CN102659283B - Process for treating and recovering dye industrial wastewater - Google Patents
Process for treating and recovering dye industrial wastewater Download PDFInfo
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Abstract
The invention discloses a process for treating and recovering dye industrial wastewater. The process comprises the following steps of: collecting cyclizing wastewater, adding a calcium hydroxide solution, reacting until the pH value is 5 to 7, and recovering a precipitate to obtain calcium hydrophosphate; adding the calcium hydroxide solution continuously, reacting until the pH value is 10 to 12, and recovering a precipitate to obtain calcium phosphate; adding an acidulant for neutralizing; collecting pigment wastewater, rectifying at the temperature of between 75 and 85 DEG C, and recovering fractions to obtain ethanol; collecting soda boiling wastewater, mixing the soda boiling wastewater and the treated cyclizing wastewater and pigment wastewater to obtain mixed wastewater, adding the acidulant into the mixed wastewater, regulating the pH value to be 2 to 4, separating a precipitate out, and performing suction filtration and distillation on the precipitate to obtain benzoic acid; and performing primary materialization treatment, biochemical treatment and advanced treatment on the treated mixed wastewater sequentially, and discharging. According to the process, useful substances in the dye wastewater are recovered, so that the production cost is saved, the load of the subsequent wastewater treatment process is reduced, the discharge of the wastewater can reach the standard, and the economic benefit is improved effectively.
Description
Technical field
The present invention relates to comprehensive utilization and the process field of waste water, relate in particular to a kind of waste water in dye production and process and recovery process.
Background technology
Textile and dyeing industry is one of Chinese conventional column industry, but it is also the blowdown rich and influential family in industry, and the waste water from dyestuff quantity discharged that produces is large, intractability is high, is the research emphasis of waste water treatment technique.The red production technique of conventional pigment mainly comprises cyclisation, soda boiling and pigmenting stage.Wherein, the cyclisation stage produces cyclisation waste water, comprises phosphoric acid, phenylformic acid waste water and washes; The soda boiling stage produces soda boiling waste water, is mainly alkaline waste water; And the pigmenting stage produces pigmenting waste water, is mainly the waste water that contains ethanol, phenyl amines, also can produce a certain amount of synthesising by-product and Pigment Intermediates in whole production technique.
The Pigment red factory effluent mainly contains following characteristics: (1) organic concentration is high: contain a large amount of benzene ring substance in waste water, as phenylformic acid, ethanol etc.; (2) biodegradability is relatively poor; (3) colourity is high: have very high colourity, usually reach more than 20000 times; (4) pollutant kind is many: waste water contains multiple synthetic byproduct and intermediate, and the indexs such as phenyl amines, ammonia nitrogen, phosphoric acid salt are all higher.
At present, both at home and abroad the tupe of Pigment red factory effluent, be mainly " coagulating sedimentation---advanced oxidation---biochemical treatment---advanced treatment ", processed waste water can reach emission standard, but the characteristics due to Pigment red waste water, the art breading investment that employing is commonly used is higher, the sludge creation amount is large, processing cost is high, is a difficult problem of sewage disposal in industry.
The patent of invention of notification number CN101955303B discloses a kind for the treatment of process of waste water from dyestuff, comprising: waste water from dyestuff is through equalizing tank, reaction tank, and preliminary sedimentation tank I, preliminary sedimentation tank II carries out pre-treatment; Enter air flotation pool, the air flotation pool water outlet is divided into two-way: the one tunnel enters oxygen compatibility pool, and another road passes back into equalizing tank, the COD in fuel diluted waste water, colourity, saltiness; The oxygen compatibility pool water outlet enters Aerobic Pond, and flocculation sedimentation tank goes to the inverse pond, goes inverse pond water outlet to enter final deposition pool radial-flow mud-water separation, static 50min, supernatant liquor discharging; Below final deposition pool water outlet COD 80mg/L, colourity is below 60.The patent of invention of notification number CN101353215B discloses a kind of dyeing waste water comprehensive treating process and reuse technology, after the waste water that pre-treating technology is processed passes through multi-medium filtering, import the catalytic ozonation treatment system and carry out ozone Oxidation Treatment, through the waste water of ozone Oxidation Treatment, then carry out continuous ultra filtration and reverse-osmosis treated.Waste water after catalytic ozonation is as elementary reuse, and the waste water after Integrated Films is processed is as the senior reuse of printing and dyeing technology water.The method can be improved the contamination phenomenon of membrane element in treating processes, and the stabilizing treatment effect is saved processing cost.The patent of invention of notification number CN100364901C discloses a kind of dye waste water treatment method based on membrane technique, mainly comprise waste water from dyestuff pre-treatment part and membrane filtration separation system part, the waste water from dyestuff pre-treatment is comprised of techniques such as waste water adjusting, flocculating settling, clarifications, and the membrane filtration separation system is comprised of ultrafiltration circulation and nanofiltration circulation technology.This invention enters the film system at waste water from dyestuff and it is carried out pre-treatment before separating, and is particularly suitable for processing through conventional sewage water treatment method the azo dye wastewater that is difficult to qualified discharge and processes.Although these three kinds of methods have all realized the processing to waste water from dyestuff, the useful component in waste water from dyestuff is not reclaimed, and the wastewater treatment process complex steps, energy consumption is larger, and processing cost is higher.
