CN110003054A - A kind of water scavenging system and water-eliminating method of phosgenation production isocyanate plant - Google Patents
A kind of water scavenging system and water-eliminating method of phosgenation production isocyanate plant Download PDFInfo
- Publication number
- CN110003054A CN110003054A CN201910237026.0A CN201910237026A CN110003054A CN 110003054 A CN110003054 A CN 110003054A CN 201910237026 A CN201910237026 A CN 201910237026A CN 110003054 A CN110003054 A CN 110003054A
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- Prior art keywords
- tower
- solvent
- reactor
- phosgene
- phosgenation
- Prior art date
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- Granted
Links
- 238000000034 method Methods 0.000 title claims abstract description 46
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 title claims abstract description 42
- 239000012948 isocyanate Substances 0.000 title claims abstract description 34
- 150000002513 isocyanates Chemical class 0.000 title claims abstract description 33
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 23
- 230000002000 scavenging effect Effects 0.000 title claims abstract description 21
- 239000002904 solvent Substances 0.000 claims abstract description 333
- 238000007670 refining Methods 0.000 claims description 119
- 238000010521 absorption reaction Methods 0.000 claims description 70
- 239000007791 liquid phase Substances 0.000 claims description 70
- MVPPADPHJFYWMZ-UHFFFAOYSA-N chlorobenzene Chemical compound ClC1=CC=CC=C1 MVPPADPHJFYWMZ-UHFFFAOYSA-N 0.000 claims description 45
- 239000007789 gas Substances 0.000 claims description 44
- YGYAWVDWMABLBF-UHFFFAOYSA-N Phosgene Chemical group ClC(Cl)=O YGYAWVDWMABLBF-UHFFFAOYSA-N 0.000 claims description 38
- 239000012071 phase Substances 0.000 claims description 25
- 238000009833 condensation Methods 0.000 claims description 19
- 230000005494 condensation Effects 0.000 claims description 19
- 239000007792 gaseous phase Substances 0.000 claims description 14
- YXFVVABEGXRONW-UHFFFAOYSA-N Toluene Chemical compound CC1=CC=CC=C1 YXFVVABEGXRONW-UHFFFAOYSA-N 0.000 claims description 12
- 239000007788 liquid Substances 0.000 claims description 10
- 239000003795 chemical substances by application Substances 0.000 claims description 9
- 238000007599 discharging Methods 0.000 claims description 9
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 claims description 6
- 238000000605 extraction Methods 0.000 claims description 4
- 238000000926 separation method Methods 0.000 claims description 4
- CTQNGGLPUBDAKN-UHFFFAOYSA-N O-Xylene Chemical compound CC1=CC=CC=C1C CTQNGGLPUBDAKN-UHFFFAOYSA-N 0.000 claims description 3
- VNGOYPQMJFJDLV-UHFFFAOYSA-N dimethyl benzene-1,3-dicarboxylate Chemical compound COC(=O)C1=CC=CC(C(=O)OC)=C1 VNGOYPQMJFJDLV-UHFFFAOYSA-N 0.000 claims description 2
- 238000009434 installation Methods 0.000 claims description 2
- 238000004090 dissolution Methods 0.000 abstract description 2
- 238000005265 energy consumption Methods 0.000 abstract description 2
- 230000002378 acidificating effect Effects 0.000 abstract 1
- 238000005260 corrosion Methods 0.000 abstract 1
- 230000007797 corrosion Effects 0.000 abstract 1
- 238000005516 engineering process Methods 0.000 abstract 1
- 238000007086 side reaction Methods 0.000 abstract 1
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 10
- 238000006243 chemical reaction Methods 0.000 description 5
- 229910052757 nitrogen Inorganic materials 0.000 description 5
- 238000010926 purge Methods 0.000 description 5
- 238000003860 storage Methods 0.000 description 5
- 230000035807 sensation Effects 0.000 description 4
- 150000001412 amines Chemical class 0.000 description 3
- MVPPADPHJFYWMZ-IDEBNGHGSA-N chlorobenzene Chemical group Cl[13C]1=[13CH][13CH]=[13CH][13CH]=[13CH]1 MVPPADPHJFYWMZ-IDEBNGHGSA-N 0.000 description 3
- 230000000052 comparative effect Effects 0.000 description 3
- 238000001035 drying Methods 0.000 description 3
- RRAMGCGOFNQTLD-UHFFFAOYSA-N hexamethylene diisocyanate Chemical compound O=C=NCCCCCCN=C=O RRAMGCGOFNQTLD-UHFFFAOYSA-N 0.000 description 3
- 239000000047 product Substances 0.000 description 3
- 239000005057 Hexamethylene diisocyanate Substances 0.000 description 2
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 229910000041 hydrogen chloride Inorganic materials 0.000 description 2
- IXCSERBJSXMMFS-UHFFFAOYSA-N hydrogen chloride Substances Cl.Cl IXCSERBJSXMMFS-UHFFFAOYSA-N 0.000 description 2
- 238000012423 maintenance Methods 0.000 description 2
- UPMLOUAZCHDJJD-UHFFFAOYSA-N 4,4'-Diphenylmethane Diisocyanate Chemical compound C1=CC(N=C=O)=CC=C1CC1=CC=C(N=C=O)C=C1 UPMLOUAZCHDJJD-UHFFFAOYSA-N 0.000 description 1
- NIXOWILDQLNWCW-UHFFFAOYSA-M Acrylate Chemical compound [O-]C(=O)C=C NIXOWILDQLNWCW-UHFFFAOYSA-M 0.000 description 1
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 1
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 description 1
- 206010054949 Metaplasia Diseases 0.000 description 1
- XSQUKJJJFZCRTK-UHFFFAOYSA-N Urea Chemical compound NC(N)=O XSQUKJJJFZCRTK-UHFFFAOYSA-N 0.000 description 1
- GCNLQHANGFOQKY-UHFFFAOYSA-N [C+4].[O-2].[O-2].[Ti+4] Chemical compound [C+4].[O-2].[O-2].[Ti+4] GCNLQHANGFOQKY-UHFFFAOYSA-N 0.000 description 1
- 239000000853 adhesive Substances 0.000 description 1
- 230000001070 adhesive effect Effects 0.000 description 1
- XLJMAIOERFSOGZ-UHFFFAOYSA-N anhydrous cyanic acid Natural products OC#N XLJMAIOERFSOGZ-UHFFFAOYSA-N 0.000 description 1
- 239000003125 aqueous solvent Substances 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 239000004202 carbamide Substances 0.000 description 1
- 229910002091 carbon monoxide Inorganic materials 0.000 description 1
- 238000001311 chemical methods and process Methods 0.000 description 1
- 239000000460 chlorine Substances 0.000 description 1
- 229910052801 chlorine Inorganic materials 0.000 description 1
- -1 cyanic acid ester Chemical class 0.000 description 1
- 230000007423 decrease Effects 0.000 description 1
