CN101623615A - Sleeve distributed gas phase phosgenation reactor and method for synthesizing isocyanate - Google Patents
Sleeve distributed gas phase phosgenation reactor and method for synthesizing isocyanate Download PDFInfo
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- CN101623615A CN101623615A CN200910070112A CN200910070112A CN101623615A CN 101623615 A CN101623615 A CN 101623615A CN 200910070112 A CN200910070112 A CN 200910070112A CN 200910070112 A CN200910070112 A CN 200910070112A CN 101623615 A CN101623615 A CN 101623615A
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Abstract
The invention relates to a sleeve distributed gas phase phosgenation reactor and a method for synthesizing isocyanate. The reactor is composed of a multi-layer sleeve distributor and a tubular reactor body, at least four layers of paralleled sleeves are arranged on the distributor in a coaxial manner, the abreast lower ends thereof are connected with the tubular reactor body, the upper ends thereof are stranded fluid feeding channel composed of non-equant round tubes with different heights, the height which at least doubles the diameter of the tubular reactor body is reserved for the inlet pipe of the sleeve arranged at the outmost layer to the lower end of the distributor, organic amine, inert components and phosgene can enter respective sleeve which is favor of controlling mixing, or the mixture of organic amine and inert components and phosgene can respectively enter a two-layer sleeve channel for alternate recycle which can easily satisfy the closely initial flow speed to reduce the difference of stay time, and the sleeve arranged at the outmost layer is used by phosgene. The reactor design in the invention and the operation method can effectively control the reaction speed, inhibits adverse reaction from occurring and reduces coking in the inner wall of the reactor.
Description
Technical field
The present invention relates to a kind of continued operation that is used for, satisfy the gas phase phosgenation reactor that appropriateness is mixed needs, particularly a kind of sleeve distributed phosgenation reactor and be used for the method for synthesizing isocyanate.
Background technology
Before 1948, the method of gas phase on-catalytic synthesizing isocyanate just is found (J.H.Saunders, R.J.Slocombe.Chemical Reviews, 1948,43 (2): 203-218), subsequently, patent GB1165831A (the ICI Ltd.1969-10-01 of gas phase phosgenation reactor occurred,), a kind of tubular reactor that has stirring arm is disclosed.But because of the temperature of gas phase phosgenation reaction is higher than 150 ℃, the solid matter that generates in the reaction is very easily attached on the wall, when serious even blocking channel, both reduced product yield, be difficult to realize serialization production again, this technology has been shelved more than two decades at this point, the substitute is the liquid phase light phosgenation.Up to 1988, Germany Bayer AG has improved reaction condition, further promote reaction temperature, adopt the tubular reactor of band central nozzle and peripheral annular space, Reynolds number greater than 4700 turbulent-flow conditions under, 300～500 ℃ of reactions, obtained high product yield (Bayer AG.1988-11-09, EP0289840B1).From then on, the gas phase phosgenation technology is paid much attention to.2006, Bayer AG announced, has developed vapor phase method TDI production new technology (pioneeringtechnology), compared with liquid phase method, and it is nearly 80% that the solvent use amount reduces, and energy-conservation nearly 40%, cost of investment reduces about 20%.
Gas phase phosgenation reactor is the core apparatus that the vapor phase method isocyanates is produced, and prevents that solid phase byproduct from depositing in reactor, closely improves the yield of isocyanates, is the target that reactor design and operation are pursued.In the High Temperature Gas phase reaction, the generation of solid matter comes from two kinds of approach, be respectively that isocyanates further transforms the semicarbazide hydrochloride of generation isocyanates and the oligomer of urea, and generate carbodiimide and isocyanide urea acid imide, these two kinds of approach all transform relevant with the degree of depth of amine and isocyanates.Work as short residence time, when having back-mixing to exist, the side reaction of first kind of approach takes place mainly, the time of staying prolongs, and will cause the generation of the second class side reaction.So the key of design gas phase phosgenation reactor is to control time of staying of fluid well to distribute.US5449818A (Bayer AG.1995-09-12) proposition reactor should remain under the plug flow conditions to be operated, and in 4 times of calibers distances, raw material mixes should reach 10
-3The Reynolds number that segregation degree, tube fluid flow is greater than 4000,0.5～5 second reaction time.EP0593334B1 has provided similar specification requirement (Rhone Poulenc Chimie.1994-04-20).
