CN202984265U - Disposal system used for solid salt waste in production of triglycidyl isocyanurate (TGIC) - Google Patents
Disposal system used for solid salt waste in production of triglycidyl isocyanurate (TGIC) Download PDFInfo
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- CN202984265U CN202984265U CN 201220639790 CN201220639790U CN202984265U CN 202984265 U CN202984265 U CN 202984265U CN 201220639790 CN201220639790 CN 201220639790 CN 201220639790 U CN201220639790 U CN 201220639790U CN 202984265 U CN202984265 U CN 202984265U
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- solid salt
- drying device
- heat
- glycidyl ester
- isocyanuric acid
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Abstract
The utility model discloses a disposal system used for solid salt waste in production of triglycidyl isocyanurate (TGIC). The disposal system used for the solid waste in the production of the TGIC comprises a filter unit used for filtering a mixture in a cyclization reaction still after a reaction is accomplished, and further comprises a dryer and an organic matter recovery unit, wherein the dryer is used for performing heating treatment on residual solid salt waste after the mixture is filtered through the filter unit, and the organic matter recovery unit is used for performing condensation recovery on escaping gas when the heating treatment is performed. Through the heating treatment on the solid salt waste obtained through filtering on the mixture in the dryer, organic matters and moisture in the solid salt waste are enabled to evaporate after being heated, salinity in the solid salt waste is enabled to be separated from other constituents in the solid salt waste, the organic matters escaped through evaporation are recovered and then utilized respectively, and therefore effective treatment is performed on the solid salt waste.
Description
Technical field
The utility model relates to the isocyanuric acid three-glycidyl ester production field, is specifically related to a kind of for the solid salt treatment of wastes produced system of isocyanuric acid three-glycidyl ester production.
Background technology
Isocyanuric acid three-glycidyl ester (TGIC) is a kind of neo-epoxy resin, has good heat resistance, weatherability, caking property and electrical properties in high temperatures, high to acid, alkali and other chemicals stability, has good especially crosslinking curing performance.Be containing one of most important curing agent of carboxyl functional group base-material, be particularly useful for the curing agent of powdery paints carboxyl polyester.
The production technology that TGIC is generally used as shown in Figure 1, being about to epoxychloropropane (ECH), cyanuric acid (CA) adds according to a certain ratio in reactor and carries out synthetic reaction with appropriate catalyst, obtain intermediate product 1,3,5-tri-(1 '-chloro-2 '-hydroxyl-propyl) chlorinated isocyanurates, again intermediate product and solid sodium hydroxide generation cyclization are obtained to the mixture that contains TGIC, this mixture after filtration, can make the TGIC finished product after the operation such as distillation, crystallization, granulation, oven dry.Although this technique can effectively be produced the TGIC finished product, it can produce a large amount of solid salt refuses in process of production, and the complicated component of these solid salt refuses, comprise NaCl, ECH, H
2the Multiple components such as O, especially ECH are poisonous volatile substances, as directly toppled over or landfill, will inevitably destroy ecological environment, contaminated soil.Therefore, how to process for a long time solid salt refuse and become the technical barrier that TGIC produces.
At present, the scheme that solid salt refuse is processed of having reported mainly adopts burning disposal or organic solvent extraction to process, wherein scheme is preferably: name is called " research of TGIC process for cleanly preparing ", Feng Deli, Deng. Speciality Petrochemicals progress .2007, 8 (1): in the document of 56-58, disclosed employing adds the ECH that suction filtration is removed in solid salt refuse after methanol extraction and makes industrial salt (referring to its open file Fig. 1), although the method can effectively be removed the ECH organic matter in solid salt refuse, but the NaCl rate of recovery is low, Gu because also contain the moisture contained in part moisture and methyl alcohol in the salt refuse, therefore can make part NaCl soluble in water, be difficult to reclaim.In addition, along with the reuse number of times raising of extracting mother liquid, produce the salt rate and also descend.Simultaneously, from industrialization angle Nacl itself, be worth not highly, the cost of methyl alcohol or ethanol extraction technique is high, operate comparatively loaded down with trivial detailsly, so is difficult to carry out industrial applications.
