CN106185986A - Phosphorus ammonium is washed ammonia and is produced oil removing slag removing system and the technique of anhydrous ammonia - Google Patents
Phosphorus ammonium is washed ammonia and is produced oil removing slag removing system and the technique of anhydrous ammonia Download PDFInfo
- Publication number
- CN106185986A CN106185986A CN201610515238.7A CN201610515238A CN106185986A CN 106185986 A CN106185986 A CN 106185986A CN 201610515238 A CN201610515238 A CN 201610515238A CN 106185986 A CN106185986 A CN 106185986A
- Authority
- CN
- China
- Prior art keywords
- ammonia
- rich solution
- oil
- light oil
- scummer
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
Classifications
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01C—AMMONIA; CYANOGEN; COMPOUNDS THEREOF
- C01C1/00—Ammonia; Compounds thereof
- C01C1/02—Preparation, purification or separation of ammonia
- C01C1/12—Separation of ammonia from gases and vapours
Abstract
The present invention provides a kind of phosphorus ammonium to wash ammonia and produces oil removing slag removing system and the technique of anhydrous ammonia, and phosphorus ammonium is washed the oil removing slag removing system of ammonia production anhydrous ammonia and included: rich solution is except light oil device, light oil separator, product ammonia grease trap and product anhydrous ammonia grease trap；Described rich solution is connected with ammonia absorber circulating pump or rich solution pump discharge except light oil device import, and described rich solution is connected with light oil separator import except light oil device top exit, and described rich solution is connected with poor rich liquid heat exchanger import except light oil device outlet at bottom；The outlet of described light oil separator light oil is connected with oil groove, and the outlet of described light oil separator rich solution is connected with ammonia absorber bottom；Described product ammonia grease trap import is connected with ammonia feeder trough；Described product anhydrous ammonia grease trap import exports with product and reflux pump and is connected.Phosphorus ammonium of the present invention is washed the oil removing slag removing system of ammonia production anhydrous ammonia and can effectively oil removing be removed the gred, environment friendly and pollution-free, is particularly well-suited to the ammonia separation field containing ammonia unstripped gas.
Description
Technical field
The present invention relates to oil removing slagging-off technology, particularly relate to a kind of phosphorus ammonium wash ammonia produce anhydrous ammonia oil removing slag removing system and
Technique.
Background technology
Phosphorus ammonium is washed ammonia and produced anhydrous ammonia technique is with the ammonia in phosphorus ammonium barren liquor washing absorption ammonia-containing gas, generates phosphorus ammonium rich
Liquid.Phosphorus ammonium pregnant liquor returns absorption cycle use through desorbing, the phosphorus ammonium barren liquor of regeneration, and ammonolysis sucks out formation ammonia simultaneously.Portion
Dividing ammonia product as the raw material of the ammonia process of desulfurization, remaining ammonia, again through rectification, obtains anhydrous ammonia product.Due to ammonia-containing gas
In possibly together with oil and the impurity such as slag (dust), as can not be well removed, stable operation and product quality will be affected.Invention
Patent " method for producing anhydrous ammonia by absorbing ammonium phosphate " (patent No. ZL 2,009 1 0068522.4) only proposes earthenware filter
Containing oil tech in removing rich solution.
Earthenware filter can separate the diameter oils more than pottery aperture, and diameter is less than oils and the slag in pottery aperture
Still stay in rich solution, eventually enter in product ammonia and product anhydrous ammonia.In addition earthenware filter need routine cleaning,
Produce a large amount of waste water (flushing water).
Summary of the invention
The purpose of invention is, washing ammonia for above-mentioned conventional phosphorus ammonium, to produce anhydrous ammonia oil removing measure imperfection, wastewater flow rate many
Problem, it is proposed that a kind of phosphorus ammonium is washed ammonia and is produced the oil removing slag removing system of anhydrous ammonia and technique, and this system and technique are removed effectively
Oil slagging-off, and environment friendly and pollution-free, it is particularly well-suited to the ammonia separation field containing ammonia unstripped gas.
For achieving the above object, the technical solution used in the present invention is: a kind of phosphorus ammonium is washed the oil removing of ammonia production anhydrous ammonia and removed
Slag system includes: rich solution is except light oil device, light oil separator, product ammonia grease trap and product anhydrous ammonia grease trap；
Rich solution is commercial equipment except light oil device, light oil separator, product ammonia grease trap and product anhydrous ammonia grease trap.
Wherein, rich solution uses cyclone separation process except light oil device, and light oil separator utilizes that rich solution is static with the density contrast of light oil to be separated, and produces
Product ammonia grease trap and product anhydrous ammonia grease trap use the materials such as NACF as adsorbent.
Described rich solution is connected with ammonia absorber circulating pump or rich solution pump discharge except light oil device import, and described rich solution removes light oil device
Top exit is connected with light oil separator import, and described rich solution is connected with poor rich liquid heat exchanger import except light oil device outlet at bottom；
The outlet of described light oil separator light oil is connected with oil groove, the outlet of described light oil separator rich solution and ammonia absorber bottom
Connect.
Described product ammonia grease trap import is connected with ammonia feeder trough, the thing that the outlet of described product ammonia grease trap is discharged
Material is the product ammonia of oil content 1～20ppm.
