CN206089513U - Device of dihydrofuran serialization production and separation - Google Patents
Device of dihydrofuran serialization production and separation Download PDFInfo
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- CN206089513U CN206089513U CN201621095508.5U CN201621095508U CN206089513U CN 206089513 U CN206089513 U CN 206089513U CN 201621095508 U CN201621095508 U CN 201621095508U CN 206089513 U CN206089513 U CN 206089513U
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Abstract
The utility model provides a device of dihydrofuran serialization production and separation, including head tank, over heater, reactor, pre -heater, condenser, feedstock pump, transfer jar, first delivery pump, first rectifying column, second rectifying column, third delivery pump, third rectifying column, the 5th delivery pump and fourth rectifying column, the head tank, feedstock pump and pre -heater shell side feed inlet are continuous in proper order, pre -heater shell side discharge gate, over heater and reactor order link to each other, the discharge gate of reactor links to each other with the tube side feed inlet of pre -heater, the tube side discharge gate of pre -heater, condensers, the transfer jar, the middle part feed inlet of first delivery pump and first rectifying column is continuous in proper order, the top discharge mouth of first rectifying column links to each other with the middle part feed inlet of second rectifying column, the feed inlet of stating bottom discharge mouth and the third rectifying column of second rectifying column is continuous in proper order, the top discharge mouth of third rectifying column links to each other with the feed inlet of fourth rectifying column. The device will synthesize and the separation coupling is in the same place, improve production efficiency.
Description
Technical field
The utility model belongs to chemical industry synthesis equipment technical field, and in particular to a kind of dihydrofuran continuous prodution and point
From device.
Background technology
Dihydrofuran is that one kind is widely used in a kind of important fine chemicals, dihydro furan in agricultural chemicals, medicine, field of polymer technology
Mutter and be divided into two kinds of isomers of DHF and DHF, about 10 DEG C of boiling-point difference；Due to olefinic double bonds position
Difference, makes two kinds of isomer nature differences very big, and then causes two kinds of products to synthesize a large amount of differences as intermediate
The different organic fine chemicals of miscellaneous various functions.Dihydrofuran chemical synthesis at present is with butadiene monoxide as raw material system
DHF is taken, then isomerization generates DHF, is isolated DHF by rectifying, the method
Presence synthesis side reaction is more, and isomerisation conversion is low, and material is easily polymerized, and two kinds of isomers are separated in industrial production needs operation
More, separation product purity is low, and isolation technics difficulty is larger, causes two kinds of isomers prices of dihydrofuran high, and then constrains
Exploitation of the dihydrofuran in fine chemicals.
Dihydrofuran：English name dihydrofuran, dihydrofuran includes two kinds of isomers, Chinese：2,
3- dihydrofuran and DHF, the now characteristic of two kinds of products of summary and the application in fine chemicals industry.
DHF, colourless transparent liquid, English name：2,5-dihydrofuran, No. CAS： 1708-29-
8, molecular formula： C4H6O, molecular weight：70.09, relative density 0.927g/ml, 65 DEG C of boiling point, -24 DEG C of flash-point.With 2,5- dihydros
Furans is initiation material, can synthesize 3- tetrahydrofurfuryl carbinols, and then synthesizes MTI-446, and the process route is succinct, waste water
Little, safety and environmental protection is measured, therefore DHF is an important intermediate for synthesizing MTI-446 agricultural chemicals.
MTI-446 (dinotefuran) is the super nicotinic insecticide of latest generation.Itself and existing nicotinic insecticide
Chemical constitution be far from each other, its tetrahydrofuran base instead of former chloro-pyridine base, chloro-thiazole base, and not contain
Halogen.Meanwhile, also different with nicotine in aspect of performance, insecticidal spectrum is wider, so, current people are referred to as " furan
Mutter nicotine " its toxicity：MTI-446 is fool proof to mammal, and its acute oral LD50 is male rat 2450mg/kg, female
The mg/kg of rat 2275；Male mice 2840mg/kg, female mice 2000mg/kg.LD50 percutaneous to rat acute>2000mg/
Kg (female, hero).Without teratogenesis, carcinogenic and mutagenicity.MTI-446 is also fool proof to aquatile.Ichthyotoxin test shows, furan worm
Amine is to carp nm (48 h)>1000mg/L, to water flea>1000mg/L.Equally, MTI-446 is also very low to birds toxicity, to quail
Acute oral LD50> 1000mg/kg.Jing learns that MTI-446 does not affect honeybee producting honey to honeybee safety to honeybee test.
