CN110833767A - Device and method for preparing anhydrous low-carbon mixed alcohol by using Fischer-Tropsch synthesis byproduct light alcohol - Google Patents
Device and method for preparing anhydrous low-carbon mixed alcohol by using Fischer-Tropsch synthesis byproduct light alcohol Download PDFInfo
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Abstract
A device and a method for preparing anhydrous low-carbon mixed alcohol by using Fischer-Tropsch synthesis byproduct light alcohol are disclosed, wherein the device comprises a pervaporation membrane dehydration unit, a hydrogenation unit and an adsorption dehydration unit which are sequentially connected through pipelines, wherein the pervaporation membrane dehydration unit comprises a raw material heater and a pervaporation membrane dehydrator which are sequentially connected through pipelines; the hydrogenation unit comprises a hydrogenation raw material heater, a hydrogenation reactor and a hydrogenation gas-liquid separator which are sequentially connected through a pipeline; the adsorption dehydration unit comprises a hydrogenation light alcohol heater and an adsorption tower which are sequentially connected through a pipeline. The invention can effectively reduce the content of water and non-alcoholic oxygen-containing organic compounds in the low-carbon mixed alcohol and improve the product quality.
Description
Technical Field
The invention belongs to the technical field of chemical industry, and particularly relates to a device and a method for preparing anhydrous low-carbon mixed alcohol by using Fischer-Tropsch synthesis byproduct light alcohol.
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 and other treatments to obtain hydrous light alcohol, mainly comprising low-carbon alcohols (methanol, ethanol, propanol and butanol) and water, and also comprising non-alcohol low-carbon oxygen-containing organic compounds such as aldehydes (acetaldehyde, propionaldehyde and butyraldehyde), ketones (acetone, butanone, pentanone and hexanone), esters (methyl acetate and ethyl acetate) and the like.
Water in the Fischer-Tropsch synthesis byproduct light alcohol and components such as ethanol, propanol, butanol and the like form an alcohol-water azeotrope, and a non-alcoholic oxygen-containing organic compound and water or alcohol form an azeotrope, so that the separation is difficult to carry out by a conventional rectification method. The existence of an azeotropic system limits the utilization of the light alcohol which is a byproduct in Fischer-Tropsch synthesis, and if the light alcohol is directly discharged, serious resource waste and environmental pollution are caused. The water in the water-containing light alcohol is removed, and the non-alcohol oxygen-containing organic compound is converted to obtain the anhydrous low-carbon mixed alcohol, so that the method has great environmental significance and economic significance.
The anhydrous 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 separation to obtain the mono-alcohol.
At present, the traditional method mainly comprises the following steps of:
1) azeotropic distillation (azeotropic distillation); adding a third component into the alcohol-water azeotropic system to form a new system, changing the relative volatility of each component in the original system, forming a minimum azeotrope by the third component and one component in the original system, and evaporating the minimum azeotrope from the tower top in a new azeotrope form, thereby realizing the separation and dehydration of alcohol and water;
2) extractive distillation; adding a third component into the alcohol-water azeotropic system to form a new system, changing the relative volatility of each component in the original system, and discharging the third component from the bottom of the tower along with the high boiling point liquid so as to realize the separation and dehydration of alcohol and water;
3) pervaporation membrane separation; the permeable component molecules are dissolved or adsorbed on the upstream surface of the membrane, then the component osmotic pressure difference in the mixture is taken as driving force to pass through the membrane, and then desorption is carried out from the downstream of the membrane, the downstream of the membrane is a vacuum system, the partial pressure at the two sides of the membrane is taken as mass transfer driving force, and the permeate is vaporized and condensed and collected in the vacuum system, so that the alcohol-water separation and dehydration are realized;
4) molecular sieve adsorption; molecular sieves are solid adsorbents having a porous network structure, typically a crystalline silicate or aluminosilicate. Each molecular sieve has a specific uniform pore size that allows only molecules smaller than its pore size to pass through, while excluding those macromolecular species, thereby serving as a "sieve". The separation of the alcohol-water system usually employs a 3A molecular sieve, i.e., a molecular sieve having a pore size of 0.3 nm. Because the water molecule diameter is about 2.65A (1A ═ 0.1nm), while the alcohol molecular diameter is larger than the molecular sieve pore diameter; in addition, the water molecules have strong positive and negative electron density and have strong polarity attraction with the molecular sieve, so that the water molecules can enter the molecular sieve and are firmly adsorbed in the molecular sieve, and the alcohol molecules are blocked outside, thereby realizing the selective adsorption separation of water and alcohol. The molecular sieve has a certain adsorption capacity, loses adsorption capacity after reaching adsorption saturation, and needs to be regenerated to remove adsorbed water so that the molecular sieve adsorbent has adsorption capacity again.
