CN102675084A - A method for producing adipic acid by using waste polyurethane soles - Google Patents
A method for producing adipic acid by using waste polyurethane soles Download PDFInfo
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- CN102675084A CN102675084A CN2012101089687A CN201210108968A CN102675084A CN 102675084 A CN102675084 A CN 102675084A CN 2012101089687 A CN2012101089687 A CN 2012101089687A CN 201210108968 A CN201210108968 A CN 201210108968A CN 102675084 A CN102675084 A CN 102675084A
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/50—Improvements relating to the production of bulk chemicals
- Y02P20/582—Recycling of unreacted starting or intermediate materials
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
- Y02W30/00—Technologies for solid waste management
- Y02W30/50—Reuse, recycling or recovery technologies
- Y02W30/62—Plastics recycling; Rubber recycling
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Abstract
The invention relates to a method for producing adipic acid by using waste polyurethane soles. The method comprises the following steps: a) crushing the waste polyurethane soles, and adding water, inorganic acids and silver salt to conduct catalytic degradation; b) dropwise adding inorganic alkali to a reactor through a head tank to adjust the pH to be 6.8-7.5; c) adding inorganic acid to enable the adipic acid to be precipitated, centrifuging, and drying to obtain the adipic acid with purity of more than 99%.The method provided by the invention uses the waste polyurethane soles as raw material to produce the adipic acid and glycol, solves the problem of recycling the waste polyurethane soles, is environmentally friendly, and can reduce production cost. Compared with classical chemical synthesis method, the method can reduce the cost by 5,000 yuan/ton with good economic benefits. The reaction condition is mild without high temperature and pressure. The yield of the adipic acid reaches more than 35% by accounting on basis of the waste polyurethane soles amount. The quality of the product is good, and the by-product glycol can be used as solvent or other industrial raw material. The amount of generated wastewater is small, the wastewater is tractable and discharge standard can be fully met.
Description
Technical field
The invention belongs to chemical field, specifically relate to a kind of technology of utilizing waste polyurethane shoe sole production hexanodioic acid.
Background technology
Hexanodioic acid (ADA) is a kind of important organic dibasic acid, is commonly called as adipic acid, is mainly used in to make nylon 66 fiber and Nylon 66; Urethane foam; In organic synthesis industry, be the basic material of adiponitrile, hexanediamine, also can be used for producing lubricant, softening agent Octyl adipate simultaneously; Also can be used for aspects such as medicine, purposes very extensively.
The working method of hexanodioic acid has four kinds of phynol method, hexanaphthene method, tetrahydrobenzene method and butadiene processs etc. at present, and before the fifties, phynol method is mainly adopted in hexanodioic acid production, at first with phenol hydrogenation, at Ni-A1
2O
3Effect under, in 95～130 ℃ down reaction generate hexalin, further dehydrogenation generates pimelinketone again, pimelinketone gets hexanodioic acid with atmospheric oxidation in acetate.The advantage of this method is that product purity is high, and production technology is ripe, and equipment need not stainless material.But phenol resource-constrained and costing an arm and a leg, product cost is high, and is superseded basically at present.Existing industrial production mainly adopts the hexanaphthene method, has also developed tetrahydrobenzene method and butadiene process.
(1) hexanaphthene method
Refining benzene generates hexanaphthene through shortening, and hexanaphthene generates KA oil (mixture that mainly contains pimelinketone and hexalin) through atmospheric oxidation, generates hexanodioic acid through the further oxidation of nitric acid again.Different according to the catalyzer that adopts, traditional hexanaphthene two-step oxidation technology can be divided into three types again: cobalt catalyst oxidation style, B catalyst oxidation style and catalyst-free oxidation style.(i) cobalt catalyst oxidation system hexanodioic acid is the method for exploitation of the forties du pont company and use, is still adopted by external many companies so far.This law technology is ripe, and is simple to operate, but yield is lower, and the slagging scorification problem is arranged.(ii) make the yield that catalyzer can improve hexalin with boric acid or boron trioxide.Hexanaphthene is oxidized to the boric acid ester of hexalin in the presence of boric acid, be hydrolyzed into hexalin then.The thermostability of boric acid ester is high, is difficult for oxidation, thereby can avoid hexalin to decompose, and hexalin content is high in the oxidation gained keto-alcohol mixture, thereby improves the cyclohexane oxidation effect.This method yield is higher, but operational path is complicated, poor continuity, and economical effectiveness is not satisfactory.(iii) the catalyst-free oxidation style is the technology of Rhone-Poulenc's exploitation, and it has the above two advantage concurrently, and oxidizing condition is gentle, and the by product of reaction is less, and selectivity and yield are higher.The raw material of cyclohexane oxidation technology also relates to hydrogen, nitric acid etc. except that refining benzene, technical process is long, and disposable fund input is big, and by product is more, has industrial triwaste pollution, and product yield is not high, but this technical maturity is that the method that extensively adopts is gone up in industry at present.The raw material of cyclohexane oxidation technology also relates to hydrogen, nitric acid etc. except that refining benzene, technical process is long, and disposable fund input is big, and by product is more, has industrial triwaste pollution, and product yield is not high.
