IE20180488U1 - α-cyanoacrylate production plant - Google Patents

Abstract

a-cyanoacrylate production plant, including: tank (F101), tank (F102), tank (F103), tank (F104) feedstock pump (J101), feedstock pump (J102), feedstock pump (J 103), feedstock pump (J104), reactor (D101), transfer pump (J105), water knockout drum (L101), condenser (C101), condenser (C102), condenser (C 103), splitting kettle (D102), tank (F105), buffer tank (F106), vacuum pump (J106), rectifying column (E101), non-boiling range product receiving tank (F107), finished product receiving tank (F108); among them, tank (F101) is used to store ethyl cyanoacetate, tank (F102) is used to store dichloroethane, tank (F103) is used to store formaldehyde, tank (F104) is used lo store dibutyl phthalate, tank (F105) is used to store crude product; among them, cone bottom height of tank (F104) is 470-474 mm.

Description

FIELD OF THE INVENTION The present invention relates to a kind of pharmaceutical synthesis plant. more particularly, relates to(] -cyanoacrylate production plant.

GENERAL BACKGROUND 0.-cyanoacrylate is mainly used for the bonding of porous and absorbent materials, used in self or mutual bonding of steel, nonferrous metals, rubber, leather, plastics, ceramics, wood, nonferrous metals, non-metallic ceramics, glass and flexible materials like plastic products, shoes, soft and hard plastics, etc. It is used widely in electrical appliances, instruments, machinery, electronics, optical instruments, medical treatment, light industry, civil and so on. Most of the existing production plant processes are complex. Thus, as a binder, the advantages and disadvantages of production equipment of or-cyanoacrylate have a great economic significant for improving product quality and reducing the by-product contents.

SUMMARY The purpose of the present invention is to provide on-cyanoacrylate production plant, including: tank (F101), tank (F102), tank (F103), tank (F104), feedstock pump (J 101), feedstock pump (J 102), feedstock pump (J 103), feedstock pump (J 104), reactor (D101), transfer pump (J 105), water knockout drum (L101), condenser (C101), condenser (C 102), condenser (C103), splitting kettle (D102), tank (F105), buffer tank (F106), vacuum pump (J 106), rectifying column (E101), non-boiling range product receiving tank (F107), finished product receiving tank (F108); among them, tank (F101) is used to store ethyl cyanoacetate, tank (F102) is used to store dichloroethane, tank (F103) is used to store formaldehyde, tank (F104) is used to store dibutyl phthalate, tank (F105) is used to store crude product; among them, cone bottom height of tank (F104) is 470-474 mm, inlet diameter of transfer pump (J 103) is 310-330 mm, outer pot diameter of reactor (D101) is 800-850 mm. (1-cyanoacrylate production plant, the production process is: firstly, pumped cyanoacetate from F101 and dichloroethane from F102 to reactor D101 according to the metering, stirred and raised the temperature to 60-65 °C. Then slowly added the mixture of formaldehyde and hexahydropyridine, maintaining the kettle temperature slightly lower than the reflux temperature, the pump speed is appropriate, completed in 40-47 min. Opened the water pipe of condenser C101, continued heating to reflux, removed water through water knockout drum L101, up to 60-65 parts of water, added dibutyl phthalate and p-toluenesulfonic acid, continued to reflux and divide water, until the steam temperature exceeds 80 °C, distilled dichloroethane. Reduced the temperature to 50-55 °C, added phosphorus pentoxide, stirred hydroquinone evenly, started vacuum pump J 106, splitting decomposed in a vacuum distillation unit under the sulfur dioxide atmosphere, collected the boiling range of 100 ~ 110 "C crude product into F105. Added 2 parts of phosphorus pentoxide and 0.5 parts of hydroquinone into the collected materials, then rectified through the rectifying column E101, collected the fraction of 82-86 °C in F108 (still under the protection of sulfur dioxide), got the finished product. The advantages of this invention are that the reaction time is reduced and the reaction rate is improved.

DESCRIPTION OF THE DRAWINGS Figure 1 or-cyanoacrylate production plant.

Include: tank (F101), tank (F102), tank (F103), tank (F104), feedstock pump (J 101), feedstock pump (J 102), feedstock pump (J 103), feedstock pump (J104), reactor (D101), transfer pump (J 105), water knockout drum (L101), condenser (C101), condenser (C102), condenser (C103), splitting kettle (D102), tank (F105), buffer tank (F106), vacuum pump (J 106), rectifying column (E101), non-boiling range product receiving tank (F107), finished product receiving tank (F108); DETAILED DESCRIPTION OF PREFERRED EMBODIMENTS The following examples with reference to specific embodiments of the present invention are further illustrated: Embodiment 1 Raw materials and dosages Cyano acetate Industrial 200 Dibutyl phthalate Industrial 40 grade grade Dichloro ethane Industrial 1 50 P-toluenesulfonic Industrial 3 grade acid grade Formaldehyde Industrial 100 Phosphorus Industrial 12 grade pentoxide grade Piperidine Industrial 1 Quinol Industrial 1 grade grade or-cyanoacrylate production plant, including: tank (F101), tank (F102), tank (F103), tank (F104), feedstock pump (J 101), feedstock pump (J 102), feedstock pump (J 103), feedstock pump (J 104), reactor (D101), transfer pump (J 105), water knockout drum (L101), condenser (C101), condenser (C102), condenser (C103), splitting kettle (D102), tank (F105), buffer tank (F106), vacuum pump (J106), rectifying column (E101), non—boiling range product receiving tank (F107), finished product receiving tank (F108); among them, tank (F101) is used to store ethyl cyanoacetate, tank (F102) is used to store dichloroethane, tank (F103) is used to store formaldehyde, tank (F104) is used to store dibutyl phthalate, tank (F105) is used to store crude product; among them, cone bottom height of tank (F104) is 470 mm, inlet diameter of transfer pump (J 103) is 310 mm, outer pot diameter of reactor (D101) is 800 mm. on-cyanoacrylate production plant, the production process is: firstly, pumped cyanoacetate from F101 and dichloroethane from F102 to reactor D101 according to the metering, stirred and raised the temperature to 60 "C. Then slowly added the mixture of formaldehyde and hexahydropyridine, maintaining the kettle temperature slightly lower than the reflux temperature, the pump speed is appropriate, completed in 40 min. Opened the water pipe of condenser C101, continued heating to reflux, removed water through water knockout drum L101, up to 60 parts of water, added dibutyl phthalate and p-toluenesulfonic acid, continued to reflux and divide water, until the steam temperature exceeds 80 "C, distilled dichloroethane. Reduced the temperature to 50 "C, added phosphorus pentoxide, stirred hydroquinone evenly, started vacuum pump J 106, splitting decomposed in a vacuum distillation unit under the sulfur dioxide atmosphere, collected the boiling range of 100 °C crude product into F105. Added 2 parts of phosphorus pentoxide and 0.5 parts of hydroquinone into the collected materials, then rectified through the rectifying column E101, collected the fraction of 82 "C in F108 (still under the protection of sulfur dioxide), got the finished product.

