CN212269947U - Device for continuously producing 1, 2-epoxy pentane - Google Patents
Device for continuously producing 1, 2-epoxy pentane Download PDFInfo
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- CN212269947U CN212269947U CN202020718617.8U CN202020718617U CN212269947U CN 212269947 U CN212269947 U CN 212269947U CN 202020718617 U CN202020718617 U CN 202020718617U CN 212269947 U CN212269947 U CN 212269947U
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Abstract
The utility model discloses a device of serialization production 1, 2-epoxy pentane is about to send into the raw materials after mixing and preheating react in the reactor, and the material after the reaction returns the reactor retrieval and utilization after through flash separation knockout drum separation 1-pentene, through methyl alcohol knockout tower separation methyl alcohol, and methyl alcohol knockout tower bottom liquid is 1, 2-epoxy pentane promptly. The utility model discloses a continuous automated control, not only the production process safety ring protects and the high-usage of the energy, makes the utility model discloses use safe and reliable more.
Description
Technical Field
The utility model relates to a chemical industry equipment technical field, concretely relates to device of serialization production 1, 2-epoxy pentane.
Background
1, 2-epoxy pentane can be used for producing 1, 2-pentanediol through ring opening under the action of acid and alkali, 1, 2-pentanediol is not only an important raw material for producing propiconazole, but also can be used for producing polyester, cosmetics and medicines, the problems that the equipment is seriously corroded in the process of using formic acid as a catalyst and hydrogen peroxide to treat 1-pentene are eliminated due to the large amount of byproduct formate, the utilization value is low, the difficulty in treating high-salt high-COD wastewater is high and the like are solved, and the novel titanium silicalite molecular sieve is widely concerned when being used as a catalyst for carrying out hydrogen peroxide epoxidation on 1-pentene;
chinese patent CN201010528124.9 discloses a method for synthesizing 1, 2-pentanediol by using titanium silicalite molecular sieve catalysis, but the process adopts kettle type batch reaction, the catalyst needs to be filtered, and in the actual engineering process, the labor intensity is high, the energy utilization rate is low and the efficiency is low;
chinese patent CN201410427953.6 discloses a method for preparing 1, 2-pentanediol by oxidizing and hydrolyzing n-pentene, but the method is only optimized according to reaction conditions and does not relate to a specific process implementation process.
SUMMERY OF THE UTILITY MODEL
In view of the above problems, the main object of the present invention is to provide a safe, environment-friendly and energy-efficient apparatus for continuously producing 1, 2-epoxypentane.
The purpose of the utility model is realized with the following mode:
the utility model provides a device of serialization production 1, 2-epoxy pentane, is including blender, raw materials pre-heater, reactor, flash separation jar and the methyl alcohol knockout tower of establishing ties in proper order, the feed inlet of blender is connected with hydrogen peroxide jar, methyl alcohol jar and head tank, the first branch pipe of flash separation jar top discharge gate with raw materials pre-heater's feed inlet is connected, the second branch union coupling of flash separation jar top discharge gate has first condenser, the discharge gate of first condenser is connected with and receives the jar, the first branch pipe of the discharge gate of receipt jar with the feed inlet of blender is connected, the second branch pipe of the discharge gate of receipt jar with the side feed inlet at methyl alcohol knockout tower top is connected, the discharge gate at methyl alcohol knockout tower top is connected with the second condenser, the discharge gate of second condenser with the receipt jar is connected, the bin outlet of second condenser is connected the flash separation jar top discharge gate with receive jar on the jar discharge gate with The side feed inlet of the lower part of the methanol separation tower is connected with a tower kettle, and the feed inlet of the lower part of the tower kettle is connected with the lower end discharge hole of the methanol separation tower.
Further, the discharge ports of the hydrogen peroxide tank and the methanol tank are connected with a first pump, the discharge port of the raw material tank is connected with a second pump, and outlets of the first pump and the second pump are connected with the mixer.
Further, flash separation jar top discharge gate is connected with the compressor, the export of compressor through first minute pipe with raw materials pre-heater's feed inlet is connected, the export of compressor through the second minute pipe with first condenser is connected.
