h, sampling after 2 hours, detecting that the concentration of the monomethylamine is more than 40%, starting to continuously pump raw material diethylene glycol into a tubular reactor of the fixed bed reactor containing a copper-filled catalyst bed layer by the metering pump, carrying out gas, liquid and solid three-phase reaction, simultaneously reducing the flow rate of the monomethylamine to 1ml/min, reducing the flow rate of the diethylene glycol to 1ml/min, wherein the molar ratio of the diethylene glycol to the monomethylamine is as follows: the method comprises the following steps of 1: 2 of diethylene glycol, reacting at 240 ℃, reacting at 0.5-0.6 MPa, circulating reaction gas at 50L/h by a high-pressure circulating gas pump, continuously reacting for 6 hours, cooling materials by a condenser, discharging a liquid-phase crude product, heating the crude product to remove redundant monomethylamine (recovering and utilizing monomethylamine), and removing a small amount of generated water to obtain 398g of liquid, wherein the liquid is analyzed by GC, and the diethylene glycol, the methylmorpholine and the morpholine are 1.4%, 95.4% and 2.2%. The crude product was rectified by a 80cm rectification column to obtain 360g of finished product (content: 99.6%) with a yield of 94%.
Example 5: reduction and pretreatment of the catalyst: after the fixed bed reactor main body 1 is filled, the pressure is tested at 1.8-2.0MPa, no obvious air leakage exists, and after nitrogen and hydrogen are replaced, the nitrogen is used: passing a mixed gas with hydrogen of 4:1 (volume ratio) through a catalyst bed, gradually heating the catalyst bed to 280 ℃, continuously aging for 72 hours, then cooling to 260 ℃ for later use, and preparing N-methylmorpholine: filling hydrogen into a fixed bed reactor to 0.4Mpa, stabilizing the temperature of a bed layer at about 240 ℃, continuously pumping monomethylamine (the pump speed is 4ml/min) by a metering pump, starting a circulating pump, circulating reaction gas, adjusting a frequency converter to ensure that the circulating gas amount is 60L/h, sampling after 2 hours, detecting that the concentration of the monomethylamine is more than 40%, starting to continuously pump raw material diethylene glycol into a tubular reactor of the fixed bed reactor containing a copper-filled catalyst bed layer by the metering pump, carrying out gas, liquid and solid three-phase reaction, simultaneously reducing the flow rate of the monomethylamine to 3ml/min, reducing the flow rate of the diethylene glycol to 1ml/min, and leading the molar ratio of the diethylene glycol to the monomethylamine: diethylene glycol 6.1:1, the reaction temperature is 260 ℃, the reaction pressure is 0.7-0.8 MPa, a high-pressure circulating gas pump circulates reaction gas at 60L/h, the reaction is continuously carried out for 6 hours, materials are cooled by a condenser, a liquid-phase crude product is discharged, the crude product is heated to remove redundant monomethylamine (monomethylamine is recycled), a small amount of generated water is removed, and 401g of liquid is obtained, wherein the content of diethylene glycol is 0.4%, methylmorpholine is 95.9%, and morpholine is 1.2% by GC analysis. The crude product is rectified by a rectifying column of 80cm to obtain 365g of finished product (the content: 99.6%) with the yield of 95.3%.