In addition, reaction temperature is also very remarkable to the influence of gas phase phosgenation reaction, synthesizes example with TDI, and main reaction is:
C
7H
10N
2(g)+2COCl
2(g)＝C
9H
6N
2O
2(g)+4HCl(g)
Reaction table reveals stronger exothermic characteristic, and under its standard state, the relation of reaction heat and temperature is plotted in accompanying drawing 3.
In order to ensure carrying out smoothly of main reaction, the control reaction speed, and shift out reaction heat in time and just seem very important, what adopt usually is the method that adds diluent.Available diluent has: nitrogen, argon gas, benzene,toluene,xylene, monochloro-benzene, o-dichlorohenzene etc.
The synthetic phosgenation reactor of the vapor phase method isocyanates of patent disclosure is divided into two big classes.One class is a concurrent flow nozzle tubular reactor, and another kind of then is nonparallel flow nozzle-type reactor.Both difference are, the way of contact during two bursts of reaction mass initial mixing.The former is in order to reduce back-mixing, and the latter has strengthened mixing.
Concurrent flow nozzle tubular reactor has: the coaxial-type nozzle of EP0699657B1 (Rhone Poulenc Chimie.1996-03-06); The micro-structural formula nozzle of CA2258194A1 (Bayer AG.1999-07-09); The venturi type nozzle of EP1275639B1 (Bayer AG.2003-01-15); The ratio of width to height of WO03045900A1 (BASF AG.2003-06-05) is greater than 2: 1 plate-type reactor, in establish the porous distributor; The tubular reactor that has central nozzle and circular passage of EP1362847A2 (Bayer AG.2003-11-19); The central aperture gas jet distribution mode of EP1319655B1 (Bayer AG.2003-06-18); The middle pressure of CN1310875C (BASF AG.2005-09-28) is the plate-type reactor of operation down; The band central nozzle of US2005113601A1 (Bayer Material Science.2005-5-26) and the tubular reactor of vortex generator; The tubular reactor that has the water conservancy diversion chuck of US2005137417A1 (Bayer Material science AG.2005-06-23)
Nonparallel flow nozzle-type reactor comprises, has the tubular reactor GB1165831A (ICI Ltd.1969-10-01) of stirring, and agitator speed is up to 800rpm, and course of reaction is mixed fully; Draft tube type jet flow device CN101372463A (.2009-02-25 of Ningbo Wanhua Polyurethane Co., Ltd.); The tubular reactor WO2008055898A1 of multi-slit formula nozzle (BASF SE.2008-05-15); Three film parallel type reactor CN101357316A (.2009-02-04 of Ningbo Wanhua Polyurethane Co., Ltd.).
The common feature of above-mentioned reactor is, the initial distribution of gas is the some input of a fluid streams from disperseing, and with another fluid streams concurrent flow or angled cross-flow around the point, thereby realize flowing and mixing of two or more fluids.In this distribution mode, the number of distributed points and the arrangement mode on the cross section have determined fluid to enter flowing and mixed effect of reactor, owing to put on the flow area that is distributed in reactor and present stronger heterogeneity, have neither part nor lot in the cross section that fluid distributes, mixed effect is not good enough, and easily forms back-mixing.
Summary of the invention
In view of the requirement of the gas phase phosgenation reaction pair piston flow type of flow, the present invention proposes on whole flow area, realize the sleeve distributed reactor of layering annular fluid input.It is compared with above-mentioned patent reactor, has following technical characterstic:
1, the initial distribution of fluid occurs on the whole flow area, and fluid is imported circlewise;
2, rely on difference on each layer fluid flow velocity,, realize the mixing of each fluid streams in the mode of interlayer crossflow and diffusion;
3, increased contact-making surface between each fluid streams, promoted to mix and successful reaction is carried out;
4, can select each fluid streams to enter different layers, reach the purpose that control mixes;
5,, be more conducive to realize flow pattern near piston flow because the layering of fluid input.
