CN108285403A - Recycling petroleum ether and chlorhydrin energy saving technique in a kind of ibuprofen sodium salt centrifuge mother liquor - Google Patents
Recycling petroleum ether and chlorhydrin energy saving technique in a kind of ibuprofen sodium salt centrifuge mother liquor Download PDFInfo
- Publication number
- CN108285403A CN108285403A CN201810248324.5A CN201810248324A CN108285403A CN 108285403 A CN108285403 A CN 108285403A CN 201810248324 A CN201810248324 A CN 201810248324A CN 108285403 A CN108285403 A CN 108285403A
- Authority
- CN
- China
- Prior art keywords
- heat exchanger
- petroleum ether
- road
- mother liquor
- sodium salt
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
- RTZKZFJDLAIYFH-UHFFFAOYSA-N Diethyl ether Chemical compound CCOCC RTZKZFJDLAIYFH-UHFFFAOYSA-N 0.000 title claims abstract description 152
- 239000003208 petroleum Substances 0.000 title claims abstract description 52
- 239000012452 mother liquor Substances 0.000 title claims abstract description 44
- SSZWWUDQMAHNAQ-UHFFFAOYSA-N 3-chloropropane-1,2-diol Chemical compound OCC(O)CCl SSZWWUDQMAHNAQ-UHFFFAOYSA-N 0.000 title claims abstract description 38
- 238000000034 method Methods 0.000 title claims abstract description 34
- PTTPUWGBPLLBKW-UHFFFAOYSA-M sodium;2-[4-(2-methylpropyl)phenyl]propanoate Chemical compound [Na+].CC(C)CC1=CC=C(C(C)C([O-])=O)C=C1 PTTPUWGBPLLBKW-UHFFFAOYSA-M 0.000 title claims abstract description 34
- 238000004064 recycling Methods 0.000 title claims abstract description 20
- SZIFAVKTNFCBPC-UHFFFAOYSA-N 2-chloroethanol Chemical compound OCCCl SZIFAVKTNFCBPC-UHFFFAOYSA-N 0.000 claims abstract description 23
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 19
- 238000000605 extraction Methods 0.000 claims abstract description 10
- 238000005265 energy consumption Methods 0.000 claims abstract description 7
- 239000000463 material Substances 0.000 claims abstract description 5
- 230000008676 import Effects 0.000 claims description 13
- 230000006835 compression Effects 0.000 claims description 7
- 238000007906 compression Methods 0.000 claims description 7
- 230000008569 process Effects 0.000 claims description 7
- HUDNNLKINUVYCQ-UHFFFAOYSA-N 2-[4-(2-methylpropyl)phenyl]propanoic acid;hydrate Chemical compound O.CC(C)CC1=CC=C(C(C)C(O)=O)C=C1 HUDNNLKINUVYCQ-UHFFFAOYSA-N 0.000 claims description 5
- 229960001680 ibuprofen Drugs 0.000 claims description 5
- 239000012071 phase Substances 0.000 claims description 5
- 238000005086 pumping Methods 0.000 claims description 4
- 239000012808 vapor phase Substances 0.000 claims description 4
- 239000007791 liquid phase Substances 0.000 claims description 3
- 238000001704 evaporation Methods 0.000 claims description 2
- 230000008020 evaporation Effects 0.000 claims description 2
- 239000004575 stone Substances 0.000 claims description 2
- 230000001476 alcoholic effect Effects 0.000 abstract description 5
- 125000001309 chloro group Chemical group Cl* 0.000 abstract description 5
- 238000004519 manufacturing process Methods 0.000 abstract description 3
- 230000000694 effects Effects 0.000 description 4
- 238000005516 engineering process Methods 0.000 description 4
- HEFNNWSXXWATRW-UHFFFAOYSA-N Ibuprofen Chemical compound CC(C)CC1=CC=C(C(C)C(O)=O)C=C1 HEFNNWSXXWATRW-UHFFFAOYSA-N 0.000 description 3
- 230000003110 anti-inflammatory effect Effects 0.000 description 3
- 238000006243 chemical reaction Methods 0.000 description 2
- 239000007788 liquid Substances 0.000 description 2
- BSYNRYMUTXBXSQ-UHFFFAOYSA-N Aspirin Chemical compound CC(=O)OC1=CC=CC=C1C(O)=O BSYNRYMUTXBXSQ-UHFFFAOYSA-N 0.000 description 1
- 229960001138 acetylsalicylic acid Drugs 0.000 description 1
- 230000036592 analgesia Effects 0.000 description 1
- 230000000202 analgesic effect Effects 0.000 description 1
- 229940035676 analgesics Drugs 0.000 description 1
- 239000000730 antalgic agent Substances 0.000 description 1
- 230000001754 anti-pyretic effect Effects 0.000 description 1
- 239000002221 antipyretic Substances 0.000 description 1
