CN1542008A - Suspension catalyst distillation process for epoxidizing alkene directly - Google Patents
Suspension catalyst distillation process for epoxidizing alkene directly Download PDFInfo
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Abstract
The suspended catalytic distillation process of epoxidizing olefin directly includes the simultaneous entering the reaction of catalytic distilling tower of powdered Ti-Si molecular sieve catalyst, solvent, hydrogen peroxide and olefin; simultaneous flow and reaction of catalyst and liquid material mixture inside the tower; separation of solvent from the easy-to-gasify material for reuse; separation of un-gasified material from the catalyst before the catalyst returns to the reaction section; separation of un-reacted olefin from tower top of reactor material for reuse; and obtaining epoxidized product via separating tower top of reactor material. The said process has reaction and separation completed in the same tower, direct application of great amount of reaction heat in evaporating and separating residual reactant and solvent resulting in high reaction heat utilization and lowered power consumption; less side reactions, high selectivity of epoxidized product and other advantages.
Description
Technical field
The present invention relates to the method that the direct epoxidation of a kind of alkene prepares epoxy compounds.More particularly, the invention relates to the epoxidation reaction that alkene and hydrogen peroxide take place and carry out fractionation by distillation simultaneously under the katalysis of fine particle HTS, highly selective generates the method for organic epoxide.
Background technology
Traditional olefin epoxidation process has gas molecule in space oxygen oxidation style, conjugated oxidation and chlorine water oxidation style.What the application of gas molecule in space oxygen oxidation style was the most successful is the production of oxyethane, is that the direct epoxidation of catalyst ethene and oxygen generates oxyethane with silver, and production process is pollution-free substantially, and the Technological Economy advanced person.Conjugated oxidation successfully is used for producing propylene oxide at present, this technology has solved the chlorine water oxidation style substantially and has produced equipment corrosion and the problem of environmental pollution that propylene oxide brings, but technical process complexity, Technological Economy often is difficult to obtain good economic benefit because of the restriction of co-product purposes and market capacity.The chlorine water oxidation style is widely used for producing propylene oxide and epoxy chloropropane at present, owing to use chlorine water as reaction raw materials, thereby by product is many, the material consumption height, energy consumption is big, and equipment corrosion is serious, and three wastes discharge amount is big, and environmental protection pressure is big.
In order to solve the problem that existing epoxide industrial production technology exists, US4833260 discloses a kind of new epoxidizing method as far back as the eighties in 20th century, this method is catalyzer with the HTS, directly alkene is carried out epoxidation with hydrogen peroxide and produces epoxide.Because have strong polar compound such as water or alcohol in the reaction system, the catalysis ring-opening reaction will partly take place in the epoxide of generation, reduce the yield of epoxide.For this reason, US4824976, US5646314, US5675026 disclose the assist measure of some raising epoxide yields.Yet because catalyst Ti-si molecular sieves is a solid in this reaction system, alkene need be dissolved in simultaneously in a kind of solvent with hydrogen peroxide and contact with catalyzer with liquid form, could guarantee to react to carry out fast.In addition, this class exothermic heat of reaction is big, and heat-obtaining is untimely, easy temperature runaway, the invalid rate of decomposition of increase hydrogen peroxide.For control reaction temperature effectively, raise the efficiency, the exploitation of chemical reaction engineering technology has obtained attention.
EP0659473 is disclosed to be a kind of trickle-bed reactor, and catalyzer divides four sections to be filled in the trickle-bed reactor with oarse-grained form, intersegmental riser and the liquid collecting plate of being provided with, and first three section of lathe bed is the main reaction section, indirect cooler of every section peripheral hardware is with heat-obtaining.Epoxidation reaction with propylene is an example, under the reaction pressure more than the 1.25MPa, the mode that reaction mass is gas-liquid two-phase and stream is flowed downward and is reacted by the bed top, on the main reaction section, reaction mixture is carried out extraction, heat exchange, returned and replenish reinforced process, be that the reacted reactant of each section is after an indirect cooler cooling, a part loops back this section, and another part and fresh feed are mixed into next section.In order to improve the transformation efficiency of hydrogen peroxide, the feed liquid that enters the 4th section does not add fresh feed, product and tail gas by bed at the bottom of extraction.This reactor structure complexity, the reaction pressure height, temperature is controlled and is relied on the realization of systemic circulation material, need also after reaction finishes that solvent is evaporated separation and recycle with realization, so energy consumption is very high.