The present invention has designed a kind of sleeve distributed phosgenation reactor, and the gas phase phosgenation that is used for isocyanates is synthetic, is the phosgenation reaction that raw material is produced toluene di-isocyanate(TDI) (TDI) with phosgene and toluenediamine (TDA) especially.
Structure of reactor as illustrated in fig. 1 and 2.
Sleeve distributed phosgenation reactor of the present invention is to be made of the telescopic distributor of multilayer and tubular reactor main body two parts.
Distributor of the present invention adopts the parallel sleeve of multilayer that is at least four layers; Telescopic distributor has coaxial arrangement mode, and concordant lower end links to each other with the tubular reactor main body, and the upper end has constituted a plurality of fluids feeding-passage for highly different non-isometrical pipes.
The air inlet pipe of outermost layer sleeve keeps the height that doubles the tubular reactor main diameter at least apart from the distributor lower end.
The urceolus of distributor equates that with the tubular reactor main diameter diameter of reactor body is 1: 20～100 with the ratio of reactor length, preferably 1: 25～50.
Adopt sleeve distributed phosgenation reactor to be used for the method for synthesizing isocyanate, organic amine, inert component photoreactive gas are entered one deck sleeve separately, or organic amine and inert component be mixed into one deck sleeve, and phosgene enters another layer sleeve, the cycle arrangement mode that so replaces; The outermost layer sleeve is that phosgene uses.
The reacting appliance of the present invention's design has following characteristics:
1, under the guide functions of the parallel sleeve of multilayer, stratification of hot gas enters tubular reactor;
2, sleeve is at least four layers, and the outermost layer sleeve uses for phosgene;
3, by the tubular reactor outer wall in the sleeve distributor fluid passage of central axis direction, alternating current is crossed two fluid streams of phosgene and organic amine and inert component mixture successively; Or phosgene, inert component and organic amine enter different sleeve passages separately respectively.Preceding a kind of gas initial distribution mode is content with very little and has close flow velocity from the fluid of different passages outflows, to reduce the difference of the time of staying; A kind of mode in back is beneficial to the mixability of control phosgene and organic amine;
4, the actual internal area of each fluid passage can equate in the sleeve, also can be designed to non-constant section and amass according to the requirement of flow velocity;
5, reactant and inert component enter the telescopic distributor of multilayer along the sleeve tangential direction, and when fluid flows out distributor, also stream or adverse current on the eddy flow direction will promote the mixing of each fluid streams.Other mode of entrance is desirable equally.
The fluid that flows out in each sleeve by the radial pulsation that exit velocity difference forms, carries out the mixing of appropriateness, makes flowing as far as possible near piston flow of fluid subsequently.
The purpose that appropriateness is mixed is in order to control reaction speed, avoids because the generation of the rapid temperature rise that fast reaction causes and a large amount of accessory substances, reduces the coking phenomenon of reactor wall.
Adopt the schlieren photograph technology under the high light focusing irradiation, mobile and admixture to the reactor inner fluid detects, carry out colorimetric analysis and digitized processing by the image that high-speed CCD is taken, calculate a certain position in the reactor, the relative concentration of different fluid component, again according to the relative concentration difference at different measuring point place, calculate the concentration variance, last computational methods (Th.N.Zwietering.The degree of mixing in continuous flow systems.Chemical Engineering Science according to the segregation degree, 1959,11 (1): 1-15), obtain near the segregation degree of the fluid to be mixed of distributor outlet.When the segregation degree was 0, the expression fluid reached fully and mixes; When the segregation degree was 1, fluid reached segregation fully.Reach the effect that appropriateness is mixed with the telescopic distributor of the method check multilayer, and contrast, and then obtain the design size of preferred distributor and tubular reactor with the phosgenation reaction effect.
Description of drawings
Fig. 1: the master of reactor looks installation diagram;
Fig. 2: the vertical view of reactor;
Fig. 3: the graph of a relation of reaction heat and temperature.
