CN212387911U - Membrane concentrate processing system of landfill leachate - Google Patents
Membrane concentrate processing system of landfill leachate Download PDFInfo
- Publication number
- CN212387911U CN212387911U CN202020806314.1U CN202020806314U CN212387911U CN 212387911 U CN212387911 U CN 212387911U CN 202020806314 U CN202020806314 U CN 202020806314U CN 212387911 U CN212387911 U CN 212387911U
- Authority
- CN
- China
- Prior art keywords
- stage
- circulation
- outlet
- inlet
- liquid
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
- 239000012528 membrane Substances 0.000 title claims abstract description 76
- 239000012141 concentrate Substances 0.000 title claims abstract description 37
- 239000000149 chemical water pollutant Substances 0.000 title claims abstract description 34
- 238000012545 processing Methods 0.000 title claims abstract description 6
- 239000000463 material Substances 0.000 claims abstract description 31
- 238000001914 filtration Methods 0.000 claims abstract description 24
- 239000007791 liquid phase Substances 0.000 claims abstract description 24
- 238000000034 method Methods 0.000 claims abstract description 18
- 239000007788 liquid Substances 0.000 claims description 71
- 238000001704 evaporation Methods 0.000 claims description 70
- 230000008020 evaporation Effects 0.000 claims description 52
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 44
- 239000012295 chemical reaction liquid Substances 0.000 claims description 43
- 238000012546 transfer Methods 0.000 claims description 22
- 239000012071 phase Substances 0.000 claims description 21
- 239000002253 acid Substances 0.000 claims description 15
- 239000010813 municipal solid waste Substances 0.000 claims description 15
- 230000008595 infiltration Effects 0.000 claims description 8
- 238000001764 infiltration Methods 0.000 claims description 8
- 230000006835 compression Effects 0.000 claims description 7
- 238000007906 compression Methods 0.000 claims description 7
- 239000007790 solid phase Substances 0.000 claims description 6
- 238000002156 mixing Methods 0.000 claims description 4
- 238000001816 cooling Methods 0.000 claims description 3
- 238000001728 nano-filtration Methods 0.000 claims description 3
- 239000006260 foam Substances 0.000 abstract description 5
- 150000003839 salts Chemical class 0.000 abstract description 5
- 239000005416 organic matter Substances 0.000 abstract description 2
- 238000000926 separation method Methods 0.000 abstract 1
- 239000000243 solution Substances 0.000 description 56
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 description 6
- 239000012452 mother liquor Substances 0.000 description 6
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 description 5
- 238000006243 chemical reaction Methods 0.000 description 5
- 239000000498 cooling water Substances 0.000 description 5
- 238000010438 heat treatment Methods 0.000 description 5
- VEXZGXHMUGYJMC-UHFFFAOYSA-M Chloride anion Chemical compound [Cl-] VEXZGXHMUGYJMC-UHFFFAOYSA-M 0.000 description 4
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 4
- 238000009835 boiling Methods 0.000 description 4
- 238000013461 design Methods 0.000 description 4
- 238000005325 percolation Methods 0.000 description 4
- QJZYHAIUNVAGQP-UHFFFAOYSA-N 3-nitrobicyclo[2.2.1]hept-5-ene-2,3-dicarboxylic acid Chemical compound C1C2C=CC1C(C(=O)O)C2(C(O)=O)[N+]([O-])=O QJZYHAIUNVAGQP-UHFFFAOYSA-N 0.000 description 3
- -1 bicarbonate radical ions Chemical class 0.000 description 3
- 238000007599 discharging Methods 0.000 description 3
- 239000004021 humic acid Substances 0.000 description 3
- 239000008346 aqueous phase Substances 0.000 description 2
- 239000012153 distilled water Substances 0.000 description 2
- 229910001039 duplex stainless steel Inorganic materials 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 238000004134 energy conservation Methods 0.000 description 2
- 239000002351 wastewater Substances 0.000 description 2
- 230000033228 biological regulation Effects 0.000 description 1
- 230000003139 buffering effect Effects 0.000 description 1
- 239000000701 coagulant Substances 0.000 description 1
- 230000007797 corrosion Effects 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 238000011026 diafiltration Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000006073 displacement reaction Methods 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 230000003203 everyday effect Effects 0.000 description 1
- 238000002474 experimental method Methods 0.000 description 1
- 230000035611 feeding Effects 0.000 description 1
- 239000011152 fibreglass Substances 0.000 description 1
- 239000007789 gas Substances 0.000 description 1
- 230000005484 gravity Effects 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 230000007774 longterm Effects 0.000 description 1
- 238000005374 membrane filtration Methods 0.000 description 1
- 238000012544 monitoring process Methods 0.000 description 1
- 230000020477 pH reduction Effects 0.000 description 1
- 238000001556 precipitation Methods 0.000 description 1
- 238000003672 processing method Methods 0.000 description 1
- 239000012047 saturated solution Substances 0.000 description 1
- 239000002002 slurry Substances 0.000 description 1
- 238000012360 testing method Methods 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
Images
Abstract
The utility model discloses a landfill leachate's membrane concentrate processing system, including material membrane, feeding holding tank, sour jar, pre-heater, two-stage MVR forced circulation evaporimeter, filtration equipment and liquid phase back flow, the liquid phase back flow is used for sending back second grade MVR forced circulation evaporimeter evaporative concentration once more with the liquid phase that the filtering separation was come out. The system also comprises a first steam pipeline provided with a first steam compressor and a second steam pipeline provided with a second steam compressor, and the first steam pipeline and the second steam pipeline are used for providing the hot steam which is pressurized and heated to the two-stage MVR forced circulation evaporator. The membrane concentrated solution treatment method of the landfill leachate based on the system can effectively solve the technical problems that the landfill leachate scales, foams are more, and salt cannot be produced due to organic matter wrapping.
Description
Technical Field
The utility model belongs to the technical field of refuse treatment, concretely relates to landfill leachate's membrane concentrate processing system.