(2) butadiene process
With divinyl and carbon monoxide is raw material, makes divinyl be converted into the 3-amylene-4 acid methyl ester earlier, generates dimethyl adipate through carbonylation again, after hydrolysis makes hexanodioic acid.Butadiene process also comprises divinyl hydrocarboxylation and divinyl hydrocyanation etc.Butadiene process has been broken traditional benzene hydrogenation method, uses cheap carbon four instead and makes raw material, and the product hexanodioic acid content that obtains is high, and yield is high, and cost is low than the hexanaphthene method, but energy consumption is high, and complex operation conversion unit is required height, and technology is immature.
(3) tetrahydrobenzene method
Adopt special catalyst to select hydrogenation to generate tetrahydrobenzene to benzene, cyclohexene hydration generates hexalin, generates hexanodioic acid through nitric acid oxidation again.This method hydrogen consumption in producing the hexalin process is less.By product is a hexanaphthene, and the process that generates hexalin does not almost have three-waste pollution, good product quality, and yield is higher, and production cost is relatively low, but has catalyst type many, costs an arm and a leg, and produces the shortcoming that a large amount of need are buried the waste residue of processing (annual tens tons).
(polyurethane(s) Polyurethane is to have on the one type of main chain that is made by polyvalent alcohol and isocyanate reaction-general name of the polymkeric substance of NHCOO-repeating unit PU) to urethane.The kind that changes polyvalent alcohol or isocyanic ester can obtain from liquid to the solid, the polymeric articles of and performance dissimilar from the soft fields such as coating, tackiness agent, plastics and rubber that are applied to hard.But urethane has become present Application Areas one of macromolecular material the most widely with its excellent physicals, good processed-type, good resistant to chemical media and ageing-resistant performance, and among the scope of its output and application constantly enlarging.But be accompanied by the expansion of production-scale expansion and Application Areas, in polyurethane production and use, produced a large amount of refuses, comprising a large amount of polyurethane foams that are used for heat insulation and Sofa cushion, waste polyurethane sole, waste polyurethane leather etc.Iff is handled these waste materials through the method for landfill and burning, and not only land occupation, and contaminate environment also is a kind of waste to resource simultaneously.Therefore, the recycling problem of urethane has been that polyurethane industrial presses for one of significant problem of solution, and waste polyurethane is carried out recycling, reduces environmental pollution, reduces the production cost of new product simultaneously, has realistic meaning.
The recycling of urethane mainly contains 3 kinds of modes, both physics method, chemical method and energy law.Existing many reports of physics method and practical technique, the product properties of the urethane gained of recovery is relatively poor, only is applicable to low-grade goods; Energy recovery is to reclaim heat through waste material is burned, and this mode can cause secondary pollution, does not re-use basically; The main method of urethane recycling at present is a chemical recycling, promptly under chemical reagent, catalyzer, heat existence condition, degradation of polyurethane is become the oligopolymer or the micromolecular compound that can utilize again, thereby realizes the recycle of waste.Different according to the kind of degradation agents and degradation condition, chemical recycling can be divided into hydrolysis method, alkaline hydrolysis method, amine-decomposing method, alcoholysis method etc.Wherein, hydrolysis method is under 250～350 ℃ of temperature, high-pressure water vapor and polyurethane reaction, but hydrolysis temperature is higher, the difficult purifying of polyvalent alcohol, and expense is high; The alkaline hydrolysis method adopts basic metal or alkaline earth metal hydroxides and polyurethane reaction, purifies through complicated separation, can obtain polyether glycol, but technology is long, and therefore the range request high temperature alkaline condition of crossing owing to reaction requires height to business equipment, and production cost is high; Amine-decomposing method decomposes polyurethane foam in amine; From urethane or urethane (urea), decompose and generate the lower hydroxyl of relative molecular mass and the compound and the non-replacement urea of amido; The ammonia hydrolysis products that obtains often is used as the polyurethane semihard foam catalyzer; But because its condition is harsh, industrial technology is still immature, and the ammonia of polyurethane waste material is separated the laboratory study stage that also only is at present; Alcoholysis method is applicable to multiple urethane, and reaction can be carried out under the condition of normal pressure, middle temperature, and the mode of the excessive available underpressure distillation of alcoholysis agent is separated; This method is used comparatively extensive, but sees from economy and technical standpoint, and alcoholysis method reclaims and relates to the solvent recuperation rectification process; Power consumption is high, and cost is high.