The working principle is as follows: the invention comprises a fixed bed reactor main body 1, a lifting ring 2, a liquid inlet 3, a diglycol feed pump 4, a monomethylamine feed pump 5, a first support base 6, an outlet collector 7, a discharge outlet 8, a feed inlet 9, an inlet distributor 10, an upper cover 11, a distribution frame 12, an upper layer channel port 13, a reaction tank 14, a lower layer channel port 15, a detachable bottom cover 16, a second support base 17, a lifting support 18, a stirring sheet 19, a positioning inner ring 20, a positioning outer ring 21, a positioning support 22, a stirring rod 23, a sealing gasket 24, a positioning base plate 25, a fixing frame 26, a multifunctional distribution plate 27, a depositor 28, a filtrate port 29, a thread 30 and a clamping ring 31, wherein diglycol and monomethylamine are input into the fixed bed reactor main body 1 through the diglycol feed pump 4 and the monomethylamine feed pump 5 during use, react in the reaction tank 14, and materials enter from the position of the feed inlet 9, the material is distributed through an inlet distributor 10, the material is discharged from a discharge port 8 after reaction, an outlet collector 7 has the function of discharging material distribution, a first support base 6 and a second support base 17 are convenient to support, when cleaning is carried out, the position of a lifting support 18 is lowered to drive a detachable bottom cover 16, a positioning inner ring 20 and a positioning outer ring 21 to descend so as to be separated from a fixed bed reactor main body 1, the positioning inner ring 20 and the positioning outer ring 21 respectively clamp the position of the fixed bed reactor main body 1, a sealing gasket 24 has a good sealing effect to prevent leakage, a stirring rod 23 rotates at the upper end of a positioning chassis 25 and is stirred through a stirring sheet 19, material liquid enters the position of a feeding port 9 and then is distributed to the position of a multifunctional distribution disc 27, and is deposited through a depositor 28, the filtrate port 29 is convenient for discharging the feed liquid and filtering impurities, and is more practical, Cu (NO3) 2.3H 2O is dissolved in water, carrier silicon dioxide and water are stirred into slurry in a kettle, simultaneously sodium carbonate aqueous solution (20 percent) and copper nitrate solution are dripped, finally the slurry solution is ensured to be neutral (PH is 7), the slurry solution is aged in a water bath at 50 +/-5 ℃ for 5 +/-1H, the slurry is centrifuged, an extrusion assistant sesbania powder is added into a filter cake, a little water is uniformly stirred, the mixture is extruded and formed by a strip extrusion machine, a cylinder with the diameter of 5mm multiplied by 5mm is cut into cylinders, the cylinders are dried, then the cylinders are roasted at the temperature of 500 ℃ for 10H and cooled to the normal temperature for standby, diethylene glycol and monomethylamine are used as raw materials, diethylene glycol and monomethylamine are continuously pumped into feed by a diethylene glycol feed pump 4 and a monomethylamine feed pump 5, the molar ratio of the diethylene glycol to the monomethylamine is 1: 1.2-8, the pumping speed of the diethylene glycol is 1-3ml/min, and the pumping speed of the monomethylamine is 0.6-6ml/min, the reaction pressure of the system is 0.5-1.0MPa, the reaction temperature is 200-260 ℃, the circulating gas flow of a circulating pump is 30-60L/h, and the crude product of the N-methylmorpholine is obtained after the reaction is finished.
It is noted that, herein, relational terms such as first and second (a, b, etc.) and the like may be used solely to distinguish one entity or action from another entity or action without necessarily requiring or implying any actual such relationship or order between such entities or actions. Also, the terms "comprises," "comprising," or any other variation thereof, are intended to cover a non-exclusive inclusion, such that a process, method, article, or apparatus that comprises a list of elements does not include only those elements but may include other elements not expressly listed or inherent to such process, method, article, or apparatus. Without further limitation, an element defined by the phrase "comprising an … …" does not exclude the presence of other identical elements in the process, method, article, or apparatus that comprises the element.
The foregoing shows and describes the general principles and broad features of the present invention and advantages thereof. It will be understood by those skilled in the art that the present invention is not limited to the embodiments described above, which are described in the specification and illustrated only to illustrate the principle of the present invention, but that various changes and modifications may be made therein without departing from the spirit and scope of the present invention, which fall within the scope of the invention as claimed. The scope of the invention is defined by the appended claims and equivalents thereof.