The specific embodiment
Multilayer sleeve as shown in Figure 1, by one group coaxial, the lower end is concordant, and the highly different non-isometrical pipe in upper end is formed, and is respectively reactor body 1 and sleeve distributor 2～7.The upper end of distributor becomes shape straggly to arrange, it is marked with the position 10 of horizontal direction arrow, can be for the intake pipeline that connects different fluid, the top of each layer sleeve (2～7), except that center sleeve 7 opened wide, remaining all had been designed to structure of cover plate, and 9 one-tenth of cover plates are circular, the outer is connected with sleeve, and middle circular hole is connected with another isometrical sleeve; The distributor lower end links to each other with reactor body 1.Only from distributor lower end inflow reactor main body 1, should guarantee that upper cover plate 9 closely contacts with each sleeve, does not stay the gap for guaranteeing fluid.Fig. 2 is the view that digs along the A-A cross section among Fig. 1 after opening, and the fluid that enters distributor from the multilayer sleeve is flowed out in the mode of advancing side by side by the annular gap of distributor lower end, mixes in reactor body 1, moves to the reactor outlet direction.Meanwhile,, be provided with four locating supports 8 of symmetry, and be arranged on equally on the interior equal height of each layer sleeve at the shortest outer layer sleeve 2 cover plates 9 places, coaxial in order to guarantee each layer sleeve with tubular reactor main body 1.
Be to the concrete test of reactor below and use example: for the material rate that is used for synthesizing isocyanate, temperature, process conditions adopt the condition of prior art to get final product when empty etc.
Embodiment 1:
With nitrogen N
2, carbon dioxide CO
2With CFC CCl
2F
2Be three kinds of analog gas, under room temperature, the normal pressure, use the reactor body internal diameter to be 20mm, length is four layers of transparent tubular reactor of sleeve of 400mm, all the other the air inlet pipe center lines of distributor except that center sleeve and the axis normal of each layer sleeve, and enter the telescopic distributor of multilayer along the sleeve tangential direction.The outermost layer air inlet pipe leaves the distribution height of 40mm to the distributor lower end.When the actual internal area of every layer of sleeve equates, and equal 28.3mm
2, CCl
2F
2And N
2Mixed airflow through center sleeve, CO
2Flow through adjacent with it ground floor sleeve, another gang CCl
2F
2And N
2Gaseous mixture flow through second layer sleeve, second gang of CO
2Flow through the 3rd layer, i.e. outermost layer sleeve, CCl
2F
2, CO
2And N
2Flow be respectively 0.5,2.0 and 0.9L/min.Adopt the measurements and calculations method of segregation degree, obtained in the tubular reactor main body of outlet 40 of distance distributor and 80mm, the segregation degree reaches 0.04 and 0.02 respectively.
Embodiment 2:
The reactor that embodiment 1 is mentioned, use six layers of telescopic distributor and 500mm tubular reactor principal length instead, all the other the air inlet pipe center lines of distributor except that center sleeve and the axis normal of each layer sleeve, and enter the telescopic distributor of multilayer along the sleeve tangential direction, to the distributor lower end, leave the distribution height of 80mm from outermost layer air inlet pipe center line.When the actual internal area of every layer of sleeve pipe equates, and equal 7.0mm
2, CCl
2F
2The center sleeve of flowing through, N
2Flow through adjacent with it ground floor sleeve, CO
2Flow through second layer sleeve, another gang CCl
2F
2, N
2And CO
2Flow through the 3rd, the 4th and the layer 5 telescopic pipe respectively.CCl
2F
2, CO
2And N
2Flow be respectively 0.5,2.0 and 0.9L/min.Adopt the measurements and calculations method of segregation degree, obtained in the tubular reactor main body of outlet 40 of distance distributor and 80mm, the segregation degree reaches 0.025 and 0.014 respectively.