- 238000000998 batch distillation Methods 0.000 description 1
- 238000006555 catalytic reaction Methods 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 239000000460 chlorine Substances 0.000 description 1
- 229910052801 chlorine Inorganic materials 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 239000000470 constituent Substances 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 239000003814 drug Substances 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 239000004744 fabric Substances 0.000 description 1
- 210000001035 gastrointestinal tract Anatomy 0.000 description 1
- 230000002607 hemopoietic effect Effects 0.000 description 1
- 230000007062 hydrolysis Effects 0.000 description 1
- 238000006460 hydrolysis reaction Methods 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- KXUHSQYYJYAXGZ-UHFFFAOYSA-N isobutylbenzene Chemical compound CC(C)CC1=CC=CC=C1 KXUHSQYYJYAXGZ-UHFFFAOYSA-N 0.000 description 1
- 238000002955 isolation Methods 0.000 description 1
- 238000005907 ketalization reaction Methods 0.000 description 1
- 210000003734 kidney Anatomy 0.000 description 1
- 210000004185 liver Anatomy 0.000 description 1
- 239000000041 non-steroidal anti-inflammatory agent Substances 0.000 description 1
- 239000000820 nonprescription drug Substances 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 230000008707 rearrangement Effects 0.000 description 1
- 238000005057 refrigeration Methods 0.000 description 1
- 230000003637 steroidlike Effects 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C7/00—Purification; Separation; Use of additives
- C07C7/005—Processes comprising at least two steps in series
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07B—GENERAL METHODS OF ORGANIC CHEMISTRY; APPARATUS THEREFOR
- C07B63/00—Purification; Separation; Stabilisation; Use of additives
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
- C07C29/74—Separation; Purification; Use of additives, e.g. for stabilisation
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
- C07C29/74—Separation; Purification; Use of additives, e.g. for stabilisation
- C07C29/76—Separation; Purification; Use of additives, e.g. for stabilisation by physical treatment
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
- C07C29/74—Separation; Purification; Use of additives, e.g. for stabilisation
- C07C29/76—Separation; Purification; Use of additives, e.g. for stabilisation by physical treatment
- C07C29/80—Separation; Purification; Use of additives, e.g. for stabilisation by physical treatment by distillation
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C7/00—Purification; Separation; Use of additives
- C07C7/04—Purification; Separation; Use of additives by distillation
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C9/00—Aliphatic saturated hydrocarbons
- C07C9/14—Aliphatic saturated hydrocarbons with five to fifteen carbon atoms
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
Abstract
The present invention relates to petroleum ether and chlorhydrin energy saving technique are recycled in a kind of ibuprofen sodium salt centrifuge mother liquor, ibuprofen sodium salt centrifuge mother liquor containing petroleum ether, chloro alcohol and water enters rectifying column D after being exchanged heat by the steam of heat exchanger H1 and the outlets evaporator E, overhead vapours is compressed into high steam through compressor P1 and exchanges heat through heat exchanger H2 with rectifying column D bottom parts material, tower base stream flows back into after heat exchanger H2 heat exchange in tower so that the ibuprofen sodium salt centrifuge mother liquor in tower constantly carries out heat and mass transfer with the steam risen in tower.Using two heat exchangers and a compressor, the mass fraction of chlorhydrin in the petroleum ether of recycling is not only realized below 0.3%, base of evaporator extraction chloro alcoholic solution petrochina ether content in 300ppm hereinafter, and greatly reduce energy consumption, reduce production cost.
