CN113185487B - Production process of Jiale musk - Google Patents
Production process of Jiale musk Download PDFInfo
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- CN113185487B CN113185487B CN202110465813.8A CN202110465813A CN113185487B CN 113185487 B CN113185487 B CN 113185487B CN 202110465813 A CN202110465813 A CN 202110465813A CN 113185487 B CN113185487 B CN 113185487B
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- C07—ORGANIC CHEMISTRY
- C07D—HETEROCYCLIC COMPOUNDS
- C07D311/00—Heterocyclic compounds containing six-membered rings having one oxygen atom as the only hetero atom, condensed with other rings
- C07D311/02—Heterocyclic compounds containing six-membered rings having one oxygen atom as the only hetero atom, condensed with other rings ortho- or peri-condensed with carbocyclic rings or ring systems
- C07D311/94—Heterocyclic compounds containing six-membered rings having one oxygen atom as the only hetero atom, condensed with other rings ortho- or peri-condensed with carbocyclic rings or ring systems condensed with rings other than six-membered or with ring systems containing such rings
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- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F9/00—Multistage treatment of water, waste water or sewage
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- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/46—Treatment of water, waste water, or sewage by electrochemical methods
- C02F1/461—Treatment of water, waste water, or sewage by electrochemical methods by electrolysis
- C02F1/463—Treatment of water, waste water, or sewage by electrochemical methods by electrolysis by electrocoagulation
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- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/46—Treatment of water, waste water, or sewage by electrochemical methods
- C02F1/461—Treatment of water, waste water, or sewage by electrochemical methods by electrolysis
- C02F1/467—Treatment of water, waste water, or sewage by electrochemical methods by electrolysis by electrochemical disinfection; by electrooxydation or by electroreduction
- C02F1/4672—Treatment of water, waste water, or sewage by electrochemical methods by electrolysis by electrochemical disinfection; by electrooxydation or by electroreduction by electrooxydation
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- C02F1/66—Treatment of water, waste water, or sewage by neutralisation; pH adjustment
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- C02F2001/007—Processes including a sedimentation step
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- C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
- C02F2103/34—Nature of the water, waste water, sewage or sludge to be treated from industrial activities not provided for in groups C02F2103/12 - C02F2103/32
- C02F2103/36—Nature of the water, waste water, sewage or sludge to be treated from industrial activities not provided for in groups C02F2103/12 - C02F2103/32 from the manufacture of organic compounds
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- C02F2305/00—Use of specific compounds during water treatment
- C02F2305/02—Specific form of oxidant
- C02F2305/023—Reactive oxygen species, singlet oxygen, OH radical
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- C02F3/30—Aerobic and anaerobic processes
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- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/34—Biological treatment of water, waste water, or sewage characterised by the microorganisms used
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- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F7/00—Aeration of stretches of water
Abstract
The invention belongs to the field of musk production, and particularly relates to a galaxolide production process which comprises a galaxolide synthesis unit, a pentamethyl indane rectification unit, a pentamethyl indane recovery unit, a galaxolide rectification unit and a three-waste treatment unit; the galaxolide synthesizing unit comprises a pentamethyl indan synthesizing module, a pentamethyl indanol synthesizing module and a galaxolide synthesizing module. Compared with the prior art, the method has the advantages of relatively simple process route, higher safety and environmental friendliness.
Description
Technical Field
The invention belongs to the field of musk production, and particularly relates to a Jiale musk production process.
Background
Galaxolide is a tricyclic isochroman type of musk that was first successfully synthesized by chemists of IFF corporation of usa and was patented in 1962. Galaxolide (Galaxolide) is a widely used synthetic musk-type fragrance that does not exist in nature. Its relative density 1.0054, refractive index 1.5342, flash point above 93 deg.C, boiling point 129 deg.C/106.6 Pa. It is colorless highly viscous liquid, can be dissolved in ethanol and oil, and is insoluble in water.
The galaxolide has high musk fragrance, elegant fragrance, sweet fragrance, excellent penetrating power and diffusion, lasting fragrance and good stability, and is commonly used in cosmetic cream, astringent, soap, daily essence, tobacco essence and edible essence to prepare cosmetic essence and perfume fixative. The musk of the product has strong fragrance, good stability, no toxicity, can not be absorbed by human internal organs, can be taken orally, and has lower price, so the Jiale musk is deeply loved by a flavoring agent. Galaxolide has shown the potential of substituted musk xylols and nitromusks and is a promising species among polycyclic musks.
At present, galaxolide is mainly synthesized by the synthesis route in patents invented by the sixties IFF company, and the process route is old, so that the following problems mainly exist: 1. the needed dihalogen alkane has difficult source, generates a plurality of foreign matters during preparation and is difficult to control; 2. the acetic acid is used in the process of preparing the indane, so that the waste liquid is difficult to treat after the reaction, and the problem of three wastes is caused; 3. in the process of preparing indanol, excessive pentamethyl indan is used as a raw material and a solvent so as to reduce the viscosity of the solution and greatly increase the cost; 4. hydrogen chloride gas is used in the process of preparing the galaxolide, and highly toxic byproduct chloromethyl ether is generated in the polyformaldehyde reaction, which has great harm to operators; 5. the added hydrogen chloride gas severely corrodes the equipment.
Disclosure of Invention
In order to solve the problems, the invention provides a production process of Jiale musk, and compared with the existing process, the production process has the advantages of relatively simple process route, higher safety and environmental friendliness.
The invention provides the following technical scheme:
a production process of galaxolide comprises a galaxolide synthesis unit, a pentamethyl indan rectification unit, a pentamethyl indan recovery unit, a galaxolide rectification unit and a three-waste treatment unit;
the galaxolide synthesizing unit comprises a pentamethyl indane synthesizing module, a pentamethyl indanol synthesizing module and a galaxolide synthesizing module;
the pentamethyl indane synthesis module comprises a styrene intermediate tank, an isoamylene intermediate tank, an indane mixing tank, an indane synthesis kettle, an indane standing elevated tank, an indane washing kettle and an indane crude product tank;
the pentamethyl indanol synthesis module comprises an indanol overhead tank, a Jiale mixing tank and an indanol synthesis kettle;
the Jiale musk synthesis module comprises a primary water metering tank, a methylal metering tank, a Jiale synthesis kettle, a Jiale crude product tank, a crude polyaluminium water tank, a polyaluminium water crude steaming tower, a polyaluminium water light component tank, a polyaluminium water steaming kettle buffer tank and a fine polyaluminium water tank;
the styrene intermediate tank and the isoamylene intermediate tank are connected with an indane mixing tank inlet, an indane mixing tank outlet is connected with an indane synthesis kettle, the indane standing elevated tank and the indane washing kettle are sequentially connected, and an indane washing kettle outlet is connected with an indane crude product tank;
the pentamethyl indan rectification unit, the indan elevated tank and the indan alcohol synthesis kettle are sequentially connected, and the Jiale mixing tank is connected with the indan alcohol synthesis kettle;
indanol synthetic cauldron, water metering tank, methylal metering tank all link to each other with the synthetic cauldron import of happy, happy synthetic cauldron export links to each other with happy crude groove, happy crude groove export is galaxy musk rectification unit, thick aluminium basin that gathers respectively, thick aluminium basin that gathers links to each other with the thick distillation tower import of gathering aluminium water, gather aluminium water thick distillation tower export and gather aluminium water light component jar, evaporate and gather aluminium water cauldron and link to each other respectively, it links to each other with evaporating and gathering aluminium water cauldron buffer tank, fine aluminium basin respectively to evaporate and gather aluminium water cauldron export.
