CN204490771U - A kind of α-naphthalenesulfonicacid continuous pressure hydrolysis device - Google Patents
A kind of α-naphthalenesulfonicacid continuous pressure hydrolysis device Download PDFInfo
- Publication number
- CN204490771U CN204490771U CN201520111498.9U CN201520111498U CN204490771U CN 204490771 U CN204490771 U CN 204490771U CN 201520111498 U CN201520111498 U CN 201520111498U CN 204490771 U CN204490771 U CN 204490771U
- Authority
- CN
- China
- Prior art keywords
- reaction pot
- hydrolytic reaction
- pot
- hydrolytic
- naphthalenesulfonicacid
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
Landscapes
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The α-naphthalenesulfonicacid continuous pressure hydrolysis device that the utility model provides, be applicable to continuous pressure hydrolysis α-naphthalenesulfonicacid, the continuous pressure hydrolysis device adopting the utility model to provide carries out the hydrolysis of sulfonation reaction mixed solution, in hydrolysate, the content of α-naphthalenesulfonicacid is 0.2 ~ 0.8%, the percent hydrolysis of α-naphthalenesulfonicacid is largely increased, effectively improve the purity of naphthalenes intermediate beta-naphthalenesulfonic-acid, reduce enterprise cost and drop into, realize the production requirement of energy-saving and emission-reduction, environmental protection.
Description
Technical field
The utility model belongs to naphthene sulfonic acid technology for hydrolyzing field, is specifically related to a kind of α-naphthalenesulfonicacid continuous pressure hydrolysis device.
Background technology
α-naphthalenesulfonicacid and beta-naphthalenesulfonic-acid are the important intermediate being used as to produce dyestuff, agricultural chemicals and medicine, and the two is that raw material obtains through sulfonation reaction with naphthalene.The naphthene sulfonic acid adopting aforesaid method to produce is usually the mixture of its various isomer, α-naphthalenesulfonicacid from beta-naphthalenesulfonic-acid because its sulfonic group position is different, performance there are differences, the production of some agricultural chemicals and medicine then needs highly purified beta-naphthalenesulfonic-acid, even but adopt the Optimum combinational scheme of beta-naphthalenesulfonic-acid synthesis condition, also still a small amount of α-naphthalenesulfonicacid can inevitably be synthesized, need the by product α-naphthalenesulfonicacid existed in the reaction solution after to sulfonation reaction to be hydrolyzed, to obtaining the higher beta-naphthalenesulfonic-acid of purity for this reason.
At present, the hydrolysis of domestic and international α-naphthalenesulfonicacid adopts the reaction that is hydrolyzed that directly adds water usually, and production technique is intermittent mode, and hydrolysis efficiency is lower, and industrial scale is less.The major cause that there are the problems referred to above is the special hydrolytic device not being applicable to α-naphthalenesulfonicacid hydrolysis at present, is therefore badly in need of providing the hydrolysis device that a kind of structure is simple, α-naphthalenesulfonicacid hydrolysis effect is good.
Utility model content
The purpose of this utility model is to provide a kind of α-naphthalenesulfonicacid continuous pressure hydrolysis device.
The purpose of this utility model realizes like this, comprise sulfonation reaction still, vapour generator, generate water collecting tank, condensate pump and hydrolytic reaction pot, described hydrolytic reaction pot comprises one-stage hydrolysis reactor, secondary hydrolytic reaction pot, tertiary effluent solution reaction kettle and level Four hydrolytic reaction pot, the discharge port of described sulfonation reaction still is connected with the opening for feed of one-stage hydrolysis reactor, the discharge port of described one-stage hydrolysis reactor is connected with the opening for feed of secondary hydrolytic reaction pot, the discharge port of described secondary hydrolytic reaction pot is connected with the opening for feed of tertiary effluent solution reaction kettle, the discharge port of described tertiary effluent solution reaction kettle is connected with the opening for feed of level Four hydrolytic reaction pot, the discharge port of described level Four hydrolytic reaction pot with blow naphthalene tower and be connected, the air outlet of described vapour generator is connected with the bottom air inlet of level Four hydrolytic reaction pot with one-stage hydrolysis reactor, secondary hydrolytic reaction pot, tertiary effluent solution reaction kettle respectively, the water-in of described condensate pump is communicated with generation water collecting tank, and the rising pipe of described condensate pump is connected with the water-in of one-stage hydrolysis reactor, secondary hydrolytic reaction pot, tertiary effluent solution reaction kettle and level Four hydrolytic reaction pot respectively.
