CN202214306U - Process device for preparing ethanol by utilizing acetic acid - Google Patents
Process device for preparing ethanol by utilizing acetic acid Download PDFInfo
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- CN202214306U CN202214306U CN2011202570711U CN201120257071U CN202214306U CN 202214306 U CN202214306 U CN 202214306U CN 2011202570711 U CN2011202570711 U CN 2011202570711U CN 201120257071 U CN201120257071 U CN 201120257071U CN 202214306 U CN202214306 U CN 202214306U
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- acetic acid
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- rectifying separation
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Abstract
The utility model relates to a process device for preparing ethanol by utilizing acetic acid, which comprises esterification kettle, a reaction rectifying tower, a tower top condenser, a reflux accumulator, a hydrogenation feeding heat exchanger, a hydrogenation feeding heater, a hydrogenation reactor, a filter, a product cooler, a gas-liquid separating tank and a rectifying separation mechanism which are sequentially connected through connecting pipelines. The esterification kettle is provided with an acetic acid raw material adding pipeline, an alkyl alcohol adding pipeline and a sulfuric acid catalyst adding pipeline. An upper separating opening arranged on the rectifying separation mechanism is communicated with the alkyl alcohol adding pipeline, and a lower separating opening on the rectifying separation mechanism separates an ethanol product. By means of the technical scheme, heat energy in the device can be effectively recycled, the heat energy input into the device is reduced, heat energy consumption is saved, and the reaction effect is ensured. Raw material gases of hydrogen and alkyl alcohol not reacted in the hydrogenation reactor can be recycled in the device so as to provide pressure guarantee for a whole recycling process, discharge inert gasses in recycling gases and ensure hydrogenation reaction efficiency.
Description
Technical field
The utility model relates to a kind of chemical technique device, particularly relates to a kind of acetic acid and prepares the alcoholic acid process unit.
Background technology
Ethanol is widely used in industries such as food, chemical industry, medicine, dyestuff, national defence, is again crucial clean energy.The ethanol calorific value is lower, the latent heat of vaporization is higher, the capability of antidetonance is good, oxygen level is high; Under the situation that less water exists, also be easy to generate and be separated; Not only can make ethanol petrol as automobile fuel as clean energy; And ethanol petrol is compared with regular gasoline, with good characteristics such as its burning are more complete, the CO quantity discharged is lower, combustionproperty is similar with gasoline, is called as 21 century " green energy resource ".
The paces that alcohol fuel is applied have all been accelerated in countries in the world; 60% of ethanol production is used as vehicle fuel; Present fuel ethanol production mainly is to be raw material with cereal; Corn Fuel Ethanol has become the important energy source of supply in a lot of countries, and China has also built a plurality of to be the fuel ethanol production project of raw material with the corn, to account for 55% of Production of Fuel Ethanol in Tenth Five-Year Plan Period; But along with world food is in short supply, alcohol production has to turn to the developing direction of non-food crop as raw material.
The acetic acid synthesis from methanol carbonylation technology is ripe at present; Industrial production device is more and more; Acetic acid market is tending towards saturated; Exploitation acetic acid derived product is an important topic, and development and use acetic acid hydrogenation preparing ethanol is an important topic, designs to be used for acetic acid hydrogenation preparing alcoholic acid industrial installation and to have important economic implications equally.
The utility model content
In order to solve the problems of the technologies described above; The utility model provides a kind of acetic acid to prepare the alcoholic acid process unit; This process unit is energy-conserving and environment-protective not only, and have realized making full use of of system's heat energy, are satisfying under the prerequisite of processing condition; Hydrogen, alkyl alcohol have obtained recycling in the raw material, have realized the maximum using of raw material.
The utility model discloses acetic acid and prepare the alcoholic acid process unit; Include and comprise esterifying kettle, reaction fractionating tower, overhead condenser, return tank; Hydrogenation feed exchanger, hydrogenation feed heater, hydrogenator, strainer, product water cooler, knockout drum, rectifying separation mechanism; And be connected through connecting tube successively; Said esterifying kettle is furnished with that raw material acetic acid adds pipeline, alkyl alcohol adds pipeline and catalyst sulfuric acid adds pipeline, and the last separating opening in the said rectifying separation mechanism is connected with alkyl alcohol adding pipeline, and the following separating opening in the said rectifying separation mechanism is isolated alcohol product.
Said knockout drum is connected with the hydrogenation feed exchanger through circulator by connecting tube.
Said knockout drum is connected with blow-down pipe with the connecting tube that circulator is connected.
Connecting tube between said circulator and the hydrogenation feed exchanger is provided with new hydrogen make mouth.
