CN105413406A - Recycling system of ammonia gas in emptying tail gas and operation method therefor - Google Patents
Recycling system of ammonia gas in emptying tail gas and operation method therefor Download PDFInfo
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- CN105413406A CN105413406A CN201510987149.8A CN201510987149A CN105413406A CN 105413406 A CN105413406 A CN 105413406A CN 201510987149 A CN201510987149 A CN 201510987149A CN 105413406 A CN105413406 A CN 105413406A
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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
- B01D53/14—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 by absorption
- B01D53/18—Absorbing units; Liquid distributors therefor
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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
- C01C1/022—Preparation of aqueous ammonia solutions, i.e. ammonia water
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2252/00—Absorbents, i.e. solvents and liquid materials for gas absorption
- B01D2252/10—Inorganic absorbents
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/40—Nitrogen compounds
- B01D2257/406—Ammonia
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- Chemical Kinetics & Catalysis (AREA)
- Treating Waste Gases (AREA)
- Gas Separation By Absorption (AREA)
Abstract
The invention relates to a recycling system of ammonia gas in emptying tail gas and an operation method therefor. The system includes an ammonia gas absorption column, a dilute ammonia water trough, a dilute ammonia water pump, a desorption waste liquid trough, a desorption waste liquid pump, a vacuum jet pump, a first heat exchanger and a second heat exchanger. In the invention, desorption waste liquid in a production system and heat exchanging devices in the ammonia gas absorption column are fully utilized, so that the ammonia gas in the emptying tail gas is reversely contacted with and fully reacted with the desorption waste liquid in the ammonia gas absorption column to generate a product dilute ammonia water which is used for a chimney desulfurization system. Production work situation required in the process can be controlled well in the system, so that the ammonia gas in the emptying tail gas can be fully recycled, thereby reducing atmosphere pollutant emission. Meanwhile, the recycled dilute ammonia water can be used for the chimney desulfurization system. Unique process pipeline design reduces emission of waste gas and waste liquid when the production system is operated, thereby providing excellent technical support for environment-friendly production in enterprises.
Description
Technical field
The present invention relates to tail gas clean-up and gas ammonia discharge field, be specifically related to recovery system and the method for operating thereof of gas ammonia in a kind of emptying end gas.
Background technology
At present, China is as global maximum developing country, and the environmental problems such as its natural environment pollution, atmosphere pollution, noxious waste pollution have become the biggest problem that country nowadays faces.In enterprise production system emission in gas ammonia be in atmosphere pollution, affect larger gaseous contaminant, great damaging effect is had to human body, environment and the ecosystem, along with the increasingly stringent of environmental requirement, the discharge of gas ammonia, more and more receive the concern of people, therefore there are strict regulation and restriction in country to the ammonia nitrogen in emptying end gas and in waste liquid.Especially a large amount of gas ammonias is contained in the emptying of carbamide production system tail gas, both polluted environment, turn increased consumption, due to the increasingly stringent of environmental requirement, emission problem as gas ammonia in tail gas can not be resolved, and the existence of manufacturing enterprise will be faced with formidable challenges.
Summary of the invention
The technical problem to be solved in the present invention is the recovery system and the method for operating thereof that provide gas ammonia in a kind of tail gas, device technique flow process is simple, operating cost is cheap, the effective gas ammonia reclaimed in emptying end gas, decrease the pollution of environment, also can obtain product weak aqua ammonia for chimney desulphurization system.
The present invention designs and adopts following scheme for this reason:
A recovery system for gas ammonia in emptying end gas, comprises gas ammonia absorption tower, weak aqua ammonia groove, weak aqua ammonia pump, decomposition of effluent groove, decomposition of effluent pump, vacuum jet pump, First Heat Exchanger, the second heat exchanger; The gaseous phase outlet of described second heat exchanger is connected with the bottom on gas ammonia absorption tower, the gas phase import of the second heat exchanger is connected with exhaust pipe, the bottom of the gentle ammonia absorber of described second heat exchanger connects lower liquid pipe respectively, described lower liquid pipe is deeply to the bottom of weak aqua ammonia groove, the vacuum inlet feeds of described vacuum jet pump is connected with the gas phase mouth at top, gas ammonia absorption tower, the diffusion mouth of pipe of vacuum jet pump is communicated with weak aqua ammonia groove upper end, and the outlet at bottom of described weak aqua ammonia groove is connected with the import of weak aqua ammonia pump;
Described weak aqua ammonia delivery side of pump is divided into three tunnels, and the 4th stop valve of leading up to is connected with vacuum jet pump, and the 3rd stop valve of leading up to is connected with the spray equipment on top, gas ammonia absorption tower, and the second control valve of leading up to is connected with chimney desulphurization system; The outlet of described decomposition of effluent trench bottom is connected with decomposition of effluent pump inlet; Described decomposition of effluent delivery side of pump is divided into three tunnels, and the second stop valve of leading up to is connected with vacuum jet pump, and the first stop valve of leading up to is connected with the spray equipment on top, gas ammonia absorption tower, and the first control valve of leading up to is connected with Waste Water Treatment; The described import of decomposition of effluent groove is connected with the outlet of First Heat Exchanger, and the import of described First Heat Exchanger is connected with decomposition of effluent pipe.