Preferably, the pentamethyl indane rectification unit comprises an indane rectification A1 tower bottom, an indane rectification A2 tower bottom, an indane rectification A3 tower bottom, an A2 tower condenser, an A2 tower top reflux tank, an isoamylene dimer storage tank, an A3 tower concentrated drying kettle, an A3 tower condenser, an A3 tower top reflux tank, an indane finished product tank, an indane rectification A4 tower bottom, an A4 tower condenser, an indane recovery front-stage tank and an indane recovery rear-stage tank;
an indan crude product tank of the galaxolide synthesis unit is connected with an inlet of an indan rectification A1 tower kettle, an outlet of the indan rectification A1 tower kettle is respectively connected with an indan rectification A2 tower kettle and an indan rectification A3 tower kettle, the indan rectification A2 tower kettle, an A2 tower condenser, an A2 tower top reflux tank and an isoamylene dimer storage tank are sequentially connected, the indan rectification A3 tower kettle, the A3 tower condenser, an A3 tower top reflux tank and an indan finished product tank are sequentially connected, and the indan rectification A3 tower kettle is further connected with an A3 tower concentrated drying kettle;
an indane recovery groove of the pentamethyl indane recovery unit is connected with an inlet of a tower kettle of the indane rectification A4, an outlet of the tower kettle of the indane rectification A4 is connected with a condenser of the A4 tower, and an outlet of the condenser of the A4 tower is respectively connected with a front indane recovery groove, a rear indane recovery groove and an indane finished product groove.
Preferably, the pentamethyl indane recovery unit comprises an indane alkali water tank, an indane washing water tank, an indane recovery kettle, a sulfuric acid tank, a hydrogen peroxide head tank and an indane recovery tank;
and front and rear storage tanks of B tower indane of the sulfuric acid tank, the hydrogen peroxide head tank and the galaxolide rectification unit are connected with inlets of indane recycling kettles, outlets of the indane recycling kettles are respectively connected with the indane recycling tank, the indane alkaline water tank and the indane washing water tank, and an outlet of the indane recycling tank is connected with an indane rectification A4 tower kettle of the pentamethyl indane rectification unit.
Preferably, the galaxolide rectification unit comprises a galaxolide rectification B tower kettle, a de-heaving tower kettle, a galaxolide first-stage tank, a galaxolide second-stage tank, a galaxolide finished product tank, a water flushing kettle, a galaxolide finished product tower kettle, a galaxolide stock solution front-back tank, a galaxolide stock solution tank, a stock solution overhead tank, a B tower water head tank, a chloropropanol reaction kettle 40, a B tower chlorobenzene front-back tank, a B tower chlorobenzene finished product section tank, a B tower indan front-back tank, a B tower indan finished product section tank, a byproduct tank, a chlorobenzene tower kettle, a chlorobenzene tower water head section tank, a chlorobenzene front-back section tank, a light component receiving tank and an alkaline tank;
the Jiale crude product groove of the Jiale musk synthesis unit is connected with the inlet of a Jiale musk rectification B tower kettle, the outlet of the Jiale musk rectification B tower kettle is respectively connected with a B tower water head groove, a B tower chlorobenzene front and back section groove, a B tower chlorobenzene finished product section groove, a B tower indan front and back section groove, a B tower indan finished product section groove and a byproduct groove, the outlet of the B tower water head groove is connected with a chloropropanol reaction kettle, the B tower chlorobenzene front and back section groove, the B tower chlorobenzene front and back section storage tank and a chlorobenzene tower kettle are sequentially connected, the outlet of the chlorobenzene tower kettle is respectively connected with a chlorobenzene tower water head section groove and a chlorobenzene front and back section groove, the chlorobenzene tower water head section groove is connected with the chloropropanol reaction kettle, the outlet of the chloropropanol reaction kettle is respectively connected with a light component receiving tank and an alkaline washing tank, the front and back section groove is connected with a B tower chlorobenzene finished product section storage tank, the outlet of the B tower chlorobenzene section groove is connected with a chlorobenzene finished product storage tank, the tower B indane front-and-back section groove, the tower B indane front-and-back section storage tank and the indane recovery kettle are sequentially connected, and an outlet of the tower B indane finished product section groove is connected with the tower B indane finished product section storage tank;
the jiale musk rectification B tower cauldron export links to each other with taking off the heavy tower cauldron, take off heavy tower cauldron export and link to each other with one section groove of jiale, two section grooves of jiale, jiale finished product groove respectively, one section groove export of jiale musk rectification B tower links to each other, two section groove exports of jiale takes off the heavy tower cauldron and links to each other, it links to each other in proper order to be happy finished product groove, water-washed cauldron, good le finished product tower cauldron, it links to each other with groove, good le stoste groove around the good le stoste respectively to be happy finished product tower cauldron export, it links to each other with the stock solution overhead tank, it links to each other with taking off the heavy tower cauldron to be happy stock solution front and back groove.
Preferably, the three wastes comprise waste liquid, waste residues and waste gas, the waste liquid comprises acidic waste liquid and alkaline waste liquid, the waste residues are mainly saline-alkali residues, and the waste gas comprises chlorine-containing waste gas and organic waste gas;
the three-waste treatment unit comprises a waste liquid treatment subunit for treating waste liquid, a waste residue treatment subunit for treating waste residues and a waste gas treatment subunit for treating waste gas;
the waste liquid treatment subunit comprises a neutralization kettle, an adjusting tank, an electric flocculation device, an electro-catalysis device, an intermediate water tank and an anaerobic-aerobic tank, wherein the acidic waste liquid and the alkaline waste liquid enter the neutralization kettle for neutralization, the upper layer waste liquid is pumped into the adjusting tank, the lower layer waste residue enters the waste residue treatment subunit, the water outlet end of the adjusting tank is connected with the water inlet end of the electric flocculation device, the water outlet end of the electric flocculation device is connected with the water inlet end of the electro-catalysis device, the water outlet end of the electro-catalysis device is connected with the water inlet end of the intermediate water tank, and the water outlet end of the intermediate water tank is connected with the water inlet end of the anaerobic-aerobic tank.
Preferably, the waste residue treatment subunit includes evaporates saline and alkaline sediment cauldron, evaporates saline and alkaline sediment cauldron condenser, and the lower floor's waste residue in the neutralization cauldron gets into and evaporates the steam heating in the saline and alkaline sediment cauldron, and the liquid that evaporates is collected through evaporating saline and alkaline sediment cauldron condenser condensation, and remaining saline and alkaline sediment bagging-off is carried away.