Separating opening adds pipeline with alkyl alcohol and is connected in the said rectifying separation mechanism, and the bottom separating opening in the said rectifying separation mechanism is connected with return tank through connecting tube.
Said return tank is connected with reaction fractionating tower through connecting tube.
Said reactive distillation tower bottom is furnished with the aqueous sulfuric acid vent line.
Said alkyl alcohol adds pipeline and is connected with reaction fractionating tower.
Said rectifying separation mechanism is made up of one or more rectifying separation tower.
The beneficial effect that the utility model can reach is: a kind of acetic acid prepares the alcoholic acid process unit; Through the present technique scheme; 1 through to the use of hydrogenation feed exchanger, makes the hydrogenator exit gas give the charging preheating as thermal source, efficient recovery heat energy in the device; Reduce heat energy input in device, practiced thrift heat energy consumption; 2, the use of hydrogenation feed heater is fully heated the raw material charging, reaches the temperature requirement of hydrogenator, has guaranteed reaction effect; 3, the use of circulator circulates the unreacted virgin gas hydrogen of hydrogenator in device, virgin gas hydrogen is fully used, once more, and for the full cycle operation provides the pressure guarantee; 4, the outfit of alkyl alcohol pipeline makes alkyl alcohol realize recycling at whole device; 5, the rare gas element in the circulation gas has been got rid of in the outfit of blow-down pipe, and the effective concentration of reactant gases is controlled within the technic index, has guaranteed hydrogenation reaction efficient.
Description of drawings:
Fig. 1 prepares alcoholic acid process unit structural representation for the utility model acetic acid.
Among the figure, 1 alkyl alcohol adds pipeline, 2 acetic acid and adds pipeline, 3 sulfuric acid and add separating opening in pipeline, 4 esterifying kettles, 5 reaction fractionating towers, 6 overhead condensers, 7 return tanks, 8 new hydrogen make mouths, 9 hydrogenation feed exchangers, 10 product water coolers, 11 hydrogenation feed heaters, 12 knockout drums, 13 blow-down pipes, 14 circulators, 15 hydrogenators, the 16 rectifying separation mechanisms, 17,18 times separating openings, 19 bottom separating openings, 20 strainers, 21 connecting tubes, 22 aqueous sulfuric acid vent lines.
Embodiment:
Be described further below in conjunction with accompanying drawing and specific embodiment technical scheme the utility model.
As shown in Figure 1; The acetic acid that the utility model relates to prepares the alcoholic acid process unit; Comprise esterifying kettle 4, reaction fractionating tower 5, overhead condenser 6, return tank 7; Hydrogenation feed exchanger 9, hydrogenation feed heater 11, hydrogenator 15, strainer 20, product water cooler 10, knockout drum 12, rectifying separation mechanism 16, and be connected through connecting tube 21 successively, said esterifying kettle 4 is furnished with acetic acid and adds pipeline 2, alkyl alcohol adding pipeline 1 and sulfuric acid adding pipeline 3; Last separating opening 17 in the said rectifying separation mechanism 16 adds pipeline 1 with alkyl alcohol and is connected, and the following separating opening 18 in the said rectifying separation mechanism 16 is isolated alcohol product.
Said knockout drum 12 is connected with hydrogenation feed exchanger 9 through circulator 14 by connecting tube 21.
Said knockout drum 12 is connected with blow-down pipe 13 with the connecting tube 21 that circulator 14 is connected.
Connecting tube 21 between said circulator 14 and the hydrogenation feed exchanger 9 is provided with new hydrogen make mouth 8.
Separating opening 17 adds pipeline 1 with alkyl alcohol and is connected in the said rectifying separation mechanism 16, and the bottom separating opening 19 in the said rectifying separation mechanism 16 is connected with return tank 7 through connecting tube 21.
Said return tank 7 is connected with reaction fractionating tower 5 through connecting tube 21.
Said reaction fractionating tower 5 bottoms are furnished with aqueous sulfuric acid vent line 22.
Said alkyl alcohol adds pipeline 1 and is connected with reaction fractionating tower 5.
Said rectifying separation mechanism 16 is made up of one or more rectifying separation tower.