MTI-446 medicament is developed by Mitsui KCC, is ultra high efficiency insecticide of new generation, with tagging,
Stomach toxicity and root absorbability is strong, quick-acting high, lasting period long 4-8 are all（Theoretical lasting effect 43 days）, it is the features such as insecticidal spectrum is wide and right
Sucking insect has excellent preventive effect, and shows very high insecticidal activity in very low dosage.Compare first and second generation desinsection
Agent, insecticidal spectrum is wider, using more convenient, the resistance risk that one or two generation insecticides can be overcome to bring.Be mainly used in prevent and treat wheat,
Aphid, leafhopper, plant hopper, thrips, aleyrodid and its resistant strain in the various crops such as paddy rice, cotton, vegetables, fruit tree, tobacco leaf, together
When coleoptera, Diptera and Lepidoptera, Diptera, beetle mesh and total wing mesh insect are had efficiently, and to blattaria, termite, housefly
Have efficiently Deng sanitary insect pest.
DHF is a kind of chemical substance, English another name：2,3-DHF, molecular weight：70.09, molecular formula is
C4H6O, boiling point：55.2 DEG C, density 0.927g/ml, for organic synthesis solvent, electronic chemical product, Special Resin, synthetic perfume
Deng being particularly used as the important source material of the pharmaceutical chemicals such as 7- ethyl tryptophols, different support polyacid.
It is Material synthesis 7- ethyl tryptophols by DHF and adjacent ethyl hydrazinobenzene hydrochloride salt, product yield reaches 70%
More than, crude product purity more than 90%, fine work purity can reach 99% after purification, and the technological operation is simple, is current industrialized production
Principal synthetic routes.7- ethyl tryptophols also known as 7- ethyl -3- indoles ethanol；7- ethyl group tryptophols；7- ethyl -3- ethoxy Yin
Diindyl；7- ethyl tryptosols, 7- ethyl tryptophols are synthesized in the middle of the key of non-steroidal anti-inflammatory analgesics Etodolac (etodolac).
Etodolac is NSAIDs, can be with relief from osteoarthritis（Degenerated joint pathology）, rheumatoid arthritis
Sings and symptoms.Pain of alleviation symptom.Rheumatoid arthritis, including the sick distinctive Cranial defect（Corrode）, articular cavity is narrow
It is narrow, osteoarthritis（Degenerative joint disease）And mild to moderate pain.
Etodolac is NSAIDs, with anti-inflammatory, antipyretic and analgesic activity.Its mechanism of action may be by resistance
The activity of abscission ring oxygenase, so as to inhibit prostaglandin（PG synthesis).This product is nonsteroid anti-inflammatory drugs（NSAIDs）.Make
For analgesia and antiphlogistic, its curative effect can be with aspirin, other antalgesics and many prescription NSAIDs phases the most frequently used at present
Than.It optionally suppresses prostaglandin biosynthesis in inflammation part, when giving rat therapeutic dose, to stomach prostaglandin
The suppression of PGE2 is slight and of short duration.This is probably the less mechanism of its gastrointestinal side effect.Rat assist agent arthritis mould
Type shows that this product can reduce the incidence and seriousness of bone and joint damage, and the progress of energy reverse disease.Animal experiment has no
Teratogenesis, has less impact to fertility and reproductive function.But animal pregnancy test shows to suppress the biological conjunction of prostaglandin
Into medicine can cause difficult labour and give a birth postpone.The biosynthetic inhibitor of some prostaglandins may interfere with closing for arterial duct
Close.
Reactor of the prior art adopts tank reactor, and using the solid catalysis process of liquid, the reaction time is long, side reaction
Many, polymerism is serious, and crotonaldehyde growing amount is big, smell weight, and difficulty of governance is big, and reaction yield is low, separates dihydrofuran purity
Relatively low, industrialization difficulty is larger；Purity requirement of the existing dihydrofuran production equipment to raw material Isosorbide-5-Nitrae-butylene glycol simultaneously is high,
Production cost is higher, and product purity is relatively low.