Aiming at an aqueous azeotropic system, the prior art is mostly a single technology, and each dehydration technology has the defects that:
1) the azeotropic distillation method has mature process and 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 use of the commonly used azeotropic agent benzene is harmful to the bodies of operators, so the method is gradually replaced by a new green and environment-friendly process;
2) the extraction and rectification method has the advantages that the extractant is extracted from the tower kettle, the energy consumption is low, the requirement on an extractant recovery tower is strict, the solvent is partially lost, new components are introduced, and the product has residues;
3) the pervaporation membrane separation method has low energy consumption and high alcohol selectivity, but the light alcohol byproduct of Fischer-Tropsch synthesis contains higher content of methanol, and methanol loss exists because the molecular diameter of the methanol is close to the pore diameter of a common membrane. If the membrane separation method is used for deep dehydration, the number of membrane components is large, and the cost is high;
4) the molecular sieve adsorption method has the advantages of simple process, no introduction of new substances, green and environment-friendly process, high purity of the obtained product, high water content of light alcohol which is a byproduct of Fischer-Tropsch synthesis, large molecular sieve loading, easy temperature runaway of a bed layer, complex regeneration process and difficult operation if the light alcohol is directly dehydrated by the molecular sieve adsorption method.
In the prior art, when the light alcohol which is a byproduct of Fischer-Tropsch synthesis is separated, a single dehydration technology is adopted, the technical adaptability is poor, and the actual condition that water and non-alcohol oxygen-containing organic compounds in the light alcohol are higher is not fully considered, so that the content of the non-alcohol oxygen-containing organic compounds in the product is high, and the alcohol content does not reach the standard.
Disclosure of Invention
In order to overcome the defects in the prior art, the invention provides a method and a device for preparing anhydrous low-carbon mixed alcohol by using light alcohol which is a Fischer-Tropsch synthesis byproduct, and the method and the device can be used for preparing the anhydrous low-carbon mixed alcohol by using the light alcohol which is the Fischer-Tropsch synthesis byproduct through two-step dehydration and two-step hydrogenation.
In order to achieve the above purpose, in one aspect, the invention provides a device for preparing anhydrous low-carbon mixed alcohol by using light alcohol as a byproduct of Fischer-Tropsch synthesis, which comprises a pervaporation membrane dehydration unit, a hydrogenation unit and an adsorption dehydration unit which are sequentially connected through pipelines,
wherein the pervaporation membrane dehydration unit comprises a raw material heater and a pervaporation membrane dehydrator which are sequentially connected through a pipeline;
the hydrogenation unit comprises a hydrogenation raw material heater, a hydrogenation reactor and a hydrogenation gas-liquid separator which are sequentially connected through a pipeline;
the adsorption dehydration unit comprises a hydrogenation light alcohol heater and an adsorption tower which are sequentially connected through a pipeline.
Preferably, the pervaporation membrane dehydration unit further comprises a raw material pump and a dehydrated light alcohol container, wherein the raw material pump is connected with the raw material heater, and the dehydrated light alcohol container is connected with the inlet of the hydrogenation unit.
Preferably, the hydrogenation raw material heater is provided with a hydrogen input pipe, the hydrogenation gas-liquid separator is used for separating hydrogenation light alcohol from unreacted hydrogen, and the separated hydrogenation light alcohol is conveyed to the adsorption dehydration unit through a pipeline.
Preferably, the adsorption tower is filled with an adsorbent, and the adsorbent is used for adsorbing water in the hydrogenated light alcohol to obtain anhydrous low-carbon mixed alcohol.
Preferably, the pervaporation membrane dehydration unit further comprises a permeate condenser and a permeate gas-liquid separator connected by a pipeline, wherein the permeate condenser is connected with a permeate gas outlet of the pervaporation membrane dehydrator.
Preferably, the permeate gas-liquid separator is connected to a vacuum device.