Summary of the invention
The object of the present invention is to provide a kind of effectively save energy and the technology of producing hexanodioic acid, and adopted this technology to can be good at solving the recovery problem of waste polyurethane sole, thereby obtained good environmental benefit and economic benefit.
The object of the invention can be realized through following technical scheme:
A kind of technology of utilizing waste polyurethane shoe sole production hexanodioic acid, this preparation technology may further comprise the steps:
A) DeR
The waste polyurethane sole that washes is broken into bulk or the strip shape body of 2.5～5.5cm, drops in the glassed steel reaction vessels, add 15%～25% mineral acid of 1.2～1.5 times of water and the urethane quality of material of urethane quality of material; Stir, heating is when feed temperature rises to 75 ℃～90 ℃; Add the silver catalyst agent; Continued to be warming up to 95 ℃～105 ℃ DeRs 3～5 hours, between degradative phase, the acid content of period sampling measuring degradation solution; Make the reaction solution acid content be not less than 6.5%, be cooled to below 60 ℃ subsequent use after DeR is accomplished;
B) neutralization reaction
With above-mentioned DeR liquid filtering and impurity removing; Drop in the neutralization reaction still, stir, inorganic alkali solution is dropped in the reaction kettle through header tank; Regulate pH value to 6.8～7.5, contain the hexanodioic acid aqueous solution of generation and the ethylene glycol mixture of degraded generation this moment in the solution;
C) acid out, whiz
Above-mentioned neutralizer is dropped in the acid precipitation reaction still; Stir, 20%～25% mineral acid that drops into above-mentioned neutralizer quality is separated out hexanodioic acid, acid out 4～8 hours; Centrifugal; Drying obtains purity greater than 99% hexanodioic acid, and mother liquor drops into the precipitation liquid bath and reclaims upper solution and obtain terepthaloyl moietie, and lower floor's mother liquor treats that blanking applies mechanically.
Described silver catalyst agent is one or more of Silver monoacetate, Sulfuric acid disilver salt, silver carbonate, Silver Nitrate, silver nitrite, silver perchlorate, silver chlorate, Silver monochloride, tachyol, Silver monobromide or Silver monoiodide.
Described silver catalyst agent consumption is 0.0002%～0.0005% of a urethane quality of material.
Described mineral alkali is one or more in alkali metal hydroxide, alkali metal hydrocarbonate and the alkaline carbonate, and said mineral acid is one or both in sulfuric acid or the hydrochloric acid.
Preferably, the preferred sodium hydroxide of described mineral alkali, mineral acid described in the step a) is a sulfuric acid, mineral acid described in the step c) is a hydrochloric acid.
Synthesis technique of the present invention compared with prior art has the following advantages:
(1) the present invention can be good at solving the recovery problem of waste polyurethane sole, and to adopt the waste polyurethane sole be raw material production hexanodioic acid and terepthaloyl moietie, thereby has obtained good environmental benefit and economic benefit;
(2) reaction conditions of the present invention is gentle, need not HTHP, degradation of polyurethane rate high (reaching more than 95%); The product yield is at (in the waste polyurethane sole) more than 35%; Good product quality (content is more than 99%) reduce by 5000 yuan/ton than the chemical synthesis cost of classics, and by product terepthaloyl moietie can be used as solvent or other uses industrial raw material; And the wastewater flow rate that produces is few, and waste water is prone to processing qualified discharge fully.
Embodiment
For the present invention is further described, sets forth with concrete embodiment below, but can not be interpreted as restriction scope of the present invention.
