CN106277145A - The apparatus and method that a kind of aromatic hydrocarbons cleaning produces - Google Patents
The apparatus and method that a kind of aromatic hydrocarbons cleaning produces Download PDFInfo
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- CN106277145A CN106277145A CN201610788615.4A CN201610788615A CN106277145A CN 106277145 A CN106277145 A CN 106277145A CN 201610788615 A CN201610788615 A CN 201610788615A CN 106277145 A CN106277145 A CN 106277145A
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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
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/46—Removing components of defined structure
- B01D53/48—Sulfur compounds
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/46—Removing components of defined structure
- B01D53/48—Sulfur compounds
- B01D53/52—Hydrogen sulfide
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/46—Removing components of defined structure
- B01D53/54—Nitrogen compounds
- B01D53/56—Nitrogen oxides
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/76—Gas phase processes, e.g. by using aerosols
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/77—Liquid phase processes
- B01D53/78—Liquid phase processes with gas-liquid contact
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01C—AMMONIA; CYANOGEN; COMPOUNDS THEREOF
- C01C1/00—Ammonia; Compounds thereof
- C01C1/02—Preparation, purification or separation of ammonia
- C01C1/10—Separation of ammonia from ammonia liquors, e.g. gas liquors
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2251/00—Reactants
- B01D2251/20—Reductants
- B01D2251/206—Ammonium compounds
- B01D2251/2062—Ammonia
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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
- Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines
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Abstract
The invention discloses the apparatus and method that a kind of aromatic hydrocarbons cleaning produces, it is made up of unit such as submarine discharge, ammonia refining, ammonia repurity, denitrating flue gas and flue gas desulfurizations, hydrogen sulfide and liquefied ammonia is extracted from the acid waste water that aromatics production process produces, purification Water Sproading after extraction utilizes, reduce the consumption of water in producing, hydrogen sulfide is for combustion heat release amount or for Recovered sulphur, after liquid ammonia gasification, and part nitrogen oxides directly and in boiler sulfur-bearing nitrogen smoke reaction removing flue gas；Part is first reacted with water and is formed ammonia, is used further to the desulfurization of flue gas, producing ammonium sulfate byproduct after denitration, the present invention turns waste into wealth, and eliminates waste water and waste gas simultaneously, it is to avoid sour water, nitrogen oxides, the oxysulfide pollution to environment, reclaim water resource, the valuable ammonium sulfate of by-product.
Description
Technical field
The invention belongs to petrochemical industry, waste water and sulfur-bearing nitrogen during a kind of aromatics production
The comprehensive treatment device of flue gas and method.
Background technology
In petrochemical production process, some sewage can be supervened, containing the sulfuration that concentration is higher in these sewage
Hydrogen and ammonia, just pollute the environment if do not removed, the normal ecosystem of welding.Sewage stripping is special disposal refinery
The acid water that each process unit is discharged, to remove the polluted medias such as H2S, NH3 of containing in acid water.Single column side line vapour at present
Put forward technique and utilize hydrogen sulfide different from the volatility of ammonia, obtaining high concentration hydrogen sulfide gas at the top of tower, and in tower
The ammonia of high concentration is extracted in portion out, but this technique and aftertreatment systems can not remove the impurity such as oil and phenols, cause recovery
Ammonia value is relatively low.
It addition, under the strictest overall background of environmental protection requirement, nitrogenous sulfur boiler smoke realizes ultra-clean discharge
It it is following development trend.The desulphurization denitration of flue gas all can realize by injecting ammonia or ammonia.Therefore, if can be by sewage
Manage the application that combines with the exhaust-gas treatment of boiler smoke, then can eliminate the pollution of waste water, the pollution of waste gas can be eliminated again.Cause
This, the integrated treatment of research sewage and waste gas is significant.
Summary of the invention
The deficiency existed for prior art, it is an object of the invention to provide device and side that a kind of aromatic hydrocarbons cleaning produces
Method, carries out comprehensive control, by submarine discharge, ammonia refining, flue gas desulfurization to waste water during aromatics production and sulfur-bearing nitrogen flue gas
With operations such as denitrating flue gas, wastewater ocean disposal is organically combined with flue gas desulfurization and denitrification, reached to eliminate sewage simultaneously
With the purpose of toxic harmful exhaust gas, and reclaim purification water.
