CN2933552Y

CN2933552Y - Consecutive mixing heat-removing chemical technology production device

Info

Publication number: CN2933552Y
Application number: CN 200620078554
Authority: CN
Inventors: 宋晓轩
Original assignee: Individual
Current assignee: Individual
Priority date: 2006-03-08
Filing date: 2006-03-08
Publication date: 2007-08-15
Anticipated expiration: 2016-03-08

Abstract

The utility model provides a chemical manufacturing device which can continuously mix and remove heat, comprising a feed distributing pipe(5), a mixed reaction chamber consisting of a dynamic reaction chamber(10) and a static reaction distributor(16). The core elements of the dynamic reaction chamber(10) are a pair of meshed rotor(9) and stator(12) with the same number of slight cuts around. The static reaction distributor(16) comprises two or more parallel connected static reaction chambers(17) which are multilevel pole structures consisting different forms of mixed elements. The feed distributing pipe(5) is fixed in dynamic reaction chamber(10) in the axis direction. With a plurality of static reaction chambers parallel connected, this utility model can not only realizes faster and better reaction and heat removal, but also eliminates the pressure drop from the dynamic reaction chamber to the static reaction chamber. The device can be particularly used for exothermic reactions such as acid and alkali, nitration and reactions in which outgrowths can be produced without even heating.

Description

Thermalization worker process units is removed in a kind of continuous mixing

Technical field

It is the chemical production device of raw material with solution-air, liquid-liquid that the utility model relates to a kind of, is specially adapted to need fully to mix and efficiently remove the chemical reaction of heat.

Background technology

Raspberry ketone (4-(4-hydroxy phenyl)-3-butene-2 ketone) is a kind of spices with quiet and tastefully laid out fruital of at present domestic and international extensive use.Not only be used to prepare flavoring essence and daily essence in a large number, and also increasingly extensive at the consumption of medicine, agricultural chemicals and dye industry.

Raspberry ketone at present preferably production method be that hydrogenating reduction obtains through post processings such as decompression distillation and recrystallizations more then with parahydroxyben-zaldehyde and acetone condensation under the base catalyst effect.Domestic present manufacturing enterprise generally adopts enamel reaction still (accompanying drawing 1), and specific requirement is: the parahydroxyben-zaldehyde that mixes, acetone soln are joined sodium hydrate aqueous solution in the reactor 1 by liquid material import 2 under vigorous stirring gradually.Cooling fluid is entered by cooling feed tube 3, and the temperature rise that cooling drain pipe 4 flows out with the control reaction mass is no more than 30 ℃.But the problem that exists is: agitator speed can only reach about 130r/min, and mixed effect is relatively poor; In addition, for obtaining comparatively ideal results, and then stirring reaction 3-4h can access the yield more than 80% generally at 2-3h the time of hydro-oxidation sodium water solution in the production.But this moment, product was vermilion, also needed to add activated carbon decolorizing to light yellow.These have all prolonged treatment process and production cycle greatly.

The utility model content

It is the chemical production device of raw material with solution-air, liquid-liquid that the purpose of this utility model provides a kind of, is specially adapted to violent exothermic reaction.

The inventor once applied for one piece of device that is composed in series by dynamic response chamber and static reaction chamber, and the patent No. is ZL200520122535.2, pointed out in the patent, and gas, liquid material is by mixing in dynamic response chamber moment, and began reaction; Enter the static reaction chamber again and proceed reaction, by the pressure heat transfer effect in static reaction chamber, reaction heat is removed well, has reduced the generation of side reaction effectively.Thereby the quality of product and reaction efficiency are further improved, and help realizing successive reaction, be particularly suitable for suitability for industrialized production.But the inventor finds through further test, and at some stronger exothermic reaction or remove the higher reaction of heat request, single dynamic response chamber and static reaction chamber series system can not satisfy fully and react requirement.Therefore the inventor further proposes a kind of improved reaction unit on original patent basis.Specifically:

The utility model comprises a mixing and reaction chamber that is composed in series by charging distributor pipe 5, dynamic response chamber 10 and static reaction distributor 16, and wherein static reaction distributor 16 is composed in parallel by two or more static reactions chamber 17.