Utility model content
The purpose of this utility model is to provide a kind of dihydrofuran continuous prodution and detached device, chemical reaction with
Rectifying separation coupling together, constitutes continuous prodution flow process, improves production efficiency；Using calandria type fixed bed catalytic reaction
Device, device provided by the utility model is applied to the raw material of Isosorbide-5-Nitrae-butylene glycol content 90 ~ 99%, low to product purity requirement,
Wide accommodation, contributes to reducing production cost.
The utility model solve the technical scheme that adopted of technical problem for：
A kind of dihydrofuran continuous prodution and detached device, it is characterised in that described device includes head tank, overheated
It is device, reactor, preheater, condenser, raw material pump, transfer tank, the first delivery pump, first rectifying column, Second distillation column, the 3rd defeated
Send pump, third distillation column, the 5th delivery pump and the 4th rectifying column；
The superheater is fixed tubular heat exchanger, plus thermal medium is high temperature heat transfer oil, and wherein material walks tube side, leads
Deep fat walks shell side；
The preheater is fixed tubular heat exchanger, and raw material walks shell side, and synthesis gaseous phase materials walk tube side.Using reactor
The gas phase mixture material of generation is preheated to raw material, can react the heat for producing with effectively utilizes, reduces energy consumption, colleague
Heat exchanger refrigerant consumption is saved, and then effectively reduces separation costs.
The reactor is tubular fixed-bed catalytic reactor, inside sets expansion joint, and thermal medium is added in heat exchanging pipe for height
Warm conduction oil, compared with high selectivity.Solid catalyst is imitated in the built-in raising of equipment, and it is contrary that material occurs gas-solid by beds
Should, there is cyclisation and dehydration in butylene glycol, generate the mixture of dihydrofuran isomer and water, and ring-closure reaction is to inhale
Thermal response, heat is provided by heat exchanging pipe high temperature conduction oil.Reactor of the prior art adopts tank reactor, using liquid
Gu catalysis process, the reaction time is long, side reaction is more, and polymerism is serious, and crotonaldehyde growing amount is big, smell weight, and difficulty of governance is big,
Reaction yield is low, and separation dihydrofuran purity is relatively low, and industrialization difficulty is larger.The fixed bed reactors that the utility model is selected are again
Packed bed reactor, bed transfixion, fluid is claimed to be reacted by bed；Solid catalyst is imitated in the built-in raising of reactor,
There is gas-solid phase reaction by beds in material；Calandria type fixed bed reactor is made up of many reaction tube parallel connections.In pipe
Or put catalyst between pipe, thermophore is flowed through between pipe or is heated or cooled in pipe, caliber generally between 25～50mm, pipe number
Can up to up to ten thousand；The advantage of fixed bed reactors is：1. back-mixing is little, and fluid can carry out effective contact with catalyst, work as reaction
With series connection side reaction when can compared with high selectivity.2. catalytic mechanical loss is little.3. simple structure.
The head tank, raw material pump are sequentially connected successively with the shell side charging aperture of preheater, the shell side discharging opening of preheater,
Successively order is connected the charging aperture of superheater and reactor bottom, the discharging opening of reactor head and the tube side charging aperture of preheater
It is connected, the middle part charging aperture of the tube side discharging opening of preheater, condenser, transfer tank, the first delivery pump and first rectifying column is successively
Order is connected, and the top discharge mouth of the first rectifying column is connected with the middle part charging aperture of Second distillation column, second rectifying
The bottom discharge mouth of tower, the 3rd delivery pump are connected with third distillation column middle part charging aperture successively order, the top of third distillation column
Discharging opening is connected with the middle part charging aperture of the 4th rectifying column, and the bottom discharge mouth of third distillation column is connected with the 5th delivery pump.
Preferably, described device also includes the second delivery pump, the bottom discharge mouth of first rectifying column, the second delivery pump and
Successively order is connected the tube side charging aperture of superheater, and first rectifying column bottom of towe collects unreacted Isosorbide-5-Nitrae-butylene glycol, and passes through
Second delivery pump is back in superheater.
Preferably, the described device also wraps the 4th delivery pump, the bottom discharge mouth of the 4th rectifying column, the 4th delivery pump
Successively order is connected with the sidepiece charging aperture of head tank, and bottom of towe produces aqueous butylene glycol, and no longer individually carries out regeneration process,
It is directly entered in synthesis procedure head tank by delivery pump.