Description
【Technical field】
Its this technology belongs to the isolation and purification field of pharmaceutical industry, and in particular in a kind of ibuprofen sodium salt centrifuge mother liquor
Recycle petroleum ether and chlorhydrin energy saving technique.
【Background technology】
Brufen is a kind of non-steroidal anti-inflammatory analgesics object, is to produce anti-inflammatory, antipyretic and analgesia class synthetic drug basis original
Material, anti-inflammatory analgesic, refrigeration function are 16~32 times stronger than aspirin.Compared with general analgesics anti-inflammatory, effect is strong and secondary
Act on it is small, to liver, kidney and hemopoietic system non-evident effect, especially to the Small side effects of gastrointestinal tract.The whole world is become most
One of non-prescription drugs salable.Currently, most domestic enterprise uses 1,2- position rotaring rearrangement method techniques when producing brufen,
I.e. using isobutylbenzene as raw material, the main lifes such as Fu Ke is acylated, catalysis is ketalization, catalytically rearranging, hydrolysis occur with 2- chlorine propionyl priority
Production process finally obtains brufen product.The technique in catalytically rearranging process, generate largely containing petroleum ether, chlorhydrin and
The ibuprofen sodium salt centrifuge mother liquor of water, traditional treatment process recycle mother liquor petrochina ether using an alembic, and mother liquor is in batches
Secondary charging, coil pipe built in alembic, is heated by steam.This technique has the following disadvantages：Technique is batch fractionating, processing
Amount is smaller, and processing capacity is poor, and energy consumption is higher, and the content of the chlorhydrin of overhead product petrochina ether is higher.
The present invention is recycled for batch distillation technique to be existed in petroleum ether and chlorhydrin in ibuprofen sodium salt centrifuge mother liquor
The problem of, an economically viable process route is developed, to improve the treating capacity of ibuprofen sodium salt centrifuge mother liquor, reduces oil
The content of chlorhydrin and chlorhydrin petrochina ether influences follow-up work on a small quantity petroleum ether and chlorhydrin is separately recovered, and removes in ether
The moisture of skill reaction.While realizing comprehensive utilization of resources, using energy integrated technology reduce energy consumption, realize energy saving and
Environmental protection.
Patent CN 201110203356.1 proposes a kind of stripping process and dress removing organic impurities in ibuprofen sodium salt
It sets, it, will in the chloro alcoholic solution of bottom of tower extraction when using stripping process processing though this technique achieves preferable removal effect
A large amount of moisture can be contained, the subsequent technological reaction of chlorhydrin is had an impact.
【Invention content】
The present invention overcomes the deficiencies in the prior art, it is proposed that in a kind of ibuprofen sodium salt centrifuge mother liquor recycling petroleum ether and
Chlorhydrin energy saving technique, while realizing that ibuprofen sodium salt centrifuge mother liquor petrochina ether and chlorhydrin recycle, using energy quantity set
Energy-saving and emission-reduction are realized at technology.