Background
The waste water generated in the process of landfill or incineration treatment of main municipal solid waste and the like in the landfill leachate contains a large amount of salt, organic matters, suspended matters and the like. In the prior art, a combined process of biochemical treatment and membrane filtration (including coagulant adding precipitation treatment, anaerobic treatment denitrification treatment and membrane treatment) is usually adopted to treat landfill leachate to obtain a concentrated solution, and then the concentrated solution is stored in a centralized manner, or is sent back to a landfill leachate tank for circulation treatment, or is directly subjected to MVR evaporation concentration (for example, a landfill leachate treatment system using an MVR evaporator disclosed in chinese patent document 201520543380.3). However, in view of the technical current situation of landfill leachate treatment engineering in China, the treatment of landfill leachate, especially landfill leachate concentrated solution still has many disadvantages, such as complex process, high energy consumption, easy scaling, large amount of foam and floating mud generation in the heating and evaporation processes, influence on the treatment effect of the concentrated solution, and great damage to equipment.
SUMMERY OF THE UTILITY MODEL
In order to overcome the problems in the prior art, the utility model provides a membrane concentrated solution treatment system and treatment method for garbage leachate.
In order to realize the above purpose, the utility model discloses the technical scheme who adopts is: a membrane concentrate treatment system for landfill leachate, comprising:
the material membrane is a nanofiltration membrane, the interception molecular weight is about 800(800 +/-200), the removal rate of COD is about 65% (65% +/-20), and the material membrane is connected with a feed pipe of the garbage percolation membrane concentrated solution and is used for receiving and intercepting the garbage percolation membrane concentrated solution to obtain a dilute phase solution;
the feeding adjusting tank is connected with the light-phase liquid outlet of the material membrane and is used for mixing and reacting the light-phase liquid with acid to obtain reaction liquid;
the acid tank is connected with the feeding adjusting tank and is used for providing acid for adjusting pH into the feeding adjusting tank;
the preheater is connected with the feeding adjusting tank and is used for preheating the reaction liquid;
the two-stage MVR forced circulation evaporator comprises a first-stage MVR forced circulation evaporator and a second-stage MVR forced circulation evaporator which are connected in series, wherein the first-stage MVR forced circulation evaporator is connected with the preheater and is used for carrying out first-stage evaporation concentration on the reaction liquid preheated by the preheater to obtain first-stage concentrated liquid; the second-stage MVR forced circulation evaporator is connected with the first-stage MVR forced circulation evaporator and is used for evaporating and concentrating the first-stage concentrated solution again to form a second-stage concentrated solution;
the first vapor pipeline is provided with a first vapor compressor, is connected with the first-stage MVR forced circulation evaporator and is used for providing hot vapor which is subjected to first-stage compression for the first-stage MVR forced circulation evaporator;
the second vapor pipeline is provided with a second vapor compressor, the inlet side of the second vapor pipeline is connected with the outlet side of the first vapor compressor, and the outlet side of the second vapor pipeline is connected with the second-stage MVR forced circulation evaporator and used for providing hot vapor subjected to two-stage compression for the second-stage MVR forced circulation evaporator;
the filtering equipment is connected with the secondary MVR forced circulation evaporator and is used for separating a solid phase from a liquid phase in the secondary concentrated solution;
the top of the secondary concentrated solution transfer tank is provided with a feed inlet connected with a discharge outlet at the bottom of the secondary evaporation chamber, and the top of the secondary concentrated solution transfer tank is also provided with a discharge outlet connected with a feed inlet of the filtering equipment;
and the inlet end of the liquid phase return pipe is connected with the liquid phase outlet end of the filtering device, and the outlet end of the liquid phase return pipe is connected with the secondary MVR forced circulation evaporator and used for returning the liquid phase separated by filtering to the secondary MVR forced circulation evaporator for secondary evaporation and concentration.
Preferably, the first-stage MVR forced circulation evaporator comprises a first-stage evaporation chamber, a first heat exchanger, a first circulation liquid outlet pipe, a first-stage circulation pump arranged on the first circulation liquid outlet pipe and a first circulation liquid inlet pipe; the shell side of the first heat exchanger is connected with a first steam pipeline, and the tube side of the first heat exchanger is provided with a first circulation inlet and a first circulation outlet; the first-stage evaporation chamber is provided with a reaction liquid inlet, a first-stage circulation outlet and a first-stage concentrated liquid outlet, the first-stage circulation inlet and the first-stage circulation outlet are positioned at the lower part of the side wall of the first-stage evaporation chamber and are positioned below the reaction liquid inlet, and the first-stage concentrated liquid outlet is positioned at the bottom of the first-stage evaporation chamber; the reaction liquid inlet is connected with the preheater, the primary circulation outlet is connected with the first circulation inlet through the first circulation liquid outlet pipe, and the primary circulation inlet is connected with the first circulation outlet through the first circulation liquid inlet pipe;
the second-stage MVR forced circulation evaporator comprises a second-stage evaporation chamber, a second heat exchanger, a second circulation liquid outlet pipe, a second-stage circulation pump arranged on the second circulation liquid outlet pipe and a second circulation liquid inlet pipe; the shell side of the second heat exchanger is connected with a second steam pipeline, and the tube side of the second heat exchanger is provided with a second circulation inlet and a second circulation outlet; the second-stage evaporation chamber is provided with a second-stage circulation inlet, a second-stage circulation outlet and a second-stage concentrated solution outlet, the second-stage circulation inlet and the second-stage circulation outlet are positioned at the lower part of the side wall of the second-stage evaporation chamber, and the second-stage concentrated solution outlet is positioned at the bottom of the second-stage evaporation chamber; the second-stage circulation outlet is connected with the second circulation inlet through a second circulation liquid outlet pipe, and the second-stage circulation inlet is connected with the second circulation outlet through a second circulation liquid inlet pipe; the outlet of the first-stage concentrated solution is connected with the second circulating liquid outlet pipe through a pipeline.