Summary of the invention
The invention provides a kind of waste water in dye production and process and recovery process, can reclaim the useful component in waste water in dye production, alleviate the burden of subsequent wastewater treatment technique, and make discharged wastewater met the national standard.
A kind of waste water in dye production is processed and recovery process, and described waste water in dye production comprises cyclisation waste water, soda boiling waste water and pigmenting waste water; Described processing and recovery process comprise the steps:
(1) collect cyclisation waste water, add aqua calcis, react to pH value and be 5-7, reclaim to precipitate and obtain secondary calcium phosphate; Continue to add aqua calcis, react to the pH value for 10-12, reclaim precipitation and obtain calcium phosphate; Add again souring agent to neutralize;
(2) collect pigmenting waste water, carry out rectifying under 75-85 ℃, reclaim cut and obtain ethanol;
(3) collect soda boiling waste water, pigmenting waste water after cyclisation waste water, step (2) after soda boiling waste water and step (1) processing are processed is mixed to get composite waste, add souring agent in composite waste, regulate the pH value to 2-4, isolate precipitation, precipitation obtains phenylformic acid through suction filtration, distillation;
(4) will discharge after the process one-level materialization processing successively of the composite waste after step (3) processing, biochemical treatment and advanced treatment.
The production technique of Pigment red mainly comprises cyclisation, soda boiling and pigmenting stage.Described cyclisation waste water is to produce in the cyclisation stage, comprises phosphoric acid, phenylformic acid waste water and washes; Described soda boiling waste water is to produce in the soda boiling stage, is mainly alkaline waste water; Described pigmenting waste water is to produce in the pigmenting stage, is mainly the waste water that contains ethanol, phenyl amines.
Technique of the present invention included with thing recovery stage and wastewater treatment stage.In useful thing recovery stage, cyclisation waste water is treated can reclaim phosphate anion, and pigmenting waste water is treated can reclaim ethanol, and remaining waste water mixes can recovery of benzoic acid by processing; In the wastewater treatment stage, waste water can be realized qualified discharge through tertiary treatment.
In step (1), described souring agent can be dilute sulphuric acid or dilute hydrochloric acid, can regulate the pH of cyclisation waste water, and can not increase the burden of subsequent wastewater treatment.
In step (2), described rectifying can be carried out in rectifying tower.Described rectification temperature is preferably 80 ℃.
In step (3), described souring agent can be dilute sulphuric acid or dilute hydrochloric acid, can regulate the pH of soda boiling waste water, and can not increase the burden of subsequent wastewater treatment.
Described distillation can be as follows: the phenylformic acid crude product that obtains after suction filtration is placed in still kettle, first temperature in the kettle is transferred to 100 ℃, reclaim head temperature and be controlled at 180 ℃, distillation for some time, receive the moisture that the prolong of going out is discharged; When no longer including the moisture discharge, temperature in the kettle is transferred to 250 ℃-260 ℃, reclaim head temperature and be controlled at 180 ℃, the cut of discharge is solid-state phenylformic acid finished product after condensation.
In step (4), before the one-level materialization is processed, can first carry out water quality, the adjusting of water yield homogenizing and pH regulator to described composite waste, can guarantee like this steady running of subsequent wastewater treatment operation.
