CN212315981U - Fischer-Tropsch synthesis byproduct light alcohol deesterification device - Google Patents
Fischer-Tropsch synthesis byproduct light alcohol deesterification device Download PDFInfo
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- CN212315981U CN212315981U CN202021799899.5U CN202021799899U CN212315981U CN 212315981 U CN212315981 U CN 212315981U CN 202021799899 U CN202021799899 U CN 202021799899U CN 212315981 U CN212315981 U CN 212315981U
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Abstract
A Fischer-Tropsch synthesis byproduct light alcohol deesterification device comprises a hydrogenation unit, an alkali-adding hydrolysis unit and an evaporation unit which are sequentially connected; the hydrogenation unit comprises a hydrogenation reactor and a hydrogenation gas-liquid separator, wherein an inlet of the hydrogenation gas-liquid separator is connected with an outlet in the hydrogenation reactor, an outlet at the top of the hydrogenation gas-liquid separator is used for discharging separated hydrogen, and an outlet at the bottom of the hydrogenation gas-liquid separator is used for discharging separated liquid hydrogenation products; the alkali-adding hydrolysis unit comprises an alkali-adding stirring tank, and an inlet of the alkali-adding stirring tank is connected with an outlet at the bottom of the hydrogen-adding gas-liquid separator through a pipeline; the evaporation unit comprises an evaporator, an inlet of the evaporator is connected with an outlet of the alkali adding stirring tank through a pipeline, a top outlet of the evaporator is used for discharging gaseous light alcohol products, and a bottom outlet of the evaporator is used for discharging carboxylate.
Description
Technical Field
The utility model belongs to the technical field of the chemical industry, concretely relates to light mellow wine deesterification device of ft synthesis byproduct can obtain the light mellow wine of high purity.
Background
In the coal indirect liquefaction of a Fischer-Tropsch synthesis route, a large amount of aqueous phase byproducts are inevitably generated, and the aqueous phase byproducts are subjected to oil removal, neutralization, rectification dehydration, pervaporation dehydration and other treatments to obtain light alcohol with low water content, mainly low carbon alcohol (such as methanol, ethanol, propanol, butanol and the like) and a small amount of water, and also contain a certain amount of ester and other oxygen-containing organic compounds.
The Fischer-Tropsch synthesis byproduct light alcohol has multiple ester types, wide distillation range and complex properties, can form an azeotropic system with water, alcohol and other oxygen-containing organic compounds, and is difficult to treat by a conventional rectification method. The existence of an azeotropic system limits the utilization of light alcohol which is a byproduct in Fischer-Tropsch synthesis, the ester content is higher, the content of the light alcohol and the alcohol in the treated monoalcohol can not reach the standard, and serious resource waste and environmental pollution can be caused if the light alcohol is directly discharged. The ester is converted and separated to obtain the low-carbon mixed alcohol without ester, and the method has great environmental significance and economic significance.
The low-carbon mixed alcohol has wide application prospect, and has the following main aspects in summary: 1) as an alternative fuel; 2) a clean gasoline additive; 3) as a Liquefied Petroleum Gas (LPG) substitute; 4) directly used as a general chemical solvent, etc.; 5) chemicals and chemical raw materials; 6) further processing to obtain the mono-alcohol.
At present, the conventional methods mainly comprise the following steps for treating ester in alcohol:
1) azeotropic distillation (azeotropic distillation); a third component is added into the azeotropic system to form a new system, the relative volatility of each component in the original system is changed, the third component and one component in the original system form the lowest azeotrope, and the lowest azeotrope is evaporated from the tower top in a new azeotrope form, so that the separation of alcohol and ester is realized.
2) An extraction and rectification method: adding an extracting agent with high boiling point into an azeotropic system to form a new system, changing the relative volatility of each component in the original system, distilling the low boiling point component from the tower top, and discharging the high boiling point component and the extracting agent from the tower bottom, thereby realizing the separation of alcohol and ester.
3) A hydrogenation method: under the action of a hydrogenation catalyst, ester containing carboxyl reacts with hydrogen to generate alcohol, so that the content of the alcohol is improved while impurities are removed, and the resource utilization of the impurities is realized.
4) A hydrolysis method; the ester contains a carboxyl group and can undergo a hydrolysis reaction with a base to form an alcohol and a carboxylate. And (3) evaporating the alkoxide mixed solution to realize alkoxide separation to obtain alcohol.