Preferably, the preheater is a two-stage preheater and comprises a first-stage preheater and a second-stage preheater which are connected in series; the device also comprises a condensate water tank, wherein the condensate water tank is provided with a condensate water inlet and a condensate water outlet, the condensate water inlet is connected with the bottom of the shell pass of the first heat exchanger and the bottom of the shell pass of the second heat exchanger through pipelines and is used for receiving condensate water formed by heat exchange and cooling of hot steam in the two-stage MVR forced circulation evaporator, and the condensate water outlet is connected with the first-stage preheater and is used for preliminarily preheating the reaction liquid; the second-stage preheater is connected with the shell pass of the first heat exchanger, the shell pass of the first heat exchanger is connected with the shell pass of the second heat exchanger through a pipeline, and the second-stage preheater is used for sending hot steam which is not condensed and carried in the two-stage MVR forced circulation evaporator into the second-stage preheater as a heat source.
Preferably, the system also comprises an expansion tank, wherein the lower part of the expansion tank is provided with a first steam inlet, and the upper part of the expansion tank is provided with a steam outlet; the upper portion of one-level evaporating chamber and the upper portion of second grade evaporating chamber all are equipped with the secondary steam export, and the secondary steam exit linkage that the first steam inlet that the lower part of expansion tank was equipped with passes through the secondary steam export that the upper portion of pipeline and one-level evaporating chamber was equipped with and/or the upper portion of second grade evaporating chamber was equipped with, and the steam outlet that the upper portion of expansion tank was equipped with passes through the entry linkage of pipeline and first steam compressor. The first-stage evaporation chamber and the second-stage evaporation chamber separate liquid drops in water vapor from the vapor to form secondary vapor, the temperature and the pressure of the secondary vapor are increased by a vapor compressor (about 15 ℃) and then return to the first-stage MVR forced circulation evaporator and the second-stage MVR forced circulation evaporator through the first vapor pipeline and the second vapor pipeline, heat energy is provided for obtaining first-stage concentrated solution and second-stage concentrated solution, low-temperature concentration is guaranteed on one hand, and on the other hand, high efficiency and energy conservation can be achieved.
Preferably, still include the concentrate transit tank, the top of concentrate transit tank is equipped with the feed inlet of being connected with the inlet pipe of rubbish infiltration membrane concentrate, and the bottom of concentrate transit tank is equipped with the discharge gate with material membrane access connection. An expansion tank is arranged in front of the compressor, so that feed liquid is prevented from entering the compressor, and preliminary pressurization and temperature rise are achieved in the expansion tank.
Preferably, still include the buffer tank, the top of buffer tank is equipped with the feed inlet through the light phase liquid exit linkage of pipeline with the material membrane, and the bottom of buffer tank is equipped with the discharge gate of being connected through pipeline and feeding adjusting tank.
Preferably, still include the reaction liquid transfer jar, the top of reaction liquid transfer jar is equipped with the feed inlet of being connected through pipeline and feeding adjusting tank, and the bottom of reaction liquid transfer jar is equipped with the discharge gate of being connected with the pre-heater for receive the reaction liquid that the feeding adjusting tank obtained, and transfer it to the pre-heater.
A membrane concentrated solution treatment method of landfill leachate is carried out based on the membrane concentrated solution treatment system of the landfill leachate provided with a material membrane and a two-stage MVR forced circulation evaporator, and comprises the following steps:
step 1, conveying the membrane concentrated solution of the landfill leachate to a material membrane through a feeding pipe of the membrane concentrated solution of the landfill leachate to obtain a light phase liquid; humic acid and Ca are intercepted by the material film2+And Mg2+，The water quality of the light phase liquid obtained after passing through the material film is as follows: the pH is 4-7, the COD is less than or equal to 9000mg/L, the ammonia nitrogen is less than or equal to 2000mg/L, the hardness is less than or equal to 7000 mg/L, the chloride ion is less than or equal to 40000mg/L, and the conductivity is about 140000 us/cm;
and 4, feeding the secondary concentrated solution obtained in the step 3 into a filtering device, separating a solid phase and a liquid phase in the secondary concentrated solution by the filtering device, feeding the separated liquid phase back to the secondary MVR forced circulation evaporator through a liquid phase return pipe, and evaporating and concentrating again.
Compared with the prior art, the utility model discloses the technological effect who gains has: through material membrane interception humic acid, macromolecular impurity etc. can improve the concentration multiple, prevent to heat the concentrated process and produce the foam, and then avoid the foam to get into the aqueous phase that evaporates out, guarantee that the aqueous phase is up to standard to discharge. The weak phase behind the material membrane is adjusted to the acidification, bicarbonate radical plasma wherein fully gets rid of, combine vapor compressor with two-stage MVR forced circulation evaporimeter again, realize low temperature acid evaporative concentration, avoid preheating, produce the scale deposit among the evaporative concentration process, guarantee the pre-heater, MVR forced circulation evaporimeter long-term effective operation, avoid influencing work efficiency and incremental cost because of the instrument damages, can effectively solve landfill leachate scale deposit, the foam is many, organic matter parcel leads to technical problem such as unable salt that goes out. In addition, the low-temperature treatment has low equipment requirement, 2205 duplex stainless steel can be selected, and the 2205 duplex stainless steel cannot be corroded.
The utility model discloses a landfill leachate's membrane concentrate processing system and processing method with two-stage MVR forced circulation evaporimeter, it is more energy-conserving, and can stabilize continuous operation, have higher treatment effeciency, the concentrated mother liquor total amount less than or equal to 10% of landfill leachate's membrane concentrate of discharging.
Drawings
Fig. 1 is a membrane concentrate treatment system diagram of landfill leachate in an embodiment of the present invention.
FIG. 2 is an enlarged view taken at Q1 in FIG. 1;
fig. 3 is an enlarged view at Q2 in fig. 1.
The reference numbers in the figures are: 1. the system comprises a condensate water tank, 2. a concentrated solution transfer tank, 3. a feed pump, 4. a material membrane, 5. a buffer tank, 6. a feed adjusting tank, 7. a reaction solution transfer tank, 8. a condensate water tank, 9. a secondary concentrated solution transfer tank, 10. an acid tank, 11. a primary preheater, 12. a secondary preheater, 13. a first heat exchanger, 14. a primary evaporation chamber, 15. a second heat exchanger, 16. a second steam compressor, 17. a secondary evaporation chamber, 18. an expansion tank, 19. a first steam compressor, 20. a primary circulating pump, 21. a secondary circulating pump, and 22. filtering equipment.
