CN112142264A - Treatment system and method for realizing zero discharge of landfill leachate and fermented biogas slurry - Google Patents
Treatment system and method for realizing zero discharge of landfill leachate and fermented biogas slurry Download PDFInfo
- Publication number
- CN112142264A CN112142264A CN202011042863.7A CN202011042863A CN112142264A CN 112142264 A CN112142264 A CN 112142264A CN 202011042863 A CN202011042863 A CN 202011042863A CN 112142264 A CN112142264 A CN 112142264A
- Authority
- CN
- China
- Prior art keywords
- pipeline
- outlet
- tower
- inlet
- wastewater
- 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.)
- Granted
Links
- 239000002002 slurry Substances 0.000 title claims abstract description 39
- 239000000149 chemical water pollutant Substances 0.000 title claims abstract description 35
- 238000000034 method Methods 0.000 title claims abstract description 31
- 239000002351 wastewater Substances 0.000 claims abstract description 68
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 claims abstract description 37
- 238000001704 evaporation Methods 0.000 claims abstract description 29
- 230000008020 evaporation Effects 0.000 claims abstract description 26
- 238000000855 fermentation Methods 0.000 claims abstract description 22
- 230000004151 fermentation Effects 0.000 claims abstract description 22
- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 claims abstract description 14
- 235000011114 ammonium hydroxide Nutrition 0.000 claims abstract description 14
- 239000007788 liquid Substances 0.000 claims abstract description 14
- 239000002699 waste material Substances 0.000 claims abstract description 10
- 238000005516 engineering process Methods 0.000 claims abstract description 8
- 238000000605 extraction Methods 0.000 claims abstract description 8
- 238000009833 condensation Methods 0.000 claims abstract description 3
- 230000005494 condensation Effects 0.000 claims abstract description 3
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 50
- 238000006481 deamination reaction Methods 0.000 claims description 40
- 230000009615 deamination Effects 0.000 claims description 38
- 238000003795 desorption Methods 0.000 claims description 27
- 239000007789 gas Substances 0.000 claims description 19
- 239000012528 membrane Substances 0.000 claims description 9
- 238000010612 desalination reaction Methods 0.000 claims description 6
- 230000015556 catabolic process Effects 0.000 claims description 4
- 238000006731 degradation reaction Methods 0.000 claims description 4
- 238000004821 distillation Methods 0.000 claims description 4
- 230000000813 microbial effect Effects 0.000 claims description 4
- 239000003795 chemical substances by application Substances 0.000 claims description 3
- 229910001873 dinitrogen Inorganic materials 0.000 claims description 3
- 238000010438 heat treatment Methods 0.000 claims description 3
- 238000010521 absorption reaction Methods 0.000 claims description 2
- 230000000694 effects Effects 0.000 claims description 2
- 238000004891 communication Methods 0.000 claims 1
- 208000028659 discharge Diseases 0.000 abstract description 17
- 230000008901 benefit Effects 0.000 abstract description 6
- 238000005265 energy consumption Methods 0.000 abstract description 5
- 150000003839 salts Chemical class 0.000 description 6
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 3
- 238000000108 ultra-filtration Methods 0.000 description 3
- VTYYLEPIZMXCLO-UHFFFAOYSA-L Calcium carbonate Chemical compound [Ca+2].[O-]C([O-])=O VTYYLEPIZMXCLO-UHFFFAOYSA-L 0.000 description 2
- CKUAXEQHGKSLHN-UHFFFAOYSA-N [C].[N] Chemical compound [C].[N] CKUAXEQHGKSLHN-UHFFFAOYSA-N 0.000 description 2
- 238000009835 boiling Methods 0.000 description 2
- 235000015097 nutrients Nutrition 0.000 description 2
- 239000002244 precipitate Substances 0.000 description 2
- 238000004064 recycling Methods 0.000 description 2
- 230000000717 retained effect Effects 0.000 description 2
- 239000010802 sludge Substances 0.000 description 2
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 description 1
- VEXZGXHMUGYJMC-UHFFFAOYSA-M Chloride anion Chemical compound [Cl-] VEXZGXHMUGYJMC-UHFFFAOYSA-M 0.000 description 1
- JLVVSXFLKOJNIY-UHFFFAOYSA-N Magnesium ion Chemical compound [Mg+2] JLVVSXFLKOJNIY-UHFFFAOYSA-N 0.000 description 1
- 229910021529 ammonia Inorganic materials 0.000 description 1
- BFNBIHQBYMNNAN-UHFFFAOYSA-N ammonium sulfate Chemical compound N.N.OS(O)(=O)=O BFNBIHQBYMNNAN-UHFFFAOYSA-N 0.000 description 1
- 229910052921 ammonium sulfate Inorganic materials 0.000 description 1
- 235000011130 ammonium sulphate Nutrition 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 230000004888 barrier function Effects 0.000 description 1
- 239000011575 calcium Substances 0.000 description 1
- 229910000019 calcium carbonate Inorganic materials 0.000 description 1
- 229910001424 calcium ion Inorganic materials 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 230000001112 coagulating effect Effects 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 238000002425 crystallisation Methods 0.000 description 1
- 230000008025 crystallization Effects 0.000 description 1
- 238000011033 desalting Methods 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