Preferably, the waste gas treatment subunit comprises a multistage water washing mechanism, a resin adsorption mechanism and a plant area incinerator, wherein the chlorine-containing waste gas is washed by the multistage water washing mechanism, and is adsorbed by the resin adsorption mechanism and then is delivered to the plant area incinerator for incineration, and the organic waste gas is directly delivered to the plant area incinerator for incineration.
Preferably, an oxidant dosing mechanism is arranged on the electric flocculation device; the waste liquid treatment subunit also comprises a clarifier which is arranged between the electric flocculation device and the electric catalysis device.
Preferably, the anaerobic-aerobic tank comprises an anaerobic tank and an aerobic tank which are communicated, the anaerobic tank and the aerobic tank are respectively provided with a strain rejuvenator, a strain rejuvenation bed is arranged in the strain rejuvenator, an inlet of the strain rejuvenator is connected with the middle section of the anaerobic tank or the aerobic tank, and an outlet of the strain rejuvenator is connected with the front section of the anaerobic tank or the aerobic tank.
Preferably, aeration devices are arranged in the adjusting tank and the middle water tank.
The invention has the beneficial effects that:
1. the production process of galaxolide comprises a galaxolide synthesis unit, a pentamethyl indan rectification unit, a pentamethyl indan recovery unit, a galaxolide rectification unit and a three-waste treatment unit, wherein the pentamethyl indan recovery unit comprises an indane alkali water tank, an indane washing water tank, an indane recovery kettle, a sulfuric acid tank, a hydrogen peroxide solution overhead tank and an indane recovery tank;
adding ferrous sulfate into an indane recovery kettle, starting stirring, conveying front and rear storage tanks (containing 60% indane) of tower B indane of a galaxolide rectification unit to the indane recovery kettle, metering sulfuric acid by a sulfuric acid tank, adding into the indane recovery kettle, dropwise adding hydrogen peroxide into the indane recovery kettle through a hydrogen peroxide overhead tank, slowly heating to 80 ℃, stopping heating, keeping the temperature at 80 ℃ for 5 hours, stopping stirring, and standing the material for half an hour.
And (3) standing the materials in the indane recovery kettle for half an hour, adding water once, stirring for 15 minutes, standing for half an hour, recovering the lower-layer water phase into an indane washing water tank after layering, adding 5% liquid alkali, starting stirring for 15 minutes, standing for 1 hour, and recovering the lower-layer alkaline water into the indane alkali water tank after layering. The indane on the upper layer in the indane recovery kettle is conveyed to the indane recovery tank through a pipeline, and then conveyed to an indane rectification A4 tower kettle of a pentamethyl indane rectification unit for rectification treatment, so that pentamethyl indane can be effectively recovered, the production cost is reduced, and the discharge of three wastes is reduced.
2. The device comprises a waste liquid treatment subunit, a waste residue treatment subunit and a waste gas treatment subunit, wherein the waste liquid treatment subunit comprises an electric flocculation device, an oxidant is added into the electric flocculation device, under the action of an electric field, an anode of the electric flocculation device generates electrons to form a 'micro-flocculant', hydroxides of iron or aluminum, particles and colloidal pollutants suspended in water lose stability under the action of the flocculant, and the destabilized pollutant particles and the micro-flocculant collide with each other to combine into macroscopic large flocs. The oxidant oxidizes ferrous ions and the like generated by the electrocoagulation reaction into ferric ions, thereby avoiding the problem of generating a large amount of foams caused by the traditional aeration oxidation, and combining the ferric ions and salt as a flocculating agent to remove part of suspended matters in the wastewater.
3. The waste liquid treatment subunit contains electro-catalytic apparatus, and the electro-catalytic oxidation produces the hydroxyl free radical, utilizes the strong oxidizing property of hydroxyl free radical to decompose macromolecular substance in the waste water, improves the B/C of waste water to improve the biodegradability of waste water.
4. The anaerobic tank and the aerobic tank are arranged, heterotrophic bacteria and autotrophic bacteria in the anaerobic tank and the aerobic tank decompose macromolecular organic matters in sewage into micromolecular organic matters, insoluble organic matters are converted into soluble organic matters, the aerator is arranged in the aerobic tank, the Roots blower provides an air source, activated sludge is extracted from the middle section of the anaerobic tank and the aerobic tank every 36-48 hours through the feed inlet to perform rejuvenation of strains, and the rejuvenated activated sludge is discharged into the anaerobic tank and the front section of the aerobic tank through an outlet, so that the rejuvenation of anaerobic bacteria and aerobic bacteria is realized.
Drawings
FIG. 1 is a flow chart of a production process of galaxolide;
FIG. 2 is a scheme for indane synthesis;
FIG. 3 is a flow diagram of the synthesis of galaxolide;
FIG. 4 is a flow chart of aluminum water treatment;
FIG. 5 is a first indane rectification scheme;
FIG. 6 is a second indane rectification scheme;
FIG. 7 indane recovery flow scheme;
FIG. 8 is a first rectification scheme of Jiale musk;
FIG. 9 is a flow diagram of the recovery of chloropropanol;
FIG. 10 is a second flow chart of the rectification of galaxolide;
FIG. 11 is a flow chart of waste liquid treatment;
FIG. 12 is a flow chart of waste residue treatment;
FIG. 13 is a flow chart of the exhaust gas treatment.