Detailed Description
The utility model discloses the following embodiment of combining does further detailing:
a membrane concentrate treatment system for landfill leachate, comprising:
the material membrane 4 is a nanofiltration membrane, is connected with a feed pipe of membrane concentrated solution of the landfill leachate, and is used for receiving and intercepting the membrane concentrated solution of the landfill leachate to obtain light-phase liquid;
the feeding adjusting tank 6 is connected with the light-phase liquid outlet of the material membrane 4 and is used for mixing and reacting the light-phase liquid and acid to obtain reaction liquid;
the acid tank 10 is connected with the feeding adjusting tank 6 through a pipeline and is used for providing acid for adjusting pH into the feeding adjusting tank 6, and a feeding pump arranged on the pipeline is a glass reinforced plastic acid pump;
the preheater is connected with the feeding adjusting tank 6 and is used for preheating the reaction liquid;
the two-stage MVR forced circulation evaporator comprises a first-stage MVR forced circulation evaporator and a second-stage MVR forced circulation evaporator which are connected in series, wherein the first-stage MVR forced circulation evaporator is connected with the preheater and is used for carrying out first-stage evaporation concentration on the reaction liquid preheated by the preheater to obtain first-stage concentrated liquid; the second-stage MVR forced circulation evaporator is connected with the first-stage MVR forced circulation evaporator and is used for evaporating and concentrating the first-stage concentrated solution again to form a second-stage concentrated solution;
the first steam pipeline is provided with a first steam compressor 19, is connected with the first-stage MVR forced circulation evaporator and is used for providing hot steam which is subjected to first-stage compression for the first-stage MVR forced circulation evaporator;
a second vapor pipeline provided with a second vapor compressor 16, wherein the inlet side of the second vapor pipeline is connected with the first vapor compressor 19, and the outlet side of the second vapor pipeline is connected with the second-stage MVR forced circulation evaporator and is used for providing hot vapor subjected to two-stage compression for the second-stage MVR forced circulation evaporator;
the filtering device 22 is connected with the secondary MVR forced circulation evaporator and is used for separating a solid phase from a liquid phase in the secondary concentrated solution;
and the inlet end of the liquid phase return pipe is connected with the liquid phase outlet end of the filtering device 22, and the outlet end of the liquid phase return pipe is connected with the secondary MVR forced circulation evaporator and used for returning the liquid phase separated by filtering to the secondary MVR forced circulation evaporator for evaporation and concentration again.
Specifically, the method comprises the following steps:
the first-stage MVR forced circulation evaporator comprises a first-stage evaporation chamber 14, a first heat exchanger 13, a first circulation liquid outlet pipe, a first-stage circulation pump 20 arranged on the first circulation liquid outlet pipe and a first circulation liquid inlet pipe; the shell side of the first heat exchanger 13 is connected with a first steam pipeline, and the tube side of the first heat exchanger 13 is provided with a first circulation inlet and a first circulation outlet; the first-stage evaporation chamber 14 is provided with a reaction liquid inlet, a first-stage circulation outlet and a first-stage concentrated liquid outlet, the first-stage circulation inlet and the first-stage circulation outlet are positioned at the lower part of the side wall of the first-stage evaporation chamber 14 and are positioned below the reaction liquid inlet, and the first-stage concentrated liquid outlet is positioned at the bottom of the first-stage evaporation chamber 14; the reaction liquid inlet is connected with the preheater, the first-stage circulation outlet is connected with the first circulation inlet through the first circulation liquid outlet pipe, and the first-stage circulation inlet is connected with the first circulation outlet through the first circulation liquid inlet pipe.
The second-stage MVR forced circulation evaporator comprises a second-stage evaporation chamber 17, a second heat exchanger 15, a second circulation liquid outlet pipe, a second-stage circulation pump 21 arranged on the second circulation liquid outlet pipe and a second circulation liquid inlet pipe; the shell side of the second heat exchanger 15 is connected with a second steam pipeline, and the tube side of the second heat exchanger 15 is provided with a second circulation inlet and a second circulation outlet; the secondary evaporation chamber 17 is provided with a secondary circulation inlet, a secondary circulation outlet and a secondary concentrated solution outlet, the secondary circulation inlet and the secondary circulation outlet are positioned at the lower part of the side wall of the secondary evaporation chamber 17, and the secondary concentrated solution outlet is positioned at the bottom of the secondary evaporation chamber 17; the second-stage circulation outlet is connected with the second circulation inlet through a second circulation liquid outlet pipe, and the second-stage circulation inlet is connected with the second circulation outlet through a second circulation liquid inlet pipe; the outlet of the first-stage concentrated solution is connected with the second circulating liquid outlet pipe through a pipeline.
The preheater is a two-stage preheater and comprises a first-stage preheater 11 and a second-stage preheater 12 which are connected in series; the device also comprises a condensate water tank 8, wherein the condensate water tank 8 is provided with a condensate water inlet and a condensate water outlet, the condensate water inlet is connected with the bottom of the shell pass of the first heat exchanger 13 and the bottom of the shell pass of the second heat exchanger 15 through pipelines and is used for receiving condensate water formed by heat exchange and cooling of hot steam in the two-stage MVR forced circulation evaporator, and the condensate water outlet is connected with the first-stage preheater 11 and is used for preliminarily preheating reaction liquid; the secondary preheater 12 is connected with the shell side of the first heat exchanger 13, and the shell side of the first heat exchanger 13 is connected with the shell side of the second heat exchanger 15 through a pipeline, and is used for sending hot steam carried by non-condensable gas in the two-stage MVR forced circulation evaporator into the secondary preheater 12 as a heat source. The reaction liquid is preheated primarily by the condensed water after the primary preheater 12 and the secondary preheater 12 are replaced, so that the heat energy is fully utilized, and the resource waste is avoided.