Preferably, the hydrogenation unit comprises one or more hydrogenation reactors connected in series, and preferably, the hydrogen separated by the hydrogenation gas-liquid separator is recycled to the hydrogenation reactor by a recycle hydrogen compressor.
Preferably, the adsorption dehydration unit comprises a plurality of adsorption towers connected in parallel.
Preferably, the adsorbent is a molecular sieve.
Preferably, the bottom of the adsorption tower is sequentially connected with a low-carbon mixed alcohol condenser and a low-carbon mixed alcohol container through pipelines, and the top of the adsorption tower is sequentially connected with a regenerated liquid condenser and a regenerated liquid container through pipelines.
Preferably, the regeneration liquid container is connected to a vacuum device.
On the other hand, the invention also provides a method for preparing anhydrous low-carbon mixed alcohol by utilizing the Fischer-Tropsch synthesis byproduct light alcohol, which comprises the following steps:
preheating the Fischer-Tropsch synthesis byproduct light alcohol, and then carrying out pervaporation membrane separation and dehydration to obtain dehydrated light alcohol;
mixing the dehydrated light alcohol with hydrogen, heating, carrying out hydrogenation reaction to carry out hydrogenation conversion on the non-alcoholic oxygen-containing organic compound, and carrying out gas-liquid separation on a reaction product to obtain hydrogenated light alcohol;
and heating and vaporizing the hydrogenated light alcohol, and adsorbing water in the hydrogenated light alcohol by using an adsorbent to obtain the anhydrous low-carbon mixed alcohol.
Preferably, the method further comprises recycling unreacted hydrogen obtained by gas-liquid separation of the reaction product, and performing hydrogenation reaction with the dehydrated light alcohol again.
Preferably, the method further comprises the step of carrying out gas-liquid separation on penetrating fluid obtained after condensation of penetrating gas obtained by separation and dehydration of the penetrating vaporization membrane.
Preferably, the method further comprises regenerating the adsorbent to obtain a regeneration gas, and the regeneration gas is condensed to obtain a regeneration liquid, and preferably, the method for regenerating the adsorbent is decompression desorption.
Preferably, the adsorption and regeneration of the adsorbent are performed alternately in a plurality of adsorption columns connected in parallel.
Compared with the prior art, the technical scheme of the invention has the following beneficial effects:
(1) aiming at the dehydration of a water-containing azeotropic system, the invention is a combined dehydration technology, and compared with a single dehydration technology, the invention has the advantages that:
① compared with azeotropic distillation and extractive distillation, it has no new substance, green process, and high product purity;
② compared with single pervaporation membrane separation method, the membrane module is less, and the loss of alcohol (especially methanol) is less;
③ compared with single molecular sieve adsorption method, the molecular sieve has small loading, less temperature runaway, and simple operation;
(2) the raw material has higher water content and is dehydrated in two steps, the raw material is primarily dehydrated by utilizing the advantage that the pervaporation membrane separation method can remove higher water content, and deep dehydration is carried out by utilizing the advantage that the molecular sieve adsorption method product has low water content;
(3) the content of non-alcoholic oxygen-containing organic compounds such as aldehyde, ketone, ester and the like in the raw materials is high, and the non-alcoholic oxygen-containing organic compounds are fully converted into alcohol by a two-step hydrogenation method, so that the product quality is improved, and the economic value is improved.
Drawings
FIG. 1 is a schematic structural diagram of an apparatus for preparing an anhydrous low-carbon mixed alcohol according to an embodiment of the present invention.
Detailed Description
In order that the objects, technical solutions and advantages of the present invention will become more apparent, the present invention will be further described in detail with reference to the accompanying drawings in conjunction with the following specific embodiments.
The invention comprehensively considers the composition of light alcohol as a Fischer-Tropsch synthesis byproduct and the adaptability of the existing dehydration technology of a water-containing azeotropic system, provides a reasonable process flow, uses a pervaporation membrane separation method to carry out preliminary dehydration, then converts non-alcoholic oxygen-containing organic compounds into alcohol through two-step hydrogenation, and finally uses a molecular sieve adsorption method to carry out deep dehydration.
As shown in fig. 1, the apparatus for preparing anhydrous low-carbon mixed alcohol by using fischer-tropsch synthesis byproduct light alcohol in the embodiment of the present invention includes: a pervaporation membrane dehydration unit, a hydrogenation unit and an adsorption dehydration unit.
