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Cellulose wastewater treatment

The main pollutants in hydroxypropyl methylcellulose wastewater are sodium chloride, isopropyl alcohol, hemicellulose derivatives, lost cellulose ether products, etc. The CODcr (dichromate oxygen demand) of the production wastewater can reach up to 60,000mg/l, and the salt content can reach up to 80,000mg/l, with a mass concentration of 7%-8%, which is a high concentration of salt-containing, hard-to-degrade wastewater.

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Because of the high osmotic pressure of hydroxypropyl methylcellulose wastewater and its high concentration of salt ions itself is toxic to microorganisms, if the conventional treatment process, such as "anaerobic + aerobic" process is used to treat this kind of wastewater, the activity of microorganisms in anaerobic sludge or aerobic sludge will decrease or even lose activity or die, and in order to maintain the operation of the system, it is necessary to In order to maintain the operation of the system, sludge must be added continuously to maintain the sludge volume of the system. The effluent treatment effect of traditional treatment process is poor, and the system operation is unstable, and the treated effluent is difficult to meet the standard discharge and cannot meet the requirement of reuse water quality at all.

Considering the difficulty of cellulose wastewater treatment and combining with the actual situation of the project, the process flow of evaporation + micro-electrolysis + Fenton oxidation + UASB + hydrolysis acidification + contact oxidation + advanced oxidation is adopted. The wastewater produced by hydroxypropyl methyl cellulose is collected and discharged to the wastewater conditioning tank of the wastewater treatment reuse device, and lifted by the pump into the evaporator. The concentrated liquid after evaporation by evaporator is separated by crystallization and centrifugation by centrifuge, and then enters the salt take-away system for reuse or other disposal; the condensate after evaporation by evaporator is mixed with other process wastewater mixing and conditioning, and enters the micro-electrolysis and Fenton oxidation, which mainly oxidizes some large molecules of organic matter into small molecules, so as to facilitate the next biochemical treatment; the mixed wastewater after oxidation is lifted by pump into UASB, UASB The anaerobic reaction process in the reactor is the same as other anaerobic biological treatment processes, including hydrolysis, acidification, acetic acid production and methane production, etc. The substrate is transformed into the final product - biogas, water and other inorganic substances through the participation of different microorganisms in the process of substrate transformation. The sludge is partially returned to the first collection tank after precipitation, and the water from the first collection tank is returned to the UASB reactor through the return pump set at the bottom of the first collection tank, and the remaining sludge in the anaerobic sedimentation tank is discharged to the sludge thickener, and the sludge is processed by the diaphragm plate and frame filter press and sent to the dry sludge transport system. After UASB treatment, the effluent organic matter is mainly large-molecule organic matter which is difficult to be directly biochemical, and it needs to be further transformed into small-molecule organic matter. the UASB effluent enters the second catchment tank, and then enters the hydrolysis acidification tank through the lifting pump set at the bottom of the second catchment tank, and the hydrolysis acidification tank decomposes part of the difficult organic matter into small-molecule organic matter to reduce the difficulty of contact oxidation, and through the Most of the organic pollutants in the water in the contact oxidation tank are decomposed and metabolized into CO2 and H2O through the metabolism of aerobic microorganisms, and the water quality is further purified. The remaining sludge in the contact oxidation tank is also transported to the sludge thickener, which is treated in the same process as the remaining sludge in the UASB sedimentation tank. The water from the contact oxidation tank enters the storage tank, except for part of the diluted water which is returned to the comprehensive wastewater conditioning tank, the remaining water from the contact oxidation tank is lifted by the pump into the sand filter tank for filtration, and the filtered water enters the advanced oxidation tank, where some of the organic pollutants remaining in the water are oxidized and decomposed by the strong oxidant ozone, and the CODcr in the water is further reduced. The effluent from the advanced oxidation tank reaches the discharge water quality standard and is discharged to the waste water discharge system.

Table 4-1 Removal efficiency table

Processing unit name	COD_Cr mg/L		NH₄-N mg/L		SS mg/L		pH
Processing unit name	Concentration mg/L	Removal rate%	Concentration mg/L	Removal rate%	Concentration mg/L	Removal rate%	—
Cooling regulator	<20000		<50		<150		6~9
pH adjustment cell	20000	—	50	—	150	—	3~4
Iron carbon micro-electrolysis	15000	25	50	—	150	—	5~6
Fenton tank	12000	20	50	—	30	80	3~4
Intermediate tank	12000	—	50	—	30	—	8~9
UASB	2640	78	40	20	30	—	7~8
Hydrolysis acidification tank	2059.2	22	34	15	30	—	6~7
Primary contact oxidation tank	782.5	62	20.4	40	30	—	6~7
Secondary contact oxidation tank	430.4	45	12.2	40	30	—	6~7
Secondary sedimentation tank	430.4	—	11.6	5	30	—	6~7
Strong oxidation tank	408.8	5	10.5	10	30	—	6~7
Discharge standard	<500		<25		＜400		6~9
Discharge standard	Comprehensive Wastewater Discharge Standard GB8978-1996 Table 4 tertiary standard