Summary of the invention
The purpose of this invention is to provide a kind of under the katalysis of powdery HTS, alkene and hydrogen peroxide are dissolved in a kind of solvent, with epoxidation reaction of olefines with separate the same equipment that places, highly selective generates the suspension catalytic distillation technology method of organic epoxide.
Method provided by the invention mainly is to carry out in a catalytic distillation tower that is made of conversion zone, distilling period and/or stripping section, and distilling period is positioned at the top of conversion zone, and stripping section is positioned at the below of conversion zone.
Method provided by the invention comprises:
Powdery titanium-silicon molecular sieve catalyst, solvent, hydrogen peroxide and alkene enter the conversion zone of catalytic distillation tower, the mixture of catalyzer and liquid material mobile material of catalysis simultaneously in tower reacts, use from the solvent cycle that the feed separation of easy vaporization goes out, Qi Hua liquid material and catalyzer be not after separating, the gained catalyst recirculation is returned conversion zone and is used, separate the unreacting olefin that obtains and recycle from cat head or tower still material, epoxide product obtains through separation from cat head or tower still material.
The present invention will react with separating to be placed in the same tower and carry out, and a large amount of reaction heat are directly used in evaporation and separate remaining reactants and solvent, utilization of Heat of Reaction rate height, and energy consumption reduces greatly; Suppress the side reaction that product takes place effectively, improved the selectivity of epoxide; Catalyzer adds or is convenient to remove, does not need to stop work; Prevented the hydrogen peroxide thermolysis effectively, hydrogen peroxide utilization ratio height.
Description of drawings
Fig. 1 is that boiling point is low, be the epoxidation principle process synoptic diagram of the alkene of gas under the normal temperature.
Fig. 2 is to be liquid but its boiling point is lower than the alkene epoxidation principle process synoptic diagram of temperature of reaction under the normal temperature.
Fig. 3 is the alkene epoxidation principle process synoptic diagram that boiling point is higher than temperature of reaction.
Embodiment
Method provided by the invention mainly is to carry out in a catalytic distillation tower that is made of conversion zone, distilling period and/or stripping section, and wherein distilling period is positioned at the top of conversion zone, and stripping section is positioned at the below of conversion zone.The catalytic distillation tower that three kinds of structures more particularly, are arranged: (1), be followed successively by distilling period, conversion zone, stripping section from top to bottom; (2), be followed successively by distilling period, conversion zone from top to bottom; (3), be followed successively by conversion zone, stripping section from top to bottom.This tower can be established three sections by the requirement of concrete reaction, and promptly distilling period, conversion zone and stripping section also can be established two sections, i.e. distilling period and conversion zone, or conversion zone and stripping section.
Method provided by the invention comprises:
Powdery titanium-silicon molecular sieve catalyst, solvent, hydrogen peroxide and alkene enter the conversion zone of tower, the mixture of catalyzer and liquid material mobile material of catalysis simultaneously in tower reacts, use from the solvent cycle that the feed separation of easy vaporization goes out, Qi Hua liquid material and catalyzer be not after separating, the gained catalyst recirculation is returned conversion zone and is used, separate the unreacting olefin that obtains and recycle from cat head or tower still material, epoxide product obtains through separation from cat head or tower still material.
Suspension catalytic distillation technology method provided by the invention is a kind of new catalytic distil process between common homogeneous reaction distillation and heterogeneous catalysis distillation.Described catalytic distillation tower and common distillation tower are identical, need not particular design, manufacturing.They can be packing tower, sieve-tray tower, valve tray column of various types etc.Conversion zone, distilling period and stripping section can adopt dissimilar towers to make up.In order to prevent to stop up, preferred sieve-tray tower or packing tower.If the employing packing tower, filler should be greater than 1000 with the catalyst particle size ratio, and the voidage of filler should be between 40～80%.The stage number of distilling period, conversion zone and stripping section or packed height are with system, the catalyst activity height of reaction, decide transformation efficiency and isolating requirement.