Description of the drawings:
10-Jiale musk synthesis unit 10-A1 styrene intermediate tank 10-A2 isoamylene intermediate tank 10-A3 indane mixing tank 10-A4 indane synthesis kettle 10-A5 indane standing elevated tank 10-A6 indane water washing kettle 10-A7 indane crude tank 10-B1 indane elevated tank 10-B2 Jiale mixing tank 10-B3 indane alcohol synthesis kettle 10-C1 one-time water metering tank 10-C2 methylal metering tank 10-C3 Jiale synthesis kettle 10-C4 Jiale crude tank 10-C5 crude polyaluminium water tank 10-C6 polyaluminium water crude distillation tower 10-C7 polyaluminium water light component tank 10-C8 polyaluminium water evaporation kettle 10-C9 polyaluminium water evaporation kettle buffer tank 10-C10 fine polyaluminium water tank
20 pentamethyl indan rectification unit 20-D1 indan rectification A1 tower bottom 20-D2 indan rectification A2 tower bottom 20-D3 indan rectification A3 tower bottom 20-D4A 2 tower condenser 20-D5A 2 tower top reflux tank 20-D6 isopentene dimer storage tank 20-D7A 3 tower concentrated dry bottom 20-D8A 3 tower condenser 20-D9A 3 tower top reflux tank 20-D10 indan finished product tank 20-D11 indan rectification A4 tower bottom 20-D12A 4 tower condenser 20-D13 indan recovery front section tank 20-D14 indan recovery rear section tank 20-D11 indan rectification A4 tower bottom 20-D12A 4 tower condenser 20-D13 indan recovery front section tank 20-D14 indan recovery front section tank
30 pentamethyl indan recovery unit 30-E1 indan alkaline water tank 30-E2 indan washing water tank 30-E3 indan recovery kettle 30-E4 sulfuric acid tank 30-E5 hydrogen peroxide solution overhead tank 30-E6 indan recovery tank
40-F1 Canon musk rectification unit 40-F1 Canon musk rectification B tower kettle 40-F2 de-heavy tower kettle 40-F3 Jiale first section groove 40-F4 Jiale second section groove 40-F5 Jiale finished product groove 40-F6 water flushing kettle 40-F7 Jiale finished product tower kettle 40-F8 Jiale stock solution front and back groove 40-F9 Jiale stock solution groove 40-F10 stock solution overhead groove 40-F11B tower water head groove 40-F12 chloropropanol reaction kettle 40-F13B tower chlorobenzene front and back section groove 40-F14B tower chlorobenzene front and back section storage tank 40-F15B tower finished product section groove 40-F16B tower finished product section storage tank 40-F17B tower indan front and back section storage tank 40-F19B indan finished product groove 40-F20B chlorobenzene finished product storage tank 40-F17B tower indan front and back section storage tank 40-F18B chlorobenzene by-F9640 chlorobenzene by-F21B tower byproduct groove 40-F18B chlorobenzene by-F22 40-F23 chlorobenzene tower water head section groove 40-F24 chlorobenzene front and rear section groove 40-F25 light component receiving groove 40-F26 alkaline washing tank
50-G1 neutralization kettle 50-G2 adjusting pool 50-G3 electric flocculation device 50-G4 electric catalysis device 50-G5 middle water pool 50-G6 anaerobic pool 50-G7 aerobic pool 50-G8 saline-alkali residue steaming kettle 50-G9 saline-alkali residue steaming kettle condenser 50-G10 multi-stage washing mechanism 50-G11 resin adsorption mechanism 50-G12 plant area incinerator 50-G13 oxidant dosing mechanism 50-G14 clarifier
Detailed Description
The present invention will be described in detail with reference to the following examples.
A production process of galaxolide comprises a galaxolide synthesis unit 10, a pentamethyl indane rectification unit 20, a pentamethyl indane recovery unit 30, a galaxolide rectification unit 40 and a three-waste treatment unit 50, and the following units are explained:
synthetic unit of 'Yi' Jiale musk
The galaxolide synthesis unit 10 is characterized in that a three-step method is adopted to synthesize a circuit, firstly, methyl styrene and isoamylene are subjected to Friedel-crafts alkylation cyclization reaction to generate pentamethyl indan, then the pentamethyl indan is subjected to hydroxyl alkylation reaction with propylene oxide under the conditions of a chlorobenzene solvent and an aluminum trichloride catalyst to generate pentamethyl indan alcohol, and finally, the pentamethyl indan alcohol and methylal are subjected to cyclization reaction in the same reaction system for generating the pentamethyl indan alcohol to generate galaxolide.
The reaction equation involved is
The galaxolide synthesizing unit 10 comprises a pentamethyl indan synthesizing module, a pentamethyl indanol synthesizing module and a galaxolide synthesizing module;
the pentamethyl indan synthesis module comprises a styrene middle groove 10-A1, an isoamylene middle groove 10-A2, an indan mixing groove 10-A3, an indan synthesis kettle 10-A4, an indan standing overhead groove 10-A5, an indan water washing kettle 10-A6 and an indan crude product tank 10-A7;
alpha-methyl styrene from one tank group and isoamylene from the two tank groups are metered into the indane mixing tank 10-A3 through a styrene intermediate tank 10-A1 and an isoamylene intermediate tank 10-A2 respectively and are stirred uniformly for standby. The indan synthesis kettle 10-A4 is firstly added with a catalyst of phosphorus pentoxide, then the mixture in the indan mixing tank 10-A3 is dropwise added at a constant speed, and an alkylation reaction is carried out in the indan synthesis kettle 10-A4 under the action of the catalyst to obtain an intermediate pentamethyl indan (indan for short). Because the reaction releases heat during dripping, chilled water needs to be introduced into a jacket of the indane synthesis kettle 10-A4 to keep the kettle at the temperature of 30-35 ℃, the temperature is kept for 2 hours, and the pressure in the kettle is normal pressure; and after the reaction is finished, the crude indane enters an indane standing elevated tank 10-A5 for standing and layering. After layering, the upper organic phase enters an indane washing kettle 10-A6, and the lower floccule is barreled. Adding a 5% NaOH solution and primary water into an indane washing kettle 10-A6, stirring, washing, standing, layering, conveying an upper organic phase to an indane crude product tank 10-A7, then rectifying in a pentamethyl indane rectifying unit 20, allowing a 5% NaOH alkaline washing water phase to enter an indane alkaline water tank 10-E1 through a self-flowing pipeline, allowing a primary water washing water phase to enter an indane washing water tank 10-E2 through a self-flowing pipeline, and collecting and recycling.
The pentamethyl indanol synthesis module comprises an indanol overhead tank 10-B1, a Jiale mixing tank 10-B2 and an indanol synthesis kettle 10-B3;
firstly, adding solid material aluminum trichloride into the indanol synthesis kettle 10-B3, and starting stirring. The finished indane from pentamethyl indane rectification unit 20 is sent to indane overhead tank 10-B1, and then is added into indanol synthesis kettle 10-B3. Respectively metering propylene oxide from a three-tank group and chlorobenzene from a four-tank group into a Jiale mixing tank 10-B2, stirring and mixing uniformly, dropwise adding the mixed materials into an indanol synthesis kettle 10-B3 through a mass flow meter, keeping the temperature of-18 to-14 ℃ through chilled water in a jacket of the indanol synthesis kettle 10-B3, stirring and reacting for 2 hours, wherein the reaction pressure in the kettle is normal pressure, and carrying out a hydroxyalkylation reaction in the reaction kettle under the action of a catalyst to obtain pentamethyl indanol (referred to as indanol for short).
The galaxolide musk synthesis module comprises a primary water metering tank 10-C1, a methylal metering tank 10-C2, a galaxolide synthesis kettle 10-C3, a galaxolide crude product tank 10-C4, a crude polyaluminium water tank 10-C5, a polyaluminium water crude evaporation tower 10-C6, a polyaluminium water light component tank 10-C7, a polyaluminium water evaporation kettle 10-C8, a polyaluminium water evaporation kettle buffer tank 10-C9 and a fine polyaluminium water tank 10-C10;
indanol in the indanol synthesis kettle 10-B3 automatically flows into the Jiale synthesis kettle 10-C3 through a pipeline, and primary water and methylal from the five-tank group are respectively added into the Jiale synthesis kettle 10-C3 through a methylal metering tank 10-C1 and a primary water metering tank 10-C2 under the stirring condition. Circulating water is filled into a jacket of the Jiale synthesis kettle 10-C3 to maintain the temperature of the reaction kettle, the stirring reaction is carried out for 2 hours, the pressure in the kettle is 0.04MPa, and cyclization reaction is carried out in the reaction kettle to obtain Jiale musk.