Summary of the invention
The purpose of this utility model is to provide a kind of for the solid salt treatment of wastes produced system of isocyanuric acid three-glycidyl ester production, and the solid salt refuse produced in can producing TGIC be processed, and improves the economic benefit of TGIC production.
A kind of for the solid salt treatment of wastes produced system of isocyanuric acid three-glycidyl ester production, comprise the filter filtered for the mixture after reaction in the cyclization still is finished, it is characterized in that: this system also comprises after filter is filtered the organic matter recovery unit that remaining solid salt refuse carries out the drying device of heat treated and escaping gas carries out the condensation recovery during to heat treated, and described organic matter recovery unit comprises escaping gas in drying device is carried out to the condenser of condensation and the liquid trap that the liquid of condensation is reclaimed.
In the application, carry out heat treated by drying device, mixture being filtered to the solid salt refuse obtained, make organic matter and moisture in solid salt refuse be subject to thermal evaporation, thereby make the salinity in solid salt refuse be separated with other components, and the organic matter that evaporation is overflowed is reclaimed, and then utilized respectively, thereby solid salt refuse is effectively processed.
The accompanying drawing explanation
Fig. 1 is the production technological process that TGIC is traditional;
Fig. 2 is structural representation of the present utility model.
The specific embodiment
The application's purpose is to provide a kind of and produces solid salt treatment of wastes produced system for isocyanuric acid three-glycidyl ester.So far in TGIC production, solid salt refuse can not get effective processing, its reason mainly contain following some: in first TGIC production process, produce to produce the organic species number and the number change that contain in solid salt refuse larger for each batch, therefore the salt refuse is not a stable mixture formed admittedly, therefore can not directly as product or raw material, be applied; It two is in prior art, also not find to carry out effectively separating to solid salt refuse reclaim and each component reclaimed carried out to the approach effectively utilized, and therefore mostly adopts to burn or calcining is processed.The scheme adopted in the application, as shown in Figure 2, the solid salt treatment of wastes produced system of a kind of production for isocyanuric acid three-glycidyl ester, comprise the filter 13 filtered for the mixture to after the interior reaction end of cyclization still 12, this system also comprises after filter 13 is filtered the organic matter recovery unit 30 that remaining solid salt refuse carries out the drying device 14 of heat treated and escaping gas carries out the condensation recovery during to heat treated, described organic matter recovery unit 30 comprises the interior escaping gas of drying device 14 is carried out to the condenser of condensation and the liquid trap that the liquid of condensation is reclaimed.Like this by solid salt refuse being carried out to heat treated drying device 14 is interior, make the organic phase in solid salt refuse evaporate and separate with moisture, thereby obtain the dry salt that volatile content is extremely low, because dry salt volatile content is extremely low, therefore raw materials for production that can be using it as antifreezing agent for building or leavening agent, and the organic matter of separating can be again as the raw material of synthetic reaction.In the application, processed recycling by the solid salt refuse in producing, thereby realized the cleaner production of TGIC.Difference due to production technology, the operation that may produce solid salt refuse respectively is not quite similar, the issuable solid salt refuse of other operations can certainly be inserted in drying device and processed, in this application, preferably adopt the mixture that interior reaction obtains after finishing to cyclization still 12 to carry out the crystallization filtration treatment, obtain solid phase and be the solid waste (wet salt) in the application, filter and make cyclization obtain moisture and the complete crystallization of salinity in mixed system by crystallization, the solid phase that filtration obtains is by 82～83% NaCl, the ECH of 4% left and right, the H of 12% left and right
2o and micro-catalyst combination form, and obtain not containing in liquid phase or containing salt hardly and moisture, make salinity, moisture separate fully with TGIC, byproduct of reaction, just can not produce solid salt refuse in other operational sequences like this.Simultaneously, the utility model adopts the method for physical separation to be processed solid salt refuse, produces the salt rate and can reach more than 80%, need consider the variation of its constituent content while avoiding solid salt waste chemistry to process and need to add helper component, be easier to realize suitability for industrialized production, improve the economic benefit that TGIC produces.