HTS of the present invention is the general name that titanium atom replaces a class zeolite of a part of Siliciumatom in the lattice framework.This class material is well known in the prior art, as has a titanium-containing zeolite of the MFI topological framework that is similar to the ZSM-5 aluminosilicate zeolite, be TS-1, have a titanium-containing zeolite of the MEL topological framework that is similar to the ZSM-11 aluminosilicate zeolite, be TS-2 and have and the molecular sieve containing titanium of mordenite, ZSM-12, MCM-41 and ZSM-48 isomorphous skeleton structure etc. wherein preferred TS-1 and TS-2.The used catalyzer of the present invention can be that the former powder of these zeolites directly uses, and also can be used behind spray shaping by the former powder of these zeolites.The used tackiness agent of spray shaping is generally selected non-acid colloidal sol for use, these colloidal sols can be selected from a kind of in titanium dioxide, silicon-dioxide, aluminum oxide and silica-alumina, the silica-titania etc., also can select some non-acid clays for use, if you would take off stone, kaolin, wilkinite and sepiolite, the content of molecular sieve is 5～80% preferred 15～60% in the catalyzer of spray shaping.The granular size of catalyzer should be able to guarantee that it can be evenly dispersed in the liquid material under suitable stirring, can continuous flow in tower and can not block up tower; But the granularity of catalyzer can not be meticulous, and meticulous catalyzer can increase the separating difficulty of catalyzer and material.The catalyst grain size scope is preferred 0.5～600 μ m of 0.2～800 μ m.
Alkene of the present invention can be selected from alkene, cycloolefin, haloolefin and a polyene hydrocarbon etc.; Preferably contain alkene, cycloolefin and the haloolefin of 3～12 carbon atoms, be more preferably propylene, propenyl chloride.These reactants can be pure product, also can contain the material that some do not have a negative impact to epoxidation reaction and product separation.
Hydrogen peroxide of the present invention can be pure product, but considers that from security standpoint and economic angle preferably use the aqueous solution of hydrogen peroxide, its concentration is 5%～90% preferred 10%～60%.
Solvent of the present invention is selected from alcohol, ketone, ester, preferably contains the ketone of pure and mild 3～5 carbon atoms of 1～4 carbon atom, is more preferably methyl alcohol, ethanol, propyl alcohol, butanols, acetone and methylethylketone etc.These solvents also have evaporation heat-obtaining function except that having the pointed dissolving function of prior art, thereby reach the purpose of control reaction temperature.
Liquid material separates with catalyzer, can adopt various liquid-solid isolation technique, as centrifugal, membrane filtration, sedimentation, spinning liquid and evaporation etc.
By method provided by the invention, the operational variable that alkene suspension catalytic distillation tower relates to comprises reaction pressure, temperature, catalyst concentration, trim the top of column amount etc.In general, absolute reaction pressure is the preferred 0.1MPa～1.0MPa of 0.1MPa～2.0MPa; Service temperature is 40 ℃～100 ℃ preferred 60 ℃～90 ℃; Catalyst concn is the heavy % in 0.5 heavy %～30 heavy % preferred 1 heavy %～15 of solvent, and the alkene mass space velocity is 0.01h
-1～10h
-1Preferred 0.1h
-1～8h
-1, in the charging mol ratio of alkene and hydrogen peroxide be 1.5: 1～10: 1 preferred 2: 1～6: 1.In order to guarantee that alkene, hydrogen peroxide can dissolvings mutually in the presence of solvent, in the conversion zone mol ratio of alkene and solvent be 1: 5～1: 30 preferred 1: 8～1: 20.The trim the top of column ratio be 1: 1～30: 1 preferred 5: 1～20: 1.
Be three kinds of embodiments of example explanation with a kind of catalytic distillation tower that is followed successively by distilling period, conversion zone, stripping section from top to bottom below, but the present invention is not limited to this three kinds of embodiments.