Further, described gas ammonia absorption tower is packed absorber, and its inside is provided with the first spray equipment, the second spray equipment, distributor and heat exchanging pipe from top to bottom successively; Described weak aqua ammonia delivery side of pump is connected with second spray equipment on top, gas ammonia absorption tower by the 3rd stop valve, and described decomposition of effluent delivery side of pump is connected with first spray equipment on top, gas ammonia absorption tower by the first stop valve.
Further, described weak aqua ammonia groove upper top is provided with the exhaust purifier for reclaiming weak aqua ammonia groove volatilization gas ammonia, and the inlet of described exhaust purifier is connected with weak aqua ammonia delivery side of pump by the 5th stop valve.
Further, the circulating water intake place of described First Heat Exchanger, the second heat exchanger and heat exchanging pipe is equipped with import water control valve.
A method of operating for the recovery system of gas ammonia in emptying end gas, comprises the following steps:
1) urea decomposition of effluent is delivered to First Heat Exchanger by decomposition of effluent pipe, decomposition of effluent groove is delivered to after First Heat Exchanger cooling, start decomposition of effluent pump, decomposition of effluent delivers to Waste Water Treatment by the first control valve, by the decomposition of effluent liquid level in the first governor valve control decomposition of effluent groove;
2) emptying end gas to be cooled the temperature reached needed for production technology by the second heat exchanger, by vacuum jet pump, the tail gas after cooling is sucked from the bottom on gas ammonia absorption tower, the pressure in gas ammonia absorption tower is controlled by the second stop valve, and the decomposition of effluent that can absorb gas ammonia in tail gas is delivered to first spray equipment on top, gas ammonia absorption tower by the first stop valve, spray downwards under the effect of the first spray equipment, gas ammonia in tail gas and cooled decomposition of effluent counter current contacting generation gas-liquid two-phase react, generate dilute ammonia solution, dilute ammonia solution enters weak aqua ammonia groove at the flows by action of potential difference,
3) when the liquid level in weak aqua ammonia groove reaches the 20%-30% of weak aqua ammonia groove volume, start weak aqua ammonia pump, the pressure in gas ammonia absorption tower is controlled by the 4th stop valve, and by the 3rd stop valve, the dilute ammonia solution in weak aqua ammonia groove is delivered to second spray equipment on top, gas ammonia absorption tower, weak aqua ammonia sprays downwards under the effect of the second spray equipment, weak aqua ammonia enters in heat exchanging pipe uniformly through distributor and cools, reverse absorption reaction is there is together in the decomposition of effluent sprayed into the first spray equipment with the gas ammonia in the tail gas entered in gas ammonia absorption tower, the weak aqua ammonia absorbed after gas ammonia flows into into weak aqua ammonia groove again,
4) after the liquid level in weak aqua ammonia groove reaches the 50%-70% of weak aqua ammonia groove volume, close the first stop valve and the second stop valve and stop injecting decomposition of effluent to gas ammonia absorption tower; By the second control valve, weak aqua ammonia is delivered to chimney desulphurization system when the weak aqua ammonia concentration of weak aqua ammonia groove reaches the concentration needed for chimney desulphurization system, after the liquid level in weak aqua ammonia groove is down to the 10%-20% of weak aqua ammonia groove volume, again open the first stop valve to the fluid infusion of weak aqua ammonia groove;
5) above-mentioned 1 is cycled to repeat)-4) step.
Beneficial effect of the present invention is:
The present invention applies in a flexible way the decomposition of effluent in production system and the heat-exchanger rig in gas ammonia absorption tower, make in gas ammonia absorption tower the gas ammonia in emptying end gas and decomposition of effluent reverse contact fully to react generate product weak aqua ammonia, for chimney desulphurization system; Present system can be good the production status required by this technique of control, the gas ammonia in emptying end gas is made to obtain sufficient recovery, decrease the discharge of Pollution Gas, reclaim the weak aqua ammonia obtained simultaneously and can also be used for chimney desulfurization, unique process pipelines design, decrease the discharge of waste gas and waste liquid when production system is run, produce for environmental protection of enterprise and provide good technical support.