Claims (8)
1. A fixed bed reactor for the continuous production of N-methylmorpholine, comprising a fixed bed reactor body (1), characterized in that: the upper end of the fixed bed reactor main body (1) is fixedly connected with an upper cover (11), the upper end of the upper cover (11) is fixedly connected with a lifting ring (2) and a feeding port (9), an inlet distributor (10) is arranged in the feeding port (9), an engine oil inlet (3) is fixedly connected to the outer side of the upper cover (11), a diethylene glycol feeding pump (4) and a monomethylamine feeding pump (5) are fixedly connected to one side of the fixed bed reactor main body (1), an upper passage port (13) and a lower passage port (15) are fixedly connected to the other side of the fixed bed reactor main body (1), a reaction tank (14) is arranged in the fixed bed reactor main body (1), a first supporting base (6) and a second supporting base (17) are fixedly connected to the outer wall of the lower end of the fixed bed reactor main body (1), a detachable bottom cover (16) is arranged at the lower end of the fixed bed reactor main body (1), the lower end of the detachable bottom cover (16) is fixedly connected with a positioning support (22) and a discharge hole (8), an outlet collector (7) is arranged inside the discharge hole (8), and the lower end of the positioning support (22) is fixedly connected with a lifting support (18).
2. A fixed bed reactor for the continuous process for the production of N-methylmorpholine according to claim 1, characterized in that: the inside fixedly connected with location chassis (25) of removable bottom (16), the upper end fixedly connected with location outer lane (21) and the location inner circle (20) of removable bottom (16), location outer lane (21) are located the outer lane of location inner circle (20), the sealed pad (24) of outer wall fixedly connected with of location inner circle (20), the upper end swing joint on location chassis (25) has puddler (23), the outer wall fixedly connected with stirring piece (19) of puddler (23).
3. A fixed bed reactor for the continuous process for the production of N-methylmorpholine according to claim 1, characterized in that: the upper end inner wall fixedly connected with of fixed bed reactor main part (1) multi-functional plate (27) of distributor, the inside fixedly connected with distribution frame (12) of multi-functional plate (27) of distributor, outer wall fixedly connected with mount (26) of multi-functional plate (27) of distributor, the lower extreme of multi-functional plate (27) of distributor is provided with depositor (28), be provided with screw thread (30) and rand (31) between multi-functional plate (27) of distributor and depositor (28), filtrate mouth (29) have been seted up to the outer wall of depositor (28).
4. A fixed bed reactor for the continuous process for the production of N-methylmorpholine according to claim 1, characterized in that: be provided with the mount No. one between fixed bed reactor main part (1) and diglycol charge pump (4), monomethylamine charge pump (5), the one end fixed connection through mount and diglycol charge pump (4), monomethylamine charge pump (5) in fixed bed reactor main part (1) one side, be provided with the mount No. two between fixed bed reactor main part (1) and upper passway (13), lower floor passway (15), the one end fixed connection of mount and lower floor passway (15) is passed through to the opposite side of fixed bed reactor main part (1).
5. A fixed bed reactor for the continuous process for the production of N-methylmorpholine according to claim 2, characterized in that: the positioning seat is arranged between the detachable bottom cover (16) and the positioning inner ring (20) and between the detachable bottom cover (16) and the positioning outer ring (21), the upper end of the detachable bottom cover (16) is fixedly connected with the lower ends of the positioning inner ring (20) and the positioning outer ring (21) through the positioning seat, a strong adhesive is arranged between the positioning inner ring (20) and the sealing gasket (24), and the outer surface of the positioning inner ring (20) is fixedly connected with the inner surface of the sealing gasket (24) through the strong adhesive.
6. A fixed bed reactor for the continuous process for the production of N-methylmorpholine according to claim 3, characterized in that: the lower end of the multifunctional distribution disc (27) is detachably connected with the upper end of the precipitator (28) through threads (30) and a clamping ring (31), a positioning piece is arranged between the multifunctional distribution disc (27) and the distribution frame (12), and the inner part of the multifunctional distribution disc (27) is fixedly connected with the outer wall of the distribution frame (12) through the positioning piece.