Embodiment one:
Powdery solid titanium-silicon molecular sieve catalyst and solvent add the catalyzer basin, mix the back and enter in the tower, in the decline process, also react with divide one or more alkene counter current contact that enters tower from the conversion zone hypomere with the top of hydrogen peroxide from the conversion zone of tower.The epoxide that reaction generates, the remaining alkene of reaction and partial solvent enter gas-liquid separator through distilling period and condenser after being reacted the liberated heat vaporization, and unreacted gas alkene recycles after removing oxygen.The liquid that comes out from gas-liquid separator enters distillation tower, and cat head goes out the thick product of epoxide, goes out solvent at the bottom of the tower, and a part is back in the tower through tundish, and another part removes the catalyzer tundish as thinner.Partial solvent, water, minor by-products and catalyzer enter stripping section, solvent is suggested and enters conversion zone, other material enters catalyst separator through the tower still, isolated catalyzer enters the catalyzer tundish and is transported to the catalyzer basin and recycles after dilution, and the liquid material that catalyst separator is told enters the post-treatment operation.The required heat of tower still and stripping section is provided by reboiler.
Embodiment two:
Powdery solid titanium-silicon molecular sieve catalyst and solvent enter the catalyzer basin, enter in the tower with the top of hydrogen peroxide from the conversion zone of tower behind thorough mixing, one or more enters the alkene counter current contact and the reaction of tower in the decline process and from the conversion zone lower section.React remaining alkene and solvent and reacted the liberated heat vaporization, through distilling period and condenser, enter gas-liquid separator, the non-condensable gas emptying of telling, liquid enters distillation tower, and cat head goes out unreacted alkene, recycle, a solvent part that goes out at the bottom of the tower is removed the catalyzer tundish as thinner, and another part is back in the tower through tundish.Be advanced into stripping section under the material that conversion zone is not vaporized, propose whole alkene and solvent and enter conversion zone, do not carry and heat up in a steamer thing and enter catalyst separator, tell catalyzer and enter the catalyzer tundish, after dilution, be transported to the catalyzer basin and recycle through the tower still; The liquid crude product of telling from catalyst separator enters the following process operation.The required heat of tower still and stripping section is provided by reboiler.
Embodiment three:
Powdery solid titanium-silicon molecular sieve catalyst and solvent enter the catalyzer basin, enter in the tower with the top of hydrogen peroxide from the conversion zone of tower behind thorough mixing; Meanwhile, alkene divides one or more top from conversion zone to enter in the tower, and contacts with catalyzer and to react.Be advanced into distilling period on the material of being vaporized by reaction heat, wherein alkene is got back to conversion zone through fractionation, and solvent vapo(u)r enters gas-liquid separator after condenser condenses, the non-condensable gas emptying of telling, a liquid solvent part is back in the tower through tundish, and another part removes the catalyzer tundish as thinner.Be advanced into stripping section under the material that conversion zone is not vaporized, propose whole solvents and get back to conversion zone, do not carry and heat up in a steamer thing and enter catalyst separator, tell catalyzer and enter the catalyzer tundish, after dilution, be transported to the catalyzer basin and recycle through the tower still; The liquid material that catalyst separator is told enters distillation tower, and cat head goes out the alkene recycle, goes out crude product at the bottom of the tower and enters the post-treatment operation.The required heat of tower still and stripping section is provided by reboiler.
Below in conjunction with accompanying drawing method provided by the present invention is further detailed, but does not limit the present invention.Catalytic distillation tower in the accompanying drawing is followed successively by distilling period 3, conversion zone 2, stripping section 8 from top to bottom.
Fig. 1 is that boiling point is low, be the epoxidation principle process synoptic diagram of the alkene of gas under the normal temperature.