For achieving the above object, the technical scheme is that the device that a kind of aromatic hydrocarbons cleaning produces, including dirt
Water stripper plant, ammonia refining device, equipment for denitrifying flue gas and flue gas desulfurization device, described sewage stripping device includes raw material sewage
Tank, feed pump, stripper, stripping tower top cooler, stripping tower top separatory tank, stripping tower bottom reboiler, thick ammonia condenser and thick
Ammonia separatory tank, the described outlet of raw material Water Tank is connected with the entrance of feed pump, described charging delivery side of pump and the tower of stripper
Top material inlet is connected, and the tower top discharging opening of described stripper is connected with the entrance of stripping tower top cooler, and described stripping tower top cools down
The outlet of device is connected with the entrance of stripping tower top separatory tank, and the top of described stripping tower top separatory tank hydrogen sulfide tail gas out goes
Sulphur recovery, the middle part discharging opening of described stripper is connected with the entrance of thick ammonia condenser, the outlet of described thick ammonia condenser with
The entrance of thick ammonia separatory tank is connected；Described ammonia refining device includes that ammonia refining tower, ammonia circulating pump, ammonia liquor separator, desulfurization are inhaled
Attached tower, ammonia condenser and liquid ammonia storage tank, the described thick top exit of ammonia separatory tank is connected with the centre entrance of ammonia refining tower, described
The outlet at bottom of thick ammonia separatory tank is connected with raw material Water Tank, the top exit of described ammonia refining tower and the entrance of ammonia liquor separator
Being connected, the top exit of described ammonia liquor separator is connected with the bottom inlet of desulfurization adsorption tower, the bottom of described ammonia liquor separator
Outlet is connected with raw material Water Tank, and the top exit of described desulfurization adsorption tower is connected with the first entrance of ammonia condenser, described ammonia
First outlet of condenser is connected with the outlet of liquid ammonia storage tank；Described equipment for denitrifying flue gas includes that liquefied ammonia delivery pump, liquefied ammonia evaporate
Device, ammonia/air mixer, dilution air, ammonia injection grid and Benitration reactor, the outlet of described liquid ammonia storage tank and liquefied ammonia
The entrance of delivery pump is connected, and described liquefied ammonia conveying delivery side of pump is connected with the entrance of liquid ammonia evaporator, described liquid ammonia evaporator
Outlet is connected with the first entrance of ammonia/air mixer, the outlet of described dilution air and the second of ammonia/air mixer
Entrance is connected, and the outlet of described ammonia/air mixer is connected with the first entrance of ammonia injection grid, described ammonia injection lattice
Second entrance of grid is connected with boiler exit gas mouth, and the outlet of described ammonia injection grid is connected with the entrance of Benitration reactor；Institute
Stating flue gas desulfurization device and include air preheater, ammonia water tank, aqua ammonia pump, circulating pump, desulfurizing tower and oxidation fan, described denitration is anti-
Answering the outlet of device to be connected with the first entrance of air preheater, the first outlet of described air preheater enters with the first of desulfurizing tower
Mouth is connected.First entrance of described ammonia water tank is connected with the outlet line of liquid ammonia evaporator, the second entrance of described ammonia water tank with
Demineralized water pipeline is connected, and the outlet of described ammonia water tank is connected with the entrance of aqua ammonia pump, the entrance of described circulating pump and desulfurizing tower
First outlet is connected, and the outlet line of described circulating pump first converges with the outlet line of aqua ammonia pump, is then divided into three branch roads, and three
Individual branch road is connected into desulfurizing tower, and the outlet of described oxidation fan is connected with the second entrance of desulfurizing tower.
As a further improvement on the present invention, also include ammonia repurity device, described ammonia repurity device include ammonia compressor,
Ammonia separator and liquefied ammonia bleacher, described ammonia compressor and ammonia separator are arranged between desulfurization adsorption tower and ammonia condenser, described
The top exit of desulfurization adsorption tower is first connected with the entrance of ammonia compressor, the entrance phase of the outlet of described ammonia compressor and ammonia separator
Even, the outlet at bottom of described ammonia separator is connected with slop tank, the top exit of described ammonia separator and the first of ammonia condenser
Entrance is connected, and described liquefied ammonia bleacher is located between ammonia condenser and liquid ammonia storage tank, the first outlet of described ammonia condenser first with
The bottom inlet of liquefied ammonia bleacher is connected, and the described top exit of liquefied ammonia bleacher is connected with the import of liquid ammonia storage tank.
As a further improvement on the present invention, the hydrogen sulfide tail gas of the top exit of described stripping tower top separatory tank is divided into
Two-way, a road goes sulphur recovery, and another road is admitted to boiler combustion system burning.
As a further improvement on the present invention, described liquefied ammonia conveying delivery side of pump is divided into two-way, and liquid ammonia evaporator is removed on a road,
Another road deammoniation treating column.