The steam-water separator further comprises an expansion tank 18, wherein a first steam inlet is formed in the lower part of the expansion tank 18, and a steam outlet is formed in the upper part of the expansion tank; the upper portion of one-level evaporating chamber 14 and the upper portion of second grade evaporating chamber 17 all are equipped with the secondary steam export, and the first steam inlet that the lower part of expansion tank 18 was equipped with passes through the secondary steam export that pipeline and the upper portion of one-level evaporating chamber 14 were equipped with and/or the secondary steam export that the upper portion of second grade evaporating chamber 17 was equipped with is connected, and the steam outlet that the upper portion of expansion tank 18 was equipped with passes through the pipeline and is connected with the entry of first steam compressor 19. The first-stage evaporation chamber 17 and the second-stage evaporation chamber 17 separate liquid drops in the water vapor from the vapor to form secondary vapor, the temperature and the pressure of the secondary vapor are increased by a vapor compressor (about 15 ℃) and then the secondary vapor returns to the first-stage MVR forced circulation evaporator and the second-stage MVR forced circulation evaporator through the first vapor pipeline and the second vapor pipeline, heat energy is provided for obtaining first-stage concentrated solution and second-stage concentrated solution, low-temperature concentration is guaranteed on one hand, and on the other hand, high efficiency and energy conservation can be achieved.
Still include concentrate transfer tank 2, the top of concentrate transfer tank 2 is equipped with the feed inlet of being connected with the inlet pipe of rubbish infiltration membrane concentrate, and the bottom of concentrate transfer tank 2 is equipped with the discharge gate with 4 access connection of material membrane. An expansion tank 18 is arranged in front of the compressor to prevent feed liquid from entering the compressor, and initial pressurization and temperature rise are achieved in the expansion tank 18.
Still include buffer tank 5, the top of buffer tank 5 is equipped with the feed inlet through the light phase liquid exit linkage of pipeline with material membrane 4, and the bottom of buffer tank 5 is equipped with the discharge gate of being connected through pipeline and feeding adjusting tank 6.
Still including reaction liquid transfer jar 7, the top of reaction liquid transfer jar 7 is equipped with the feed inlet of being connected through pipeline and feeding adjusting tank 6, and the bottom of reaction liquid transfer jar 7 is equipped with the discharge gate of being connected with the pre-heater for receive the reaction liquid that feeding adjusting tank 6 obtained, and transfer it to the pre-heater.
Still include second grade concentrate transit tank 9, the top is equipped with the feed inlet of being connected with second grade evaporation chamber 17 bottom discharge gate, and the top still is equipped with the discharge gate of being connected with filtration equipment 22 feed inlet.
The utility model discloses a filtration equipment is any one of filter, centrifuge or vacuum suction filter, and the filter is chooseed for use to this embodiment. The vapor compressor is any one of a centrifugal compressor, a positive displacement compressor or a screw compressor, and the centrifugal compressor is selected in the embodiment. The utility model discloses the rubbish filtration membrane concentrate of handling can be RO membrane concentrate, DTRO membrane concentrate, receive filter membrane concentrate or DT and receive filter membrane concentrate, and the concentrate that this embodiment was handled is DTRO membrane concentrate, (the embodiment is recorded should be one of them embodiment, can not understand as the restriction to it) the utility model discloses the function of three storage tanks before advancing the MVR system can exchange or share, including also can realizing functions such as buffering, regulation, feeding with two jars.
A method for treating a garbage infiltration membrane concentrated solution is carried out based on a garbage infiltration membrane concentrated solution treatment system provided with a two-stage MVR forced circulation evaporator, the water quality of the concentrated solution treated by the embodiment is shown in a table 1, and the specific treatment method comprises the following steps:
step 1, conveying the garbage infiltration membrane concentrated solution to a material membrane 4 through a feeding pipe of the garbage infiltration membrane concentrated solution to obtain a light phase solution; the water quality of the garbage percolation membrane concentrated solution before and after passing through the material membrane 4 is shown in table 2, the material membrane 4 intercepts humic acid and does not intercept Ca2+And Mg2+，The water quality of the light phase liquid obtained after passing through the material film 4 is as follows: the pH is 4-6, the COD is less than or equal to 2000mg/L, the ammonia nitrogen is less than or equal to 2000mg/L, the hardness is less than or equal to 975mg/L, the chloride ion is less than or equal to 29250mg/L, and the conductivity is 95 us/cm.
TABLE 1 reference water quality for concentrated water of DTRO membrane
| Serial number | Item | Detecting data |
| 1 | pH | 4～7 |
| 2 | COD(mg/L) | ≤25000 |
| 3 | Ammonia nitrogen (mg/L) | ≤2000 |
| 4 | Hardness (mg/L) | ≤7000 |
| 5 | Chloride ion (mg/L) | ≤40000 |
| 6 | Conductivity (us/cm) | ≤140000 |
TABLE 2 Water quality of the refuse diafiltration Membrane concentrate before and after passing through the Material Membrane
| Serial number | Item | Quality of inlet water | Quality of effluent water | Retention rate |
| 1 | pH | 4～7 | 4-7 | / |
| 2 | COD(mg/L) | ≤25000 | ≤10000 | 60％ |
| 3 | Ammonia nitrogen (mg/L) | ≤2000 | ≤2000 | 0％ |
| 4 | Hardness (mg/L) | ≤7000 | ≤7000 | 0％ |
| 5 | Chloride ion (mg/L) | ≤40000 | ≤40000 | 0％ |
| 6 | Conductivity (ms/cm) | ≤2140 | ≤133 | About 5 percent |
The material membrane 4 of the embodiment has a molecular weight interception less than 800 and a removal rate of COD of about 65%.
And 2, sending the light phase liquid obtained in the step 1 into a feeding adjusting tank 6, conveying hydrochloric acid (or sulfuric acid) into the feeding adjusting tank 6, and fully mixing the hydrochloric acid with the light phase liquid and removing bicarbonate radical ions to obtain a reaction liquid.