The principle process of this scheme is as follows:
Powdery solid titanium-silicon molecular sieve catalyst and solvent add catalyzer basin 1 through pipeline 11 and 12 respectively, mix after pipeline 13 enters in the tower through the top of pipeline 15 from the conversion zone 2 of tower with the hydrogen peroxide from pipeline 14, in the decline process with from the conversion zone hypomere, also react through 16 fens one or more alkene counter current contact that enter tower of pipeline.After the epoxide that reaction generates, the remaining alkene of reaction and partial solvent are reacted the liberated heat vaporization, enter gas-liquid separator 5 through distilling period 3, pipeline 17, condenser 4, pipeline 18 successively, unreacted gas alkene through removing oxygen after pipeline 19 is drawn recycles.The liquid that comes out from gas-liquid separator 5 enters distillation tower 6 through pipeline 20, the thick product of epoxide at distillation tower 6 tops is through pipeline 21 caterpillars, the solvent of distillation tower 6 bottoms is divided into two portions, wherein a part is back in the tower through pipeline 22, tundish 7, pipeline 24 successively, and another part then removes catalyzer tundish 12 as thinner through pipeline 23.
Partial solvent, water, minor by-products and catalyzer autoreaction section 2 enter stripping section 8, solvent is suggested and enters conversion zone, other material then enters catalyst separator 11 through tower still 9, pipeline 25 successively, isolated catalyzer enters catalyzer tundish 12 through pipeline 29, behind solvent cut from pipeline 23, be transported to catalyzer basin 1 through pipeline 30 and recycle, the liquid material that catalyst separator 11 is told then enters the following process operation through pipeline 28.The required heat of tower still and stripping section is provided by the material through pipeline 26, reboiler 10, pipeline 27 successively.
Fig. 2 is to be liquid but its boiling point is lower than the alkene epoxidation principle process synoptic diagram of temperature of reaction under the normal temperature.
The principle process of this scheme is as follows:
Powdery solid titanium-silicon molecular sieve catalyst and solvent enter catalyzer basin 1 through pipeline 11 and 12 respectively, mix after pipeline 13 enters in the tower through the top of pipeline 15 from the conversion zone 2 of tower with the hydrogen peroxide from pipeline 14, in the decline process with from the conversion zone hypomere, also react through 16 fens one or more alkene counter current contact that enter tower of pipeline.React after remaining alkene and partial solvent reacted liberated heat vaporization, enter gas-liquid separator 5 through distilling period 3, pipeline 17, condenser 4, pipeline 18 successively, the non-condensable gas of telling is through pipeline 31 emptyings, the liquid that comes out from gas-liquid separator 5 enters distillation tower 6 through pipeline 20, the unreacted gas alkene in distillation tower 6 tops through removing oxygen after pipeline 19 is drawn recycles.The solvent of distillation tower 6 bottoms is divided into two portions, and wherein a part is back in the tower through pipeline 22, tundish 7, pipeline 24 successively, and another part then removes catalyzer tundish 12 as thinner through pipeline 23.
Be advanced into stripping section 8 under the material that conversion zone 2 is not vaporized, propose whole alkene and solvent and enter conversion zone 2, do not carry and heat up in a steamer thing and then enter catalyst separator 11 through tower still 9, pipeline 25 successively, isolated catalyzer enters catalyzer tundish 12 through pipeline 29, behind solvent cut, be transported to catalyzer basin 1 through pipeline 30 and recycle from pipeline 23; The liquid crude product of telling from catalyst separator 11 enters the following process operation through pipeline 32.The required heat of tower still and stripping section is provided by the material through pipeline 26, reboiler 10, pipeline 27 successively.
Fig. 3 is the alkene epoxidation principle process synoptic diagram that boiling point is higher than temperature of reaction.
The principle process of this scheme is as follows:
Powdery solid titanium-silicon molecular sieve catalyst and solvent enter catalyzer basin 1 through pipeline 11 and 12 respectively, mix after pipeline 13 enters in the tower through the top of pipeline 15 from the conversion zone 2 of tower with the hydrogen peroxide from pipeline 14, meanwhile, alkene divides one or more to enter in the tower through the top of pipeline 16 from conversion zone 2, and contacts with catalyzer and to react.Be advanced into distilling period 3 on the material of being vaporized by reaction heat, wherein alkene is got back to conversion zone 2 through fractionation, solvent vapo(u)r enters gas-liquid separator 5 through distilling period 3, pipeline 17, condenser 4, pipeline 18 successively, the non-condensable gas of telling is through pipeline 31 emptyings, the liquid solvent of drawing through pipeline 20 is divided into two portions, wherein a part is back in the tower through pipeline 22, tundish 7, pipeline 24 successively, and another part then removes catalyzer tundish 12 as thinner through pipeline 23.
