CN112479227A - Equipment and process for purifying crude ammonia water - Google Patents
Equipment and process for purifying crude ammonia water Download PDFInfo
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- CN112479227A CN112479227A CN202011464652.2A CN202011464652A CN112479227A CN 112479227 A CN112479227 A CN 112479227A CN 202011464652 A CN202011464652 A CN 202011464652A CN 112479227 A CN112479227 A CN 112479227A
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- ammonia
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- deamination
- heat exchanger
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- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 title claims abstract description 96
- 235000011114 ammonium hydroxide Nutrition 0.000 title claims abstract description 96
- 238000000034 method Methods 0.000 title claims abstract description 14
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims abstract description 134
- 238000006481 deamination reaction Methods 0.000 claims abstract description 71
- NBIIXXVUZAFLBC-UHFFFAOYSA-N Phosphoric acid Chemical compound OP(O)(O)=O NBIIXXVUZAFLBC-UHFFFAOYSA-N 0.000 claims abstract description 53
- 238000000746 purification Methods 0.000 claims abstract description 44
- 229910021529 ammonia Inorganic materials 0.000 claims abstract description 40
- 239000005696 Diammonium phosphate Substances 0.000 claims abstract description 39
- MNNHAPBLZZVQHP-UHFFFAOYSA-N diammonium hydrogen phosphate Chemical compound [NH4+].[NH4+].OP([O-])([O-])=O MNNHAPBLZZVQHP-UHFFFAOYSA-N 0.000 claims abstract description 39
- 229910000388 diammonium phosphate Inorganic materials 0.000 claims abstract description 39
- 235000019838 diammonium phosphate Nutrition 0.000 claims abstract description 39
- 229910000147 aluminium phosphate Inorganic materials 0.000 claims abstract description 27
- 239000002994 raw material Substances 0.000 claims abstract description 17
- 238000010521 absorption reaction Methods 0.000 claims abstract description 12
- 239000000376 reactant Substances 0.000 claims abstract description 8
- 239000007795 chemical reaction product Substances 0.000 claims abstract description 7
- 239000007788 liquid Substances 0.000 claims description 86
- 230000009615 deamination Effects 0.000 claims description 50
- 238000010438 heat treatment Methods 0.000 claims description 39
- LFVGISIMTYGQHF-UHFFFAOYSA-N ammonium dihydrogen phosphate Chemical compound [NH4+].OP(O)([O-])=O LFVGISIMTYGQHF-UHFFFAOYSA-N 0.000 claims description 27
- 229910000387 ammonium dihydrogen phosphate Inorganic materials 0.000 claims description 27
- 239000006012 monoammonium phosphate Substances 0.000 claims description 27
- 235000019837 monoammonium phosphate Nutrition 0.000 claims description 27
- 239000008234 soft water Substances 0.000 claims description 16
- 239000012535 impurity Substances 0.000 claims description 15
- 238000010992 reflux Methods 0.000 claims description 14
- JVDHWXLTNDKLIZ-WCCKRBBISA-N (2s)-2-amino-5-(diaminomethylideneamino)pentanoic acid;hydrate Chemical compound O.OC(=O)[C@@H](N)CCCNC(N)=N JVDHWXLTNDKLIZ-WCCKRBBISA-N 0.000 claims description 7
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 4
- 239000000243 solution Substances 0.000 claims description 2
- 238000006243 chemical reaction Methods 0.000 abstract description 12
- 239000000047 product Substances 0.000 abstract description 9
- 239000002699 waste material Substances 0.000 abstract description 6
- 230000007613 environmental effect Effects 0.000 abstract description 5
- 239000002912 waste gas Substances 0.000 abstract description 5
- 239000000126 substance Substances 0.000 abstract description 4
- 238000003795 desorption Methods 0.000 abstract 1
- 239000007789 gas Substances 0.000 description 7
- 239000002351 wastewater Substances 0.000 description 6
- 230000000694 effects Effects 0.000 description 3
- 238000005516 engineering process Methods 0.000 description 3
- 238000005086 pumping Methods 0.000 description 3
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 2
- 239000002253 acid Substances 0.000 description 2
- 230000009286 beneficial effect Effects 0.000 description 2
- 239000003546 flue gas Substances 0.000 description 2
- -1 hydrogen ions Chemical class 0.000 description 2
- 238000004065 wastewater treatment Methods 0.000 description 2
- 230000002378 acidificating effect Effects 0.000 description 1
- 239000012295 chemical reaction liquid Substances 0.000 description 1
- 238000004939 coking Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000004821 distillation Methods 0.000 description 1
- 239000003337 fertilizer Substances 0.000 description 1
- 239000001257 hydrogen Substances 0.000 description 1
- 229910052739 hydrogen Inorganic materials 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 239000005416 organic matter Substances 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- 230000009469 supplementation Effects 0.000 description 1
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Classifications
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01C—AMMONIA; CYANOGEN; COMPOUNDS THEREOF
- C01C1/00—Ammonia; Compounds thereof
- C01C1/02—Preparation, purification or separation of ammonia