Concrete scheme is, this production system also comprises the vavuum pump 33 that drying device 14 is vacuumized, described drying device 14 gas outlets connect the first condenser 31, the first condenser 31 liquid flowing outlets are connected with main liquid trap 32, the air inlet pipe of vavuum pump 33 is connected with main liquid trap 32 intracavity inter-connections, the blast pipe of vavuum pump 33 is connected and is connected with the second condenser 34 air inlets, and the liquid flowing outlet of the second condenser 34 is connected with secondary liquid trap 35.The liquid that described major and minor liquid trap 32,35 is collected is delivered to respectively separator 36 and carries out the component separation, separates to obtain organic phase and be delivered to that synthesis reaction vessel 11 is interior participates in reaction again as raw material.The gas (that is organic matter and moisture of volatilization) produced during 30 pairs of heat treated of organic matter recovery unit by arranging carries out recycling, due to the liquid hot water of more employings when the practical operation as heat-conducting fluid, temperature when solid salt refuse is carried out to heat treated can't be higher like this, therefore, for guaranteeing that the organic matter in solid salt refuse can be steamed recovery fully, in the application, adopt 33 pairs of drying devices of vavuum pump to be vacuumized.Be provided with condenser and liquid trap on the inlet and outlet pipeline of vavuum pump 13 in this application, its purpose guarantees that organic matter is reclaimed by complete evaporative condenser first, second, during due to heat treated, evaporation escaping gas amount is larger, by most of gas is collected in the interior condensation of the first condenser 31 and by main liquid trap 32, the gas volume that enters like this vavuum pump 33 reduces greatly, thereby by the vavuum pump 33 of less rate of air sucked in required is set, just can meet the requirement that drying device 14 is vacuumized, reduce the equipment cost of whole system.If the vavuum pump 33 of larger rate of air sucked in required is set certainly here, also can cancel the setting of the first condenser 31 and main liquid trap 32, the secondary liquid trap 35 here can directly consist of a water tank.
For realizing production energy-saving, this system also comprises the thermal-arrest unit 20 that liberated heat is collected when reacting in synthesis reaction vessel 11, and this thermal-arrest unit 20 is connected with the heating unit that adds thermosetting salt refuse arranged on drying device 14 by pipeline.The reaction of synthesis reaction vessel 11 interior generations is exothermic reaction, therefore, by this reaction being emitted to heat with acting on the solid salt refuse of heating, saves the energy.Concrete is: described thermal-arrest unit 20 combines for first cavity for holding heat-conducting fluid of synthesis reaction vessel 11 perisporiums and/or inner setting, described the first cavity is connected and is connected by outlet pipe 21 and heat storage can 22 for storing heat-conducting fluid, described heating unit is that drying device 14 perisporiums and/or inner the second cavity for holding heat-conducting fluid arranged combine, described the second cavity is by connecting pipe 23, 24 and the pump housing 25 form with heat storage can 22 peripheral passage that heat-conducting fluids circulate, that is, heat storage can 22 delivery ports are connected and are connected with the water inlet of the second cavity on drying device 14 by connecting pipe 23, the delivery port of the second cavity on drying device 14 is connected and is connected with heat storage can 22 water inlets by connecting pipe 24, the pump housing 25 is set on connecting pipe 24.First and second cavity here can by synthesis reaction vessel 11 and drying device 14 perisporiums the inner full pipe arranged or partly be in charge of, helix tube etc. forms, and also perisporium can be arranged to sandwich for being received into hot fluid.Due to synthesis reaction vessel 11 interior when reaction required heat when liberated heat is greater than solid salt refuse heat treated, therefore be provided with heat storage can 22 in the application, heat storage can 22 and heating unit are passed through to connecting pipe 23,24 and little water circulation path of the pump housing 25 formation, thereby solid salt refuse is carried out to effective heat treated, and the unnecessary heat of heat storage can 22 interior storages also can be utilized by other operations like this.Certainly, also can adopt directly first and second cavity is is directly connected and composed to water circulation path by pipeline, but the utilization rate of the waste heat that whole like this synthetic reaction is emitted is lower.