The technical scheme is that：Recycling petroleum ether and the energy saving work of chlorhydrin in a kind of ibuprofen sodium salt centrifuge mother liquor
Skill, which is characterized in that the process unit is as follows：Rectifying column D, heat exchanger H1, heat exchanger H2, compressor P, return tank R, split-phase
Device S, evaporator E；Pump P2；Material import and export is connect by pipeline and evaporator E outlet streams with heat exchanger H1；Heat exchanger H1
Outlet streams are connect with rectifying column D by the road；Rectifying column D overhead vapor phases outlet streams are connected by pipeline and compressor P1 imports
It connects, rectifying column D bottom of tower liquid phase exit streams are connect with heat exchanger H2 and evaporator E entrances respectively by pipeline, pump P2 and heat exchange
Device H2 is connected；The logistics of heat exchanger H2 associated outlets is connect with rectifying column D bottom of tower imports by the road；Compressor P outlet streams are through pipe
Road is connect with heat exchanger H2 imports；Heat exchanger H2 outlet streams are connect with return tank R imports by the road；Return tank R outlet streams
It is connect respectively with rectifying column D tower tops import and phase-splitter S imports by the road；
This method comprises the following steps：
(1) containing petroleum ether, chloro alcohol and water ibuprofen sodium salt centrifuge mother liquor by pipeline 1 after heat exchanger H1 heat exchange simultaneously
2 enter rectifying column D by the road, deliver into and change through pumping, pumping P2 and pipeline 11 by pipeline 10 in rectifying column D bottom of tower fraction of stream
Hot device H2 exchanges heat with the overhead high pressure steam of compressor P1 compressions, and the outlet streams after heat exchange 12 flow back to rectifying by the road
In tower D, heat and mass transfer are carried out with cold logistics in tower；
(2) outlet streams of rectifying column D overhead vapor phases 3 carry out both vapor compression into compressor P1 by the road, compressed
Steam 4 enters heat exchanger H2 by the road, and the outlet streams after heat exchanger H2 heat exchange 5 enter return tank R, return tank R by the road
Fraction of stream 7 is back to rectifying column D by the road；The logistics of return tank R another part 6 carries out split-phase into phase-splitter S by the road,
The tops phase-splitter S 9 extraction petroleum ether by the road, in the lower parts phase-splitter S 8 recovered water by the road；
(3) in the bottoms of tower rectifying column D another part logistics 13 entrance evaporator E evaporations by the road, evaporator E upper outlet objects
It flows through pipeline 15 and enters heat exchanger H1 heat exchange, 16 petroleum ether is produced by the road in the outlets heat exchanger H1, in the lower parts evaporator E through pipe
Road 14 produces chlorhydrin.
Recycling petroleum ether and chlorhydrin energy saving technique in a kind of ibuprofen sodium salt centrifuge mother liquor, it is characterised in that：Use this
Technique makes rectifying column D tower tops steam in petroleum ether chloro alcohol content 0.3% hereinafter, in the bottoms evaporator E extraction chlorhydrin
Oil ether content is in 300ppm hereinafter, the recycling of petroleum ether and chlorhydrin can be realized effectively；
Recycling petroleum ether and chlorhydrin energy saving technique in a kind of ibuprofen sodium salt centrifuge mother liquor, it is characterised in that：Containing oil
Ether, chloro alcohol and water the cold logistics of ibuprofen sodium salt centrifuge mother liquor after the heat exchanger H1 heat exchange, containing petroleum ether, chloro alcohol and water
Ibuprofen sodium salt centrifuge mother liquor temperature is increased to 60-80 DEG C by 10 DEG C~15 DEG C, and part petroleum ether is converted into steam, realizes logistics
Preheating；
Recycling petroleum ether and chlorhydrin energy saving technique in a kind of ibuprofen sodium salt centrifuge mother liquor, it is characterised in that：Rectifying column D
Overhead vapours exchanges heat with rectifying column D tower base streams through heat exchanger H2 after compressor P1 compressions, without using condenser and again
Boil device；
Recycling petroleum ether and chlorhydrin energy saving technique in a kind of ibuprofen sodium salt centrifuge mother liquor, it is characterised in that：Save energy
Consumption is 10-15%.
Recycling petroleum ether and chlorhydrin energy saving technique specifically describe such as in a kind of ibuprofen sodium salt centrifuge mother liquor in the present invention
Under：
After the present invention will contain petroleum ether, chlorhydrin and water ibuprofen sodium salt centrifuge mother liquor by a heat exchanger H1 heat exchange
Temperature is increased to 60-80 DEG C by 10 DEG C~15 DEG C, is sent into tower from the middle and upper parts rectifying column D, and partial material is passed through in the bottoms rectifying column D
The steam that heat exchanger H2 is compressed with tower top through compressor P1 exchanges heat, and logistics is flowed back into through heat exchanger H2 in tower, the cloth in tower
Ibuprofen sodium salt centrifuge mother liquor constantly carries out heat and mass transfer with the steam risen in tower.Most petroleum ether and water can not
It is disconnected to be enriched in vapour phase, rise to tower top extraction petroleum ether and water after heat exchanger H1 and phase-splitter S layerings；Heavy constituent in tower
Chlorhydrin can be constantly enriched with drops to bottom of tower in the liquid phase.The chlorhydrin of bottom of tower extraction enters evaporator E, residual in evaporator E
It deposits petroleum ether to be evaporated, by producing after heat exchanger H1 heat exchange at the top of evaporator E, the chloro alcoholic solution of concentration is by the bottoms evaporator E
Portion produces.
The present invention has the advantages that compared with the prior art：：
(1) present invention uses continuous rectificating technique, is effectively reduced chlorhydrin and bottom of tower in overhead petroleum ether
The content of distillate chlorhydrin petrochina ether, chloro alcohol content is down to 0.3% hereinafter, bottom of tower distillates in the petroleum ether that tower top steams
The content of object chlorhydrin petrochina ether is down to 300ppm or less.
(2) present invention only uses two heat exchangers and a compressor, without condenser and reboiler, without using water vapour with
Recirculated water reduces production cost while saving energy expenditure.
【Description of the drawings】
Accompanying drawing 1 is the structural representation of the present invention
In figure, D is rectifying column；H1, H2 are heat exchanger；P1 is compressor；P1 is pump；R is return tank；S is phase-splitter；E
For evaporator；P2 is pump；Digital 1-16 is pipeline.
【Specific implementation mode】
It is further illustrated below in conjunction with attached drawing 1, not limits range according to the present invention
As shown in the picture, the present invention is first by ibuprofen sodium salt centrifuge mother liquor by in heat exchanger H1 and rectifying column D towers
Enter in rectifying column D after the steam heat-exchanging to certain temperature risen, rectifying column D bottom of tower fraction of stream is through heat exchanger H2 and compressor P1
Enter return tank R after the overhead vapours heat exchange of compression.Extraction enters phase-splitter S, petroleum ether from the bottoms return tank R for petroleum ether and water
It is produced from the tops phase-splitter S, water is produced from the bottoms phase-splitter S.Containing for the bottoms of tower rectifying column D another part logistics extraction is a small amount of remaining
The chloro alcoholic solution of petroleum ether enters evaporator E, and remaining petroleum ether steams in evaporator E through heat exchanger in chloro alcoholic solution
It is produced after H1 condensations, the bottoms evaporator E produce the chlorhydrin of high-purity.
It is the specific implementation example of the present invention below：
Embodiment 1：The inlet amount of ibuprofen sodium salt centrifuge mother liquor be 800kmol/h, oil ether content be 0.65 (mole
Score), chloro alcohol content is 0.32 (molar fraction), and water content is 0.03 (molar fraction), by heat exchanger H1 heat exchange stepmothers
Liquid temperature is increased to 70 DEG C from 12 DEG C.Chloro alcohol content is 0.28% in the petroleum ether of recycling, stone in scraper evaporator discharge liquor
Oily ether content is 268ppm, saves energy consumption about 12%.
Embodiment 2：The inlet amount of ibuprofen sodium salt centrifuge mother liquor be 500kmol/h, oil ether content be 0.70 (mole
Score), chloro alcohol content is 0.28 (molar fraction), and water content is 0.02 (mass fraction), by heat exchanger H1 heat exchange stepmothers
Liquid temperature is increased to 68 DEG C from 10 DEG C.Chloro alcohol content is 0.3% in the petroleum ether of recycling, and evaporator discharge liquor petrochina ether contains
Amount is 300ppm, saves energy consumption about 10%.
Embodiment 3：The inlet amount of ibuprofen sodium salt centrifuge mother liquor is 1000kmol/h, and oil ether content (rubs for 0.73
That score), chloro alcohol content is 0.16 (molar fraction), and water content is 0.01 (molar fraction), after heat exchanger H1 heat exchange
Mother liquor temperature is increased to 75 DEG C from 14 DEG C.Chloro alcohol content is 0.27% in the petroleum ether of recycling, evaporator discharge liquor petrochina
Ether content is 250ppm.
Embodiment 4：The inlet amount of ibuprofen sodium salt centrifuge mother liquor is 1200kmol/h, and oil ether content (rubs for 0.76
That score), chloro alcohol content is 0.20 (molar fraction), and water content is 0.02 (molar fraction), after heat exchanger H1 heat exchange
Mother liquor temperature is increased to 78 DEG C from 15 DEG C.Chloro alcohol content is 0.26% in the petroleum ether of recycling, evaporator discharge liquor petrochina
Ether content is 288ppm.