Furthermore, the discharge port of the second condenser is connected with the feed port of the compressor through a fan.
Further, the discharge gate of receiving the jar is connected with the third pump, the export of third pump through first branch pipe with the feed inlet of blender is connected, the export of third pump through the second branch pipe with the side feed inlet at methanol separation tower top is connected.
Further, a discharge hole at the lower end of the methanol separation tower is connected with a fourth pump.
Further, the reactor is a tubular inductor, and a granular catalyst is arranged in the tubular inductor.
Further, the flash separation tank is provided at an upper portion thereof with a tray and a demister for efficient separation of pentene-and methanol.
Further, the mixer is a static mixer.
Still further, the mixer is a venturi mixer, an orifice plate mixer, or a jet mixer.
The utility model has the advantages that:
1. the utility model adopts continuous automatic control, such as DCS operation, which not only has high automation degree, but also has higher production efficiency;
2. the production process of the utility model is safe and environment-friendly, the reactor adopts normal pressure or micro positive pressure, the reaction temperature is 50 ℃, no by-product is produced, and only trace methanol enters the waste gas system, thereby the energy utilization rate is high;
3. the utility model discloses well hydrogen peroxide solution conversion is 100%, and 1-pentene conversion is 99%, and the yield of 1, 2-epoxypentane reaches more than 95%, therefore raw and other materials high-usage.
Drawings
In order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the drawings used in the description of the embodiments or the prior art will be briefly described below, it is obvious that the drawings in the following description are only some embodiments of the present invention, and for those skilled in the art, other drawings can be obtained according to these drawings without creative efforts. In the drawings:
fig. 1 is a schematic view of the production system of the present invention.
The notation in the figure is: the system comprises a hydrogen peroxide tank V101, a methanol tank V102, a raw material tank V103, a mixer M101, a flash separation tank V104, a first pump P101, a second pump P102, a third pump P103, a fourth pump P104, a mixer M101, a raw material preheater E101, a first condenser E102, a second condenser E103, a reactor R101, a flash separation tank V104, a receiving tank V105, a compressor B101, a fan B102, a methanol separation tower T101 and a tower bottom T102.
Detailed Description
The technical solutions in the embodiments of the present invention will be described clearly and completely with reference to the accompanying drawings in the embodiments of the present invention, and it is obvious that the described embodiments are only some embodiments of the present invention, not all embodiments. Based on the embodiments in the present invention, all other embodiments obtained by a person skilled in the art without creative work belong to the protection scope of the present invention.
Referring to fig. 1, the apparatus for continuously producing 1, 2-epoxypentane as shown in fig. 1 comprises a mixer M101, a raw material preheater E101, a reactor R101, a flash separation tank V104 and a methanol separation tower T101 which are sequentially connected in series, wherein a feed inlet of the mixer M101 is connected with a hydrogen peroxide tank V101, a methanol tank V102 and a raw material tank V103, a first branch pipe of a discharge outlet at the top end of the flash separation tank V104 is connected with a feed inlet of the raw material preheater E101, a second branch pipe of a discharge outlet at the top end of the flash separation tank V104 is connected with a first condenser E102, a discharge outlet of the first condenser E102 is connected with a receiving tank V105, a first branch pipe of a discharge outlet of the receiving tank V105 is connected with the feed inlet of the mixer M101, a second branch pipe of the discharge outlet of the receiving tank V105 is connected with a side feed inlet at the top of the methanol separation tower T101, a discharge outlet at the top of the methanol separation tower T101 is connected with, the discharge gate of second condenser E103 with receive jar V105 and connect, the bin outlet of second condenser E103 is connected flash separation jar V104 top discharge gate with receive on the jar V105, the side feed inlet of methanol separation tower T101 lower part is connected with tower cauldron T102, tower cauldron T102 lower part feed inlet with the lower extreme discharge gate of methanol separation tower T101 is connected.
Preferably, the outlets of the hydrogen peroxide tank V101 and the methanol tank V102 are connected to a first pump P101, the outlet of the raw material tank V103 is connected to a second pump P102, and the outlets of the first pump P101 and the second pump P102 are both connected to the mixer M101.
Preferably, a discharge port at the top end of the flash separation tank V104 is connected with a compressor B101, an outlet of the compressor B101 is connected with a feed port of the raw material preheater E101 through a first branch pipe, and an outlet of the compressor B101 is connected with the first condenser E102 through a second branch pipe.
Preferably, the discharge port of the second condenser E103 is connected to the feed port of the compressor B101 through a fan B102.
Preferably, the discharge port of the receiving tank V105 is connected with a third pump P103, the outlet of the third pump P103 is connected with the feed port of the mixer M101 through a first branch pipe, and the outlet of the third pump P103 is connected with the side feed port at the top of the methanol separation column T101 through a second branch pipe.
Preferably, a lower discharge port of the methanol separation tower T101 is connected with a fourth pump P104.
Preferably, the reactor R101 is a shell and tube type inductor, and a granular catalyst is disposed in the shell and tube type inductor.
Preferably, the flash separation tank V104 is provided at its upper portion with trays and a demister for efficient separation of 1-pentene and methanol.
Preferably, the mixer M101 is a static mixer.
Preferably, the mixer M101 is a venturi mixer, an orifice plate mixer or a jet mixer.
Preferably, the raw material tank V103 contains 1-pentene.
Preferably, the number of the reactors R101 is 2, and the reaction temperature of the reactor R101 is 50 ℃.
Preferably, the amount of the particulate catalyst is 1.5 t.
Preferably, the tubular reactor takes 1-pentene and hydrogen peroxide as raw materials, methanol as a recycled solvent, the three are mixed after flow rate control according to a certain proportion, and the recycled methanol in the production process only needs a very small amount of supplement.
Setting working parameters: in the continuous operation process, adding 1335kg/hr of hydrogen peroxide with the content of 30 percent and 15kg/hr of methanol, adding 784kg/hr of 1-pentene, mixing with recovered methanol and 1-pentene, preheating to 60 ℃ by the raw material preheater E101, adding into a tubular reactor with the specification of phi 25 multiplied by 2 and filled with 1.5t of catalyst, separating 1-pentene by a flash separation tank and separating methanol by a rectifying tower to obtain about 2100kg of 1, 2-epoxypentane aqueous solution with the content of 43 percent.
The working process is as follows: fresh materials from a hydrogen peroxide tank V101 and a methanol tank V102 are pumped into a mixer M101 by a first pump P101 after flow measurement, 1-pentene passes through a second pump P102 from a raw material tank V103 and is pumped into the mixer M101 after flow measurement, pentene and methanol recovered from a receiving tank V105 are pumped into the mixer M101 by a third pump P103, the raw materials are mixed and enter a raw material preheater E101, the raw materials are preheated to 60 ℃ by steam and enter a reactor R101, reacted gas enters a flash separation tank V104, part of gas at the top of the V104 tank passes through a compressor B101 and returns to an inlet of the raw material preheater E101, the other part of gas after passing through the compressor B101 enters a receiving tank V105 after being condensed by the first condenser E102, tail gas removal treatment is carried out on non-condensable gas condensed by the first condenser E102, a liquid phase in the flash separation tank V104 enters a methanol separation tower T101, and a top gas phase in the methanol separation tower T101 is condensed by the third condenser E103, the non-condensable gas in the condenser E103 is pumped into an inlet of a compressor B101 through a fan B102 to be compressed again; a part of the liquid-phase methanol from the receiving tank V105 is refluxed to the methanol separation tower T101 by a pump P103, and the other part thereof is returned to the inlet of the raw material preheater E101 by the pump P103, and finally the acceptable 1, 2-epoxypentane aqueous solution remaining at the bottom of the methanol separation tower T101 and in the column bottom T102 is pumped out by a pump P104.
The above is only a preferred embodiment of the present invention, and is not intended to limit the present invention, and various modifications and changes will occur to those skilled in the art. Any modification, equivalent replacement, or improvement made within the spirit and principle of the present invention should be included in the protection scope of the present invention.
Claims (10)
1. The device for continuously producing 1, 2-cyclopentane epoxide is characterized by comprising a mixer (M101), a raw material preheater (E101), a reactor (R101), a flash separation tank (V104) and a methanol separation tower (T101) which are sequentially connected in series, wherein a feed inlet of the mixer (M101) is connected with a hydrogen peroxide tank (V101), a methanol tank (V102) and a raw material tank (V103), a first branch pipe of a discharge outlet at the top end of the flash separation tank (V104) is connected with a feed inlet of the raw material preheater (E101), a second branch pipe of a discharge outlet at the top end of the flash separation tank (V104) is connected with a first condenser (E102), a discharge outlet of the first condenser (E102) is connected with a receiving tank (V105), a first branch pipe of a discharge outlet of the receiving tank (V105) is connected with a feed inlet of the mixer (M101), a second branch pipe of a discharge outlet of the receiving tank (V105) is connected with a feed inlet at the top of the methanol separation tower (T101), the discharge gate at methanol separation tower (T101) top is connected with second condenser (E103), the discharge gate of second condenser (E103) with receiving jar (V105) and connecting, the bin outlet of second condenser (E103) is connected flash separation jar (V104) top discharge gate with on receiving jar (V105), the side feed inlet of methanol separation tower (T101) lower part is connected with tower cauldron (T102), tower cauldron (T102) lower part feed inlet with the lower extreme discharge gate of methanol separation tower (T101) is connected.
2. The device for continuously producing 1, 2-epoxy pentane according to claim 1, wherein the discharge ports of the hydrogen peroxide tank (V101) and the methanol tank (V102) are connected with a first pump (P101), the discharge port of the raw material tank (V103) is connected with a second pump (P102), and the outlets of the first pump (P101) and the second pump (P102) are connected with the mixer (M101).
3. The device for continuously producing 1, 2-epoxypentane according to claim 1, characterized in that the discharge port at the top end of the flash separation tank (V104) is connected with a compressor (B101), the outlet of the compressor (B101) is connected with the feed port of the raw material preheater (E101) through a first branch pipe, and the outlet of the compressor (B101) is connected with the first condenser (E102) through a second branch pipe.
4. The continuous production device of 1, 2-epoxy pentane according to claim 3, wherein the discharge outlet of the second condenser (E103) is connected with the inlet of the compressor (B101) through a fan (B102).
5. The device for continuously producing 1, 2-epoxypentane according to claim 1, characterized in that the discharge port of the receiving tank (V105) is connected with a third pump (P103), the outlet of the third pump (P103) is connected with the feed port of the mixer (M101) through a first branch pipe, and the outlet of the third pump (P103) is connected with the side feed port at the top of the methanol separation tower (T101) through a second branch pipe.
6. The continuous production device of 1, 2-epoxy pentane according to claim 1, wherein the lower discharge port of the methanol separation tower (T101) is connected with a fourth pump (P104).
7. The continuous production device of 1, 2-epoxy pentane according to claim 1, wherein the reactor (R101) is a shell and tube type inductor, and a granular catalyst is arranged in the shell and tube type inductor.
8. The continuous production apparatus of 1, 2-epoxypentane of claim 1, characterized in that the flash separation tank (V104) is equipped with trays and demister at the upper part for effective separation of 1-pentene and methanol.
9. The continuous production plant for 1, 2-epoxypentane according to claim 1, characterized in that said mixer (M101) is a static mixer.
10. The plant for the continuous production of 1, 2-epoxypentane according to claim 9, wherein the mixer (M101) is a venturi mixer, an orifice plate mixer or a jet mixer.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202020718617.8U CN212269947U (en) | 2020-04-30 | 2020-04-30 | Device for continuously producing 1, 2-epoxy pentane |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202020718617.8U CN212269947U (en) | 2020-04-30 | 2020-04-30 | Device for continuously producing 1, 2-epoxy pentane |
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| Publication Number | Publication Date |
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| CN212269947U true CN212269947U (en) | 2021-01-01 |
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| Application Number | Title | Priority Date | Filing Date |
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| CN202020718617.8U Active CN212269947U (en) | 2020-04-30 | 2020-04-30 | Device for continuously producing 1, 2-epoxy pentane |
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