And 3, preheating the reaction liquid obtained in the step 2 to about 51 ℃ by a primary preheater 11, then preheating the reaction liquid to about 65 ℃ by a secondary preheater 12, feeding the reaction liquid subjected to two-stage preheating into a first heat exchanger 13, and heating the reaction liquid to flow into a primary evaporation chamber 14 by heat exchange to obtain a primary concentrated liquid. The primary concentrated solution is pumped to a second circulating liquid outlet pipe by a pump, then enters a second heat exchanger 15, enters a secondary evaporation chamber 17 after being subjected to heat exchange and heating by the second heat exchanger 15, and is evaporated and concentrated to obtain a secondary concentrated solution. The heat source for heating the reaction liquid by the first heat exchanger 13 is hot steam which is compressed by the first steam compressor 19 in one stage, the temperature of the hot steam is 76-74 ℃, the hot steam which is used for heat exchange and heating the concentrated solution in one stage by the second heat exchanger 15 is obtained by two-stage pressurization and temperature rise of the first steam compressor 19 and the second steam compressor 16 in sequence, the temperature of the obtained hot steam is about 85 ℃, and the pressure is about 57 KPa. The inlet sides of the first vapor compressor 19 and the second vapor compressor 16 are each connected to a vapor line for delivering live vapor for providing a source of heat upon system start-up.
In the first and second evaporation chambers, the secondary steam rises along the inner wall, the liquid droplets flow downwards under the action of gravity to be separated from the secondary steam, and the water vapor rises from the center, passes through the rotary vane separator to be separated into liquid droplets again and then enters the first steam compressor 19 for pressurization.
And 4, enabling the secondary concentrated solution obtained in the step 3 to enter a filtering device 22, separating a solid phase and a liquid phase in the secondary concentrated solution by the filtering device 22, sending the separated liquid phase back to the secondary MVR forced circulation evaporator through a liquid phase return pipe, and evaporating and concentrating again.
The two-stage MVR forced evaporator system of the embodiment adopts 1 vapor compressor to compress secondary vapor, so that the temperature of the secondary vapor can be increased by 15 ℃, and the secondary vapor is used as a heat source for evaporation of the system. In order to remove the superheat of the secondary steam generated by compression, water is injected at the compressor outlet. The two-stage MVR forced evaporator system is more energy-saving than a common evaporation process and is more stable than the common evaporation process, the mass of the mother liquor (namely, the mass of the second-stage concentrated solution) of the two-stage MVR forced evaporator system is less than or equal to 10% of the mass of the feeding amount (namely, the mass of the reaction solution) by the two-stage MVR forced evaporator system, and the equipment is free from corrosion and scaling.
In the process flow of the embodiment, each process condition is provided with a field display or parameter transmitter, the field display or parameter transmitter is controlled by a PLC in a centralized way, and monitoring, alarming and automatic control are carried out through configuration software of an industrial personal computer.
The specific process parameters of the above embodiment are as follows:
the feed concentration: a salt content of about 5%; feeding temperature: not less than 20 ℃; feed rate of material film 4: 150T/D; MVR feeding amount is 6.25 tons/hour;
evaporation capacity: greater than 5.343T/h; evaporation temperature: 40-100 ℃, and the temperature of the embodiment is preferably about 60 ℃; boiling point of saturated solution is increased: less than or equal to 40 ℃ and more preferably less than or equal to 16 ℃ in this example.
Discharging material state: filtering and discharging
Power consumption of the compressor: 52Kwh/T ≦ (determined by design)
Supplementary steam flow: < 20Kg/Hr (preheated to boiling point before start)
Circulating cooling water inlet water temperature: the return water temperature of the circulating cooling water is less than or equal to 32 ℃: less than or equal to 37 DEG C
Circulating cooling water inlet pressure: 0.25-0.5MPa
The return water pressure of the circulating cooling water is as follows: 0-0.1MPa
Flow rate of circulating cooling water: less than or equal to 40T/h
Power source capacity: 380V50Hz 4 line 600KVA
The occupied area is as follows: square meter not greater than 180 (determined by design)
Height of the equipment: less than or equal to 20 meters (determined by design)
Ambient temperature: 5-35 deg.C
Ambient humidity: 30 to 85 percent
Average air pressure: 101Kpa
Seismic intensity: less than or equal to 7 DEG
Ambient wind speed: less than or equal to 5 m/s.
150 tons of raw water per day (garbage percolation membrane concentrated solution) passes through the material membrane 4, the COD is less than or equal to 2000mg/L, and the concentration multiple is 18 times. The reaction solution enters a two-stage MVR forced circulation evaporator, and the concentration multiple is 10 times (the concentration multiple of the first-stage concentrated solution is 2-10 times). The feed rate of the two-stage MVR forced circulation evaporator is 6.25 tons/hour, the distilled water is 5.5 tons/hour, about 2.5 tons of salt slurry (which refers to a solid phase separated by filtration of the filtration device 22) is discharged every day, and about 15 tons of concentrated mother liquor (which refers to the concentrated mother liquor and the evaporation concentrated mother liquor after passing through the material membrane 4) is discharged. The total amount of the discharged concentrated mother liquor is less than or equal to 10 percent of the concentrated solution of the garbage infiltration membrane. According to the boiling point test result of the waste water, the boiling point is increased within 16 degrees within 10 times of concentration times. The experiment detects that the CODCr of the distilled water is less than or equal to 300mg/L, the ammonia nitrogen is less than or equal to 300mg/L and the pH is 2-10.5.
The above description is only the preferred embodiment of the present invention, but the scope of the present invention is not limited thereto, and any person skilled in the art can substitute or change the technical solution and the concept of the present invention within the technical scope disclosed in the present invention.
The utility model discloses not confine the following embodiment to, general technical personnel in this field can adopt other multiple embodiment to implement according to the utility model discloses a, perhaps all adopt the utility model discloses a design structure and thinking do simple change or change, all fall into the utility model discloses a protection scope. It should be noted that, in the present invention, the embodiments and features of the embodiments may be combined with each other without conflict.
In the description of the present invention, it is to be understood that the terms "center", "longitudinal", "lateral", "up", "down", "front", "back", "left", "right", "vertical", "horizontal", "top", "bottom", "inner", "outer", and the like, indicate orientations or positional relationships based on the orientations or positional relationships shown in the drawings, and are used merely for convenience of description and for simplicity of description, and do not indicate or imply that the device or element being referred to must have a particular orientation, be constructed and operated in a particular orientation, and therefore, should not be construed as limiting the present invention. Furthermore, the terms "first", "second", etc. are used for descriptive purposes only and are not to be construed as indicating or implying relative importance or implicitly indicating the number of technical features indicated. Thus, a feature defined as "first," "second," etc. may explicitly or implicitly include one or more of that feature. In the description of the present invention, "a plurality" means two or more unless otherwise specified.