Preferably, the first rectifying column is serialization rectifying column, Second distillation column is divided-wall distillation column, and the 3rd is smart
It is serialization rectifying column to evaporate tower, and the 4th rectifying column is extracting rectifying tower, and tower bottom reboiler is heated using pump forced circulation, tower
Top condenser is cooled down using recirculated water and chilled water twin-stage.Second distillation column is divided-wall distillation column, can simultaneously separate furan
Mutter, three kinds of cuts of DHF and crude product DHF, due to reaction less, and 2, the 3- dihydro furan that generates furans amount
Mutter fewer than DHF content, therefore two conventional tower clastotypes are substituted using divided-wall distillation column, reduce production work
Sequence, with larger economic benefit.
Preferably, first rectifying column number of theoretical plate sum is 16 ~ 25 pieces, wherein, theoretical number of plates of rectifying section is 10 ~
15 pieces, profit reduction and reserving section number of theoretical plate is 6 ~ 10 pieces.
Preferably, the Second distillation column next door rectifying column pattern, Second distillation column theoretical plate sum is 60 ~ 70 pieces,
Wherein, 15 ~ 20 pieces of theoretical number of plates of rectifying section, profit reduction and reserving section number of theoretical plate is 20 ~ 26 pieces, 35 ~ 40 pieces of partition wall section number of theoretical plate.
Preferably, third distillation column number of theoretical plate sum is 30 ~ 40 pieces, wherein, theoretical number of plates of rectifying section is 20 ~
25 pieces, profit reduction and reserving section number of theoretical plate is 10 ~ 15 pieces.
Preferably, the 4th rectifying column number of theoretical plate sum is 45 ~ 55 pieces, wherein, rectifying clean-up stage number of theoretical plate
For ~ 5 pieces, extraction section number of theoretical plate is 25 ~ 30 pieces, 15 ~ 20 pieces of stripping section number of theoretical plate.
The beneficial effects of the utility model are：
1st, device provided by the utility model constitutes continuous prodution by chemical reaction together with rectifying separation coupling
Flow process, improves production efficiency, conversion rate of products and high income, and gained DHF product purity is 96 ~ 99.9%, water
Divide≤0.05%；Gained DHF product purity >=99%, moisture≤0.05%.
2nd, Second distillation column is divided-wall distillation column, can simultaneously separate furans, DHF and crude product 2,5- bis-
Three kinds of cuts of hydrogen furans, it is less due to reacting generation furans amount, and DHF is fewer than DHF content, therefore adopt
Two conventional tower clastotypes are substituted with divided-wall distillation column, production process is reduced, with larger economic benefit.
3rd, the 4th rectifying column adopts extractive distillation column, the anhydrous DHF of overhead extraction, bottom of towe to produce aqueous butylene
Glycol, without the need for carrying out regeneration process to it, is pumped directly into operation synthesis material tank, recycles, and reduces wastewater treatment operation.
4th, dihydrofuran continuous prodution provided by the utility model and detached method, it is adaptable to Isosorbide-5-Nitrae-butylene glycol
The raw material of content 90 ~ 99%, to product purity low, wide accommodation is required, contributes to reducing production cost.
5th, using device provided by the utility model, gained waste water COD is significantly reduced, and can directly carry out biochemical treatment,
Prevent technique from endangering, improve efficiency of energy utilization.
Description of the drawings
Fig. 1 is structural representation of the present utility model.
In figure, 1, head tank, 2, superheater, 3, reactor, 4, preheater, 5, condenser, 6, raw material pump, 7, transfer tank,
8th, the first delivery pump, the 9, second delivery pump, 10, first rectifying column, 11, Second distillation column, 12, third distillation column, the 14, the 4th is defeated
Send pump, the 15, the 5th delivery pump, the 16, the 4th rectifying column.
Specific embodiment
In order that the technical solution of the utility model and advantage become more apparent, it is new to this practicality with reference to embodiments
Type is further elaborated.It should be appreciated that specific embodiment described herein is only to explain the utility model, not
For limiting the utility model.