Embodiment 5：The inlet amount of ibuprofen sodium salt centrifuge mother liquor is 1500kmol/h, and oil ether content (rubs for 0.72
That score), chloro alcohol content is 0.26 (molar fraction), and water content is 0.02 (molar fraction), after heat exchanger H1 heat exchange
Mother liquor temperature is increased to 80 DEG C from 15 DEG C.Chloro alcohol content is 0.29% in the petroleum ether of recycling, evaporator discharge liquor petrochina
Ether content is 275ppm.
Embodiment 6：The inlet amount of ibuprofen sodium salt centrifuge mother liquor is 1800kmol/h, and oil ether content (rubs for 0.67
That score), chloro alcohol content is 0.30 (molar fraction), and water content is 0.03 (molar fraction), after heat exchanger H1 heat exchange
Mother liquor temperature is increased to 74 DEG C from 12 DEG C.Chloro alcohol content is 0.29% in the petroleum ether of recycling, evaporator discharge liquor petrochina
Ether content is 283ppm.
Claims (5)
1. recycling petroleum ether and chlorhydrin energy saving technique in a kind of ibuprofen sodium salt centrifuge mother liquor, which is characterized in that containing petroleum ether,
The ibuprofen sodium salt centrifuge mother liquor of chloro alcohol and water；
The process unit is as follows：Rectifying column D, heat exchanger H1, heat exchanger H2, compressor P, return tank R, phase-splitter S, evaporator
E；Pump P2；Material import and export is connect by pipeline and evaporator E outlet streams with heat exchanger H1；Heat exchanger H1 outlet streams pass through
Pipeline is connect with rectifying column D；Rectifying column D overhead vapor phases outlet streams are connect by pipeline with compressor P1 imports, rectifying column D towers
Bottom liquid phase exit stream is connect with heat exchanger H2 and evaporator E entrances respectively by pipeline, and pump P2 is connected with heat exchanger H2；Heat exchange
The logistics of device H2 associated outlets is connect with rectifying column D bottom of tower imports by the road；Compressor P outlet streams by the road with heat exchanger H2 into
Mouth connection；Heat exchanger H2 outlet streams are connect with return tank R imports by the road；Return tank R outlet streams by the road respectively with essence
Tower D tower tops import is evaporated to connect with phase-splitter S imports；
This method comprises the following steps：
(1) containing petroleum ether, chloro alcohol and water ibuprofen sodium salt centrifuge mother liquor by pipeline 1 after heat exchanger H1 heat exchange and through pipe
Road 2 enters rectifying column D, and heat exchanger is delivered into through pumping, pumping P2 and pipeline 11 by pipeline 10 in rectifying column D bottom of tower fraction of stream
H2 exchanges heat with the overhead high pressure steam of compressor P1 compressions, and the outlet streams after heat exchange 12 flow back to rectifying column D by the road
It is interior, carry out heat and mass transfer with cold logistics in tower；
(2) outlet streams of rectifying column D overhead vapor phases 3 carry out both vapor compression, compressed steam into compressor P1 by the road
4 enter heat exchanger H2 by the road, and the outlet streams after heat exchanger H2 heat exchange 5 enter return tank R, return tank R-portion by the road
Logistics 7 is back to rectifying column D by the road；The logistics of return tank R another part 6 carries out split-phase into phase-splitter S by the road, in split-phase
The tops device S 9 extraction petroleum ether by the road, in the lower parts phase-splitter S 8 recovered water by the road.
(3) in the bottoms of tower rectifying column D another part logistics 13 entrance evaporator E evaporations by the road, evaporator E upper outlet logistics warp
Pipeline 15 enters heat exchanger H1 heat exchange, in the outlets heat exchanger H1 16 extraction petroleum ether by the road, in the lower parts evaporator E by the road 14
Produce chlorhydrin.
2. petroleum ether and chlorhydrin energy saving technique are recycled in a kind of ibuprofen sodium salt centrifuge mother liquor according to claim 1,
It is characterized in that：Use the technique that rectifying column D tower tops is made to steam in petroleum ether chloro alcohol content 0.3% hereinafter, evaporator E
Bottom produces chlorhydrin petrochina ether content in 300ppm hereinafter, the recycling of petroleum ether and chlorhydrin can be realized effectively.
3. petroleum ether and chlorhydrin energy saving technique are recycled in a kind of ibuprofen sodium salt centrifuge mother liquor according to claim 1,
It is characterized in that：Containing petroleum ether, chloro alcohol and water the cold logistics of ibuprofen sodium salt centrifuge mother liquor after heat exchanger H1 heat exchange, contain stone
Oily ether, chloro alcohol and water ibuprofen sodium salt centrifuge mother liquor temperature be increased to 60-80 DEG C by 10 DEG C~15 DEG C, part petroleum ether turns
Steam is turned to, realizes the preheating of logistics.
4. petroleum ether and chlorhydrin energy saving technique are recycled in a kind of ibuprofen sodium salt centrifuge mother liquor according to claim 1,
It is characterized in that：Rectifying column D overhead vapours is changed with rectifying column D tower base streams through heat exchanger H2 after compressor P1 compressions
Heat does not use condenser and reboiler.
5. recycling petroleum ether and chlorhydrin section in a kind of ibuprofen sodium salt centrifuge mother liquor according to claim 1,2,3 and 4
Energy technique, it is characterised in that：Saving energy consumption is 10-15%.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201810248324.5A CN108285403A (en) | 2018-03-24 | 2018-03-24 | Recycling petroleum ether and chlorhydrin energy saving technique in a kind of ibuprofen sodium salt centrifuge mother liquor |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201810248324.5A CN108285403A (en) | 2018-03-24 | 2018-03-24 | Recycling petroleum ether and chlorhydrin energy saving technique in a kind of ibuprofen sodium salt centrifuge mother liquor |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN108285403A true CN108285403A (en) | 2018-07-17 |
Family
ID=62833618
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201810248324.5A Pending CN108285403A (en) | 2018-03-24 | 2018-03-24 | Recycling petroleum ether and chlorhydrin energy saving technique in a kind of ibuprofen sodium salt centrifuge mother liquor |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN108285403A (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111807949A (en) * | 2020-07-23 | 2020-10-23 | 青岛科技大学 | Method for recovering ibuprofen sodium salt from ibuprofen sodium salt mother liquor |
| CN116574531A (en) * | 2023-07-13 | 2023-08-11 | 大庆亿鑫化工股份有限公司 | Furnace type device and production process for producing petroleum ether |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1082022A (en) * | 1992-08-14 | 1994-02-16 | 山东新华制药厂 | Molecular transposition prepares the technology of Ibuprofen BP/EP under the catalysis |
| RU2013130880A (en) * | 2013-07-05 | 2015-01-10 | Закрытое акционерное общество "ЭКОС-1" | METHOD FOR PRODUCING PETROLEUM ETHERS-EXTRAGENTS FOR VEGETABLE AND ESSENTIAL OILS |
| CN104844420A (en) * | 2015-01-21 | 2015-08-19 | 青岛科技大学 | Continuous treatment process and device of neopentyl glycol condensed washing mother liquor |
| CN104926609A (en) * | 2015-04-13 | 2015-09-23 | 青岛科技大学 | Method for processing neopentyl glycol mother liquor in ibuprofen synthesis process, and process flow thereof |
| CN107488094A (en) * | 2017-07-18 | 2017-12-19 | 青岛三瑞节能环保技术有限公司 | A kind of ibuprofen sodium salt centrifuge mother liquor petrochina ether recovery process and device |
-
2018
- 2018-03-24 CN CN201810248324.5A patent/CN108285403A/en active Pending
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1082022A (en) * | 1992-08-14 | 1994-02-16 | 山东新华制药厂 | Molecular transposition prepares the technology of Ibuprofen BP/EP under the catalysis |
| RU2013130880A (en) * | 2013-07-05 | 2015-01-10 | Закрытое акционерное общество "ЭКОС-1" | METHOD FOR PRODUCING PETROLEUM ETHERS-EXTRAGENTS FOR VEGETABLE AND ESSENTIAL OILS |
| CN104844420A (en) * | 2015-01-21 | 2015-08-19 | 青岛科技大学 | Continuous treatment process and device of neopentyl glycol condensed washing mother liquor |
| CN104926609A (en) * | 2015-04-13 | 2015-09-23 | 青岛科技大学 | Method for processing neopentyl glycol mother liquor in ibuprofen synthesis process, and process flow thereof |
