CN212504443U - Comprehensive wastewater treatment device for bismuth pectin bulk drug, acridone acetic acid, acyclovir and thiodipropionate medical intermediate - Google Patents

Comprehensive wastewater treatment device for bismuth pectin bulk drug, acridone acetic acid, acyclovir and thiodipropionate medical intermediate Download PDF

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Publication number
CN212504443U
CN212504443U CN202020553445.3U CN202020553445U CN212504443U CN 212504443 U CN212504443 U CN 212504443U CN 202020553445 U CN202020553445 U CN 202020553445U CN 212504443 U CN212504443 U CN 212504443U
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tank
communicated
pipeline
inlet
outlet
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钮劲涛
陈新强
彭学辉
王亚飞
张萌
余飞虎
马三贵
陈长安
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Henan Hengan Environmental Protection Technology Co ltd
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Abstract

A process for treating the sewage generated by preparing the raw materials of bismuth pectin, acridone acetic acid, acyclovir, thiodipropionate, the evaporator is communicated with grate channel, which is communicated with comprehensive regulation pool, which is communicated with sludge pool, pH acidifying regulation pool, Fenton regulation pool, pH regulating back pool, hydrolysis-acidification pool, intermediate pool, anaerobic reactor, biological contact oxidation pool, secondary sedimentation pool, flocculation sedimentation pool, and sludge pool, and features scientific and reasonable design, low concentration of sewage, effectively removes COD, BOD and NH3-N, and has good social and economic benefits.

Description

Comprehensive wastewater treatment device for bismuth pectin bulk drug, acridone acetic acid, acyclovir and thiodipropionate medical intermediate
Technical Field
The utility model relates to a wastewater treatment device, in particular to a comprehensive wastewater treatment device for bismuth pectin raw material medicines, acridone acetic acid, acyclovir and thiodipropionate medical intermediates.
Background
The wastewater produced by the chemical synthesis medicine is characterized by high Chemical Oxygen Demand (COD), low Biological Oxygen Demand (BOD), large salt content, more various complex organic matters, metals and waste acid and waste alkali in the wastewater, large change of water quality and water quantity, most difficultly biodegradable substances and microorganism growth inhibitors, and the wastewater produced by the chemical synthesis medicine is the most serious pollution and the most difficult to treat in the five types of wastewater discharged in the pharmaceutical industry production, and the water quality of the wastewater is characterized in that: specific pollutants: aniline; conventional pollutants, namely COD, BOD, suspended matters (SS), chromaticity, ammonia nitrogen and other pollutants; secondly, the biodegradability is poor; the wastewater contains residual products, reactants, catalysts, solvents and the like, and the concentration of BOD, COD and Total Suspended Solids (TSS) is high; fourthly, the water quantity and the water quality of the wastewater fluctuate greatly; fifthly, the wastewater has insufficient nutrient source, and certain components have biological toxicity, thus increasing the difficulty of biological treatment. Therefore, the pretreatment of the wastewater is required to be enhanced, and the biodegradability of the wastewater is improved.
SUMMERY OF THE UTILITY MODEL
To above-mentioned condition, for overcoming prior art's defect, the utility model aims to provide a pectin bismuth bulk drug, acridone acetic acid and acyclovir, thiodipropionate medical intermediate synthesize waste water treatment facilities, can effectively solve the quality of water problem of pectin bismuth bulk drug, acridone acetic acid and acyclovir, thiodipropionate medical intermediate synthesize waste water to reach emission standard.
