CN109323273A - A kind of organic raffinat and waste water combined purifying system capacity dynamic equilibrium control method - Google Patents
A kind of organic raffinat and waste water combined purifying system capacity dynamic equilibrium control method Download PDFInfo
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- CN109323273A CN109323273A CN201811366508.8A CN201811366508A CN109323273A CN 109323273 A CN109323273 A CN 109323273A CN 201811366508 A CN201811366508 A CN 201811366508A CN 109323273 A CN109323273 A CN 109323273A
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- 239000002351 wastewater Substances 0.000 title claims abstract description 74
- 238000000034 method Methods 0.000 title claims abstract description 32
- 238000010438 heat treatment Methods 0.000 claims abstract description 17
- 238000002485 combustion reaction Methods 0.000 claims abstract description 16
- 230000013632 homeostatic process Effects 0.000 claims abstract description 6
- 239000007788 liquid Substances 0.000 claims description 18
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 18
- 238000006243 chemical reaction Methods 0.000 claims description 15
- 238000010521 absorption reaction Methods 0.000 claims description 10
- 238000007254 oxidation reaction Methods 0.000 claims description 9
- 230000003647 oxidation Effects 0.000 claims description 8
- 239000010808 liquid waste Substances 0.000 claims description 7
- 238000009834 vaporization Methods 0.000 claims description 7
- 230000008016 vaporization Effects 0.000 claims description 7
- 239000003054 catalyst Substances 0.000 claims description 4
- 230000007423 decrease Effects 0.000 claims description 4
- 238000000926 separation method Methods 0.000 claims description 4
- 238000004065 wastewater treatment Methods 0.000 claims description 4
- 238000004364 calculation method Methods 0.000 claims description 3
- 238000001816 cooling Methods 0.000 claims description 3
- 230000003472 neutralizing effect Effects 0.000 claims description 3
- 150000002894 organic compounds Chemical class 0.000 claims description 3
- 239000005416 organic matter Substances 0.000 claims description 3
- 238000009833 condensation Methods 0.000 claims description 2
- 230000005494 condensation Effects 0.000 claims description 2
- 238000012544 monitoring process Methods 0.000 claims description 2
- 238000000465 moulding Methods 0.000 claims 1
- 238000005303 weighing Methods 0.000 claims 1
- 238000006555 catalytic reaction Methods 0.000 abstract description 8
- 230000003197 catalytic effect Effects 0.000 description 6
- 238000005265 energy consumption Methods 0.000 description 4
- 239000010842 industrial wastewater Substances 0.000 description 4
- 238000004821 distillation Methods 0.000 description 3
- 239000002699 waste material Substances 0.000 description 3
- FPYUJUBAXZAQNL-UHFFFAOYSA-N 2-chlorobenzaldehyde Chemical compound ClC1=CC=CC=C1C=O FPYUJUBAXZAQNL-UHFFFAOYSA-N 0.000 description 2
- AVPYQKSLYISFPO-UHFFFAOYSA-N 4-chlorobenzaldehyde Chemical compound ClC1=CC=C(C=O)C=C1 AVPYQKSLYISFPO-UHFFFAOYSA-N 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 238000000746 purification Methods 0.000 description 2
- 239000002253 acid Substances 0.000 description 1
- 239000003513 alkali Substances 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 239000003034 coal gas Substances 0.000 description 1
- 239000000470 constituent Substances 0.000 description 1
- 230000008878 coupling Effects 0.000 description 1
- 238000010168 coupling process Methods 0.000 description 1
- 238000005859 coupling reaction Methods 0.000 description 1
- 230000001351 cycling effect Effects 0.000 description 1
- 239000003814 drug Substances 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000005485 electric heating Methods 0.000 description 1
- 230000005611 electricity Effects 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 239000000575 pesticide Substances 0.000 description 1
- 238000011897 real-time detection Methods 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 230000011218 segmentation Effects 0.000 description 1
- 238000010792 warming Methods 0.000 description 1
- 238000005406 washing Methods 0.000 description 1
Classifications
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
- F23G7/00—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals
- F23G7/04—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals of waste liquors, e.g. sulfite liquors
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- Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Mechanical Engineering (AREA)
- General Engineering & Computer Science (AREA)
- Heat Treatment Of Water, Waste Water Or Sewage (AREA)
- Treatment Of Water By Oxidation Or Reduction (AREA)
Abstract
The present invention provides a kind of organic raffinats and waste water combined purifying system capacity dynamic equilibrium control method.Catalysis combustion integrative processing is carried out to raffinate and waste water in a fluidized bed.To guarantee that system is stablized, the present invention is to raffinate and wastewater feed design energy dynamic equilibrium controller.Using two close cycles variable-ratio control thought, firstly, carrying out heat balance to raffinate and waste water, the initial ratio of controller is determined by heat balance；Then, it carries out real-time heat according to the variation of raffinate calorific value and waste water COD during system operation and accounts, adjusted in real time according to ratio of the calculated result to controller, guarantee best charge proportion；Finally, homeostasis energy controller has safety allowance control function simultaneously, and when fluidized-bed temperature goes beyond the limit of range, dynamic power balance controller can further adjust heating furnace heating voltage, to guarantee the constant of fluidized bed internal temperature, the homeostasis energy of entire processing system is realized.