The pervaporation membrane dehydration unit comprises a raw material pump P1, a raw material heater H1, a pervaporation membrane dehydrator B1, a dehydrated light alcohol tank D1, a dehydrated light alcohol delivery pump P2, a permeate condenser H2, a permeate gas-liquid separator D2, a condensate pump P3, a vacuum pump P4, and a light alcohol inlet pipe, a light alcohol outlet pipe and a flow control system attached to P1, a light alcohol inlet pipe, a light alcohol outlet pipe, a heating system and a temperature control system attached to H1, a light alcohol, a dehydrated light alcohol outlet pipe, a permeate gas inlet pipe and a heat supplementing system attached to B1, a dehydrated light alcohol inlet pipe, a dehydrated light alcohol outlet pipe attached to D1, a dehydrated light alcohol inlet pipe, a dehydrated light alcohol outlet pipe and a pump flow control system attached to P2, a permeate gas inlet pipe, a permeate outlet pipe, a cooling system and a temperature control system attached to H2, a permeate gas inlet pipe, a permeate outlet pipe, an air inlet pipe, a permeate inlet pipe, a permeate outlet pipe and a flow control system attached to P3, and an air intake inlet pipe, an air intake outlet pipe and a vacuum control system attached to P4.
The membrane material of the pervaporation membrane dehydrator is an organic membrane material or an inorganic membrane material; the feed state to the pervaporation membrane dehydrator is gas phase or liquid phase, preferably gas phase.
The hydrogenation unit comprises a hydrogenation raw material heater H3, a hydrogenation reactor R1, a hydrogenation reactor R2, a hydrogenation gas-liquid separator D3, a hydrogenation light alcohol pump P5, a recycle hydrogen compressor C1, a hydrogenation raw material inlet pipe, a hydrogenation raw material outlet pipe, a cooling system and a temperature control system which are attached to H3, an inlet pipe, an outlet pipe and a temperature control system which are attached to R1/R2, a hydrogenation light alcohol inlet pipe, a hydrogenation light alcohol outlet pipe and a hydrogen outlet pipe which are attached to D3, a hydrogenation product inlet pipe, a hydrogenation light alcohol outlet pipe and a flow control system which are attached to P5, and a recycle hydrogen inlet pipe, a recycle hydrogen outlet pipe and a compressor control system which are attached to C1.
The hydrogenation catalyst is a nickel catalyst, a copper catalyst or a noble metal catalyst, preferably a nickel catalyst; the hydrogenation reactor is an isothermal tubular reactor or an adiabatic fixed bed reactor; the hydrogenation mode is gas phase hydrogenation or liquid phase hydrogenation, and liquid phase hydrogenation is preferred.
The adsorption dehydration unit comprises a hydrogenated light alcohol heater H4, an adsorption tower T1, an adsorption tower T2, a low-carbon mixed alcohol condenser H5, a low-carbon mixed alcohol tank D4, a low-carbon mixed alcohol pump P6, a secondary regenerated liquid condenser H6, a regenerated liquid tank D5, a regenerated liquid pump P7, a vacuum pump P8, a hydrogenated light alcohol inlet pipe, a hydrogenated light alcohol outlet pipe, a heating system and a temperature control system which are attached to H4, a hydrogenated light alcohol inlet pipe, a low-carbon mixed alcohol outlet pipe, a regenerated gas outlet pipe and an adsorption tower pressure control system which are attached to T1/T2, a low-carbon mixed alcohol inlet pipe, a low-carbon mixed alcohol outlet pipe, a regenerated gas outlet pipe and an adsorption tower pressure control system which are attached to H5, a low-carbon mixed alcohol inlet pipe, a low-carbon mixed alcohol outlet pipe, a cooling system and a temperature control system which are attached to D4, a low-carbon mixed alcohol inlet pipe, a low-carbon mixed, a regeneration liquid inlet pipe, a regeneration liquid outlet pipe and an air extraction outlet pipe which are attached to the D5, a regeneration liquid inlet pipe, a regeneration liquid outlet pipe and a flow control system which are attached to the P7, and an air extraction inlet pipe, an air extraction outlet pipe and a vacuum degree control system which are attached to the P8.
The adsorbent of adsorption column T1/T2 may be molecular sieves.
