CN101879425A - Reactor and method for preparing isocyanate - Google Patents
Reactor and method for preparing isocyanate Download PDFInfo
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- CN101879425A CN101879425A CN 201010232065 CN201010232065A CN101879425A CN 101879425 A CN101879425 A CN 101879425A CN 201010232065 CN201010232065 CN 201010232065 CN 201010232065 A CN201010232065 A CN 201010232065A CN 101879425 A CN101879425 A CN 101879425A
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Abstract
The invention relates to a reactor for preparing isocyanate in a gas phase, which comprises a mixer and a tubular reactor, wherein a 5 to 45 variable-diameter connecting element is arranged between the mixer and the tubular reactor; an internal member is arranged in the tubular reactor. The invention also discloses a method for preparing isocyanate by using the reactor, which comprises the following steps: diluting primary amine with an inert gas or vapor of an inert solvent, and mixing and reacting the mixed gas of diluted primary amine with phosgene in the mixer; and allowing the obtained reaction product to flow into the tubular reactor from the mixer and the variable-diameter connecting element of the tubular reactor to undergo a further reaction, and cooling and absorbing the product of the reaction to obtain an isocyanate product. When the reactor provided by the invention is adopted, the length of the tubular reactor is reduced by arranging the variable-diameter connecting element between the mixer and the tubular reactor; and as the internal member is arranged in the tubular reactor, the reaction effect in the reactor is improved and the product yield is improved.
Description
Technical field
The present invention relates to a kind of method that in gas phase, prepares the reactor of isocyanates and pass through this reactor made isocyanates.
Background technology
The vapor phase production isocyanates is meant with gas phase primary amine and phosgene and reacts the method that generates isocyanates.European patent EP 0593334A has described a kind of method for preparing aromatic isocyanate in gas phase, do not comprise any dynamic tumbler in the tubular reactor that this method adopted, only utilize the contractile response wall to increase disturbance, compare with the mixed effect that the standard of use hybrid element is obtained, its mixed effect is relatively poor, and this bad mixing will cause forming undesirable solid product.
European patent EP 0699657A has described a kind of method for preparing aromatic isocyanate in gas phase, being reflected in the mixing reactor of aromatic diamine and phosgene carried out, this reactor is divided into two zones, inner region accounts for 20～80% of total reactor volume for the Mixed Zone that the diamines photoreactive gas mixes; Exterior domain is the conversion zone near the piston flow form, accounts for 80～20% of total reaction volume.Yet, because at least 20% reaction volume desirable back-mixing can not occur, therefore cause the uneven time of staying to distribute, form undesirable solid product.
European patent EP 1362847A has described a kind of method for preparing isocyanates in gas phase, in the method, by with the center of relevant measure of flowing as adding homogenizing element and definite gas phase educt in reactor, improve the response characteristic in the tubular reactor, thereby avoid deposit in the reactor and cause the formation of the secondary species of the polymerization that reactor lifetime shortens.
European patent EP 1555258A has described a kind of blender and method for preparing isocyanates in gas phase, a kind of tubular reactor also is provided, it has the double wall conduit that extends along the center on the reactor direction of rotation, the concentric annular gap that between the inner and outer wall of double wall conduit, forms, improve the mixing of raw material in the tubular reactor by the method, reduce the possibility that accessory substance forms.
European patent EP 0749958A has described a kind of method for preparing triisocyanate, and in the method, triamine and phosgene are with the flow velocity continuous light gasification reaction of 3m/s at least in 200-600 ℃ the cylindricality reaction compartment in the temperature that does not comprise any motion assembly.
More than prepare in the invention of isocyanates about vapor phase method, good initial mixing, enough reaction times and in tubular reactor enough turbulent extent and temperature control be necessary, complex optimum by above-mentioned condition, can obtain preferable reaction effect, be the generation of higher selectivity and less solid sediment, improve the yield of end product.In order to satisfy above-mentioned condition simultaneously, especially in the process of preparation aromatic isocyanate, need the long time of staying, guarantee that simultaneously the fluid in the tubular reactor has enough flowing velocities.Usually the tubular reactor in the industrialized unit has very long length, even adopt the plate-type reactor described in the EP01451150A to avoid, and the difficulty when this causes the increase of plant construction investment and practical operation.In a word, in industrialized gas phase phosgenation reaction, use the large tubular reactor, reducing its length has realistic meaning.