- 238000001914 filtration Methods 0.000 description 1
- ZLNQQNXFFQJAID-UHFFFAOYSA-L magnesium carbonate Chemical compound [Mg+2].[O-]C([O-])=O ZLNQQNXFFQJAID-UHFFFAOYSA-L 0.000 description 1
- 229910000021 magnesium carbonate Inorganic materials 0.000 description 1
- 239000001095 magnesium carbonate Substances 0.000 description 1
- 229910001425 magnesium ion Inorganic materials 0.000 description 1
- 244000005700 microbiome Species 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 238000001728 nano-filtration Methods 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 230000000737 periodic effect Effects 0.000 description 1
- 238000004062 sedimentation Methods 0.000 description 1
- 239000010865 sewage Substances 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 238000004065 wastewater treatment Methods 0.000 description 1
Images
Classifications
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F9/00—Multistage treatment of water, waste water or sewage
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/02—Treatment of water, waste water, or sewage by heating
- C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
- C02F1/041—Treatment of water, waste water, or sewage by heating by distillation or evaporation by means of vapour compression
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/02—Treatment of water, waste water, or sewage by heating
- C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
- C02F1/06—Flash evaporation
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/02—Treatment of water, waste water, or sewage by heating
- C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
- C02F1/10—Treatment of water, waste water, or sewage by heating by distillation or evaporation by direct contact with a particulate solid or with a fluid, as a heat transfer medium
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/20—Treatment of water, waste water, or sewage by degassing, i.e. liberation of dissolved gases
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
- C02F2101/10—Inorganic compounds
- C02F2101/16—Nitrogen compounds, e.g. ammonia
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
- C02F2103/06—Contaminated groundwater or leachate
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2301/00—General aspects of water treatment
- C02F2301/08—Multistage treatments, e.g. repetition of the same process step under different conditions
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
Landscapes
- Life Sciences & Earth Sciences (AREA)
- Hydrology & Water Resources (AREA)
- Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Water Supply & Treatment (AREA)
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Heat Treatment Of Water, Waste Water Or Sewage (AREA)
- Physical Water Treatments (AREA)
Abstract
The invention relates to a treatment system and a method for realizing zero discharge of landfill leachate and fermented biogas slurry, wherein waste water of the landfill leachate and the fermented biogas slurry is subjected to two times of heat extraction to remove most of ammonia nitrogen in the waste water, and ammonia water is obtained after condensation; removing residual ammonia nitrogen and volatilizable micromolecule COD by adopting a mechanical vapor recompression technology (MVR for short) and a forced circulation flash evaporation technology, and sending the ammonia nitrogen and the volatilizable micromolecule COD into a biochemical reactor for biochemical treatment to obtain regenerated backwater; carrying out innocent treatment on the residual high-concentration waste liquid; thereby realizing the zero discharge of the landfill leachate and the fermented biogas slurry. By adopting the system and the method, the waste water can be completely recycled, the zero discharge treatment of the high-ammonia-nitrogen and high-COD garbage percolate and the fermentation biogas slurry is realized, the biodegradability of the waste water is improved, the produced ammonia water can bring certain economic benefit, the operation and investment cost of the system is reduced, the heat energy in the system is recycled repeatedly, and the system and the method have the advantages of low energy consumption and high efficiency.
Description
Technical Field
The invention relates to the technical field of wastewater treatment and resource utilization, in particular to a treatment system and a treatment method for realizing zero discharge of garbage leachate and fermented biogas slurry.
Background
The landfill leachate and the fermentation biogas slurry are high-concentration organic wastewater, have high salt content, high chloride ion content, high COD concentration, high ammonia nitrogen content, complex components, seriously imbalanced proportion of microbial nutrient elements, difficult degradation and poor biodegradability, and belong to the wastewater which is difficult to treat. Aiming at the characteristics of high COD, ammonia nitrogen and salt content in landfill leachate and fermentation biogas slurry, the domestic current treatment process method for the wastewater mainly comprises the following steps: coagulating sedimentation, membrane method desalting, stripping deamination, evaporative crystallization, biochemical treatment and the like.