In order to realize the purpose, the utility model provides a technical scheme is that, a pectin bismuth bulk drug, acridone acetic acid and acyclovir, thiodipropionate medical intermediate comprehensive waste water treatment device, including evaporimeter and equalizing basin, the export of evaporimeter be linked together through the pipeline with the high salt waste water inlet of grid canal, the export of grid canal is linked together through the pipeline with the import of comprehensive equalizing basin, the precipitation export of comprehensive equalizing basin is linked together through the pipeline with the import of sludge impoundment, the export of comprehensive equalizing basin is linked together through the pipeline with the import of pH acidizing equalizing basin, the export of pH acidizing equalizing basin is linked together through the pipeline with the import of Fenton equalizing basin, the precipitation export of Fenton equalizing basin is linked together through the pipeline with the import of sludge impoundment, the export of Fenton equalizing basin is linked together through the pipeline with the import of pH readjustment basin, the export of pH readjustment basin is linked together through the pipeline with the import of hydrolysis, the outlet of the hydrolysis acidification tank is communicated with the inlet of the sludge tank through a pipeline, the outlet of the hydrolysis acidification tank is communicated with the inlet of an intermediate water tank through a pipeline, the outlet of the intermediate water tank is communicated with the inlet of an anaerobic reactor (UASB) through a pipeline, the outlet of the anaerobic reactor is communicated with the inlet of an anoxic tank (A tank) through a pipeline, the outlet of the anoxic tank is communicated with the inlet of a biological contact oxidation tank (O tank) through a pipeline, a nitrified liquid reflux port of the biological contact oxidation tank is communicated with the inlet of the anoxic tank through a pipeline, the outlet of the biological contact oxidation tank is communicated with the inlet of a secondary sedimentation tank through a pipeline, the secondary sedimentation outlet of the secondary sedimentation tank is communicated with the inlet of the sludge tank through a pipeline, the water outlet of the secondary sedimentation tank is communicated with the inlet of a flocculation sedimentation tank through a pipeline, and the flocculation sedimentation outlet of the flocculation sedimentation tank is, the water outlet of the flocculation sedimentation tank is communicated with a wastewater discharge pipeline which reaches the standard, and the reflux port of the sedimentation tank of the secondary sedimentation tank and the reflux port of the flocculation sedimentation tank are communicated with the sludge inlet of the anoxic tank through a three-way pipeline.
The utility model has the advantages of scientific and reasonable design, reduced waste water pollutant concentration, do benefit to further processing and reach standard, effectively get rid of COD, BOD and NH3-N, reach emission standard, have good society and economic benefits.
Drawings
Fig. 1 is a diagram of the structure block of the present invention.
Detailed Description
The following detailed description of the embodiments of the present invention will be made with reference to the accompanying drawings.
The device comprises an evaporator and an adjusting tank, and is characterized in that an outlet of the evaporator 1 is communicated with a high-salinity wastewater inlet of a grid channel 2 through a pipeline, an outlet of the grid channel 2 is communicated with an inlet of an integrated adjusting tank 3 through a pipeline, a precipitation outlet of the integrated adjusting tank 3 is communicated with an inlet of a sludge tank 13 through a pipeline, an outlet of the integrated adjusting tank 3 is communicated with an inlet of a pH acidification adjusting tank 4 through a pipeline, an outlet of the pH acidification adjusting tank 4 is communicated with an inlet of a Fenton adjusting tank 5 through a pipeline, a precipitation outlet of the Fenton adjusting tank 5 is communicated with an inlet of the sludge tank 13 through a pipeline, an outlet of the Fenton adjusting tank 5 is communicated with an inlet of a pH adjusting tank 6 through a pipeline, an outlet of the pH adjusting tank 6 is communicated with an inlet of a hydrolysis acidification tank 7 through a pipeline, the sedimentation outlet of the hydrolysis acidification tank 7 is communicated with the inlet of a sludge tank 13 through a pipeline, the outlet of the hydrolysis acidification tank 7 is communicated with the inlet of an intermediate water tank 8 through a pipeline, the outlet of the intermediate water tank 8 is communicated with the inlet of an anaerobic reactor 9 through a pipeline, the outlet of an anaerobic reactor 9 is communicated with the inlet of an anoxic tank 10 through a pipeline, the outlet of the anoxic tank 10 is communicated with the inlet of a biological contact oxidation tank 10-1 through a pipeline, the nitrifying liquid return port of the biological contact oxidation tank 10-1 is communicated with the inlet of the anoxic tank 10 through a pipeline, the outlet of the biological contact oxidation tank 10-1 is communicated with the inlet of a secondary sedimentation tank 11 through a pipeline, the secondary sedimentation outlet 11-1 of the secondary sedimentation tank 11 is communicated with the inlet of the sludge tank 13 through a pipeline, the water outlet of the secondary sedimentation tank 11 is communicated with the inlet of a flocculation sedimentation tank 12 through a pipeline, and the flocculation sedimentation outlet 12-1 of the flocculation sedimentation tank 12, the water outlet of the flocculation sedimentation tank 12 is communicated with a wastewater standard discharge pipeline 16, and the return port 11-2 of the sedimentation tank of the secondary sedimentation tank 11 and the return port 12-2 of the flocculation sedimentation tank 12 are communicated with the sludge inlet of the anoxic tank 10 through a three-way pipeline 15.