Summary of the invention
The purpose of this invention is to provide a kind of novel reactor and the process that in gas phase, prepare isocyanates, adopt this reactor, under the prerequisite that guarantees enough mixed effects, can shorten the length of needed tubular reactor effectively, thereby reduce the operation easier of plant construction investment and actual industrial phosgenation device, the applicability of intensifier; Another object of the present invention is the less turbulence that improves in the tubular reactor, strengthens mass transfer, heat-transfer effect, improves reaction effect.
In order to achieve the above object, reactor provided by the present invention comprises interior feed pipe, outer feed pipe, blender, reducing connection element and tubular reactor, wherein, feed pipe is arranged on internal mixer in described, described outer feed pipe is communicated with blender by the sidewall of blender, the downstream of described blender links to each other with tubular reactor by the reducing connection element, and makes the diameter of tubular reactor greater than the diameter of blender, is provided with inner member in the described tubular reactor.
According to reactor provided by the present invention, the joint face of the reducing connection element of wherein said blender is regular or irregular, includes but not limited to curved surface or stepped joint face etc., and described reducing connection element is preferably conical butt; Angle between described joint face and the reactor axis is 5～45 °, is preferably 10～30 °; When described joint face is irregular, the two ends of joint face are connected with straight line, calculate the angle between this straight line and the reactor axis then.
According to reactor provided by the present invention, wherein said blender is dynamic mixer, static mixer or central jet formula blender.
According to a kind of concrete embodiment of reactor provided by the present invention, the lower end of wherein said interior feed pipe is provided with nozzle, and generally speaking, in order to guarantee good initial mixing effect, the flow velocity of phosgene is at least 1m/s before needing to guarantee to mix; Amine gas is 12-120m/s at the flow velocity at interior feed pipe nozzle place.Therefore, should not the diameter design of preliminary Mixed Zone is excessive, this causes the diameter of reactor can not be excessive, and in order to guarantee the abundant mixing of reaction raw materials in reactor, usually has only the length that prolongs tubular reactor, this has not only increased equipment cost, has also increased industrialized operation easier.The present invention is by being provided with the reducing connection element with blender and tubular reactor combination in blender and tubular reactor, when the diameter that guarantees blender is not increased, can increase the diameter of tubular reactor easily, thereby reduce the length of tubular reactor.
In the present invention,, inner member is set in tubular reactor, strengthens the transmission effect in the tubular reactor to improve the turbulent extent in the tubular reactor in order to guarantee the reaction effect after reactor length reduces.These inner members can be rules, also can be irregular, preferably regular.Known inner member includes but not limited to porous plate, screen cloth, structured packing, dumped packing etc., is preferably structured packing; Described inner member can be one section, also can be multistage, and the total length of common inner member is 2-8 a times of tubular reactor diameter, is preferably 3-5 doubly; When described inner member was multistage, the spacing between adjacent two sections inner members was 0.5-1 a times of tubular reactor diameter; Described inner member is dismountable, that is, can be easily take out from tubular reactor and clean, and be reentered in the reactor and use; The material of described inner member can adopt metal material or nonmetallic materials, the preferred nonmetal porous material of inertia under the phosgenation reaction condition, as pottery, carborundum, quartz glass etc., the material that further preferably has good thermal conductive property under the phosgenation reaction condition is as carborundum etc.; Every section inner member is placed in the tubular reactor by support plate, and support plate generally adopts grid type, also can adopt other form, and as orifice-plate type, support plate can be dismantled, and is convenient to the dismounting of inner member.
According to reactor provided by the present invention, wherein said tubular reactor comprises single hose reactor, shell and tube reactor, one-board reactor or strake formula reactor.According to of the present invention preferred embodiment a kind of, described tubular reactor is the single hose reactor, preferably is the axisymmetric single circular pipe type reactor in center, ratio≤1 between the pipe range of its cross-sectional diameter and tubular reactor, preferred≤0.5; According to another preferred embodiment of the present invention, described tubular reactor is the one-board reactor, and the ratio of width to height of the inner passage in this plate-type reactor was at least 2: 1.