5) Resin adsorption method: the macroporous resin is used for adsorbing the higher fatty acid ester, has the advantages of good selectivity, large adsorption capacity, high mechanical strength, convenient regeneration treatment, easy desorption and the like, is suitable for removing the higher fatty acid ester in the low alcohol wine, prevents the higher fatty acid ester in the low alcohol wine from being separated out at low temperature to influence the appearance of the wine, and does not influence the flavor of the wine.
For the treatment of ester compounds, most of the existing technologies are single technologies, and each treatment technology has the following defects:
1) azeotropic distillation: the process is mature and has wide application, but the azeotropic agent is extracted from the top of the tower, so the energy consumption is higher; introducing new components, and leaving residues in the product; moreover, the commonly used azeotropic agent is harmful to the body of the operator, so the method is gradually replaced by a new green and environment-friendly process. Meanwhile, the carbon number distribution of the light alcohol component which is the byproduct of the Fischer-Tropsch synthesis is wide, the boiling point difference is large, and the azeotropic agent suitable for industrial production is difficult to find.
2) An extraction and rectification method: the process is mature and has wide application, but the dosage of the extracting agent is large, the recycling of the extracting agent needs to be considered, and the energy consumption is high; new components are introduced and residues remain in the product. Meanwhile, the Fischer-Tropsch synthesis byproduct light alcohol components are more in variety and have large boiling point difference, so that the extracting agent suitable for industrial production is difficult to find.
3) A hydrogenation method: the Fischer-Tropsch synthesis byproduct light alcohol component is complex, and comprises aldehyde, ketone and other oxygen-containing organic compounds besides ester, wherein the hydrogenation capability of the aldehyde is more than that of the ketone, and the hydrogenation conversion effect of the aldehyde and the ketone is better and the ester is poorer by adopting a hydrogenation method. Generally, the hydrogenation reaction temperature of aldehyde and ketone is low, and the hydrogenation reaction temperature of ester is high, but by adopting high-temperature hydrogenation, side reactions of aldehyde, ketone and other oxygen-containing organic compounds can occur, intermolecular or intramolecular dehydration reaction of alcohol can occur, ether or olefin is generated, the loss of alcohol is caused, and new non-alcohol impurities are generated.
4) A hydrolysis method: the carboxylic ester can be treated by hydrolysis with an alkali, but the treatment requires the addition of an alkali to form a salt, and the alcohol and the salt are separated to obtain a high-purity alcohol. As the light alcohol which is the byproduct of the Fischer-Tropsch synthesis also contains compounds containing carbonyl groups, such as aldehyde, ketone and the like, the condensation reaction can be carried out under the action of alkali, and more impurities are generated.
5) Resin adsorption method: it is commonly used for the removal of higher fatty esters from alcohols. Most of the ester in the Fischer-Tropsch synthesis byproduct light alcohol is acetate, and the selectivity is not ideal.
SUMMERY OF THE UTILITY MODEL
In order to solve the problems existing in the prior art, the utility model provides a Fischer-Tropsch synthesis byproduct light alcohol deesterification device, which can improve the purity of light alcohol.
In order to achieve the above purpose, the utility model adopts the following technical scheme:
a Fischer-Tropsch synthesis byproduct light alcohol deesterification device comprises a hydrogenation unit, an alkali-adding hydrolysis unit and an evaporation unit which are sequentially connected;
the hydrogenation unit comprises a hydrogenation reactor and a hydrogenation gas-liquid separator, wherein an inlet of the hydrogenation gas-liquid separator is connected with an outlet in the hydrogenation reactor, an outlet at the top of the hydrogenation gas-liquid separator is used for discharging separated hydrogen, and an outlet at the bottom of the hydrogenation gas-liquid separator is used for discharging separated liquid hydrogenation products;
the alkali-adding hydrolysis unit comprises an alkali-adding stirring tank, and an inlet of the alkali-adding stirring tank is connected with an outlet at the bottom of the hydrogen-adding gas-liquid separator through a pipeline;
the evaporation unit comprises an evaporator, an inlet of the evaporator is connected with an outlet of the alkali adding stirring tank through a pipeline, a top outlet of the evaporator is used for discharging gaseous light alcohol products, and a bottom outlet of the evaporator is used for discharging carboxylate.