Embodiment 3:
In the reactor identical with embodiment 2.CCl
2F
2And N
2Mixed airflow through center sleeve, CO
2Flow through adjacent with it ground floor sleeve, another gang CCl
2F
2And N
2Gaseous mixture flow through second layer sleeve, second gang of CO
2Flow through the 3rd layer of sleeve, the 3rd gang of CCl
2F
2And N
2Gaseous mixture flow through the 4th layer of sleeve, the 3rd gang of CO
2Flow through layer 5, i.e. the outermost layer sleeve.CCl
2F
2, CO
2And N
2Flow be respectively 0.5,2.0 and 0.9L/min.Adopt the measurements and calculations method of segregation degree, obtained in the tubular reactor main body of outlet 40 of distance distributor and 80mm, the segregation degree reaches 0.016 and 0.008 respectively.
Embodiment 4:
With the reactor and the flow distribution pattern of embodiment 3 same diameter, reactor length is 2000mm.CCl
2F
2, CO
2And N
2Flow be respectively 1.5,4.5 and 3L/min.Adopt the measurements and calculations method of segregation degree, obtained in the tubular reactor main body of outlet 40 of distance distributor and 80mm, the segregation degree reaches 0.007 and 0.003 respectively.
Embodiment 5: four layers of sleeve distributed reactor that adopt embodiment 1, the tubular reactor principal length is 1000mm, all the other the air inlet pipe center lines of distributor except that center sleeve and the axis normal of each layer sleeve, and enter the telescopic distributor of multilayer along the sleeve tangential direction, to the distributor lower end, leave the distribution height of 80mm from outermost layer air inlet pipe center line.When the actual internal area of every layer of sleeve pipe equates, and equal 28.3mm
2The time, one CO
2The center sleeve of flowing through, CCl
2F
2And N
2Gaseous mixture flow through adjacent with it ground floor sleeve, another gang CO
2Flow through second layer sleeve, second gang of CCl
2F
2And N
2Gaseous mixture flow through the 3rd layer, i.e. outermost layer sleeve, CCl
2F
2, CO
2And N
2Flow be respectively 0.5,2.0 and 0.9L/min.Adopt the measurements and calculations method of segregation degree, obtained in the tubular reactor main body of outlet 40 of distance distributor and 80mm, the segregation degree reaches 0.036 and 0.017 respectively.
Embodiment 6: adopt six layers of sleeve distributed reactor of embodiment 2, carrying out with the toluenediamine photoreactive gas is raw material, and nitrogen is the gas phase phosgenation reaction of inert diluent.
The reactor body internal diameter is 20mm, and length is 500mm, the axis normal of the air inlet pipe of distributor and each layer sleeve, and enter the telescopic distributor of multilayer along the sleeve tangential direction, to the distributor lower end, leave the distribution height of 80mm from air inlet pipe.The actual internal area of every layer of sleeve pipe equates, and equals 7.0mm
2
Toluenediamine, phosgene and nitrogen respectively are divided into two strands, and first strand of phosgene enters layer 5, and promptly 2, the first strands of inert component nitrogen of outermost layer sleeve enter adjacent with it 3, the first strands of toluenediamines of the 4th layer of sleeve and flow into the 3rd layer of sleeve 4; Second strand of phosgene enters 5, the second strands of nitrogen of second layer sleeve and enters 6, the second strands of toluenediamines of ground floor sleeve and enter center sleeve 7.The flow of toluenediamine, phosgene and nitrogen is respectively 1.0,3.0 and 0.5g/min.Enter before the distributor, toluenediamine, phosgene and nitrogen are preheated to 320 ℃, and reactor is controlled at 0.1MPa, and 300 ℃ of operations down are 3.6s when empty, and the yield of TDI is 0.89.React after 90 hours, reactor wall does not have coking phenomenon.
Embodiment 7: in the reactor identical with embodiment 6, carrying out with the toluenediamine photoreactive gas is raw material, and nitrogen is the gas phase phosgenation reaction of inert diluent.