The present invention also provides a kind of method that adopts above-mentioned reactor made isocyanates, said method comprising the steps of:
1) the primary amine photoreactive gas is preheated to gas; Adopt the steam dilution primary amine gas of inert gas or atent solvent, resulting primary amine mist after dilution enters blender by interior feed pipe; Phosgene enters blender by outer feed pipe, and two strands of materials mix in blender, react;
2) reactant that mixes in blender, obtains after the reaction reducing connection element of flowing through enters further reaction in the tubular reactor, and reaction products resulting obtains isocyanate products after absorption condensation is handled.
According to the method for preparing isocyanates provided by the present invention, the preheat temperature of wherein said primary amine photoreactive gas is higher 10～200 ℃ than the boiling point of described primary amine, and is preferably high 20～100 ℃ than the boiling point of described primary amine.
According to the method for preparing isocyanates provided by the present invention, wherein said primary amine photoreactive gas can adopt modes such as electrical heating, Steam Heating, fused salt heating to carry out preheating, finally make the primary amine photoreactive gas be gasificated into 290～500 ℃ gas, be preferably 300～400 ℃ gas, and wherein do not contain any not primary amine or the phosgene drop of gasification; Primary amine gas adopts inert gas or atent solvent to dilute, described inert gas is selected from one or more in nitrogen, argon gas, helium, the carbon dioxide, described atent solvent is that halogen replaces or unsubstituted aromatic hydrocarbons, for example toluene, dimethylbenzene, o-dichlorohenzene or decahydronaphthalenes.The steam of described inert gas or atent solvent and the mol ratio of primary amine are 8: 1～1: 1, are preferably 5: 1～1.2: 1; The steam of inert gas or atent solvent with preferably be preheated to the temperature identical before primary amine gas mixes with primary amine gas.
According to the method for preparing isocyanates provided by the present invention, the mol ratio of the amido in wherein said phosgene and the primary amine is 10: 1～1: 1, is preferably 6: 1～2: 1; The incorporation time of two strands of reaction masses in blender was less than 0.1 second; Through the time of staying of reaction logistics in tubular reactor of mixing, reaction obtains is 1～30 second, preferred 2～20 seconds, and further preferred 3～15 seconds.
According to the method for preparing isocyanates provided by the present invention, wherein said primary amine comprises primary aromatic amine or Armeen, not resolvent diamines after the preferred gasification, for example toluenediamine (TDA), methylene dianiline (MDA) (MDA), 1, in 6-hexamethylene diamine (HDA), the IPD (IPDA), not resolvent aromatic diamine after more preferably gasifying, for example toluenediamine, methylene dianiline (MDA) etc., further preferred mass than be 80/20 or 65/25 2,4/2,6-toluenediamine mixture or 2, the 4-toluenediamine.
In the present invention, commonly used absorption tower, this area or condenser all can be used as absorption plant and resulting gas product in the tubular reactor is carried out absorption condensation handle.Method provided by the present invention is fit to preparation toluene di-isocyanate(TDI) (TDI), methyl diphenylene diisocyanate (MDI), 1, hexamethylene-diisocyanate (HDI), IPDI (IPDI) are particularly suitable for preparing toluene di-isocyanate(TDI) (TDI).
In the present invention, owing in DESIGN OF REACTOR, adopted the reducing connection, the diameter of tubular reactor can increase greatly, under the prerequisite that guarantees the sufficiently long time of staying, can significantly reduce the entire length of tubular reactor, increased the operability of equipment, the investment of whole device is obviously reduced; In addition, owing in tubular reactor, be provided with inner member, even under the lower situation of the gas speed in reactor, also can guarantee the transmission effect in the reactor, thereby reach a comparatively desirable reaction effect.
Description of drawings
Fig. 1 is the structural representation of a kind of preferred reactor of the present invention, wherein: 1 is interior feed pipe, and 2 is outer feed pipe, and 3 is blender, 4 is the reducing connection element, 5 is tubular reactor, and 6 is the filler inner member, and 7 is support plate, α is the angle of reducing connection element and reactor axis, F1 is the charging of primary amine mist, and F2 is the phosgene charging, and F3 is a gaseous product.