Described one-level materialization is processed can comprise coagulation, flocculation and precipitation process; The coagulating treatment stage adds coagulating agent and molysite, and carries out mechanical stirring, and coagulating agent can adopt dye wastewater treatment coagulating agent commonly used; The flocculation treatment stage adds flocculation agent, and carries out mechanical stirring, and flocculation agent can adopt dye wastewater treatment flocculation agent commonly used.By coagulation, flocculation and precipitation process, can remove the indexs such as the most of suspended solid in composite waste, the COD, the SS that reduce waste water, phosphoric acid salt, for follow-up biochemical treatment provides condition.
Described biochemical treatment can be adopted the anaerobic-anoxic-oxic active sludge treatment, i.e. the A/A/O biochemical processing.
Preferably, in the anaerobic-anoxic-oxic Activated Sludge Process, anaerobic activated sludge is processed and is adopted upflow anaerobic sludge blanket reactor (UASB); Upflow anaerobic sludge blanket reactor is processed the biogas that produces and be used for energy supply after being collected.The upflow anaerobic sludge blanket reactor operation is convenient, the mud utilization ratio is high, can be used for the processing of high-concentration waste water, particularly some larger molecular organicses than difficult degradation there is good removal effect, the macromolecule organic in composite waste can be resolved into small organic molecule.
Preferably, with the mixed solution after aerobic activated sludge is processed by inner circulating reflux to the hypoxia activity sludge treatment stage.The mixed solution internal reflux is set can promote denitrification to realize ammonia nitrogen in waste water, phosphatic removing.
Preferably, the composite waste after aerobic activated sludge is processed is carried out solid-liquid separation, isolated mud is back to the hypoxia activity sludge treatment stage by outer circulation.The sludge concentration that the mud external reflux can improve the hypoxia activity sludge treatment stage is set, replenishes living microorganism.
Described advanced treatment can comprise secondary materialization processing and advanced oxidation processing.Preferably, described secondary materialization is processed and is comprised coagulation, flocculation and precipitation process; Described advanced oxidation is processed and is adopted high-frequency impulse electrochemistry to process.Advanced treatment is guarantees that waste water reaches the tertiary treatment technology of emission standard, and SS and the colourity that can further remove in composite waste is processed in the secondary materialization, near emission standard; Process and the colour developing group thoroughly can be interrupted by high-frequency impulse electrochemistry again, guarantee discharged wastewater met the national standard.
For the mud that produces in whole technological process, can adopt following processing mode: collect the mud that produces in one-level materialization processing, biochemical treatment and advanced treatment process, mix, mud cake is made in dehydration.
Waste water in dye production of the present invention is processed with recovery process and can be carried out in corresponding system, and described system comprises: the neutralizing well, alkalization groove and the acidifying groove that are used for reclaiming phosphate anion; Be used for reclaiming the rectifying tower of ethanol; The mixing pit, acidification pool and the still kettle that are used for recovery of benzoic acid; Equalizing tank, the pH that is used for wastewater treatment adjusts pond, one-level coagulation basin, one-level flocculation basin, one-level settling tank, UASB pump sump, UASB anaerobic reactor, UASB settling tank, anoxic pond, aerobic aeration pond, secondary sedimentation basins, two-stage coagulation pond, secondary flocculation basin, second-level settling pond and advanced oxidation reaction tank; The sludge sump and the sludge dewatering equipment that are used for sludge treatment.
The present invention is directed to different recovery, the treatment process of characteristics design of three strands of waste water that produce between the Pigment red dye vehicle.One is high-concentration phosphorus-containing wastewater, secondary calcium phosphate and calcium phosphate can be reclaimed through neutralization, alkalization, acidification; One is the waste water that contains a large amount of ethanol, ethanol can be reclaimed through rectifying; Because benzoic acid content in three strands of waste water is all higher, the waste water after front two bursts of processing mixes with the 3rd strand of waste water, phenylformic acid can be reclaimed through acidifying, distillation, and remaining waste water enters equalizing tank.Waste water carries out being mixed of water quality, the water yield in equalizing tank; Flowing into pH adjusts the pond and carries out the adjustment of pH again; Enter subsequently the one-level materialization and process, the one-level materialization is processed and is comprised coagulation, flocculation and precipitation; Waste water enters biochemical treatment after precipitation, is at first anaerobic treatment, and anaerobic treatment comprises UASB pump sump, UASB anaerobic reactor and UASB settling tank, between reactor and settling tank, sludge reflux is set; Water outlet after anaerobic treatment enters anoxic pond, aerobic aeration pond and secondary sedimentation basins, between aerobic aeration pond and anoxic pond, internal circulation system is set, and the sludge reflux system is set between second pond and anoxic pond, and the second pond excess sludge discharges; Waste water after biochemical treatment enters the secondary materialization and processes, waste water passes through coagulation, flocculation, precipitation successively, waste water after spoil disposal enters the advanced oxidation reaction tank, this reaction tank is made of high-frequency impulse electrochemistry reactor and settling system, after waste water reacts through high-frequency impulse electrochemistry, most organic matter is effectively removed, waste water finally flows into sampling and discharges the pond, and the discharge water in this pond can qualified discharge.