Embodiment 1
A kind of dihydrofuran continuous prodution and detached device, including head tank 1, superheater 2, reactor 3, preheater
4th, condenser 5, raw material pump 6, transfer tank 7, the first delivery pump 8, the second delivery pump 9, first rectifying column 10, Second distillation column 11,
3rd delivery pump 12, third distillation column 13, the 4th delivery pump 14, the 5th delivery pump 15 and the 4th rectifying column 16；
The superheater 2 is fixed tubular heat exchanger, plus thermal medium is high temperature heat transfer oil, and wherein material walks tube side,
Conduction oil walks shell side；
The preheater 4 is fixed tubular heat exchanger, and raw material walks shell side, and synthesis gaseous phase materials walk tube side；
The reactor 3 is tubular fixed-bed catalytic reactor, inside sets expansion joint, and thermal medium is added in heat exchanging pipe for height
Warm conduction oil；
The head tank 1, raw material pump 6 are sequentially connected successively with the downside charging aperture of preheater 4, and the shell side of preheater 4 goes out
Material mouth, superheater 2 are sequentially connected successively with the charging aperture of the bottom of reactor 3, discharging opening and the preheater 4 at the top of reactor 3
Tube side charging aperture is connected, the tube side discharging opening of preheater 4, condenser 5, transfer tank 7, the first delivery pump 8 and first rectifying column 10
Middle part charging aperture successively order be connected；The top discharge mouth of the first rectifying column 10 feeds with the middle part of Second distillation column 11
Mouth is connected, and the bottom discharge mouth of first rectifying column 10, the second delivery pump 9 are sequentially connected successively with the tube side charging aperture of superheater 2；
The middle part charging aperture of the bottom discharge mouth, the 3rd delivery pump 12 and third distillation column 13 of the Second distillation column 11 order phase successively
Even, the top discharge mouth of third distillation column 13 is connected with the middle part charging aperture of the 4th rectifying column 16, the bottom of third distillation column 13
Discharging opening is connected with the 5th delivery pump 15；The sidepiece of the bottom discharge mouth, the 4th delivery pump 14 and head tank 1 of the 4th rectifying column 16
Successively order is connected charging aperture；
The first rectifying column 10 be serialization rectifying column, Second distillation column 11 be divided-wall distillation column, third distillation column
13 is serialization rectifying column, and the 4th rectifying column 16 is extracting rectifying tower, and tower bottom reboiler is heated using pump forced circulation, tower
Top condenser is cooled down using recirculated water and chilled water twin-stage；
The number of theoretical plate of first rectifying column 10 sum is 16 ~ 25 pieces, wherein, theoretical number of plates of rectifying section is 10 ~ 15 pieces, retains a percentage of the total profits for the enterprise's own use section
Number of theoretical plate is 6 ~ 10 pieces；Second distillation column 11 is next door rectifying column pattern, and Second distillation column theoretical plate sum is 60 ~ 70 pieces,
Wherein, 15 ~ 20 pieces of theoretical number of plates of rectifying section, profit reduction and reserving section number of theoretical plate is 20 ~ 26 pieces, 35 ~ 40 pieces of partition wall section number of theoretical plate；The
The number of theoretical plate of three rectifying column 13 sum is 30 ~ 40 pieces, wherein, theoretical number of plates of rectifying section is 20 ~ 25 pieces, and profit reduction and reserving section number of theoretical plate is
10 ~ 15 pieces；The number of theoretical plate of 4th rectifying column 16 sum is 45 ~ 55 pieces, wherein, rectifying clean-up stage number of theoretical plate is ~ 5 pieces,
Extraction section number of theoretical plate is 25 ~ 30 pieces, 15 ~ 20 pieces of stripping section number of theoretical plate.
Operation principle of the present utility model is：
(1) mixed material containing Isosorbide-5-Nitrae-butylene glycol is added in head tank 1, then Jing raw materials pump 6 is pumped in preheater 4
80-120 DEG C is preheated to, the raw material after preheating enters back into and 140-300 DEG C is superheated in superheater 2, and gained gaseous phase materials enter anti-
In answering device 3, under catalyst action, in 150-300 DEG C, gas phase dihydro furan is obtained Jing after gas and solid phase catalyzing normal pressure or Depressor response
The Synthesis liquid muttered with water, the reaction velocity is 0.5-2.5/h, and the vacuum of the Depressor response is 0 ~ 0.08MPa.