In order to ensure better implementation effect, a plurality of aeration discs arranged on aeration pipelines are respectively and uniformly distributed at the bottoms of the comprehensive adjusting tank 3 and the biological contact oxidation tank 10-1, and the air outlet of the Roots blower 14 is respectively communicated with the air inlets of the comprehensive adjusting tank 3 and the biological contact oxidation tank 10-1 through the aeration pipelines.
A first lifting pump 17a is arranged on a pipeline communicated with the comprehensive adjusting tank 3 and the pH acidification adjusting tank 4, and a second lifting pump 17b is arranged on a pipeline communicated with the intermediate water tank 8 and the anaerobic reactor 9.
The evaporator 1 is a three-effect evaporator or MVR2 evaporator.
The inclination angle of the grid ditch 2 is 60 degrees, the grid is a stainless steel manual or mechanical grid above 304, and the flow velocity of the passing grid is 0.6 m/s-0.8 m/s.
The biological contact oxidation tank 10-1 is internally suspended with a combined filler made of plastic flower sheets, and the diameter of the combined filler is phi 150 and 180 mm.
The comprehensive adjusting tank 3, the pH acidification adjusting tank 4 and the pH readjustment tank 6 are respectively connected with an automatic medicine feeding device and an industrial pH meter.
The anoxic pond 10 and the biological contact oxidation pond 10-1 are made of steel concrete and are square, and the volume ratio of the anoxic pond 10 to the biological contact oxidation pond 10-1 is 1:3 or 1: 4.
The Fenton reagent in the Fenton adjusting tank 5 is ferrous sulfate and H2O2And ferrous sulfate: h2O2The mass ratio is 2: 1-6: 1.
it should be noted that above-mentioned each part is prior art, the product of selling, the utility model discloses a contribution lies in, reforms these known parts into pectin bismuth bulk drug, acridone acetic acid and acyclovir, thiodipropionate medical intermediate comprehensive waste water treatment device through scientific design overall arrangement repacking, effectively solves prior art's defect, satisfies the production needs.
The utility model discloses when concrete implementation, the behavior is:
(1) desalting the high-salt wastewater by a triple-effect evaporator or MVR2 evaporator, mixing the treated condensed water with non-high-salt raw water, and allowing the mixed condensed water to enter a grid channel for removing larger suspended matters, floating matters, fiber substances and solid particle substances in the wastewater, so as to ensure the normal operation of a subsequent treatment structure and reduce the treatment load of the subsequent treatment structure, wherein the grid is a stainless steel artificial or mechanical grid with the inclination angle of over 304 degrees, and the flow rate of the grid passing through is 0.6-0.8 m/s;
(2) the production of the bulk drugs of the bismuth pectin bulk drug, the acridone acetic acid, the acyclovir and the thiodipropionate medicine is mostly intermittent production, the fluctuation of water quantity and water quality is large, the purification function of the wastewater treatment equipment is not favorably realized, in order to improve the impact capacity of a sewage treatment facility on organic matter load and reduce the fluctuation of the water quality, a comprehensive adjusting tank is required to be arranged to adjust the water quantity and the water quality of wastewater, and an acidic substance H is added into the comprehensive adjusting tank by an automatic dosing device2SO4Reacting the wastewater with an alkaline substance NaOH in the comprehensive adjusting tank for 40h, controlling the pH value of the wastewater in the comprehensive adjusting tank to be 6-9 by an industrial pH meter, discharging a small amount of materialized and biological sludge and scum generated in the treatment process into a sludge tank through a precipitation outlet by regular static pressure, dehydrating by a sludge filter press, and transporting to a local refuse landfill for harmless treatment;
the bottom of the comprehensive regulating tank is provided with a plurality of microporous aeration discs, the microporous aeration discs are arranged on an aeration pipeline, a branch pipe is divided from a Roots blower for blowing aeration to a biochemical system through a fan room and communicated with an air inlet of the aeration pipeline for pre-aeration, the waste water in the comprehensive regulating tank is subjected to gas stirring, organic matters are prevented from settling to the bottom of the tank and being acidified and corrupted, and part of COD and BOD can be removed through the pre-aeration;
(3) the water outlet of the comprehensive adjusting tank is communicated with the water inlet of a first lifting pump which is controlled to be started and stopped by a liquid level floating ball, wastewater is pumped into a pH acidification adjusting tank through the first lifting pump, and a better effect can be obtained only when the pH value of the wastewater is 3-4 due to Fenton reaction, so that the wastewater enters the pH acidification adjusting tank before the Fenton reaction, an acid substance is added through an automatic medicine adding device, the pH value of the wastewater in the pH acidification adjusting tank is controlled to be 2.5-3.5 by using an industrial pH meter, and the treated wastewater enters the Fenton adjusting tank;