In the description of the present invention, it is to be noted that, unless otherwise explicitly specified or limited, the terms "mounted," "connected," and "connected" are to be construed broadly, and may be, for example, fixedly connected, detachably connected, or integrally connected; can be mechanically or electrically connected; they may be connected directly or indirectly through intervening media, or they may be interconnected between two elements. The specific meaning of the above terms in the present invention can be understood by those of ordinary skill in the art through specific situations.
Claims (7)
1. The utility model provides a membrane concentrate processing system of landfill leachate which characterized in that: the method comprises the following steps:
the material membrane is a nanofiltration membrane, has the interception molecular weight of 800 +/-200 and the removal rate of COD of 65% +/-20%, is connected with a feed pipe of membrane concentrated solution of the landfill leachate, and is used for receiving and intercepting the membrane concentrated solution of the filtered landfill leachate to obtain light-phase liquid;
the feeding adjusting tank is connected with the light-phase liquid outlet of the material membrane and is used for mixing and reacting the light-phase liquid with acid to obtain reaction liquid;
the acid tank is connected with the feeding adjusting tank and is used for providing acid for adjusting pH into the feeding adjusting tank;
the preheater is connected with the feeding adjusting tank and is used for preheating the reaction liquid;
the two-stage MVR forced circulation evaporator comprises a first-stage MVR forced circulation evaporator and a second-stage MVR forced circulation evaporator which are connected in series, wherein the first-stage MVR forced circulation evaporator is connected with the preheater and is used for carrying out first-stage evaporation concentration on the reaction liquid preheated by the preheater to obtain first-stage concentrated liquid; the second-stage MVR forced circulation evaporator is connected with the first-stage MVR forced circulation evaporator and is used for evaporating and concentrating the first-stage concentrated solution again to form a second-stage concentrated solution;
the first vapor pipeline is provided with a first vapor compressor, is connected with the first-stage MVR forced circulation evaporator and is used for providing hot vapor which is subjected to first-stage compression for the first-stage MVR forced circulation evaporator;
the second vapor pipeline is provided with a second vapor compressor, the inlet side of the second vapor pipeline is connected with the outlet side of the first vapor compressor, and the outlet side of the second vapor pipeline is connected with the second-stage MVR forced circulation evaporator and used for providing hot vapor subjected to two-stage compression for the second-stage MVR forced circulation evaporator;
the filtering equipment is connected with the secondary MVR forced circulation evaporator and is used for separating a solid phase from a liquid phase in the secondary concentrated solution;
the top of the secondary concentrated solution transfer tank is provided with a feed inlet connected with a discharge outlet at the bottom of the secondary evaporation chamber, and the top of the secondary concentrated solution transfer tank is also provided with a discharge outlet connected with a feed inlet of the filtering equipment;
and the inlet end of the liquid phase return pipe is connected with the liquid phase outlet end of the filtering device, and the outlet end of the liquid phase return pipe is connected with the secondary MVR forced circulation evaporator and used for returning the liquid phase separated by filtering to the secondary MVR forced circulation evaporator for secondary evaporation and concentration.
2. The membrane concentrate treatment system for landfill leachate of claim 1, wherein: the first-stage MVR forced circulation evaporator comprises a first-stage evaporation chamber, a first heat exchanger, a first circulation liquid outlet pipe, a first-stage circulation pump arranged on the first circulation liquid outlet pipe and a first circulation liquid inlet pipe; the shell side of the first heat exchanger is connected with a first steam pipeline, and the tube side of the first heat exchanger is provided with a first circulation inlet and a first circulation outlet; the first-stage evaporation chamber is provided with a reaction liquid inlet, a first-stage circulation outlet and a first-stage concentrated liquid outlet, the first-stage circulation inlet and the first-stage circulation outlet are positioned at the lower part of the side wall of the first-stage evaporation chamber and below the reaction liquid inlet, and the first-stage concentrated liquid outlet is positioned at the bottom of the first-stage evaporation chamber; the reaction liquid inlet is connected with the preheater, the primary circulation outlet is connected with the first circulation inlet through the first circulation liquid outlet pipe, and the primary circulation inlet is connected with the first circulation outlet through the first circulation liquid inlet pipe;
the second-stage MVR forced circulation evaporator comprises a second-stage evaporation chamber, a second heat exchanger, a second circulation liquid outlet pipe, a second-stage circulation pump arranged on the second circulation liquid outlet pipe and a second circulation liquid inlet pipe; the shell side of the second heat exchanger is connected with a second steam pipeline, and the tube side of the second heat exchanger is provided with a second circulation inlet and a second circulation outlet; the secondary evaporation chamber is provided with a secondary circulation inlet, a secondary circulation outlet and a secondary concentrated solution outlet, the secondary circulation inlet and the secondary circulation outlet are positioned at the lower part of the side wall of the secondary evaporation chamber, and the secondary concentrated solution outlet is positioned at the bottom of the secondary evaporation chamber; the second-stage circulation outlet is connected with the second circulation inlet through a second circulation liquid outlet pipe, and the second-stage circulation inlet is connected with the second circulation outlet through a second circulation liquid inlet pipe; the outlet of the first-stage concentrated solution is connected with the second circulating liquid outlet pipe through a pipeline.
3. The membrane concentrate treatment system for landfill leachate of claim 2, wherein: the preheater is a two-stage preheater and comprises a first-stage preheater and a second-stage preheater which are connected in series; the device also comprises a condensate water tank, wherein the condensate water tank is provided with a condensate water inlet and a condensate water outlet, the condensate water inlet is connected with the bottom of the shell pass of the first heat exchanger and the bottom of the shell pass of the second heat exchanger through pipelines and is used for receiving condensate water formed by heat exchange and cooling of hot steam in the two-stage MVR forced circulation evaporator, and the condensate water outlet is connected with the first-stage preheater and is used for preliminarily preheating the reaction liquid; the secondary preheater is connected with the shell pass of the first heat exchanger, the shell pass of the first heat exchanger is connected with the shell pass of the second heat exchanger through a pipeline, and the secondary preheater is used for sending hot steam carried by non-condensable gas in the two-stage MVR forced circulation evaporator into the secondary preheater as a heat source.