The α-naphthalenesulfonicacid continuous pressure hydrolysis device that the utility model provides, be applicable to continuous pressure hydrolysis α-naphthalenesulfonicacid, the continuous pressure hydrolysis device adopting the utility model to provide carries out the hydrolysis of sulfonation reaction mixed solution, in hydrolysate, the content of α-naphthalenesulfonicacid is 0.2 ~ 0.8%, the percent hydrolysis of α-naphthalenesulfonicacid is largely increased, effectively improve the purity of naphthalenes intermediate beta-naphthalenesulfonic-acid, reduce enterprise cost and drop into, realize the production requirement of energy-saving and emission-reduction, environmental protection.
Accompanying drawing explanation
Fig. 1 is structural representation of the present utility model;
In figure: 1-sulfonation reaction still, 2-vapour generator, 3-generation water collecting tank, 4-condensate pump, 5-one-stage hydrolysis reactor, 6-secondary hydrolytic reaction pot, 7-tertiary effluent solution reaction kettle, 8-level Four hydrolytic reaction pot, 9-blow naphthalene tower.
Embodiment
Be further described the utility model below in conjunction with drawings and Examples, but limited the utility model never in any form, any change done based on the utility model training centre or improvement, all belong to protection domain of the present utility model.
As shown in Figure 1, the α-naphthalenesulfonicacid continuous pressure hydrolysis device that the utility model provides comprises sulfonation reaction still 1, vapour generator 2, generate water collecting tank 3, condensate pump 4 and hydrolytic reaction pot, described hydrolytic reaction pot comprises one-stage hydrolysis reactor 5, secondary hydrolytic reaction pot 6, tertiary effluent solution reaction kettle 7 and level Four hydrolytic reaction pot 8, the discharge port of described sulfonation reaction still 1 is connected with the opening for feed of one-stage hydrolysis reactor 5, the discharge port of described one-stage hydrolysis reactor 5 is connected with the opening for feed of secondary hydrolytic reaction pot 6, the discharge port of described secondary hydrolytic reaction pot 6 is connected with the opening for feed of tertiary effluent solution reaction kettle 7, the discharge port of described tertiary effluent solution reaction kettle 7 is connected with the opening for feed of level Four hydrolytic reaction pot 8, the discharge port of described level Four hydrolytic reaction pot 8 with blow naphthalene tower 9 and be connected, the air outlet of described vapour generator 2 is connected with the bottom air inlet of level Four hydrolytic reaction pot 8 with one-stage hydrolysis reactor 5, secondary hydrolytic reaction pot 6, tertiary effluent solution reaction kettle 7 respectively, the water-in of described condensate pump 4 is communicated with generation water collecting tank 3, and the rising pipe of described condensate pump 4 is connected with the water-in of one-stage hydrolysis reactor 5, secondary hydrolytic reaction pot 6, tertiary effluent solution reaction kettle 7 and level Four hydrolytic reaction pot 8 respectively.
Described hydrolytic reaction pot is the enamel reaction still of jacketed, and uniform 3 air inlet rotary-atomizing shower nozzles bottom still, each atomizer is fitted with reverse checkvalve respectively.
Described condensate pump 4 is trash-type impeller structure, and net positive suction head (NPSH) is 5 ~ 8m.
Described vapour generator 2 is low-pressure saturated steam producer, and its air outlet place arranges pressure maintaining valve.