7. A fixed bed reactor for the continuous process for the production of N-methylmorpholine according to claim 1, characterized in that: the fixed bed reactor body (1) is formed by stacking silicon dioxide loaded copper catalyst particles with the particle size of phi 5 x (4-5) mm, and the silicon dioxide loaded copper catalyst comprises the following components in parts by weight: 20-60% of copper and 30-80% of silicon dioxide.
8. A fixed bed reactor for the continuous process for the production of N-methylmorpholine according to claim 1, characterized in that: the reaction temperature in the fixed bed reactor main body (1) is 200-260 ℃, the reaction pressure in the fixed bed reactor main body (1) is 0.5-1.0Mpa, and the circulating gas quantity of the circulating pump in the fixed bed reactor main body (1) is 30-60L/h.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202011445396.2A CN114618390B (en) | 2020-12-08 | 2020-12-08 | Fixed bed reactor for producing N-methylmorpholine by continuous method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202011445396.2A CN114618390B (en) | 2020-12-08 | 2020-12-08 | Fixed bed reactor for producing N-methylmorpholine by continuous method |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN114618390A true CN114618390A (en) | 2022-06-14 |
| CN114618390B CN114618390B (en) | 2024-02-20 |
Family
ID=81894988
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202011445396.2A Active CN114618390B (en) | 2020-12-08 | 2020-12-08 | Fixed bed reactor for producing N-methylmorpholine by continuous method |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN114618390B (en) |
Citations (11)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4910304A (en) * | 1988-04-20 | 1990-03-20 | Basf Aktiengesellschaft | Preparation of N-substituted cyclic amines |
| CA2228613A1 (en) * | 1997-03-07 | 1998-09-07 | Joachim Simon | The n-alkylation of amines |
| CN1265336A (en) * | 1998-03-17 | 2000-09-06 | Basf公司 | Reactor for chemical reaction |
| CN1911505A (en) * | 2005-08-11 | 2007-02-14 | 中国石油天然气集团公司 | Catalyst required for coproducing N-methyl morpholine and morpholine |
| CN1911919A (en) * | 2005-08-11 | 2007-02-14 | 中国石油天然气集团公司 | Method of coproducing N-methyl morpholine and morpholine |
| CN103626721A (en) * | 2012-08-27 | 2014-03-12 | 中国石油化工股份有限公司 | Method for combined production of N-methyl morpholine and bis (2-dimethylaminoethyl) ether |
| EP2918332A1 (en) * | 2014-03-14 | 2015-09-16 | Morten Müller Ltd., ApS | Scale collection and predistribution tray for vessel with downwards two-phase flow |
| WO2020020794A1 (en) * | 2018-07-23 | 2020-01-30 | Total Raffinage Chimie | Filtration device for a co-current downflow reactor |
| CN111111670A (en) * | 2019-12-05 | 2020-05-08 | 华茂伟业绿色科技股份有限公司 | Supported catalyst and preparation method and application thereof |
| CN111821981A (en) * | 2020-08-12 | 2020-10-27 | 四川鸿鹏新材料有限公司 | Catalyst for preparing morpholine by using diethylene glycol method and preparation method thereof |
| CN111821938A (en) * | 2020-08-05 | 2020-10-27 | 刘涛 | Reactor for cosmetic production |
-
2020
- 2020-12-08 CN CN202011445396.2A patent/CN114618390B/en active Active
Patent Citations (11)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4910304A (en) * | 1988-04-20 | 1990-03-20 | Basf Aktiengesellschaft | Preparation of N-substituted cyclic amines |
| CA2228613A1 (en) * | 1997-03-07 | 1998-09-07 | Joachim Simon | The n-alkylation of amines |
| CN1265336A (en) * | 1998-03-17 | 2000-09-06 | Basf公司 | Reactor for chemical reaction |
| CN1911505A (en) * | 2005-08-11 | 2007-02-14 | 中国石油天然气集团公司 | Catalyst required for coproducing N-methyl morpholine and morpholine |