After the reaction is finished, slowly adding water into the Jiale synthesis kettle 10-C3, introducing steam, keeping the temperature and stirring for 30 min. Adding alkali liquor, washing with alkali, delivering the upper organic phase (crude galaxolide) to a galaxolide crude product tank 10-C4, and then delivering galaxolide rectification unit 40 for rectification to obtain a finished galaxolide product; the lower layer water phase is conveyed to a crude polyaluminium chloride water tank 10-C5 through a pipeline and then conveyed to a crude polyaluminium chloride water distillation tower 10-C6 for reduced pressure distillation. And (3) condensing and collecting distilled gas phase, conveying the condensed and collected distilled gas phase to a light component tank 10-C7 of the polyaluminium water, then conveying the condensed and collected polyaluminium water to a factory incinerator 50-G12 for incineration treatment, pumping concentrated solution into a polyaluminium water evaporation kettle 10-C8 for further reduced pressure distillation, condensing and collecting the distilled gas phase, then condensing and recycling the condensed and used in a buffer tank 10-C9 of the polyaluminium water evaporation kettle, standing and layering the lower concentrated solution, conveying the refined polyaluminium water to a refined polyaluminium water tank 10-C10, recycling the refined polyaluminium water and using the rest to a tank group.
Rectifying unit for di-pentamethyl indane
The pentamethyl indane rectification unit comprises an indane rectification A1 tower kettle 20-D1, an indane rectification A2 tower kettle 20-D2, an indane rectification A3 tower kettle 20-D3, an A2 tower condenser 20-D4, an A2 tower top reflux tank 20-D5, an isoamylene dimer storage tank 20-D6, an A3 tower concentrated drying kettle 20-D7, an A3 tower condenser 20-D8, an A3 tower top reflux tank 20-D9, an indane finished product tank 20-D10, an indane rectification A4 tower kettle 20-D11, an A4 tower condenser 20-D12, an indane recovery front section tank 20-D13 and an indane recovery rear section tank 20-D14;
crude indan in an indan crude tank 10-A7 from a galaxolide synthesis unit is pumped to an indan rectification A1 tower kettle 20-D1, reduced pressure rectification is carried out at 150 ℃, a light component gas phase at the tower top enters an indan rectification A2 tower kettle 20-D2, and a heavy component liquid phase is pumped to an indan rectification A3 tower kettle 20-D3.
Performing reduced pressure distillation on a tower kettle 20-D2 of an indane rectification A2 at 120 ℃, condensing a tower top light component gas phase to an A2 tower top reflux tank 20-D5 through an A2 tower condenser 20-D4, flowing to an isoamylene dimer storage tank 20-D6 by gravity, barreling and selling, removing non-condensable gas to an A tower vacuum system, and pumping a heavy component liquid phase to an indane rectification A1 tower kettle 20-D1.
Performing reduced pressure distillation on an indane rectification A3 tower bottom 20-D3 at 130 ℃, condensing a tower top light component gas phase to an A3 tower top reflux tank 20-D9 through an A3 tower condenser 20-D8 to be used as an indane finished product, automatically flowing the indane finished product to an indane finished product tank 20-D10, conveying to an indane overhead tank 10-B1 for indane alcohol synthesis, introducing non-condensable gas to an A tower vacuum system, introducing a heavy component liquid phase to an A3 tower concentrated drying kettle 20-D7, heating the tower A3 concentrated drying kettle 20-D7 jacket by 0.5MPa steam, performing gas-liquid circulation with the indane rectification A3 tower bottom 20-D3, and conveying residual liquid at the bottom of the A3 tower concentrated drying kettle 20-D7 to a barrel for external treatment.
Crude indan in an indan recovery tank 30-E6 from a pentamethyl indan recovery unit 30 is pumped to an indan rectification A4 tower bottom 20-D11, vacuum rectification is carried out at 160 ℃, light component gas phase at the tower top is condensed and refluxed by an A4 tower condenser 20-D12, sectionally extracted into a indan recovery front-stage tank 20-D13 and an indan recovery rear-stage tank 20-D14, and then is put in a barrel for sale, and an indan finished product tank 20-D10, and then an indan elevated tank 10-B1 is pumped for indan synthesis, and non-condensable gas is sent to an A tower vacuum system.
Tri-and pentamethyl indane recovery unit
The pentamethyl indane recovery unit comprises an indane alkali water tank 30-E1, an indane washing tank 30-E2, an indane recovery kettle 30-E3, a sulfuric acid tank 30-E4, a hydrogen peroxide solution head tank 30-E5 and an indane recovery tank 30-E6;
firstly, adding ferrous sulfate into an indane recovery kettle 30-E3, starting stirring, then conveying a front-section storage tank 40-F18 (containing 60% indane) and a rear-section storage tank 40-F18 of tower B indane of a galaxolide rectification unit 40 to an indane recovery kettle 30-E3, metering sulfuric acid by a sulfuric acid tank 30-E4, adding the indane recovery kettle 30-E3 into the sulfuric acid tank, dropwise adding hydrogen peroxide into the indane recovery kettle 30-E3 by a hydrogen peroxide overhead tank 30-E5, slowly heating to 80 ℃, stopping heating, keeping the temperature at 80 ℃ for 5 hours, closing stirring, and standing the materials for half an hour.
And (3) standing the materials in the indane recovery kettle 30-E3 for half an hour, adding water once, stirring for 15 minutes, standing for half an hour, recovering the lower-layer water phase into the indane washing tank 30-E2 after layering, adding 5% liquid alkali, starting stirring for 15 minutes, standing for 1 hour, and recovering the lower-layer alkaline water into the indane alkaline water tank 30-E1 after layering. The indane on the upper layer in the indane recovery kettle 30-E3 is sent to the indane recovery tank 30-E6 through a pipeline, and then is sent to an indane rectification A4 tower kettle 20-D11 of a pentamethyl indane rectification unit 20 for rectification treatment.
Rectification unit for "Sijiale" musk
The galaxolide rectification unit 40 comprises a galaxolide rectification B tower bottom 40-F1, a de-heaving tower bottom 40-F2, a galaxolide first-section groove 40-F3, a galaxolide second-section groove 40-F4, a galaxolide finished product groove 40-F5, a water flushing kettle 40-F6, a galaxolide finished product tower bottom 40-F7, a galaxolide raw liquid front and back groove 40-F8, a galaxolide raw liquid groove 40-F9, a raw liquid overhead groove 40-F10, a B tower water head groove 40-F11, a chloropropanol reaction kettle 40-F12, a B tower chlorobenzene front and back section groove 40-F13, a B tower chlorobenzene front and back section storage tank 40-F14, a B tower chlorobenzene finished product section groove 40-F15, a B tower chlorobenzene finished product storage tank 40-F16, a B tower front and back section groove 40-F6, a B tower indan front and back section storage tank 40-F18, a B tower finished product groove 40-F19, a B tower finished product storage tank 40-F3673729, a B tower front and a water head groove 40-F20, The device comprises a by-product tank 40-F21, a chlorobenzene tower kettle 40-F22, a chlorobenzene tower water head tank 40-F23, a chlorobenzene front-back tank 40-F24, a light component receiving tank 40-F25 and an alkaline washing tank 40-F26.