principle of work of the present utility model and working process as follows:
Sulfonation reaction mixed solution enters one-stage hydrolysis reactor from sulfonation reaction still 1, sulfonation reaction generates water of condensation self-generating water collecting tank 3 and sends into one-stage hydrolysis reactor 5 through condensate pump 4, low-pressure saturated steam contacts with sulfonation reaction mixed solution with vaporific reflux type bottom one-stage hydrolysis reactor 5 from vapour generator 2, and sulfonation reaction mixed solution reacts 30min in one-stage hydrolysis reactor 5; Mixed solution after one-level pressurized hydrolysis enters secondary hydrolytic reaction pot 6 from one-stage hydrolysis reactor 5, sulfonation reaction generates water of condensation self-generating water collecting tank 3 and sends into secondary hydrolytic reaction pot 6 through condensate pump 4, low-pressure saturated steam contacts with the mixed solution after one-level pressurized hydrolysis with vaporific reflux type bottom secondary hydrolytic reaction pot 6 from vapour generator 2, and the mixed solution after one-level pressurized hydrolysis reacts 30min in secondary hydrolytic reaction pot 6; Mixed solution after two-stage pressurizing hydrolysis enters tertiary effluent solution reaction kettle 7 from secondary hydrolytic reaction pot 6, sulfonation reaction generates water of condensation self-generating water collecting tank 3 and sends into tertiary effluent solution reaction kettle 7 through condensate pump 4, the mixed solution of low-pressure saturated steam after vapour generator 2 is hydrolyzed with two-stage pressurizing with vaporific reflux type bottom tertiary effluent solution reaction kettle 7 contacts, and the mixed solution after two-stage pressurizing hydrolysis reacts 30min in tertiary effluent solution reaction kettle 7; Mixed solution after three times' lifting hydrolysis enters level Four hydrolytic reaction pot 8 from tertiary effluent solution reaction kettle 7, sulfonation reaction generates water of condensation self-generating water collecting tank 3 and sends into level Four hydrolytic reaction pot 8 through condensate pump 4, the mixed solution of low-pressure saturated steam after vapour generator 2 is hydrolyzed with three times' lifting with vaporific reflux type bottom level Four hydrolytic reaction pot 8 contacts, and the mixed solution after three times' lifting hydrolysis reacts 30min in level Four hydrolytic reaction pot 8; In said hydrolyzed reaction process, the sulfonation reaction sent in one-stage hydrolysis reactor 5, secondary hydrolytic reaction pot 6, tertiary effluent solution reaction kettle 7, level Four hydrolytic reaction pot 8 generates water of condensation and adds all in two steps, namely the sulfonation reaction first adding theoretical water consumption 40% needed for hydrolysis reaction generates water of condensation, passing into pressure is 0.46MPa, temperature is supplement after the low-pressure saturated steam of 146 DEG C to add sulfonation reaction generation water of condensation again, and the temperature that described sulfonation reaction generates water of condensation is 85 DEG C; Keep the hydrolysis pressure in one-stage hydrolysis reactor 5, secondary hydrolytic reaction pot 6, tertiary effluent solution reaction kettle 7, level Four hydrolytic reaction pot 8 to be 0.10MPa simultaneously, hydrolysis temperature is 155 DEG C, after level Four hydrolysis reaction completes, in hydrolysate, the content of α-naphthalenesulfonicacid is 0.21%.
The utility model breaks traditions the restriction of α-naphthalenesulfonicacid interval ordinary-pressure hydrolysis method, adopts continuous pressure hydrolysis α-naphthalenesulfonicacid; In traditional batch ordinary-pressure hydrolysis process water hydrolysis products, the content of α-naphthalenesulfonicacid is 1 ~ 3%, the continuous pressure hydrolysis device adopting the utility model to provide carries out the hydrolysis of sulfonation reaction mixed solution, in hydrolysate, the content of α-naphthalenesulfonicacid is 0.2 ~ 0.8%, the percent hydrolysis of α-naphthalenesulfonicacid is largely increased, effectively improve the purity of naphthalenes intermediate beta-naphthalenesulfonic-acid, reduce enterprise cost to drop into, realize the production requirement of energy-saving and emission-reduction, environmental protection.
The continuous pressure hydrolysis device that the utility model provides has good expansibility, namely realizes expanding by increase and decrease hydrolysis progression and supporting hydrolysis device; In actual production process, can according to the requirement of actual percent hydrolysis, increase and decrease hydrolysis progression, thus effective cost-saving input.