The specific embodiment
Further specify the present invention below with reference to Fig. 1.
Fig. 1 is a kind of preferred reactor for preparing isocyanates in gas phase provided by the present invention.Described reactor comprises interior feed pipe 1, outer feed pipe 2, blender 3, reducing connection element 4 and tubular reactor 5, wherein, interior feed pipe 1 and blender 3 coaxial installations, outer feed pipe 2 is communicated with blender 3 by the sidewall of blender, the lower end of blender 3 links to each other with tubular reactor 5 through reducing connection element 4, be provided with two sections filler inner members 6 in the tubular reactor 5, every section filler inner member is arranged in the tubular reactor 5 by gripper shoe 7.Reducing connection element 4 is a conical butt, and the angle α between the axis of its joint face and reactor is 5～45 °.As shown in Figure 1, with the steam preheating of primary amine and inert gas or atent solvent temperature to the boiling point 10-200 that is higher than primary amine ℃, wherein primary amine is gasificated into the steam formation primary amine mist of gas and above-mentioned inert gas or atent solvent, enter interior feed pipe 1 along F1, after phosgene is preheating to the temperature identical with the primary amine mist simultaneously, feed pipe 2 outside F2 enters, and above-mentioned two strands of material gases are in the nozzle place rapid mixing of blender 3 and carry out preliminary reaction.Unstripped gas is through after preliminary mixing, reacting, the product that is generated through reducing connection element 4, enters into tubular reactor 5 then and further reacts earlier, and the time of staying of described product in tubular reactor 5 is 1～30 second, preferred 2～20 seconds, further preferred 3～15 seconds.The gaseous product that reaction obtains enters absorption plant along F 3 and carries out condensation absorption processing, obtains isocyanate products.
Following examples will further specify reactor provided by the present invention and adopt the method for this reactor made isocyanates, but therefore the present invention is not subjected to any restriction.
Comparative Examples 1
Adopting diameter is Yantai Wanhua Polyurethane Co., Ltd's homemade central jet formula blender of 1m, and the lower end of this blender connects single circular pipe type reactor, and the diameter of this tubular reactor is identical with central jet formula blender.Feed pipe and outer feed pipe in described central jet formula blender is provided with, under 320 ℃ be with mass ratio 80: 20 2,4-toluenediamine and 2, the mist of 6-toluenediamine mixes, dilutes with o-dichlorohenzene, and o-dichlorohenzene (ODCB) is 3: 1 with the mol ratio of diamines.Enter tubular reactor after diamines mist after the dilution and the phosgene process blender rapid mixing, the mol ratio of the amino in phosgene and the toluenediamine is 5: 1.The reaction time of vapor-phase reactant in tubular reactor is 7 seconds.Reaction gas speed in this tubular reactor is 3m/s.In order to guarantee enough reaction times, the length of this tubular reactor is 21m.After reactor, gaseous product absorbs through condensation and obtains toluene di-isocyanate(TDI).Inlet amount with toluenediamine is calculated, and the yield of final phosgenation reaction is 97.2%.
Comparative Examples 2
Adopt the central jet formula blender identical with Comparative Examples 1, and the lower end of this blender connects single circular pipe type reactor by the reducing connection element shown in Fig. 1, this connection element is 0.866m along the length on the blender axis direction, and the angle between the joint face of reducing connection element and the blender axis is 30 °.Through the reducing connection element, the diameter of single circular pipe type reactor becomes 2m, and length is 4.8m, and the total length of reducing connection element and tubular reactor is about 5.7m, the length of the tubular reactor in the Comparative Examples 1.
Under 320 ℃, with mass ratio be 80: 20 2,4-toluenediamine and 2, the mist of 6-toluenediamine mixes, dilutes with o-dichlorohenzene, the mol ratio of o-dichlorohenzene (ODCB) and diamines is 3: 1.Diamines mist after the dilution and phosgene be rapid mixing in central jet formula blender, behind initial reaction, enter tubular reactor, the mol ratio of the amino in phosgene and the toluenediamine is 5: 1, and the time of staying of the admixture of gas of initial reaction gained in tubular reactor is 7 seconds.The speed of the material pneumatic in the tubular reactor is 0.75m/s.After reactor, gaseous product absorbs through condensation and obtains toluene di-isocyanate(TDI).Inlet amount with toluenediamine is calculated, and the yield of final phosgenation reaction is 95.1%.