- 238000004821 distillation Methods 0.000 description 1
- 238000004880 explosion Methods 0.000 description 1
- 239000000945 filler Substances 0.000 description 1
- 238000002309 gasification Methods 0.000 description 1
- 239000004519 grease Substances 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 230000035987 intoxication Effects 0.000 description 1
- 231100000566 intoxication Toxicity 0.000 description 1
- NIMLQBUJDJZYEJ-UHFFFAOYSA-N isophorone diisocyanate Chemical compound CC1(C)CC(N=C=O)CC(C)(CN=C=O)C1 NIMLQBUJDJZYEJ-UHFFFAOYSA-N 0.000 description 1
- 230000015689 metaplastic ossification Effects 0.000 description 1
- 150000003141 primary amines Chemical class 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 238000012797 qualification Methods 0.000 description 1
- 238000004904 shortening Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 238000011144 upstream manufacturing Methods 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
- 239000008096 xylene Substances 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C263/00—Preparation of derivatives of isocyanic acid
- C07C263/10—Preparation of derivatives of isocyanic acid by reaction of amines with carbonyl halides, e.g. with phosgene
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C263/00—Preparation of derivatives of isocyanic acid
- C07C263/18—Separation; Purification; Stabilisation; Use of additives
- C07C263/20—Separation; Purification
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C2601/00—Systems containing only non-condensed rings
- C07C2601/12—Systems containing only non-condensed rings with a six-membered ring
- C07C2601/14—The ring being saturated
Abstract
The present invention discloses the water scavenging system and water-eliminating method of a kind of phosgenation production isocyanate plant.It is driven initial stage by producing isocyanate plant in phosgenation, is operated in water scavenging system using solvent, in a solvent by moisture remaining in system dissolution, recycled solvent, moisture is enriched with outlet.The technology can effectively reduce moisture in system, reduces moisture after feeding intake and there is corrosion of the acidic environment formed to equipment, reduces moisture and side reaction occurs for isocyanate products.It can effectively reduce the energy consumption in removal process simultaneously, shorten the solvent operating water removal time.The water scavenging system and water-eliminating method process are simple and convenient to operate, are energy-efficient.
Description
Technical field
The invention belongs to chemical process field, it is related to a kind of process units water scavenging system and water-eliminating method, is specifically related to
A kind of water scavenging system and water-eliminating method of phosgenation production isocyanate plant.
Technical background
Isocyanates is widely used in the industries such as household electrical appliances, automobile, building, shoes industry, furniture, adhesive.Existing industry metaplasia
Producing isocyanate products mainly uses primary amine light phosgenation to produce: so that chlorine and reaction of carbon monoxide is generated phosgene first, secondly
It reacts phosgene in a solvent with organic amine and generates isocyanates and hydrogen chloride, again by isocyanates and hydrogen chloride from solvent
It separates.
Reactor, storage tank, the tower etc. of phosgenation production isocyanate plant work at high temperature under high pressure, exist because of equipment
Corrode and induces the risks such as intoxication accident and fire explosion, and the presence of moisture is that equipment corrodes most important original in system
Cause.
Due to containing unsaturated bond in isocyanate structural, there is high activity, reacted with water and generate amine and titanium dioxide
Carbon, amine, which is further reacted with isocyanates, generates urea, and isocyanate products loss is caused to decline with quality.
Phosgenation produces isocyanate plant during normal production, is not easily introduced moisture.Moisture mainly after a stoppage, if
Standby introducing system during opening maintenance etc..It is full in order to guarantee that, when phosgene enters device, device moisture can reach zone of reasonableness
Sufficient production requirement, phosgenation, which produces isocyanate plant, must take moisture content in method reduction system at driving initial stage.
A kind of acrylate chemical product de-watering apparatus is disclosed in patent CN104311454A, which passes through liter
Magnificent tower, condenser and with gun barrel removing by-product water is used in combination, the patent is not to grease layered effect and draining side
Method is described, and package unit System drainage is not described, and the tower that distils uses packed tower, needs to pump toluene solution
It is transmitted back to distillation tower to wash filler, waste of energy.
It is not yet found that technical literature discloses isocyanate plant water-eliminating method, therefore, produced for current phosgenation different
The water removal of cyanic acid ester apparatus there are the problem of, need to develop a kind of efficient phosgenation production isocyanate plant water removal techniques.
Summary of the invention
Object of the present invention is to overcome the shortage of prior art, a kind of water scavenging system of phosgenation production isocyanate plant is provided
And water-eliminating method.It drives initial stage in phosgenation production isocyanate plant, is operated in water scavenging system using solvent, it will be in system
In a solvent, recycled solvent, moisture is enriched with outlet for remaining moisture dissolution.Both the moisture in effective removing system meets
Production requirement, but it is energy-efficient, to strive for more production times for device, improve unit service factor.