Accompanying drawing explanation
Be described further with regard to the specific embodiment of the present invention below in conjunction with accompanying drawing, wherein:
Fig. 1 is process equipment flow chart of the present invention.
Detailed description of the invention
With reference to the recovery system of gas ammonia in a kind of emptying end gas shown in Fig. 1, comprise gas ammonia absorption tower 2, weak aqua ammonia groove 6, weak aqua ammonia pump 11, decomposition of effluent groove 13, decomposition of effluent pump 12, vacuum jet pump 8, First Heat Exchanger 14, second heat exchanger 1; The gaseous phase outlet of described second heat exchanger 1 is connected with the bottom on gas ammonia absorption tower 2, the gas phase import of the second heat exchanger 1 is connected with exhaust pipe, the bottom of the gentle ammonia absorber of described second heat exchanger 12 connects lower liquid pipe 21 respectively, described lower liquid pipe 21 is deeply to the bottom of weak aqua ammonia groove 6, the vacuum inlet feeds of described vacuum jet pump 8 is connected with the gas phase mouth at top, gas ammonia absorption tower 2, the diffusion mouth of pipe of vacuum jet pump 8 is communicated with weak aqua ammonia groove 6 upper end, and the outlet at bottom of described weak aqua ammonia groove 6 is connected with the import of weak aqua ammonia pump 11.
The outlet of described weak aqua ammonia pump 11 is divided into three tunnels, the 4th stop valve 19 of leading up to is connected with vacuum jet pump 8, the 3rd stop valve 17 of leading up to is connected with second spray equipment 4 on top, gas ammonia absorption tower 2, and the second control valve 15 of leading up to is connected with chimney desulphurization system.
Outlet bottom described decomposition of effluent groove 13 is connected with decomposition of effluent pump 12 import; The outlet of described decomposition of effluent pump 12 is divided into three tunnels, second stop valve 20 of leading up to is connected with vacuum jet pump 8, first stop valve 18 of leading up to is connected with first spray equipment 3 on top, gas ammonia absorption tower 2, and the first control valve 16 of leading up to is connected with Waste Water Treatment.
The import of described decomposition of effluent groove 13 is connected with the outlet of First Heat Exchanger 14, and the import of described First Heat Exchanger 14 is connected with decomposition of effluent pipe.
Described vacuum jet pump 8 is for controlling the pressure in gas ammonia absorption tower 2, weak aqua ammonia and decomposition of effluent is aspirated to weak aqua ammonia groove by the 4th stop valve 19 and the second stop valve 20, react in tail gas inhaling air ammonia absorber 2 in vacuum orifice, control the pressure on whole gas ammonia absorption tower 2 between-20kpa ~-30kpa.
Described gas ammonia absorption tower 2 is packed absorber, and its inside is provided with the first spray equipment 3, second spray equipment 4, distributor 7 and heat exchanging pipe 5 from top to bottom successively; The circulating water intake place of described First Heat Exchanger 14, second heat exchanger 1 and heat exchanging pipe 5 is respectively equipped with import water control valve 23,9,10, the quantity of circulating water regulated by import water control valve 23,9,10 controls the reaction temperature in gas ammonia absorption tower 2, and the reaction temperature in gas ammonia absorption tower 2 is controlled between 40-50 DEG C.
Described weak aqua ammonia groove 6 upper top is provided with exhaust purifier 21, and the inlet of described exhaust purifier 21 is connected with the outlet of weak aqua ammonia pump 11 by the 5th stop valve 22; Exhaust purifier 21 absorbs the gas ammonia of the volatilization made in weak aqua ammonia groove 6, and is recycled in weak aqua ammonia groove 6 by weak aqua ammonia recoil.
System operation methods of the present invention, comprises the following steps:
1) urea decomposition of effluent is delivered to First Heat Exchanger 14 by decomposition of effluent pipe, decomposition of effluent groove 13 is delivered to after First Heat Exchanger 14 cools, start decomposition of effluent pump 12, decomposition of effluent delivers to Waste Water Treatment by the first control valve 16, is controlled the decomposition of effluent liquid level in decomposition of effluent groove 13 by the first control valve 16.
2) emptying end gas to be cooled the temperature reached needed for production technology by the second heat exchanger 1, by vacuum jet pump 8, the tail gas after cooling is sucked from the bottom on gas ammonia absorption tower 2, the pressure in gas ammonia absorption tower 2 is controlled by the second stop valve 20, and the decomposition of effluent that can absorb gas ammonia in tail gas is delivered to first spray equipment 3 on top, gas ammonia absorption tower 2 by the first stop valve 18, spray downwards under the effect of the first spray equipment 3, gas ammonia in tail gas and cooled decomposition of effluent counter current contacting generation gas-liquid two-phase react, generate dilute ammonia solution, dilute ammonia solution enters weak aqua ammonia groove 6 at the flows by action of potential difference.