In some embodiments, the hydrogenation unit further comprises a recycle hydrogen compressor connected to the top outlet of the hydrogenation gas-liquid separator for pressurizing and recycling the separated hydrogen gas to the hydrogenation reactor.
In some embodiments, the hydrogenation unit further comprises a hydrogenation raw material heater, and the light alcohol and the hydrogen gas which are byproducts of the fischer-tropsch synthesis enter the hydrogenation reactor after being heated by the hydrogenation raw material heater.
In some embodiments, the hydrogenation unit further comprises a hydrogenation product cooler disposed on the conduit between the hydrogen-added gas-liquid separator and the alkali-added agitator tank.
In some embodiments, the hydrogenation unit comprises a plurality of hydrogenation reactors in series.
In some embodiments, the hydrogenation reactor is an isothermal shell and tube reactor or an adiabatic fixed bed reactor.
In some embodiments, the hydrogenation unit further comprises a feedstock pump for pumping fischer-tropsch synthesis by-product light alcohols into the hydrogenation reactor.
In some embodiments, a pipe between the alkali-adding stirring tank and the hydrogen-adding gas-liquid separator is provided with an alkali-adding stirring tank feeding pump.
In some embodiments, an evaporator feed pump is disposed on the conduit between the evaporator and the alkalizing agitation tank.
In some embodiments, the evaporator is heated by steam or electricity.
Compared with the prior art, the utility model discloses the composition characteristics and the prior art adaptability of taking comprehensive consideration of ft synthesis byproduct light alcohol provide a reasonable process flow, one step of hydrogenation, one step of alkali that adds, one step of evaporation, the advantage is as follows:
(1) to the ester in the light alcohol of ft synthesis byproduct, the utility model discloses a combination treatment technique compares with single processing technique, and the advantage is obvious:
compared with an azeotropic distillation method and an extractive distillation method, no new substance is introduced, the process is green, and the product purity is high;
compared with a single hydrogenation treatment method, ester can be completely converted, the reaction temperature is low, side reactions are few, and the alcohol content in the product is high;
compared with a single alkali hydrolysis method, the side reaction is less;
(2) the raw material contains a certain amount of aldehyde and ketone besides ester, and the aldehyde and ketone are converted into alcohol while most of the ester is processed by a one-step hydrogenation method.
(3) On the basis of most of ester and all aldehyde and ketone in the hydrogenation treatment, the residual ester is converted into alcohol and carboxylate by the method of adding alkali for hydrolysis, and then the alcohol and salt are separated by the method of evaporation to obtain high-purity light alcohol.
Drawings
The drawings are only intended to illustrate and explain the present invention and do not limit the scope of the invention. Wherein:
FIG. 1 is a schematic structural view of a Fischer-Tropsch synthesis byproduct light alcohol deesterification device according to an embodiment of the present invention;
FIG. 2 is a schematic structural view of a Fischer-Tropsch synthesis byproduct light alcohol deesterification device according to another embodiment of the present invention;
FIG. 3 is a flow chart of a method for removing ester from Fischer-Tropsch synthesis byproduct light alcohol according to an embodiment of the present invention;
description of reference numerals:
1-a hydrogenation reactor; 2-a hydrogenation feedstock heater; 3-a recycle hydrogen compressor; 4-hydrogen adding gas-liquid separator; 5-hydrogenation product cooler; 6-raw material pump; 7-adding alkali stirring tank; 8-alkali adding stirring tank feeding pump; 9-an evaporator; 10-evaporator feed pump.
Detailed Description
In order to make the objects, technical solutions and advantages of the present invention more apparent, the present invention will be described in detail with reference to the accompanying drawings.
In the description of the present invention, reference to "one embodiment" means that a specific feature, structure, or parameter, step, or the like described in the embodiment is included in at least one embodiment according to the present invention. Thus, the use of terms such as "in one embodiment," "in one embodiment," and the like, in the description of the invention is not intended to refer specifically to the same embodiment, nor is the use of terms such as "in another embodiment," "in a different embodiment of the invention," "in another embodiment of the invention," and the like, in the description of the invention intended to refer specifically to features that are included in a particular different embodiment. Those of skill in the art will understand that the particular features, structures or parameters, steps, etc., disclosed in one or more embodiments of the present disclosure may be combined in any suitable manner.