For example, chinese patent application CN201610357093.2 discloses a system and method for treating chemical wastewater based on a steam stripping and MVR combined process; the Chinese patent application CN201710789803.3 discloses a technology for treating high ammonia nitrogen wastewater by recovering ammonium sulfate through MVR ammonia distillation; the Chinese patent application CN201510525708.3 discloses a high-efficiency energy-saving sewage treatment method and a device. However, most of the existing documents only seek a single process method aiming at certain characteristics of the treated object, such as high ammonia nitrogen characteristics, and neglect the consideration of many aspects such as pursuing process method energy consumption, economic benefit, external environmental pollution and the like; for zero treatment discharge treatment devices of biogas slurry and leachate, a combination form of a pretreatment device, an anaerobic device, a nitrification and denitrification device, an ultrafiltration device, a nanofiltration device, an evaporation device and a sludge treatment device is mostly adopted, and the water quality characteristics of high ammonia nitrogen, high COD and high salt bring huge challenges to zero treatment discharge; the conventional treatment process is long and complicated, sludge is generated by adopting the traditional biochemical treatment process, and the concentrated solution treatment problem is generated by adopting the traditional membrane technology.
Disclosure of Invention
The invention aims to provide a treatment system and a treatment method for realizing zero discharge of landfill leachate and fermented biogas slurry, which aim to solve the problems of complex and long flow, easy membrane blockage, high energy consumption, poor biodegradability, insufficient utilization of valuable resources in wastewater and the like in the prior art, and seek a process method which has low treatment energy consumption and can realize the recycling and zero discharge of wastewater from the aspect of improving the biodegradability of the landfill leachate and the fermented biogas slurry so as to effectively remove ammonia nitrogen and COD in the wastewater.
In order to achieve the purpose, the technical scheme of the invention is as follows:
the invention discloses a treatment system for realizing zero discharge of landfill leachate and fermented biogas slurry, which is characterized by comprising the following components: the system comprises a water inlet preheater, a desorption tower, a deamination tower, an MVR evaporator, a forced circulation heat exchanger, a biochemical reactor and a condenser;
the cold side inlet of the water inlet preheater is connected with the outlet of the water inlet pump through a pipeline, the cold side outlet of the water inlet preheater is connected with the waste water inlet at the upper part of the analysis tower through a pipeline, the hot side inlet of the water inlet preheater is connected with the outlet of the condensate pump through a pipeline, and the hot side outlet of the water inlet preheater is connected with the biochemical reactor through a pipeline; the tower bottom outlet of the desorption tower is connected with the wastewater inlet at the upper part of the deamination tower through a pipeline; a steam outlet at the top of the deamination tower is connected with a gas phase inlet at the lower part of the desorption tower through a pipeline, and an outlet at the bottom of the deamination tower is connected with an inlet of a deamination circulating pump through a pipeline; the pipeline of the outlet of the deamination circulating pump is divided into two paths, one path is connected with the inlet of the reboiler, and the other path is connected with the water inlet of the MVR evaporator; the top outlet of the reboiler is connected with the reboiling liquid inlet of the deamination tower through a pipeline;
the vapor outlet of the MVR evaporator is connected with the inlet of a vapor compressor through a pipeline, and the concentrated solution outlet at the bottom of the MVR evaporator is connected with an evaporation circulating pump through a pipeline; the pipeline of the outlet of the evaporation circulating pump is divided into two paths, one path is connected with the tube pass inlet of the forced circulation heat exchanger through a pipeline, and the other path is connected with external concentrated solution treatment equipment (such as an incinerator) through a pipeline; a tube pass outlet of the forced circulation heat exchanger is connected with a concentrated solution inlet of the MVR evaporator through a pipeline, and the concentrated solution is sent back to the evaporator for circulating concentration; the outlet of the steam compressor is connected with the shell side inlet of the forced circulation heat exchanger through a pipeline; the shell pass outlet of the forced circulation heat exchanger is connected with the hot side inlet of the water inlet preheater through a pipeline;
the tower top steam outlet of the desorption tower is connected with the air inlet of the condenser through a pipeline; the ammonia water discharge port of condenser is connected with outside ammonia water storage facilities through the pipeline, and its noncondensable gas discharge port links to each other with the tail gas tower through the pipeline, the tail gas tower is equipped with the delivery pipe and communicates with each other with the atmosphere.
The treatment method for the landfill leachate and the fermentation biogas slurry by adopting the treatment system for realizing zero discharge of the landfill leachate and the fermentation biogas slurry comprises the following steps:
the method for treating the landfill leachate and the fermentation biogas slurry by using the treatment system for realizing zero discharge of the landfill leachate and the fermentation biogas slurry is characterized in that waste water of the landfill leachate and the fermentation biogas slurry is subjected to two times of heat extraction to remove most of ammonia nitrogen in the waste water, and ammonia water is obtained after condensation; removing residual ammonia nitrogen and volatilizable micromolecule COD by adopting a mechanical vapor recompression technology (MVR for short) and a forced circulation flash evaporation technology, and sending the ammonia nitrogen and the volatilizable micromolecule COD into a biochemical reactor for biochemical treatment to obtain regenerated backwater; carrying out innocent treatment on the residual high-concentration waste liquid; thereby realizing the zero discharge of the landfill leachate and the fermented biogas slurry.