Claims (4)
1. one kind is applicable to the device of α-naphthalenesulfonicacid continuous pressure method for hydrolysis, comprise sulfonation reaction still (1), vapour generator (2), generate water collecting tank (3), condensate pump (4) and hydrolytic reaction pot, described hydrolytic reaction pot comprises one-stage hydrolysis reactor (5), secondary hydrolytic reaction pot (6), tertiary effluent solution reaction kettle (7) and level Four hydrolytic reaction pot (8), it is characterized in that the discharge port of described sulfonation reaction still (1) is connected with the opening for feed of one-stage hydrolysis reactor (5), the discharge port of described one-stage hydrolysis reactor (5) is connected with the opening for feed of secondary hydrolytic reaction pot (6), the discharge port of described secondary hydrolytic reaction pot (6) is connected with the opening for feed of tertiary effluent solution reaction kettle (7), the discharge port of described tertiary effluent solution reaction kettle (7) is connected with the opening for feed of level Four hydrolytic reaction pot (8), the discharge port of described level Four hydrolytic reaction pot (8) with blow naphthalene tower (9) and be connected, the air outlet of described vapour generator (2) is connected with the bottom air inlet of level Four hydrolytic reaction pot (8) with one-stage hydrolysis reactor (5), secondary hydrolytic reaction pot (6), tertiary effluent solution reaction kettle (7) respectively, the water-in of described condensate pump (4) is communicated with generation water collecting tank (3), and the rising pipe of described condensate pump (4) is connected with the water-in of one-stage hydrolysis reactor (5), secondary hydrolytic reaction pot (6), tertiary effluent solution reaction kettle (7) and level Four hydrolytic reaction pot (8) respectively.
2. device according to claim 1, is characterized in that described hydrolytic reaction pot is the enamel reaction still of jacketed, and uniform 3 air inlet rotary-atomizing shower nozzles bottom still, each atomizer is fitted with reverse checkvalve respectively.
3. device according to claim 1, it is characterized in that described condensate pump (4) is for trash-type impeller structure, net positive suction head (NPSH) is 5 ~ 8m.
4. device according to claim 1, it is characterized in that described vapour generator (2) is for low-pressure saturated steam producer, its air outlet place arranges pressure maintaining valve.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201520111498.9U CN204490771U (en) | 2015-02-16 | 2015-02-16 | A kind of α-naphthalenesulfonicacid continuous pressure hydrolysis device |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201520111498.9U CN204490771U (en) | 2015-02-16 | 2015-02-16 | A kind of α-naphthalenesulfonicacid continuous pressure hydrolysis device |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN204490771U true CN204490771U (en) | 2015-07-22 |
Family
ID=53570061
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201520111498.9U Active CN204490771U (en) | 2015-02-16 | 2015-02-16 | A kind of α-naphthalenesulfonicacid continuous pressure hydrolysis device |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN204490771U (en) |
-
2015
- 2015-02-16 CN CN201520111498.9U patent/CN204490771U/en active Active
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN204490771U (en) | A kind of α-naphthalenesulfonicacid continuous pressure hydrolysis device | |
| CN202569630U (en) | Additive reaction kettle vapour condensation device | |
| CN104628607A (en) | Continuous alpha-naphthalene sulfonic acid pressure hydrolysis method and device | |
| CN208454855U (en) | A kind of continuous reaction system for preparing epoxy chloropropane by using glycerol method | |
| CN204097444U (en) | Waste heat utilization system in a kind of white liquor distilling technique | |
| CN203280774U (en) | Sterilization device for brewing jar | |
| CN202315356U (en) | Step circulation recovery device of waste heat in xylose production | |
| CN201818565U (en) | Heat pump with vacuum effect | |
| CN115253337A (en) | Method and device for preparing isopropanol through two-tower thermal coupling reaction-variable pressure mixed rectification and application | |
| CN205032160U (en) | Recovery solution preparation of steam condensate water | |
| CN204298287U (en) | M-phthaloyl chloride production equipment | |
| CN102827115A (en) | Continuous refining system for producing maleic anhydride | |
| CN204251370U (en) | Alcohol natural pond liquid deamination equipment | |
| CN203487061U (en) | Methanol recycling device for biodiesel production process | |
| CN204138573U (en) | 2-phosphonobutane-1,2,4-tricarboxylic acid five-ester hydrolysis continuous device | |
| CN112299943A (en) | Acetylene cleaning device and method in vinyl acetate production process | |
| CN201953673U (en) | Water saving device of water-ring vacuum pump | |
| CN201280531Y (en) | Apparatus for trimethylamine preparation | |
| CN203253184U (en) | Reduced pressure distillation apparatus of methanol | |
| CN205823759U (en) | A kind of modified model vacuum pump group | |
| CN203700231U (en) | Continuous manufacturing system for chloromethyl ether | |
| CN202658106U (en) | Clomazone production device | |
| CN203999626U (en) | The oil field displacement of reservoir oil microbial inoculum reaction unit that spreads cultivation | |
| CN216550430U (en) | Biopolymer gamma-polyglutamic acid industrial fermentation tank | |
| CN203878082U (en) | High-concentration methylal production process device |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant |