CN205170713U - Adopt device of liquid SO3 sulphonate production leather fatting agent - Google Patents
Adopt device of liquid SO3 sulphonate production leather fatting agent Download PDFInfo
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- CN205170713U CN205170713U CN201520859257.2U CN201520859257U CN205170713U CN 205170713 U CN205170713 U CN 205170713U CN 201520859257 U CN201520859257 U CN 201520859257U CN 205170713 U CN205170713 U CN 205170713U
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- CN
- China
- Prior art keywords
- pipeline
- liquid
- vacuum ejector
- evaporating pot
- sulfonation
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Abstract
The utility model relates to an adopt device of liquid SO3 sulphonate production leather fatting agent. The purpose is that the device that provides has that the facility request is not high, stable characteristics simply, are easily maintained and move in the installation. Technical scheme is: an adopt device of liquid SO3 sulphonate production leather fatting agent which characterized in that the device includes: by the centrifugal pump carry and vacuum ejector through pipeline input animals and plants grease, through the pipeline connect gradually the homogeneity pump of vacuum ejector export and heat exchanger and through second pipeline input liquid SO3 and through first pipeline intercommunication vacuum ejector induction port with the gaseous SO3 evaporating pot of output SO3, the heat exchanger export is through third pipeline intercommunication centrifugal pump entry the time, switch -on output material is in order to make the pipeline that further reacts again.
Description
Technical field
The utility model relates to chemical field, is specially a kind of employing liquid SO
3the device of sulfonation production leather fat.
Background technology
Leather fat can give leather good to moisten, to fill, the performance such as plentiful, soft and for shelf-stable, be the key element in leather production, leather quality and use properties played a decisive role.Current conventional leather fat product mainly contains sulphonated oil, is generally to obtain by carrying out sulfonation processing to animal-plant oil.Existing comparatively ripe process for sulfonation generally adopts gas phase SO
3process for sulfonation, mainly comprises SO
3generation systems, sulfonation system, exhaust treatment system.
Existing conventional SO
3generation systems technique mainly contains combustion sulphur method and liquid SO
3method of evaporation.Combustion sulphur method refers to that sulfur burning obtains SO
2be catalytically converted into sulphur trioxide through catalyst again, period is mixed into a large amount of dry air and finally obtains the dense sulfur trioxide gas about 2-5% of gas for sulfonation; Liquid SO
3method of evaporation adopts existing liquid SO
3, sulfan in vaporizer after direct heating evaporation, then is diluted to the dense sulfur trioxide gas for 2-5% of gas with dry air.These two kinds of methods all need to use a large amount of dry air, and equipment is complicated, and energy consumption is large.Conventional sulfonation system generally adopts film sulfonator, organic material is formed liquid film and SO
3gas directly contacts and reacts, and equipment requirements is higher, and quality of forming film and gas diffusion velocity will directly affect sulfonation quality.In addition owing to introducing large quantity of air, after sulfonation reaction, these air can entrainment portions organic material drop and part unreacted SO
3, therefore need exhaust treatment system; Because air quantity is comparatively large, cause exhaust treatment system pressure comparatively large, generally can produce more electrostatic demist nigrotic acid, environmental benefit is poor.
Use liquid SO
3directly contact with animal-plant oil and carry out sulfonation reaction; Due to liquid SO
3molecular structure is Trimeric structures, directly contacts with animal-plant oil and can produce excessive sulfonation, cause grease carbonization blackening even coking phenomenon.Also have and use solvent method to utilize solvent cut grease to reduce liquid SO
3contact to control sulfonation degree with grease, but also face the problems such as solvent treatment, environmental effect is poor.
Utility model content
The purpose of this utility model overcomes the deficiency in above-mentioned background technology, provides a kind of and adopt liquid SO
3the method of sulfonation production leather fat and device thereof.This device have equipment requirements not high, install simple and easy, for ease of maintenaince and stable feature.
The technical scheme that the utility model provides is:
A kind of employing liquid SO
3the device of sulfonation production leather fat, is characterized in that this device comprises:
To be carried by impeller pump and by the vacuum ejector of pipeline input animal-plant oil, the Homogenizing pump being connected in turn vacuum ejector outlet by pipeline and interchanger and by second pipe infusion fluid SO
3and by the first pipeline communication vacuum ejector suction opening to export SO
3the SO of gas
3evaporating pot, heat exchanger exit, by while the 3rd pipeline communication impeller pump entrance, connects again outputting material to make the pipeline of reaction further.
Described SO
3evaporating pot configuration heating unit, includes but not limited to spiral heater or jacketed type well heater.
Described SO
3evaporating pot also configures whipping appts, includes but not limited to mechanical stirrer or magnetic stirring apparatus.