Be advanced into stripping section 8 under the material that conversion zone 2 is not vaporized, propose whole alkene and solvent and enter conversion zone 2, do not carry and heat up in a steamer thing and then enter catalyst separator 11 through tower still 9, pipeline 25 successively, isolated catalyzer enters catalyzer tundish 12 through pipeline 29, behind solvent cut, be transported to catalyzer basin 1 through pipeline 30 and recycle from pipeline 23; The liquid material of telling from catalyst separator 11 enters distillation tower 34 through pipeline 33, and the alkene at distillation tower 34 tops is drawn through pipeline 35 and recycled, and the liquid crude product is then drawn through pipeline 36 and entered the following process operation.The required heat of tower still and stripping section is provided by the material through pipeline 26, reboiler 10, pipeline 27 successively.
Method provided by the invention is applicable to the direct epoxidation reaction of alkene, haloolefin and other alkene, is specially adapted to the direct epoxidation reaction of propylene or propenyl chloride and hydrogen peroxide.The advantage of this processing method is in particular in:
(1) adopts the direct epoxidation of hydrogen peroxide, fundamentally solved heavy corrosion and pollution problem that chlorohydrination technology exists;
(2) because the epoxide that reaction generates has in time shifted out reaction zone, suppressed the side reaction that product takes place effectively, improved the selectivity of epoxide;
(3) catalyzer adds or is convenient to remove, does not need to stop work;
(4) adopt the solvent evaporation heat-obtaining, temperature of reaction control has steadily prevented the hydrogen peroxide thermolysis, hydrogen peroxide utilization ratio height effectively;
(5) reaction is carried out with separating to be coupling in the tower, and flow process is simple, reduces investment outlay;
(6) epoxidation process a large amount of reaction heat of emitting are directly used in evaporation and are separated remaining reactants and solvent, and utilization of Heat of Reaction rate height need special heat-obtaining facility, thereby device construction is simple, and the energy consumption of production process reduces greatly.
The following examples will give further instruction to present method, but therefore not limit present method.
The used catalyzer trade mark is HTS in the example, builds feldspar oiling worker limited-liability company by the Hunan and produces, and active ingredient is TS-1.
The definition of the transformation efficiency of hydrogen peroxide and epoxidised selectivity is in the example:
The transformation efficiency of hydrogen peroxide=[(n
0-n
r)/n
0] * 100%
The epoxidised selectivity of hydrogen peroxide=[n
E/ (n
0-n
r)] * 100%
Wherein, n
0The charging mole number of expression hydrogen peroxide, n
rThe remaining mole number of expression hydrogen peroxide, n
EExpression generates the mole number of epoxide.
The situation of present embodiment explanation propylone direct opoxidation system propylene oxide.
Fig. 1 operation is pressed in test, and reaction tower is a sieve-tray tower.Used catalyzer is HTS, and the granules of catalyst diameter Distribution is 1～200 μ m; Reaction raw materials is 27% industrial hydrogen peroxide and 99.9% above polymerization-grade industry propylene; Solvent is an analytical pure methyl alcohol.The preparation catalyst concn is 5% methanol slurry in the catalyzer basin, and abundant dispersed with stirring is with standby.Under the condition of setting, device is carried out trial trip with methyl alcohol, treat that device operates steadily after, catalyst slurry, hydrogen peroxide, propylene are added the conversion zone in the tower.Absolute reaction pressure is 0.12MPa, and the conversion zone temperature is 65 ℃, and the mol ratio of conversion zone propylene and methyl alcohol is 1: 12, and the propylene mass space velocity is 1.5h
-1, the methanol eddy ratio is 7: 1.The raw materials components mole ratio of propylene and hydrogen peroxide is 2: 1, the disposable adding apparatus of catalyzer and methyl alcohol, and closed cycle is used in device, and unreacted propylene is incorporated the fresh propylene pipeline into and is utilized.Reaction result: hydrogen peroxide conversion is 100%, and the epoxidised selectivity of hydrogen peroxide is 96.5%.