- C01C1/022—Preparation of aqueous ammonia solutions, i.e. ammonia water
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- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Analytical Chemistry (AREA)
- Inorganic Chemistry (AREA)
- Removal Of Specific Substances (AREA)
Abstract
The application relates to the technical field of chemical equipment, in particular to coarse ammonia water purification equipment and a process, wherein the coarse ammonia water purification equipment comprises: the ammonia absorption reaction system comprises a reactor, wherein the reactor is injected with crude ammonia water and reactant raw materials so as to generate an ammonia absorption reaction to absorb ammonia in the crude ammonia water; the deamination reaction system is communicated with the ammonia absorption reaction system, and reaction products in the reactor can enter the deamination reaction system; and the rectification system is communicated with the deamination reaction system, and part of reaction products given by the deamination reaction system enters the rectification system. The coarse ammonia water purification equipment that this embodiment provided is through to satisfying phosphoric acid and the reaction condition that the aqueous ammonia reaction generated ammonia and diammonium phosphate to provide ammonia absorption, the environmental condition of desorption reaction, realize the purification of coarse ammonia water and prepare high-purity aqueous ammonia and liquid ammonia, can be used for the waste gas denitration, accomplish to treat waste with useless, the product can regard as the commodity to sell, is showing and has improved economic benefits, and simple structure, and the cost is controllable, has higher practical value.
Description
Technical Field
The application relates to the technical field of chemical equipment, in particular to coarse ammonia water purification equipment and a coarse ammonia water purification process.
Background
Along with the progress of society, the living standard of people is increasingly improved, the quality requirement on the atmospheric environment is also increasingly high, and the denitration of waste gas is a technical means for improving the atmospheric environment and is also the requirement of the current environmental regulation. The existing common denitration technology is ammonia denitration, a large amount of waste gas needing denitration is generated in enterprises of chemical fertilizers, coking, coal-to-liquids, coal-to-gas and coal-to-chemical products, and a large amount of crude ammonia water is generated in the enterprises.
Disclosure of Invention
The application aims to provide a coarse ammonia water purification device and a coarse ammonia water purification process, so as to solve the technical problems of complex structure, single product and low economic benefit of the existing deamination device in the prior art to a certain extent.
The application provides a coarse ammonia purification equipment includes:
the ammonia absorption reaction system comprises a reactor, wherein the reactor is filled with crude ammonia water and reactant raw materials;
the deamination reaction system is communicated with the ammonia absorption reaction system, and reaction products in the reactor can enter the deamination reaction system;
and the rectification system is communicated with the deamination reaction system, and part of reaction products supplied by the deamination reaction system enters the rectification system.
In the above technical solution, further, the reactant raw materials at least include a recycled monoammonium phosphate solution, and phosphoric acid and soft water for adjusting acidity of the reactant raw materials; the monoammonium phosphate solution can react with the coarse ammonia water to generate diammonium phosphate.
In any one of the above technical solutions, further, the ammonia absorption reaction system further includes:
the soft water tank is communicated with the reactor, and a first pump body is arranged between the soft water tank and the reactor;
the phosphoric acid tank is communicated with the reactor, and a second pump body is arranged between the phosphoric acid tank and the reactor;
the crude ammonia water tank is communicated with the reactor, and a third pump body is arranged between the crude ammonia water tank and the reactor;
the liquid inlet of the purifier is communicated with the liquid outlet of the reactor, the first liquid outlet of the purifier is connected with an impurity tank, and the second liquid outlet of the purifier is connected with a liquid storage tank.
In any of the above technical solutions, further, a liquid outlet of the liquid storage tank is connected to a liquid inlet of the first heat exchanger, and a fourth pump body is disposed between the liquid storage tank and the first heat exchanger;
a first liquid outlet of the first heat exchanger is connected with a deacidification device; the second liquid outlet of the first heat exchanger is communicated with the reactor, and a first cooler is arranged between the second liquid outlet of the heat exchanger and the reactor.