The method that a kind of aromatic hydrocarbons cleaning produces, it is characterised in that: comprise the following steps:
A, through feed pump sewage in raw material Water Tank being sent into stripper, described stripper uses 1.0MPa steam to add
Heat, tower top material enters stripping tower top cooler cooling, enters stripping tower top separatory tank, from stripping tower top separatory tank gas out
Phase hydrogen sulfide is sent into boiler combustion or goes sulfur recycle section Recovered sulphur, and liquid phase returns raw material Water Tank；In described stripper
The 150-160 DEG C of thick ammonia of gas phase is derived in portion, and the thick ammonia of gas phase, after thick ammonia condenser condenses, enters thick ammonia separatory tank separatory, from
Thick ammonia separatory the tank out rear and outlet of liquefied ammonia delivery pump liquefied ammonia enters ammonia refining tower after mixing；Bottom described stripper after stripping
Purification water cooling after return upstream device recycle；
B, liquefied ammonia and thick ammonia are mixed into ammonia refining tower, and ammoniacal liquor at the bottom of tower is delivered to top of tower through ammonia circulating pump and is circulated
Cleaning, the hydrogen sulfide in removing ammonia, ammonia water containing sulfur drains into raw material Water Tank from interruption at the bottom of tower, and ammonia enters ammoniacal liquor from tower top and divides
From device；The sewage that described ammonia liquor separator outlet at bottom is discharged returns raw material Water Tank, described ammonia liquor separator top exit
Gas-phase product enters desulfurization adsorption tower and carries out desulfurization process, and the ammonia after desulfurization sends into ammonia compressor；
Ammonia after c, desulfurization sends into ammonia compressor supercharging, described ammonia compressor outlet pressure 1.2-1.5MPa, the ammonia after supercharging
Gas enters ammonia separator and separates the oil phase of liquefaction, and the ammonia of gas phase liquefies after ammonia condenser condenses, and liquefied ammonia sends into liquefied ammonia decolouring
Tank removing phenols and oils, subsequently into liquid ammonia storage tank；
Liquefied ammonia in d, described liquid ammonia storage tank is through liquefied ammonia delivery pump feeding liquid ammonia evaporator by liquid ammonia gasification, and described liquefied ammonia steams
Sending out device outlet ammonia temperature 40-55 DEG C, pressure 0.3-0.5MPa, after ammonia mixes according to volume ratio 1:100-2:100 with air
Entering ammonia injection, grid is full and uniform with the boiler smoke of sulfur-bearing nitride mixes, and then gaseous mixture entrance Benitration reactor is anti-
Nitrogen oxides should be reduced to nitrogen, and denitration reaction temperature is 355-370 DEG C；
After e, denitration, boiler smoke is cooled further to 160-170 DEG C of entrance desulfurizing tower through air preheater, at desulfurizing tower
Interior ammonia mixes with flue gas by the way of spray, is blasted air in the bottom of desulfurizing tower by oxidation fan, at ammonia and air
The lower sulfurous gas removed in boiler smoke of effect, the used ammonia of desulfurizing tower is to be mixed by ammonia and demineralized water in ammonia water tank
Close preparation, then in aqua ammonia pump injects desulfurizing tower.
As a further improvement on the present invention, described stripper overhead temperature 40-60 DEG C, pressure 0.5-0.8MPa, at the bottom of tower
Temperature 150-175 DEG C, pressure 0.4-0.55MPa.
As a further improvement on the present invention, the operation temperature of described ammonia refining tower maintains-10～0 DEG C.
As a further improvement on the present invention, in described liquefied ammonia bleacher, decolorizing adsorbent is activated carbon.
Apparatus and method of the present invention passes through submarine discharge, ammonia refining, flue gas desulfurization and denitrating flue gas operation unit by dirt
Water Sproading utilizes and organically combines with flue gas desulfurization and denitrification, and the desulfurization making steam stripped ammonia in sewage be directly used in flue gas takes off
Nitre, has reached to eliminate sewage and the purpose of toxic harmful exhaust gas simultaneously, and has realized recycling of water resource, decreased waste water
Outer row；After the ammonia gas purification that is stripped off processes, directly apply to the ultra-clean discharge of boiler smoke, make sulfur dioxide in flue gas and
The content of nitrogen oxides all reaches the requirement of ultra-clean discharge, and the present invention turns waste into wealth, in eliminating chemical plant installations production process
Waste water and waste gas while, also reclaimed part of sulfuric acid ammonium, economic benefit and environmental benefit the most notable.
Accompanying drawing explanation
Fig. 1 is the structural representation of the present invention.
Detailed description of the invention
Below in conjunction with the embodiment given by accompanying drawing, the present invention is described in further detail.