Embodiment 1:
A) DeR
The waste polyurethane sole that washes is broken into bulk or the strip shape body of 2.5～5.5cm, takes by weighing 1000kg and drop in the 5000L glassed steel reaction vessels, add 1500kg water and 150kg sulfuric acid; Stir, heating is when feed temperature rises to 75 ℃～90 ℃; Add catalyst sulfuric acid silver 5g; Continued to be warming up to 95 ℃～105 ℃ DeRs 3 hours, between degradative phase, the acid content of period sampling measuring degradation solution; Make the reaction solution acid content be not less than 6.5%, be cooled to below 60 ℃ subsequent use after DeR is accomplished;
B) neutralization reaction
Reacting liquid filtering removal of impurities with above-mentioned degraded; Drop in the neutralization reaction still of 5000L; Stir; Sodium hydroxide 132.5kg is added water be mixed with 30% solution and drop in the reaction kettle, regulate pH value to 6.8～7.5, contain the hexanodioic acid aqueous solution of generation and the ethylene glycol mixture of degraded generation this moment in the solution through header tank;
C) acid out, whiz
Above-mentioned neutralizer is dropped in the acid precipitation reaction still of 5000L, stir, drop into 618kg hydrochloric acid hexanodioic acid is separated out; Acid out 8 hours, centrifugal, it is 99.5% hexanodioic acid 350kg that drying obtains purity; Mother liquor drops into the precipitation liquid bath and reclaims upper solution and obtain terepthaloyl moietie, and lower floor's mother liquor treats that blanking applies mechanically.
Embodiment 2:
A) DeR
The waste polyurethane sole that washes is broken into bulk or the strip shape body of 2.5～5.5cm, takes by weighing 1000kg and drop in the 5000L glassed steel reaction vessels, add 1200kg water and 250kg sulfuric acid; Stir, heating is when feed temperature rises to 75 ℃～90 ℃; Add catalyst sulfuric acid silver 2g; Continued to be warming up to 95 ℃～105 ℃ DeRs 3.5 hours, between degradative phase, the acid content of period sampling measuring degradation solution; Make the reaction solution acid content be not less than 6.5%, be cooled to below 60 ℃ subsequent use after DeR is accomplished;
B) neutralization reaction
Reacting liquid filtering removal of impurities with above-mentioned degraded; Drop in the neutralization reaction still of 5000L; Stir; Sodium hydroxide 159kg is added water be mixed with 30% solution and drop in the reaction kettle, regulate pH value to 6.8～7.5, contain the hexanodioic acid aqueous solution of generation and the ethylene glycol mixture of degraded generation this moment in the solution through header tank;
C) acid out, whiz
Above-mentioned neutralizer is dropped in the acid precipitation reaction still of 5000L, stir, drop into 745kg hydrochloric acid hexanodioic acid is separated out; Acid out 4 hours, centrifugal, it is 99.8% hexanodioic acid 354kg that drying obtains purity; Mother liquor drops into the precipitation liquid bath and reclaims upper solution and obtain terepthaloyl moietie, and lower floor's mother liquor treats that blanking applies mechanically.
Embodiment 3:
A) DeR
The waste polyurethane sole that washes is broken into bulk or the strip shape body of 2.5～5.5cm, takes by weighing 1000kg and drop in the 5000L glassed steel reaction vessels, add 1350kg water and 200kg concentrated hydrochloric acid; Stir, heating is when feed temperature rises to 75 ℃～90 ℃; Add catalyzer silver perchlorate 4.5g; Continued to be warming up to 95 ℃～105 ℃ DeRs 5 hours, between degradative phase, the acid content of period sampling measuring degradation solution; Make the reaction solution acid content be not less than 6.5%, be cooled to below 60 ℃ subsequent use after DeR is accomplished;
B) neutralization reaction
Reacting liquid filtering removal of impurities with above-mentioned degraded; Drop in the neutralization reaction still of 5000L; Stir; Sodium hydroxide 140kg is added water be mixed with 25% solution and drop in the reaction kettle, regulate pH value to 6.8～7.5, contain the hexanodioic acid aqueous solution of generation and the ethylene glycol mixture of degraded generation this moment in the solution through header tank;
C) acid out, whiz
Above-mentioned neutralizer is dropped in the acid precipitation reaction still of 5000L; Stir, drop into 612kg sulfuric acid hexanodioic acid is separated out, acid out 4 hours; Centrifugal; Drying obtains purity greater than 99.8% hexanodioic acid 355kg, and mother liquor drops into the precipitation liquid bath and reclaims upper solution and obtain terepthaloyl moietie, and lower floor's mother liquor treats that blanking applies mechanically.