Description
Technical field
The invention belongs to the friendships of field of environment protection organic raffinat and waste water combined purifying process and industrial automation technology
Fork field, and in particular to organic raffinat and waste water combined purifying system capacity dynamic equilibrium control method.
Background technique
The important source of pollution first is that industrial wastewater, wherein organic wastewater with high concentration total emission volumn increases year by year, to current
Wastewater treatment and recycling bring huge technological challenge.Industrial wastewater is mainly derived from fine chemistry industry, medicine, print
The production processes such as dye, papermaking and pesticide, are usually expressed as high organic content in waste water, complicated component, have peculiar smell and strong acid
The characteristics such as alkali.In the catalysis burning process to waste water, can efficient coupling utilize Coal Gas Washing Cycling Water organic matter catalysis
The heat that oxidation reaction releases, realizes the self-sufficiency of energy, so that the energy consumption of wastewater treatment equipment be effectively reduced, realize it is low at
Sheet, low energy consumption, zero-emission economical operation.
Summary of the invention
The application is that a kind of organic raffinat and waste water combined purifying system are provided for technical problem of the existing technology
Homeostasis energy control method.This method is in the catalysis burning process of organic raffinat and waste water, by organic
The heat balance of raffinate and waste water, in real time adjust raffinate and waste water best charge proportion, guarantee the maximization of catalytic efficiency with
And the saving of energy.
The purpose of the present invention can be achieved through the following technical solutions:
A kind of organic raffinat and waste water combined purifying system capacity dynamic equilibrium control method, this method includes following step
It is rapid:
(1) before raffinate and wastewater treatment, heat balance is carried out according to organic matter calorific value in raffinate and COD value of waste water,
The heat balance that the total amount of heat and waste water vaporization absorption and air circulation that organic compound combustion is released are taken away, with this determine raffinate with
The charge proportion of waste water；
(2) to raffinate and one homeostasis energy controller of wastewater feed flow design, which uses two close cycles
Variable-ratio control scheme, wherein raffinate inlet amount is main momentum, and wastewater feed amount is to move during the reaction to energy from momentum
State balance calculates in real time, is adjusted in real time according to ratio of the calculated charge ratio to controller；
(3) it is heated up using heating furnace temperature-gradient method control system to fluidized bed before processing, reaches catalysis burning
It reacts the initial temperature occurred and keeps stable；
(4) after the completion of step (3), start to be passed through raffinate, waste water and sky into fluidized bed by the charge proportion calculated
Gas carries out catalyst combustion reaction, enters fixed bed from the gas of fluidized bed outlet discharge and further reacts, the gas warp handled
After heat exchange condensation, gas-liquid separation, obtained liquid enters the neutralizing tank containing sig water, finally enters rainwater direct discharge system.