Further, applicant's long term test finds that in this system, temperature and the vacuum on solid salt refuse heat treated is larger on the impact of producing the salt rate, therefore the applicant is by constantly revising technical scheme, final determine that the temperature of heat treated is 80～95 ℃, the vacuum that drying device 14 vacuumizes is-0.08～-0.094Mpa.Described drying device 14 is rake type drier.Under this condition, Gu the product salt rate that the salt refuse is processed and the organic matter rate of recovery can improve 2～4 percentage points with respect to the technical scheme that realizes other parameters of the utility model purpose.
When concrete operations, mixture in cyclization still 12 is placed in filter 13 and carries out the crystallization filtration, the wet salt (consolidating the salt refuse) obtained is placed in rake type drier, be provided with rabbling mechanism in rake type drier, drying machine is double-decker, can lead to hot water in interlayer, combination of lumens becomes the second cavity, start vavuum pump 33 and first, two condensers 31, 34 pairs of rake type driers are vacuumized, as reach-0.08Mpa of vacuum, open the inlet valve arranged on rake type drier, thereby the wet salt in rake type drier is heated, wet salt is heated gradually and heats up, organic matter and moisture are constantly overflowed and are entered first from evaporation in material, two condensers 31, 34 and main, secondary liquid trap 32, collection is condensed in 35, after heat treated after a while, organic component in wet salt and moisture are evaporated complete, obtain industrial dry salt (moisture below 3%), close the inlet valve and the vavuum pump 33 that arrange on rake type drier, take out the raw materials for production that the interior dry salt of rake type drier can be used as antifreezing agent for building and leavening agent.The liquid of collecting in major and minor liquid trap 32,35 is inserted in separator 36 and carried out stratification, then the organic phase of separation is again dropped in synthesis reaction vessel 11 and reacted, the water of separation can be used as again industrial water.
At present, the dry salt obtained by the solid salt refuse of aforesaid operations processing is to detect through Anhui Province's product quality supervision and testing institute, and all technical meets the index request of company standard " antifreezing agent Q/DQS002-20082 " and " cement leavening agent Q/DQS004-2008 ".End in August, 2012, industry accumulative total in bright and beautiful peak reclaims 120 batches, solid salt refuse, reclaims altogether more than 80 tons of dry salt, the ECH3.6 ton, and accumulative total reduces 85 tons of solid waste discharges, is more than 90,000 yuan of enterprise's additional incomes.
The utility model can effectively be realized solid salt refuse in isocyanuric acid three-glycidyl ester production is processed in a word, the waste heat that solid salt refuse during TGIC is produced and reaction produce carries out recycling, realize cleaner production, production energy-saving and green production, improve the economic benefit that TGIC produces.
Claims (7)
1. produce solid salt treatment of wastes produced system for isocyanuric acid three-glycidyl ester for one kind, comprise the filter (13) filtered for the mixture after reaction in cyclization still (12) is finished, it is characterized in that: this system also comprises after filter (13) is filtered the organic matter recovery unit (30) that remaining solid salt refuse carries out the drying device (14) of heat treated and escaping gas carries out the condensation recovery during to heat treated.
2. as claimed in claim 1ly for isocyanuric acid three-glycidyl ester, produce solid salt treatment of wastes produced system, it is characterized in that: described organic matter recovery unit (30) comprises the interior escaping gas of drying device (14) is carried out to the condenser of condensation and the liquid trap that the liquid of condensation is reclaimed.