Device embodiment 1
The device produced with reference to the cleaning of a kind of aromatic hydrocarbons shown in Fig. 1 is the purest including sewage stripping device, ammonia refining device, ammonia
Gasifying device, equipment for denitrifying flue gas and flue gas desulfurization device, described sewage stripping device includes raw material Water Tank 1, feed pump 2, vapour
Stripper 3, stripping tower top cooler 4, stripping tower top separatory tank 5, stripping tower bottom reboiler 6, thick ammonia condenser 7 and thick ammonia separatory tank
8, the outlet of raw material Water Tank 1 is connected with the entrance of feed pump 2, and the outlet of feed pump 2 feeds with the tower top of stripper 3 and is connected,
The tower top discharging opening of stripper 3 is connected with the entrance of stripping tower top cooler 4, the outlet of stripping tower top cooler 4 and stripper
The entrance of top separatory tank 5 is connected, and the hydrogen sulfide tail gas of the top exit of stripping tower top separatory tank 5 is divided into two-way, a road desulfuration
Sulphur reclaims, and another road is admitted to boiler combustion system burning, the entrance phase of the middle part discharging opening of stripper 3 and thick ammonia condenser 7
Even, the outlet of thick ammonia condenser 7 is connected with the entrance of thick ammonia separatory tank 8；Ammonia refining device includes that ammonia refining tower 9, ammoniacal liquor circulate
Pump 10, ammonia liquor separator 11, desulfurization adsorption tower 12, ammonia condenser 15 and liquid ammonia storage tank 17, the top exit of thick ammonia separatory tank 8 with
The centre entrance of ammonia refining tower 9 is connected, and the outlet at bottom of thick ammonia separatory tank 8 is connected with raw material Water Tank 1, the top of ammonia refining tower 9
Portion's outlet is connected with the entrance of ammonia liquor separator 11, the top exit of ammonia liquor separator 11 and the bottom inlet of desulfurization adsorption tower 12
Being connected, the outlet at bottom of ammonia liquor separator 11 is connected with raw material Water Tank 1, the top exit of desulfurization adsorption tower 12 and ammonia condenser
First entrance of 15 is connected, and the first outlet of ammonia condenser 15 is connected with the outlet of liquid ammonia storage tank 17；Ammonia repurity device includes
Ammonia compressor 13, ammonia separator 14 and liquefied ammonia bleacher 16, ammonia compressor 13 and ammonia separator 14 are arranged on desulfurization adsorption tower 12 and ammonia
Between condenser 15, the top exit of desulfurization adsorption tower 12 is first connected with the entrance of ammonia compressor 13, the outlet of ammonia compressor 13 and ammonia
The entrance of separator 14 is connected, and the outlet at bottom of ammonia separator 14 is connected with slop tank, the top exit of ammonia separator 14 and ammonia
First entrance of condenser 15 is connected, and liquefied ammonia bleacher 16 is located between ammonia condenser 15 and liquid ammonia storage tank 17, ammonia condenser 15
The first outlet be first connected with the bottom inlet of liquefied ammonia bleacher 16, the top exit of liquefied ammonia bleacher 16 and liquid ammonia storage tank 17
Import is connected；Equipment for denitrifying flue gas includes liquefied ammonia delivery pump 18, liquid ammonia evaporator 19, ammonia/air mixer 20, dilution air
21, ammonia injection grid 22 and Benitration reactor 23, the outlet of liquid ammonia storage tank 17 is connected with the entrance of liquefied ammonia delivery pump 18, liquefied ammonia
The outlet of delivery pump 18 is divided into two-way, and liquid ammonia evaporator 19 is removed on a road, another road deammoniation treating column 9, going out of liquid ammonia evaporator 19
Mouth is connected with the first entrance of ammonia/air mixer 20, the outlet of dilution air 21 and the second of ammonia/air mixer 20
Entrance is connected, and the outlet of ammonia/air mixer 20 is connected with the first entrance of ammonia injection grid 22, ammonia injection grid 22
The second entrance be connected with boiler exit gas mouth, ammonia injection grid 22 outlet be connected with the entrance of Benitration reactor 23；Flue gas
Desulfurizer includes air preheater 24, ammonia water tank 25, aqua ammonia pump 26, circulating pump 27, desulfurizing tower 28 and oxidation fan 29, denitration
The outlet of reactor 23 is connected with the first entrance of air preheater 24, the first outlet and the desulfurizing tower 28 of air preheater 24
First entrance is connected.First entrance of ammonia water tank 25 is connected with the outlet line of liquid ammonia evaporator 19, and the second of ammonia water tank 25 enters
Mouth is connected with demineralized water pipeline, and the outlet of ammonia water tank 25 is connected with the entrance of aqua ammonia pump 26, the entrance of circulating pump 27 and desulfurizing tower
First outlet of 28 is connected, and first and aqua ammonia pump 26 the outlet line of the outlet line of circulating pump 27 converges, and is then divided into three
Road, three branch roads are connected into desulfurizing tower 28, and the outlet of oxidation fan 29 is connected with the second entrance of desulfurizing tower 28.
Embodiment of the method 1
A, through feed pump 2, sewage in raw material Water Tank 1 being sent into stripper 3, stripper 3 uses 1.0MPa steam to add
Heat, stripper 3 tower top temperature 40 DEG C, pressure 0.5MPa, column bottom temperature 163 DEG C, pressure 0.53MPa, tower top material enters stripping
Tower top cooler 4 cools down, and enters stripping tower top separatory tank 5, sends into boiler from stripping tower top separatory tank 5 hydrogen sulphide in the vapor phase out
Burning or go sulfur recycle section Recovered sulphur, liquid phase returns raw material Water Tank 1；155 DEG C of thick ammonia of gas phase are derived in the middle part of stripper 3
Gas, the thick ammonia of gas phase, after thick ammonia condenser 7 condenses, enters thick ammonia separatory tank 8 separatory, the out rear and liquid from thick ammonia separatory tank 8
Ammonia refining tower 9 is entered after the liquefied ammonia mixing of ammonia delivery pump 18 outlet；On returning after purification water cooling after stripping bottom stripper 3
Trip device recycles.