In the description of the present invention, it is to be noted that, unless otherwise explicitly specified or limited, the terms "connected" and "connected" are to be interpreted broadly, and may be, for example, fixedly connected, detachably connected, or integrally connected; may be directly connected or indirectly connected through an intermediate. The specific meaning of the above terms in the present invention can be understood as appropriate by those of ordinary skill in the art.
The utility model discloses synthesize the light mellow wine of taking into account Fischer-Tropsch synthesis byproduct and constitute and have ester processing technology adaptability of water azeotropy system now, propose a reasonable light mellow wine of Fischer-Tropsch synthesis byproduct and take off ester device and process flow, adopt the method of hydrogenation to turn into alcohol (the aldehyde that exists in the raw materials and ketone are also turned into alcohol simultaneously) with most ester under the suitable temperature earlier, adopt the method of adding alkali hydrolysis again to turn into alcohol and carboxylate with remaining ester, evaporate at last and make the separation of alcohol and salt, obtain the light mellow wine that does not contain ester.
As shown in FIG. 1, in one embodiment, the device for removing ester from byproduct of Fischer-Tropsch synthesis of the present invention comprises a hydrogenation unit, an alkaline hydrolysis unit and an evaporation unit, which are connected in sequence.
The hydrogenation unit comprises a hydrogenation reactor 1, a hydrogenation raw material heater 2, a recycle hydrogen compressor 3, a hydrogenation gas-liquid separator 4 and a gas-added product cooler 5, a raw material pump 6 is connected with an inlet of the hydrogenation raw material heater 2 through a raw material conveying pipeline and is used for pumping light alcohol into the hydrogenation raw material heater 2, a hydrogen source is connected with an inlet of the hydrogenation raw material heater 2 through a gas pipeline, an outlet of the hydrogenation raw material heater 2 is connected with an inlet of hydrogen passing through the hydrogenation raw material heater 2, an outlet of the hydrogenation raw material heater 2 is connected with an inlet of the hydrogen-liquid separator 4, a hydrogen outlet is formed in the top of the hydrogen-liquid separator 4 and is used for discharging unreacted hydrogen, the recycle hydrogen compressor 3 is connected with the hydrogen outlet and is used for compressing a part of discharged hydrogen and conveying the compressed hydrogen into the hydrogenation raw material heater 2, the rest tail gas can be discharged, and a hydrogenation product outlet is formed in, the outlet of the hydrogenated product is connected with the inlet of the aerated product cooler 5, and the outlet of the aerated product cooler 5 is connected with the alkali-adding hydrolysis unit.
The alkali adding hydrolysis unit comprises an alkali adding stirring tank 7, a stirrer, a hydrogenation product inlet and an alkali inlet are arranged on the alkali adding stirring tank 7, the hydrogenation product inlet is connected with an outlet of the hydrogenation product cooler 5 through a pipeline, an alkali adding stirring tank feed pump 8 is arranged on the pipeline, an opening is formed in the bottom of the alkali adding stirring tank 7, and the opening is connected with the evaporation unit.
The evaporation unit comprises an evaporator 9, an inlet of the evaporator 9 is connected with a bottom opening of the alkali-adding stirring tank 7 through a pipeline, an evaporator feed pump 10 is arranged on the pipeline, the evaporator 9 separates the hydrolysate into vaporous low-carbon mixed alcohol and crystallized carboxylate, the low-carbon mixed alcohol is discharged from a top outlet of the evaporator 9, and the crystallized carboxylate is discharged from a bottom opening of the evaporator 9. The evaporator 9 may be heated by steam or electric heating. Preferably, an agitator may be provided on the evaporator 9.
In an embodiment of the present invention, the hydrogenation unit may comprise a plurality of hydrogenation reactors connected in series.
In another embodiment, as shown in fig. 2, the fischer-tropsch synthesis byproduct light alcohol deesterification apparatus of the present invention may not include a recycle hydrogen compressor, and is used in situations where the throughput is low, or the content of esters and other non-alcoholic oxygen-containing organic compounds in the light alcohol is low and the hydrogen consumption is low, and there is no need to recover hydrogen.
