CN209010416U - A kind of device using the light alcohol preparation anhydrous low-carbon mixed alcohol of F- T synthesis by-product - Google Patents
A kind of device using the light alcohol preparation anhydrous low-carbon mixed alcohol of F- T synthesis by-product Download PDFInfo
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- CN209010416U CN209010416U CN201821338855.5U CN201821338855U CN209010416U CN 209010416 U CN209010416 U CN 209010416U CN 201821338855 U CN201821338855 U CN 201821338855U CN 209010416 U CN209010416 U CN 209010416U
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Abstract
A kind of device using the light alcohol preparation anhydrous low-carbon mixed alcohol of F- T synthesis by-product, described device includes by the sequentially connected infiltrating and vaporizing membrane dewatering unit of pipeline, hydrogenation unit and adsorption dewatering unit, wherein the infiltrating and vaporizing membrane dewatering unit includes passing through the sequentially connected feed heater of pipeline and infiltrating and vaporizing membrane dehydrator；The hydrogenation unit includes passing through the sequentially connected hydrogenating materials heater of pipeline, hydrogenator and hydrogenation liquid/gas separator；The adsorption dewatering unit includes adding the light alcohol heater of hydrogen and adsorption tower by the way that pipeline is sequentially connected.The content of water and non-alcohols oxygen-containing organic compound in low carbon mixed alcohol can be effectively reduced in the utility model, improves product quality.
Description
Technical field
The utility model belongs to chemical technology field, and in particular to it is a kind of using the light alcohol of F- T synthesis by-product prepare it is anhydrous low
The device of carbon mixed alcohol.
Background technique
In the ICL for Indirect Coal Liquefaction of F- T synthesis route, a large amount of aqueous phase by-product, water phase by-product are inevitably generated
Object obtains aqueous light alcohol, predominantly low-carbon alcohols (methanol, ethyl alcohol, propyl alcohol, butanol) by the processing such as oil removing, neutralization, rectifying and dewatering
And water, also contain aldehyde (acetaldehyde, propionic aldehyde, butyraldehyde), ketone (acetone, butanone, pentanone, hexanone), ester (methyl acetate, ethyl acetate) etc.
Non-alcohols low-carbon oxygen-containing organic compound.
The components such as water and ethyl alcohol, propyl alcohol, butanol in the light alcohol of F- T synthesis by-product form alcohol-water azeotropic mixture, and non-alcohols contain
Oxygen organic compound and water or alcohol form azeotropic mixture, it is difficult to be separated by conventional rectification method.The presence of azeotropic system, limit
The utilization of the light alcohol of F- T synthesis by-product is made, if light alcohol direct emission will cause the serious wasting of resources and environmental pollution.
The moisture in aqueous light alcohol is removed, non-alcohols oxygen-containing organic compound is converted, obtains anhydrous low-carbon mixed alcohol, is had huge
Significance for Environment and economic significance.
Anhydrous low-carbon mixed alcohol has broad application prospects, and summing up mainly has the following aspects: 1) being used as substitution
Fuel；2) clean gasoline additive；3) it is used as liquefied petroleum gas (LPG) substitute；4) directly as general chemistry solvent etc.；5)
Chemicals and industrial chemicals；6) further separation, is made single methanol.
Currently, being directed to the dehydration containing water azeotropic system, conventional method mainly has:
1) azeotropic distillation (constant boiling rectification method)；Third component is added in alcohol-water azeotropic system and forms new system, changes
Relative volatility in substance system between each component, and one of third component and substance system component form minimum azeotropic mixture,
It is steamed in the form of new azeotropic mixture from tower top, alcohol-water separation is realized with this and is dehydrated；
2) extraction fractional distillation；Third component is added in alcohol-water azeotropic system and forms new system, changes each group in substance system
/ relative volatility, third component with high boiling liquid from tower bottom be discharged, alcohol-water separation is realized with this and is dehydrated；
3) infiltration evaporation membrane separation process；The component molecular easily permeated dissolves or is adsorbed in the upstream face of film, then with mixed
Closing component permeable pressure head in object is motive force by film, then from the downstream desorption of film, and film downstream is vacuum system, the two sides point of film
Pressure is mass transfer force, is vaporized in vacuum system through object and the collection that is condensed, and realizes alcohol-water separation with this and is dehydrated；
4) molecular sieve adsorption；Molecular sieve is the solid absorbent with porous network structure, generally the silicon of crystalline state
Hydrochlorate or alumino-silicate.Every kind of molecular sieve has specific uniform aperture, and the molecule smaller than its pore size is only allowed to pass through, and
By those macromolecular substances exclusions, to play the role of " sieving ".Separation alcohol-water object system generallys use 3A molecular sieve,
I.e. the pore size of molecular sieve is 0.3nm.Because hydrone diameter is about 2.65A (1A=0.1nm), and alcohol molecular diameter score
Son sieve micro-pore diameter is big；In addition, hydrone has very strong positron-electron density, with molecular sieve there are highly polar sucking action,
Hydrone can enter molecular sieve and is firmly adsorbed on inside molecular sieve in this way, and alcohol molecule is then blocked in outside, thus real
Now water and alcohol are selectively adsorbing and separating.Molecular sieve has certain adsorption capacity, after reaching adsorption saturation, lose adsorption energy
Power needs to regenerate molecular sieve, removes the water of absorption, adsorbent of molecular sieve is made to have adsorption capacity again.