In order to reach the goals above, the present invention adopts the following technical scheme:
A kind of water scavenging system of phosgenation production isocyanate plant, comprising: absorption tower 1, phosgenation reactor 2, phosgene
Change reactor tower reactor reboiler 10, de- phosgene tower 3, de- phosgene tower reactor reboiler 11, solvent removal tower 4, solvent removal tower reactor again
Boil device 12, solvent removal tower top cooler 15, solvent removal tower top knockout drum 8, thick solvent surge tank 6, solvent refining tower
5, solvent refining tower reactor reboiler 13, de- phosgene tower and solvent refining tower top cooler 14, de- phosgene tower and solvent refining tower top
Knockout drum 9, solvent tank 7；
1 top of absorption tower be arranged absorption tower solvent feed pipe 16,1 tower reactor bottom of absorption tower by liquid phase pipeline 20 with slightly it is molten
Agent surge tank 6 connects, and thick solvent surge tank 6 is connect with 5 top of solvent refining tower, and the top of solvent refining tower 5 passes through gas phase pipe
Line is connect with de- phosgene tower and solvent refining tower top cooler 14,
5 tower reactor bottom of solvent refining tower is connect by liquid phase pipeline with solvent tank 7；
Phosgenation reactor solvent feed pipe 17 is arranged in 2 top of phosgenation reactor, and the top of phosgenation reactor 2 passes through
Vapor delivery line is connect with 1 tower reactor of absorption tower；
2 tower reactor bottom of phosgenation reactor takes off the top of phosgene tower 3 by connecting in the middle part of liquid phase pipeline and de- phosgene tower 3
It is connect by vapor delivery line with de- phosgene tower and solvent refining tower top cooler 14, de- 3 tower reactor bottom of phosgene tower passes through liquid-phase tube
Line is connect with 4 top of solvent removal tower, and the top of solvent removal tower 4 is connected by vapor delivery line and solvent removal tower top cooler 15
It connects, solvent removal tower top cooler 15 is connect with solvent removal tower top knockout drum 8, solvent removal tower top knockout drum 8
Bottom is connect by liquid phase pipeline 21 with solvent tank 7, passes through vapor delivery line and suction at the top of solvent removal tower top knockout drum 8
Receive the connection of 1 tower reactor of tower；
De- phosgene tower and solvent refining tower top cooler 14 and de- phosgene tower and solvent refining tower top knockout drum 9 connect
It connects, de- phosgene tower and 9 bottom of solvent refining tower top knockout drum are connect by liquid phase pipeline with 5 top of solvent refining tower, are taken off
It is connect with 1 tower reactor of absorption tower at the top of phosgene tower and solvent refining tower top knockout drum 9 by vapor delivery line, de- phosgene tower and molten
Agent refines tower overhead gas liquid knockout drum 9 and drainpipe 19 is arranged；
Tail gas discharging pipe 18 is arranged in the top on absorption tower 1.
The tower reactor point of phosgenation reactor 2 of the present invention, de- phosgene tower 3, solvent removal tower 4 and solvent refining tower 5
Not An Zhuan reboiler, for will corresponding column bottom liquid phase heating after be recycled back to tower bottom.Wherein, light is installed in 2 bottom of phosgenation reactor
Gasification reactor tower reactor reboiler 10.The bottom of de- phosgene tower 3 is installed by de- phosgene tower reactor reboiler 11.4 bottom of solvent removal tower
Solvent removal tower reactor reboiler 12 is installed.5 bottom of solvent refining tower is installed by solvent refining tower reactor reboiler 13.
As a preferred option, solvent tank 7 of the present invention by pipeline and absorption tower solvent feed pipe 16 and/or
Phosgenation reactor solvent feed pipe 17 connects, optional in solvent tank 7 and absorption tower solvent feed pipe 16 and/or phosgenation
Cooler is set on the pipeline that reactor solvent feed pipe 17 connects.
A method of it is removed water, is included the following steps using system of the present invention；
Solvent is added into absorption tower 1 from absorption tower solvent feed pipe 16, it is slow to go to thick solvent from 1 tower reactor bottom of absorption tower
Rush tank 6；The solvent of thick solvent surge tank 6 enters 5 top of solvent refining tower, and the top gas phase of solvent refining tower 5 is by de- phosgene
Tower and solvent refining tower top cooler 14 enter de- phosgene tower and solvent refining tower top knockout drum 9 after condensing；Solvent refining
5 tower reactor bottom of tower extraction liquid phase enters solvent tank 7；
Solvent, the top of phosgenation reactor 2 are added from phosgenation reactor solvent feed pipe 17 to phosgenation reactor 2
Gas phase enters 1 tower reactor of absorption tower, and the tower reactor bottom liquid phases of phosgenation reactor 2 enter de- 3 middle part of phosgene tower；
De- 3 top gaseous phase of phosgene tower enters de- phosgene tower after de- phosgene tower and solvent refining tower top cooler 14 condense
With solvent refining tower top knockout drum 9；
Gas phase and liquid phase are obtained in de- phosgene tower and solvent refining tower top knockout drum 9, gained gas phase enters absorption tower 1
Tower reactor, gained liquid phase enter 5 top of solvent refining tower, water is enriched in de- phosgene tower and solvent refining tower top knockout drum 9,
Layering, is discharged by drainpipe 19；
De- 3 tower reactor bottom of phosgene tower extraction liquid phase enters 4 top of solvent removal tower, the top gas phase warp of solvent removal tower 4
It crosses after solvent removal tower top cooler 15 condenses and obtains gas phase and liquid phase into solvent removal tower top knockout drum 8, brought about the desired sensation
Mutually enter 1 tower reactor of absorption tower, gained liquid phase enters solvent tank 7；
Tail gas is discharged from tail gas discharging pipe 18.
Solvent in solvent tank 7 of the present invention can be used as solvent be supplied to absorption tower solvent feed pipe 16 and/or
Phosgenation reactor solvent feed pipe 17.
In method of the present invention, the solvent be selected from dimethyl isophthalate, benzene,toluene,xylene, chlorobenzene and
One of o-dichlorohenzene is a variety of, preferably chlorobenzene and o-dichlorohenzene, more preferably chlorobenzene.
In method of the present invention, moisture content is 0-0.400wt%, preferably 0-0.0300wt% in the solvent.
In method of the present invention, the temperature of the solvent is 10-60 DEG C, preferably 20-50 degree, more preferably 30-40
℃。
In method of the present invention, the gauge pressure on the absorption tower 1 is 100-150KPa, preferably 100-130KPa, more excellent
Select 100-110KPa.
In method of the present invention, the gauge pressure of the phosgenation reactor 2 is 100-150KPa, preferably 100-
130KPa, more preferable 100-110KPa；The bottom temperature of the phosgenation reactor 2 be 130-170 DEG C, preferably 140-160 DEG C,
More preferably 150-160 DEG C.