The qualities of the product are as follows: Exterior Colorless transparent liquid Bond strength 22 MPa (metal-metal) Viscosity 5 mPa-s / / (25 °C) Embodiment 2 Raw materials and dosages Cyanoacetate Industrial 230 Dibutyl Industrial 50 grade phthalate grade Dichloroethane Industrial 190 P-toluenesulfo Industrial 4 grade nic acid grade Formaldehyde Industrial 130 Phosphorus Industrial 1 5 grade pentoxide grade Piperidine Industrial 1 .5 Quinol Industrial 2 grade grade ot-cyanoacrylate production plant, including: tank (F101), tank (F102), tank (F103), tank (F104), feedstock pump (J 101), feedstock pump (J 102), feedstock pump (J 103), feedstock pump (J 104), reactor (D101), transfer pump (J 105), water knockout drum (L101), condenser (C101), condenser (C102), condenser (C103), splitting kettle (D102), tank (F105), buffer tank (F106), vacuum pump (J106), rectifying column (E101), non-boiling range product receiving tank (F107), finished product receiving tank (F 108); among them, tank (F101) is used to store ethyl cyanoacetate, tank (F102) is used to store dichloroethane, tank (F103) is used to store formaldehyde, tank (F104) is used to store dibutyl phthalate, tank (F105) is used to store crude product; among them, cone bottom height of tank (F104) is 474 mm, inlet diameter of transfer pump (J103) is 330 mm, outer pot diameter of reactor (D101) is 850 mm. or-cyanoacrylate production plant, the production process is: firstly, pumped cyanoacetate from F 101 and dichloroethane from F102 to reactor D101 according to the metering, stirred and raised the temperature to 65 °C. Then slowly added the mixture of formaldehyde and hexahydropyridine, maintaining the kettle temperature slightly lower than the reflux temperature, the pump speed is appropriate, completed in 47 min. Opened the water pipe of condenser C101, continued heating to reflux, removed water through water knockout drum L101, up to 65 parts of water, added dibutyl phthalate and p-toluenesulfonic acid, continued to reflux and divide water, until the steam temperature exceeds 80 °C, distilled dichloroethane. Reduced the temperature to 55 “C, added phosphorus pentoxide, stirred hydroquinone evenly, started vacuum pump J 106, splitting decomposed in a vacuum distillation unit under the sulfur dioxide atmosphere, collected the boiling range of 110 °C crude product into F105. Added 2 parts of phosphorus pentoxide and 0.5 parts of hydroquinone into the collected materials, then rectified through the rectifying column E101, collected the fraction of 86 "C in F108 (still under the protection of sulfur dioxide), got the finished product.

The qualities of the product are as follows: Exterior Colorless Bond strength (metal-metal) 24 MPa transparent liquid Viscosity 7 mPa-s / / (25 °C) The embodiments of the present invention are merely preferred embodiments of the present invention, but the range of the present invention is not limited this, and any person who is familiar with those skilled in the arts, within the technical range of the present invention. It is intended that the technical solution and its inventive concept be replaced or modified equivalently with reference to the range of the invention.

Claims (3)

Claims

1. 0.-cyanoacrylate production plant, including: tank (F101), tank (F102), tank (F103), tank (F104), feedstock pump (J 101), feedstock pump (J 1 02), feedstock pump (J 103), feedstock pump (J 104), reactor (D101), transfer pump (J 105), water knockout drum (L101), condenser (C101), condenser (C102), condenser (C103), splitting kettle (D102), tank (F105), buffer tank (F106), vacuum pump (J106), rectifying column (E101), non—boiling range product receiving tank (F107), finished product receiving tank (F108); among them, tank (F101) is used to store ethyl cyanoacetate, tank (F102) is used to store dichloroethane, tank (F103) is used to store formaldehyde, tank (F104) is used to store dibutyl phthalate, tank (F105) is used to store crude product; among them, cone bottom height of tank (F104) is 470-474 mm.

2. ot-cyanoacrylate production plant according to claim 1 wherein inlet diameter oftransfer pump (Jl03) is 310-330 mm.

3. or-cyanoacrylate production plant according to claim 1 wherein outer pot diameter of reactor (D101) is 800-850 mm.