Correspondingly, the utility model relates to a ft synthesis by-product light alcohol deesterification method, this method adopt the method of three step treatment to realize the processing of ester in the light alcohol, and wherein most ester turns into alcohol through one-step hydrogenation, and remaining ester is taken to add alkali and is turned into alcohol and carboxylate with ester, adopts the method of evaporative crystallization at last to separate alcohol and salt and obtain alcohol, guarantees that alcohol content is up to standard in the product, guarantees simultaneously that impurity content does not exceed standard.
As shown in fig. 1 and 3, in one embodiment, the method for removing ester from light alcohol byproduct from fischer-tropsch synthesis of the present invention comprises the following steps:
1) the light alcohol raw material is pressurized by a raw material pump 6, external hydrogen and circulating hydrogen are mixed, the mixture enters a hydrogenation raw material heater 2 after the mixture is mixed, and then enters a hydrogenation reactor 1 for hydrogenation reaction. And (4) feeding the hydrogenated light alcohol into a hydrogen adding gas-liquid separator 4 to obtain circulating hydrogen and hydrogenated light alcohol. One part of the recycle hydrogen is pressurized by the recycle hydrogen compressor 3 and then mixed with the fresh hydrogen, and one part of the recycle hydrogen is discharged. The hydrogenated light alcohol is cooled by a hydrogenated product cooler 5 and then enters an alkali adding stirring tank 7 through an alkali adding stirring tank feeding pump 8;
2) adding alkali into the alkali adding stirring tank 7, mixing with light alcohol under the action of a stirrer and reacting. The light alcohol containing salt which is fully stirred and mixed is sent to an evaporator 9 through an evaporator feeding pump 10;
3) the light alcohol product in vapor state is obtained at the top of the evaporator 9, and the carboxylate as a byproduct is obtained at the bottom of the evaporator 9.
To determine suitable hydrogenation reaction conditions, the light alcohol component may be analyzed prior to hydrogenation. Within certain limits, the higher the temperature and pressure, the better the hydrodeesterification, but side reactions may increase. In an embodiment of the present invention, the reaction pressure of the hydrogenation reactor 1 is 1.0 to 6.0MPa (e.g. 2.0MPa, 3.0MPa, 4.0MPa or 5.0MPa), and the reaction temperature is 80 ℃ to 300 ℃ (e.g. 100 ℃, 150 ℃, 200 ℃ or 250 ℃); the hydrogenation catalyst may be a nickel catalyst, a copper catalyst or a noble metal catalyst, preferably a nickel catalyst. The hydrogenation reactor can be an isothermal tubular reactor or an adiabatic fixed bed reactor. The hydrogenation mode is liquid phase hydrogenation or gas phase hydrogenation, and liquid phase hydrogenation is preferred.
The pressure of the alkali-adding stirring tank 7 is 0.05MPa to 0.5MPa (e.g., 0.1MPa, 0.2MPa, 0.3MPa or 0.4MPa), and the temperature is 20 ℃ to 80 ℃ (e.g., 30 ℃, 40 ℃, 50 ℃, 60 ℃ or 70 ℃); the alkali added may be sodium hydroxide, potassium hydroxide or quicklime, preferably sodium hydroxide. The base to be added may be a solid base or a liquid base solution, preferably a solid base.
The pressure of the evaporator 9 is 0.05MPa to 0.15MPa (e.g., 0.08MPa, 0.1MPa, or 0.12MPa), and the temperature is 100 ℃ to 200 ℃ (e.g., 120 ℃, 150 ℃, or 180 ℃).
Example 1
1) The light alcohol raw material is pressurized by a raw material pump 6, external hydrogen and circulating hydrogen are mixed, the mixture enters a hydrogenation raw material heater 2 after the mixture is mixed, and then enters a hydrogenation reactor 1 for hydrogenation reaction.
The hydrogenation reactor 1 is an isothermal tubular reactor, the reaction pressure is 1.0MPa, the reaction temperature is 300 ℃, the hydrogenation catalyst is a nickel catalyst, and the hydrogenation mode is liquid phase hydrogenation. And (4) feeding the hydrogenated light alcohol into a hydrogen adding gas-liquid separator 4 to obtain circulating hydrogen and hydrogenated light alcohol. One part of the recycle hydrogen is pressurized by the recycle hydrogen compressor 3 and then mixed with the fresh hydrogen, and one part of the recycle hydrogen is discharged. The hydrogenated light alcohol is cooled by a hydrogenated product cooler 5 and then enters an alkali adding stirring tank 7 through an alkali adding stirring tank feeding pump 8;
2) adding solid sodium hydroxide into an alkali adding stirring tank 7, wherein the pressure of the alkali adding stirring tank 7 is 0.05MPa, and the temperature is 20 ℃. The sodium hydroxide is mixed with the light alcohol under the action of a stirrer and reacts. The light alcohol containing salt which is fully stirred and mixed is sent to an evaporator 9 through an evaporator feeding pump 10;
3) the pressure of the evaporator 9 is kept at 0.05MPa, the temperature is kept at 100 ℃, the low-carbon mixed alcohol in a vapor state is obtained at the top of the evaporator 9, and the byproduct sodium carboxylate is obtained at the bottom of the evaporator 9.