More specifically, the method for treating the landfill leachate and the fermentation biogas slurry by using the treatment system for realizing zero emission of the landfill leachate and the fermentation biogas slurry is characterized by comprising the following steps of:
(1) feeding fresh wastewater consisting of landfill leachate and fermentation biogas slurry into the water inlet preheater, and exchanging heat with MVR condensate generated by the MVR evaporator to obtain preheated wastewater;
(2) feeding the preheated wastewater into the desorption tower, and stripping part of ammonia nitrogen in the preheated wastewater by adopting a stripping distillation process to obtain stripped wastewater; the ammonia nitrogen gas removed is sent into the condenser to be condensed into ammonia water with certain concentration, and the tail gas is discharged after being qualified through absorption treatment of the tail gas tower;
(3) the stripped wastewater is sent into the deamination tower, and ammonia nitrogen in the wastewater is extracted by adopting a thermal extraction method to obtain deamination wastewater and ammonia nitrogen steam; the ammonia nitrogen steam is sent back to the desorption tower to be used as a stripping heat source and a carrying agent of the desorption tower;
(4) the deamination wastewater is sent into the MVR evaporator for evaporation and desalination, and the desalination wastewater is sent into the forced circulation heat exchanger to obtain heat and then sent into the MVR evaporator for flash evaporation; the water, ammonia nitrogen and the micromolecule COD steam with lower boiling point which are separated by evaporation and flash evaporation are sent to the steam compressor to be upgraded into high-grade steam, and then the high-grade steam enters the forced circulation heat exchanger to be used as a heating heat source; after repeated evaporation and flash evaporation, salt and macromolecular COD are retained, the desalted wastewater is gradually concentrated into concentrated waste liquid with high calorific value, and then is discharged for harmless treatment;
(5) condensing the high-grade steam in the forced circulation heat exchanger to obtain MVR condensate, and then sending the MVR condensate back to the water inlet preheater to be used as a heat source;
(6) and the MVR condensate is subjected to heat exchange with the fresh wastewater in the water inlet preheater and then is further cooled, and then is sent into the biochemical reactor, ammonia nitrogen and micromolecule COD are removed by utilizing the microbial degradation effect, and finally the regenerated backwater is obtained.
Compared with the prior art, the invention has the following advantages:
the invention provides a system and a method for treating landfill leachate and fermentation biogas slurry, which are used for treating the landfill leachate and the fermentation biogas slurry with high ammonia nitrogen and high COD content through the working procedures of preheating, stripping analysis, heat extraction deamination, evaporation desalination, biochemical treatment and the like. By adopting the system and the method, the waste water can be completely recycled, the zero discharge treatment of the high-ammonia nitrogen and high-COD garbage percolate and the fermentation biogas slurry is realized, and the pollution to the external environment is avoided; the thermal extraction method is adopted in the deamination step, so that a large deamination tower is not needed, the pH value of the wastewater is not required to be increased in advance, and the operation and investment cost of a system can be reduced; the carbon-nitrogen ratio of the evaporated condensate is proper, so that the biodegradability of the wastewater is improved, no additional nutrient source is required, and the operation cost is reduced; the heat energy in the system is recycled repeatedly, and the system has the advantages of low energy consumption and high efficiency; meanwhile, the ammonia water with a use value is produced, and certain economic benefits can be brought while the problem of wastewater pollution is solved.
Drawings
FIG. 1 is a schematic view of a treatment system for realizing zero discharge of landfill leachate and fermented biogas slurry;
in the figure, 1-water inlet buffer tank, 2-water inlet pump, 3-water inlet preheater, 4-desorption tower, 5-intermediate transfer pump, 6-deamination tower, 7-deamination circulating pump, 8-reboiler, 9-MVR evaporator, 10-evaporation circulating pump, 11-vapor compressor, 12-forced circulation heat exchanger, 13-hot well, 14-condensate pump, 15-biochemical reactor, 16-blower, 17-suction pump, 18-condenser and 19-tail gas tower.
Detailed Description
It should be understood by those skilled in the art that the present embodiment is only for illustrating the present invention and is not to be used as a limitation of the present invention, and changes and modifications of the embodiment can be made within the scope of the claims of the present invention.