Embodiment 4:
A) DeR
The waste polyurethane sole that washes is broken into bulk or the strip shape body of 2.5～5.5cm, takes by weighing 1000kg and drop in the 5000L glassed steel reaction vessels, add 1200kg water and 250kg hydrochloric acid; Stir, heating is when feed temperature rises to 75 ℃～90 ℃; Add catalyzer Silver monobromide 3.5g; Continued to be warming up to 95 ℃～105 ℃ DeRs 3.5 hours, between degradative phase, the acid content of period sampling measuring degradation solution; Make the reaction solution acid content be not less than 6.5%, be cooled to below 60 ℃ subsequent use after DeR is accomplished;
B) neutralization reaction
Reacting liquid filtering removal of impurities with above-mentioned degraded; Drop in the neutralization reaction still of 5000L; Stir; Sodium hydroxide 125kg is added water be mixed with 30% solution and drop in the reaction kettle, regulate pH value to 6.8～7.5, contain the hexanodioic acid aqueous solution of generation and the ethylene glycol mixture of degraded generation this moment in the solution through header tank;
C) acid out, whiz
Above-mentioned neutralizer is dropped in the acid precipitation reaction still of 5000L, stir, drop into 600kg hydrochloric acid hexanodioic acid is separated out; Acid out 6 hours, centrifugal, it is 99.5% hexanodioic acid 357kg that drying obtains purity; Mother liquor drops into the precipitation liquid bath and reclaims upper solution and obtain terepthaloyl moietie, and lower floor's mother liquor treats that blanking applies mechanically.
Embodiment 5:
A) DeR
The waste polyurethane sole that washes is broken into bulk or the strip shape body of 2.5～5.5cm, takes by weighing 1000kg and drop in the 5000L glassed steel reaction vessels, add 1500kg water and 150kg sulfuric acid; Stir, heating is when feed temperature rises to 75 ℃～90 ℃; Add catalyst sulfuric acid silver 5g; Continued to be warming up to 95 ℃～105 ℃ DeRs 5 hours, between degradative phase, the acid content of period sampling measuring degradation solution; Make the reaction solution acid content be not less than 6.5%, be cooled to below 60 ℃ subsequent use after DeR is accomplished;
B) neutralization reaction
Reacting liquid filtering removal of impurities with above-mentioned degraded; Drop in the neutralization reaction still of 5000L; Stir; Pottasium Hydroxide 186kg is added water be mixed with 30% solution and drop in the reaction kettle, regulate pH value to 6.8～7.5, contain the hexanodioic acid aqueous solution of generation and the ethylene glycol mixture of degraded generation this moment in the solution through header tank;
C) acid out, whiz
Above-mentioned neutralizer is dropped in the acid precipitation reaction still of 5000L, stir, drop into 618kg hydrochloric acid hexanodioic acid is separated out; Acid out 6 hours, centrifugal, it is 99.6% hexanodioic acid 362kg that drying obtains purity; Mother liquor drops into the precipitation liquid bath and reclaims upper solution and obtain terepthaloyl moietie, and lower floor's mother liquor treats that blanking applies mechanically.
Embodiment 6:
A) DeR
The waste polyurethane sole that washes is broken into bulk or the strip shape body of 2.5～5.5cm, takes by weighing 1000kg and drop in the 5000L glassed steel reaction vessels, add 1200kg water and 200kg sulfuric acid; Stir, heating is when feed temperature rises to 75 ℃～90 ℃; Add catalyst sulfuric acid silver 3.5g; Continued to be warming up to 95 ℃～105 ℃ DeRs 4 hours, between degradative phase, the acid content of period sampling measuring degradation solution; Make the reaction solution acid content be not less than 6.5%, be cooled to below 60 ℃ subsequent use after DeR is accomplished;
B) neutralization reaction
Reacting liquid filtering removal of impurities with above-mentioned degraded; Drop in the neutralization reaction still of 5000L; Stir; Sodium hydroxide 140kg is added water be mixed with 30% solution and drop in the reaction kettle, regulate pH value to 6.8～7.5, contain the hexanodioic acid aqueous solution of generation and the ethylene glycol mixture of degraded generation this moment in the solution through header tank;
C) acid out, whiz
Above-mentioned neutralizer is dropped in the acid precipitation reaction still of 5000L, stir, drop into 645kg hydrochloric acid hexanodioic acid is separated out; Acid out 5 hours, centrifugal, it is 99.6% hexanodioic acid 358kg that drying obtains purity; Mother liquor drops into the precipitation liquid bath and reclaims upper solution and obtain terepthaloyl moietie, and lower floor's mother liquor treats that blanking applies mechanically.