Pumping crude galaxolide from a galaxolide crude product tank 10-C4 of a galaxolide synthesis unit 10 to a galaxolide rectification B tower kettle 40-F1, carrying out reduced pressure rectification operation at 170 ℃, condensing and refluxing light component gas phase at the top of the B tower through B, sending non-condensable gas to a B tower vacuum system, extracting in sections, extracting a chloropropanol removal reaction kettle 40-F12 from a B tower water head tank 40-F11 for recovery treatment, extracting from a B tower chlorobenzene front and rear section tank 40-F13 to a chlorobenzene front and rear section storage tank 40-F14 for treatment, extracting from a B tower chlorobenzene finished product tank 40-F15 to a chlorobenzene finished product tank 40-F16, extracting from a B tower indan front and rear section tank 40-F17 to a B tower indan front and rear section storage tank 40-F18 for treatment, extracting from a B tower indan finished product tank 40-F19 to a B tower indan finished product storage tank 40-F20, extracting from a B tower indan front and a byproduct tank 40-F21 from a B tower indan rear section tank, and removing heavy components in the tower bottom of the tower B to the tower bottom of the heavy component removing tower 40-F2.
Pumping materials from front and rear chlorobenzene storage tanks 40-F14 of a tower B to a chlorobenzene tower kettle 40-F22, carrying out reduced pressure rectification operation at 120 ℃, condensing and refluxing light component gas phase at the top of the chlorobenzene tower through a chlorobenzene tower condenser, sending non-condensable gas to a tower B vacuum system, extracting in sections, extracting from a chlorobenzene tower water head section tank 40-F23, conveying to a chloropropanol reaction kettle 40-F12 for treatment, extracting from chlorobenzene front and rear chlorobenzene storage tanks 40-F24, and conveying to a chlorobenzene finished product section storage tank 40-F16 of the tower B for treatment.
Collecting materials in a B tower water head tank 40-F11 and a chlorobenzene tower water head section tank 40-F23 to a chloropropanol reaction kettle 40-F12, adding 20% of liquid alkali solution into the chloropropanol reaction kettle 40-F12, starting stirring, introducing steam into a reaction kettle jacket, heating to 100 ℃, wherein the reaction pressure in the kettle is-0.08 MPa, condensing and collecting gas phase in the kettle to a light component receiving tank 40-F25, conveying to a plant area incinerator 50-G12 for incineration treatment, and conveying liquid phase in the kettle to an alkali washing tank 40-F26 for recycling.
Materials from a Jiale musk rectification B tower kettle 40-F1, a Jiale two-stage tank 40-F4 and a Jiale stock solution front and rear tank 40-F8 are conveyed to a de-emphasis tower kettle 40-F2 through a pump, reduced pressure rectification is carried out at 80 ℃, the materials are condensed at the top of the de-emphasis tower kettle 40-F2 and are extracted in sections, the Jiale musk rectification B tower kettle 40-F1 is collected from the Jiale first-stage tank 40-F3, the Jiale two-stage tank 40-F4 is collected from the de-emphasis tower kettle 40-F2 and the Jiale finished product tank 40-F5 is collected from a water flushing kettle 40-F6, and the water flushing kettle 40-F6 is used for heating a Jiale musk finished product and then the Jiale finished product tower kettle 40-F7 is further processed.
The finished galaxolide product from the water flushing kettle 40-F6 enters a galaxolide finished product tower kettle 40-F7, is condensed at the top of the galaxolide finished product tower kettle 40-F and is collected in sections, and galaxolide stock solution is collected in a front tank 40-F8 and is returned to a de-weighting tower kettle 40-F2, and a galaxolide stock solution tank 40-F9 is collected in a stock solution overhead tank 40-F10.
Mixing and packaging: adding the galaxolide finished product into each mixing kettle from a stock solution overhead tank 40-F10, adding different diluents according to market requirements, uniformly stirring, and putting into a barrel to an automatic packaging line to obtain the galaxolide product.
Five, three wastes processing unit
The three wastes comprise waste liquid, waste residues and waste gas, the waste liquid comprises acidic waste liquid and alkaline waste liquid, the waste residues are mainly saline-alkali residues, and the waste gas comprises chlorine-containing waste gas and organic waste gas;
the three-waste treatment unit 50 comprises a waste liquid treatment subunit for treating waste liquid, a waste residue treatment subunit for treating waste residues and a waste gas treatment subunit for treating waste gas;
the waste liquid treatment sub-unit comprises a neutralization kettle 50-G1, a regulating tank 50-G2, an electric flocculation device 50-G3, an electric catalysis device 50-G4, an intermediate water tank 50-G5 and an anaerobic-aerobic tank, the acid waste liquid and the alkaline waste liquid enter a neutralization kettle 50-G1 for neutralization, the upper layer waste liquid is pumped into an adjusting tank 50-G2, the lower layer waste residue enters a waste residue treatment subunit, the water outlet end of the regulating tank 50-G2 is connected with the water inlet end of the electric flocculation device 50-G3, the water outlet end of the electroflocculation device 50-G3 is connected with the water inlet end of the electrocatalysis device 50-G4, the water outlet end of the electro-catalytic device 50-G4 is connected with the water inlet end of the middle water pool 50-G5, the water outlet end of the intermediate water tank 50-G5 is connected with the water inlet end of the anaerobic-aerobic tank.
The waste residue treatment subunit comprises a saline-alkali residue steaming kettle 50-G8 and a saline-alkali residue steaming kettle condenser 50-G9, wherein lower waste residues in the neutralization kettle 50-G1 enter the saline-alkali residue steaming kettle 50-G8 for steam heating, evaporated liquid is condensed and collected through the saline-alkali residue steaming kettle condenser 50-G9, and the remaining saline-alkali residues are bagged and carried away.
The waste gas treatment subunit comprises a multistage water washing mechanism 50-G10, a resin adsorption mechanism 50-G11 and a plant area incinerator 50-G12, wherein chlorine-containing waste gas is washed by the multistage water washing mechanism 50-G10, and is sent to the plant area incinerator 50-G12 for incineration after being adsorbed by the resin adsorption mechanism 50-G11, and organic waste gas is directly sent to the plant area incinerator 50-G12 for incineration.
And an oxidant dosing mechanism 50-G13 is arranged on the electric flocculation device 50-G3.
The waste liquid treatment subunit also comprises a clarifier 50-G14, and the clarifier 50-G14 is arranged between the electric flocculation device 50-G3 and the electric catalysis device 50-G4.