| CN107488094A (en) * | 2017-07-18 | 2017-12-19 | 青岛三瑞节能环保技术有限公司 | A kind of ibuprofen sodium salt centrifuge mother liquor petrochina ether recovery process and device |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111807949A (en) * | 2020-07-23 | 2020-10-23 | 青岛科技大学 | Method for recovering ibuprofen sodium salt from ibuprofen sodium salt mother liquor |
| CN111807949B (en) * | 2020-07-23 | 2022-02-11 | 青岛科技大学 | Method for recovering ibuprofen sodium salt from ibuprofen sodium salt mother liquor |
| CN116574531A (en) * | 2023-07-13 | 2023-08-11 | 大庆亿鑫化工股份有限公司 | Furnace type device and production process for producing petroleum ether |
| CN116574531B (en) * | 2023-07-13 | 2023-10-27 | 大庆亿鑫化工股份有限公司 | Furnace type device and production process for producing petroleum ether |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN100378051C (en) | Rectifying tech. and equipment of high purity methanol | |
| CN205730426U (en) | A kind of rectifying column | |
| CN104513159A (en) | Butyl acetate energy saving production method | |
| CN108546243A (en) | A kind of lithium battery production double tower NMP recycling purification systems and its recycling method of purification | |
| CN106745421A (en) | A kind of multiple Intermediate Heat Exchanger rectification method treatment low concentration DMF waste water systems of band | |
| CN110256202A (en) | A kind of refining crude methanol process of four towers quadruple effect | |
| CN108285403A (en) | Recycling petroleum ether and chlorhydrin energy saving technique in a kind of ibuprofen sodium salt centrifuge mother liquor | |
| CN107721820A (en) | A kind of method for being thermally integrated three tower variable-pressure rectification separation of tertiary azeotropic mixtures completely | |
| CN107473947A (en) | A kind of method that three tower is thermally integrated separation of extractive distillation acetone isopropanol water | |
| CN107551586B (en) | Device for producing methanol by utilizing bulkhead tower to combine multiple-effect rectification | |
| CN103724192B (en) | A kind of method of energy-saving purified acetic acid ester | |
| CN107011172B (en) | A kind of method and device that vinyl acetate is refined using partition tower | |
| CN103706136B (en) | For the double rectification column separation method of purification of methyl tertiary butyl ether(MTBE) in statins building-up process waste liquid-tetrahydrofuran recycling | |
| CN106748883B (en) | A method of being thermally integrated three tower variable-pressure rectification separating acetonitriles-Methanol-benzene ternary azeotrope | |
| CN106045832B (en) | The method of thermal coupling transformation batch fractionating acetone-normal heptane | |
| CN105566030A (en) | Method for separating BTX | |
| CN105732319B (en) | A kind of method for being thermally integrated transformation batch fractionating separation methanol-acetonitrile azeotropic mixture | |
| CN105964007A (en) | Device and process for separating n-butyl alcohol and isobutanol mixture | |
| CN110483249A (en) | A kind of six tower quadruple effect rectificating method of single column steam drive type methanol of not by-product fusel oil | |
| CN104447829A (en) | Energy-saving separation method and device of ultrapure triethylene glycol methyl ether borate | |
| CN206081667U (en) | MVR distillation plant | |
| CN205832659U (en) | Ethylene glycol distills multistage energy recovery system | |
| CN208995418U (en) | A kind of acetic synthesis separation and recovery of catalyst device | |
| CN107488094A (en) | A kind of ibuprofen sodium salt centrifuge mother liquor petrochina ether recovery process and device | |
| CN104628608B (en) | A kind of tower negative pressure continuous noble gas air stripping blows naphthalene method and device thereof |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| RJ01 | Rejection of invention patent application after publication | ||
| RJ01 | Rejection of invention patent application after publication |
Application publication date: 20180717 |