In method of the present invention, the gauge pressure of the de- phosgene tower 3 is 100-150KPa, preferably 100-130KPa, more
It is preferred that 100-110KPa；The bottom temperature of the de- phosgene tower 3 be 130-170 DEG C, preferably 140-160 DEG C, more preferable 150-160
℃。
In method of the present invention, the gauge pressure of the solvent removal tower 4 is 20-80KPa, preferably 30-70KPa, more excellent
Select 40-60KPa；The bottom temperature of the solvent removal tower 4 be 100-150 DEG C, preferably 110-140 DEG C, more preferable 120-130
℃。
In method of the present invention, the gauge pressure of the solvent refining tower 5 is 100-150KPa, preferably 100-130KPa,
More preferable 100-110KPa；The bottom temperature of the solvent refining tower 5 be 130-180 DEG C, preferably 140-170 DEG C, more preferably
150-160℃。
Condensation liquidus temperature in method of the present invention, in the de- phosgene tower and solvent refining tower top cooler 14
It is 50-100 DEG C, preferably 60-90 DEG C, more preferable 70-80 DEG C.
In method of the present invention, the condensation liquidus temperature in the solvent removal tower top cooler 15 is 50-100
DEG C, preferably 60-90 DEG C, more preferable 70-80 DEG C.
Absorption tower of the present invention, phosgenation reactor, de- phosgene tower, solvent removal tower, solvent refining tower can be
Equipment well known in the art.
Preferably, absorption tower of the present invention is packed tower；Phosgenation reactor of the present invention is plate column；The present invention
The de- phosgene tower is plate column；Solvent removal tower of the present invention is plate column；Solvent refining tower of the present invention is board-like
Tower.
Water scavenging system and water-eliminating method of the invention is suitable for the reaction unit that light phosgenation prepares isocyanates, institute
Stating isocyanates includes but is not limited to toluene di-isocyanate(TDI) (TDI), isophorone diisocyanate (IPDI), diphenyl methane
Diisocyanate (MDI), dicyclohexyl methyl hydride diisocyanate (HMDI), hexamethylene diisocyanate (HDI) etc..
In the technique of phosgenation production isocyanates, absorption tower 1 is used to absorb the light in the exhaust of phosgenation reactor 2
Gas；Phosgenation reactor 2 is for carrying out phosgenation reaction；De- phosgene tower 3 is in the mixed liquor after removing phosgenation reaction
Phosgene；Solvent removal tower 4 is for the solvent in the mixed liquor after removing phosgenation reaction；Solvent refining tower 5 is miscellaneous for that will contain
The solvent of matter is refined；Surge tank of the thick solvent surge tank 6 for the solvent containing impurity that removing comes out in system；Solvent
Storage tank 7 is used to store the solvent after purification qualification.
Water-eliminating method of the present invention can be used in combination with other water-eliminating methods well known in the art, including but not
It is limited to nitrogen purging.As a preferred scheme, nitrogen purging can be first carried out, then uses water removal of the present invention again
Method further removes water.
Using in water-eliminating method of the present invention treated phosgenation production isocyanate plant, biodiversity content
100ppm can be reached hereinafter, representing moisture content in device with the moisture content in the solvent in thick solvent surge tank 6.
Water scavenging system and method for the invention opens maintenance etc. especially suitable for removing phosgenation production isocyanate plant
The water being introduced into system in the process improves driving efficiency.Solvent operating water removal is quick, efficient in the present invention, especially in solvent
It operates in process route selection, takes and system upstream solvent is delivered to downstream solvent treating column with minimal path, avoid downstream
Aqueous solvent returns to up-stream system, removes water the principle that qualified solvent is sent directly into qualified solvent tank, dramatically simplifies
Process route shortens the solvent duration of runs, improves efficiency.
Detailed description of the invention
Fig. 1 is the schematic diagram of water scavenging system of the present invention；
Fig. 2 is the schematic diagram of the water scavenging system of comparative example 1；
1. absorption tower；2. phosgenation reactor；3. de- phosgene tower；4. solvent removal tower；5. solvent refining tower；6. thick solvent
Surge tank；7 solvent tanks；8. solvent removal tower top knockout drum；9. de- phosgene tower and solvent refining tower top knockout drum；
10. phosgenation reactor tower reactor reboiler；11. de- phosgene tower reactor reboiler；12. solvent removal tower reactor reboiler；13. solvent is smart
Tower reactor reboiler processed；14. de- phosgene tower and solvent refining tower top cooler；15. solvent removal tower top cooler；16. absorption tower
Solvent feed pipe；17. phosgenation reactor solvent feed pipe；18. tail gas discharging pipe；19. drainpipe；20. connecting 1 tower of absorption tower
The liquid phase pipeline in bottom portion and thick solvent surge tank 6；21. connecting the liquid of solvent removal tower top knockout drum 8 and solvent tank 7
Phase pipeline；22. connecting the liquid phase pipeline of absorption tower 1 tower reactor bottom and 2 tower reactor of phosgenation reactor；23. connecting solvent removal tower
Push up the liquid phase pipeline of knockout drum 8 and thick solvent surge tank 6.
Specific embodiment
The following examples will to will be further described to method provided by the present invention, but the present invention is not limited to
Listed embodiment should also include other any well known changes in scope of the presently claimed invention.
In the present invention, it is to be understood that term " on ", "top", "bottom", " in " etc. instructions positional relationship be based on
Positional relationship shown in the drawings, is merely for convenience of description of the present invention and simplification of the description, rather than the dress of indication or suggestion meaning
It sets or element must have specific position, with specific placement configurations and operation, therefore should not be understood as to limit of the invention
System.
Moisture content is measured using karl Fischer moisture teller in solvent.