The anaerobic-aerobic pool comprises an anaerobic pool 50-G6 and an aerobic pool 50-G7 which are communicated, a strain rejuvenator 50-G15 is arranged in the anaerobic pool 50-G6 and the aerobic pool 50-G7 respectively, a strain rejuvenation bed is arranged in the strain rejuvenator 50-G15, an inlet of the strain rejuvenator 50-G15 is connected with the middle section of the anaerobic pool 50-G6 or the aerobic pool 50-G7, an outlet of the strain rejuvenator 50-G15 is connected with the front section of the anaerobic pool 50-G6 or the aerobic pool 50-G7, activated sludge is periodically extracted from the middle sections of the anaerobic pool 50-G6 and the aerobic pool 50-G7 through a feeding port to perform strain rejuvenation, and the rejuvenated activated sludge is discharged into the front sections of the anaerobic pool 50-G6 and the aerobic pool 50-G7 through the outlet to realize the rejuvenation of anaerobic bacteria and aerobic bacteria.
Aeration devices are arranged in the regulating tank 50-G2 and the middle water tank 50-G5.
Waste liquid from a factory area is firstly neutralized in a neutralization kettle, upper layer waste liquid is pumped into a regulating tank, the retention time in the regulating tank is 12-24 hours, an aeration device is utilized for stirring, the water quality is homogenized, then the waste liquid is pumped into an electric flocculation device, an oxidant is added into the electric flocculation device, under the action of an electric field, an anode of the electric flocculation device generates electrons to form a 'micro-flocculant', hydroxide of iron or aluminum, suspended particles and colloidal pollutants in water lose stability under the action of the flocculant, and the destabilized pollutant particles and the micro-flocculant collide with each other to combine into macroscopic large flocs. Oxidizing ferrous ions and the like generated by an electrocoagulation reaction into ferric ions by an oxidant so as to avoid the problem of generation of a large amount of foams caused by the traditional aeration oxidation, combining the ferric ions and salts into a flocculating agent to remove part of suspended matters in wastewater, pumping supernatant in the electrocoagulation device into an electrocatalytic device, generating hydroxyl radicals by the electrocatalytic oxidation, decomposing macromolecular substances in the wastewater by utilizing the strong oxidation of the hydroxyl radicals to improve the B/C of the wastewater so as to improve the biodegradability of the wastewater, allowing the electrocatalytic wastewater to flow into an intermediate water tank for buffering, allowing the hydraulic retention time of the intermediate water tank to be 12-24h, stirring by an aeration device to homogenize the water quality, allowing the wastewater to flow into an anaerobic tank, an aerobic tank, an anaerobic tank and a pH control tank to be 25-30 ℃, wherein the pH is controlled to be about 7.5, hanging a combined filler in the tanks, and allowing the combined filler to flow into the anaerobic tank, Heterotrophic bacteria and autotrophic bacteria in the aerobic tank decompose macromolecular organic matters in sewage into micromolecular organic matters, insoluble organic matters are converted into soluble organic matters, an aerator is arranged in the aerobic tank, a Roots blower provides an air source, activated sludge is extracted from the middle sections of the anaerobic tank and the aerobic tank every 36-48 hours through a feed inlet to rejuvenate strains, and the rejuvenated activated sludge is discharged into the front sections of the anaerobic tank and the aerobic tank through an outlet to realize the rejuvenation of anaerobic bacteria and aerobic bacteria. And (3) discharging the excess sludge produced by the system to a sludge tank, performing pressure filtration by a sludge dewatering machine, transporting the treated sludge outside, and returning the filtrate to the regulating tank.
Although the present invention has been described in detail with reference to the foregoing embodiments, it will be apparent to those skilled in the art that changes may be made in the embodiments and/or equivalents thereof without departing from the spirit and scope of the invention. Any modification, equivalent replacement, or improvement made within the spirit and principle of the present invention should be included in the protection scope of the present invention.
Claims (6)
1. A galaxolide production system is characterized by comprising a galaxolide synthesis unit, a pentamethyl indan rectification unit, a pentamethyl indan recovery unit, a galaxolide rectification unit and a three-waste treatment unit;
the galaxolide synthesizing unit comprises a pentamethyl indane synthesizing module, a pentamethyl indanol synthesizing module and a galaxolide synthesizing module;
the pentamethyl indane synthesis module comprises a styrene intermediate tank, an isoamylene intermediate tank, an indane mixing tank, an indane synthesis kettle, an indane standing elevated tank, an indane washing kettle and an indane crude product tank;
the pentamethyl indanol synthesis module comprises an indanol overhead tank, a Jiale mixing tank and an indanol synthesis kettle;
the Jiale musk synthesis module comprises a primary water metering tank, a methylal metering tank, a Jiale synthesis kettle, a Jiale crude product tank, a crude polyaluminium water tank, a polyaluminium water crude steaming tower, a polyaluminium water light component tank, a polyaluminium water steaming kettle buffer tank and a fine polyaluminium water tank;
the styrene intermediate tank and the isoamylene intermediate tank are connected with an indane mixing tank inlet, an indane mixing tank outlet is connected with an indane synthesis kettle, the indane standing elevated tank and the indane washing kettle are sequentially connected, and an indane washing kettle outlet is connected with an indane crude product tank;
the pentamethyl indan rectification unit, the indan elevated tank and the indan alcohol synthesis kettle are sequentially connected, and the Jiale mixing tank is connected with the indan alcohol synthesis kettle;
the indanol synthesis kettle, the primary water metering tank and the methylal metering tank are all connected with an inlet of a Jiale synthesis kettle, an outlet of the Jiale synthesis kettle is connected with a Jiale crude product tank, an outlet of the Jiale crude product tank is respectively connected with a Jiale musk rectification unit and a crude polyaluminium chloride water tank, the crude polyaluminium chloride water tank is connected with an inlet of a polyaluminium chloride water crude distillation tower, an outlet of the polyaluminium chloride water crude distillation tower is respectively connected with a polyaluminium chloride water light component tank and a polyaluminium chloride water kettle, and an outlet of the polyaluminium chloride water kettle is respectively connected with a polyaluminium chloride water kettle buffer tank and a purified polyaluminium chloride water tank;
the pentamethyl indane rectification unit comprises an indane rectification A1 tower bottom, an indane rectification A2 tower bottom, an indane rectification A3 tower bottom, an A2 tower condenser, an A2 tower top reflux tank, an isoamylene dimer storage tank, an A3 tower concentrated drying kettle, an A3 tower condenser, an A3 tower top reflux tank, an indane finished product tank, an indane rectification A4 tower bottom, an A4 tower condenser, a indane recovery front-stage tank and an indane recovery rear-stage tank;
an indan crude product tank of the galaxolide synthesis unit is connected with an inlet of an indan rectification A1 tower kettle, an outlet of the indan rectification A1 tower kettle is respectively connected with an indan rectification A2 tower kettle and an indan rectification A3 tower kettle, the indan rectification A2 tower kettle, an A2 tower condenser, an A2 tower top reflux tank and an isoamylene dimer storage tank are sequentially connected, the indan rectification A3 tower kettle, the A3 tower condenser, an A3 tower top reflux tank and an indan finished product tank are sequentially connected, and the indan rectification A3 tower kettle is further connected with an A3 tower concentrated drying kettle;