In some preferred technical solutions: during step (4) carry out, controller is according to raffinate calorific value, waste water
COD value and feed rate carry out heat balance, right according to calculated best charge ratio when above-mentioned parameter fluctuates
The ratio value of the change ratio control of design carries out real-time monitoring, guarantees the constant of fluidized bed internal temperature, makes reacting balance
It carries out.
In above-mentioned technical proposal: when charge ratio adjusting is unable to maintain that fluidized bed internal temperature is stablized, starting fluidized bed electricity
Furnace temp compensates control model, guarantees that reacting balance carries out；When temperature is lower than lower limit value Tmin, fluidized bed electric heating furnace temperature
It spends controller and starts temperature raising control routine, increase heating voltage, fluidized-bed temperature increases, until temperature is returned to most preferably instead
Answer temperature；Similarly, when temperature is higher than upper limit value Tmax, fluidized bed temperature Control of Electric Heater device starting cooling control program, drop
Low heating voltage, fluidized-bed temperature decrease, until temperature is returned to optimal reaction temperature.
In some specific technical solutions, the initial charge ratio of waste water and raffinate is led to by raffinate calorific value and COD value of waste water
Heat balance calculation is crossed to determine, specific as follows:
Organic compound combustion reaction equation:
If the feed rate of air is Vairm3/ h, the feed rate of organic wastewater are Vwwm3/ h, density ρw, combustion heat value
For qn；The feed rate of organic raffinat is VwlL/h, density ρl, combustion heat value ql, oxidation operation discharges heat in waste water
For Qow, oxidation operation release heat is Q in raffinateol, then total thermal discharge is Q0=Qow+Qol.Wherein:
If water vapour thermal capacitance isThe latent heat of vaporization of the water at 100 DEG C is qH, 100, thermal capacitance Cpw；Organic liquid waste mole matter
Amount is Mibt, thermal capacitance Cporg；The heat that water vapor absorbs is Qawv, it is Q that water, which is increased to the sensible heat that 100 DEG C absorb from room temperature,aws,
The sensible heat that water vapour after vaporization is increased to reaction temperature absorption from 100 DEG C is Qass, it is Q that organic liquid waste, which absorbs sensible heat,aorg, then
The total amount of heat of absorption are as follows: Qa=Qawv+Qaws+Qass+Qaorg, in which:
Qawv=ρwVwwqH, 100/1000 (4)
Qaws=Cpw(373-Tin)·ρwVww/1000 (5)
Work as Q0=QaWhen reach heat balance, so that it is determined that the charging ratio K of raffinate and waste water, at this time:
The present invention controls fluidized bed catalytic burning process by way of heat balance, guarantees catalysis combustion
Energy is saved while burning efficiency.The phase calculates the suction heat evolution relationship of raffinate and waste water before the reaction, determines initial charge ratio；Benefit
It is heated up with heating furnace to fluidized bed, after reaching catalysis burning initial temperature, starts the charging of raffinate and waste water；In reaction process
In, controller adjusts charge ratio according to raffinate calorific value and waste water COD real-time perfoming heat balance, guarantees that charge ratio is best.When
When charge ratio adjusting is unable to maintain that fluidized bed internal temperature is stablized, by way of adjusting electric furnace voltage, guarantee that reaction is flat
It is steady to carry out.When temperature is lower than lower limit value Tmin, heating voltage is increased, fluidized-bed temperature increases；When temperature is higher than upper limit value
Tmax, heating furnace voltage is reduced, fluidized-bed temperature decreases.
Beneficial effects of the present invention:
The present invention devises a kind of organic raffinat and waste water combined purifying system capacity dynamic equilibrium control method.With it is common
Flow rate set value control method compare, the present invention in raffinate and during waste water combined purifying, to raffinate calorific value and waste water COD into
Row real-time detection adjusts the charge proportion of raffinate and waste water in real time according to system thermal equilibrium principle, both ensure that system temperature
It is constant, and saved energy.Meanwhile second is provided to reaction temperature in the heating furnace of fluidized bed outer wall and is ensured again, it is ensured that
The maximization of catalytic efficiency.
Detailed description of the invention
Fig. 1 is waste water of the invention and waste liquid initial charge ratio calculation flow chart.