Dynamic response cell structure wherein is similar to present widely used pipeline high shear and disperses homogenizer (mulser), and the internal core element is a pair of intermeshing rotor and stator, the elongated cuts that change, the stator periphery all has equal number; The working chamber intermediate solid drive shaft adopts cantilevered, and power transmission shaft and motor are taked direct connection.When rotor high-speed rotates, produce very big centrifugal force, the material that is sucked by rotor axial is sprayed from the elongated cuts of rotor, form radially discharging.High tangential velocity and high frequency mechanical effect that high speed rotation by rotor is produced produce powerful kinetic energy, make that material is subjected in the limited space of stator and rotor that strong fluid power is sheared, comprehensive functions such as ion extruding and turbulent flow, and two-phase was evenly disperseed in moment; Rotor speed of the present utility model is not less than 200r/min, preferred 800～3000r/min.

Parallel is shown two or more static reactions chamber in the static reaction distributor.The multilayer column structure that each static reaction chamber is made up of multi-form hybrid element, its structure also is similar to the static mixer that uses on the market.Its principle be fluid circuit structure by the nothing of different structure machinery moving part with mixed material under the static pressure effect, by some construction units, repeatedly cut apart, compound, rotation, compression and expansion.Because fluid constantly changes flow direction in the static reaction chamber, improve the turbulent extent of fluid greatly, thereby reduced the thickness of laminar flow layer, reduce the thermal resistance of laminar flow layer, have heat-transfer effect preferably.Hybrid element wherein can have polytype, as corrugated plate type, single-screw type, double helical form, horizontal stripe type etc., is respectively SV type, SK type, SH type, SX type corresponding to the static mixer of commercialization.Wherein, preferred SK type, it is to be that two spiral metal sheets of 90 ° constitute a hybrid element unit by 90 ° of directions staggered linking by moment of torsion, and each cell cube becomes a cylinder by the certain orientation tandem compound, and the length of each unit is about 0.5～1 times of static reaction chamber caliber.Length/footpath, static reaction of the present utility model chamber is not more than 60, and material reaction flow velocity therein is not less than 0.01m/s.The caliber of reative cell can be determined according to material heat exchange requirement and operation flow velocity, be not more than 50mm usually.

The dynamic response chamber is axially arranged with the charging distributor pipe, guarantees that the axial feed inlet of the final driven attitude reative cell of all materials sucks.Set up gas feed tube inlet and liquid feed pipe inlet on the distributor pipe respectively, requirement according to reaction mass, can establish one or more gas feed tube inlets, or one or more liquid feed pipe inlet, feedstock direction the utility model of gas or liquid is not done special qualification.Undertaken by set charge ratio for guaranteeing to react, the utility model requires gas feed mouth of pipe pressure greater than the liquid feed pipe mouth pressure, and the liquid feed pipe mouth pressure should be greater than reacting product outlet pressure, and the pressure reduction between the three is 0.05～0.3MPa.

The outside, mixing and reaction chamber has cooling jacket, is used for the cooling of dynamic response chamber and static reaction chamber.This cooling jacket can be the cooling structure of integral type, also can adopt dynamic response chamber and the independent respectively form of cooling off of static reaction distributor, its chuck heat transfer carrier temperature≤-20 ℃.

Static reaction distributor pipe of the present utility model has adopted the mode of a plurality of static reactions chamber parallel connection, and it is faster, effective not only to make reaction and reaction remove heat, and has eliminated the dynamic response chamber and fallen problem to the pressure of static reaction chamber.Therefore the reaction that is particularly suitable for soda acid, very exothermic reaction such as nitrated and under the irregular state that is heated, easily generates accessory substance.

Figure of description

The structural representation of enamel reaction still in Fig. 1 prior art

Fig. 2 structural representation of the present utility model

The A-A cross-sectional view of Fig. 3 the utility model material feeding tube

The B-B generalized section of Fig. 4 the utility model static reaction distributor

The specific embodiment

Adopt the synthetic 4-(4-hydroxy phenyl) of the device-3-butene-2 ketone of the utility model (accompanying drawing 2).

Mode shown in the accompanying drawing 3 is adopted in the charging of material.With measuring pump charge ratio in accordance with regulations, liquid feed pipe inlet 6,7 on charging distributor pipe 5 is squeezed into dynamic response chamber inlet 8 with acetone and parahydroxyben-zaldehyde respectively, simultaneously, with another measuring pump will be both quantitative, and concentration is that 11% NaOH is squeezed into dynamic response chamber inlet 8 through liquid feed pipe inlet 2.