When work, acetic acid, sulfuric acid and the alkyl alcohol that can recycle, fresh alkyl alcohol get into esterifying kettle 4 through pipeline and carry out esterification; Esterifying kettle 4 dischargings get into reaction fractionating tower 5, and aqueous sulfuric acid vent line 22 effluxes for the mixed solution of sulfuric acid and esterification product water, and the acetic acid alkyl alcohol charging that reaction fractionating tower 5 connects is to handle unreacted acetic acid in esterifying kettle 4 supplied materials; Reaction fractionating tower 5 top discharges get into return tank 7 after overhead condenser 6 condensations, overhead condenser 6 low-temperature receivers are recirculated water, and rectifying separation mechanism 16 isolated acetic acid alkyl alcohols get into return tank 7; Reclaim unreacted acetic acid alkyl alcohol in the hydrogenation reaction, return tank 7 liquid phase dischargings, new hydrogen make mouth 8 replenish in fresh hydrogen, the device round-robin hydrogen and additional fresh hydrogen and get into hydrogenation feed exchanger 9 in the lump and carry out heat exchange, get into hydrogenation feed heater 11 then; Heat the back by steam and get into hydrogenator 15, said hydrogenator 15 is a calandria type fixed bed reactor, the granular hydrogenation catalyst of filling solid in the tubulation; Shell side is the cold carrier (like de-salted water) that shifts out reaction heat; The hydrogenation products that shifts out gets into 10 coolings of product water cooler after 5 heat exchange of hydrogenation feed exchanger, carry out the hydrogenation products gas-liquid separation at knockout drum 12; The gas of volume percent 80-100% gets into circulator 14; Raw hydrogen is recycled, and the gas of volume percent 1-20% passes through blow-down pipe 13 with gas emptying, rare gas elementes such as cumulative nitrogen, argon gas in the discharger; Liquid phase gets into rectifying separation mechanism 16 and separates; By drawing product ethanol in the following separating opening 18 in the rectifying separation mechanism 16, last separating opening 17 isolated alkyl alcohols add pipeline 1 with alkyl alcohol and are connected, and return esterification system and recycle; The unreacted acetic ester of hydrogenation turns back to return tank through rectifying separation mechanism 16 upper bottom portion separating openings 19 with acetic ester.
The above is merely the preferred embodiment of the utility model, is not the protection domain that is used to limit the utility model.
Claims (9)
1. an acetic acid prepares the alcoholic acid process unit; It is characterized in that; Include esterifying kettle, reaction fractionating tower, overhead condenser, return tank; Hydrogenation feed exchanger, hydrogenation feed heater, hydrogenator, strainer, product water cooler, knockout drum, rectifying separation mechanism, and be connected through connecting tube successively, said esterifying kettle is furnished with raw material acetic acid and adds pipeline, alkyl alcohol adding pipeline and catalyst sulfuric acid adding pipeline; Last separating opening in the said rectifying separation mechanism adds pipeline with alkyl alcohol and is connected, and the following separating opening in the said rectifying separation mechanism is isolated alcohol product.
2. acetic acid according to claim 1 prepares the alcoholic acid process unit, it is characterized in that, said knockout drum is connected with the hydrogenation feed exchanger through circulator by connecting tube.
3. acetic acid according to claim 2 prepares the alcoholic acid process unit, it is characterized in that, said knockout drum is connected with blow-down pipe with the connecting tube that circulator is connected.
4. acetic acid according to claim 2 prepares the alcoholic acid process unit, it is characterized in that, the connecting tube between said circulator and the hydrogenation feed exchanger is provided with new hydrogen make mouth.
5. acetic acid according to claim 1 prepares the alcoholic acid process unit; It is characterized in that; Separating opening adds pipeline with alkyl alcohol and is connected in the said rectifying separation mechanism, and the bottom separating opening in the said rectifying separation mechanism is connected with return tank through connecting tube.
6. acetic acid according to claim 1 prepares the alcoholic acid process unit, it is characterized in that, said return tank is connected with reaction fractionating tower through connecting tube.
7. acetic acid according to claim 1 prepares the alcoholic acid process unit, it is characterized in that, said reactive distillation tower bottom is furnished with the aqueous sulfuric acid vent line.
8. acetic acid according to claim 1 prepares the alcoholic acid process unit, it is characterized in that, said alkyl alcohol adds pipeline and is connected with reaction fractionating tower.