(4) fenton's reagent, namely ferrous sulfate and H is added into a Fenton adjusting tank2O2Wherein, ferrous sulfate: h2O2The mass ratio of (A) to (B) is 6: 1-2: 1, wastewater reacts in a Fenton adjusting tank for 40-90 min, advanced oxidation is carried out on the wastewater with poor biodegradability, a part of COD is removed, the biodegradability of the wastewater is improved, the pH value of the wastewater treated in the Fenton adjusting tank is 5-6, then the wastewater enters a pH adjusting tank, a small amount of materialization, biological sludge and scum generated in the treatment process are discharged into a sludge tank through a precipitation outlet at regular static pressure, and the wastewater is dewatered by a sludge filter press and then transported to a local refuse landfill for harmless treatment;
(5) after the wastewater enters a pH adjusting tank, alkaline substances are added through an automatic dosing device, an industrial pH meter is used for controlling the pH value to be 6.5-8.5, and the wastewater treated under the subsequent biochemical treatment condition is ensured to enter a hydrolysis acidification tank;
(6) the hydrolysis acidification pool is internally provided with an elastic filler made of hydroformylation silk fiber, the diameter of the elastic filler is phi 150-180mm, the filling rate is 50-60%, the wastewater reacts in the hydrolysis acidification pool for 40h, insoluble organic matters are hydrolyzed into soluble organic matters and macromolecular substances to be decomposed into micromolecular substances through the action of hydrolytic bacteria and acid-producing bacteria in the hydrolysis process, the biodegradability of the wastewater is further improved, the wastewater is more suitable for subsequent biochemical treatment, a small amount of materialization, biological sludge and scum generated in the treatment process are discharged into a sludge pool through a precipitation outlet by regular static pressure, the sludge is dewatered by a sludge filter press, the wastewater is transported to a local refuse landfill for harmless treatment, and the wastewater treated by the hydrolysis acidification pool enters an intermediate pool;
(7) pumping the waste water in the intermediate water tank into an anaerobic reactor through a second lifting pump, separating three phases in the anaerobic reactor, separating the waste water into a gas phase, a liquid phase and a solid phase, wherein the liquid phase enters the anaerobic tank from the anaerobic reactor, and the COD volume load of the anaerobic reactor is 2-4kgCOD/m3Upward flow velocity<0.3m/s;
(8) AO technology: the wastewater is subjected to the action of nitrifying bacteria and denitrifying bacteria in an anoxic tank to convert ammonia nitrogen in the wastewater into N2Thereby removing ammonia nitrogen pollutants and TN in water, leading the wastewater after denitrification treatment to enter a biological contact oxidation tank connected with an air blower, suspending a combined filler made of plastic flower sheets in the biological contact oxidation tank, wherein the diameter of the combined filler is phi 150 and 180mm, and the volume load of the BOD filler is 1-1.2kgBOD/m3The wastewater reacts for 12-15h in the biological contact oxidation tank, the Roots blower of the blower room provides aeration, the aeration is realized by uniformly distributing microporous aeration discs at the bottom of the tank to uniformly supply air, the diameter of each aeration disc is 215mm, and the air-water ratio is 15-20: 1, returning the nitrified liquid to an anoxic tank through a pipeline;
(9) the wastewater separated by the biological contact oxidation tank enters a secondary sedimentation tank, sedimentation is carried out for 1.5-2h, sludge and clear water are separated, a part of the generated sludge flows back to the anoxic tank, the rest sludge enters the sludge tank, and the clear water reaching the standard is discharged into a flocculation sedimentation tank through a pipeline;
(10) the suspended matters remained in the wastewater treated by the secondary sedimentation tank are biological floccules with the particle size of several millimeters to 10 mu m and uncoagulated colloid particles, which are the main cause of the chromaticity of the pharmaceutical wastewater, the particles are basically organic, 50 to 80 percent of BOD value comes from the particles, 10 percent of PAC and 0.1 percent of PAM are added into the flocculation sedimentation tank for improving the clarity and stability of the secondary sedimentation wastewater, the wastewater reacts in the flocculation sedimentation tank for 0.5 to 1 hour, a part of sludge generated in the reaction process flows back to the anoxic tank, the rest sludge enters the sludge tank, and the supernatant is discharged through a wastewater standard discharge pipeline.