For water azeotropic system is contained, existing technology is mostly monotechnics, and each dehydration technique all has the disadvantage that
1) constant boiling rectification method, technical maturity are widely used, but nonvariant boiling reagent is produced from top of tower, and energy consumption is higher；Introduce new group
Point, there is residual in product；And the use of common nonvariant boiling reagent benzene is harmful to operator's body, therefore will be gradually by environmentally protective
Replaced new process；
2) extraction fractional distillation, extractant are produced from tower reactor, and energy consumption is smaller, but require extractant recovery tower harsh, solvent
There is partial loss, and introduce new component, has residual in product；
3) infiltration evaporation membrane separation process, low energy consumption, and alcohol selectivity is high, but the light alcohol of F- T synthesis by-product contains high level
Methanol, since methanol molecules diameter and common membrane pores diameter are close, there are methanol loss.Such as depth is carried out with membrane separation process
Dehydration, membrane module quantity is big, higher cost；
4) molecular sieve adsorption, simple process do not introduce novel substance, and process is environmentally protective, and products obtained therefrom purity is higher, but
The light alcohol water content of F- T synthesis by-product is higher, is such as directly dehydrated with molecular sieve adsorption, molecular sieve loadings are big, bed Workflow
Temperature, regenerative process process is complicated, operating difficulties.
The prior art all uses single dehydration technique in the light alcohol of separation F- T synthesis by-product, and technological adaptability is poor, and
Water and all higher actual conditions of non-alcohols oxygen-containing organic compound in light alcohol are not fully considered, cause non-alcohols in product oxygen-containing
Organic compound content is high, and alcohol content is not up to standard.
Utility model content
In order to overcome the defects of the prior art, it is prepared the utility model proposes a kind of using the light alcohol of F- T synthesis by-product
The device of anhydrous low-carbon mixed alcohol adds hydrogen by the dehydration of two steps and two steps, can be used for being prepared by the light alcohol of F- T synthesis by-product anhydrous
Low-carbon mixes alcohol.
In order to achieve the above objectives, it is mixed using the light alcohol preparation anhydrous low-carbon of F- T synthesis by-product that the utility model proposes a kind of
The device of alcohol is closed, including passes through the sequentially connected infiltrating and vaporizing membrane dewatering unit of pipeline, hydrogenation unit and adsorption dewatering unit,
Wherein the infiltrating and vaporizing membrane dewatering unit includes passing through the sequentially connected feed heater of pipeline and infiltration evaporation
Film dehydrator；
The hydrogenation unit includes passing through the sequentially connected hydrogenating materials heater of pipeline, hydrogenator and hydrogenation liquid
Separator；
The adsorption dewatering unit includes adding the light alcohol heater of hydrogen and adsorption tower by the way that pipeline is sequentially connected.
Preferably, the infiltrating and vaporizing membrane dewatering unit further includes raw material pump and is dehydrated light alcohol container, raw material pump with it is described
Feed heater is connected, and the light alcohol container of dehydration is connected with the entrance of the hydrogenation unit.
Preferably, hydrogen inlet manifold is provided on the hydrogenating materials heater, the hydrogenation liquid/gas separator is used for will
Add the light alcohol of hydrogen and unreacted Hydrogen Separation, separation adds the light alcohol of hydrogen to pass through pipeline to the adsorption dewatering unit.
Preferably, adsorbent is filled in the adsorption tower, the adsorbent, which is used to adsorb, adds the water in the light alcohol of hydrogen to obtain
Anhydrous low-carbon mixed alcohol.
Preferably, the infiltrating and vaporizing membrane dewatering unit further includes the permeate condenser connected by pipeline and infiltration gas
Liquid/gas separator, the permeate condenser are connected with the infiltration vent outlet of the infiltrating and vaporizing membrane dehydrator.