Thinking of the present utility model is under utilizing vacuum, SO
3gaseous phase is close to the SO after drying Dilution air
3gaseous phase, coordinates vacuum ejector and Homogenizing pump to carry out Forced Mixing, there will not be directly utilize SO for sulfonation
3the oversulfonate phenomenon that liquid causes, the more conventional membrane-type sulfonation of sulfonation effect is more excellent.
For SO under vacuum
3extremely evaporable feature, at SO
3inside add part of sulfuric acid and make SO
3form oleum system in evaporating pot, make system gas phase SO needed for sulfonation
3steady-state evaporation can be realized under temperature (40 ~ 70 DEG C), certain vacuum (1-50kpa).As long as control vacuum tightness, gas phase SO in actual motion
3stablizing, along with liquid SO of temperature
3stablely to add, SO
3in evaporating pot, oleum system can reach equilibrium concentration rapidly automatically, the SO of maintenance
3steady-state evaporation.When in evaporating pot, oleum concentration is higher, make the corresponding decline of its boiling point, gas phase SO
3temperature and then declines, and causes evaporation to be accelerated, due to liquid SO
3add constant flow, oleum concentration can decline rapidly and reach target value; Otherwise when oleum concentration in evaporating pot is on the low side also can corresponding automatic adjustment, finally make vacuum tightness, gas phase SO
3temperature, gas phase SO
3velocity of evaporation reaches process goal value.
The utility model compared with prior art, has following outstanding advantages and positively effect:
1) contrast conventional gas-phase process for sulfonation, eliminate the complicated complex appts such as dry gas generation, tail gas absorption, equipment is simple, energy consumption is low.
2) vacuum ejector is utilized to produce negative pressure of vacuum evaporation SO
3, obtain the SO under high vacuum
3gas, its state performance is close to the dense 2-5% gas phase SO of gas
3, can well avoid directly using liquid SO for sulfonation
3the oversulfonate problem that sulfonation causes, the sulfonated product color and luster obtained is good.
3) utilize vacuum ejector and Homogenizing pump to SO
3realize Forced Mixing with animal-plant oil, relatively traditional membrane-type sulfonation, sulfonation reaction is more stable, and product quality is better.
4) the utility model less investment, not high to equipment requirements, all devices configured is the matured product of outsourcing, installs simple and easy, and for ease of maintenaince, simultaneity factor is stable, is easy to control.
Accompanying drawing explanation
Fig. 1 is the apparatus structure schematic diagram of employing liquid SO3 sulfonation production leather fat described in the utility model.
Wherein 1 is animal-plant oil, and 2 is SO
3, 3 is transferpump, and 4 is SO
3evaporating pot, 5 is vacuum ejector, and 6 is Homogenizing pump, and 7 is interchanger, and 8 is sulphonate (sulfuric ester).
Embodiment
The use liquid SO that the utility model provides
3carry out the device of sulfonation, comprising:
1) animal-plant oil 1 is conducted through by transferpump 3 fluid intake that pipeline enters vacuum ejector 5, liquid SO
32 deliver into SO by second pipe
3evaporating pot 4, SO
3the SO of evaporation in evaporating pot
3gas enters vacuum ejector suction opening by the first pipeline simultaneously;
Described SO
3evaporating pot is configured with heating unit, and heating unit recommends spiral heater or jacketed type well heater;
Described SO
3evaporating pot is also configured with whipping appts, and whipping appts recommends mechanical stirrer or magnetic stirring apparatus;
2) vacuum ejector outlet connects Homogenizing pump 6, interchanger 7 successively by pipeline; In heat exchanger exit material, partial material is by the 3rd pipe section cyclically utilizing to transferpump entrance, and partial material 8 removes lower stepping single step reaction by Cemented filling.
Further illustrate below by way of specific embodiment.
Embodiment 1
The sulfonation of 1t/h rapeseed oil
SO
350L conventional belt coil pipe stirred autoclave selected by evaporating pot, adds the about 10L vitriol oil in advance.
Rapeseed oil enters vacuum ejector by the flow of 1t/h, liquid SO
3sO is entered by the flow of 55kg/h
3evaporating pot.After steady running, control interchanger Posterior circle reuse mass flow and make vacuum ejector form the vacuum of 40kpa, SO
3evaporating pot 55 DEG C, under 40kpa condition for the velocity-stabilization press 50kg/h evaporates SO
3(control weight by weight scale to maintain, SO
3evaporating pot is about 40%), material by vacuum ejector out after through by the further hybrid reaction of Homogenizing pump, the interchanger control temperature system that enters, to after 45 DEG C, neutralizes by the speed of about 1.05t/h and liquid caustic soda and obtains sulphonated oil product, the product obtained meets top grade product index, specific as follows:
| Project | Index |
| Outward appearance (25 DEG C) | Yellowish brown liquid |
| Binding capacity, % | 5.2 |
| Vitriol, % | 0.9 |
| Color and luster, Hazen (5% hexane solution) | 352 |
Embodiment 2
The palmitic sulfonation of 2t/h
SO
350L conventional belt coil pipe stirred autoclave selected by evaporating pot, adds the about 10L vitriol oil in advance.