The detection shows that the content of ester in the obtained light alcohol product is 0.05%.
Example 2
1) The light alcohol raw material is pressurized by a raw material pump 6, external hydrogen and circulating hydrogen are mixed, the mixture enters a hydrogenation raw material heater 2 after the mixture is mixed, and then enters a hydrogenation reactor 1 for hydrogenation reaction.
The hydrogenation reactor 1 is an isothermal tubular reactor, the reaction pressure is 6.0MPa, the reaction temperature is 80 ℃, the hydrogenation catalyst is a nickel catalyst, and the hydrogenation mode is liquid phase hydrogenation.
And (4) feeding the hydrogenated light alcohol into a hydrogen adding gas-liquid separator 4 to obtain circulating hydrogen and hydrogenated light alcohol. One part of the recycle hydrogen is pressurized by the recycle hydrogen compressor 3 and then mixed with the fresh hydrogen, and one part of the recycle hydrogen is discharged. The hydrogenated light alcohol is cooled by a hydrogenated product cooler 5 and then enters an alkali adding stirring tank 7 through an alkali adding stirring tank feeding pump 8;
2) adding the quicklime into an alkali adding stirring tank 7, wherein the pressure of the alkali adding stirring tank 7 is 0.5MPa, and the temperature is 80 ℃. The quicklime is mixed with the light alcohol and reacts under the action of the stirrer. The light alcohol containing salt which is fully stirred and mixed is sent to an evaporator 9 through an evaporator feeding pump 10;
3) the pressure of the evaporator 9 is kept at 0.15MPa, the temperature is kept at 200 ℃, the low-carbon mixed alcohol in a vapor state is obtained at the top of the evaporator 9, and the by-product calcium carboxylate is obtained at the bottom of the evaporator 9.
The detection shows that the content of ester in the obtained light alcohol product is 0.08%.
Comparative example 1
The light alcohol raw material is pressurized by a raw material pump 6, external hydrogen and circulating hydrogen are mixed, the mixture enters a hydrogenation raw material heater 2 after the mixture is mixed, and then enters a hydrogenation reactor 1 for hydrogenation reaction.
The hydrogenation reactor 1 is an isothermal tubular reactor, the reaction pressure is 5.0MPa, the reaction temperature is 150 ℃, the hydrogenation catalyst is a nickel catalyst, and the hydrogenation mode is liquid phase hydrogenation.
And (4) feeding the hydrogenated light alcohol into a hydrogen adding gas-liquid separator 4 to obtain circulating hydrogen and hydrogenated light alcohol. One part of the recycle hydrogen is pressurized by the recycle hydrogen compressor 3 and then mixed with the fresh hydrogen, and one part of the recycle hydrogen is discharged. And cooling the hydrogenated light alcohol by a hydrogenated product cooler 5 to obtain a light alcohol product.
The detection shows that the content of ester in the obtained light alcohol product is 0.45%.
Comparative example 2
The light alcohol raw material enters an alkali-adding stirring tank 7 through an alkali-adding stirring tank feeding pump 8;
adding solid sodium hydroxide into an alkali adding stirring tank 7, wherein the pressure of the alkali adding stirring tank 7 is 0.05MPa, and the temperature is 20 ℃. The sodium hydroxide is mixed with the light alcohol under the action of a stirrer and reacts. The light alcohol containing salt which is fully stirred and mixed is sent to an evaporator 9 through an evaporator feeding pump 10;
the pressure of the evaporator 9 is kept at 0.05MPa, the temperature is kept at 150 ℃, the low-carbon mixed alcohol in a vapor state is obtained at the top of the evaporator 9, and the byproduct sodium carboxylate is obtained at the bottom of the evaporator 9.