Utilize present method, the benzoic rate of recovery can reach 60-75%, and the rate of recovery of ethanol is near 99%, and secondary calcium phosphate and calcium phosphate yield are considerable, and the clearance of phosphate radical is more than 99.9%; And the waste water from dyestuff of processing can reach the primary standard in integrated wastewater discharge standard GB8978-1996.
In the present invention, by the recycling of useful matter in waste water, on the one hand, can reduce the environmental protection investments of enterprise, save production cost, form economic return preferably; On the other hand, greatly alleviated the load of waste water treatment process, guaranteed discharged wastewater met the national standard, reached economic environmental protection, clean environment firendly, environmental protection win-win.System features in convenient of the present invention can realize full automatic control; Waste Water Treatment running cost is lower, and system's investment economizes, and can promote cleaner production, produces certain economic benefit.
Description of drawings
Fig. 1 is pigment wastewater processing technological flow schematic diagram in the embodiment of the present invention.
Fig. 2 is sludge treatment technique schematic flow sheet in the embodiment of the present invention.
Embodiment
Embodiment
Wenzhou District of Zhejiang Province pigment factory, every day, the factory effluent generation was 600t/d, carried out processing and the recovery of waste water according to following technique.
1, pigment wastewater recovery technology
(1) regeneration of phosphate radical
Collect cyclisation waste water (high-concentration phosphorus-containing wastewater), squeeze in the neutralizing well that lime solution (aqua calcis) is housed and react, when the pH value reaches 6, the solid phosphoric acid hydrogen calcium that generates is separated; Then reacted cyclisation waste water is squeezed into the alkalization groove, continues to add calcium hydroxide, react to pH be 11 o'clock, the solid phosphoric acid calcium that generates is separated, the content of cyclisation this moment Phosphorus From Wastewater is less than 1%; Then squeeze in the acidifying groove, add dilute sulphuric acid and neutralize; Cyclisation waste water after processing enters mixing pit.
(2) recovery of ethanol
Collect pigmenting waste water, send into rectifying tower, in control tower, temperature is 80 degree, and the rectifying liquid cooling is but namely reclaimed afterwards and obtained ethanol; Pigmenting waste water after processing enters mixing pit.
(3) benzoic recovery
Collect soda boiling waste water, squeeze into mixing pit, process with step (1) and step (2) waste water that obtains and mix; Composite waste imports acidification pool, adds souring agent with pH regulator to 3.0, the phenylformic acid in composite waste can be separated out fully; The phenylformic acid of separating out is filtered, drains moisture, obtain the phenylformic acid crude product; Enter still kettle again, first temperature is transferred to 100 degree, reclaim head temperature and be controlled at 180 ℃, the prolong of going out receives moisture, until the moisture evaporate to dryness; Then temperature in the kettle is controlled at 250 ℃-260 ℃, reclaims head temperature and be controlled at 180 ℃, by the cooling phenylformic acid finished product of collecting solid; The low composite waste of phenylformic acid that contains after processing imports equalizing tank.
2, waste water treatment technique
(1) (pre-treatment) processed in the one-level materialization
The one-level physicochemical treatment unit comprises that equalizing tank, pH adjust pond, one-level materialization treatment system (one-level coagulation basin, one-level flocculation basin, one-level settling tank).
Wherein, add coagulating agent and molysite during the one-level coagulating treatment, and carry out mechanical stirring; Add flocculation agent during the one-level flocculation treatment, and carry out mechanical stirring.