Rapeseed oil enters vacuum ejector by the flow of 2t/h, liquid SO
3sO is entered by the flow of 120kg/h
3evaporating pot.After steady running, control interchanger Posterior circle reuse mass flow and make vacuum ejector form the vacuum of 45kpa, SO
3evaporating pot 60 DEG C, under 45kpa condition for the velocity-stabilization press 120kg/h evaporates SO
3(control weight by weight scale to maintain, SO
3evaporating pot is about 40%), material by vacuum ejector out after through by the further hybrid reaction of Homogenizing pump, the interchanger control temperature system that enters, to after 50 DEG C, neutralizes by the speed of about 2.1t/h and liquid caustic soda and obtains sulphonated oil product, the product obtained meets top grade product index, specific as follows:
| Project | Index |
| Outward appearance (25 DEG C) | Yellowish brown liquid |
| Binding capacity, % | 5.3 |
| Vitriol, % | 1.1 |
| Color and luster, Hazen (5% hexane solution) | 309 |
Embodiment 3
The sulfonation of 1t/h lard
SO
350L conventional belt coil pipe stirred autoclave selected by evaporating pot, adds the about 10L vitriol oil in advance.
Rapeseed oil enters vacuum ejector by the flow of 1t/h, liquid SO
3sO is entered by the flow of 60kg/h
3evaporating pot.After steady running, control interchanger Posterior circle reuse mass flow and make vacuum ejector form the vacuum of 45kpa, SO
3evaporating pot 55 DEG C, under 45kpa condition for the velocity-stabilization press 60kg/h evaporates SO
3(control weight by weight scale to maintain, SO
3evaporating pot is about 40%), material by vacuum ejector out after through by the further hybrid reaction of Homogenizing pump, the interchanger control temperature system that enters, to after 50 DEG C, neutralizes by the speed of about 1.1t/h and liquid caustic soda and obtains sulphonated oil product, the product obtained meets top grade product index, specific as follows:
| Project | Index |
| Outward appearance (25 DEG C) | Yellowish brown liquid |
| Binding capacity, % | 5.3 |
| Vitriol, % | 1.1 |
| Color and luster, Hazen (5% hexane solution) | 412 |
Claims (3)
1. one kind adopts liquid SO
3the device of sulfonation production leather fat, is characterized in that this device comprises:
Carried by impeller pump (3) and inputted the vacuum ejector (5) of animal-plant oil (1), the Homogenizing pump (6) being connected in turn vacuum ejector outlet by pipeline and interchanger (7) by pipeline and pass through second pipe infusion fluid SO
3(2) and by the first pipeline communication vacuum ejector suction opening to export SO
3the SO of gas
3evaporating pot (4), heat exchanger exit, by while the 3rd pipeline communication impeller pump entrance, connects again outputting material to make the pipeline of reaction further.
2. employing liquid SO according to claim 1
3the device of sulfonation production leather fat, is characterized in that: described SO
3the heating unit of evaporating pot configuration comprises spiral heater or jacketed type well heater.
3. employing liquid SO according to claim 2
3the device of sulfonation production leather fat, is characterized in that: described SO
3the whipping appts of evaporating pot configuration comprises mechanical stirrer or magnetic stirring apparatus.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201520859257.2U CN205170713U (en) | 2015-10-30 | 2015-10-30 | Adopt device of liquid SO3 sulphonate production leather fatting agent |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201520859257.2U CN205170713U (en) | 2015-10-30 | 2015-10-30 | Adopt device of liquid SO3 sulphonate production leather fatting agent |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN205170713U true CN205170713U (en) | 2016-04-20 |
Family
ID=55734728
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201520859257.2U Expired - Fee Related CN205170713U (en) | 2015-10-30 | 2015-10-30 | Adopt device of liquid SO3 sulphonate production leather fatting agent |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN205170713U (en) |
-
2015
- 2015-10-30 CN CN201520859257.2U patent/CN205170713U/en not_active Expired - Fee Related
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| C56 | Change in the name or address of the patentee | ||
| CP01 | Change in the name or title of a patent holder |
Address after: Hangzhou City, Zhejiang province 310009 City Shangcheng District No. 128 Lane Patentee after: Praise Technology Group Limited by Share Ltd Patentee after: Jiaxing Zanyu Technology Co., Ltd. Address before: Hangzhou City, Zhejiang province 310009 City Shangcheng District No. 128 Lane Patentee before: Zhejiang Zanyu Technology Co., Ltd. Patentee before: Jiaxing Zanyu Technology Co., Ltd. |
|
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20160420 Termination date: 20201030 |
|
| CF01 | Termination of patent right due to non-payment of annual fee |