A processing system for realizing zero emission of landfill leachate and fermented biogas slurry comprises: a water inlet preheater 3, a desorption tower 4, a deamination tower 6, an MVR evaporator 9, a forced circulation heat exchanger 12, a biochemical reactor 15 and a condenser 18;
a cold side inlet of the water inlet preheater 3 is connected with an outlet of the water inlet pump 2 through a pipeline, a cold side outlet of the water inlet preheater is connected with a wastewater inlet at the upper part of the analysis tower 4 through a pipeline, a hot side inlet of the water inlet preheater is connected with an outlet of a condensate pump 14 through a pipeline, and a hot side outlet of the water inlet preheater is connected with the biochemical reactor 15 through a pipeline; the tower bottom outlet of the desorption tower 4 is connected with the wastewater inlet at the upper part of the deamination tower 6 through a pipeline; a steam outlet at the top of the deamination tower 6 is connected with a gas phase inlet at the lower part of the desorption tower 4 through a pipeline, and an outlet at the bottom of the deamination tower is connected with an inlet of a deamination circulating pump 7 through a pipeline; the pipeline at the outlet of the deamination circulating pump 7 is divided into two paths, one path is connected with the inlet of a reboiler 8, and the other path is connected with the water inlet of the MVR evaporator 9; the top outlet of the reboiler 8 is connected with the reboiling liquid inlet of the deamination tower 6 through a pipeline;
a steam outlet at the top of the MVR evaporator 9 is connected with an inlet of a steam compressor 11 through a pipeline, and a concentrated solution outlet at the bottom of the MVR evaporator is connected with an evaporation circulating pump 10 through a pipeline; the pipeline at the outlet of the evaporation circulating pump 10 is divided into two paths, one path is connected with the tube pass inlet of the forced circulation heat exchanger 12 through a pipeline, and the other path is connected with external concentrated waste liquid treatment equipment (such as an incinerator) through a pipeline; the tube pass outlet of the forced circulation heat exchanger 12 is connected with the concentrated solution inlet of the MVR evaporator 9 through a pipeline, and the concentrated solution is sent back to the evaporator for circulating concentration; the outlet of the vapor compressor 11 is connected with the shell side inlet of the forced circulation heat exchanger 12 through a pipeline; the shell side outlet of the forced circulation heat exchanger 12 is connected with the hot side inlet of the water inlet preheater heat 3 through a pipeline;
the top steam outlet of the desorption tower 4 is connected with the air inlet of the condenser 18 through a pipeline; the ammonia water discharge port of the condenser 18 is connected with an external ammonia water storage device through a pipeline.
Further, the water inlet of the water inlet pump 2 is connected with the water inlet buffer tank 1 of the landfill leachate and the fermentation biogas slurry.
Furthermore, an intermediate transfer pump 5 is arranged on a pipeline connecting the bottom outlet of the desorption tower 4 and the deamination tower 6.
Further, a hot well 13 is arranged at the outlet of the shell side of the forced circulation heat exchanger 12 and is used for collecting MVR condensate flowing out of the shell side; the outlet at the bottom of the hot well 13 is connected with the inlet of a condensate pump 14 through a pipeline, and the outlet of the condensate pump 14 is connected with the inlet at the hot side of the water inlet preheater 3 through a pipeline.
Further, the biochemical reactor 15 is a built-in membrane bioreactor, and a suction pump 17 is arranged on the biochemical reactor for conveying the water produced by the ultrafiltration membrane component to other places for recycling.
Further, the biochemical reactor 15 is connected with an air blower 16, and the air blower 16 is used for providing oxygen required by active microorganisms to the biochemical reactor and performing air friction cleaning on the ultrafiltration membrane module.
Further, a non-condensable gas discharge port of the condenser 18 is connected with a tail gas tower 19 through a pipeline and used for absorbing residual ammonia gas and COD micromolecules in the non-condensable gas, and the tail gas tower 19 is provided with a discharge pipe communicated with the atmosphere.
Example 1
The method for treating the landfill leachate and the fermentation biogas slurry by adopting the treatment system for realizing zero discharge of the landfill leachate and the fermentation biogas slurry comprises the following steps:
(1) feeding fresh wastewater consisting of landfill leachate and fermentation biogas slurry into a water inlet buffer tank 1 from the outside, then feeding the fresh wastewater into a water inlet preheater (plate-frame heat exchanger) 3 by a water inlet pump 2, performing heat exchange with condensate of MVR steam generated by an MVR evaporator 9, and further cooling the MVR condensate while primarily preheating the wastewater to obtain preheated wastewater;
(2) sending the preheated wastewater into the desorption tower 4 from a wastewater inlet at the upper part of the desorption tower, and stripping part of ammonia nitrogen in the wastewater by adopting a stripping distillation process in the desorption tower 4 to obtain stripped wastewater; ammonia nitrogen gas removed by stripping is sent into a condenser 18 from the top of the tower to be condensed into ammonia water with certain concentration, and tail gas is discharged after being absorbed and treated by a tail gas tower 19; the resolved wastewater is sent into a deamination tower 6 from a tower bottom outlet; because the leachate and the fermented biogas slurry contain HCO3-The desorption stripping can remove most of HCO3-Conversion to CO3 2-，CO3 2-Reacting with calcium and magnesium ions in the wastewater to generate calcium carbonate and magnesium carbonate precipitates, and removing the precipitates through periodic salt discharge to prevent scaling in the subsequent treatment process;
(3) the stripped wastewater is sent into a deamination tower 6, most ammonia nitrogen in the wastewater is extracted by a thermal extraction method, and deamination wastewater and ammonia nitrogen steam are obtained; the ammonia nitrogen steam is sent back to the desorption tower 4 and is used as a stripping heat source and a carrying agent of the desorption tower 4;
(4) the deamination wastewater is sent into an MVR evaporator 9 for evaporation and desalination, and external raw steam is adopted as a heat source in a deamination tower; the desalted wastewater is sent into a forced circulation heat exchanger 12 from a bottom outlet, and is sent into an MVR evaporator 9 again to be flashed after obtaining heat; evaporating and flashing in an MVR evaporator 9, evaporating water, ammonia nitrogen and micromolecule COD with lower boiling point to form secondary steam, sending the secondary steam into a mechanical steam compressor 11, improving the secondary steam into high-grade steam, and then sending the high-grade steam into a forced circulation heat exchanger 12 to be used as a heat source for heating desalted wastewater; after repeated evaporation and flash evaporation, salt and macromolecular COD are retained, the desalted wastewater is gradually concentrated into concentrated waste liquid with high calorific value, and then the concentrated waste liquid is discharged for harmless treatment (for example, the concentrated waste liquid is sent into an incinerator for incineration treatment);
(5) condensing the high-grade steam in a forced circulation heat exchanger, collecting the high-grade steam in a hot well to obtain MVR condensate containing ammonia nitrogen and micromolecular COD, wherein the MVR condensate has higher temperature and is sent back to the water inlet preheater 3 to be used as a heat source; the MVR condensate has the carbon-nitrogen ratio of 4-6, has strong biochemical property, can be directly subjected to biochemical treatment after being cooled, and solves the problem of low biochemical property of landfill leachate and fermented biogas slurry;
(6) the MVR condensate is subjected to heat exchange with fresh wastewater in the water inlet preheater 3, then is further cooled to a proper temperature, and then is sent into the membrane bioreactor 15, ammonia nitrogen and micromolecule COD are removed by utilizing the microbial degradation, the barrier filtration of the membrane enables the effluent to reach the standard stably, and finally the regenerated backwater is obtained.
Claims (9)
1. The utility model provides a realize processing system of landfill leachate and fermentation natural pond liquid zero release which characterized in that includes: the device comprises a water inlet preheater (3), a desorption tower (4), a deamination tower (6), an MVR evaporator (9), a forced circulation heat exchanger (12), a biochemical reactor (15) and a condenser (18);
a cold side inlet of the water inlet preheater (3) is connected with an outlet of the water inlet pump (2) through a pipeline, a cold side outlet of the water inlet preheater is connected with a waste water inlet at the upper part of the analysis tower (4) through a pipeline, a hot side inlet of the water inlet preheater is connected with an outlet of a condensate pump (14) through a pipeline, and a hot side outlet of the water inlet preheater is connected with the biochemical reactor (15) through a pipeline; the tower bottom outlet of the desorption tower (4) is connected with the wastewater inlet at the upper part of the deamination tower (6) through a pipeline; a steam outlet at the top of the deamination tower (6) is connected with a gas-phase inlet at the lower part of the desorption tower (4) through a pipeline, and an outlet at the bottom of the deamination tower is connected with an inlet of a deamination circulating pump (7) through a pipeline; the pipeline at the outlet of the deamination circulating pump (7) is divided into two paths, one path is connected with the inlet of the reboiler (8), and the other path is connected with the water inlet of the MVR evaporator (9); the top outlet of the reboiler (8) is connected with the reboiling liquid inlet of the deamination tower (6) through a pipeline;
a steam outlet of the MVR evaporator (9) is connected with an inlet of a steam compressor (11) through a pipeline, and a concentrated solution outlet at the bottom of the MVR evaporator is connected with an evaporation circulating pump (10) through a pipeline; the pipeline at the outlet of the evaporation circulating pump (10) is divided into two paths, one path is connected with the tube pass inlet of the forced circulation heat exchanger (12) through a pipeline, and the other path is connected with external concentrated waste liquid treatment equipment through a pipeline; the tube pass outlet of the forced circulation heat exchanger (12) is connected with the concentrated solution inlet of the MVR evaporator (9) through a pipeline; the outlet of the steam compressor (11) is connected with the shell side inlet of the forced circulation heat exchanger (12) through a pipeline; the shell side outlet of the forced circulation heat exchanger (12) is connected with the hot side inlet of the water inlet preheater (3) through a pipeline;
the top steam outlet of the desorption tower (4) is connected with the air inlet of the condenser (18) through a pipeline; and an ammonia water discharge port of the condenser (18) is connected with an external ammonia water storage device through a pipeline.
2. The treatment system according to claim 1, wherein the water inlet of the water inlet pump (2) is connected with a water inlet buffer tank (1) for landfill leachate and fermented biogas slurry.
3. The treatment system according to claim 1, wherein an intermediate transfer pump (5) is arranged on a pipeline connecting the bottom outlet of the desorption tower (4) and the deamination tower (6).
4. The treatment system according to claim 1, wherein a hot well (13) is provided at the shell-side outlet of the forced circulation heat exchanger (12); the bottom outlet of the hot well (13) is connected with the inlet of a condensate pump (14) through a pipeline, and the outlet of the condensate pump (14) is connected with the hot side inlet of the water inlet preheater (3) through a pipeline.