Content disclosed according to the present invention, those skilled in the art can use the present invention to greatest extent.Therefore, above-mentioned preferred embodiment only illustrates, but not limits scope of the present invention by any way.
Claims (5)
1. technology of utilizing waste polyurethane shoe sole production hexanodioic acid, it is characterized in that: this preparation technology may further comprise the steps:
A) DeR
The waste polyurethane sole that washes is broken into bulk or the strip shape body of 2.5～5.5cm, drops in the glassed steel reaction vessels, add 15%～25% mineral acid of 1.2～1.5 times of water and the urethane quality of material of urethane quality of material; Stir, heating is when feed temperature rises to 75 ℃～90 ℃; Add the silver catalyst agent; Continued to be warming up to 95 ℃～105 ℃ DeRs 3～5 hours, between degradative phase, the acid content of period sampling measuring degradation solution; Make the reaction solution acid content be not less than 6.5%, be cooled to below 60 ℃ subsequent use after DeR is accomplished;
B) neutralization reaction
With above-mentioned DeR liquid filtering and impurity removing; Drop in the neutralization reaction still, stir, inorganic alkali solution is dropped in the reaction kettle through header tank; Regulate pH value to 6.8～7.5, contain the hexanodioic acid aqueous solution of generation and the ethylene glycol mixture of degraded generation this moment in the solution;
C) acid out, whiz
Above-mentioned neutralizer is dropped in the acid precipitation reaction still; Stir, 20%～25% mineral acid that drops into above-mentioned neutralizer quality is separated out hexanodioic acid, acid out 4～8 hours; Centrifugal; Drying obtains purity greater than 99% hexanodioic acid, and mother liquor drops into the precipitation liquid bath and reclaims upper solution and obtain terepthaloyl moietie, and lower floor's mother liquor treats that blanking applies mechanically.
2. a kind of technology of utilizing waste polyurethane shoe sole production hexanodioic acid according to claim 1 is characterized in that: described silver catalyst agent is one or more of Silver monoacetate, Sulfuric acid disilver salt, silver carbonate, Silver Nitrate, silver nitrite, silver perchlorate, silver chlorate, Silver monochloride, tachyol, Silver monobromide or Silver monoiodide.
3. a kind of technology of utilizing waste polyurethane shoe sole production hexanodioic acid according to claim 1 and 2 is characterized in that: described silver catalyst agent consumption is 0.0002%～0.0005% of a urethane quality of material.
4. a kind of technology of utilizing waste polyurethane shoe sole production hexanodioic acid according to claim 1; It is characterized in that: described mineral alkali is one or more in alkali metal hydroxide, alkali metal hydrocarbonate and the alkaline carbonate, and said mineral acid is one or both in sulfuric acid or the hydrochloric acid.
5. according to claim 1 or 4 described a kind of technologies of utilizing waste polyurethane shoe sole production hexanodioic acid, it is characterized in that: the preferred sodium hydroxide of described mineral alkali, the preferably sulfuric acid of mineral acid described in the step a), the preferred hydrochloric acid of mineral acid described in the step c).
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN115260579A (en) * | 2022-08-12 | 2022-11-01 | 浙江工业大学 | Application of metal compound catalyst in catalysis of acidolysis reaction of waste polyurethane foam |
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| US4605762A (en) * | 1982-04-23 | 1986-08-12 | Celanese Mexicana S.A. | Depolymerization of condensation polymers |
| WO2002010228A2 (en) * | 2000-07-27 | 2002-02-07 | E.I. Dupont De Nemours And Company | Transformation of polymers to useful chemicals by oxidation |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN115260579A (en) * | 2022-08-12 | 2022-11-01 | 浙江工业大学 | Application of metal compound catalyst in catalysis of acidolysis reaction of waste polyurethane foam |
| CN115260579B (en) * | 2022-08-12 | 2023-09-05 | 浙江工业大学 | Application of metal compound catalyst in catalyzing acidolysis reaction of waste polyurethane foam |
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