The utility model discloses through application and test implementation, very good beneficial effect has been obtained, and specific data is as follows:
can find out by the aforesaid, the utility model discloses a high salt waste water desalination preliminary treatment-Fenton materialization preliminary treatment-hydrolytic acidification-UASB-AO-flocculation and precipitation technology handles waste water, and the engineering takes up an area of fewly, and the expense is low, and the operation management is convenient, has reduced intensity of labour, has practiced thrift the manpower, compares with prior art, has following advantage:
(1) adopting a technical principle of quality-divided pretreatment, evaporating a small amount of high-salt high-ammonia nitrogen wastewater by triple effect or MVR2 to remove high-salt components affecting biochemical treatment in the wastewater;
(2) the wastewater after the quality-divided pretreatment is mixed, so that the concentration of raw water pollutants is reduced, and the further treatment is facilitated to reach the standard;
(3) the mixed wastewater is treated by Fenton advanced oxidation technology, anaerobic biological treatment technology (hydrolytic acidification + UASB), anoxic and aerobic treatment technology (AO) and physical chemical treatment technology (flocculation precipitation) in sequence, and COD, BOD and NH3The N removal rate can reach more than 90 percent, the TN removal rate reaches 70 percent, the aniline removal rate reaches 92 percent, the current local standard is stably reached, the treated wastewater and sludge can be recycled, the resources are greatly saved, the pollution of the wastewater to the environment is effectively reduced, the energy conservation and environmental protection are really realized, and the social and economic benefits are good.

Claims (8)

1. A comprehensive wastewater treatment device for bismuth pectin bulk drugs, acridone acetic acid, acyclovir and thiodipropionate medical intermediates comprises an evaporator and an adjusting tank, and is characterized in that an outlet of the evaporator (1) is communicated with a high-salinity wastewater inlet of a grid channel (2) through a pipeline, an outlet of the grid channel (2) is communicated with an inlet of a comprehensive adjusting tank (3) through a pipeline, a precipitation outlet of the comprehensive adjusting tank (3) is communicated with an inlet of a sludge tank (13) through a pipeline, an outlet of the comprehensive adjusting tank (3) is communicated with an inlet of a pH acidification adjusting tank (4) through a pipeline, an outlet of the pH acidification adjusting tank (4) is communicated with an inlet of a Fenton adjusting tank (5) through a pipeline, a precipitation outlet of the Fenton adjusting tank (5) is communicated with an inlet of the sludge tank (13) through a pipeline, an outlet of the Fenton adjusting tank (5) is communicated with an inlet of a pH adjusting tank (6) through a pipeline, the outlet of the pH adjusting tank (6) is communicated with the inlet of the hydrolysis acidification tank (7) through a pipeline, the precipitation outlet of the hydrolysis acidification tank (7) is communicated with the inlet of the sludge tank (13) through a pipeline, the outlet of the hydrolysis acidification tank (7) is communicated with the inlet of the intermediate water tank (8) through a pipeline, the outlet of the intermediate water tank (8) is communicated with the inlet of an anaerobic reactor (9) through a pipeline, the outlet of the anaerobic reactor (9) is communicated with the inlet of an anoxic tank (10) through a pipeline, the outlet of the anoxic tank (10) is communicated with the inlet of a biological contact oxidation tank (10-1) through a pipeline, the nitrified liquid return port of the biological contact oxidation tank (10-1) is communicated with the inlet of the anoxic tank (10) through a pipeline, the outlet of the biological contact oxidation tank (10-1) is communicated with the inlet of a secondary precipitation tank (11) through a pipeline, and the secondary