5. The treatment system according to claim 1, wherein the biochemical reactor (15) is a built-in membrane bioreactor having a suction pump (17) disposed thereon.
6. The processing system according to claim 1, wherein a blower (16) is connected to the biochemical reactor (15).
7. The treatment system according to claim 1, wherein the non-condensable gas discharge of the condenser (18) is connected by means of a pipe to a tail gas tower (19), the tail gas tower (19) being provided with a discharge pipe in communication with the atmosphere.
8. The method for treating the landfill leachate and the fermentation biogas slurry by adopting the treatment system as claimed in any one of claims 1 to 7, is characterized in that the waste water of the landfill leachate and the fermentation biogas slurry is subjected to two times of heat extraction to remove most of ammonia nitrogen in the waste water, and ammonia water is obtained after condensation; removing residual ammonia nitrogen and volatilizable micromolecule COD by adopting a mechanical vapor recompression technology and a forced circulation flash evaporation technology, and sending the ammonia nitrogen and the volatilizable micromolecule COD into a biochemical reactor for biochemical treatment to obtain regenerated backwater; carrying out innocent treatment on the residual high-concentration waste liquid; thereby realizing the zero discharge of the landfill leachate and the fermented biogas slurry.
9. The method for treating landfill leachate and fermented biogas slurry according to claim 8, comprising the steps of:
(1) feeding fresh wastewater consisting of landfill leachate and fermentation biogas slurry into the water inlet preheater, and exchanging heat with MVR condensate generated by the MVR evaporator to obtain preheated wastewater;
(2) feeding the preheated wastewater into the desorption tower, and stripping part of ammonia nitrogen in the preheated wastewater by adopting a stripping distillation process to obtain stripped wastewater; the ammonia nitrogen gas removed is sent into the condenser to be condensed into ammonia water with certain concentration, and the tail gas is discharged after being qualified through absorption treatment of the tail gas tower;
(3) the stripped wastewater is sent into the deamination tower, and ammonia nitrogen in the wastewater is extracted by adopting a thermal extraction method to obtain deamination wastewater and ammonia nitrogen steam; the ammonia nitrogen steam is sent back to the desorption tower to be used as a stripping heat source and a carrying agent of the desorption tower;
(4) the deamination wastewater is sent into the MVR evaporator for evaporation and desalination, and the desalination wastewater is sent into the forced circulation heat exchanger to obtain heat and then sent into the MVR evaporator for flash evaporation; the steam separated by evaporation and flash evaporation is sent into the steam compressor to be upgraded into high-grade steam, and then enters the forced circulation heat exchanger to be used as a heating heat source; after repeated evaporation and flash evaporation, the desalted wastewater is gradually concentrated into concentrated waste liquid with high calorific value, and then is discharged for harmless treatment;
(5) condensing the high-grade steam in the forced circulation heat exchanger to obtain MVR condensate, and then sending the MVR condensate back to the water inlet preheater to be used as a heat source;
(6) and the MVR condensate is subjected to heat exchange with the fresh wastewater in the water inlet preheater and then is further cooled, and then is sent into the biochemical reactor, ammonia nitrogen and micromolecule COD are removed by utilizing the microbial degradation effect, and finally the regenerated backwater is obtained.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202011042863.7A CN112142264B (en) | 2020-09-28 | 2020-09-28 | Treatment system and method for realizing zero emission of landfill leachate and fermented biogas slurry |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202011042863.7A CN112142264B (en) | 2020-09-28 | 2020-09-28 | Treatment system and method for realizing zero emission of landfill leachate and fermented biogas slurry |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN112142264A true CN112142264A (en) | 2020-12-29 |
| CN112142264B CN112142264B (en) | 2024-04-09 |
Family
ID=73895845
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202011042863.7A Active CN112142264B (en) | 2020-09-28 | 2020-09-28 | Treatment system and method for realizing zero emission of landfill leachate and fermented biogas slurry |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN112142264B (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112897785A (en) * | 2021-02-01 | 2021-06-04 | 上海瀛济环境科技有限公司 | Garbage leachate and fermentation biogas slurry wastewater zero-discharge process |
Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2004067922A (en) * | 2002-08-08 | 2004-03-04 | Sumikin Air Water Chemical Inc | Process for treating de-ammoniacal liquor |