an indane recovery groove of the pentamethyl indane recovery unit is connected with an indane rectification A4 tower kettle inlet, an indane rectification A4 tower kettle outlet is connected with an A4 tower condenser, and an A4 tower condenser outlet is respectively connected with an indane recovery front section groove, an indane recovery rear section groove and an indane finished product groove;
the pentamethyl indane recovery unit comprises an indane alkali water tank, an indane washing water tank, an indane recovery kettle, a sulfuric acid tank, a hydrogen peroxide overhead tank and an indane recovery tank;
the front and rear storage tanks of the B tower indane of the sulfuric acid tank, the hydrogen peroxide head tank and the galaxolide rectification unit are all connected with inlets of an indane recycling kettle, outlets of the indane recycling kettle are respectively connected with an indane recycling tank, an indane alkali water tank and an indane washing water tank, and an outlet of the indane recycling tank is connected with a tower kettle of an indane rectification A4 tower of the pentamethyl indane rectification unit;
the galaxolide rectification unit comprises a galaxolide rectification B tower kettle, a de-heavy tower kettle, a galaxolide first-stage groove, a galaxolide second-stage groove, a galaxolide finished product groove, a water flushing kettle, a galaxolide finished product tower kettle, a galaxolide stock solution front and back groove, a galaxolide stock solution groove, a stock solution overhead groove, a B tower water head groove, a chloropropanol reaction kettle, a B tower chlorobenzene front and back section groove, a B tower chlorobenzene front and back section storage tank, a B tower chlorobenzene finished product section groove, a B tower chlorobenzene front and back section groove, a B tower indan front and back section storage tank, a B tower indan finished product section groove, a B tower indan finished product section storage tank, a byproduct groove, a chlorobenzene tower kettle, a chlorobenzene tower water head section groove, a chlorobenzene front and back section groove, a light component receiving groove and an alkali washing tank;
the Jiale crude product groove of the Jiale musk synthesis unit is connected with the inlet of a Jiale musk rectification B tower kettle, the outlet of the Jiale musk rectification B tower kettle is respectively connected with a B tower water head groove, a B tower chlorobenzene front and back section groove, a B tower chlorobenzene finished product section groove, a B tower indan front and back section groove, a B tower indan finished product section groove and a byproduct groove, the outlet of the B tower water head groove is connected with a chloropropanol reaction kettle, the B tower chlorobenzene front and back section groove, the B tower chlorobenzene front and back section storage tank and a chlorobenzene tower kettle are sequentially connected, the outlet of the chlorobenzene tower kettle is respectively connected with a chlorobenzene tower water head section groove and a chlorobenzene front and back section groove, the chlorobenzene tower water head section groove is connected with the chloropropanol reaction kettle, the outlet of the chloropropanol reaction kettle is respectively connected with a light component receiving tank and an alkaline washing tank, the front and back section groove is connected with a B tower chlorobenzene finished product section storage tank, the outlet of the B tower chlorobenzene section groove is connected with a chlorobenzene finished product storage tank, the tower B indane front-and-back section groove, the tower B indane front-and-back section storage tank and the indane recovery kettle are sequentially connected, and an outlet of the tower B indane finished product section groove is connected with the tower B indane finished product section storage tank;
the outlet of the Jiale musk rectification B tower kettle is connected with a de-emphasis tower kettle, the outlet of the de-emphasis tower kettle is respectively connected with a Jiale first-stage groove, a Jiale second-stage groove and a Jiale finished product groove, the outlet of the Jiale first-stage groove is connected with a Jiale musk rectification B tower, the outlet of the Jiale second-stage groove is connected with a de-emphasis tower kettle, the Jiale finished product groove, a water flushing kettle and a Jiale finished product tower kettle are sequentially connected, the outlet of the Jiale finished product tower kettle is respectively connected with a Jiale stock solution front-back groove and a Jiale stock solution groove, the Jiale stock solution groove is connected with a stock solution overhead groove, and the Jiale stock solution front-back groove is connected with the de-emphasis tower kettle;
the three wastes comprise waste liquid, waste residues and waste gas, the waste liquid comprises acidic waste liquid and alkaline waste liquid, the waste residues are mainly saline-alkali residues, and the waste gas comprises chlorine-containing waste gas and organic waste gas;
the three-waste treatment unit comprises a waste liquid treatment subunit for treating waste liquid, a waste residue treatment subunit for treating waste residues and a waste gas treatment subunit for treating waste gas;
the waste liquid treatment subunit comprises a neutralization kettle, an adjusting tank, an electric flocculation device, an electro-catalysis device, an intermediate water tank and an anaerobic-aerobic tank, wherein the acidic waste liquid and the alkaline waste liquid enter the neutralization kettle for neutralization, the upper layer waste liquid is pumped into the adjusting tank, the lower layer waste residue enters the waste residue treatment subunit, the water outlet end of the adjusting tank is connected with the water inlet end of the electric flocculation device, the water outlet end of the electric flocculation device is connected with the water inlet end of the electro-catalysis device, the water outlet end of the electro-catalysis device is connected with the water inlet end of the intermediate water tank, and the water outlet end of the intermediate water tank is connected with the water inlet end of the anaerobic-aerobic tank.
2. The galaxolide production system as claimed in claim 1, wherein the waste residue treatment sub-unit comprises a salt and alkali residue steaming kettle and a salt and alkali residue steaming kettle condenser, wherein lower waste residue in the neutralization kettle is heated by steam in the salt and alkali residue steaming kettle, evaporated liquid is condensed and collected by the salt and alkali residue steaming kettle condenser, and the remaining salt and alkali residue is bagged and transported away.
3. The galaxolide production system according to claim 1, wherein the waste gas treatment subunit comprises a multi-stage water washing mechanism, a resin adsorption mechanism and a plant incinerator, wherein chlorine-containing waste gas is washed by the multi-stage water washing mechanism and adsorbed by the resin adsorption mechanism and then sent to the plant incinerator for incineration, and organic waste gas is directly sent to the plant incinerator for incineration.
4. The galaxolide production system according to claim 1, wherein an oxidant feeding mechanism is arranged on the electroflocculation device; the waste liquid treatment subunit also comprises a clarifier which is arranged between the electric flocculation device and the electric catalysis device.
5. The galaxolide production system according to claim 1, wherein the anaerobic-aerobic tank comprises an anaerobic tank and an aerobic tank which are communicated with each other, a strain rejuvenating device is respectively arranged in the anaerobic tank and the aerobic tank, a strain rejuvenating bed is arranged in the strain rejuvenating device, an inlet of the strain rejuvenating device is connected with the middle section of the anaerobic tank or the aerobic tank, and an outlet of the strain rejuvenating device is connected with the front section of the anaerobic tank or the aerobic tank.
6. The galaxolide production system according to claim 1, wherein aeration devices are disposed in the adjusting tank and the intermediate water tank.
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| CN114085124A (en) * | 2021-11-17 | 2022-02-25 | 安徽金轩科技有限公司 | Industrial impurity removal method for prophase waste liquid of Jiale musk chlorobenzene |
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