The situation of present embodiment explanation propylone direct opoxidation system propylene oxide.
Fig. 1 operation is pressed in test, and reaction tower is a sieve-tray tower.Used catalyzer is for being the HTS of binding agent spray shaping with the silicon sol, and the content of HTS is 30%, and granules of catalyst is distributed as 20～500 μ m; Reaction raw materials, solvent and other condition are with embodiment 1.Different is that catalyst concn is 12.5%, and absolute reaction pressure is 0.15MPa, and the conversion zone temperature is 75 ℃, propylene mass space velocity 6.0h
-1The methanol eddy ratio is 18: 1, and the mol ratio of propylene and methyl alcohol is 1: 15 in the conversion zone, and the raw materials components mole ratio of propylene and hydrogen peroxide is 4: 1, reaction result: hydrogen peroxide conversion is 99.5%, and the epoxidised selectivity of hydrogen peroxide is 95.5%.
The situation of the direct epoxidation system epoxy chloropropane of present embodiment explanation propenyl chloride.
Fig. 2 operation is pressed in test, and reaction tower is a packing tower, and the filler voidage is 73%.Used catalyzer is for being the HTS of binding agent spray shaping with aluminium colloidal sol, and the content of HTS is 40%, and the granules of catalyst mean diameter is 40～600 μ m; Reaction raw materials is industrial goods, and wherein the purity of hydrogen peroxide is 27%, and the purity of propenyl chloride is 96.5%; Solvent is an analytical pure methyl alcohol.The preparation catalyst concn is 8.5% methanol slurry in the catalyzer basin, and abundant dispersed with stirring is with standby.Under the condition of setting, device is carried out trial trip with methyl alcohol, treat that device operates steadily after, catalyst slurry, hydrogen peroxide, propenyl chloride are added the conversion zone in the tower.Absolute reaction pressure is 0.12MPa, and the conversion zone temperature is 65 ℃, and the mol ratio of conversion zone propenyl chloride and methyl alcohol is 1: 14, and the mol ratio of propenyl chloride and hydrogen peroxide charging is 3: 1, propenyl chloride mass space velocity 3h
-1, reflux ratio 6: 1.The disposable adding apparatus of catalyzer and methyl alcohol, closed cycle is used in device, and unreacted propenyl chloride is incorporated fresh propenyl chloride pipeline into and is utilized.Reaction result: hydrogen peroxide conversion is 100%, and the epoxidised selectivity of hydrogen peroxide is 94.9%.
The situation of the direct epoxidation system epoxy chloropropane of present embodiment explanation propenyl chloride.
Fig. 2 operation is pressed in test, and reaction tower is a sieve-tray tower.Used catalyzer is HTS, and the granules of catalyst mean diameter is 1～200 μ m.Reaction raw materials, solvent and other condition are with embodiment 3, and different is that catalyst concn is 3%, and absolute reaction pressure is 0.2MPa, and the conversion zone temperature is 80 ℃, propenyl chloride mass space velocity 2h
-1The methanol eddy ratio is 12: 1, and the mol ratio of propenyl chloride and methyl alcohol is 1: 10 in the conversion zone, and the raw materials components mole ratio of propenyl chloride and hydrogen peroxide is 3: 1.Reaction result: hydrogen peroxide conversion is 100%, and the epoxidised selectivity of hydrogen peroxide is 96.1%.
The direct epoxidation system 1 of present embodiment explanation tetrahydrobenzene, the situation of 2-epoxy cyclohexane.
