CN219449378U - Energy-saving deacidification ammonia distillation device - Google Patents
Energy-saving deacidification ammonia distillation device Download PDFInfo
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- CN219449378U CN219449378U CN202320082668.XU CN202320082668U CN219449378U CN 219449378 U CN219449378 U CN 219449378U CN 202320082668 U CN202320082668 U CN 202320082668U CN 219449378 U CN219449378 U CN 219449378U
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- deacidification
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- water
- ammonia distillation
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
Abstract
The utility model relates to the technical field of industrial wastewater treatment, in particular to an energy-saving deacidification ammonia distillation device. Comprises a deacidification ammonia distillation tower, a reboiler, a residual ammonia water cooler, a No. 1 waste heat water heat exchanger, a waste water cooler, a vapor-liquid separator, a No. 2 waste heat water heat exchanger and an ammonia condenser; the bottom of the deacidification ammonia distillation tower, the No. 1 waste heat water heat exchanger, the waste water cooler and the phenol-cyanogen waste water treatment device are connected through pipelines in sequence; the residual ammonia water pipeline, the residual ammonia water cooler and the top of the deacidification ammonia distillation tower are connected in turn through pipelines; the top of the deacidification ammonia distillation tower is connected with a gas pipeline before desulfurization or an ammonium sulfate saturator pipeline in an ammonium sulfate process; the middle part of the deacidification ammonia distillation tower, the vapor-liquid separator, the No. 2 waste heat water heat exchanger and the ammonia condenser are connected through pipelines in sequence; the waste water pipeline at the bottom of the deacidification ammonia still is connected with a reboiler pipeline, and the outlet of the reboiler is connected with a vapor phase space pipeline at the bottom of the deacidification ammonia still. Can greatly reduce the energy consumption and the running cost of the coking ammonia distillation, and has the advantages of less equipment investment and low operating cost.
Description
Technical Field
The utility model relates to the technical field of industrial wastewater treatment, in particular to an energy-saving deacidification ammonia distillation device.
Background
Coking residual ammonia water is complex in composition, wherein impurity ammonia exists in three forms: free NH 3 Volatile ammonium salts and fixed ammonium salts. The volatile ammonium salt is mainly ammonium carbonate, ammonium sulfide, ammonium cyanide and the like, and is easy to decompose into ammonia, hydrogen sulfide, carbon dioxide, hydrogen cyanide and other gases when heated, but the fixed ammonium salt can be decomposed by adding alkali.
At present, the coking residual ammonia water is deaminated by adopting a steam stripping method, and the vaporized ammonia steam is sent to a gas pipeline or a saturator before a desulfurization unit, or is prepared into concentrated ammonia water for take-out, and the like. The deamination process by the stripping method is mature and widely applied, but the method has higher steam consumption and higher operation cost, and the common coking ammonia distillation process is pure energy input, so that no product profit is available.
The common residual ammonia water ammonia distillation process in the coking industry generally comprises a conventional normal pressure ammonia distillation process and a heat pump ammonia distillation process; the conventional normal-pressure ammonia distillation process has mature technology and stable operation, but the process consumes large steam quantity, consumes about 170-200 kg of low-pressure steam per 1 ton of residual ammonia water, and has large energy consumption and high running cost. In order to reduce the energy consumption of ammonia distillation, the heat pump ammonia distillation process adopts a second type of absorption heat pump to recover the latent heat of ammonia vapor at the top of the ammonia distillation tower for heating the wastewater at the bottom of the tower, so that partial heat sources are provided, and the energy consumption of ammonia distillation is saved. The process can reduce 34% of ammonia distillation operation cost, but the process adds more equipment, has larger investment on fixed equipment and also makes the ammonia distillation operation more complicated.
Disclosure of Invention
In order to overcome the defects of the prior art, the utility model provides the energy-saving deacidification ammonia distillation device which can greatly reduce the energy consumption and the running cost of coking ammonia distillation, and has the advantages of less equipment investment, low operation cost and simple process flow.
In order to achieve the above purpose, the utility model is realized by adopting the following technical scheme:
an energy-saving deacidification ammonia distillation device comprises a deacidification ammonia distillation tower, a reboiler, a residual ammonia water cooler, a No. 1 waste heat water heat exchanger, a waste water cooler, a vapor-liquid separator, a No. 2 waste heat water heat exchanger and an ammonia condenser; the bottom of the deacidification ammonia distillation tower, the No. 1 waste heat water heat exchanger, the waste water cooler and the phenol-cyanogen waste water treatment device are connected through pipelines in sequence; the residual ammonia water pipeline, the residual ammonia water cooler and the top of the deacidification ammonia distillation tower are connected in turn through pipelines; the top of the deacidification ammonia distillation tower is connected with a gas pipeline before desulfurization or an ammonium sulfate saturator pipeline in an ammonium sulfate process; the middle part of the deacidification ammonia distillation tower, the vapor-liquid separator, the No. 2 waste heat water heat exchanger and the ammonia condenser are connected through pipelines in sequence; the waste water pipeline at the bottom of the deacidification ammonia still is connected with a reboiler pipeline, and the outlet of the reboiler is connected with a vapor phase space pipeline at the bottom of the deacidification ammonia still.