B, liquefied ammonia and thick ammonia are mixed into ammonia refining tower 9, and the operation temperature of ammonia refining tower 9 maintains-5 DEG C, ammonia at the bottom of tower
Liquid is delivered to top of tower through ammonia circulating pump 10 and is circulated cleaning, the hydrogen sulfide in removing ammonia, and ammonia water containing sulfur is interrupted from the bottom of tower
Draining into raw material Water Tank 1, ammonia enters ammonia liquor separator 11 from tower top；The sewage that ammonia liquor separator 11 outlet at bottom is discharged returns
Raw material Water Tank 1, the gas-phase product of ammonia liquor separator 11 top exit enters desulfurization adsorption tower 12 and carries out desulfurization process, after desulfurization
Ammonia send into ammonia compressor 13.
Ammonia after c, desulfurization sends into ammonia compressor 13 supercharging, ammonia compressor outlet pressure 1.2MPa, and the ammonia after supercharging enters
Ammonia separator 14 separates the oil phase of liquefaction, and the ammonia of gas phase liquefies after ammonia condenser 15 condenses, and liquefied ammonia sends into liquefied ammonia bleacher
16, in liquefied ammonia bleacher 16, decolorizing adsorbent is activated carbon, removes phenols and oils, liquefied ammonia after decolouring in liquefied ammonia bleacher 16
Middle phenols residuals content is not more than 0.4%, and liquefied ammonia content is more than 99.6%, subsequently into liquid ammonia storage tank 17.
Liquefied ammonia in d, liquid ammonia storage tank 17 is sent into liquid ammonia evaporator 19 through liquefied ammonia delivery pump 18 and liquid ammonia gasification, liquefied ammonia is evaporated
Device 19 exports ammonia temperature 47 DEG C, pressure 0.39MPa, and ammonia enters ammonia injection with air after mixing according to volume ratio 1:100
Grid 22 is full and uniform with the boiler smoke of sulfur-bearing nitride to be mixed, and then gaseous mixture entrance Benitration reactor 23 reacts nitrogen oxygen
Compound is reduced to nitrogen, and denitration reaction temperature is 355 DEG C.
After e, denitration, boiler smoke is cooled further to 166 DEG C of entrance desulfurizing towers 28 through air preheater 24, at desulfurizing tower
Ammonia SO by the way of spray and in flue gas in 282Reaction generates (NH4)2SO3, in the bottom of desulfurizing tower 28 by oxidation wind
Machine 29 blasts air, by (NH4)2SO3It is oxidized to ammonium sulfate.The used ammonia of desulfurizing tower 28 in ammonia water tank 25 by ammonia with remove
Saline is mixed with, the SO then in aqua ammonia pump 26 injects desulfurizing tower 28, after desulfurizing tower 28, in flue gas2Content is little
In 30mg/Nm3；After Benitration reactor, in flue gas, the content of NOx is not more than 40mg/Nm3。
Prepare as a example by aromatics production technique by the heavy oil of 2,000,000 tons/year, the present embodiment the most recyclable purification water
120t, liquefied ammonia 800kg, greatly reduce the impact on environment of boiler smoke nitrogen oxides and oxysulfide, real economy simultaneously
Benefit and environmental benefit are the most notable.
Embodiment of the method 2
A, through feed pump 2, sewage in raw material Water Tank 1 being sent into stripper 3, stripper 3 uses 1.0MPa steam to add
Heat, stripper 3 tower top temperature 60 DEG C, pressure 0.7MPa, column bottom temperature 170 DEG C, pressure 0.50MPa, tower top material enters stripping
Tower top cooler 4 cools down, and enters stripping tower top separatory tank 5, sends into boiler from stripping tower top separatory tank 5 hydrogen sulphide in the vapor phase out
Burning or go sulfur recycle section Recovered sulphur, liquid phase returns raw material Water Tank 1；150 DEG C of thick ammonia of gas phase are derived in the middle part of stripper 3
Gas, the thick ammonia of gas phase, after thick ammonia condenser 7 condenses, enters thick ammonia separatory tank 8 separatory, the out rear and liquid from thick ammonia separatory tank 8
Ammonia refining tower 9 is entered after the liquefied ammonia mixing of ammonia delivery pump 18 outlet；On returning after purification water cooling after stripping bottom stripper 3
Trip device recycles.
B, liquefied ammonia and thick ammonia are mixed into ammonia refining tower 9, and the operation temperature of ammonia refining tower 9 maintains-10 DEG C, ammonia at the bottom of tower
Liquid is delivered to top of tower through ammonia circulating pump 10 and is circulated cleaning, the hydrogen sulfide in removing ammonia, and ammonia water containing sulfur is interrupted from the bottom of tower
Draining into raw material Water Tank 1, ammonia enters ammonia liquor separator 11 from tower top；The sewage that ammonia liquor separator 11 outlet at bottom is discharged returns
Raw material Water Tank 1, the gas-phase product of ammonia liquor separator 11 top exit enters desulfurization adsorption tower 12 and carries out desulfurization process, after desulfurization
Ammonia send into ammonia compressor 13.