3) when the liquid level in weak aqua ammonia groove 6 reaches the 20%-30% of weak aqua ammonia groove 6 volume, start weak aqua ammonia pump 11, the pressure in gas ammonia absorption tower 2 is controlled by the 4th stop valve 19, and by the 3rd stop valve 17, the dilute ammonia solution in weak aqua ammonia groove is delivered to second spray equipment 4 on top, gas ammonia absorption tower 2, weak aqua ammonia sprays downwards under the effect of the second spray equipment 4, weak aqua ammonia enters uniformly in heat exchanging pipe 5 through distributor 7 and cools, reverse absorption reaction is there is together in the decomposition of effluent sprayed into the first spray equipment 3 with the gas ammonia in the tail gas entered in gas ammonia absorption tower 2, the weak aqua ammonia absorbed after gas ammonia flows into again into weak aqua ammonia groove 6.
4) after the liquid level in weak aqua ammonia groove 6 reaches the 50%-70% of weak aqua ammonia groove 6 volume, the first stop valve 18 is closed and the second stop valve 20 stops injecting decomposition of effluent to gas ammonia absorption tower 2; By the second control valve 15, weak aqua ammonia is delivered to chimney desulphurization system when the weak aqua ammonia concentration of weak aqua ammonia groove 6 reaches the concentration needed for chimney desulphurization system, after the liquid level in weak aqua ammonia groove 6 is down to the 10%-20% of weak aqua ammonia groove 6 volume, again open the first stop valve 18 to weak aqua ammonia groove 6 fluid infusion.
5) above-mentioned 1 is cycled to repeat)-4) step.
The above; be only the better detailed description of the invention of the present invention, but scope is not limited thereto, is anyly familiar with those skilled in the art in the technical scope that the present invention discloses; the change that can expect easily or replacement, all should be encompassed within protection scope of the present invention.Therefore scope is as the criterion with the protection domain of claims.
Claims (5)
1. the recovery system of gas ammonia in emptying end gas, is characterized in that, comprise gas ammonia absorption tower, weak aqua ammonia groove, weak aqua ammonia pump, decomposition of effluent groove, decomposition of effluent pump, vacuum jet pump, First Heat Exchanger, the second heat exchanger; The gaseous phase outlet of described second heat exchanger is connected with the bottom on gas ammonia absorption tower, the gas phase import of the second heat exchanger is connected with exhaust pipe, the bottom of the gentle ammonia absorber of described second heat exchanger connects lower liquid pipe respectively, described lower liquid pipe is deeply to the bottom of weak aqua ammonia groove, the vacuum inlet feeds of described vacuum jet pump is connected with the gas phase mouth at top, gas ammonia absorption tower, the diffusion mouth of pipe of vacuum jet pump is communicated with weak aqua ammonia groove upper end, and the outlet at bottom of described weak aqua ammonia groove is connected with the import of weak aqua ammonia pump;
Described weak aqua ammonia delivery side of pump is divided into three tunnels, and the 4th stop valve of leading up to is connected with vacuum jet pump, and the 3rd stop valve of leading up to is connected with the spray equipment on top, gas ammonia absorption tower, and the second control valve of leading up to is connected with chimney desulphurization system; The outlet of described decomposition of effluent trench bottom is connected with decomposition of effluent pump inlet; Described decomposition of effluent delivery side of pump is divided into three tunnels, and the second stop valve of leading up to is connected with vacuum jet pump, and the first stop valve of leading up to is connected with the spray equipment on top, gas ammonia absorption tower, and the first control valve of leading up to is connected with Waste Water Treatment; The described import of decomposition of effluent groove is connected with the outlet of First Heat Exchanger, and the import of described First Heat Exchanger is connected with decomposition of effluent pipe.
2. the recovery system of gas ammonia in a kind of emptying end gas according to claim 1, it is characterized in that, described gas ammonia absorption tower is packed absorber, and its inside is provided with the first spray equipment, the second spray equipment, distributor and heat exchanging pipe from top to bottom successively; Described weak aqua ammonia delivery side of pump is connected with second spray equipment on top, gas ammonia absorption tower by the 3rd stop valve, and described decomposition of effluent delivery side of pump is connected with first spray equipment on top, gas ammonia absorption tower by the first stop valve.