When the device is used for preparing the anhydrous low-carbon mixed alcohol, the light alcohol is added with H1 from P1, heated, enters a B1 pervaporation membrane for separation and dehydration, enters D1 after dehydration, is pressurized by P2, is mixed with circulating hydrogen, then is fed into H3, enters R1 and R2 in sequence after heating for hydrogenation reaction to carry out hydrogenation conversion on non-alcohol oxygen-containing organic compounds (such as aldehyde, ketone, ester and the like), and enters D3 for gas-liquid separation after hydrogenation conversion. The hydrogen gas at the top of the D3 is sent into the C1 to be pressurized and then is mixed with fresh hydrogen to obtain the circulating hydrogen. The hydrogenated light alcohol at the bottom of D3 is fed into H4 through P5, heated and vaporized, then fed into T1/T2 to be adsorbed and dehydrated to obtain low-carbon mixed alcohol, then fed into H5 to be condensed, fed into D4, and fed out of the device through P6. The permeating gas of B1 enters H2 to be condensed and then enters D2 to obtain permeating liquid, and the permeating liquid is sent out of the device through P3. D2 gas is pumped out from P4, the vacuum degree of the B1 permeation side is maintained, and the pervaporation dehydration effect is ensured; T1/T2 are arranged in parallel, and when one tower (adsorption tower) is in an adsorption dehydration working condition, the other tower (regeneration tower) is in a pressure reduction, regeneration or pressure increase working condition. The regenerated gas of the regeneration tower enters H6 for condensation, enters D5 to obtain regenerated liquid, and is sent out of the device through P7. D5 gas is pumped out from P8, the vacuum degree of the regeneration tower is maintained, and the regeneration effect of the adsorbent is ensured.
In one embodiment, the main process conditions for preparing the anhydrous low-carbon mixed alcohol are as follows:
pervaporation dehydrator B1: the pressure of the dehydration side is 0.1MPa to 0.5MPa, and the temperature is 80 ℃ to 180 ℃;
the pressure of the infiltration side is-0.1-0 MPa, and the temperature is 80-180 ℃;
hydrogenation reactor R1/R2: the reaction pressure is 0.3-8.0 MPa, and the reaction temperature is 90-300 ℃;
adsorption column T1/T2: the adsorption pressure is 0.1-0.5 MPa, and the adsorption temperature is 80-180 ℃;
the regeneration pressure is-0.1-0 MPa, and the regeneration temperature is 80-180 ℃.
The result shows that the invention can effectively reduce the content of water and non-alcoholic oxygen-containing organic compounds in the low-carbon mixed alcohol and improve the product quality.
The above-mentioned embodiments are intended to illustrate the objects, technical solutions and advantages of the present invention in further detail, and it should be understood that the above-mentioned embodiments are only exemplary embodiments of the present invention and are not intended to limit the present invention, and any modifications, equivalents, improvements and the like made within the spirit and principle of the present invention should be included in the protection scope of the present invention.
Claims (10)
1. A device for preparing anhydrous low-carbon mixed alcohol by using Fischer-Tropsch synthesis byproduct light alcohol is characterized by comprising a pervaporation membrane dehydration unit, a hydrogenation unit and an adsorption dehydration unit which are sequentially connected through pipelines;
wherein the pervaporation membrane dehydration unit comprises a raw material heater and a pervaporation membrane dehydrator which are sequentially connected through a pipeline;
the hydrogenation unit comprises a hydrogenation raw material heater, a hydrogenation reactor and a hydrogenation gas-liquid separator which are sequentially connected through a pipeline;
the adsorption dehydration unit comprises a hydrogenation light alcohol heater and an adsorption tower which are sequentially connected through a pipeline.
2. The apparatus of claim 1, wherein the pervaporation membrane dehydration unit further comprises a permeate condenser and a permeate gas-liquid separator connected by a pipe, the permeate condenser being connected to the permeate gas outlet of the pervaporation membrane dehydrator, preferably the permeate gas-liquid separator being connected to a vacuum device.
3. The apparatus of claim 1, wherein the hydrogenation unit comprises one or more hydrogenation reactors connected in series, and preferably, the hydrogen separated by the hydrogenation gas-liquid separator is recycled to the hydrogenation reactor by a recycle hydrogen compressor.