Ammonia after c, desulfurization sends into ammonia compressor 13 supercharging, ammonia compressor outlet pressure 1.3MPa, and the ammonia after supercharging enters
Ammonia separator 14 separates the oil phase of liquefaction, and the ammonia of gas phase liquefies after ammonia condenser 15 condenses, and liquefied ammonia sends into liquefied ammonia bleacher
16, in liquefied ammonia bleacher 16, decolorizing adsorbent is activated carbon, removes phenols and oils, liquefied ammonia after decolouring in liquefied ammonia bleacher 16
Middle phenols residuals content is not more than 0.4%, and liquefied ammonia content is more than 99.6%, subsequently into liquid ammonia storage tank 17.
Liquefied ammonia in d, liquid ammonia storage tank 17 is sent into liquid ammonia evaporator 19 through liquefied ammonia delivery pump 18 and liquid ammonia gasification, liquefied ammonia is evaporated
Device 19 exports ammonia temperature 52 DEG C, pressure 0.43MPa, and ammonia enters ammonia injection with air after mixing according to volume ratio 2:100
Grid 22 is full and uniform with the boiler smoke of sulfur-bearing nitride to be mixed, and then gaseous mixture entrance Benitration reactor 23 reacts nitrogen oxygen
Compound is reduced to nitrogen, and denitration reaction temperature is 370 DEG C.
After e, denitration, boiler smoke is cooled further to 168 DEG C of entrance desulfurizing towers 28 through air preheater 24, at desulfurizing tower
Ammonia SO by the way of spray and in flue gas in 282Reaction generates (NH4)2SO3, in the bottom of desulfurizing tower 28 by oxidation wind
Machine 29 blasts air, by (NH4)2SO3It is oxidized to ammonium sulfate.The used ammonia of desulfurizing tower 28 in ammonia water tank 25 by ammonia with remove
Saline is mixed with, the SO then in aqua ammonia pump 26 injects desulfurizing tower 28, after desulfurizing tower 28, in flue gas2Content is little
In 30mg/Nm3；After Benitration reactor, in flue gas, the content of NOx is not more than 40mg/Nm3。
Prepare as a example by aromatics production technique by the heavy oil of 2,000,000 tons/year, the present embodiment the most recyclable purification water
110t, liquefied ammonia 700kg, greatly reduce the impact on environment of boiler smoke nitrogen oxides and oxysulfide, real economy simultaneously
Benefit and environmental benefit are the most notable.
Below being only the preferred embodiment of the present invention, protection scope of the present invention is not limited merely to above-described embodiment,
All technical schemes belonged under thinking of the present invention belong to protection scope of the present invention.It should be pointed out that, for the art
For those of ordinary skill, some improvements and modifications without departing from the principles of the present invention, these improvements and modifications also should
It is considered as protection scope of the present invention.
Claims (8)
1. the device that an aromatic hydrocarbons cleaning produces, it is characterised in that: include sewage stripping device, ammonia refining device, denitrating flue gas
Device and flue gas desulfurization device, described sewage stripping device includes raw material Water Tank (1), feed pump (2), stripper (3), stripping
Tower top cooler (4), stripping tower top separatory tank (5), stripping tower bottom reboiler (6), thick ammonia condenser (7) and thick ammonia separatory tank
(8), the outlet of described raw material Water Tank (1) is connected with the entrance of feed pump (2), the outlet of described feed pump (2) and stripper
(3) tower top charging is connected, and the tower top discharging opening of described stripper (3) is connected with the entrance of stripping tower top cooler (4), described
The outlet of stripping tower top cooler (4) is connected with the entrance of stripping tower top separatory tank (5), described stripping tower top separatory tank (5)
Top hydrogen sulfide tail gas out removes the entrance of sulphur recovery, the middle part discharging opening of described stripper (3) and thick ammonia condenser (7)
Being connected, the outlet of described thick ammonia condenser (7) is connected with the entrance of thick ammonia separatory tank (8)；Described ammonia refining device includes ammonia essence
Tower processed (9), ammonia circulating pump (10), ammonia liquor separator (11), desulfurization adsorption tower (12), ammonia condenser (15) and liquid ammonia storage tank
(17), the described top exit of thick ammonia separatory tank (8) is connected with the centre entrance of ammonia refining tower (9), described thick ammonia separatory tank (8)
Outlet at bottom be connected with raw material Water Tank (1), the top exit of described ammonia refining tower (9) and the entrance of ammonia liquor separator (11)
Being connected, the top exit of described ammonia liquor separator (11) is connected with the bottom inlet of desulfurization adsorption tower (12), and described ammoniacal liquor separates
The outlet at bottom of device (11) is connected with raw material Water Tank (1), the top exit of described desulfurization adsorption tower (12) and ammonia condenser
(15) the first entrance is connected, and the first outlet of described ammonia condenser (15) is connected with the outlet of liquid ammonia storage tank (17)；Described cigarette