4. The membrane concentrate treatment system for landfill leachate of claim 2, wherein: the steam-water separator further comprises an expansion tank, wherein the lower part of the expansion tank is provided with a first steam inlet, and the upper part of the expansion tank is provided with a steam outlet; the upper portion of one-level evaporating chamber and the upper portion of second grade evaporating chamber all are equipped with the secondary steam export, the secondary steam exit that the first steam inlet that the lower part of expansion tank was equipped with through the secondary steam export that pipeline and the upper portion of one-level evaporating chamber were equipped with and/or the secondary steam exit that the upper portion of second grade evaporating chamber was equipped with is connected, the steam outlet that the upper portion of expansion tank was equipped with passes through the entry linkage of pipeline and first steam compressor.
5. The membrane concentrate treatment system for landfill leachate of claim 1, wherein: still include the concentrate transit tank, the top of concentrate transit tank is equipped with the feed inlet of being connected with the inlet pipe of rubbish infiltration membrane concentrate, and the bottom of concentrate transit tank is equipped with the discharge gate with material membrane access connection.
6. The membrane concentrate treatment system for landfill leachate of claim 1, wherein: still include the buffer tank, the top of buffer tank is equipped with the feed inlet through the light phase liquid exit linkage of pipeline with the material membrane, the bottom of buffer tank is equipped with the discharge gate of being connected through pipeline and feeding adjusting tank.
7. The membrane concentrate treatment system for landfill leachate of claim 1, wherein: still include the reaction liquid transfer jar, the top of reaction liquid transfer jar is equipped with the feed inlet of being connected through pipeline and feeding adjusting tank, and the bottom of reaction liquid transfer jar is equipped with the discharge gate of being connected with the pre-heater for receive the reaction liquid that the feeding adjusting tank obtained, and transfer to the pre-heater in it.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202020806314.1U CN212387911U (en) | 2020-05-15 | 2020-05-15 | Membrane concentrate processing system of landfill leachate |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202020806314.1U CN212387911U (en) | 2020-05-15 | 2020-05-15 | Membrane concentrate processing system of landfill leachate |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN212387911U true CN212387911U (en) | 2021-01-22 |
Family
ID=74250236
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202020806314.1U Active CN212387911U (en) | 2020-05-15 | 2020-05-15 | Membrane concentrate processing system of landfill leachate |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN212387911U (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111392951A (en) * | 2020-05-15 | 2020-07-10 | 常州中源工程技术有限公司 | Membrane concentrated solution treatment system and treatment method for landfill leachate |
-
2020
- 2020-05-15 CN CN202020806314.1U patent/CN212387911U/en active Active
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111392951A (en) * | 2020-05-15 | 2020-07-10 | 常州中源工程技术有限公司 | Membrane concentrated solution treatment system and treatment method for landfill leachate |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN111392951A (en) | Membrane concentrated solution treatment system and treatment method for landfill leachate | |
| CN104341072A (en) | Energy-saving waste-water continuous evaporating crystallizing system | |
| CN112624475A (en) | Zero-discharge treatment system and process for landfill leachate | |
| CN212387911U (en) | Membrane concentrate processing system of landfill leachate | |
| CN104310514A (en) | Efficient mechanical vapor recompression seawater desalination method | |
| CN204588906U (en) | Mercury-containing waste water desalination special processor | |
| CN211971803U (en) | Novel materialized wastewater triple-effect evaporation system | |
| CN110790333A (en) | Leachate treatment system of hazardous waste disposal center | |
| CN114349093A (en) | Multi-effect evaporation system for evaporating and concentrating high-salinity wastewater and adjusting method | |
| CN210764418U (en) | Evaporation crystallization separation integration system | |
| CN104014144A (en) | Multiple-effect evaporation system evaporation condensation water heat energy reutilizationoun device | |
| CN212269512U (en) | Concentrated material of MVR evaporimeter system of evaporating again | |
| CN210367047U (en) | Multistage flash distillation desulfurization effluent treatment plant | |
| CN203935630U (en) | Multi-effect evaporation system evaporation condensed water heat energy recycling device | |
| CN106744720A (en) | The circulation recycling system and its operation process of trichloroacetaldehyde by-product dilute sulfuric acid | |
| CN204151184U (en) | A kind of energy-conservation waste water continuous evaporative crystallization system | |
| CN113816549A (en) | Ammonia nitrogen recovery method in kitchen waste treatment process | |
| CN209890424U (en) | Treatment system for recycling nanofiltration concentrated solution | |
| CN213077507U (en) | Continuous enrichment facility of corrosivity feed liquid | |
| CN220618504U (en) | High-efficient denitrification negative pressure low temperature evaporation plant | |
| CN217773246U (en) | Single-effect evaporation waste heat utilization system | |
| CN215049413U (en) | High salt water treatment facilities | |
| CN218478566U (en) | High concentration sewage concentration system | |
| CN102745755A (en) | Process for recovering sodium sulfate crystal in sebacic acid production | |
| CN215798981U (en) | Leachate concentrated water disposal system device |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| GR01 | Patent grant | ||
| GR01 | Patent grant | ||
| CP03 | Change of name, title or address |
Address after: 213000, No. 16 Donggang Second Road, Weicun Street, Xinbei District, Changzhou City, Jiangsu Province Patentee after: Changzhou Zhongyuan Technology Co.,Ltd. Country or region after: China Address before: 213000 No.82 anjiazhenxing Road, Chunjiang Town, Xinbei District, Changzhou City, Jiangsu Province Patentee before: CHANGZHOU ZHONGYUAN ENGINEERING TECHNOLOGY Co.,Ltd. Country or region before: China |
|
| CP03 | Change of name, title or address |