4. The apparatus of claim 1, wherein the adsorption dehydration unit comprises a plurality of parallel adsorption towers, and preferably, the adsorbent in the adsorption towers is molecular sieve.
5. The device of claim 1, wherein the bottom of the adsorption tower is sequentially connected with a low-carbon mixed alcohol condenser and a low-carbon mixed alcohol container through pipelines, the top of the adsorption tower is sequentially connected with a regenerated liquid condenser and a regenerated liquid container through pipelines, and the regenerated liquid container is connected with a vacuum device.
6. A method for preparing anhydrous low-carbon mixed alcohol by utilizing Fischer-Tropsch synthesis byproduct light alcohol is characterized by comprising the following steps:
preheating the Fischer-Tropsch synthesis byproduct light alcohol, and then carrying out pervaporation membrane separation and dehydration to obtain dehydrated light alcohol;
mixing the dehydrated light alcohol with hydrogen, heating, carrying out hydrogenation reaction to carry out hydrogenation conversion on the non-alcoholic oxygen-containing organic compound, and carrying out gas-liquid separation on a reaction product to obtain hydrogenated light alcohol;
and heating and vaporizing the hydrogenated light alcohol, and adsorbing water in the hydrogenated light alcohol by using an adsorbent to obtain the anhydrous low-carbon mixed alcohol.
7. The method of claim 6, further comprising recycling unreacted hydrogen obtained by gas-liquid separation of the reaction product and performing hydrogenation reaction with dehydrated light alcohol.
8. The method according to claim 6, further comprising a step of performing gas-liquid separation on a permeate obtained by condensing the permeate obtained by the separation and dehydration of the permeate by a pervaporation membrane.
9. The method of claim 6, wherein the method further comprises regenerating the adsorbent to obtain a regeneration gas, and the regeneration gas is condensed to obtain a regeneration liquid, and preferably, the method for regenerating the adsorbent is decompression desorption.
10. The method of claim 6, wherein the adsorption and regeneration of the adsorbent are performed alternately in a plurality of parallel adsorption columns.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201810947189.3A CN110833767A (en) | 2018-08-16 | 2018-08-16 | Device and method for preparing anhydrous low-carbon mixed alcohol by using Fischer-Tropsch synthesis byproduct light alcohol |
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| CN201810947189.3A CN110833767A (en) | 2018-08-16 | 2018-08-16 | Device and method for preparing anhydrous low-carbon mixed alcohol by using Fischer-Tropsch synthesis byproduct light alcohol |
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| CN201810947189.3A Pending CN110833767A (en) | 2018-08-16 | 2018-08-16 | Device and method for preparing anhydrous low-carbon mixed alcohol by using Fischer-Tropsch synthesis byproduct light alcohol |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114887354A (en) * | 2022-05-26 | 2022-08-12 | 上海淳然环境工程有限公司 | Solvent dehydration device and process based on adsorption coupling of molecular sieve membrane and molecular sieve |
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| US20120277483A1 (en) * | 2011-04-26 | 2012-11-01 | Celanese International Corporation | Water Control In Alcohol Production From Hydrogenation |
| CN103071307A (en) * | 2013-01-23 | 2013-05-01 | 江苏九天高科技股份有限公司 | Rectification-steam penetration-coupled organic solvent dewatering method and device |
| CN209010416U (en) * | 2018-08-16 | 2019-06-21 | 内蒙古伊泰煤基新材料研究院有限公司 | A kind of device using the light alcohol preparation anhydrous low-carbon mixed alcohol of F- T synthesis by-product |
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Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20120277483A1 (en) * | 2011-04-26 | 2012-11-01 | Celanese International Corporation | Water Control In Alcohol Production From Hydrogenation |
| CN103071307A (en) * | 2013-01-23 | 2013-05-01 | 江苏九天高科技股份有限公司 | Rectification-steam penetration-coupled organic solvent dewatering method and device |
| CN209010416U (en) * | 2018-08-16 | 2019-06-21 | 内蒙古伊泰煤基新材料研究院有限公司 | A kind of device using the light alcohol preparation anhydrous low-carbon mixed alcohol of F- T synthesis by-product |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114887354A (en) * | 2022-05-26 | 2022-08-12 | 上海淳然环境工程有限公司 | Solvent dehydration device and process based on adsorption coupling of molecular sieve membrane and molecular sieve |
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