Gas denitrification apparatus include liquefied ammonia delivery pump (18), liquid ammonia evaporator (19), ammonia/air mixer (20), dilution air (21),
The entrance of ammonia injection grid (22) and Benitration reactor (23), the outlet of described liquid ammonia storage tank (17) and liquefied ammonia delivery pump (18)
Being connected, the outlet of described liquefied ammonia delivery pump (18) is connected with the entrance of liquid ammonia evaporator (19), described liquid ammonia evaporator (19)
Outlet is connected with the first entrance of ammonia/air mixer (20), and the outlet of described dilution air (21) mixes with ammonia/air
Second entrance of device (20) is connected, and the outlet of described ammonia/air mixer (20) enters with the first of ammonia injection grid (22)
Mouth is connected, and the second entrance of described ammonia injection grid (22) is connected with boiler exit gas mouth, described ammonia injection grid (22)
Outlet is connected with the entrance of Benitration reactor (23)；Described flue gas desulfurization device include air preheater (24), ammonia water tank (25),
Aqua ammonia pump (26), circulating pump (27), desulfurizing tower (28) and oxidation fan (29), the outlet of described Benitration reactor (23) and air
First entrance of preheater (24) is connected, the first outlet of described air preheater (24) and the first entrance phase of desulfurizing tower (28)
Even.First entrance of described ammonia water tank (25) is connected with the outlet line of liquid ammonia evaporator (19), the of described ammonia water tank (25)
Two entrances are connected with demineralized water pipeline, and the outlet of described ammonia water tank (25) is connected with the entrance of aqua ammonia pump (26), described circulating pump
(27) entrance is connected with the first outlet of desulfurizing tower (28), and the outlet line of described circulating pump (27) is first and aqua ammonia pump (26)
Outlet line converges, and is then divided into three branch roads, three branch roads to be connected into desulfurizing tower (28), the outlet of described oxidation fan (29) with
Second entrance of desulfurizing tower (28) is connected.
The device that a kind of aromatic hydrocarbons the most according to claim 1 cleaning produces, it is characterised in that: also include that ammonia repurity fills
Putting, described ammonia repurity device includes ammonia compressor (13), ammonia separator (14) and liquefied ammonia bleacher (16), described ammonia compressor (13)
With ammonia separator (14) is arranged between desulfurization adsorption tower (12) and ammonia condenser (15), the top of described desulfurization adsorption tower (12)
Outlet is first connected with the entrance of ammonia compressor (13), and the outlet of described ammonia compressor (13) is connected with the entrance of ammonia separator (14), institute
The outlet at bottom stating ammonia separator (14) is connected with slop tank, the top exit of described ammonia separator (14) and ammonia condenser (15)
The first entrance be connected, described liquefied ammonia bleacher (16) is located between ammonia condenser (15) and liquid ammonia storage tank (17), and described ammonia is cold
First outlet of condenser (15) is first connected with the bottom inlet of liquefied ammonia bleacher (16), and the top of described liquefied ammonia bleacher (16) goes out
Mouth is connected with the import of liquid ammonia storage tank (17).
The device that a kind of aromatic hydrocarbons the most according to claim 1 cleaning produces, it is characterised in that: described stripping tower top separatory tank
(5) hydrogen sulfide tail gas of top exit is divided into two-way, and sulphur recovery is gone on a road, and another road is admitted to boiler combustion system combustion
Burn.
4. the device produced is cleaned according to a kind of aromatic hydrocarbons described in any one of claim 1-3, it is characterised in that: described liquefied ammonia is defeated
The outlet sending pump (18) is divided into two-way, and liquid ammonia evaporator (19) is removed on a road, another road deammoniation treating column (9).
5. the method that an aromatic hydrocarbons cleaning produces, it is characterised in that: comprise the following steps:
A, by sewage in raw material Water Tank (1) through feed pump (2) send into stripper (3), described stripper (3) use 1.0MPa steam
Vapour heats, and tower top material enters stripping tower top cooler (4) cooling, enters stripping tower top separatory tank (5), from stripping tower top
Separatory tank (5) hydrogen sulphide in the vapor phase out is sent into boiler combustion or goes sulfur recycle section Recovered sulphur, and it is dirty that liquid phase returns raw material
Water pot (1)；The 150-160 DEG C of thick ammonia of gas phase is derived at described stripper (3) middle part, and the thick ammonia of gas phase is cold through thick ammonia condenser (7)
After Ning, entering thick ammonia separatory tank (8) separatory, the liquefied ammonia that and liquefied ammonia delivery pump (18) out rear from thick ammonia separatory tank (8) exports mixes
Ammonia refining tower (9) is entered after conjunction；Return upstream device after purification water cooling after the stripping of described stripper (3) bottom and reclaim profit
With；
B, liquefied ammonia and thick ammonia are mixed into ammonia refining tower (9), and ammoniacal liquor at the bottom of tower is delivered to top of tower through ammonia circulating pump (10) and carried out
Wash cycles, the hydrogen sulfide in removing ammonia, ammonia water containing sulfur drains into raw material Water Tank (1) from interruption at the bottom of tower, and ammonia enters from tower top
Enter ammonia liquor separator (11)；The sewage that described ammonia liquor separator (11) outlet at bottom is discharged returns raw material Water Tank (1), described ammonia
The gas-phase product of liquid/gas separator (11) top exit enters desulfurization adsorption tower (12) and carries out desulfurization process, and the ammonia after desulfurization is sent into
Ammonia compressor (13)；
Ammonia after c, desulfurization sends into ammonia compressor (13) supercharging, and described ammonia compressor (13) outlet pressure 1.2-1.5MPa, after supercharging
Ammonia enter ammonia separator (14) and separate the oil phase of liquefaction, the ammonia of gas phase liquefies after ammonia condenser (15) condenses, liquefied ammonia
Send into liquefied ammonia bleacher (16) removing phenols and oils, subsequently into liquid ammonia storage tank (17)；
Liquefied ammonia in d, described liquid ammonia storage tank (17) sends into liquid ammonia evaporator (19) by liquid ammonia gasification, institute through liquefied ammonia delivery pump (18)
Stating liquid ammonia evaporator (19) outlet ammonia temperature 40-55 DEG C, pressure 0.3-0.5MPa, ammonia and air are according to volume ratio 1:100-
After 2:100 mixing, entrance ammonia injection grid (22) is full and uniform with the boiler smoke of sulfur-bearing nitride mixes, then gaseous mixture
Entering Benitration reactor (23) reaction and nitrogen oxides is reduced to nitrogen, denitration reaction temperature is 355-370 DEG C；
After e, denitration, boiler smoke is cooled further to 160-170 DEG C of entrance desulfurizing tower (28) through air preheater (24), de-
Sulfur tower (28) interior ammonia mixes with flue gas by the way of spray, is blasted air in the bottom of desulfurizing tower by oxidation fan (29),
Removing the sulfurous gas in boiler smoke under the effect of ammonia and air, desulfurizing tower (28) used ammonia is in ammonia water tank (25)
In be to be mixed with by ammonia and demineralized water, then in aqua ammonia pump (26) injects desulfurizing tower (28).
The method that a kind of aromatic hydrocarbons the most according to claim 5 cleaning produces, it is characterised in that: described stripper (3) tower top
Temperature 40-60 DEG C, pressure 0.5-0.8MPa, column bottom temperature 150-175 DEG C, pressure 0.4-0.55MPa.
The method that a kind of aromatic hydrocarbons the most according to claim 6 cleaning produces, it is characterised in that: described ammonia refining tower (9)
Operation temperature maintains-10～0 DEG C.
8. the method produced is cleaned according to a kind of aromatic hydrocarbons described in any one of claim 5-7, it is characterised in that: described liquefied ammonia takes off
In color tank (16), decolorizing adsorbent is activated carbon.
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| CN201610788615.4A CN106277145A (en) | 2016-08-30 | 2016-08-30 | The apparatus and method that a kind of aromatic hydrocarbons cleaning produces |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108970353A (en) * | 2018-07-16 | 2018-12-11 | 西安华大骄阳绿色科技有限公司 | A kind of synthesis desulfurating method of denitration being catalyzed flue gas and the sour gas containing ammonia |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH08192029A (en) * | 1995-01-13 | 1996-07-30 | Nippon Kankyo Asesumento Center:Kk | Denitrifying and desulfurizing method and device therefor |
| CN1145877A (en) * | 1995-09-18 | 1997-03-26 | 宗立海 | Process for recovering high purity liquid ammonia from oil-refining waste water |
| CN1587045A (en) * | 2004-08-16 | 2005-03-02 | 中国石油化工集团公司 | Ammonia refining combined process |
| US20140056777A1 (en) * | 2009-10-22 | 2014-02-27 | Mitsubishi Heavy Industries, Ltd. | Ammonia recovery device and recovery method |
| CN205145971U (en) * | 2015-11-13 | 2016-04-13 | 西南化工研究设计院有限公司 | Coke oven flue gas desulfurization denitration dust removal integration system |
-
2016
- 2016-08-30 CN CN201610788615.4A patent/CN106277145A/en active Pending
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH08192029A (en) * | 1995-01-13 | 1996-07-30 | Nippon Kankyo Asesumento Center:Kk | Denitrifying and desulfurizing method and device therefor |
| CN1145877A (en) * | 1995-09-18 | 1997-03-26 | 宗立海 | Process for recovering high purity liquid ammonia from oil-refining waste water |
| CN1587045A (en) * | 2004-08-16 | 2005-03-02 | 中国石油化工集团公司 | Ammonia refining combined process |
| US20140056777A1 (en) * | 2009-10-22 | 2014-02-27 | Mitsubishi Heavy Industries, Ltd. | Ammonia recovery device and recovery method |
| CN205145971U (en) * | 2015-11-13 | 2016-04-13 | 西南化工研究设计院有限公司 | Coke oven flue gas desulfurization denitration dust removal integration system |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108970353A (en) * | 2018-07-16 | 2018-12-11 | 西安华大骄阳绿色科技有限公司 | A kind of synthesis desulfurating method of denitration being catalyzed flue gas and the sour gas containing ammonia |
| CN108970353B (en) * | 2018-07-16 | 2021-04-30 | 西安华大骄阳绿色科技有限公司 | Comprehensive desulfurization and denitrification method for catalytic flue gas and ammonia-containing acid gas |
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