The detection shows that the content of ester in the obtained light alcohol product is 0.85%.
The method of the utility model can firstly convert most ester, aldehyde and ketone in the raw material into alcohol, then convert the residual ester into alcohol and carboxylate through further alkali adding hydrolysis, and finally separate the alcohol and salt by using the evaporation method to obtain the high-purity light alcohol. As can be seen from the above examples and comparative examples, the method of the present invention can significantly reduce the ester content in the light alcohol product, and compared with the existing light alcohol product, the ester content can be reduced to 1/10-1/20, the quality of the light alcohol product is significantly improved, and the economic value of the product is significantly improved.
The above-mentioned embodiments, further detailed description of the objects, technical solutions and advantages of the present invention, it should be understood that the above-mentioned embodiments are only specific embodiments of the present invention, and are not intended to limit the present invention, and any modifications, equivalent substitutions, improvements, etc. made within the spirit and principle of the present invention should be included in the scope of the present invention.
Claims (10)
1. A Fischer-Tropsch synthesis byproduct light alcohol deesterification device is characterized by comprising a hydrogenation unit, an alkali-adding hydrolysis unit and an evaporation unit which are sequentially connected;
the hydrogenation unit comprises a hydrogenation reactor and a hydrogenation gas-liquid separator, wherein an inlet of the hydrogenation gas-liquid separator is connected with an outlet in the hydrogenation reactor, an outlet at the top of the hydrogenation gas-liquid separator is used for discharging separated hydrogen, and an outlet at the bottom of the hydrogenation gas-liquid separator is used for discharging separated liquid hydrogenation products;
the alkali-adding hydrolysis unit comprises an alkali-adding stirring tank, and an inlet of the alkali-adding stirring tank is connected with an outlet at the bottom of the hydrogen-adding gas-liquid separator through a pipeline;
the evaporation unit comprises an evaporator, an inlet of the evaporator is connected with an outlet of the alkali adding stirring tank through a pipeline, a top outlet of the evaporator is used for discharging gaseous light alcohol products, and a bottom outlet of the evaporator is used for discharging carboxylate.
2. The Fischer-Tropsch synthesis byproduct light alcohol deesterification device of claim 1, wherein the hydrogenation unit further comprises a recycle hydrogen compressor, and the recycle hydrogen compressor is connected with a top outlet of the hydrogen adding gas-liquid separator and is used for pressurizing and circulating the separated hydrogen to the hydrogenation reactor.
3. The Fischer-Tropsch synthesis byproduct light alcohol deesterification device of claim 1, wherein the hydrogenation unit further comprises a hydrogenation raw material heater, and the Fischer-Tropsch synthesis byproduct light alcohol and hydrogen gas enter the hydrogenation reactor after being heated by the hydrogenation raw material heater.
4. The Fischer-Tropsch synthesis byproduct light alcohol deesterification device of claim 1, wherein the hydrogenation unit further comprises a hydrogenation product cooler, and the hydrogenation product cooler is arranged on a pipeline between the hydrogen-adding gas-liquid separator and the alkali-adding stirring tank.
5. The Fischer-Tropsch synthesis byproduct light alcohol deesterification device of claim 1, wherein the hydrogenation unit comprises a plurality of hydrogenation reactors in series.
6. The Fischer-Tropsch synthesis byproduct light alcohol deesterification device of claim 1, wherein the hydrogenation reactor is an isothermal tubular reactor or an adiabatic fixed bed reactor.
7. The Fischer-Tropsch synthesis byproduct light alcohol deesterification device of claim 1, wherein the hydrogenation unit further comprises a raw material pump for pumping the Fischer-Tropsch synthesis byproduct light alcohol into the hydrogenation reactor.
8. The Fischer-Tropsch synthesis byproduct light alcohol deesterification device of claim 1, wherein a pipeline between the alkali-adding agitator tank and the hydrogen-adding gas-liquid separator is provided with an alkali-adding agitator tank feed pump.
9. The Fischer-Tropsch synthesis byproduct light alcohol deesterification device of claim 1, wherein an evaporator feed pump is arranged on a pipeline between the evaporator and the alkali adding stirring tank.
10. The Fischer-Tropsch synthesis byproduct light alcohol deesterification device of claim 1, wherein the evaporator is heated by steam or electricity.
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