precipitation outlet (11-1) of the secondary precipitation tank (11) is communicated with the inlet of the sludge tank The system is characterized by comprising a secondary sedimentation tank (11), wherein a water outlet of the secondary sedimentation tank (11) is communicated with an inlet of a flocculation sedimentation tank (12) through a pipeline, a flocculation sedimentation outlet (12-1) of the flocculation sedimentation tank (12) is communicated with an inlet of a sludge tank (13) through a pipeline, a water outlet of the flocculation sedimentation tank (12) is communicated with a wastewater standard discharge pipeline (16), and a sedimentation tank return port (11-2) of the secondary sedimentation tank (11) and a flocculation sedimentation tank return port (12-2) of the flocculation sedimentation tank (12) are communicated with a sludge inlet of an anoxic tank (10) through a three-way pipeline (15).
2. The integrated wastewater treatment device for the bismuth pectin bulk drug, the acridone acetic acid, the acyclovir and the thiodipropionate medical intermediate as claimed in claim 1, wherein a plurality of aeration discs arranged on aeration pipelines are respectively and uniformly distributed at the bottoms of the integrated regulating tank (3) and the biological contact oxidation tank (10-1), and the air outlet of the Roots blower (14) is respectively communicated with the air inlets of the integrated regulating tank (3) and the biological contact oxidation tank (10-1) through the aeration pipelines.
3. The comprehensive wastewater treatment device for bismuth pectin bulk drugs, acridone acetic acid, acyclovir and thiodipropionate medical intermediates according to claim 1, characterized in that a first lift pump (17 a) is arranged on a pipeline communicated with the comprehensive adjusting tank (3) and the pH acidification adjusting tank (4), and a second lift pump (17 b) is arranged on a pipeline communicated with the intermediate water tank (8) and the anaerobic reactor (9).
4. The comprehensive wastewater treatment device for bismuth pectin bulk drugs, acridone acetic acid and acyclovir, thiodipropionate medical intermediates according to claim 1, characterized in that the evaporator (1) is a triple-effect evaporator or MVR2 evaporator.
5. The comprehensive wastewater treatment device for medical intermediates of bismuth pectin, acridone acetic acid, acyclovir and thiodipropionate according to claim 1, characterized in that the inclination angle of the grid channel (2) is 60 degrees, the grid is a stainless steel artificial or mechanical grid with the flow rate of 0.6-0.8 m/s, and the grid is more than 304 degrees.
6. The comprehensive wastewater treatment device for medical intermediates of bismuth pectin, acridone acetic acid, acyclovir and thiodipropionate according to claim 1, characterized in that a combined filler made of plastic flower sheets is suspended in the biological contact oxidation tank (10-1), and the diameter of the combined filler is phi 150-180 mm.
7. The comprehensive wastewater treatment device for bismuth pectin bulk drugs, acridone acetic acid, acyclovir and thiodipropionate medical intermediates according to claim 1, characterized in that the comprehensive adjusting tank (3), the pH acidification adjusting tank (4) and the pH readjustment tank (6) are respectively connected with an automatic dosing device and an industrial pH meter.
8. The comprehensive wastewater treatment device for the medical intermediates of bismuth pectin, acridone acetic acid, acyclovir and thiodipropionate according to claim 1, characterized in that the anoxic tank (10) and the biological contact oxidation tank (10-1) are made of steel concrete and are square, and the volume ratio of the anoxic tank (10) to the biological contact oxidation tank (10-1) is 1:3 or 1: 4.
CN202020553445.3U 2020-04-15 2020-04-15 Comprehensive wastewater treatment device for bismuth pectin bulk drug, acridone acetic acid, acyclovir and thiodipropionate medical intermediate Active CN212504443U (en)

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