Embodiment 1
Water scavenging system for phosgenation production isocyanate plant as shown in Figure 1 comprising: absorption tower 1, phosgenation
It is reactor 2, phosgenation reactor tower reactor reboiler 10, de- phosgene tower 3, de- phosgene tower reactor reboiler 11, solvent removal tower 4, molten
Agent removes tower reactor reboiler 12, solvent removal tower top cooler 15, solvent removal tower top knockout drum 8, thick solvent surge tank
6, solvent refining tower 5, solvent refining tower reactor reboiler 13, de- phosgene tower and solvent refining tower top cooler 14, de- phosgene tower and
Solvent refining tower top knockout drum 9, solvent tank 7；
1 top of absorption tower be arranged absorption tower solvent feed pipe 16,1 tower reactor bottom of absorption tower by liquid phase pipeline 20 with slightly it is molten
Agent surge tank 6 connects, and thick solvent surge tank 6 is connect with 5 top of solvent refining tower, and the top of solvent refining tower 5 passes through gas phase pipe
Line is connect with de- phosgene tower and solvent refining tower top cooler 14,
5 tower reactor bottom of solvent refining tower is connect by liquid phase pipeline with solvent tank 7；
Phosgenation reactor solvent feed pipe 17 is arranged in 2 top of phosgenation reactor, and the top of phosgenation reactor 2 passes through
Vapor delivery line is connect with 1 tower reactor of absorption tower；
2 tower reactor bottom of phosgenation reactor takes off the top of phosgene tower 3 by connecting in the middle part of liquid phase pipeline and de- phosgene tower 3
It is connect by vapor delivery line with de- phosgene tower and solvent refining tower top cooler 14, de- 3 tower reactor bottom of phosgene tower passes through liquid-phase tube
Line is connect with 4 top of solvent removal tower, and the top of solvent removal tower 4 is connected by vapor delivery line and solvent removal tower top cooler 15
It connects, solvent removal tower top cooler 15 is connect with solvent removal tower top knockout drum 8, solvent removal tower top knockout drum 8
Bottom is connect by liquid phase pipeline 21 with solvent tank 7, passes through vapor delivery line and suction at the top of solvent removal tower top knockout drum 8
Receive the connection of 1 tower reactor of tower；
De- phosgene tower and solvent refining tower top cooler 14 and de- phosgene tower and solvent refining tower top knockout drum 9 connect
It connects, de- phosgene tower and 9 bottom of solvent refining tower top knockout drum are connect by liquid phase pipeline with 5 top of solvent refining tower, are taken off
It is connect with 1 tower reactor of absorption tower at the top of phosgene tower and solvent refining tower top knockout drum 9 by vapor delivery line, de- phosgene tower and molten
Agent refines tower overhead gas liquid knockout drum 9 and drainpipe 19 is arranged；
Tail gas discharging pipe 18 is arranged in the top on absorption tower 1.
Phosgenation reactor 2, the tower reactor for taking off phosgene tower 3, solvent removal tower 4 and solvent refining tower 5 install reboiler respectively,
For corresponding column bottom liquid phase circulation to be returned tower bottom.Wherein, phosgenation reactor tower reactor reboiler is installed in 2 bottom of phosgenation reactor
10.The bottom of de- phosgene tower 3 is installed by de- phosgene tower reactor reboiler 11.4 bottom of solvent removal tower installation solvent removal tower reactor is boiled again
Device 12.5 bottom of solvent refining tower is installed by solvent refining tower reactor reboiler 13.
Capital equipment capacity parameter is as follows:
Absorption tower 1: size φ 1800mm × 30225mm, tower reactor capacity 9m3；
Phosgenation reactor 2: size φ 5200mm × 38350mm, tower reactor capacity 70m3；
De- phosgene tower 3: size φ 2200mm × 25650mm, tower reactor capacity 10m3；
Solvent removal tower 4: size φ 5200mm × 15350mm, tower reactor capacity 17m3；
Solvent refining tower 5: size φ 3000mm × 26080mm, tower reactor capacity 12m3；
Thick solvent surge tank 6: size φ 2500mm × 5590mm, capacity 24m3；
Solvent tank 7: size φ 3500mm × 8013mm, capacity 70m3。
Embodiment 2
The present embodiment is the water scavenging system using embodiment 1, the dewatering process for phosgenation production isocyanate plant.
Into before solvent, under normal pressure, it is -40 DEG C that system, which purges drying to dew point using nitrogen,.
Solvent is chlorobenzene, and moisture content is 0.0125wt% in chlorobenzene, and solvent-based quality, temperature is 30 DEG C.
Absorption tower 1 is packed tower, and tower top operating pressure is gauge pressure 100KPa.
The tower top operating pressure of phosgenation reactor 2 is gauge pressure 110KPa, and tower reactor operation temperature is 130 DEG C.
De- 3 operating pressure of phosgene tower is gauge pressure 110KPa, and 150 DEG C of tower reactor operation temperature, overhead condensation liquid phase is 70 DEG C.
4 operating pressure of solvent removal tower is gauge pressure 50KPa, and tower reactor operation temperature is 130 DEG C, and overhead condensation liquid phase temperature is
80℃。
5 operating pressure of solvent refining tower is gauge pressure 102KPa, and bottom temperature is 160 DEG C.Overhead condensation liquid phase temperature is 70
℃。
Chlorobenzene, inlet amount about 20m are added into absorption tower 1 from absorption tower solvent feed pipe 163/ h, from 1 tower reactor of absorption tower
Bottom is delivered to thick solvent surge tank 6.
Chlorobenzene, inlet amount about 80m are added from phosgenation reactor solvent feed pipe 17 to phosgenation reactor 23/ h, phosgene
Change 2 top gaseous phase of reactor and enter 1 tower reactor of absorption tower, the tower bottom liquid phase of phosgenation reactor 2 enters de- 3 middle part of phosgene tower.
De- 3 top gaseous phase of phosgene tower enters de- phosgene tower after de- phosgene tower and solvent refining overhead condenser 14 condense
In solvent refining tower top knockout drum 9；De- 3 tower reactor liquid phase of phosgene tower enters 4 top of solvent removal tower.
The top gaseous phase of solvent removal tower 4 enters solvent removal tower overhead gas after the condensation of solvent removal tower top cooler 15
Liquid knockout drum 8 obtains gas phase and liquid phase, and gained gas phase enters 1 tower reactor of absorption tower, and liquid phase enters solvent tank 7.