Preferably, the infiltration gas-liquid separator is connected with vacuum plant.
Preferably, the hydrogenation unit includes one or more concatenated hydrogenators, it is preferable that the hydrogenation liquid
The hydrogen of separator separation is recycled in the hydrogenator by circulating hydrogen compressor.
Preferably, the adsorption dewatering unit includes the adsorption tower of multiple parallel connections.
Preferably, the adsorbent is molecular sieve.
Preferably, the bottom of the adsorption tower by pipeline successively with low carbon mixed alcohol condenser and low carbon mixed alcohol container
It is connected, the top of the adsorption tower is successively connected with regenerated liquid condenser and regeneration liquid container by pipeline.
Preferably, the regeneration liquid container is connected with vacuum plant.
Compared with prior art, the technical solution of the utility model has the advantages that
(1) it is directed to the dehydration containing water azeotropic system, the utility model is combination dehydration technique, with single dehydration technique phase
Than advantage is obvious:
1. comparing azeotropic distillation and extraction fractional distillation, novel substance is not introduced, process is green, and product purity is higher；
2. comparing single infiltration evaporation membrane separation process, membrane module is less, and alcohol (especially methanol) loss is smaller；
3. comparing single molecular sieve adsorption, molecular sieve loadings are smaller, are not easy temperature runaway, easy to operate；
(2) the advantages of feed moisture content is higher, is dehydrated in two steps, can take off high level water using infiltration evaporation membrane separation process
Preliminary hydro-extraction is carried out to raw material, carries out deep dehydration using the low advantage of molecular sieve adsorption product moisture content；
(3) non-alcohols such as aldehyde, ketone, ester oxygen-containing organic compound content is higher in raw material, and the method for hydrogen is added with two steps, will be non-
Alcohols oxygen-containing organic compound is fully converted into alcohol, improves product quality, improves economic value.
Detailed description of the invention
Fig. 1 is the structural schematic diagram that the device of anhydrous low-carbon mixed alcohol is prepared in the utility model embodiment.
Specific embodiment
For the purpose of this utility model, technical solution and advantage is more clearly understood, below in conjunction with specific embodiment, and
Referring to attached drawing, the utility model is described in further detail.
The utility model comprehensively considers the light alcohol compositions of F- T synthesis by-product and the existing dehydration technique containing water azeotropic system to adapt to
Property, it proposes a kind of reasonable process flow, carries out preliminary hydro-extraction with infiltration evaporation membrane separation process, then add hydrogen by non-alcohols through two steps
Transforming oxygenated organic compound is alcohol, finally carries out deep dehydration with molecular sieve adsorption.
As shown in Figure 1, preparing anhydrous low-carbon mixed alcohol using the light alcohol of F- T synthesis by-product in the utility model embodiment
Device include: infiltrating and vaporizing membrane dewatering unit, hydrogenation unit and adsorption dewatering unit.
Infiltrating and vaporizing membrane dewatering unit includes raw material pump P1, feed heater H1, infiltrating and vaporizing membrane dehydrator B1, and dehydration is light
Alcohol tank D1 is dehydrated light alcohol delivery pump P2, permeate condenser H2, permeates gas-liquid separator D2, and lime set pumps P3, vacuum pump P4, with
And light alcohol inlet tube, light alcohol outlet pipe and flow control system that P1 is attached, H1 attached light alcohol inlet tube, light alcohol outlet pipe,
Heating system and temperature control system, B1 attached light alcohol inlet tube, the light alcohol outlet pipe of dehydration, infiltration gas outlet and concurrent heating system
System, the light alcohol inlet tube of D1 attached dehydration, the light alcohol outlet pipe of dehydration, the light alcohol inlet tube of P2 attached dehydration, the light alcohol outlet of dehydration
Pipe and pump flow control system, H2 attached infiltration gas inlet pipe, penetrating fluid outlet, cooling system and temperature control system,
D2 attached penetrating fluid inlet tube, penetrating fluid outlet and pumping air outlet, P3 attached penetrating fluid inlet tube, penetrating fluid go out
Mouth pipe and flow control system, P4 attached evacuation gas inlet pipe take out air outlet and vacuum degree control system.
The membrane material of infiltrating and vaporizing membrane dehydrator is organic film material or inorganic material film；The charging of infiltrating and vaporizing membrane dehydrator
State is gas phase or liquid phase, preferably gas phase.