Toluenediamine, phosgene and nitrogen respectively are divided into three strands, and first strand of phosgene enters layer 5, promptly 2, the first strands of inert component nitrogen of outermost layer sleeve with enter adjacent with it 3, the second strands of phosgene of the 4th layer of sleeve after first strand of toluenediamine mixes and flow into the 3rd layer of sleeve 4; Second strand of nitrogen and second strand of toluenediamine are mixed into and enter center sleeve 7 after 5, the three strands of phosgene of second layer sleeve enter 6, the three strands of nitrogen of ground floor sleeve and the 3rd burst of toluenediamine mixing.The flow of toluenediamine, phosgene and nitrogen is respectively 1.0,3.0 and 0.5g/min.Enter before the distributor, toluenediamine, phosgene and nitrogen are preheated to 400 ℃, and reactor is controlled at 0.1MPa, and 300 ℃ of operations down are 3.6s when empty, and the yield of TDI is 0.91.React after 90 hours, reactor wall has slight coking phenomenon.
Embodiment 8: with the reactor of embodiment 6 same diameter and distributor structure in, carrying out with the toluenediamine photoreactive gas is raw material, nitrogen is the gas phase phosgenation reaction of inert diluent.The tubular reactor principal length increases to 2000mm.
Toluenediamine, phosgene and nitrogen respectively are divided into three strands, and first strand of phosgene enters layer 5, promptly 2, the first strands of inert component nitrogen of outermost layer sleeve with enter adjacent with it 3, the second strands of phosgene of the 4th layer of sleeve after first strand of toluenediamine mixes and flow into the 3rd layer of sleeve 4; Second strand of nitrogen and second strand of toluenediamine are mixed into and enter center sleeve 7 after 5, the three strands of phosgene of second layer sleeve enter 6, the three strands of nitrogen of ground floor sleeve and the 3rd burst of toluenediamine mixing.The flow of toluenediamine, phosgene and nitrogen is respectively 9.0,21.0 and 12.0g/min.Enter before the distributor, toluenediamine, phosgene and nitrogen are preheated to 320 ℃, and reactor is controlled at 0.1MPa, and 300 ℃ of operations down are 1.1s when empty, and the yield of TDI is 0.98.React after 100 hours, reactor wall does not have tangible coking phenomenon.
Embodiment 9: in the tubular reactor that five layers of sleeve with embodiment 6 same diameter distribute, carrying out with the toluenediamine photoreactive gas is raw material, and nitrogen is the gas phase phosgenation reaction of inert diluent.All the other the air inlet pipe center lines of distributor except that center sleeve and the axis normal of each layer sleeve, and enter the telescopic distributor of multilayer along the sleeve tangential direction, to the distributor lower end, leave the distribution height of 40mm from air inlet pipe.When the actual internal area of every layer of sleeve pipe equates, and equal 19.5mm
2, the tubular reactor principal length is 1000mm.
Toluenediamine and nitrogen respectively are divided into three strands, and phosgene is divided into two strands.First strand of inert component nitrogen with enter layer 5 after first strand of toluenediamine mixes, i.e. outermost layer sleeve, first strand of phosgene enters the 4th layer of adjacent with it sleeve, second strand of nitrogen and second strand of toluenediamine are mixed into the 3rd layer of sleeve; Second strand of phosgene flows into second layer sleeve, enters center sleeve after the 3rd strand of nitrogen and the 3rd strand of toluenediamine mix.The flow of toluenediamine, phosgene and nitrogen is respectively 9.0,21.0 and 12.0g/min.Enter before the distributor, toluenediamine, phosgene and nitrogen are preheated to 320 ℃, and reactor is controlled at 0.1MPa, and 350 ℃ of operations down are 0.8s when empty, and the yield of TDI is 0.88.React after 40 hours, coking phenomenon obviously takes place in reactor wall.
The present invention open and sleeve distributed phosgenation reactor that discloses and the method that is used for synthesizing isocyanate.Although product of the present invention and method are described by preferred embodiment, but those skilled in the art obviously can change the techniques described herein in not breaking away from content of the present invention, spirit and scope, more particularly, the replacement that all are similar and change apparent to those skilled in the artly, they are regarded as being included in spirit of the present invention, scope and the content.