The major function of this processing unit be remove most of suspended solid in waste water, reduce COD, SS in waste water, the index such as phosphoric acid salt, for biochemical treatment system provides condition.
(2) biochemical treatment
The biochemical treatment unit adopts the A/A/O technology, is comprised of UASB anaerobic reaction system (UASB pump sump, UASB anaerobic reactor, UASB settling tank), anoxic pond, aerobic aeration pond and secondary sedimentation basins.
Wherein, collect the biogas that the UASB anaerobic reactor produces, be used for energy supply.
This processing unit, system resolves into small organic molecule with the macromolecule organic in waste water by the UASB anaerobic reaction; And utilize anoxic pond and aerobic aeration tank mixed solution internal reflux and mud external reflux, and realize biological eliminating ammonia nitrogen and phosphoric acid salt function, make waste water near emissions object.
(3) advanced treatment
Advanced treatment is guarantees that waste water reaches the tertiary treatment technology of emission standard, comprises secondary materialization treatment system (two-stage coagulation pond, secondary flocculation basin, second-level settling pond) and advanced oxidation reaction tank (high-frequency impulse electrochemistry reactor, settling system).
Wherein, two-stage coagulation adds molysite when processing, and carries out mechanical stirring; Add flocculation agent during the secondary flocculation treatment, and carry out mechanical stirring.Add ST reagent and SY reagent during the advanced oxidation reaction, and carry out mechanical stirring.
At first this processing unit further removes SS and colourity in waste water by flocculation sediment, near emission standard; Thoroughly interrupt by the advanced electrochemical oxidation group that will develop the color again, guarantee discharged wastewater met the national standard.
(4) sludge treating system
Sludge treating system comprises sludge sump (materialized mud pond, biochemical sludge pond) and sludge dewatering equipment.
The mud discharging of one-level settling tank, second-level settling pond, advanced oxidation reaction tank is to the materialized mud pond; The residue anaerobic sludge of UASB settling tank, the residue aerobic sludge of secondary sedimentation basins are discharged into the biochemical sludge pond, and this pond is Reinforced Concrete Structure; After mud dewatered through sludge dewatering equipment, dried mud was made the outer operation ultimate disposal of mud cake, and filtrate can be circulated to equalizing tank and use.
In the present embodiment, 7,490,000 yuan of construction investments, running cost is 7.5 yuan/tons of waste water.The waste water from dyestuff of processing reaches the primary standard in integrated wastewater discharge standard GB8978-1996.
After above art breading, the phenylformic acid that dropped in a day is at 4 tons, and amount every day of recovery of benzoic acid, recovery value was considerable between 2.4 tons-3 tons; Recyclable secondary calcium phosphate is 0.41 ton; The amount of calcium phosphate is 0.7 ton, can be except phosphate radical more than 99.9%, and the phosphate content of final outflow water is up to standard; The ethanol rate of recovery reaches 99%.After conversion, can save nearly 20,000 yuan of production cost every day.
Claims (10)
1. a waste water in dye production is processed and recovery process, comprising:
(1) collect cyclisation waste water, add aqua calcis, react to pH value and be 5-7, reclaim to precipitate and obtain secondary calcium phosphate; Continue to add aqua calcis, react to the pH value for 10-12, reclaim precipitation and obtain calcium phosphate; Add again souring agent to neutralize;
(2) collect pigmenting waste water, carry out rectifying under 75-85 ℃, reclaim cut and obtain ethanol;
(3) collect soda boiling waste water, pigmenting waste water after cyclisation waste water, step (2) after soda boiling waste water and step (1) processing are processed is mixed to get composite waste, add souring agent in composite waste, regulate the pH value to 2-4, isolate precipitation, precipitation obtains phenylformic acid through suction filtration, distillation;
Described distillation is: the phenylformic acid crude product that obtains after suction filtration is placed in still kettle, first temperature in the kettle is transferred to 100 ℃, reclaim head temperature and be controlled at 180 ℃, distillation for some time, receive the moisture that the prolong of going out is discharged; When no longer including the moisture discharge, temperature in the kettle is transferred to 250 ℃-260 ℃, reclaim head temperature and be controlled at 180 ℃, the cut of discharge is solid-state phenylformic acid finished product after condensation;
(4) will discharge after the process one-level materialization processing successively of the composite waste after step (3) processing, biochemical treatment and advanced treatment.