Fig. 2 is energy balance controller dynamic control flow chart of the invention.
Fig. 3 is a specific embodiment of the invention process flow chart.
Fig. 4 is present invention specific implementation case effect picture.
Specific embodiment
Below with reference to embodiment, the present invention will be further described, and but the scope of the present invention is not limited thereto:
Organic raffinat and waste water combined purifying system capacity dynamic equilibrium control method, in a kind of neighbour/p-chlorobenzaldehyde essence
Evaporate the application in the combined purifying system of raffinate and technique waste water.
The process flow of combined purifying system is as shown in Figure 1-3, entire purification system is roughly divided into three parts, respectively
Fluidized bed, fixed bed and gas-liquid separation absorption plant.
Start the combined purifying processing unit of neighbour/p-chlorobenzaldehyde distillation residual liquid and technique waste water.
Start blower first, compressed air is passed through into fluidized bed, the purpose is to guarantee the oxygen-supplying amount in reaction process.
It followed by heats up to fluidized bed and fixed bed, heating furnace is housed in fluidized bed and fixed bed outer wall, using adding
The control of hot stove automatic segmentation temperature program by fluidized bed and fixed bed be warming up to 380 DEG C (catalyst combustion reaction temperature range are as follows:
350~450 DEG C).It is passed through chlorobenzaldehyde distillation residual liquid and technique waste water in proportion respectively, is fired in the catalysis of organic raffinat and waste water
It burns in treatment process, by the heat balance to organic raffinat and waste water, adjusts the best charge proportion of raffinate and waste water in real time,
Guarantee the maximization of catalytic efficiency and the saving of energy.
Be finally to reserved after fixed bed processing gas carry out the gas-liquid separator of gas-liquid separation absorption, absorption tower and in
And tank, the VOC of absorption tower discharge gas, the COD of neutralizing tank discharge liquid are detected, it is desirable that VOC content does not surpass in gas
Cross 45mg/m3, COD value is less than 80mgO in liquid2/L。
In the purification system, the organic raffinat thermal value range into fluidized bed is 10000~40000kJ/kg, waste water
COD is less than or equal to 50000mgO2/L.In view of the fluctuation of waste liquid calorific value, waste water COD, pass through the heat to organic raffinat and waste water
Amount is accounted, and using two close cycles variable-ratio control thought design energy dynamic equilibrium controller, is adjusted in real time with industrial wastewater most
Good charge proportion guarantees that the maximization of catalytic efficiency and plant energy consumption are minimum.Waste water and raffinate are fed, wherein chlorobenzaldehyde
Distillation residual liquid inlet amount is main momentum, and industrial wastewater inlet amount is from momentum.If oxidation operation release heat is Q in waste waterow,
Oxidation operation release heat is Q in raffinateol, then total thermal discharge is Q0=Qow+Qol；
The feed rate of air is Vair=110m3/ h, the feed rate of organic wastewater are Vww, COD value 40700mgO2/
L density is ρw=993.93kg/m3, combustion heat value qn=14000kJ/kg；The feed rate of organic liquid waste is Vwl=10L/h,
Density is ρl=770kg/m3, combustion heat value ql=35000kJ/kgO2, oxidation operation release heat is Q in waste waterow, residual
Oxidation operation release heat is Q in liquidol, then total thermal discharge is Q0=Qow+Qol.Wherein:
Water vapour thermal capacitance is Cps=4200J/ (molK), the latent heat of vaporization of the water at 100 DEG C are qH, 100=
2257.6kJ/kg thermal capacitance Cpw=4200J/ (molK)；Organic liquid waste molal weight is Mibt=168, thermal capacitance Cporg=
260.7kJ/(mol·K)；The heat that water vapor absorbs is Qawv, it is Q that water, which is increased to the sensible heat that 100 DEG C absorb from room temperature,aws, vapour
The sensible heat that water vapour after change is increased to reaction temperature absorption from 100 DEG C is Qass, it is Q that organic liquid waste, which absorbs sensible heat,aorg, then inhale
The total amount of heat of receipts are as follows: Qa=Qawv+Qaws+Qass+Qaorg, in which:
Work as Q0=QaWhen reach heat balance, so that it is determined that the charging ratio K of raffinate and waste water, at this time:
It is 40700mg/L that original state, which measures COD value of waste water, and waste liquid calorific value is 35000kJ/kg, unit COD organic wastewater
Combustion heat value be 14000kJ/kgO2, by the optimum ratio K=1.7 of the raffinate and waste water calculated, set two close cycles ratio
The ratio of controller enters the inlet amount of fluidized bed raffinate and waste water by the control of two close cycles ratio controller.
In fluidized bed catalytic burning process, controller can be real-time according to the variation of raffinate calorific value and waste water COD
Heat balance is calculated, the charge proportion (1~10:1) of raffinate and waste water is adjusted.
In adjustment process, when fluidized-bed temperature is lower than 360 DEG C, the starting heating of fluidized bed temperature Control of Electric Heater device
Program is controlled, adjusts heating voltage, fluidized-bed temperature increases, until temperature is returned to 380 DEG C of optimal reaction temperature；Work as stream
When changing bed tempertaure higher than 400 DEG C, fluidized bed temperature Control of Electric Heater device starting cooling control program reduces heating voltage, flows
Change bed tempertaure to decrease, until temperature is returned to 380 DEG C of optimal reaction temperature.
The gas and liquid sample that go out after processing are detected, VOC content is in 13mg/m in exhaust gas3~38mg/m3(<45mg/
m3) between in liquid COD value in 30mgO2/ L~67mgO2/L(<80mgO2/ L) between, meet emission request, it is right before and after the processing
Such as shown in Fig. 4 and following table.Flow rate set value control method and homeostasis energy control compare, and the present invention is dynamic by using energy
State balance controls more traditional flow setting control, and system operates normally stability and increases, and can effectively overcome feed constituents and stream
Amount disturbance, and energy consumption 20% can be reduced.
Claims (4)
1. a kind of organic raffinat and waste water combined purifying system capacity dynamic equilibrium control method, it is characterised in that: this method packet
Include following steps:
(1) before raffinate and wastewater treatment, heat balance is carried out according to organic matter calorific value in raffinate and COD value of waste water, it is organic
Total amount of heat and waste water vaporization absorption that object burning is released and the heat balance that air circulation is taken away, determine raffinate and waste water with this
Charge proportion；
(2) to raffinate and one homeostasis energy controller of wastewater feed flow design, which uses two close cycles no-load voltage ratio
It is worth control program, wherein raffinate inlet amount is main momentum, and wastewater feed amount is to put down during the reaction to energy dynamics from momentum
Weighing apparatus calculates in real time, is adjusted in real time according to ratio of the calculated charge ratio to controller；
(3) it is heated up using heating furnace temperature-gradient method control system to fluidized bed before processing, reaches catalyst combustion reaction
The initial temperature of generation simultaneously keeps stable；
(4) after the completion of step (3), start to be passed through raffinate, waste water and air into fluidized bed by the charge proportion calculated, into
Row catalyst combustion reaction enters fixed bed from the gas of fluidized bed outlet discharge and further reacts, and the gas handled is through exchanging heat
After condensation, gas-liquid separation, obtained liquid enters the neutralizing tank containing sig water, finally enters rainwater direct discharge system.
2. organic raffinat according to claim 1 and waste water combined purifying system capacity dynamic equilibrium control method, special
Sign is: during step (4) carry out, controller carries out heat according to raffinate calorific value, COD value of waste water and feed rate
It accounts, when above-mentioned parameter fluctuates, according to calculated best charge ratio, to the ratio of the change ratio control of design
Value carries out real-time monitoring, guarantees the constant of fluidized bed internal temperature, carries out reacting balance.