Claims (6)
1. a sleeve distributed phosgenation reactor is characterized in that reactor is made of the telescopic distributor of multilayer and tubular reactor main body two parts.
2. sleeve distributed phosgenation reactor as claimed in claim 1 is characterized in that distributor adopts the parallel sleeve of multilayer that is at least four layers; Telescopic distributor has coaxial arrangement mode, and concordant lower end links to each other with the tubular reactor main body, and the upper end is a plurality of fluids feeding-passage that highly different non-isometrical pipes constitutes.
3. sleeve distributed phosgenation reactor as claimed in claim 2, it is characterized in that, center sleeve (7) is from mouth of pipe air inlet, the center line of all the other sleeve air inlet pipe (10) and the axis normal of each layer sleeve, and enter the telescopic distributor of multilayer along the sleeve tangential direction; Except that center sleeve, all the other sleeves are provided with cover plate (9), and the top cover closure of each layer sleeve, cover plate (9) become circular, and the outer is connected with sleeve, and middle circular hole is connected with another isometrical sleeve.
4. sleeve distributed phosgenation reactor as claimed in claim 2, the air inlet pipe that it is characterized in that the outermost layer sleeve keep the height that doubles the tubular reactor main diameter at least apart from the distributor lower end.
5. sleeve distributed phosgenation reactor as claimed in claim 1 is characterized in that the urceolus of distributor equates with the tubular reactor main diameter, and the diameter of reactor body is 1: 20～100 with the ratio of reactor length.
6. adopt the method for the described sleeve distributed phosgenation reactor synthesizing isocyanate of claim 1, it is characterized in that organic amine, inert component photoreactive gas enter one deck sleeve separately, or organic amine and inert component are mixed into one deck sleeve, phosgene enters another layer sleeve, the cycle arrangement mode that so replaces; The outermost layer sleeve is that phosgene uses.
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103224457A (en) * | 2013-04-15 | 2013-07-31 | 湘潭大学 | Method and device for continuous preparation of carbamyl chloride |
| CN105170069A (en) * | 2015-10-09 | 2015-12-23 | 中国科学院过程工程研究所 | Tower-type gas-liquid contact equipment even gas distribution device and application thereof |
| CN107715808A (en) * | 2017-10-24 | 2018-02-23 | 薛永和 | A kind of gas phase phosgenation reactor and its application in organic isocyanate synthesis |
Family Cites Families (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE3717058A1 (en) * | 1987-05-21 | 1988-12-08 | Bayer Ag | MIXER FOR MIXING AT LEAST TWO FLOWABLE SUBSTANCES, ESPECIALLY UNDERSTANDING OR. INITIATING A REACTION DURING MIXING |
| DE3744001C1 (en) * | 1987-12-24 | 1989-06-08 | Bayer Ag | Process for the continuous production of mono- or polyisocyanates |
| CN101372463B (en) * | 2007-08-21 | 2011-04-20 | 宁波万华聚氨酯有限公司 | Draft tube type jet flow reactor and method for preparing isocyanate using the same |
-
2009
- 2009-08-11 CN CN2009100701123A patent/CN101623615B/en active Active
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103224457A (en) * | 2013-04-15 | 2013-07-31 | 湘潭大学 | Method and device for continuous preparation of carbamyl chloride |
| CN105170069A (en) * | 2015-10-09 | 2015-12-23 | 中国科学院过程工程研究所 | Tower-type gas-liquid contact equipment even gas distribution device and application thereof |
| CN105170069B (en) * | 2015-10-09 | 2018-03-13 | 中国科学院过程工程研究所 | A kind of uniform distribution device of tower gas-liquid contanct equipment and application thereof |
| CN107715808A (en) * | 2017-10-24 | 2018-02-23 | 薛永和 | A kind of gas phase phosgenation reactor and its application in organic isocyanate synthesis |
| CN107715808B (en) * | 2017-10-24 | 2023-12-22 | 摩珈(上海)生物科技有限公司 | Gas-phase phosgenation reactor and application thereof in synthesis of organic isocyanate |
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|---|---|
| CN101623615B (en) | 2011-11-23 |
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