(2) gained vapor- phase synthesis liquid is discharged from the discharging opening at the top of reactor 3, sequentially enters preheater 4 and condenser 5,
After being cooled to 20-30 DEG C, the middle part of first rectifying column 10 is delivered to into raw material transfer tank 7, then the first delivery pumps of Jing 8, in first
The bottom of towe of rectifying column 10 collects unreacted 1,4- butylene glycols（Content is 85 ~ 95%）, and be back to by the second delivery pump 9
In hot device 2, the overhead collection of first rectifying column 10 mixing dihydrofuran cut, and it is delivered to the middle part of Second distillation column 11；First is smart
Evaporating tower operating condition is：0 ~ 0.08MPa of vacuum, 5 ~ 75 DEG C of tower top temperature, 150 ~ 240 DEG C of column bottom temperature, reflux ratio R=0.5 ~
3；
(3) the overhead extraction furans of Second distillation column 11, purity is 50 ~ 99.5%, rectifying column middle part extraction 2,3- dihydro furans
Mutter finished product, purity 99.5%, bottom of towe extraction DHF heavy constituent（Purity 50 ~ 75%）, the cut is by the 3rd delivery pump
12 pump into the middle part of third distillation column 13；Second distillation column operating condition is：Atmospheric operation, reflux ratio R=30 ~ 60, tower top temperature 32
~50℃；0 ~ 54.5 DEG C of temperature in tower；66 ~ 75 DEG C of column bottom temperature；
(4) bottom of towe of third distillation column 13 is produced at rectifying waste liquid and the follow-up environmental protection of Jing by the serialization of the 5th delivery pump 15
Reason, side line gas phase extracted waste water Jing biochemical treatments（Containing crotonaldehyde 0.01 ~ 0.3%）, overhead extraction DHF is total to water
Boiling thing（Purity 96 ~ 99.5%, aqueous 0 ~ 5%）, the azeotropic mixture is into the middle part of the 4th rectifying column 16；Third distillation column operating condition
For：Atmospheric operation, reflux ratio R=1.0 ~ 1.5,65 DEG C of tower top temperature, 102 ~ 170 DEG C of column bottom temperature, side take-off temperature 102 ~
105℃；
(5) the 4th rectifying columns 16 adopt extractant Isosorbide-5-Nitrae-butylene glycol extracting rectifying, solvent ratio（Extractant：Inlet amount）
For 0.5 ~ 1；1, overhead extraction finished product DHF（Purity 96 ~ 99.5%, aqueous≤0.05%）, the aqueous Isosorbide-5-Nitrae of bottom of towe extraction-
Butylene glycol（Moisture 0 ~ 5%）.4th rectifying column operating condition is：Atmospheric operation, reflux ratio R=1.0 ~ 1.5, solvent is than 0.5 ~ 1；
1,66 DEG C of tower top temperature, 150 ~ 170 DEG C of column bottom temperature.
Embodiment described above is a kind of preferably scheme of the present utility model, not makees any to the utility model
Pro forma restriction, also has other variants and remodeling on the premise of without departing from the technical scheme described in claim.
Claims (8)
1. a kind of dihydrofuran continuous prodution and detached device, it is characterised in that described device includes head tank（1）, mistake
Hot device（2）, reactor（3）, preheater（4）, condenser（5）, raw material pump（6）, transfer tank（7）, the first delivery pump（8）, first
Rectifying column（10）, Second distillation column（11）, the 3rd delivery pump（12）, third distillation column（13）, the 5th delivery pump（15）With the 4th
Rectifying column（16）；
The superheater（2）Oily for high temperature heat transfer for fixed tubular heat exchanger, plus thermal medium, wherein material walks tube side, leads
Deep fat walks shell side；
The preheater（4）To fix tubular heat exchanger, raw material walks shell side, and synthesis gaseous phase materials walk tube side；
The reactor（3）For tubular fixed-bed catalytic reactor, expansion joint is inside set, add thermal medium to be high temperature in heat exchanging pipe
Conduction oil；
The head tank（1）, raw material pump（6）And preheater（4）Shell side charging aperture successively order be connected, preheater（4）Shell
Journey discharging opening, superheater（2）And reactor（3）Successively order is connected the charging aperture of bottom, reactor（3）Top discharging opening with
Preheater（4）Tube side charging aperture be connected, preheater（4）Tube side discharging opening, condenser（5）, transfer tank（7）, first conveying
Pump（8）And first rectifying column（10）Middle part charging aperture successively order be connected, the first rectifying column（10）Top discharge mouth
With Second distillation column（11）Middle part charging aperture be connected, the Second distillation column（11）Bottom discharge mouth, the 3rd delivery pump
（12）And third distillation column（13）Middle part charging aperture successively order be connected, third distillation column（13）Top discharge mouth and the 4th
Rectifying column（16）Middle part charging aperture be connected, third distillation column（13）Bottom discharge mouth and the 5th delivery pump（15）It is connected.