3. as claimed in claim 1 or 2 for the solid salt treatment of wastes produced system of isocyanuric acid three-glycidyl ester production, it is characterized in that: this system also comprises the vavuum pump (33) that drying device (14) is vacuumized, described drying device (14) gas outlet connects the first condenser (31), the first condenser (31) liquid flowing outlet is connected with main liquid trap (32), the air inlet pipe of vavuum pump (33) is connected with main liquid trap (32) intracavity inter-connection, the blast pipe of vavuum pump (33) is connected and is connected with the second condenser (34) air inlet, the liquid flowing outlet of the second condenser (34) is connected with secondary liquid trap (35).
4. as claimed in claim 1 or 2 for the solid salt treatment of wastes produced system of isocyanuric acid three-glycidyl ester production, it is characterized in that: this system also comprises the thermal-arrest unit (20) that liberated heat is collected when reacting in synthesis reaction vessel (11), and this thermal-arrest unit (20) is connected by pipeline and the upper heating unit that adds thermosetting salt refuse arranged of drying device (14).
5. as claimed in claim 1 or 2 for the solid salt treatment of wastes produced system of isocyanuric acid three-glycidyl ester production, it is characterized in that: described drying device (14) is rake type drier.
6. as claimed in claim 4 for the solid salt treatment of wastes produced system of isocyanuric acid three-glycidyl ester production, it is characterized in that: described thermal-arrest unit (20) combines for first cavity for holding heat-conducting fluid of synthesis reaction vessel (11) perisporium and/or inner setting, described the first cavity is connected and is connected by outlet pipe (21) and heat storage can (22) for storing heat-conducting fluid, described heating unit is that drying device (14) perisporium and/or inner the second cavity for holding heat-conducting fluid arranged combine, described the second cavity is by connecting pipe (23, 24) and the pump housing (25) and heat storage can (22) form the peripheral passage that heat-conducting fluid circulates.
7. as claimed in claim 3 for the solid salt treatment of wastes produced system of isocyanuric acid three-glycidyl ester production, it is characterized in that: the liquid that described major and minor liquid trap (32,35) is collected is delivered to respectively separator (36) and carries out the component separation, separates to obtain organic phase and be delivered in synthesis reaction vessel (11) and again participate in reaction as raw material.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 201220639790 CN202984265U (en) | 2012-11-28 | 2012-11-28 | Disposal system used for solid salt waste in production of triglycidyl isocyanurate (TGIC) |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 201220639790 CN202984265U (en) | 2012-11-28 | 2012-11-28 | Disposal system used for solid salt waste in production of triglycidyl isocyanurate (TGIC) |
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| CN202984265U true CN202984265U (en) | 2013-06-12 |
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| CN 201220639790 Withdrawn - After Issue CN202984265U (en) | 2012-11-28 | 2012-11-28 | Disposal system used for solid salt waste in production of triglycidyl isocyanurate (TGIC) |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102941214A (en) * | 2012-11-28 | 2013-02-27 | 黄山锦峰实业有限公司 | Treatment system for solid salt waste in triglycidyl isocyanurate production |
| CN102964341A (en) * | 2012-11-28 | 2013-03-13 | 黄山锦峰实业有限公司 | Production system of triglycidyl isocyanurate |
-
2012
- 2012-11-28 CN CN 201220639790 patent/CN202984265U/en not_active Withdrawn - After Issue
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102941214A (en) * | 2012-11-28 | 2013-02-27 | 黄山锦峰实业有限公司 | Treatment system for solid salt waste in triglycidyl isocyanurate production |
| CN102964341A (en) * | 2012-11-28 | 2013-03-13 | 黄山锦峰实业有限公司 | Production system of triglycidyl isocyanurate |
| CN102941214B (en) * | 2012-11-28 | 2015-08-19 | 黄山锦峰实业有限公司 | Solid salt treatment of wastes produced system in producing for isocyanuric acid three-glycidyl ester |
| CN102964341B (en) * | 2012-11-28 | 2016-02-24 | 黄山锦峰实业有限公司 | The production system of isocyanuric acid three-glycidyl ester |
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| GR01 | Patent grant | ||
| AV01 | Patent right actively abandoned |
Granted publication date: 20130612 Effective date of abandoning: 20150819 |
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| RGAV | Abandon patent right to avoid regrant |