Further, the deacidification ammonia distillation device also comprises a wastewater pump, and the bottom of the deacidification ammonia distillation tower is connected with an inlet pipeline of the wastewater pump; and the outlet of the wastewater pump is connected with a pipeline of the No. 1 waste heat water heat exchanger.
Further, the liquid phase interface end of the vapor-liquid separator is connected with a pipeline in the middle of the deacidification ammonia distillation tower; the gas phase interface end of the gas-liquid separator is connected with an ammonia gas inlet pipeline of the No. 2 waste heat water heat exchanger.
Compared with the prior art, the utility model has the beneficial effects that:
1. in the aspect of energy consumption saving, compared with the traditional ammonia distillation which needs to consume 170 kg-200 kg of steam/ton of residual ammonia water, the technology disclosed by the utility model only needs to consume 135kg of steam/ton of residual ammonia water, thereby saving the steam consumption by about 32%; compared with the traditional coking ammonia distillation process with about 8-9 t circulating water/ton residual ammonia water consumption, the circulating water consumption is low, and is only 3.3t circulating water/ton residual ammonia water, so that the circulating water consumption is saved by 63%.
2. In the aspect of waste heat recovery, unlike the existing ammonia distillation technology, the process can recover 5.8t of circulating hot water/ton of residual ammonia water, and the circulating hot water for recovering the ammonia distillation waste heat can be used as a heat source for a summer refrigerator or a winter heating supply of a coking plant or as a heat source of a vacuum potassium carbonate desulfurization regeneration tower, so that the self energy utilization rate of the coking plant is greatly improved, and the running cost of a production enterprise is reduced.
3. Compared with the conventional normal-pressure ammonia distillation process, the process disclosed by the utility model uses the cooled residual ammonia water as the cold reflux liquid at the top of the tower, and performs direct mass transfer and heat transfer with the rising stripping steam in the tower, so that an ammonia distillation tower top separator is not required to be additionally arranged, the use of titanium materials of the separator is reduced, the residual ammonia water cooler is made of carbon steel, and the process reduces the equipment investment.
4. In terms of equipment arrangement, unlike the prior ammonia distillation technology in which an ammonia separator is arranged at the top of an ammonia distillation tower, the residual ammonia water cooler in the process can be arranged on the ground, so that the strength requirement of the ammonia distillation tower is further reduced, and the requirement of an operator on the operation of the tower top is reduced.
The utility model cools the residual ammonia water, and then the residual ammonia water enters the top of the deacidification ammonia distillation tower, clean ammonia vapor is extracted from the middle side line of the deacidification ammonia distillation tower and is used for preparing relatively clean concentrated ammonia water, and the waste heat of the ammonia vapor extracted from the side line and the waste water at the bottom of the deacidification ammonia distillation tower can be used for preparing hot water at 63-73 ℃ for heat recycling, so that a heat source can be provided for a refrigerator in summer or heating in winter of a coking plant, the coking waste heat utilization rate is improved, and the utility model is an ammonia distillation process with less equipment investment, low operation cost and simple process flow.
Drawings
FIG. 1 is a schematic structural and process diagram of the present utility model.
In the figure: 1-deacidification ammonia distillation tower, 2-reboiler, 3-wastewater pump, 4-surplus aqueous ammonia cooler, 5-1# waste heat water heat exchanger, 6-waste water cooler, 7-vapour-liquid separator, 8-2# waste heat water heat exchanger, 9-ammonia condenser.
Detailed Description
Embodiments of the present utility model are described in detail below, examples of which are illustrated in the accompanying drawings, wherein like or similar reference numerals refer to like or similar elements or elements having like or similar functions throughout. The embodiments described below by referring to the drawings are illustrative only and are not to be construed as limiting the utility model.
In the description of the present utility model, it should be understood that the terms "center", "longitudinal", "lateral", "length", "width", "thickness", "upper", "lower", "left", "right", "vertical", "horizontal", "top", "bottom", "inner", "outer", "axial", "radial", "circumferential", etc. indicate orientations or positional relationships based on the orientations or positional relationships shown in the drawings are merely for convenience in describing the present utility model and simplifying the description, and do not indicate or imply that the device or element in question must have a specific orientation, be configured and operated in a specific orientation, and therefore should not be construed as limiting the present utility model. In the description of the present utility model, it should be noted that, unless explicitly specified and limited otherwise, the terms "mounted," "connected," and "connected" are to be construed broadly, and may be either fixedly connected, detachably connected, or integrally connected, for example; can be directly connected or indirectly connected through an intermediate medium, and can be communication between two elements. The specific meaning of the above terms in the present utility model will be understood in specific cases by those of ordinary skill in the art.
The following is a further description of embodiments of the utility model, taken in conjunction with the accompanying drawings:
as shown in fig. 1, the energy-saving deacidification ammonia distillation device comprises a deacidification ammonia distillation tower 1, a reboiler 2, a waste water pump 3, a residual ammonia water cooler 4, a No. 1 waste heat water heat exchanger 5, a waste water cooler 6, a vapor-liquid separator 7, a No. 2 waste heat water heat exchanger 8 and an ammonia condenser 9.
The bottom of the deacidification ammonia distillation tower 1 is connected with an inlet pipeline of a wastewater pump 3, and an outlet of the wastewater pump 3 is connected with a pipeline of a No. 1 waste heat water heat exchanger 5; the outlet of the No. 1 waste heat water heat exchanger 5 is connected with the inlet pipeline of the waste water cooler 6; the wastewater outlet of the wastewater cooler 6 is connected with a pipeline of the phenol-cyanogen wastewater treatment device.
The residual ammonia water pipeline is connected with an ammonia water inlet pipeline of the residual ammonia water cooler 4; the ammonia water outlet of the residual ammonia water cooler 4 is connected with a pipeline at the top of the deacidification ammonia distillation tower 1; the top of the deacidification ammonia distillation tower 1 is connected with a gas pipeline before desulfurization or an ammonium sulfate saturator pipeline in an ammonium sulfate process.
The middle part of the deacidification ammonia distillation tower 1 is connected with a pipeline of a vapor-liquid separator 7; the liquid phase interface end of the vapor-liquid separator 7 is connected with the middle pipeline of the deacidification ammonia distillation tower 1; the gas phase interface end of the gas-liquid separator 7 is connected with an ammonia gas inlet pipeline of the No. 2 waste heat water heat exchanger 8; the ammonia gas outlet of the No. 2 waste heat water heat exchanger 8 is connected with the ammonia condenser 9 pipeline.
The waste water pipeline at the bottom of the deacidification ammonia distillation tower 1 is connected with the pipeline of the reboiler 2; the outlet of the reboiler 2 is connected with a vapor phase space pipeline at the bottom of the deacidification ammonia still 1.
The technological principle and the working process of the utility model specifically comprise the following steps:
1. cooling the coking residual ammonia water by a residual ammonia water cooler 4, and then entering the top of the upper tower section of the deacidification ammonia distillation tower 1 for ammonia distillation operation; the vapor phase discharging part at the top of the deacidification ammonia still 1 is sent to a gas pipeline or an ammonium sulfate saturator before desulfurization.
The temperature of the residual ammonia water entering the top of the upper tower section of the deacidification ammonia distillation tower 1 is 60-66 ℃; the pressure at the top of the deacidification ammonia distillation tower 1 is 20 kPag-50 kPag; the temperature of the ammonia-containing gas discharged from the top of the deacidification ammonia distillation tower 1 is 85-102 ℃.
2. The concentrated ammonia vapor extracted from the middle side line of the deacidification ammonia distillation tower 1 enters a vapor-liquid separator 7 to remove micro liquid drops possibly carried by the liquid, and the liquid phase part after vapor-liquid separation is discharged into the middle of the deacidification ammonia distillation tower 1 through a liquid seal.
The temperature of the concentrated ammonia vapor extracted from the middle lateral line of the deacidification ammonia distillation tower 1 is 102-110 ℃; the mass fraction of ammonia in the concentrated ammonia vapor extracted from the middle side line of the deacidification ammonia distillation tower is 15-25%.
3. The vapor phase part after vapor-liquid separation enters an ammonia condenser 9 for condensation and cooling to become clean concentrated ammonia water.
4. The waste water at the bottom of the deacidification ammonia distillation tower 1 is pumped by a waste water pump 3, enters into circulating hot water (63-73 ℃), enters into a waste water cooler 6 to be cooled to about 40 ℃, and is sent to a phenol-cyanogen waste water treatment device.
The temperature of the wastewater at the bottom of the deacidification ammonia distillation tower 1 is 110-120 ℃; the temperature of the waste water at the bottom of the deacidification ammonia still 1 after heat exchange with the circulating hot water is 70 ℃.
In the aspect of energy consumption saving, compared with the traditional ammonia distillation which needs to consume 170 kg-200 kg of steam/ton of residual ammonia water, the technology disclosed by the utility model only needs to consume 135kg of steam/ton of residual ammonia water, thereby saving the steam consumption by about 32%; compared with the traditional coking ammonia distillation process with about 8-9 t circulating water/ton residual ammonia water consumption, the circulating water consumption is low, and is only 3.3t circulating water/ton residual ammonia water, so that the circulating water consumption is saved by 63%.
In the aspect of waste heat recovery, unlike the existing ammonia distillation technology, the process can recover 5.8t of circulating hot water/ton of residual ammonia water, and the circulating hot water for recovering the ammonia distillation waste heat can be used as a heat source for a summer refrigerator or a winter heating supply of a coking plant or as a heat source of a vacuum potassium carbonate desulfurization regeneration tower, so that the self energy utilization rate of the coking plant is greatly improved, and the running cost of a production enterprise is reduced.
Compared with the conventional normal-pressure ammonia distillation process, the process disclosed by the utility model uses the cooled residual ammonia water as the cold reflux liquid at the top of the tower, and performs direct mass transfer and heat transfer with the rising stripping steam in the tower, so that an ammonia distillation tower top separator is not required to be additionally arranged, the use of titanium materials of the separator is reduced, the residual ammonia water cooler is made of carbon steel, and the process reduces the equipment investment.
In terms of equipment arrangement, unlike the prior ammonia distillation technology in which an ammonia separator is arranged at the top of an ammonia distillation tower, the residual ammonia water cooler in the process can be arranged on the ground, so that the strength requirement of the ammonia distillation tower is further reduced, and the requirement of an operator on the operation of the tower top is reduced.
According to the utility model, after the rest ammonia water is cooled, the rest ammonia water completely enters the top of the deacidification ammonia distillation tower 1, clean ammonia steam is extracted from the side line in the middle of the deacidification ammonia distillation tower 1 and is used for preparing relatively clean concentrated ammonia water, and the waste heat of the ammonia steam extracted from the side line and the waste heat of the waste water at the bottom of the deacidification ammonia distillation tower can be used for preparing hot water at 63-73 ℃ for heat recovery and utilization, so that a heat source can be provided for a summer refrigerator or winter heating of a coking plant, the coking waste heat utilization rate is improved, and the utility model is an ammonia distillation process with less equipment investment, low operation cost and simple process flow.
The foregoing is only a preferred embodiment of the present utility model, but the scope of the present utility model is not limited thereto, and any person skilled in the art, who is within the scope of the present utility model, should make equivalent substitutions or modifications according to the technical scheme of the present utility model and the inventive concept thereof, and should be covered by the scope of the present utility model.
Claims (3)
1. An energy-saving deacidification ammonia distillation device is characterized by comprising a deacidification ammonia distillation tower, a reboiler, a residual ammonia water cooler, a No. 1 waste heat water heat exchanger, a waste water cooler, a vapor-liquid separator, a No. 2 waste heat water heat exchanger and an ammonia condenser; the bottom of the deacidification ammonia distillation tower, the No. 1 waste heat water heat exchanger, the waste water cooler and the phenol-cyanogen waste water treatment device are connected through pipelines in sequence; the residual ammonia water pipeline, the residual ammonia water cooler and the top of the deacidification ammonia distillation tower are connected in turn through pipelines; the top of the deacidification ammonia distillation tower is connected with a gas pipeline before desulfurization or an ammonium sulfate saturator pipeline in an ammonium sulfate process; the middle part of the deacidification ammonia distillation tower, the vapor-liquid separator, the No. 2 waste heat water heat exchanger and the ammonia condenser are connected through pipelines in sequence; the waste water pipeline at the bottom of the deacidification ammonia still is connected with a reboiler pipeline, and the outlet of the reboiler is connected with a vapor phase space pipeline at the bottom of the deacidification ammonia still.
2. The energy-saving deacidification and ammonia distillation device according to claim 1, further comprising a wastewater pump, wherein the bottom of the deacidification and ammonia distillation tower is connected with an inlet pipeline of the wastewater pump; and the outlet of the wastewater pump is connected with a pipeline of the No. 1 waste heat water heat exchanger.
3. The energy-saving deacidification and ammonia distillation device according to claim 1, wherein the liquid phase interface end of the vapor-liquid separator is connected with a middle pipeline of the deacidification and ammonia distillation tower; the gas phase interface end of the gas-liquid separator is connected with an ammonia gas inlet pipeline of the No. 2 waste heat water heat exchanger.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202320082668.XU CN219449378U (en) | 2023-01-28 | 2023-01-28 | Energy-saving deacidification ammonia distillation device |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202320082668.XU CN219449378U (en) | 2023-01-28 | 2023-01-28 | Energy-saving deacidification ammonia distillation device |
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| CN219449378U true CN219449378U (en) | 2023-08-01 |
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| CN202320082668.XU Active CN219449378U (en) | 2023-01-28 | 2023-01-28 | Energy-saving deacidification ammonia distillation device |
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- 2023-01-28 CN CN202320082668.XU patent/CN219449378U/en active Active
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