In any of the above technical solutions, further, the deamination reaction system includes:
the ammonia removal tower is provided with a first steam interface;
the ammonia gas outlet of the deamination tower is communicated with the first inlet of the second heat exchanger; the deacidification device is communicated with a second inlet of the second heat exchanger, and liquid subjected to deacidification treatment by the deacidification device enters the second heat exchanger to exchange heat with the ammonia and the water vapor and then enters the deamination tower through a first outlet of the second heat exchanger;
and a second outlet of the second heat exchanger is communicated with an air inlet of a second cooler, and a liquid outlet of the second cooler is connected with an arginine water tank.
In any one of the above technical solutions, further, the deamination reaction system further includes a first heating device, a liquid outlet of the deamination tower is communicated with a liquid inlet of the first heating device, a liquid outlet of the first heating device is communicated with the deamination tower, and a fifth pump body is arranged between the deamination tower and the first heating device; the first heating device is used for heating part of raw materials in the deamination tower and conveying the raw materials back to the deamination tower after the heating is finished.
In any of the above technical solutions, further, the rectification system includes:
the rectifying tower is provided with a second steam interface;
a liquid outlet of the rectifying tower is connected with a third heat exchanger, and a liquid outlet of the third heat exchanger is communicated with the rectifying tower;
the arginine water tank is communicated with the third heat exchanger, and a sixth pump body is arranged between the arginine water tank and the third heat exchanger;
a gas outlet of the rectifying tower is connected with a condenser, and a liquid outlet of the condenser is provided with a liquid ammonia tank;
a reflux groove is arranged between the condenser and the liquid ammonia tank;
the reflux tank is communicated with the liquid ammonia tank and the rectifying tower;
and a seventh pump body is arranged at the liquid outlet of the reflux groove.
In any of the above technical solutions, further, the rectification system further includes a second heating device;
a liquid inlet of the second heating device is communicated with a liquid outlet of the rectifying tower, and a liquid outlet of the second heating device is communicated with the rectifying tower;
an eighth pump body is arranged between the rectifying tower and the second heating device.
In any one of the above technical solutions, further, the pressure in the deamination tower is 980-1490 kPa;
the pressure in the rectifying tower is 1290-1650 Kpa.
The application also provides a process for purifying the coarse ammonia water, which comprises the following process flows:
injecting soft water and phosphoric acid into the reactor to adjust the acidity of the phosphoric acid; injecting coarse ammonia water into the reactor, and generating diammonium phosphate in the reactor;
introducing the diammonium phosphate into a purifier for purification, and removing impurities in the diammonium phosphate;
introducing purified diammonium phosphate into a deamination tower for deamination treatment to generate monoammonium phosphate and release ammonia;
introducing the ammonia gas and steam evaporated together with the ammonia gas into a cooler to liquefy the ammonia gas into high-purity ammonia water;
introducing the high-purity ammonia water into a rectifying tower for rectification treatment and releasing high-purity ammonia gas;
and introducing the high-purity ammonia gas into a condenser, and condensing the high-purity ammonia water into liquid ammonia.
Compared with the prior art, the beneficial effect of this application is:
the coarse ammonia water purification equipment that this embodiment provided, through to satisfying the reaction condition that monoammonium phosphate and coarse ammonia water reaction generated diammonium phosphate to provide deamination reaction, distillation reaction's environmental condition, realize the purification of coarse ammonia water and prepare high-purity aqueous ammonia and liquid ammonia, wherein high-purity aqueous ammonia can be used for the waste gas denitration, accomplishes to control waste with the waste, the product can regard as the commodity to sell, is showing and is improving economic benefits, and simple structure, the cost is controllable, has higher practical value.
In the initial start-up period, phosphoric acid may be used to replace monoammonium phosphate and react with the coarse ammonia water until the circulating monoammonium phosphate enters the reactor.
The application provides a coarse ammonia water purification technology, include the aforesaid coarse ammonia water purification equipment, specifically be suitable for above-mentioned coarse ammonia water purification equipment, realize the purification of coarse ammonia water on the one hand, can generate high-purity aqueous ammonia and the multiple product of liquid ammonia simultaneously, wherein, high-purity aqueous ammonia can be used to the flue gas denitration, when accomplishing to treat waste with useless, but subsidiary product reutilization or sell as the commodity, has higher economic benefits and use value, and the simple easily operation of process flow.
Drawings
In order to more clearly illustrate the detailed description of the present application or the technical solutions in the prior art, the drawings needed to be used in the detailed description of the present application or the prior art description will be briefly introduced below, and it is obvious that the drawings in the following description are some embodiments of the present application, and other drawings can be obtained by those skilled in the art without creative efforts.
Fig. 1 is a schematic structural diagram of a coarse ammonia water purification apparatus provided in an embodiment of the present application.
Reference numerals:
1-reactor, 2-soft water tank, 3-phosphoric acid tank, 4-crude ammonia tank, 5-purifier, 6-first pump body, 7-second pump body, 8-third pump body, 9-impurity tank, 10-liquid storage tank, 11-first heat exchanger, 12-fourth pump body, 13-deacidification device, 14-first cooler, 15-deamination tower, 151-first steam interface, 152-ammonia outlet, 16-second heat exchanger, 17-second cooler, 18-refined ammonia tank, 19-first heating device, 20-fifth pump body, 21-rectification tower, 211-second steam interface, 22-third heat exchanger, 23-condenser, 24-reflux tank, 25-liquid ammonia tank, 26-seventh pump body, 27-second heating device, 28-eighth pump, 29-sixth pump, 30-ninth pump.
Detailed Description
The technical solutions of the present application will be described clearly and completely with reference to the accompanying drawings, and it should be understood that the described embodiments are only some embodiments of the present application, but not all embodiments.
The components of the embodiments of the present application, generally described and illustrated in the figures herein, can be arranged and designed in a wide variety of different configurations. Thus, the following detailed description of the embodiments of the present application, presented in the accompanying drawings, is not intended to limit the scope of the claimed application, but is merely representative of selected embodiments of the application.
All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the protection scope of the present application.
In the description of the present application, it should be noted that the terms "center", "upper", "lower", "left", "right", "vertical", "horizontal", "inner", "outer", and the like indicate orientations or positional relationships based on the orientations or positional relationships shown in the drawings, and are only for convenience of description and 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 thus, should not be construed as limiting the present application. Furthermore, the terms "first," "second," and "third" are used for descriptive purposes only and are not to be construed as indicating or implying relative importance.
In the description of the present application, it is to be noted that, unless otherwise explicitly specified or limited, the terms "mounted," "connected," and "connected" are to be construed broadly, e.g., as meaning either a fixed connection, a removable connection, or an integral connection; 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 application can be understood in a specific case by those of ordinary skill in the art.
The purification apparatus of crude aqueous ammonia and the purification process of crude aqueous ammonia according to some embodiments of the present application are described below with reference to fig. 1.
Referring to fig. 1, an embodiment of the present application provides a crude ammonia water purification apparatus, including: the ammonia absorption reaction system, the deamination reaction system and the rectification system are connected in sequence, wherein the ammonia absorption reaction system specifically comprises a reactor 1, a soft water tank 2, a phosphoric acid tank 3, a coarse ammonia water tank 4 and a purifier 5, reaction raw materials can be introduced into the reactor 1, and the reaction raw materials specifically comprise monoammonium phosphate reacted with coarse ammonia water (the coarse ammonia water in the application can be specifically a solution with lower ammonia content and a certain amount of impurities), phosphoric acid and soft water for adjusting the acidity of reaction liquid (monoammonium phosphate and coarse ammonia water); monoammonium phosphate can react with coarse ammonia water to generate diammonium phosphate, and it should be noted that the source of monoammonium phosphate is mainly generated and recycled with the following deamination tower 15 and supplied to the reactor 1, and at the initial stage of start-up, the amount of phosphoric acid can be properly adjusted to replace monoammonium phosphate, and when sufficient monoammonium phosphate enters the reactor 1, the amount of phosphoric acid can be reduced; the soft water tank 2 is communicated with the reactor 1 through a pipeline, a first pump body 6 is arranged on the pipeline between the soft water tank 2 and the reactor 1 and used for pumping the soft water into the reactor 1, the phosphoric acid tank 3 is also communicated with the reactor 1 through another pipeline, a second pump body 7 is arranged on the pipeline between the phosphoric acid tank 3 and the reactor 1 and used for pumping the phosphoric acid into the reactor 1, and the acidity of the phosphoric acid entering the reactor 1 can be adjusted by controlling the proportion of the soft water and the phosphoric acid; the coarse ammonia water is communicated with the reactor 1 through a pipeline, a third pump body 8 is arranged on the pipeline between the coarse ammonia water and the reactor 1, the coarse ammonia water is pumped into the reactor 1 through the third pump body 8, the coarse ammonia water and monoammonium phosphate react in the reactor 1, hydrogen ions in the monoammonium phosphate are gradually replaced by ammonia ions, a reaction product can be controlled to be diammonium phosphate solution through a method for controlling acidity, a liquid outlet is arranged at a position close to the middle upper part of the reactor 1, the diammonium phosphate solution in the reactor 1 enters the purifier 5 through an overflow mode, the diammonium phosphate solution has high density, the solubility of acid gas is lower than that of the ammonia water, the diammonium phosphate solution is easy to separate from organic matters and other impurities, the separated organic matters and other impurities can be blown to the liquid level in the purifier 5 through ventilating the purifier 5, and the purifier 5 is provided with an overflow port (namely a first liquid outlet), organic matter and other impurity flow out and flow into to impurity groove 9 in from the overflow mouth through the mode of overflow, retrieve, handle impurity, and clarifier 5 still is provided with the second liquid outlet, and preferably, the second liquid outlet is located the bottom of clarifier 5, and diammonium phosphate solution through purification treatment flows into reservoir 10 through the second liquid outlet.
In the embodiment of the present application, a liquid outlet of the liquid storage tank 10 is connected to a first heat exchanger 11, a liquid outlet of the liquid storage tank 10 is communicated with a liquid inlet of the first heat exchanger 11 through a pipeline, and a fourth pump body 12 is arranged on the pipeline between the liquid storage tank 10 and the first heat exchanger 11, and is used for pumping a diammonium phosphate solution in the liquid storage tank 10 into the first heat exchanger 11; the first heat exchanger 11 is further provided with a first liquid outlet and a second liquid outlet, wherein the first liquid outlet of the first heat exchanger 11 is connected with a deacidification device 13, a diammonium phosphate solution entering the first heat exchanger 11 enters the deacidification device 13 through heat exchange for deacidification treatment, the liquid outlet of the deacidification device 13 is communicated with a deamination tower 15, the diammonium phosphate deacidified by the deacidification device 13 can enter the deamination tower 15, for example, diammonium phosphate deacidified by the deacidification device 13 can enter the deamination tower 15 through a ninth pump body 30 and a second heat exchanger 16; the second liquid outlet of the first heat exchanger 11 is communicated with the reactor 1, and a first cooler 14 is arranged between the second liquid outlet of the first heat exchanger 11 and the reactor 1.
Further, in this embodiment, the deamination reaction system includes: the deammoniation tower comprises a deammoniation tower 15, a second heat exchanger 16, a first heating device 19 and a second cooler 17, wherein an outlet end of the second cooler 17 is connected with an ammonia water tank 18, specifically, the deammoniation tower 15 is provided with a first steam interface 151 for introducing steam into the deammoniation tower 15 to adjust the temperature in the deammoniation tower 15, diammonium phosphate entering the deammoniation tower 15 is unstable under a higher temperature condition (a specific temperature range value is shown below), ammonia gas is separated from diammonium phosphate to generate monoammonium phosphate, a liquid outlet is formed in the bottom of the deammoniation tower 15, the liquid outlet of the deammoniation tower 15 is communicated with the first heat exchanger 11, monoammonium phosphate in the deammoniation tower 15 enters the first heat exchanger 11 through the liquid outlet in the bottom to exchange heat with diammonium phosphate entering the first heat exchanger 11, monoammonium phosphate flowing out from a second liquid outlet of the first heat exchanger 11 firstly enters the first cooler 14 to be cooled, and the liquid outlet of the, when monoammonium phosphate is injected into the reactor 1, the original operation of continuously injecting phosphoric acid into the reactor 1 is changed into intermittent phosphoric acid supplementation, so that the over-strong acidity in the reactor 1 is avoided; the top of the deamination tower 15 is provided with an ammonia outlet 152, ammonia generated in the deamination tower 15 and steam injected through a first steam interface 151 escape through the ammonia outlet 152 at the top of the deamination tower 15 and enter the second heat exchanger 16 through a pipeline together, diammonium phosphate flowing out of the deacidification device 13 firstly enters the second heat exchanger 16 to exchange heat with ammonia and water steam and then enters the deamination tower 15, so that the ammonia flows out of the second heat exchanger 16 after being primarily cooled, and then the ammonia and the water steam enter a cooler through a pipeline to be further cooled and liquefied to be changed into liquid high-purity ammonia water from a gas state to enter and be stored in the refined ammonia water tank 18.
In this embodiment of the application, the deamination reaction system further includes a first heating device 19, a liquid outlet of the deamination tower 15 is communicated with a liquid inlet of the first heating device 19, a liquid outlet of the first heating device 19 is communicated with the deamination tower 15, and a fifth pump body 20 is arranged between the deamination tower 15 and the first heating device 19; the first heating device 19 is used for heating part of raw materials in the deamination tower 15 and conveying the heated raw materials back to the deamination tower 15.
Specifically, a part of monoammonium phosphate flowing out of a liquid outlet of the deamination tower 15 flows to the first heat exchanger 11 to exchange heat with diammonium phosphate, and the other part of monoammonium phosphate is pumped into the first heating device 19 by the fifth pump body 20 to be heated and flows back to the deamination tower 15, so that heat is provided for the deamination tower 15. The first heating device 19 may be, but is not limited to, a heating furnace as is common in the art.
In one embodiment of the present application, a rectification system includes: a rectifying tower 21, a third heat exchanger 22, a condenser 23, a reflux tank 24 and a liquid nitrogen tank; the rectifying tower 21 is provided with a second steam interface 211, which is used for injecting high-temperature steam into the rectifying tower 21 to provide heat for the rectifying tower 21, and the mode is a mode for providing heat for the rectifying tower 21; under certain temperature and pressure conditions in the rectifying tower 21 (specific conditions of temperature and pressure in the rectifying tower 21 are described below), ammonia gas is released from high-purity ammonia water entering the rectifying tower 21 and a residual liquid (hereinafter referred to as waste water) is left, the waste water enters the third heat exchanger 22 through a liquid outlet arranged at the bottom of the rectifying tower 21 and exchanges heat with the high-purity ammonia water entering the third heat exchanger 22, the high-purity ammonia water is heated to a certain degree to enter the temperature of the high-purity ammonia water in the rectifying tower 21, the high-purity ammonia gas with high purity in the rectifying tower 21 escapes from a gas outlet at the top of the rectifying tower 21 and flows into the condenser 23 to be condensed and liquefied to form liquid ammonia, the liquid ammonia enters the reflux tank 24, part of the liquid ammonia is sent to the top of the rectifying tower as reflux of the rectifying tower 21 under the action of the seventh pump body 26, and the other part of the liquid ammonia is stored in the liquid ammonia.
In the present embodiment, the rectification system further includes a second heating device 27; a liquid inlet of the second heating device 27 is communicated with a liquid outlet of the rectifying tower 21, and a liquid outlet of the second heating device 27 is communicated with the rectifying tower 21; an eighth pump body 28 is provided between the rectifying tower 21 and the second heating device 27.
Specifically, a part of the wastewater flowing out of the rectifying tower 21 enters the third heat exchanger 22 to exchange heat with the high-purity ammonia water and flow to the wastewater treatment system, and another part of the wastewater enters the second heating device 27 to be heated under the action of the eighth pump body 28 and flows back to the rectifying tower 21 to provide heat for the rectifying tower 21, which is another way to provide heat for the rectifying tower 21.
It should be noted that, in order to meet the reaction conditions of the deamination and rectification processes, both the deamination tower 15 and the rectification tower 21 have higher pressure environmental conditions, wherein the pressure in the deamination tower 15 is specifically 980-1490 kPa at the top of the deamination tower 15; the pressure in the rectifying tower 21 is specifically 1290-1650 Kpa at the top of the rectifying tower 21.
The coarse ammonia water purification equipment that this embodiment provided is through satisfying the reaction condition that monoammonium phosphate and coarse ammonia water reaction generated diammonium phosphate to provide the environmental condition of deamination and rectification, realize the purification of coarse ammonia water and prepare high-purity aqueous ammonia and liquid ammonia, wherein high-purity aqueous ammonia can be used for the waste gas denitration, accomplishes to control useless with the useless, the product can regard as the commodity to sell, is showing and has improved economic benefits, and simple structure, and the cost is controllable, has higher practical value.
The embodiment of this application still provides a coarse ammonia purification technology, uses above-mentioned embodiment the coarse ammonia purification equipment, therefore, has this coarse ammonia purification equipment's whole beneficial technological effect, here, no longer gives details.
The purification process of the crude ammonia water provided by the embodiment specifically comprises the following process flows:
(1) injecting soft water and phosphoric acid into the reactor 1 to adjust the acidity of the phosphoric acid, injecting coarse ammonia water into the reactor 1, and generating diammonium phosphate in the reactor 1; by controlling the acidity and ensuring that the concentration of the coarse ammonia water entering the reactor 1 is 5-23% and the temperature is 0-60 ℃, the reaction of phosphoric acid and the coarse ammonia water to generate diammonium phosphate can be realized at the temperature by controlling the acidity of the solution obtained by mixing 1 reactant in the reactor.
(2) Introducing diammonium phosphate into a purifier 5 for purification, and removing impurities in the diammonium phosphate; the purifier 5 filters the diammonium phosphate to remove organic matters and other impurities therein, and performs centralized treatment on the impurities, in addition, the purified diammonium phosphate needs to exchange heat with monoammonium phosphate through the first heat exchanger 11, and then the diammonium phosphate after heat exchange is introduced into the deacidification device 13 for deacidification treatment, the temperature of the diammonium phosphate after heat exchange treatment, namely the diammonium phosphate solution entering the deacidification device 13, is less than or equal to 132 ℃, and the generated acidic gas needs to be collected and treated.
(3) Introducing the purified diammonium phosphate subjected to deacidification treatment into a deamination tower 15 for deamination treatment to generate monoammonium phosphate and release ammonia; in the process, the temperature of the top of the deamination tower 15 is 170-205 ℃, the pressure of the top of the deamination tower is 980-1490 kPa (liquid raw materials exist at the bottom of the deamination tower, and no excessive limitation is made), in addition, the temperature of the diammonium phosphate solution flowing into the deamination tower 15 is 160-195 ℃, and the temperature of the monoammonium phosphate solution flowing out of the deamination tower 15 is 181-216 ℃.
(4) The ammonia and the vapor escaping from the deamination tower 15 are introduced into a cooler to condense the ammonia into high-purity ammonia water, and the high-purity ammonia water is stored in an arginine water tank 18.
(5) Introducing the high-purity ammonia water in the refined ammonia water tank 18 into a rectifying tower 21 for rectification treatment and releasing high-purity ammonia gas; in order to ensure the rectification effect, the pressure at the top of the rectification tower 21 is within the range of 1290-1605 Kpa, the temperature at the top of the rectification tower 21 is within the range of 36.8-42.6 ℃, the temperature at the bottom of the rectification tower is within the range of 182-217 ℃, and the content of acid gas of each raw material entering the rectification tower 21 is less than or equal to 0.15 percent through the treatment of the deacidification device 13, so as to ensure the concentration of liquid ammonia generated subsequently.
(6) Introducing high-purity ammonia gas into a condenser 23 to liquefy the high-purity ammonia water into liquid ammonia; the generated liquid ammonia flows into a reflux tank 24, a part of the liquid ammonia in the reflux tank 24 enters a rectifying tower 21 and is sent to the top of the tower as reflux of the rectifying tower 21, the other part of the liquid ammonia in the reflux tank 24 enters a liquid ammonia tank 25 for storage, the concentration of the liquid ammonia is not less than 99.8 percent, and the impurity content is not more than 0.2 percent; waste water is generated in the rectification process and is discharged to a waste water treatment system, and the ammonia content of the waste water is less than or equal to 1000ppm, namely, the coarse ammonia water purification equipment and the process have higher purification effect.
Therefore, the purification process of the coarse ammonia water is particularly suitable for the purification equipment of the coarse ammonia water, on one hand, the purification of the coarse ammonia water is realized, and various products of high-purity ammonia water and liquid ammonia can be generated, wherein the high-purity ammonia water can be used for flue gas denitration, so that the waste is treated by waste, meanwhile, the products can be fully utilized or sold as commodities, the economic benefit and the use value are high, and the process flow is simple and easy to operate.
Finally, it should be noted that: the above embodiments are only used for illustrating the technical solutions of the present application, and not for limiting the same; although the present application has been described in detail with reference to the foregoing embodiments, it should be understood by those of ordinary skill in the art that: the technical solutions described in the foregoing embodiments may still be modified, or some or all of the technical features may be equivalently replaced; and the modifications or the substitutions do not make the essence of the corresponding technical solutions depart from the scope of the technical solutions of the embodiments of the present application.
Claims (10)
1. A crude ammonia water purification apparatus, comprising:
the ammonia absorption reaction system comprises a reactor, wherein the reactor is filled with crude ammonia water and reactant raw materials;
the deamination reaction system is communicated with the ammonia absorption reaction system, and reaction products in the reactor can enter the deamination reaction system;
and the rectification system is communicated with the deamination reaction system, and part of reaction products supplied by the deamination reaction system enters the rectification system.
2. The purification apparatus of crude aqueous ammonia according to claim 1, wherein the reactant raw materials comprise at least a recycled monoammonium phosphate solution and phosphoric acid and soft water for adjusting the acidity of the reactant raw materials; the monoammonium phosphate solution can react with the coarse ammonia water to generate diammonium phosphate.
3. The purification apparatus of crude aqueous ammonia according to claim 1, wherein the ammonia absorption reaction system further comprises:
the soft water tank is communicated with the reactor, and a first pump body is arranged between the soft water tank and the reactor;
the phosphoric acid tank is communicated with the reactor, and a second pump body is arranged between the phosphoric acid tank and the reactor;
the crude ammonia water tank is communicated with the reactor, and a third pump body is arranged between the crude ammonia water tank and the reactor;
the liquid inlet of the purifier is communicated with the liquid outlet of the reactor, the first liquid outlet of the purifier is connected with an impurity tank, and the second liquid outlet of the purifier is connected with a liquid storage tank.
4. The purification equipment of the coarse ammonia water as claimed in claim 3, wherein a liquid outlet of the liquid storage tank is connected with a liquid inlet of a first heat exchanger, and a fourth pump body is arranged between the liquid storage tank and the first heat exchanger;
a first liquid outlet of the first heat exchanger is connected with a deacidification device; the second liquid outlet of the first heat exchanger is communicated with the reactor, and a first cooler is arranged between the second liquid outlet of the heat exchanger and the reactor.
5. The purification apparatus of crude aqueous ammonia according to claim 4, wherein said deamination reaction system comprises:
the ammonia removal tower is provided with a first steam interface;
the ammonia gas outlet of the deamination tower is communicated with the first inlet of the second heat exchanger; the deacidification device is communicated with a second inlet of the second heat exchanger, and liquid subjected to deacidification treatment by the deacidification device enters the second heat exchanger to exchange heat with the ammonia and the water vapor and then enters the deamination tower through a first outlet of the second heat exchanger;
and a second outlet of the second heat exchanger is communicated with an air inlet of a second cooler, and a liquid outlet of the second cooler is connected with an arginine water tank.
6. The coarse ammonia water purification equipment according to claim 5, wherein the deamination reaction system further comprises a first heating device, a liquid outlet of the deamination tower is communicated with a liquid inlet of the first heating device, a liquid outlet of the first heating device is communicated with the deamination tower, and a fifth pump body is arranged between the deamination tower and the first heating device; the first heating device is used for heating part of raw materials in the deamination tower and conveying the raw materials back to the deamination tower after the heating is finished.
7. The purification apparatus of crude aqueous ammonia according to claim 5, wherein said rectification system comprises:
the rectifying tower is provided with a second steam interface;
a liquid outlet of the rectifying tower is connected with a third heat exchanger, and a liquid outlet of the third heat exchanger is communicated with the rectifying tower;
the arginine water tank is communicated with the third heat exchanger, and a sixth pump body is arranged between the arginine water tank and the third heat exchanger;
a gas outlet of the rectifying tower is connected with a condenser, and a liquid outlet of the condenser is provided with a liquid ammonia tank;
a reflux groove is arranged between the condenser and the liquid ammonia tank;
the reflux tank is communicated with the liquid ammonia tank and the rectifying tower;
and a seventh pump body is arranged at the liquid outlet of the reflux groove.
8. The purification plant of crude aqueous ammonia according to claim 7, wherein said rectification system further comprises a second heating device;
a liquid inlet of the second heating device is communicated with a liquid outlet of the rectifying tower, and a liquid outlet of the second heating device is communicated with the rectifying tower;
an eighth pump body is arranged between the rectifying tower and the second heating device.
9. The purification equipment of the coarse ammonia water as claimed in claim 7, wherein the pressure in the deamination tower is 980-1490 kPa;
the pressure in the rectifying tower is 1290-1650 Kpa.
10. The purification process of the crude ammonia water is characterized by comprising the following process flows of:
injecting soft water and phosphoric acid into the reactor to adjust the acidity of the phosphoric acid; injecting coarse ammonia water into the reactor, and generating diammonium phosphate in the reactor;
introducing the diammonium phosphate into a purifier for purification, and removing impurities in the diammonium phosphate;
introducing purified diammonium phosphate into a deamination tower for deamination treatment to generate monoammonium phosphate and release ammonia;
introducing the ammonia gas and steam evaporated together with the ammonia gas into a cooler to liquefy the ammonia gas into high-purity ammonia water;
introducing the high-purity ammonia water into a rectifying tower for rectification treatment and releasing high-purity ammonia gas;
and introducing the high-purity ammonia gas into a condenser, and condensing the high-purity ammonia water into liquid ammonia.
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| CN113044854A (en) * | 2021-03-23 | 2021-06-29 | 江西江氨科技有限公司 | High-purity ammonia preparation method and system |
| CN114262109A (en) * | 2021-11-03 | 2022-04-01 | 青川县青云上锰业有限公司 | Ammonia recovery method of low-concentration ammonium sulfate solution |
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