Hydrogenation unit includes hydrogenating materials heater H3, hydrogenator R1, hydrogenator R2, hydrogenation liquid/gas separator
D3 adds the light alcohol pump P5 of hydrogen, circulating hydrogen compressor C1 and H3 attached hydrogenating materials inlet tube, hydrogenating materials outlet, cooling
System and temperature control system, R1/R2 attached inlet tube, outlet and temperature control system, D3 it is attached plus the light alcohol of hydrogen into
Mouth pipe plus the light alcohol outlet pipe of hydrogen and hydrogen outlet pipe, P5 attached hydrogenated products inlet tube plus the light alcohol outlet pipe of hydrogen and flow control
System processed, C1 attached recycle hydrogen inlet tube, recycle hydrogen outlet and compressor control system.
Hydrogenation catalyst is Raney nickel, copper catalyst or noble metal catalyst, preferably Raney nickel；Hydrogenator is
Isothermal shell and tube reactor or insulation fix bed reactor；Adding hydrogen mode is gas phase hydrogenation or liquid-phase hydrogenatin, and preferred liquid phase adds hydrogen.
Adsorption dewatering unit includes adding the light alcohol heater H4 of hydrogen, adsorption tower T1, adsorption tower T2, low carbon mixed alcohol condenser
H5, low carbon mixed alcohol tank D4, low carbon mixed alcohol pump P6, regenerated liquid condenser H6, regenerate flow container D5, regenerate liquid pump P7, vacuum pump
P8 and H4 is attached to be added the light alcohol inlet tube of hydrogen, adds the light alcohol outlet pipe of hydrogen, heating system and temperature control system, T1/T2 attached
Plus the light alcohol inlet tube of hydrogen, low carbon mixed alcohol outlet, regeneration gas outlet and adsorption column pressure control system, attached low of H5
Carbon mixed alcohol inlet tube, low-carbon mix alcohol outlet pipe, cooling system and temperature control system, D4 low carbon mixed alcohol inlet tube, low
Carbon mixed alcohol outlet, P6 attached low carbon mixed alcohol inlet tube, low carbon mixed alcohol outlet and flow control system, H6 are attached
Regeneration gas inlet pipe, regenerated liquid outlet, cooling system and temperature control system, D5 attached regenerated liquid inlet tube, regeneration
Liquid outlet takes out air outlet, and P7 attached regenerated liquid inlet tube, regenerated liquid outlet and flow control system, P8 are attached
Evacuation gas inlet pipe, take out air outlet and vacuum degree control system.
The adsorbent of adsorption tower T1/T2 can be molecular sieve.
When using described device preparation anhydrous low-carbon mixed alcohol, light alcohol is added after H1 is heated by P1 enters B1 infiltration evaporation
UF membrane dehydration, enters D1, then pressurize through P2, H3 is sent into after mixing with recycle hydrogen, sequentially enters R1 and R2 after heating after dehydration
Hydrogenation reaction occurs by non-alcohols oxygen-containing organic compound (such as aldehyde, ketone, ester etc.) hydro-conversion, enter after hydro-conversion D3 into
Row gas-liquid separation.Hydrogen at the top of D3 is mixed with fresh hydrogen Ji Wei recycle hydrogen after being sent into C1 pressurization.The bottom D3 adds the light alcohol warp of hydrogen
P5 is sent into H4, enters T1/T2 adsorption dewatering after heating vaporization and obtains low carbon mixed alcohol, enters after D4 after entering back into H5 condensation through P6
Carrying device.The infiltration gas of B1, which enters after H2 condensation, obtains penetrating fluid into D2, through P3 carrying device.P4 takes out D2 gas, maintains
The vacuum degree of B1 per-meate side guarantees osmotic, evaporating and dewatering effect；T1/T2 is arranged in parallel, and it is de- that a tower (adsorption tower) is in absorption
Another tower (regenerator) is in decompression, regeneration or boosting operating condition when water condition.The regeneration gas of regenerator enters H6 condensation, enters
D5 obtains regenerated liquid, through P7 carrying device.P8 takes out D5 gas, maintains the vacuum degree of regenerator, guarantees adsorbent regeneration effect.
In one embodiment, technological condition when preparing anhydrous low-carbon mixed alcohol is as follows:
Osmotic, evaporating and dewatering device B1: dehydration lateral pressure 0.1MPa~0.5MPa, 80 DEG C~180 DEG C of temperature；
Osmotic lateral pressure -0.1~0MPa, 80 DEG C~180 DEG C of temperature；
Hydrogenator R1/R2: 0.3~8.0MPa of reaction pressure, 90 DEG C~300 DEG C of reaction temperature；
Adsorption tower T1/T2: 0.1~0.5MPa of adsorptive pressure, 80 DEG C~180 DEG C of adsorption temp；
Regeneration pressure -0.1~0MPa, 80 DEG C~180 DEG C of regeneration temperature.