The solvent of thick solvent surge tank 6 enters 5 top of solvent refining tower, and 5 top gaseous phase of solvent refining tower is by de- phosgene
Tower and solvent refining tower top cooler 14 enter after condensing in de- phosgene tower and solvent refining tower top knockout drum 9；
Gas-liquid separation is carried out in de- phosgene tower and solvent refining tower top knockout drum 9 and obtains gas phase and liquid phase, is brought about the desired sensation
Mutually enter 1 tower reactor of absorption tower；After the operating of solvent refining tower 5 is stablized, take off in phosgene tower and solvent refining tower top knockout drum 9
Liquid phase contained in moisture enrichment, layering, every 2 hours by water of 19 row of drainpipe, every time with 1m3/ h flow row
0.5 hour, intermittently by the water discharge system after layering, to reduce moisture in system.5 tower reactor liquid phase of solvent refining tower is sent to molten
Agent storage tank 7.
Tail gas is discharged from tail gas discharging pipe 18.
It operates under such an approach, the timing since operating when (temperature, pressure) is stablized solvent refining tower 5 monitors thick solvent
When the biodiversity content of chlorobenzene is reduced to 100ppm (thick solvent surge tank chlorobenzene is up to standard) in surge tank 6, the System drainage used time
As shown in table 1.
Embodiment 3
The present embodiment is the water scavenging system using embodiment 1, the dewatering process for phosgenation production isocyanate plant.
Into before solvent, under normal pressure, it is -40 DEG C that system, which purges drying to dew point using nitrogen,.
Solvent is chlorobenzene, and moisture content is 0.0270wt% in chlorobenzene, and solvent-based quality, temperature is 30 DEG C.
Absorption tower 1 is packed tower, and tower top operating pressure is gauge pressure 120KP.
The tower top operating pressure of phosgenation reactor 2 is gauge pressure 130KPa, and tower reactor operation temperature is 150 DEG C
De- 3 operating pressure of phosgene tower is gauge pressure 130KPa, and 165 DEG C of tower reactor operation temperature, overhead condensation liquid phase is 80 DEG C.
4 operating pressure of solvent removal tower is gauge pressure 30KPa, and tower reactor operation temperature is 110 DEG C, and overhead condensation liquid phase temperature is
80℃。
5 operating pressure gauge pressure 130KPa of solvent refining tower, bottom temperature are 170 DEG C, and overhead condensation liquid phase temperature is 80 DEG C.
Chlorobenzene, inlet amount about 20m are added into absorption tower 1 from absorption tower solvent feed pipe 163/ h, from 1 tower reactor of absorption tower
Bottom is delivered to thick solvent surge tank 6.
Chlorobenzene, inlet amount about 80m are added from phosgenation reactor solvent feed pipe 17 to phosgenation reactor 23/ h, phosgene
Change 2 top gaseous phase of reactor and enter 1 tower reactor of absorption tower, the tower bottom liquid phase of phosgenation reactor 2 enters de- 3 middle part of phosgene tower.
De- 3 top gaseous phase of phosgene tower enters de- phosgene tower after de- phosgene tower and solvent refining overhead condenser 14 condense
In solvent refining tower top knockout drum 9；De- 3 tower reactor liquid phase of phosgene tower enters 4 top of solvent removal tower.
The top gaseous phase of solvent removal tower 4 enters solvent removal tower overhead gas after the condensation of solvent removal tower top cooler 15
Liquid knockout drum 8 obtains gas phase and liquid phase, and gained gas phase enters 1 tower reactor of absorption tower, and liquid phase enters solvent tank 7.
The solvent of thick solvent surge tank 6 enters 5 top of solvent refining tower, and 5 top gaseous phase of solvent refining tower is by de- phosgene
Tower and solvent refining tower top cooler 14 enter after condensing in de- phosgene tower and solvent refining tower top knockout drum 9；
Gas-liquid separation is carried out in de- phosgene tower and solvent refining tower top knockout drum 9 and obtains gas phase and liquid phase, is brought about the desired sensation
Mutually enter 1 tower reactor of absorption tower；After the operating of solvent refining tower 5 is stablized, take off in phosgene tower and solvent refining tower top knockout drum 9
Liquid phase contained in moisture enrichment, layering, every 2 hours by water of 19 row of drainpipe, every time with 1m3/ h flow row
0.5 hour, intermittently by the water discharge system after layering, to reduce moisture in system.5 tower reactor liquid phase of solvent refining tower is sent to molten
Agent storage tank 7.
Tail gas is discharged from tail gas discharging pipe 18.
It operates under such an approach, the timing since operating when (temperature, pressure) is stablized solvent refining tower 5 monitors thick solvent
When the biodiversity content of chlorobenzene is reduced to 100ppm (thick solvent surge tank chlorobenzene is up to standard) in surge tank 6, the System drainage used time
As shown in table 1.
Comparative example 1
Using the water scavenging system for phosgenation production isocyanate plant as shown in Figure 2, cancel liquid phase in embodiment 1
The setting of pipeline 20,21 is changed to connect 1 tower reactor bottom of absorption tower and 2 tower reactor of phosgenation reactor, liquid phase using liquid phase pipeline 22
Pipeline 23 connects solvent removal tower top knockout drum 8 and thick solvent surge tank 6.The system is that phosgenation produces isocyanates dress
The normal production system set.Into before solvent, under normal pressure, it is -40 DEG C that system, which purges drying to dew point using nitrogen,.
Solvent is chlorobenzene, and moisture content is 0.0270wt% in chlorobenzene, and solvent-based quality, temperature is 30 DEG C.
Absorption tower 1 is packed tower, and tower top operating pressure is gauge pressure 100KPa.
The tower top operating pressure gauge pressure 110KPa of phosgenation reactor 2, tower reactor operation temperature are 130 DEG C.
De- 3 operating pressure of phosgene tower is gauge pressure 110KPa, and 150 DEG C of tower reactor operation temperature, overhead condensation liquid phase is 70 DEG C.
4 operating pressure gauge pressure 50KPa of solvent removal tower, tower reactor operation temperature are 110 DEG C, and overhead condensation liquid phase temperature is 80
℃。
5 operating pressure gauge pressure 110KPa of solvent refining tower, bottom temperature are 165 DEG C.Overhead condensation liquid phase temperature is 70 DEG C.
Chlorobenzene, inlet amount about 20m are added into absorption tower 1 from absorption tower solvent feed pipe 163/ h, from 1 tower reactor of absorption tower
Bottom is delivered to 2 tower reactor of phosgenation reactor.