| CN104445799A (en) * | 2014-10-09 | 2015-03-25 | 厦门紫金矿冶技术有限公司 | Treatment method of gold smelting plant high-salt wastewater hard to treat and containing ammonia and nitrogen |
| CN105036461A (en) * | 2015-07-02 | 2015-11-11 | 合肥白云环卫设备有限公司 | High-concentration ammonia nitrogen garbage leachate deep processing method |
| CN109455884A (en) * | 2018-12-21 | 2019-03-12 | 上海市政工程设计研究总院（集团）有限公司 | A kind of nitrogen resource thermal extraction recovery system |
| CN110482632A (en) * | 2019-09-27 | 2019-11-22 | 北京天地人环保科技有限公司 | Rubbish percolation liquid membrane concentrate evaporating concentrating method and system |
| CN111115933A (en) * | 2019-12-05 | 2020-05-08 | 江苏中圣高科技产业有限公司 | Flameless torch type ultra-clean discharge process for high-ammonia nitrogen wastewater containing VOCs |
| CN214115259U (en) * | 2020-09-28 | 2021-09-03 | 上海市政工程设计研究总院（集团）有限公司 | Treatment system for realizing zero discharge of landfill leachate and fermented biogas slurry |
-
2020
- 2020-09-28 CN CN202011042863.7A patent/CN112142264B/en active Active
Patent Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2004067922A (en) * | 2002-08-08 | 2004-03-04 | Sumikin Air Water Chemical Inc | Process for treating de-ammoniacal liquor |
| CN104445799A (en) * | 2014-10-09 | 2015-03-25 | 厦门紫金矿冶技术有限公司 | Treatment method of gold smelting plant high-salt wastewater hard to treat and containing ammonia and nitrogen |
| CN105036461A (en) * | 2015-07-02 | 2015-11-11 | 合肥白云环卫设备有限公司 | High-concentration ammonia nitrogen garbage leachate deep processing method |
| CN109455884A (en) * | 2018-12-21 | 2019-03-12 | 上海市政工程设计研究总院（集团）有限公司 | A kind of nitrogen resource thermal extraction recovery system |
| CN110482632A (en) * | 2019-09-27 | 2019-11-22 | 北京天地人环保科技有限公司 | Rubbish percolation liquid membrane concentrate evaporating concentrating method and system |
| CN111115933A (en) * | 2019-12-05 | 2020-05-08 | 江苏中圣高科技产业有限公司 | Flameless torch type ultra-clean discharge process for high-ammonia nitrogen wastewater containing VOCs |
| CN214115259U (en) * | 2020-09-28 | 2021-09-03 | 上海市政工程设计研究总院（集团）有限公司 | Treatment system for realizing zero discharge of landfill leachate and fermented biogas slurry |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112897785A (en) * | 2021-02-01 | 2021-06-04 | 上海瀛济环境科技有限公司 | Garbage leachate and fermentation biogas slurry wastewater zero-discharge process |
Also Published As
| Publication number | Publication date |
|---|---|
| CN112142264B (en) | 2024-04-09 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN101209881B (en) | System for processing leachate of garbage burning factory | |
| CN102910777B (en) | Treatment method for wastewater generated in cellulosic ethanol production | |
| CN107399876A (en) | A kind of processing method of high ammonia-nitrogen wastewater | |
| CN103922543A (en) | Garbage leaching liquor treatment method | |
| WO2014094484A1 (en) | Garbage leachate treatment method and system | |
| CN112093981A (en) | Sewage treatment device and process for synchronously and efficiently removing pollutants and comprehensively recycling pollutants | |
| CN112125461A (en) | Comprehensive treatment system and method for high-concentration ammonia nitrogen wastewater | |
| CN214115259U (en) | Treatment system for realizing zero discharge of landfill leachate and fermented biogas slurry | |
| CN111960590A (en) | Membrane concentrate treatment system of waste incineration power plant | |
| CN112142264B (en) | Treatment system and method for realizing zero emission of landfill leachate and fermented biogas slurry | |
| CN209618920U (en) | A kind of processing unit for landfill leachate | |
| CN104628065A (en) | Chemical pharmaceutical wastewater treatment system and method | |
| CN214360828U (en) | Sewage treatment device for synchronously removing high-efficiency pollutants and comprehensively recycling pollutants | |
| CN112897785A (en) | Garbage leachate and fermentation biogas slurry wastewater zero-discharge process | |
| CN104973642A (en) | Method of treating salt-containing waste water with low-temperature waste heat in flue gas | |
| CN103449591B (en) | High-concentration ammonia nitrogen wastewater treatment device | |
| CN117164037A (en) | Concentrated crystallization of high salt wastewater contains salt desalination water processing apparatus through heat pump | |
| CN207002529U (en) | Pyrazolone production wastewater treatment device | |
| CN103771649B (en) | Treatment method of 1,3-propanediol production wastewater | |
| CN115259518A (en) | System and method for treating percolate concentrated solution | |
| CN212425760U (en) | Chemical nickel plating effluent treatment plant | |
| CN111470564B (en) | Evaporation equipment and method with coupling of direct contact heat transfer and indirect contact heat transfer | |
| CN107188378A (en) | Pyrazolone production wastewater treatment device and its handling process | |
| CN110697959B (en) | Resource recycling method for high-salt high-ammonia nitrogen wastewater | |
| CN112661215A (en) | Treatment process and system for landfill leachate membrane concentrated solution |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant |