CN110723771A - Novel phenol ammonia recovery device for efficiently recovering ammonia - Google Patents
Novel phenol ammonia recovery device for efficiently recovering ammonia Download PDFInfo
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- CN110723771A CN110723771A CN201911083670.3A CN201911083670A CN110723771A CN 110723771 A CN110723771 A CN 110723771A CN 201911083670 A CN201911083670 A CN 201911083670A CN 110723771 A CN110723771 A CN 110723771A
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- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 title claims abstract description 340
- 229910021529 ammonia Inorganic materials 0.000 title claims abstract description 124
- 238000011084 recovery Methods 0.000 title claims abstract description 23
- XABJJJZIQNZSIM-UHFFFAOYSA-N azane;phenol Chemical compound [NH4+].[O-]C1=CC=CC=C1 XABJJJZIQNZSIM-UHFFFAOYSA-N 0.000 title claims abstract description 19
- 238000000746 purification Methods 0.000 claims abstract description 67
- 230000009615 deamination Effects 0.000 claims abstract description 41
- 238000006481 deamination reaction Methods 0.000 claims abstract description 41
- 238000010521 absorption reaction Methods 0.000 claims abstract description 29
- 238000009833 condensation Methods 0.000 claims abstract description 25
- 230000005494 condensation Effects 0.000 claims abstract description 25
- 239000000463 material Substances 0.000 claims abstract description 19
- 239000012535 impurity Substances 0.000 claims abstract description 5
- 238000005204 segregation Methods 0.000 claims abstract 7
- 239000007789 gas Substances 0.000 claims description 107
- 239000012071 phase Substances 0.000 claims description 83
- 239000007788 liquid Substances 0.000 claims description 51
- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 claims description 35
- 235000011114 ammonium hydroxide Nutrition 0.000 claims description 34
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 23
- 238000000926 separation method Methods 0.000 claims description 16
- 230000001105 regulatory effect Effects 0.000 claims description 14
- 239000007791 liquid phase Substances 0.000 claims description 12
- 238000010438 heat treatment Methods 0.000 claims description 10
- 239000007792 gaseous phase Substances 0.000 claims description 6
- 230000001276 controlling effect Effects 0.000 claims description 5
- 238000012423 maintenance Methods 0.000 claims description 4
- 238000006073 displacement reaction Methods 0.000 claims description 3
- 238000012856 packing Methods 0.000 claims description 3
- 230000008878 coupling Effects 0.000 claims 4
- 238000010168 coupling process Methods 0.000 claims 4
- 238000005859 coupling reaction Methods 0.000 claims 4
- 239000003921 oil Substances 0.000 abstract description 20
- 150000002989 phenols Chemical class 0.000 abstract description 15
- 230000009471 action Effects 0.000 abstract description 2
- 238000010992 reflux Methods 0.000 description 14
- ISWSIDIOOBJBQZ-UHFFFAOYSA-N phenol group Chemical group C1(=CC=CC=C1)O ISWSIDIOOBJBQZ-UHFFFAOYSA-N 0.000 description 12
- 239000000126 substance Substances 0.000 description 11
- 239000002351 wastewater Substances 0.000 description 9
- 238000001816 cooling Methods 0.000 description 5
- 239000013072 incoming material Substances 0.000 description 3
- 238000004064 recycling Methods 0.000 description 3
- 239000003245 coal Substances 0.000 description 2
- 238000013461 design Methods 0.000 description 2
- 238000006477 desulfuration reaction Methods 0.000 description 2
- 230000023556 desulfurization Effects 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 238000002309 gasification Methods 0.000 description 2
- 238000000034 method Methods 0.000 description 2
- 239000002253 acid Substances 0.000 description 1
- 230000002378 acidificating effect Effects 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000007872 degassing Methods 0.000 description 1
- 239000000428 dust Substances 0.000 description 1
- 238000001704 evaporation Methods 0.000 description 1
- 230000005484 gravity Effects 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 238000005457 optimization Methods 0.000 description 1
- KSSNXJHPEFVKHY-UHFFFAOYSA-N phenol;hydrate Chemical compound O.OC1=CC=CC=C1 KSSNXJHPEFVKHY-UHFFFAOYSA-N 0.000 description 1
- 230000008569 process Effects 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 238000005070 sampling Methods 0.000 description 1
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- 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
- C01—INORGANIC CHEMISTRY
- C01C—AMMONIA; CYANOGEN; COMPOUNDS THEREOF
- C01C1/00—Ammonia; Compounds thereof
- C01C1/02—Preparation, purification or separation of ammonia
- C01C1/024—Purification
-
- 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
- C02F1/048—Purification of waste water by evaporation
-
- 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
- C02F2101/00—Nature of the contaminant
- C02F2101/30—Organic compounds
- C02F2101/34—Organic compounds containing oxygen
- C02F2101/345—Phenols
-
- 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
- C02F2103/34—Nature of the water, waste water, sewage or sludge to be treated from industrial activities not provided for in groups C02F2103/12 - C02F2103/32
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- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Life Sciences & Earth Sciences (AREA)
- Hydrology & Water Resources (AREA)
- Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Water Supply & Treatment (AREA)
- Analytical Chemistry (AREA)
- Inorganic Chemistry (AREA)
- Degasification And Air Bubble Elimination (AREA)
Abstract
The invention relates to the technical field of ammonia recovery devices, in particular to a novel phenol ammonia recovery device for efficiently recovering ammonia, which comprises a deamination tower, a multistage segregation system, an ammonia purification tower, a pressure regulation group valve and an ammonia absorption cooler, wherein the gas phase outlet end at the top of the deamination tower is connected with the gas phase input end pipe of the multistage segregation system, the gas phase output end of the multistage segregation system is connected with the material inlet end pipe at the lower side of the ammonia purification tower, and the pressure regulation group valve is arranged at the top of the ammonia purification tower. The multi-stage fractional condensation system has a reasonable and compact structure, most of the impurities such as phenols, oils and the like in the mixed gas can be separated from the mixed gas in a condensate mode through the multi-stage fractional condensation system, purified ammonia with high purity can be obtained at a gas phase outlet end of the multi-stage fractional condensation system, and high-purity ammonia can be formed under the combined action of the heat-source-free ammonia purification tower, the ammonia absorption cooler, the multi-stage fractional condensation system and the intercooling circulation device.
Description
Technical Field
The invention relates to the technical field of ammonia gas recovery devices, in particular to a novel phenol ammonia recovery device for efficiently recovering ammonia.
Background
The method comprises the steps of firstly, cooling, decompressing and flash evaporating degassing by a gas water separation device, then removing dust and oil by using the gravity settling principle, carrying out gas-water separation treatment, sending coal gasification wastewater rich in acid gas, ammonia gas and phenolic substances to a phenol-ammonia recovery device for deacidification and deamination, sending the wastewater subjected to deacidification and deamination to a rear system for dephenolization, and sending the dephenolized dilute phenol water to a downstream device for further treatment to realize the purposes of wastewater recycling and zero discharge. The existing phenol ammonia recovery device is unreasonable in design, so that the quality of the produced recovered ammonia water is poor, the ammonia concentration is low, and total phenol, oil and H in the ammonia water are low2The content of S and the like exceeds the standard, the requirement of desulfurization and denitration on the quality of ammonia water cannot be met, secondary treatment is needed, and the cost of ammonia recycling is high.
Disclosure of Invention
The invention provides a novel phenol ammonia recovery device for efficiently recovering ammonia, and overcomes the prior artThe defects of the technology can effectively solve the problems that the quality of the produced recovered ammonia water is poor, the ammonia concentration is low and the total phenol, oil and H in the ammonia water are low due to the unreasonable design of the existing phenol ammonia recovery device2The content of S and the like exceeds the standard, the requirement of desulfurization and denitration on the quality of ammonia water cannot be met, secondary treatment is needed, and the ammonia recycling cost is high.
The purpose of the application is realized as follows: the novel phenol ammonia recovery device for efficiently recovering ammonia comprises a deamination tower, a multi-stage fractional condensation system, an ammonia gas purification tower, a pressure regulating group valve and an ammonia gas absorption cooler, wherein the deamination tower is a rectifying tower provided with a steam heating pipeline and a feeding pipeline, the gas phase outlet end at the top of the deamination tower is connected with the gas phase input end of the multi-stage fractional condensation system so as to reduce the temperature of gas phase materials at the top of the tower and condense and separate impurity materials, the gas phase output end of the multi-stage fractional condensation system is connected with the material inlet end at the lower side of the ammonia gas purification tower, the liquid phase output end of the multi-stage fractional condensation system is connected with an ammonia condensation liquid tank through a pipe, the ammonia condensation liquid tank is provided with a first reflux pipeline and a discharge pipeline, the upper part of the deamination tower is communicated with the ammonia condensation liquid tank through the first reflux pipeline, a first circulating pump is installed on the first reflux pipeline, the ammonia gas purification tower is a, one end of the tower top gas phase pipeline is communicated with the tower top gas phase outlet end of the ammonia gas purification tower, the other end of the tower top gas phase pipeline is communicated with the inlet end of the ammonia gas absorption cooler, the pressure adjusting valve is arranged on the tower top gas phase pipeline, the inlet end of the ammonia gas absorption cooler is also provided with an absorption water pipeline, the absorption water pipeline is provided with a water quantity control valve, the outlet end of the ammonia gas absorption cooler is connected with an ammonia tank, the ammonia tank is provided with a product output pipeline, and a second return pipeline communicated with the upper part of the ammonia gas purification tower is provided with a second circulating pump, the ammonia gas purification tower is also provided with an inter-cooling circulating device capable of circulating the tower bottom liquid of the ammonia gas purification tower to the tower top, a tower bottom liquid outlet end of the ammonia gas purification tower is communicated with an ammonia condensate tank pipe through a third return pipeline, and the third return pipeline is provided with a third circulating pump.
The following is further optimization or/and improvement of the technical scheme of the invention: further, the multistage fractional condensation system comprises a primary ammonia condenser, a secondary ammonia condenser, a tertiary ammonia condenser and an ammonia condensate cooler, wherein the gas phase inlet end of the primary ammonia condenser is connected with the gas phase outlet end of the tower top of the deamination tower through a pipe, the gas phase outlet end of the primary ammonia condenser is communicated with a first fractional liquid tank, the gas phase outlet end of the first fractional liquid tank is connected with the gas phase inlet end of the secondary ammonia condenser through a pipe, the liquid phase outlet end of the primary liquid separating tank is connected with the inlet end of the ammonia condensate cooler through a pipe, the gas phase outlet end of the secondary ammonia condenser is communicated with a second fractional liquid tank, the gas phase outlet end of the second fractional liquid tank is communicated with the gas phase inlet end of the tertiary ammonia condenser through a pipe, the liquid phase outlet end of the second fractional liquid tank is also connected with the inlet end of the ammonia condensate cooler through a pipe, the outlet end of the ammonia condensate cooler is connected with the ammonia condensate tank through, the gas phase outlet end of the three-stage liquid separation tank is connected with a material inlet end pipe at the bottom of the ammonia gas purification tower, and the liquid phase outlet end of the three-stage liquid separation tank is also connected with an ammonia condensate tank pipe.
Further, the intercooling circulation device comprises a large-displacement intercooling circulation pump and an intercooling circulation cooler, a plurality of packing layers are arranged in the ammonia gas purification tower, a fourth backflow pipeline which is used for communicating the tower bottom with the tower top is arranged on the ammonia gas purification tower, and the intercooling circulation pump and the intercooling circulation cooler are arranged on the fourth backflow pipeline.
Further, pressure adjustment group valve includes the pneumatic valve, the preceding hand valve, the back hand valve, the pneumatic valve, the preceding hand valve, the back hand valve is all installed on the top of the tower gaseous phase pipeline, the pneumatic valve sets up between preceding hand valve and back hand valve, still be provided with the bypass pipeline that bypasses the pneumatic valve on the top of the tower gaseous phase pipeline, the preceding hand valve, the back hand valve, the one end of bypass pipeline is linked together with the top of the tower gaseous phase pipeline in preceding hand valve the place ahead, the other end of bypass pipeline is linked together with the top of the tower gaseous phase pipeline behind the back hand valve, install on the bypass pipeline and overhaul the hand valve.
Furthermore, a safety pipeline communicated with the gas phase pipeline at the top of the tower is further arranged at the gas phase outlet end of the three-stage liquid separation tank, the safety pipeline is arranged in front of the pressure regulating group valve, a first safety hand valve for controlling the safety pipeline to be switched on and off is arranged on the safety pipeline, and a second safety hand valve is arranged on a pipeline connected with the material inlet end on the lower side of the ammonia gas purification tower.
The invention has reasonable and compact structure, after the wastewater to be treated enters the deamination tower, mixed gas consisting of ammonia gas, phenols, oils and the like is formed at the gas phase outlet end at the top of the deamination tower, the mixed gas extracted from the top of the deamination tower can be cooled, depressurized and condensed by the multi-stage fractional condensation system, most of the phenols, oils and other impurities in the mixed gas are separated from the mixed gas in a condensate mode and stored in the ammonia condensate tank, further purified ammonia with higher purity can be obtained at the gas phase outlet end of the multi-stage fractional condensation system, and the purified ammonia entering the ammonia purification tower can be further purified under the combined action of a non-heat-source ammonia purification tower, an ammonia absorption cooler, the multi-stage fractional condensation system and an intercooling circulation device under the low-temperature and high-pressure environment to form high-purity ammonia, continuously extracted high-purity ammonia gas forms high-concentration recovered ammonia water at an ammonia gas absorption cooler, and the high-concentration recovered ammonia water flows into an ammonia water tank for storage and utilization by downstream devices; the low temperature cauldron liquid at the bottom of the ammonia gas purification tower enters into the ammonia condensate tank through the third circulating pump, originally collect phenol in the ammonia condensate tank, the condensate of oils returns to the deamination tower as the reflux liquid of deamination tower together, can be under the condition of guaranteeing the normal work of deamination tower, reduce the top of the tower temperature of deamination tower, thereby can effectively reduce waste water in the deamination stage, because high temperature and lead to in a large amount of formation of phenol material and entering into follow-up device, finally lead to in the recovery aqueous ammonia that total phenol exceeds standard, influence the problem of aqueous ammonia quality.
Drawings
The specific structure of the application is given by the following figures and examples:
FIG. 1 is a schematic view of the connection structure of a novel phenol ammonia recovery device for efficiently recovering ammonia.
Legend: 1. deamination tower, 2, ammonia gas purification tower, 3, ammonia gas absorption cooler, 4, incoming material pipeline, 5, ammonia condensate tank, 6, first return pipeline, 7, discharge pipeline, 8, first circulating pump, 9, tower top gas phase pipeline, 10, absorption water pipeline, 11, water amount control valve, 12, ammonia water tank, 13, product output pipeline, 14, second return pipeline, 15, second circulating pump, 16, third return pipeline, 17, third circulating pump, 18, primary ammonia condenser, 19, secondary ammonia condenser, 20, tertiary ammonia condenser, 21, primary separating tank, 22, secondary separating tank, 23, tertiary separating tank, 24, ammonia condensate cooler, 25, intercooling circulating pump, 26, intercooling circulation cooler, 27, pneumatic valve, 28, forehand valve, 29, rear hand valve, 30, bypass pipeline, 31, hand maintenance valve, 32, safety pipeline, 33, water condensate tank, 6, first return pipeline, 7, discharge pipeline, 8, first circulating pump, 9, tower top gas phase pipeline, 10, absorption water pipeline, 11, water amount control valve, 12, ammonia tank, ammonia, A first safety hand valve, 34 and a second safety hand valve.
Detailed Description
The present application is not limited to the following examples, and specific implementations may be determined according to the technical solutions and practical situations of the present application.
In the present invention, for convenience of description, the description of the relative positional relationship of the components is described according to the layout pattern of fig. 1 of the specification, such as: the positional relationship of up, down, left, right, etc. is determined in accordance with the layout direction of fig. 1 in the specification.
The invention is further described below with reference to examples and figures, examples being: as shown in figure 1, the novel phenol ammonia recovery device for efficiently recovering ammonia comprises a deamination tower 1, a multi-stage fractional condensation system, an ammonia gas purification tower 2, a pressure regulation group valve and an ammonia gas absorption cooler 3, wherein the deamination tower 1 is a rectifying tower provided with a steam heating pipeline and a feeding pipeline 4, the gas phase outlet end at the top of the deamination tower 1 is connected with the gas phase input end of the multi-stage fractional condensation system for reducing the temperature of gas phase materials at the top of the tower and condensing and separating impurity materials, the gas phase outlet end of the multi-stage fractional condensation system is connected with the material inlet end at the lower side of the ammonia gas purification tower 2, the liquid phase outlet end of the multi-stage fractional condensation system is connected with an ammonia condensate tank 5 in a pipe way, the ammonia condensate tank 5 is provided with a first reflux pipeline 6 and a discharge pipeline 7, the first reflux pipeline 6 connects the upper part of the deamination tower 1 with the ammonia condensate tank 5, the first reflux pipeline 6 is provided with a first circulating pump 8, the ammonia gas purification, a tower top gas phase pipeline 9 is arranged on the tower top of the ammonia gas purification tower 2, one end of the tower top gas phase pipeline 9 is communicated with the tower top gas phase outlet end of the ammonia gas purification tower 2, the other end of the tower top gas phase pipeline 9 is communicated with the inlet end of the ammonia gas absorption cooler 3, a pressure adjusting group valve is arranged on the tower top gas phase pipeline 9, an absorption water pipeline 10 is also arranged on the inlet end of the ammonia gas absorption cooler 3, a water quantity control valve 11 is arranged on the absorption water pipeline 10, an ammonia water tank 12 is connected with the outlet end of the ammonia gas absorption cooler 3, a product output pipeline 13 and a second reflux pipeline 14 communicated with the upper part of the ammonia gas purification tower 2 are arranged on the ammonia water tank 12, a second circulating pump 15 is arranged on the second reflux pipeline 14, an inter-cooling circulating device capable of circulating the tower bottom liquid of the ammonia gas purification tower 2 to the tower top is also arranged outside the ammonia gas purification tower 2, a third reflux pipeline 16 is arranged between the tower bottom liquid, a third circulation pump 17 is installed on the third return line 16.
During operation, the coal gasification wastewater rich in acidic gas, ammonia gas and phenolic substances enters the deammoniation tower 1 through the incoming material pipeline 4 after being deacidified, steam in the steam heating pipeline is in reverse contact with the wastewater in the deammoniation tower 1, volatile ammonia gas, oil, phenols and other substances in the wastewater and steam form mixed gas under the heating of the steam, the mixed gas enters the multistage fractional condensation system from a gas phase outlet end at the top of the deammoniation tower 1, the multistage fractional condensation system is used for cooling, depressurizing and liquefying the mixed gas to form condensate, the condensate flows into the ammonia condensate tank 5, the condensate contains most of the phenols, oil substances and part of the ammonia gas, so that purified ammonia gas with high purity is obtained at a gas phase outlet end of the multistage fractional condensation system, the condensate in the ammonia condensate tank 5 is used as reflux liquid of the deammoniation tower 1 and returns to the deammoniation tower 1 through the first reflux pipeline 6 and the first circulating pump 8, compared with the conventional ammonia purification tower 2, the ammonia purification tower 2 provided by the invention does not have a steam heating pipeline for providing a heat source for the ammonia purification tower, the ammonia purification tower works at normal temperature, the heating steam is zero in consumption, the operation cost is greatly reduced, the purified ammonia continuously enters the ammonia purification tower 2, the self pressure in the ammonia purification tower 2 is gradually increased in a self-suppressing mode, the pressure regulating group valve is set to a proper opening in advance, and the ammonia can be finally enabled to be finally obtainedThe pressure in the purification tower 2 is in a certain set dynamic balance state, the ammonia gas in the ammonia gas purification tower 2 can be continuously extracted out of the tower, the extracted ammonia gas can be absorbed by desalted water in the absorption water pipeline 10 to form finished ammonia water to be stored in the ammonia water tank 12 when passing through the ammonia gas absorption cooler 3, the ammonia gas absorption cooler 3 can further reduce the temperature of desalted water so as to more fully absorb the ammonia gas, the solubility of the ammonia gas is increased along with the reduction of the temperature, the second circulating pump 15 can reflux the ammonia water with lower temperature in the ammonia water tank 12 into the ammonia gas purification tower 2, so that a low-temperature and high-pressure environment can be established in the ammonia gas purification tower 2, a small amount of residual phenols and oil substances in the ammonia gas are remained in the ammonia gas purification tower 2 in the form of tower bottom liquid to obtain high-purity ammonia gas, the ammonia content in the recovered ammonia water can be increased from 19% to 30%, the total phenol content is 240 mg.L-1Reduced to 60 mg.L-1Therefore, the concentration of the recovered ammonia water in the ammonia water tank 12 is ensured by energy efficiency, the total phenol content in the ammonia water is reduced, and the quality of the ammonia water is improved.
In the prior art, the tower bottom liquid of an ammonia purification tower 2 is directed to a gas water separation device, while the tower bottom liquid of the ammonia purification tower 2 is directed to an ammonia condensate tank 5 to increase the cold quantity in the ammonia condensate tank 5, all low-temperature liquid in the ammonia condensate tank 5 is sent back to a deamination tower 1 to be recycled as reflux liquid of the deamination tower 1 by starting a first circulating pump 8, so that the tower bottom temperature of the deamination tower 1 can be controlled between 155 and 157 ℃, the tower top temperature is controlled between 130 and 149 ℃, the tower top pressure of the deamination tower 1 is controlled between 0.45 and 0.48MPa, the tower bottom pressure of the deamination tower 1 is controlled between 0.48 and 0.53MPa, compared with the tower top temperature of the deamination tower 1 in the prior art, the tower top temperature of the invention is reduced by about 10 ℃, thereby not only the deamination can be normally carried out, but also the use amount of heating steam in a steam heating pipeline can be reduced, the operation cost is reduced, and meanwhile, the problem that the quality of the ammonia water is influenced because the total phenols in the recovered ammonia water exceed the standard is finally caused in the process that the deamination is caused by the overhigh temperature at the top of the deamination tower 1 and a large amount of phenols are formed and enter a follow-up device. Because a large amount of oil substances exist in the ammonia condensate tank 5, the ammonia condensate tank 5 is required to be periodically collected through the discharge pipeline 7, and after sampling analysis, if the oil is qualified, the oil is sent to a tank area, and if the oil is not qualified, the oil is sent to a gas-water separation device. The ammonia gas purifying tower 2 in the prior art has no pressure control measure, the pressure fluctuation is large, the produced ammonia water has low concentration, high total phenol content and poor quality, the pressure regulating valve group is added, the stable operation of the ammonia gas purifying tower 2 under high pressure can be ensured, the quality of the recovered ammonia water in the ammonia water tank 12 is improved, and the ammonia water with high ammonia content and low phenol content is obtained.
According to the actual need, the novel phenol ammonia recovery device for efficiently recovering ammonia is further optimized or/and improved: further, as shown in the attached drawing 1, the multistage fractional condensation system comprises a primary ammonia condenser 18, a secondary ammonia condenser 19, a tertiary ammonia condenser 20 and an ammonia condensate cooler 24, wherein a gas phase inlet end of the primary ammonia condenser 18 is connected with a gas phase outlet end at the top of the deamination tower 1 through a pipe, a gas phase outlet end of the primary ammonia condenser 18 is communicated with a primary fractional liquid tank 21, a gas phase outlet end of the primary fractional liquid tank 21 is connected with a gas phase inlet end of the secondary ammonia condenser 19 through a pipe, a liquid phase outlet end of the primary fractional liquid tank 21 is connected with an inlet end of the ammonia condensate cooler 24 through a pipe, a gas phase outlet end of the secondary ammonia condenser 19 is communicated with a secondary fractional liquid tank 22, a gas phase outlet end of the secondary fractional liquid tank 22 is communicated with a gas phase inlet end of the tertiary ammonia condenser 20 through a pipe, a liquid phase outlet end of the secondary fractional liquid tank 22 is also connected with an inlet end of the ammonia condensate cooler 24 through a pipe, an outlet end, the gas phase outlet end of the three-stage ammonia condenser 20 is connected with a three-stage liquid separation tank 23 through a pipe, the gas phase outlet end of the three-stage liquid separation tank 23 is connected with a material inlet end at the bottom of the ammonia purification tower 2 through a pipe, and the liquid phase outlet end of the three-stage liquid separation tank 23 is also connected with an ammonia condensate tank 5 through a pipe.
In the technical scheme provided by the invention, wastewater sent by an incoming material pipeline 4 enters a deamination tower 1 to remove ammonia gas after being deacidified, deaminated ammonia water extracted from a tower kettle of the deamination tower 1 is sent to a post-system to remove phenol, mixed gas generated from a gas phase outlet end at the tower top of the deamination tower 1 contains ammonia gas, phenols and oil substances, when the mixed gas passes through a primary ammonia condenser 18, the mixed gas is cooled to 100-130 ℃, a part of the ammonia gas, the phenols and the oil substances in the mixed gas are separated out in the form of condensate liquid and enter a primary liquid separating tank 21, the mixed gas is purified for the first time, the rest mixed gas then enters a secondary ammonia condenser 19 and is cooled to 60-90 ℃, a part of the ammonia gas, the phenols and the oil substances in the mixed gas are separated out in the form of condensate liquid and enter a secondary liquid separating tank 22, at the moment, the mixed gas is purified for the second time, the rest mixed gas finally enters the three-stage ammonia gas condenser 20 and is cooled to 33-45 ℃, a part of ammonia gas, phenols and oil substances in the mixed gas can be separated out in the form of condensate and enter the three-stage liquid separation tank 23, the mixed gas is purified for the third time, and through the multi-stage cooling and condensation, the phenols and oil substances in the mixed gas can be effectively removed, so that the components of the mixed gas entering the ammonia gas purification tower 2 are basically ammonia gas at the end, and the problem that the quality of the ammonia water is influenced because a large amount of phenols are formed and enter a subsequent device, and finally the total phenols in the recovered ammonia water exceed the standard is solved.
Further, as shown in fig. 1, the intercooling device includes a large-displacement intercooling circulating pump 25 and an intercooling circulating cooler 26, a plurality of packing layers are arranged in the ammonia gas purification tower 2, a fourth return line for communicating the tower bottom with the tower top is arranged on the ammonia gas purification tower 2, and the intercooling circulating pump 25 and the intercooling circulating cooler 26 are installed on the fourth return line. The intercooling device is a well-known technology, and the purpose of the intercooling device is to ensure the stable and efficient operation of the ammonia gas purification tower 2.
Further, as shown in fig. 1, the pressure regulating group valve includes an air-operated valve 27, a front hand valve 28, and a rear hand valve 29, the air-operated valve 27, the front hand valve 28, and the rear hand valve 29 are all mounted on the tower top gas phase pipeline 9, the air-operated valve 27 is disposed between the front hand valve 28 and the rear hand valve 29, a bypass pipeline 30 bypassing the air-operated valve 27, the front hand valve 28, and the rear hand valve 29 is further disposed on the tower top gas phase pipeline 9, one end of the bypass pipeline 30 is communicated with the tower top gas phase pipeline 9 in front of the front hand valve 28, the other end of the bypass pipeline 30 is communicated with the tower top gas phase pipeline 9 behind the rear hand valve 29, and a service hand valve 31 is mounted on the bypass pipeline 30.
When the air-operated valve 27 is in a fault state, the front hand valve 28 and the rear hand valve 29 are all in an open state, and when the air-operated valve 27 is in a fault state, the front hand valve 28 and the rear hand valve 29 can be closed, and the maintenance hand valve 31 on the bypass pipeline 30 is opened, so that the air-operated valve 27 can be maintained, and continuous normal work of the invention is not influenced.
Further, as shown in fig. 1, a safety pipeline 32 communicated with the gas phase pipeline 9 at the top of the tower is further arranged at the gas phase outlet end of the three-stage liquid separation tank 23, the safety pipeline 32 is arranged in front of the pressure regulating valve, a first safety hand valve 33 for controlling the safety pipeline 32 to be opened and closed is arranged on the safety pipeline 32, and a second safety hand valve 34 is arranged on a pipeline connected with the material inlet end at the lower side of the ammonia gas purification tower 2.
When the ammonia gas purification tower 2 normally operates, the safety pipeline 32 is always in a disconnected state, the second safety hand valve 34 and the pressure regulating group valve are in an open state, when the ammonia gas purification tower 2 breaks down, the first safety hand valve 33 is opened, the second safety hand valve 34 is closed, ammonia gas discharged from the gas phase outlet end of the three-stage liquid separating tank 23 is directly absorbed by desalted water in the absorption water pipeline 10 through the safety pipeline 32 and the pressure regulating group valve and flows into the ammonia water tank 12, and finally the ammonia gas is led out through the product output pipeline 13, so that the ammonia gas discharged from the deamination tower 1 is temporarily treated, the ammonia gas purification tower 2 can be maintained under the condition that the ammonia gas purification tower is not closed, and the ammonia gas purification tower has high practicability.
The foregoing description is by way of example only and is not intended as limiting the embodiments of the present application. All obvious variations and modifications of the present invention are within the scope of the present invention.
Claims (8)
1. A novel phenol ammonia recovery device for efficiently recovering ammonia is characterized by comprising a deamination tower, a multistage segregation system, an ammonia gas purification tower, a pressure regulating group valve and an ammonia gas absorption cooler, wherein the deamination tower is a rectifying tower provided with a steam heating pipeline and a feeding pipeline, the gas phase outlet end at the top of the deamination tower is connected with the gas phase input end pipe of the multistage segregation system to reduce the temperature of the gas phase material at the top of the tower and condense and separate impurity materials, the gas phase output end of the multistage segregation system is connected with the material inlet end pipe at the lower side of the ammonia gas purification tower, the liquid phase output end of the multistage segregation system is connected with an ammonia condensate tank pipe, the ammonia condensate tank is provided with a first backflow pipeline and a discharge pipeline, the upper part of the deamination tower is communicated with the ammonia condensate tank by the first backflow pipeline, a first circulating pump is arranged on the first backflow pipeline, the ammonia gas purification tower is a packed tower without the steam heating pipeline, the tower top of the ammonia gas purification tower is provided with a tower top gas phase pipeline, one end of the tower top gas phase pipeline is communicated with the tower top gas phase outlet end of the ammonia gas purification tower, the other end of the tower top gas phase pipeline is communicated with the inlet end of an ammonia gas absorption cooler, a pressure adjusting group valve is arranged on the tower top gas phase pipeline, the inlet end of the ammonia gas absorption cooler is also provided with an absorption water pipeline, a water quantity control valve is arranged on the absorption water pipeline, the outlet end of the ammonia gas absorption cooler is connected with an ammonia water tank, the ammonia water tank is provided with a product output pipeline and a second return pipeline communicated with the upper part of the ammonia gas purification tower, a second circulating pump is arranged on the second return pipeline, the ammonia gas purification tower is also provided with an intercooling circulation device which can circulate the tower bottom liquid of the ammonia gas purification tower to the tower top, and the tower bottom liquid outlet end of the ammonia gas purification, and a third circulating pump is arranged on the third return pipeline.
2. The novel phenol ammonia recovery device for efficiently recovering ammonia according to claim 1, wherein the multistage fractional condensation system comprises a primary ammonia condenser, a secondary ammonia condenser, a tertiary ammonia condenser and an ammonia condensate cooler, a gas phase inlet end of the primary ammonia condenser is connected with a gas phase outlet end pipe at the top of the deamination tower, a gas phase outlet end pipe of the primary ammonia condenser is communicated with a primary fractional liquid tank, a gas phase outlet end of the primary fractional liquid tank is connected with a gas phase inlet end pipe of the secondary ammonia condenser, a liquid phase outlet end of the primary liquid separation tank is connected with an inlet end pipe of the ammonia condensate cooler, a gas phase outlet end pipe of the secondary ammonia condenser is communicated with a secondary fractional liquid tank, a gas phase outlet end of the secondary fractional liquid tank is communicated with a gas phase inlet end pipe of the tertiary ammonia condenser, and a liquid phase outlet end of the secondary fractional liquid tank is also connected with an inlet end pipe of the ammonia condensate, the exit end and the ammonia condensate jar union coupling of ammonia condensate cooler, the gaseous phase exit end and the tertiary knockout drum union coupling of tertiary ammonia condenser, the gaseous phase exit end and the material entry end union coupling of ammonia purification tower bottom of three-stage knockout drum, the liquid phase exit end of tertiary knockout drum also with ammonia condensate jar union coupling.
3. The novel phenol ammonia recovery device for efficiently recovering ammonia according to claim 1 or 2, wherein the intercooling device comprises a large-displacement intercooling circulating pump and an intercooling cooler, a plurality of packing layers are arranged in the ammonia gas purification tower, a fourth return pipeline for communicating the tower bottom with the tower top is arranged on the ammonia gas purification tower, and the intercooling circulating pump and the intercooling cooler are arranged on the fourth return pipeline.
4. The novel phenol ammonia recovery device for efficiently recovering ammonia according to claim 1 or 2, wherein the pressure regulating valve comprises a pneumatic valve, a front hand valve and a rear hand valve, the pneumatic valve, the front hand valve and the rear hand valve are all installed on the gas phase pipeline at the top of the tower, the pneumatic valve is arranged between the front hand valve and the rear hand valve, a bypass pipeline bypassing the pneumatic valve, the front hand valve and the rear hand valve is further arranged on the gas phase pipeline at the top of the tower, one end of the bypass pipeline is communicated with the gas phase pipeline at the top of the tower in front of the front hand valve, the other end of the bypass pipeline is communicated with the gas phase pipeline at the top of the tower in rear of the rear hand valve, and the maintenance hand valve is installed on the bypass pipeline.
5. The novel phenol ammonia recovery device for efficiently recovering ammonia according to claim 3, wherein the pressure regulating valve comprises a pneumatic valve, a front hand valve and a rear hand valve, the pneumatic valve, the front hand valve and the rear hand valve are all installed on the tower top gas phase pipeline, the pneumatic valve is arranged between the front hand valve and the rear hand valve, a bypass pipeline bypassing the pneumatic valve, the front hand valve and the rear hand valve is further arranged on the tower top gas phase pipeline, one end of the bypass pipeline is communicated with the tower top gas phase pipeline in front of the front hand valve, the other end of the bypass pipeline is communicated with the tower top gas phase pipeline behind the rear hand valve, and the maintenance hand valve is installed on the bypass pipeline.
6. A novel phenol ammonia recovery device for efficiently recovering ammonia according to claim 1, 2 or 5, which is characterized in that a safety pipeline communicated with a gas phase pipeline at the top of the tower is further arranged at the gas phase outlet end of the three-stage liquid separation tank, the safety pipeline is arranged in front of the pressure regulating valve, a first safety hand valve for controlling the on-off of the safety pipeline is arranged on the safety pipeline, and a second safety hand valve is arranged on a pipeline connected with a material inlet end at the lower side of the ammonia gas purification tower.
7. The novel phenol ammonia recovery device for efficiently recovering ammonia according to claim 3, wherein a safety pipeline communicated with the gas phase pipeline at the top of the tower is further arranged at the gas phase outlet end of the three-stage liquid separation tank, the safety pipeline is arranged in front of the pressure regulating valve set, a first safety hand valve for controlling the safety pipeline to be switched on and off is arranged on the safety pipeline, and a second safety hand valve is arranged on a pipeline connected with the material inlet end at the lower side of the ammonia gas purification tower.
8. The novel phenol ammonia recovery device for efficiently recovering ammonia according to claim 4, wherein a safety pipeline communicated with the gas phase pipeline at the top of the tower is further arranged at the gas phase outlet end of the three-stage liquid separation tank, the safety pipeline is arranged in front of the pressure regulating valve set, a first safety hand valve for controlling the safety pipeline to be switched on and off is arranged on the safety pipeline, and a second safety hand valve is arranged on a pipeline connected with the material inlet end at the lower side of the ammonia gas purification tower.
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| CN201911083670.3A CN110723771A (en) | 2019-11-07 | 2019-11-07 | Novel phenol ammonia recovery device for efficiently recovering ammonia |
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| CN201911083670.3A CN110723771A (en) | 2019-11-07 | 2019-11-07 | Novel phenol ammonia recovery device for efficiently recovering ammonia |
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| CN112499710A (en) * | 2020-10-20 | 2021-03-16 | 阮氏化工（常熟）有限公司 | Device and method for purifying ammonia water by using ammonia-containing wastewater |
| CN114455687A (en) * | 2022-03-17 | 2022-05-10 | 北京中科康仑环境科技研究院有限公司 | Method for recovering oil-free ammonia water from oil-containing ammonia-containing wastewater by deamination |
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