Fig. 3 operation is pressed in test, and reaction tower is a sieve-tray tower.Used catalyzer is HTS, and the granules of catalyst mean diameter is 1～200 μ m.Reaction raw materials is industrial goods, and wherein the purity of hydrogen peroxide is 50%, and the purity of tetrahydrobenzene is 92.1%; Solvent is an analytical pure acetone.The preparation catalyst concn is 5% acetone slurry in the catalyzer basin, and abundant dispersed with stirring is with standby.Under the condition of setting, device is carried out trial trip with acetone, treat that device operates steadily after, catalyst slurry, hydrogen peroxide, tetrahydrobenzene are added the conversion zone in the tower.Absolute reaction pressure is 0.15MPa, and the conversion zone temperature is 75 ℃, and the mol ratio of conversion zone tetrahydrobenzene and acetone is 1: 14, and the mol ratio of tetrahydrobenzene and hydrogen peroxide charging is 5: 1, tetrahydrobenzene mass space velocity 2h
-1, reflux ratio 10: 1.The disposable adding apparatus of catalyzer and acetone, closed cycle is used in device, and unreacted tetrahydrobenzene is incorporated fresh tetrahydrobenzene pipeline into and is utilized.Reaction result: hydrogen peroxide conversion is 100%, and the epoxidised selectivity of hydrogen peroxide is 88.6%.
Claims (16)
1, the direct epoxidised suspension catalytic distillation technology method of a kind of alkene, it is characterized in that the powdery titanium-silicon molecular sieve catalyst, solvent, hydrogen peroxide and alkene enter the conversion zone of catalytic distillation tower, the mixture of catalyzer and liquid material mobile material of catalysis simultaneously in tower reacts, use from the solvent cycle that the feed separation of easy vaporization goes out, Qi Hua liquid material and catalyzer be not after separating, the gained catalyst recirculation is returned conversion zone and is used, separate the unreacting olefin that obtains and recycle from cat head or tower still material, epoxide product obtains through separation from cat head or tower still material.
2, according to the method for claim 1, it is characterized in that described catalytic distillation tower is made of conversion zone, distilling period and/or stripping section, wherein distilling period is positioned at the top of conversion zone, and stripping section is positioned at the below of conversion zone.
3,, it is characterized in that described alkene is alkene, cycloolefin, haloolefin or a polyene hydrocarbon according to the method for claim 1.
4,, it is characterized in that described alkene is alkene, cycloolefin or the haloolefin that contains 3～18 carbon atoms according to the method for claim 1 or 3.
5,, it is characterized in that described alkene is propylene, propenyl chloride according to the method for claim 1 or 3.
6,, it is characterized in that described solvent is alcohol, ketone, ester according to the method for claim 1.
7,, it is characterized in that described solvent is the alcohol that contains 1～4 carbon atom according to the method for claim 1 or 6.
8,, it is characterized in that described solvent is the ketone that contains 3～5 carbon atoms according to the method for claim 1 or 6.
9, according to the method for claim 1, the mol ratio that it is characterized in that alkene and hydrogen peroxide is 1.5: 1～10: 1.
10, according to the method for claim 1 or 9, the mol ratio that it is characterized in that alkene and hydrogen peroxide is 2: 1～6: 1.
11, according to the method for claim 1, the mol ratio that it is characterized in that conversion zone alkene and solvent is 1: 5～1: 30, and temperature of reaction is 40 ℃～100 ℃, and absolute reaction pressure is 0.1～2.0MPa, and the alkene mass space velocity is 0.05～10h
-1
12, according to the method for claim 1 or 10, the mol ratio that it is characterized in that conversion zone alkene and solvent is 1: 8～1: 20, and temperature of reaction is 60 ℃～90 ℃, and the reaction absolute pressure is 0.1～1.0MPa, and the alkene mass space velocity is 0.1～8h
-1
13,, it is characterized in that the catalyst grain size scope is 0.2～800 μ m according to the method for claim 1.
14,, it is characterized in that the catalyst grain size scope is 0.5～600 μ m according to the method for claim 1 or 13.
15,, it is characterized in that reacting section catalyst concentration is the heavy % in 0.5 heavy %～30 of solvent according to the method for claim 1.
16,, it is characterized in that reacting section catalyst concentration is the heavy % in 1 heavy %～15 of solvent according to the method for claim 1 or 15.
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