Chlorobenzene, inlet amount about 80m are added from phosgenation reactor solvent feed pipe 17 to phosgenation reactor 23/ h, phosgene
Change 2 top gaseous phase of reactor and enter 1 tower reactor of absorption tower, the tower bottom liquid phase of phosgenation reactor 2 enters de- 3 middle part of phosgene tower.
De- 3 top gaseous phase of phosgene tower enters de- phosgene tower after de- phosgene tower and solvent refining overhead condenser 14 condense
In solvent refining tower top knockout drum 9；De- 3 tower reactor liquid phase of phosgene tower enters 4 top of solvent removal tower.
The top gaseous phase of solvent removal tower 4 enters solvent removal tower overhead gas after the condensation of solvent removal tower top cooler 15
Liquid knockout drum 8 obtains gas phase and liquid phase, and gained gas phase enters 1 tower reactor of absorption tower, and liquid phase enters thick solvent surge tank 6.
The solvent of thick solvent surge tank 6 enters 5 top of solvent refining tower, and 5 top gaseous phase of solvent refining tower is by de- phosgene
Tower and solvent refining tower top cooler 14 enter after condensing in de- phosgene tower and solvent refining tower top knockout drum 9；
Gas-liquid separation is carried out in de- phosgene tower and solvent refining tower top knockout drum 9 and obtains gas phase and liquid phase, is brought about the desired sensation
Mutually enter 1 tower reactor of absorption tower；After the operating of solvent refining tower 5 is stablized, take off in phosgene tower and solvent refining tower top knockout drum 9
Liquid phase contained in moisture enrichment, layering, every 2 hours by water of 19 row of drainpipe, every time with 1m3/ h flow row
0.5 hour, intermittently by the water discharge system after layering, to reduce moisture in system.5 tower reactor liquid phase of solvent refining tower is sent to molten
Agent storage tank 7.
Tail gas is discharged from tail gas discharging pipe 18.
It operates under such an approach, the timing since operating when (temperature, pressure) is stablized solvent refining tower 5 monitors thick solvent
When the biodiversity content of chlorobenzene is reduced to 100ppm (thick solvent surge tank chlorobenzene is up to standard) in surge tank 6, the System drainage used time
As shown in table 1.
1 embodiment of table and comparative example result
It drives initial stage as it can be seen from table 1 the method for the present invention can quickly, efficiently reduce phosgenation production isocyanate plant
Moisture in system, greatly shortening device are driven the water removal time at initial stage, and energy consumption is saved.
Claims (10)
1. a kind of water scavenging system of phosgenation production isocyanate plant, comprising: absorption tower (1), phosgenation reactor (2) take off
It is phosgene tower (3), solvent removal tower (4), solvent removal tower top cooler (15), solvent removal tower top knockout drum (8), thick molten
Agent surge tank (6), solvent refining tower (5), de- phosgene tower and solvent refining tower top cooler (14), de- phosgene tower and solvent refining
Tower top knockout drum (9), solvent tank (7)；
Absorption tower (1) top be arranged absorption tower solvent feed pipe (16), absorption tower (1) tower reactor bottom by liquid phase pipeline (20) with
Thick solvent surge tank (6) connection, thick solvent surge tank (6) connect with solvent refining tower (5) top, the top of solvent refining tower (5)
Portion is connect by vapor delivery line with de- phosgene tower and solvent refining tower top cooler (14),
Solvent refining tower (5) tower reactor bottom is connect by liquid phase pipeline with solvent tank (7)；
Phosgenation reactor solvent feed pipe (17) are arranged in phosgenation reactor (2) top, and the top of phosgenation reactor (2) is logical
Vapor delivery line is crossed to connect with absorption tower (1) tower reactor；
Phosgenation reactor (2) tower reactor bottom takes off the top of phosgene tower (3) by connecting in the middle part of liquid phase pipeline and de- phosgene tower (3)
Portion is connect by vapor delivery line with de- phosgene tower and solvent refining tower top cooler (14), and de- phosgene tower (3) tower reactor bottom passes through
Liquid phase pipeline is connect with solvent removal tower (4) top, and the top of solvent removal tower (4) passes through vapor delivery line and solvent removal tower top
Cooler (15) connection, solvent removal tower top cooler (15) are connect with solvent removal tower top knockout drum (8), solvent removal
Tower top knockout drum (8) bottom is connect by liquid phase pipeline (21) with solvent tank (7), solvent removal tower top knockout drum
(8) top is connect by vapor delivery line with absorption tower (1) tower reactor；
De- phosgene tower and solvent refining tower top cooler (14) and de- phosgene tower and solvent refining tower top knockout drum (9) are even
It connects, takes off phosgene tower and solvent refining tower top knockout drum (9) bottom and connected by liquid phase pipeline and solvent refining tower (5) top
It connects, is connect, taken off with absorption tower (1) tower reactor by vapor delivery line at the top of de- phosgene tower and solvent refining tower top knockout drum (9)
Phosgene tower and solvent refining tower top knockout drum (9) setting drainpipe (19)；
Tail gas discharging pipe (18) are arranged in the top on absorption tower (1).
2. water scavenging system according to claim 1, which is characterized in that the solvent tank (7) is by pipeline and absorbs
Tower solvent feed pipe (16) and/or phosgenation reactor solvent feed pipe (17) connection, it is optional in solvent tank (7) and to absorb
Cooler is set on tower solvent feed pipe (16) and/or the pipeline of phosgenation reactor solvent feed pipe (17) connection.
3. system according to claim 1 or 2, which is characterized in that install phosgenation in phosgenation reactor (2) bottom
The bottom of reactor tower reactor reboiler (10), the de- phosgene tower (3) is installed de- phosgene tower reactor reboiler (11), and the solvent is de-
Except solvent removal tower reactor reboiler (12) are installed in tower (4) bottom, solvent refining tower (5) the bottom installation solvent refining tower reactor is again
It boils device (13).