| CN1911919A (en) * | 2005-08-11 | 2007-02-14 | 中国石油天然气集团公司 | Method of coproducing N-methyl morpholine and morpholine |
| CN103626721A (en) * | 2012-08-27 | 2014-03-12 | 中国石油化工股份有限公司 | Method for combined production of N-methyl morpholine and bis (2-dimethylaminoethyl) ether |
| EP2918332A1 (en) * | 2014-03-14 | 2015-09-16 | Morten Müller Ltd., ApS | Scale collection and predistribution tray for vessel with downwards two-phase flow |
| WO2020020794A1 (en) * | 2018-07-23 | 2020-01-30 | Total Raffinage Chimie | Filtration device for a co-current downflow reactor |
| CN111111670A (en) * | 2019-12-05 | 2020-05-08 | 华茂伟业绿色科技股份有限公司 | Supported catalyst and preparation method and application thereof |
| CN111821938A (en) * | 2020-08-05 | 2020-10-27 | 刘涛 | Reactor for cosmetic production |
| CN111821981A (en) * | 2020-08-12 | 2020-10-27 | 四川鸿鹏新材料有限公司 | Catalyst for preparing morpholine by using diethylene glycol method and preparation method thereof |
Non-Patent Citations (2)
| Title |
|---|
| 张吉波;唐宇昕;李志涛;庞玉荣;: "固定床连续催化合成N-甲酰吗啉工艺的研究", 吉林化工学院学报, no. 03, pages 4 - 6 * |
| 王之德: "制造N-甲基吗啉的新方法", 《广东化工》, no. 1, pages 30 - 31 * |
Also Published As
| Publication number | Publication date |
|---|---|
| CN114618390B (en) | 2024-02-20 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN101575295B (en) | Method for preparing diaminonaphthalene by catalytic hydrogenation of dinitronaphthalene | |
| CN1169917C (en) | Isomerization dewaxing catalyst and its prepn. | |
| CN103619798A (en) | Process for preparing formic acid | |
| CN102276483A (en) | Production method of oamino pheylmethyl ether | |
| CN106986756A (en) | A kind of continuous preparation technology of vanillic aldehyde | |
| CN102964278A (en) | Method for preparing CLT acid (2-amino-4-methyl-5-chlorobenzene sulfonic acid) by continuous catalytic hydrogenation reduction | |
| CN105601588B (en) | The synthetic method of N- hydroxyethyl piperazine coproduction piperazines | |
| CN210434480U (en) | High-efficient hydrogenation unit of production hexamethylene diamine piperidine | |
| CN114618390A (en) | Fixed bed reactor for producing N-methylmorpholine by continuous method | |
| CN109761819B (en) | Continuous preparation method of N, N-dimethylpropylamine | |
| CN110003140B (en) | Device and method for synthesizing epichlorohydrin and regenerating catalyst on line | |
| CN212640339U (en) | Equipment for preparing p-anisidine | |
| CN1814582A (en) | One-step method for preparing N-alkyl aromatic amine from aromatic nitro substance | |
| CN103193660B (en) | Synthetic method of 4-alkoxy phenylamine compound | |
| CN113735688B (en) | Recycling method of waste liquid of butanol device | |
| CN110002970A (en) | The production method and production system of sandaler | |
| CN110172029B (en) | Method for continuously synthesizing 2-amino-2-methyl-1-propanol | |
| CN104086451A (en) | Method for synthesizing 1-amino anthraquinone via continuous hydrogenation of industrial water phases | |
| CN1108241A (en) | Improved process for preparing acyl aminophenols | |
| CN102659698A (en) | Synthesis method of benzotriazole compounds | |
| CN108033872B (en) | Method and equipment for clean and environment-friendly production of 1,1',2, 3-tetrachloropropene | |
| CN112500369B (en) | Continuous production method of methyl morpholine | |
| CN107304166B (en) | Industrial preparation method of 1-naphthylamine | |
| CN109082681B (en) | Preparation device and method of template agent of ammoximation catalyst | |
| CN115583865B (en) | Continuous preparation method of chiral phenethyl alcohol |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant |