CN202912868U - Device for producing ethylene glycol - Google Patents
Device for producing ethylene glycol Download PDFInfo
- Publication number
- CN202912868U CN202912868U CN 201220509721 CN201220509721U CN202912868U CN 202912868 U CN202912868 U CN 202912868U CN 201220509721 CN201220509721 CN 201220509721 CN 201220509721 U CN201220509721 U CN 201220509721U CN 202912868 U CN202912868 U CN 202912868U
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- Prior art keywords
- preheater
- outlet
- ethylene glycol
- heated
- condenser
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Abstract
The utility model discloses a device for producing ethylene glycol, and relates to a production device for a chemical product. The device has the advantages that the structure is simple, the energy is saved, and the consumption is reduced. The device comprises a heater (1), a hydrogenation reactor (2), a condenser (3), a gas-liquid separator (4) and a preheater (5), wherein a to-be-heated material inlet of the preheater (5) is communicated with a dimethyl oxalate conveying pipe (61) and an H2 conveying pipe (62); a to-be-heated material outlet of the preheater (5) is connected with a to-be-heated material inlet of the heater (1); a to-be-heated material outlet of the heater (1) is connected with a reaction material inlet of the hydrogenation reactor (2); a reaction material outlet of the hydrogenation reactor (2) is connected with a heating medium inlet of the preheater (5); a heating medium outlet of the preheater (5) is connected with a condensation material inlet of the condenser (3); and a condensation material gas outlet and a condensation material liquid outlet of the condenser (3) are respectively connected with an inlet of the gas-liquid separator (4).
Description
Technical field
The utility model relates to a kind of Chemicals production unit, particularly relates to a kind of synthetic gas preparing ethylene glycol production unit.
Background technology
(chemical formula is (CH to ethylene glycol
2OH)
2) preparation be that (chemical formula is (COOCH with the gas phase dimethyl oxalate
3)
2) and H
2Be blended in temperature and be 190-210 ℃, pressure and be 2.5MPA, catalyzer and be under the condition of copper Si catalyst and react, reaction formula is as follows:
(COOCH
3)
2＋4H
2—→(CH
2OH)
2+2CH
3OH
As shown in Figure 1, in existing production method, raw material H
2Be mixed into well heater 1 ' with dimethyl oxalate, well heater 1 ' enters reactor 2 ' with mixture after the mixture heating up to 190 ℃ and carries out hydrogenation reaction, this reaction is that a thermopositive reaction and temperature of reaction are 190-210 ℃, exothermic heat of reaction is absorbed by the heat transferring medium in the reactor shell, hydrogenation reaction finish after product ethylene glycol (liquid phase) and not the temperature of the unstripped gas of complete reaction be 190-210 ℃, then high temperature glycol (liquid phase) and not the unstripped gas of complete reaction directly enter condenser 3 ' and carry out condensation, enter gas-liquid separator 4 ' after the condensation, separating the liquid that obtains is thick ethylene glycol product.In above-mentioned production process, the reaction product ethylene glycol (liquid phase) of high temperature and the complete unstripped gas of unreacted directly entered condenser condenses after hydrogenation reaction was finished, need to consume more phlegma, and used phlegma need to be lowered the temperature equally in order to recycle, and has caused like this waste of energy.
The utility model content
The technical problems to be solved in the utility model provides a kind of ethylene glycol production unit simple in structure, energy-saving and cost-reducing.
The utility model ethylene glycol production unit comprises well heater, hydrogenator, condenser and gas-liquid separator, also comprises preheater, wherein material entrance to be heated and dimethyl oxalate transport pipe and the H of preheater
2Transport pipe communicates, the material outlet to be heated of preheater links to each other with the material entrance to be heated of well heater, the material outlet to be heated of well heater links to each other with the reaction mass entrance of hydrogenator, the reacting material outlet of hydrogenator links to each other with the heating medium entrance of preheater, the heating medium outlet of preheater links to each other with the condensation material inlet of condenser, and outlet links to each other with the gas-liquid separator entrance respectively the condensation material pneumatic outlet of condenser with the condensation feed liquid.
The utility model ethylene glycol production unit, wherein said hydrogenator is fixed-bed reactor.
The use procedure of the utility model ethylene glycol production unit is as follows:
Gas phase dimethyl oxalate and H
2Enter preheater, enter well heater be preheated to 160-170 ℃ in preheater after, well heater is with gas phase dimethyl oxalate and H
2Mixed gas be heated to 190-200 ℃ after, mixed gas enters hydrogenator, under 190-210 ℃ condition, carry out hydrogenation reaction, this reaction is thermopositive reaction, liberated heat is taken away by the heat transferring medium of hydrogenator shell, the complete unstripped gas temperature when leaving hydrogenator of gained liquid-phase reaction product ethylene glycol and unreacted is 190-200 ℃, the complete unstripped gas of this high-temperature reaction product and unreacted enters preheater as heating medium, heating medium and material to be heated (dimethyl oxalate and H before the reaction
2) heat exchange in preheater, enter well heater after temperature rises to 160-170 ℃ after the material heat absorption to be heated, heating medium enters into condenser and carries out condensation after being cooled to 160-170 ℃ after the preheater heat release, enter afterwards gas-liquid separator again, obtains liquid product ethylene glycol.
The utility model ethylene glycol production unit difference from prior art is: increased preheater and carried out dimethyl oxalate and H
2Preheating, be to have utilized the entrained heat of the material after the hydrogenation reaction, dimethyl oxalate and H in the warm
2Preheating can save in the well heater consumption as the steam of heating medium; Simultaneously the material after the hydrogenation reaction is equivalent to carry out precooling in preheater, is cooled to first 160-170 ℃ by 190-200 ℃, and then enters condenser condenses, can save like this consumption of phlegma; The utility model ethylene glycol production unit is by to the simple transformation of original production unit, realized recycling energy, energy-saving and cost-reducing purpose in internal system.
Below in conjunction with accompanying drawing the utility model ethylene glycol production unit is described further.
Description of drawings
Fig. 1 is the structural representation of the utility model ethylene glycol production unit prior art;
Fig. 2 is the structural representation of the utility model ethylene glycol production unit.
Embodiment
As shown in Figure 2, the utility model ethylene glycol production unit comprises well heater 1, hydrogenator 2, condenser 3, gas-liquid separator 4, also comprises preheater 5, wherein material entrance to be heated and dimethyl oxalate transport pipe 61 and the H of preheater 5
2 Transport pipe 62 communicates, the material outlet to be heated of preheater 5 links to each other with the material entrance to be heated of well heater 1, the material outlet to be heated of well heater 1 links to each other with the reaction mass entrance of hydrogenator 2, the reacting material outlet of hydrogenator 2 links to each other with the heating medium entrance of preheater 5, the heating medium outlet of preheater 5 links to each other with the condensation material inlet of condenser 3, and outlet links to each other with gas-liquid separator 4 entrances respectively the condensation material pneumatic outlet of condenser 3 with the condensation feed liquid.
Above-described embodiment is described preferred implementation of the present utility model; be not that scope of the present utility model is limited; under the prerequisite that does not break away from the utility model design spirit; various distortion and improvement that those of ordinary skills make the technical solution of the utility model all should fall in the definite protection domain of the utility model claims.
Claims (2)
1. ethylene glycol production unit, comprise well heater (1), hydrogenator (2), condenser (3), gas-liquid separator (4), it is characterized in that: also comprise preheater (5), the material entrance to be heated of wherein said preheater (5) and dimethyl oxalate transport pipe (61) and H
2Transport pipe (62) communicates, the material outlet to be heated of preheater (5) links to each other with the material entrance to be heated of well heater (1), the material outlet to be heated of well heater (1) links to each other with the reaction mass entrance of hydrogenator (2), the reacting material outlet of hydrogenator (2) links to each other with the heating medium entrance of preheater (5), the heating medium outlet of preheater (5) links to each other with the condensation material inlet of condenser (3), and outlet links to each other with gas-liquid separator (4) entrance respectively the condensation material pneumatic outlet of condenser (3) with the condensation feed liquid.
2. ethylene glycol production unit according to claim 1, it is characterized in that: described hydrogenator (2) is fixed-bed reactor.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 201220509721 CN202912868U (en) | 2012-09-27 | 2012-09-27 | Device for producing ethylene glycol |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 201220509721 CN202912868U (en) | 2012-09-27 | 2012-09-27 | Device for producing ethylene glycol |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN202912868U true CN202912868U (en) | 2013-05-01 |
Family
ID=48161196
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 201220509721 Expired - Fee Related CN202912868U (en) | 2012-09-27 | 2012-09-27 | Device for producing ethylene glycol |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN202912868U (en) |
-
2012
- 2012-09-27 CN CN 201220509721 patent/CN202912868U/en not_active Expired - Fee Related
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CF01 | Termination of patent right due to non-payment of annual fee | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20130501 Termination date: 20160927 |