In dynamic response chamber 10, power transmission shaft 14 is direct-connected with motor, drives rotor 9 and rotates, and rotating speed is 2200rpm.For guaranteeing that reactant is fast by outlet each static reaction chambers 17 that enter in the static reaction distributor pipe 16 15, dynamic response chamber, be total to parallel in the distributor pipe 16 and show 40 static reaction chambers 17, every caliber is Ф 15mm, pipe range 300mm, hybrid element 18 models in the static reaction chamber 17 are SK type (Qidong blender factory), hydraulic diameter 7.5mm.The caliber of distributor pipe 16 is Ф 400mm, pipe range 300mm.

Concrete building-up process is: the rotor 9 in the dynamic response chamber 10 rotates down, and material is mixed by moment between stator 12 rotors 9, ejection from otch 13; Each static reaction chambers 17 that flowed in the static reaction distributors 16 by dynamic response chamber outlet 15 subsequently, through a plurality of hybrid elements 18 hybrid reactions in the reative cell 17 and remove heat, the final reaction product flows out through reaction outlet 19.

The mixing and reaction chamber adopts the integral type chuck to cool off.Cooling jacket 11 interior 10 ℃ of mobile ethylene glycol antifreezes are flowed into by import 3, are flowed out by outlet 4, and reaction heat is withdrawn by ethylene glycol antifreeze, and the temperature of ethylene glycol rises to 25 ℃ by 10 ℃ gradually in preceding 20min, after tend to be steady.Whole materials of proportioning finish at the 30min internal reaction in accordance with regulations.

Compare with former reactor (accompanying drawing 1), use this device to add the aqueous slkali time and be reduced in the 0.5hr by 3hr; No longer continue reaction 6hr.Former reactor causes reacting inhomogeneous because of mixing speed slow (130r/min), and product is peony; After using this device, product is shallow vermilion, no longer uses activated carbon decolorizing.And yield can improve 10%.

Claims

1. continuous heat of mixing chemical production device, it is characterized in that comprising a mixing and reaction chamber that is composed in series by charging distributor pipe (5), dynamic response chamber (10) and static reaction distributor (16), dynamic response chamber (10) internal core element wherein is a pair of intermeshing rotor (9) and stator (12), the elongated cuts (13) that change, the stator periphery all has equal number; Static reaction distributor (16) is composed in parallel by two or more static reactions chamber (17), the multilayer column structure that each static reaction chamber (17) is made up of multi-form hybrid element, hybrid element can be corrugated plate type, single-screw type, double helical form, horizontal stripe type; Dynamic response chamber (10) is axially arranged with charging distributor pipe (5), sets up one or more gas feed tube inlets (2) and liquid feed pipe inlet (6,7) on the distributor pipe (5) respectively.

2. thermalization worker process units is removed in continuous mixing according to claim 1, it is characterized in that rotor (9) rotating speed 800～3000r/min in the dynamic response chamber (10).

3. thermalization worker process units is removed in continuous mixing according to claim 1, the hybrid element that it is characterized in that each the static reaction chamber (17) in the static distribution device (16) is that two spiral metal sheets of 90 ° are formed by the staggered linking of 90 ° of directions by moment of torsion, and each hybrid element length is about 0.5～1 times of static reaction chamber caliber.

4. thermalization worker process units is removed in continuous mixing according to claim 3, it is characterized in that the caliber of each the static reaction chamber (17) in the static distribution device (16) is not more than 50mm.

5. thermalization worker process units is removed in continuous mixing according to claim 1, it is characterized in that being positioned at gas feed pipe (2) mouth of pipe pressure on the charging distributor pipe (5) of dynamic response chamber (10) axial location greater than liquid feed pipe (6,7) mouth of pipe pressure, the liquid feed pipe mouth pressure is greater than reacting product outlet pressure, and the pressure reduction between the three is 0.05～0.3MPa.

6. thermalization worker process units is removed in continuous mixing according to claim 1, it is characterized in that comprising that an outside, mixing and reaction chamber that is composed in series by charging distributor pipe (5), dynamic response chamber (10) and static reaction distributor (16) has cooling jacket (11), cooling jacket is the cooling structure of integral type, or adopt dynamic response chamber and the independent respectively form of cooling off of static reaction distributor, its chuck heat transfer carrier temperature is not more than-20 ℃.