9. acetic acid according to claim 1 prepares the alcoholic acid process unit, it is characterized in that, said rectifying separation mechanism is made up of one or more rectifying separation tower.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2011202570711U CN202214306U (en) | 2011-07-20 | 2011-07-20 | Process device for preparing ethanol by utilizing acetic acid |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2011202570711U CN202214306U (en) | 2011-07-20 | 2011-07-20 | Process device for preparing ethanol by utilizing acetic acid |
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| Publication Number | Publication Date |
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| CN202214306U true CN202214306U (en) | 2012-05-09 |
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| Application Number | Title | Priority Date | Filing Date |
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| CN2011202570711U Expired - Lifetime CN202214306U (en) | 2011-07-20 | 2011-07-20 | Process device for preparing ethanol by utilizing acetic acid |
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| CN (1) | CN202214306U (en) |
Cited By (12)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103570495A (en) * | 2012-07-25 | 2014-02-12 | 上海浦景化工技术有限公司 | Device and method for multistage acetic acid or acetate catalytic hydrogenation-based ethanol preparation |
| US8748673B2 (en) | 2011-11-18 | 2014-06-10 | Celanese International Corporation | Process of recovery of ethanol from hydrogenolysis process |
| US8802901B2 (en) | 2011-11-18 | 2014-08-12 | Celanese International Corporation | Continuous ethyl acetate production and hydrogenolysis thereof |
| US8829251B2 (en) | 2011-11-18 | 2014-09-09 | Celanese International Corporation | Liquid esterification method to produce ester feed for hydrogenolysis |
| US8829249B2 (en) | 2011-11-18 | 2014-09-09 | Celanese International Corporation | Integrated esterification and hydrogenolysis process for producing ethanol |
| US8853468B2 (en) | 2011-11-18 | 2014-10-07 | Celanese International Corporation | Vapor esterification method to produce ester feed for hydrogenolysis |
| US8853470B2 (en) | 2011-11-22 | 2014-10-07 | Celanese International Corporation | Esterifying an ethanol and acetic acid mixture to produce an ester feed for hydrogenolysis |
| US8859827B2 (en) | 2011-11-18 | 2014-10-14 | Celanese International Corporation | Esterifying acetic acid to produce ester feed for hydrogenolysis |
| US8975451B2 (en) | 2013-03-15 | 2015-03-10 | Celanese International Corporation | Single phase ester feed for hydrogenolysis |
| US9024089B2 (en) | 2011-11-18 | 2015-05-05 | Celanese International Corporation | Esterification process using extractive separation to produce feed for hydrogenolysis |
| US9029614B2 (en) | 2011-12-14 | 2015-05-12 | Celanese International Corporation | Phasing reactor product from hydrogenating acetic acid into ethyl acetate feed to produce ethanol |
| US9353035B2 (en) | 2014-04-28 | 2016-05-31 | Celanese International Corporation | Process for producing ethanol with zonal catalysts |
-
2011
- 2011-07-20 CN CN2011202570711U patent/CN202214306U/en not_active Expired - Lifetime
Cited By (13)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US9024089B2 (en) | 2011-11-18 | 2015-05-05 | Celanese International Corporation | Esterification process using extractive separation to produce feed for hydrogenolysis |
| US8748673B2 (en) | 2011-11-18 | 2014-06-10 | Celanese International Corporation | Process of recovery of ethanol from hydrogenolysis process |
| US8802901B2 (en) | 2011-11-18 | 2014-08-12 | Celanese International Corporation | Continuous ethyl acetate production and hydrogenolysis thereof |
| US8829251B2 (en) | 2011-11-18 | 2014-09-09 | Celanese International Corporation | Liquid esterification method to produce ester feed for hydrogenolysis |
| US8829249B2 (en) | 2011-11-18 | 2014-09-09 | Celanese International Corporation | Integrated esterification and hydrogenolysis process for producing ethanol |
| US8853468B2 (en) | 2011-11-18 | 2014-10-07 | Celanese International Corporation | Vapor esterification method to produce ester feed for hydrogenolysis |
| US8859827B2 (en) | 2011-11-18 | 2014-10-14 | Celanese International Corporation | Esterifying acetic acid to produce ester feed for hydrogenolysis |
| US8853470B2 (en) | 2011-11-22 | 2014-10-07 | Celanese International Corporation | Esterifying an ethanol and acetic acid mixture to produce an ester feed for hydrogenolysis |
| US9029614B2 (en) | 2011-12-14 | 2015-05-12 | Celanese International Corporation | Phasing reactor product from hydrogenating acetic acid into ethyl acetate feed to produce ethanol |
| CN103570495A (en) * | 2012-07-25 | 2014-02-12 | 上海浦景化工技术有限公司 | Device and method for multistage acetic acid or acetate catalytic hydrogenation-based ethanol preparation |
| CN103570495B (en) * | 2012-07-25 | 2016-02-17 | 上海浦景化工技术股份有限公司 | The device and method of a kind of multistage acetic acid or acetic ester shortening ethanol |
| US8975451B2 (en) | 2013-03-15 | 2015-03-10 | Celanese International Corporation | Single phase ester feed for hydrogenolysis |
| US9353035B2 (en) | 2014-04-28 | 2016-05-31 | Celanese International Corporation | Process for producing ethanol with zonal catalysts |
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| Date | Code | Title | Description |
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| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CX01 | Expiry of patent term |
Granted publication date: 20120509 |
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| CX01 | Expiry of patent term |