4. a kind of method that water scavenging system according to claim 1-3 is removed water, includes the following steps；
Solvent is added in from absorption tower solvent feed pipe (16) to absorption tower (1), goes to thick solvent from absorption tower (1) tower reactor bottom
Surge tank (6)；The solvent of thick solvent surge tank (6) enters solvent refining tower (5) top, the top gas phase of solvent refining tower (5)
Enter de- phosgene tower and solvent refining tower top gas-liquid separation after de- phosgene tower and solvent refining tower top cooler (14) condensation
Tank (9)；Solvent refining tower (5) tower reactor bottom extraction liquid phase enters solvent tank (7)；
Solvent, the top of phosgenation reactor (2) are added from phosgenation reactor solvent feed pipe (17) to phosgenation reactor (2)
Portion's gas phase enters absorption tower (1) tower reactor, and the tower reactor bottom liquid phases of phosgenation reactor (2) enter in the middle part of de- phosgene tower (3)；
De- phosgene tower (3) top gaseous phase enters de- phosgene tower after de- phosgene tower and solvent refining tower top cooler (14) condensation
With solvent refining tower top knockout drum (9)；
Gas phase and liquid phase are obtained in de- phosgene tower and solvent refining tower top knockout drum (9), gained gas phase enters absorption tower (1)
Tower reactor, gained liquid phase enter solvent refining tower (5) top, and water is in de- phosgene tower and solvent refining tower top knockout drum (9)
Enrichment, layering, are discharged by drainpipe (19)；
De- phosgene tower (3) tower reactor bottom extraction liquid phase enters solvent removal tower (4) top, the top gas phase of solvent removal tower (4)
Enter solvent removal tower top knockout drum (8) after solvent removal tower top cooler (15) condensation and obtain gas phase and liquid phase,
Gained gas phase enters absorption tower (1) tower reactor, and gained liquid phase enters solvent tank (7)；
Tail gas is discharged from tail gas discharging pipe (18).
5. according to the method described in claim 4, it is characterized in that, the solvent in the solvent tank (7) is provided as solvent
To absorption tower solvent feed pipe (16) and/or phosgenation reactor solvent feed pipe (17).
6. method according to claim 4 or 5, which is characterized in that the solvent be selected from dimethyl isophthalate, benzene,
One of toluene, dimethylbenzene, chlorobenzene and o-dichlorohenzene are a variety of, preferably chlorobenzene and o-dichlorohenzene, more preferably chlorobenzene.
7. according to the described in any item methods of claim 4-6, which is characterized in that moisture content is 0- in the solvent
0.400wt%, preferably 0-0.0300wt%.
8. according to the described in any item methods of claim 4-7, which is characterized in that the temperature of the solvent is 10-60 DEG C, preferably
20-50 degree, more preferably 30-40 DEG C.
9. according to the described in any item methods of claim 4-8, which is characterized in that the gauge pressure of the absorption tower (1) is 100-
150KPa, preferably 100-130KPa, more preferable 100-110KPa；
The gauge pressure of the phosgenation reactor (2) is 100-150KPa, preferably 100-130KPa, more preferable 100-110KPa；Institute
The bottom temperature for stating phosgenation reactor (2) is 130-170 DEG C, preferably 140-160 DEG C, more preferable 150-160 DEG C；
The gauge pressure of the de- phosgene tower (3) is 100-150KPa, preferably 100-130KPa, more preferable 100-110KPa；It is described de-
The bottom temperature of phosgene tower (3) is 130-170 DEG C, preferably 140-160 DEG C, more preferable 150-160 DEG C；
The gauge pressure of the solvent removal tower (4) is 20-80KPa, preferably 30-70KPa, more preferable 40-60KPa；The solvent is de-
Except the bottom temperature of tower (4) is 100-150 DEG C, preferably 110-140 DEG C, more preferable 120-130 DEG C；
The gauge pressure of the solvent refining tower (5) is 100-150KPa, preferably 100-130KPa, more preferable 100-110KPa；It is described
The bottom temperature of solvent refining tower (5) is 130-180 DEG C, preferably 140-170 DEG C, more preferable 150-160 DEG C.
10. according to the described in any item methods of claim 4-9, which is characterized in that the de- phosgene tower and solvent refining tower top
Condensation liquidus temperature in cooler (14) is 50-100 DEG C, preferably 60-90 DEG C, more preferable 70-80 DEG C；
Condensation liquidus temperature in the solvent removal tower top cooler (15) is 50-100 DEG C, preferably 60-90 DEG C, more preferably
70-80℃。
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| CN201910237026.0A CN110003054B (en) | 2019-03-27 | Water removal system and water removal method of isocyanate production device by phosgenation |
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| Application Number | Priority Date | Filing Date | Title |
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| CN201910237026.0A CN110003054B (en) | 2019-03-27 | Water removal system and water removal method of isocyanate production device by phosgenation |
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|---|---|---|---|---|
| CN103613515A (en) * | 2013-12-13 | 2014-03-05 | 青岛科技大学 | Method for recycling phosgene during isocyanate production process |
| CN107353231A (en) * | 2017-07-17 | 2017-11-17 | 薛永和 | A kind of method for preparing organic isocyanate |
| CN107652208A (en) * | 2017-08-30 | 2018-02-02 | 万华化学（宁波）有限公司 | The method and system of desolvation in a kind of isocyanate product obtained from phosgenation reaction |
| CN107935889A (en) * | 2017-11-29 | 2018-04-20 | 万华化学集团股份有限公司 | The preparation method and system of a kind of monoisocyanates |
| CN210001801U (en) * | 2019-03-27 | 2020-01-31 | 万华化学集团股份有限公司 | Water removal system of phosgenation isocyanate production device |
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|---|---|---|---|---|
| CN103613515A (en) * | 2013-12-13 | 2014-03-05 | 青岛科技大学 | Method for recycling phosgene during isocyanate production process |
| CN107353231A (en) * | 2017-07-17 | 2017-11-17 | 薛永和 | A kind of method for preparing organic isocyanate |
| CN107652208A (en) * | 2017-08-30 | 2018-02-02 | 万华化学（宁波）有限公司 | The method and system of desolvation in a kind of isocyanate product obtained from phosgenation reaction |
| CN107935889A (en) * | 2017-11-29 | 2018-04-20 | 万华化学集团股份有限公司 | The preparation method and system of a kind of monoisocyanates |
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