Embodiment 1
Adopt central jet formula blender, reducing connection element and the single circular pipe type reactor identical with Comparative Examples 2, the structured packing that has increased carborundum simultaneously in tubular reactor is with mass transfer, heat-transfer effect in the increase course of reaction.Described carborundum structured packing is the customization of Shenyang metal research institute of the Chinese Academy of Sciences, begin to place from the lower end of reducing connection element, two sections carborundum structured packings are set in tubular reactor, every section is adopted grid support plate to fix, every section long 2m of filler, between two sections fillers apart from 0.6m.
Under 320 ℃, with mass ratio be 80: 20 2,4-toluenediamine and 2, the mist of 6-toluenediamine mixes, dilutes with o-dichlorohenzene, the mol ratio of o-dichlorohenzene (ODCB) and diamines is 3: 1.Diamines mist after the dilution and phosgene be rapid mixing in central jet formula blender, behind initial reaction, enter tubular reactor, the mol ratio of the amino in phosgene and the toluenediamine is 5: 1, and the time of staying of the admixture of gas of initial reaction gained in tubular reactor is 7 seconds.The speed of the material pneumatic in the tubular reactor is 0.75m/s.After reactor, gaseous product absorbs through condensation and obtains toluene di-isocyanate(TDI).Inlet amount with toluenediamine is calculated, and the yield of final phosgenation reaction is 97.4%.The reactor made isocyanates that the reducing connection element is set of the present invention is adopted in this explanation between blender and tubular reactor, not only significantly reduced the length of tubular reactor, simultaneously by inner member is set in tubular reactor, improve reaction effect, also guaranteed product yield.
Claims (15)
1. reactor for preparing isocyanates, it is characterized in that: this reactor comprises interior feed pipe, outer feed pipe, blender, reducing connection element and tubular reactor; Wherein, feed pipe is arranged at internal mixer in described, described outer feed pipe is communicated with blender by the sidewall of blender, the lower end of described blender links to each other with tubular reactor by the reducing connection element, and make the diameter of tubular reactor greater than the diameter of blender, be provided with inner member in the described tubular reactor.
2. reactor according to claim 1 is characterized in that, the joint face and the angle between the reactor axis of described reducing connection element are 5～45 °, are preferably 10～30 °; Described joint face is regular or irregular, preferably regular.
3. reactor according to claim 2 is characterized in that described inner member is dismountable, and it is selected from porous plate, screen cloth, structured packing, the dumped packing one or more, is preferably structured packing; The material of described inner member adopts metal material or nonmetallic materials, is preferably the nonmetal porous material of inertia.
4. reactor according to claim 3 is characterized in that, described inner member material adopts pottery, carborundum, quartz glass, preferably adopts carborundum; Described inner member is one or more snippets, and the total length of inner member is 2-8 a times of tubular reactor diameter, and preferred 3-5 doubly; Every section inner member is placed in the tubular reactor by support plate, and support plate adopts grid type or orifice-plate type, and described support plate is dismountable; When inner member was multistage, the spacing between adjacent two sections inner members was 0.5-1 a times of tubular reactor diameter.
5. reactor according to claim 4 is characterized in that, described blender is dynamic mixer, static mixer or central jet formula blender.
6. reactor according to claim 5 is characterized in that, described tubular reactor is single hose reactor, shell and tube reactor, one-board reactor or strake formula reactor.
7. reactor according to claim 6 is characterized in that described tubular reactor is the single hose reactor, is preferably to be the axisymmetric single circular pipe type reactor in center ratio≤1 between the pipe range of its cross-sectional diameter and tubular reactor, preferred≤0.5.
8. reactor according to claim 6 is characterized in that, described tubular reactor is the one-board reactor, and the ratio of width to height of the inner passage in the described one-board reactor was at least 2: 1.