2. dihydrofuran continuous prodution as claimed in claim 1 and detached device, it is characterised in that described device also includes
Second delivery pump（9）, first rectifying column（10）Bottom discharge mouth, the second delivery pump（9）And superheater（2）Tube side charging aperture
Successively order is connected.
3. dihydrofuran continuous prodution as claimed in claim 1 or 2 and detached device, it is characterised in that described device is also
Wrap the 4th delivery pump（14）, the 4th rectifying column（16）Bottom discharge mouth, the 4th delivery pump（14）And head tank（1）Sidepiece enter
Successively order is connected material mouth.
4. dihydrofuran continuous prodution as claimed in claim 1 and detached device, it is characterised in that the first rectifying column
（10）For serialization rectifying column, Second distillation column（11）For divided-wall distillation column, third distillation column（13）For serialization rectifying column,
4th rectifying column（16）For extracting rectifying tower, using the heating of pump forced circulation, overhead condenser is adopted tower bottom reboiler
Recirculated water and chilled water twin-stage are cooled down.
5. dihydrofuran continuous prodution and detached device as described in claim 1 or 4, it is characterised in that described first is smart
Evaporate tower（10）Number of theoretical plate sum is 16 ~ 25 pieces, wherein, theoretical number of plates of rectifying section is 10 ~ 15 pieces, profit reduction and reserving section number of theoretical plate is 6 ~
10 pieces.
6. dihydrofuran continuous prodution and detached device as described in claim 1 or 4, it is characterised in that described second is smart
Evaporate tower（11）For next door rectifying column pattern, Second distillation column theoretical plate sum is 60 ~ 70 pieces, wherein, theoretical number of plates of rectifying section 15 ~
20 pieces, profit reduction and reserving section number of theoretical plate is 20 ~ 26 pieces, 35 ~ 40 pieces of partition wall section number of theoretical plate.
7. dihydrofuran continuous prodution and detached device as described in claim 1 or 4, it is characterised in that the described 3rd is smart
Evaporate tower（13）Number of theoretical plate sum is 30 ~ 40 pieces, wherein, theoretical number of plates of rectifying section is 20 ~ 25 pieces, and profit reduction and reserving section number of theoretical plate is 10
~ 15 pieces.
8. dihydrofuran continuous prodution and detached device as described in claim 1 or 4, it is characterised in that the described 4th is smart
Evaporate tower（16）Number of theoretical plate sum is 45 ~ 55 pieces, wherein, rectifying clean-up stage number of theoretical plate is 3 ~ 5 pieces, and extraction section number of theoretical plate is
25 ~ 30 pieces, 15 ~ 20 pieces of stripping section number of theoretical plate.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201621095508.5U CN206089513U (en) | 2016-09-30 | 2016-09-30 | Device of dihydrofuran serialization production and separation |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201621095508.5U CN206089513U (en) | 2016-09-30 | 2016-09-30 | Device of dihydrofuran serialization production and separation |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN206089513U true CN206089513U (en) | 2017-04-12 |
Family
ID=58482095
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201621095508.5U Withdrawn - After Issue CN206089513U (en) | 2016-09-30 | 2016-09-30 | Device of dihydrofuran serialization production and separation |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN206089513U (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106432143A (en) * | 2016-09-30 | 2017-02-22 | 浙江捷达科技有限公司 | Continuous dihydrofuran production and separation device |
-
2016
- 2016-09-30 CN CN201621095508.5U patent/CN206089513U/en not_active Withdrawn - After Issue
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106432143A (en) * | 2016-09-30 | 2017-02-22 | 浙江捷达科技有限公司 | Continuous dihydrofuran production and separation device |
| CN106432143B (en) * | 2016-09-30 | 2019-02-19 | 浙江捷达科技有限公司 | A kind of dihydrofuran continuous production and isolated device |
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