3. organic raffinat according to claim 2 and waste water combined purifying system capacity dynamic equilibrium control method, special
Sign is: when charge ratio adjusting is unable to maintain that fluidized bed internal temperature is stablized, starting the temperature-compensating control of fluidized bed electric furnace
Molding formula guarantees that reacting balance carries out；When temperature is lower than lower limit value Tmin, the starting heating of fluidized bed temperature Control of Electric Heater device
Program is controlled, increases heating voltage, fluidized-bed temperature increases, until temperature is returned to optimal reaction temperature；Similarly, work as temperature
Degree is higher than upper limit value Tmax, and fluidized bed temperature Control of Electric Heater device starting cooling control program reduces heating voltage, fluidized bed
Temperature decreases, until temperature is returned to optimal reaction temperature.
4. organic raffinat according to claim 1-3 and waste water combined purifying system capacity dynamic equilibrium controlling party
Method, it is characterised in that: the initial charge ratio of waste water and raffinate is true by Heat balance calculation by raffinate calorific value and COD value of waste water
It is fixed, specific as follows:
Organic compound combustion reaction equation:
If the feed rate of air is Vair m3/ h, the feed rate of organic wastewater are Vww m3/ h, density ρw, combustion heat value is
qn；The feed rate of organic raffinat is VwlL/h, density ρl, combustion heat value ql, oxidation operation release heat is in waste water
Qow, oxidation operation release heat is Q in raffinateol, then total thermal discharge is Q0=Qow+Qol；
Wherein:
If water vapour thermal capacitance isThe latent heat of vaporization of the water at 100 DEG C is qH, 100, thermal capacitance Cpw；Organic liquid waste molal weight is
Mibt, thermal capacitance Cporg；The heat that water vapor absorbs is Qawv, it is Q that water, which is increased to the sensible heat that 100 DEG C absorb from room temperature,aws, vaporization
The sensible heat that water vapour afterwards is increased to reaction temperature absorption from 100 DEG C is Qass, it is Q that organic liquid waste, which absorbs sensible heat,aorg, then absorb
Total amount of heat are as follows: Qa=Qawv+Qaws+Qass+Qaorg, in which:
Qawv=ρwVwwqH, 100/1000 (4)
Qaws=Cpw(373-Tin)·ρwVww/1000 (5)
Work as Q0=QaWhen reach heat balance, so that it is determined that the charging ratio K of raffinate and waste water, at this time:
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Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN2401789Y (en) * | 2000-01-27 | 2000-10-18 | 溧阳市河海起重设备有限公司 | Organic waste liquid cremation equipment |
| US20020170862A1 (en) * | 2001-03-19 | 2002-11-21 | Rudyuk Nikolay Vasillievich | Method of utilizing organic waste |
| CN107010761A (en) * | 2017-05-27 | 2017-08-04 | 南京工业大学 | A kind of combined purifying method of neighbour/4-chloro-benzaldehyde distillation residual liquid and technique waste water |
| CN107010709A (en) * | 2017-05-27 | 2017-08-04 | 南京工业大学 | The purification method of high-concentration phenolic wastewater during a kind of neighbour/Process of Hydroquinone Production |
| CN107055743A (en) * | 2017-05-27 | 2017-08-18 | 南京工业大学 | A kind of catalytic purification method of chlorination toluene Hydrolyze method producing benzaldehyde distillation residual liquid |
-
2018
- 2018-11-16 CN CN201811366508.8A patent/CN109323273B/en active Active
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN2401789Y (en) * | 2000-01-27 | 2000-10-18 | 溧阳市河海起重设备有限公司 | Organic waste liquid cremation equipment |
| US20020170862A1 (en) * | 2001-03-19 | 2002-11-21 | Rudyuk Nikolay Vasillievich | Method of utilizing organic waste |
| CN107010761A (en) * | 2017-05-27 | 2017-08-04 | 南京工业大学 | A kind of combined purifying method of neighbour/4-chloro-benzaldehyde distillation residual liquid and technique waste water |
| CN107010709A (en) * | 2017-05-27 | 2017-08-04 | 南京工业大学 | The purification method of high-concentration phenolic wastewater during a kind of neighbour/Process of Hydroquinone Production |
| CN107055743A (en) * | 2017-05-27 | 2017-08-18 | 南京工业大学 | A kind of catalytic purification method of chlorination toluene Hydrolyze method producing benzaldehyde distillation residual liquid |
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