9. adopt the method for the described reactor made isocyanates of aforementioned each claim, this method may further comprise the steps:
1) the primary amine photoreactive gas is preheated to gas; Adopt the steam dilution primary amine gas of inert gas or atent solvent, resulting primary amine mist after dilution enters blender by interior feed pipe; Phosgene enters blender by outer feed pipe, and two strands of materials mix in blender, react;
2) reactant that mixes in blender, obtains after the reaction reducing connection element of flowing through enters further reaction in the tubular reactor, and reaction products resulting obtains isocyanate products after absorption condensation is handled.
10. method according to claim 9, it is characterized in that, in the step 1) steam of inert gas or atent solvent be preheated to and the identical temperature of described primary amine gas before primary amine gas mixes, preheat temperature is higher 10～200 ℃ than the boiling point of described primary amine, and is preferred high 20～100 ℃.
11. method according to claim 10 is characterized in that, the steam of described inert gas or atent solvent and the mol ratio of primary amine are 8: 1～1: 1, are preferably 5: 1～1.2: 1.
12. method according to claim 11 is characterized in that, the mol ratio of the amino in described phosgene and the primary amine is 10: 1～1: 1, is preferably 6: 1～2: 1.
13., it is characterized in that described primary amine mist and the incorporation time of phosgene in blender were less than 0.1 second according to each described method among the claim 10-12; The time of staying of product in tubular reactor that obtains after described mixing in blender, the reaction is 1～30 second, is preferably 2～20 seconds, more preferably 3～15 seconds.
14. method according to claim 13 is characterized in that, described primary amine comprises primary aromatic amine or Armeen, not resolvent diamines after the preferred gasification, not resolvent aromatic diamine after the further preferred gasification.
15. method according to claim 14 is characterized in that, described primary amine is selected from toluenediamine, methylene dianiline (MDA), 1, a kind of in 6-hexamethylene diamine, the IPD; Preferably, described primary amine is toluenediamine or methylene dianiline (MDA), more preferably mass ratio be 80/20 or 65/25 2,4/2,6-toluenediamine mixture or 2,4-toluenediamine.
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Cited By (7)
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| CN104874335A (en) * | 2015-05-14 | 2015-09-02 | 万华化学集团股份有限公司 | Reactor for preparing isocyanate and method of reactor for preparing isocyanate |
| CN105032307A (en) * | 2015-07-21 | 2015-11-11 | 万华化学集团股份有限公司 | Dynamic self-cleaning reactor and method for preparing isocyanate |
| CN105617957A (en) * | 2014-10-27 | 2016-06-01 | 中国科学院大连化学物理研究所 | Method for strengthening mixing and reaction of fluids in micro-reactor |
| 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 |
| CN109810024A (en) * | 2019-03-28 | 2019-05-28 | 南京工业大学 | A kind of spray circuits reactor being used to prepare penta diisocyanate and its application method |
| CN111957260A (en) * | 2020-09-08 | 2020-11-20 | 泰安科赛尔化学科技有限公司 | Thiophene production mixer and production mixer assembly thereof |
| CN114685315A (en) * | 2022-05-09 | 2022-07-01 | 山东新和成精化科技有限公司 | Preparation method and device of isocyanate |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN105617957A (en) * | 2014-10-27 | 2016-06-01 | 中国科学院大连化学物理研究所 | Method for strengthening mixing and reaction of fluids in micro-reactor |
| CN105617957B (en) * | 2014-10-27 | 2018-03-20 | 中国科学院大连化学物理研究所 | A kind of method of fluid mixing and reaction in reinforcing microreactor |
| CN104874335A (en) * | 2015-05-14 | 2015-09-02 | 万华化学集团股份有限公司 | Reactor for preparing isocyanate and method of reactor for preparing isocyanate |
| CN105032307A (en) * | 2015-07-21 | 2015-11-11 | 万华化学集团股份有限公司 | Dynamic self-cleaning reactor and method for preparing isocyanate |
| 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 |
| CN109810024A (en) * | 2019-03-28 | 2019-05-28 | 南京工业大学 | A kind of spray circuits reactor being used to prepare penta diisocyanate and its application method |
| CN111957260A (en) * | 2020-09-08 | 2020-11-20 | 泰安科赛尔化学科技有限公司 | Thiophene production mixer and production mixer assembly thereof |
| CN114685315A (en) * | 2022-05-09 | 2022-07-01 | 山东新和成精化科技有限公司 | Preparation method and device of isocyanate |
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