The result shows that water and non-alcohols oxygen-containing organic compound in low carbon mixed alcohol can be effectively reduced in the utility model
Content, improve product quality.
Particular embodiments described above has carried out into one the purpose of this utility model, technical scheme and beneficial effects
Step is described in detail, it should be understood that the foregoing is merely specific embodiment of the utility model, are not limited to this reality
With novel, within the spirit and principle of the utility model, any modification, equivalent substitution, improvement and etc. done should all include
It is within the protection scope of the utility model.
Claims (10)
1. a kind of device using the light alcohol preparation anhydrous low-carbon mixed alcohol of F- T synthesis by-product, which is characterized in that including passing through pipe
The sequentially connected infiltrating and vaporizing membrane dewatering unit in road, hydrogenation unit and adsorption dewatering unit；
Wherein the infiltrating and vaporizing membrane dewatering unit includes de- by the sequentially connected feed heater of pipeline and infiltrating and vaporizing membrane
Hydrophone；
The hydrogenation unit includes by the sequentially connected hydrogenating materials heater of pipeline, hydrogenator and the separation of hydrogenation liquid
Device；
The adsorption dewatering unit includes adding the light alcohol heater of hydrogen and adsorption tower by the way that pipeline is sequentially connected.
2. device as described in claim 1, wherein the infiltrating and vaporizing membrane dewatering unit further includes the infiltration connected by pipeline
Transparent liquid condenser and infiltration gas-liquid separator, the infiltration vent outlet of the permeate condenser and the infiltrating and vaporizing membrane dehydrator
It is connected.
3. device as claimed in claim 2, wherein the infiltration gas-liquid separator is connected with vacuum plant.
4. device as described in claim 1, wherein the hydrogenation unit includes one or more concatenated hydrogenators.
5. device as described in claim 1, wherein the hydrogen of the hydrogenation liquid/gas separator separation passes through circulating hydrogen compressor
It is recycled in the hydrogenator.
6. device as described in claim 1, wherein the adsorption dewatering unit includes the adsorption tower of multiple parallel connections.
7. device as described in claim 1, wherein the adsorbent in the adsorption tower is molecular sieve.
8. device as described in claim 1, wherein the bottom of the adsorption tower is successively condensed with low carbon mixed alcohol by pipeline
Device is connected with low carbon mixed alcohol container, the top of the adsorption tower by pipeline successively with regenerated liquid condenser and regenerate liquid container
It is connected, the regeneration liquid container is connected with vacuum plant.
9. device as described in claim 1, wherein the infiltrating and vaporizing membrane dewatering unit further includes raw material pump and is dehydrated light alcohol
Container, the raw material pump are connected with the feed heater, and the light alcohol container of dehydration is connected with the entrance of the hydrogenation unit.
10. device as described in claim 1, wherein hydrogen inlet manifold is provided on the hydrogenating materials heater, it is described to add
Hydrogen liquid/gas separator for that will add the light alcohol of hydrogen and unreacted Hydrogen Separation, separation plus the light alcohol of hydrogen pass through pipeline to described
Adsorption dewatering unit.
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| Application Number | Priority Date | Filing Date | Title |
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| CN201821338855.5U CN209010416U (en) | 2018-08-16 | 2018-08-16 | A kind of device using the light alcohol preparation anhydrous low-carbon mixed alcohol of F- T synthesis by-product |
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|---|---|---|---|
| CN201821338855.5U CN209010416U (en) | 2018-08-16 | 2018-08-16 | A kind of device using the light alcohol preparation anhydrous low-carbon mixed alcohol of F- T synthesis by-product |
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| CN209010416U true CN209010416U (en) | 2019-06-21 |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110833767A (en) * | 2018-08-16 | 2020-02-25 | 内蒙古伊泰煤基新材料研究院有限公司 | Device and method for preparing anhydrous low-carbon mixed alcohol by using Fischer-Tropsch synthesis byproduct light alcohol |
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2018
- 2018-08-16 CN CN201821338855.5U patent/CN209010416U/en active Active
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110833767A (en) * | 2018-08-16 | 2020-02-25 | 内蒙古伊泰煤基新材料研究院有限公司 | Device and method for preparing anhydrous low-carbon mixed alcohol by using Fischer-Tropsch synthesis byproduct light alcohol |
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