2. waste water in dye production according to claim 1 is processed and recovery process, it is characterized in that, in step (1) or step (3), described souring agent is dilute sulphuric acid or dilute hydrochloric acid.
3. waste water in dye production according to claim 1 is processed and recovery process, it is characterized in that, in step (4), before the one-level materialization is processed, described composite waste is carried out water quality, the adjusting of water yield homogenizing and pH regulator.
4. waste water in dye production according to claim 1 is processed and recovery process, it is characterized in that, in step (4), described one-level materialization is processed and comprised coagulation, flocculation and precipitation process.
5. waste water in dye production according to claim 1 is processed and recovery process, it is characterized in that, in step (4), the anaerobic-anoxic-oxic active sludge treatment is adopted in described biochemical treatment.
6. waste water in dye production according to claim 5 is processed and recovery process, it is characterized in that, in the anaerobic-anoxic-oxic Activated Sludge Process, anaerobic activated sludge is processed and adopted upflow anaerobic sludge blanket reactor.
7. waste water in dye production according to claim 5 is processed and recovery process, it is characterized in that, with the mixed solution after aerobic activated sludge is processed by inner circulating reflux to the hypoxia activity sludge treatment stage.
8. waste water in dye production according to claim 1 is processed and recovery process, it is characterized in that, in step (4), described advanced treatment comprises secondary materialization processing and advanced oxidation processing.
9. waste water in dye production according to claim 8 is processed and recovery process, it is characterized in that, described advanced oxidation is processed and adopted high-frequency impulse electrochemistry to process.
10. waste water in dye production according to claim 1 is processed and recovery process, it is characterized in that, in step (4), collects the mud that produces in one-level materialization processing, biochemical treatment and advanced treatment process, mixes, and mud cake is made in dehydration.
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| CN103755021B (en) * | 2013-12-30 | 2016-05-25 | 河海大学 | A kind of improvement upflow type anaerobic ammoniation reactor and method for the treatment of high organic nitrogen dyeing waste water |
| CN103771659B (en) * | 2014-01-15 | 2015-07-29 | 河海大学 | The treatment process that the degraded of dyeing waste water high-enriched organics and total nitrogen are cut down |
| CN104478159B (en) * | 2014-11-20 | 2016-01-06 | 湘潭大学 | The method of a kind of sodium formate method sodium hydrosulfite wastewater process |
| CN105948377A (en) * | 2015-12-30 | 2016-09-21 | 天津市顶鑫源纺织材料有限公司 | Recycling apparatus and recycling method for treating printing and dyeing wastewater |
| CN105836966A (en) * | 2016-05-11 | 2016-08-10 | 北京迅世达环保科技有限公司 | High-concentration organic wastewater treatment process technology |
| CN108249696A (en) * | 2017-12-30 | 2018-07-06 | 珠海市斗门区永兴盛环保工业废弃物回收综合处理有限公司 | A kind of purifying treatment method of comprehensive wastewater |
| CN108996846A (en) * | 2018-09-04 | 2018-12-14 | 杭州开源环保工程有限公司 | A kind of dyeing waste water sludge decrement processing apparatus and method |
| CN109293058A (en) * | 2018-10-26 | 2019-02-01 | 洪湖市泰科技有限公司 | A kind of method of phosphorus-containing wastewater recycled and waste resource recovery utilizes |
| CN111115977B (en) * | 2020-01-17 | 2023-06-30 | 湖南诚通天岳环保科技有限公司 | Quinacridone production wastewater treatment method and system |
| JP7323224B1 (en) | 2022-04-28 | 2023-08-08 | ▲暁▼▲行▼ ▲姫▼ | Crude drug residue treatment method |
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Denomination of invention: Process for treating and recovering dye industrial wastewater Effective date of registration: 20140331 Granted publication date: 20130619 Pledgee: Uni-Power Group Co.,Ltd. Pledgor: Zhejiang Bestwa Environmental Protection Science and Technology Co., Ltd. Registration number: 2014990000216 |
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Date of cancellation: 20160419 Granted publication date: 20130619 Pledgee: Uni-Power Group Co.,Ltd. Pledgor: Zhejiang Bestwa Environmental Protection Science and Technology Co., Ltd. Registration number: 2014990000216 |
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