3. the recovery system of gas ammonia in a kind of emptying end gas according to claim 1, it is characterized in that, described weak aqua ammonia groove upper top is provided with the exhaust purifier for reclaiming weak aqua ammonia groove volatilization gas ammonia, and the inlet of described exhaust purifier is connected with weak aqua ammonia delivery side of pump by the 5th stop valve.
4. the recovery system of gas ammonia in a kind of emptying end gas according to claim 2, it is characterized in that, the circulating water intake place of described First Heat Exchanger, the second heat exchanger and heat exchanging pipe is equipped with import water control valve.
5. the method for operating of the recovery system of gas ammonia in a kind of emptying end gas according to claim 1-4, is characterized in that, comprise the following steps:
1) urea decomposition of effluent is delivered to First Heat Exchanger by decomposition of effluent pipe, decomposition of effluent groove is delivered to after First Heat Exchanger cooling, start decomposition of effluent pump, decomposition of effluent delivers to Waste Water Treatment by the first control valve, by the decomposition of effluent liquid level in the first governor valve control decomposition of effluent groove;
2) emptying end gas to be cooled the temperature reached needed for production technology by the second heat exchanger, by vacuum jet pump, the tail gas after cooling is sucked from the bottom on gas ammonia absorption tower, the pressure in gas ammonia absorption tower is controlled by the second stop valve, and the decomposition of effluent that can absorb gas ammonia in tail gas is delivered to first spray equipment on top, gas ammonia absorption tower by the first stop valve, spray downwards under the effect of the first spray equipment, gas ammonia in tail gas and cooled decomposition of effluent counter current contacting generation gas-liquid two-phase react, generate dilute ammonia solution, dilute ammonia solution enters weak aqua ammonia groove at the flows by action of potential difference,
3) when the liquid level in weak aqua ammonia groove reaches the 20%-30% of weak aqua ammonia groove volume, start weak aqua ammonia pump, the pressure in gas ammonia absorption tower is controlled by the 4th stop valve, and by the 3rd stop valve, the dilute ammonia solution in weak aqua ammonia groove is delivered to second spray equipment on top, gas ammonia absorption tower, weak aqua ammonia sprays downwards under the effect of the second spray equipment, weak aqua ammonia enters in heat exchanging pipe uniformly through distributor and cools, reverse absorption reaction is there is together in the decomposition of effluent sprayed into the first spray equipment with the gas ammonia in the tail gas entered in gas ammonia absorption tower, the weak aqua ammonia absorbed after gas ammonia flows into into weak aqua ammonia groove again,
4) after the liquid level in weak aqua ammonia groove reaches the 50%-70% of weak aqua ammonia groove volume, close the first stop valve and the second stop valve and stop injecting decomposition of effluent to gas ammonia absorption tower; By the second control valve, weak aqua ammonia is delivered to chimney desulphurization system when the weak aqua ammonia concentration of weak aqua ammonia groove reaches the concentration needed for chimney desulphurization system, after the liquid level in weak aqua ammonia groove is down to the 10%-20% of weak aqua ammonia groove volume, again open the first stop valve to the fluid infusion of weak aqua ammonia groove;
5) above-mentioned 1 is cycled to repeat)-4) step.
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Cited By (7)
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| CN107555448A (en) * | 2017-08-23 | 2018-01-09 | 江苏安顺新材料科技有限公司 | The method for preparing high concentration ammoniacal liquor using tail gas caused by glycine is produced |
| CN109589753A (en) * | 2018-11-25 | 2019-04-09 | 鲁西化工集团股份有限公司 | A kind for the treatment of process of the ammonium fluid in urea absorption system |
| CN110026405A (en) * | 2019-04-04 | 2019-07-19 | 北京卫星制造厂有限公司 | A kind of waste gas and waste liquid reclaimer based on recoverable airship solar heat protection formed product |
| CN111214928A (en) * | 2018-11-26 | 2020-06-02 | 中国科学院大连化学物理研究所 | Factory waste gas treatment system containing ammonia gas |
| CN111991994A (en) * | 2020-08-18 | 2020-11-27 | 江苏华昌化工股份有限公司 | Treatment method for volatilizing ammonia gas |
| CN112678845A (en) * | 2020-12-19 | 2021-04-20 | 宁波四明化工有限公司 | Ammonia water synthesis process |
| CN113144871A (en) * | 2020-01-22 | 2021-07-23 | 福建省坤宁环保工程有限公司 | Dust removal desulfurizing tower |
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| CN112678845A (en) * | 2020-12-19 | 2021-04-20 | 宁波四明化工有限公司 | Ammonia water synthesis process |
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| CN105413406B (en) | 2017-10-24 |
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