Described product anhydrous ammonia grease trap import exports with product and reflux pump and is connected, and described product anhydrous ammonia grease trap goes out
The product anhydrous ammonia that material is oil content 1～20ppm that mouth is discharged.
Further, described phosphorus ammonium wash ammonia produce anhydrous ammonia oil removing slag removing system include unstripped gas oil removing scummer, institute
State unstripped gas oil removing scummer import to be connected with unstripped gas pipeline, described unstripped gas oil removing scummer top exit and ammonia absorber
Connect；Being unstripped gas oil removing scummer slag-drip opening bottom described unstripped gas oil removing scummer, described unstripped gas oil removing scummer is arranged
Hydraulic fluid port is positioned at unstripped gas oil removing scummer slag-drip opening top.
Further, described phosphorus ammonium wash ammonia produce anhydrous ammonia oil removing slag removing system include that rich solution removes heavy oil scummer, institute
Stating rich solution and be connected with ammonia absorber circulating pump or rich solution pump discharge except heavy oil scummer import, described rich solution is except heavy oil scummer top
Portion's outlet is connected except light oil device import with rich solution, and described rich solution is except removing heavy oil scummer deslagging for rich solution bottom heavy oil scummer
Mouthful, described rich solution is positioned at rich solution except heavy oil scummer slag-drip opening top except heavy oil scummer re-scheduling hydraulic fluid port.
Further, described phosphorus ammonium wash ammonia produce anhydrous ammonia oil removing slag removing system include that rich solution removes heavy oil scummer, institute
State rich solution to be connected except heavy oil scummer import removes light oil device outlet at bottom with rich solution, described except rich solution heavy oil scummer top exit
Being connected with poor rich liquid heat exchanger import, described rich solution is except removing heavy oil scummer slag-drip opening for rich solution bottom heavy oil scummer, described
Rich solution is positioned at rich solution except heavy oil scummer slag-drip opening top except heavy oil scummer re-scheduling hydraulic fluid port.
Another object of the present invention additionally provide a kind of phosphorus ammonium with oil removing slag removing function wash ammonia produce anhydrous ammonia system
System, it includes that above-mentioned phosphorus ammonium is washed ammonia and produced the oil removing slag removing system of anhydrous ammonia.
Another object of the present invention additionally provides a kind of phosphorus ammonium and washes the oil removing deslagging process of ammonia production anhydrous ammonia, including such as
Lower step:
Rich solution from ammonia absorber enters rich solution except light oil device, the light oil (85～95wt%) in rich solution, trace heavy oil
And slag is separated in rich solution is except light oil device；
The rich solution that rich solution is discharged except light oil device top exit enters light oil separator, light oil separator for further separation rich solution
In light oil, by light oil separate after rich solution return ammonia absorber；
Residue in the trace amount (30～300ppm) in ammonia and anhydrous ammonia, respectively product ammonia grease trap and product without
Water ammonia grease trap is adsorbed be removed to 1～20ppm.In the case of above-mentioned steps is generally used for not having heavy oil and slag.
Further, phosphorus ammonium is washed ammonia and is produced the oil removing deslagging process of anhydrous ammonia, comprises the steps:
Rich solution from ammonia absorber enters rich solution and removes heavy oil scummer, and heavy oil (90～96wt%) and slag in rich solution exist
Rich solution is except being separated in heavy oil scummer；
Rich solution enters rich solution except light oil device from rich solution except heavy oil scummer top exit, light oil in rich solution (85～
95wt%), residual heavy oil and slag are separated in rich solution is except light oil device；
The rich solution that rich solution is discharged except light oil device top exit enters light oil separator, light oil separator for further separation rich solution
In light oil, by light oil separate after rich solution return ammonia absorber；
Residue in 30 in ammonia and anhydrous ammonia～300ppm oil, remove at product ammonia grease trap and product anhydrous ammonia respectively
Oil device is adsorbed is removed to 1～20ppm.
Further, phosphorus ammonium is washed ammonia and is produced the oil removing deslagging process of anhydrous ammonia, comprises the steps:
90～95wt% oil droplets and slag in unstripped gas are separated in unstripped gas oil removing scummer；
Rich solution from ammonia absorber enters rich solution except light oil device, and 85～95% light oil in rich solution, trace heavy oil (are less than
Equal to 0.5wt%) and slag at rich solution except light oil device is separated；
The rich solution that rich solution is discharged except light oil device top exit enters light oil separator, and the rich solution after being separated by light oil returns ammonia
Absorption tower；
The rich solution that rich solution is discharged except light oil device outlet at bottom enters except heavy oil scummer, 90～96wt% heavy oil in rich solution
Separated except heavy oil scummer at rich solution with slag；
Residue in 30 in ammonia and anhydrous ammonia～300ppm oil, remove at product ammonia grease trap and product anhydrous ammonia respectively
Oil device is adsorbed being removed to 1～20ppm.
Further, phosphorus ammonium is washed ammonia and is produced the oil removing deslagging process of anhydrous ammonia, comprises the steps:
90～95wt% oil droplets and slag in unstripped gas are separated in unstripped gas oil removing scummer；When unstripped gas does not contains
When slag or dregginess are little, time such as less than equal to 0.5wt%, slag-drip opening and the oil drain out of unstripped gas oil removing scummer can merge
Become an outlet；This step can remove 90～95wt% oil droplet and slag in unstripped gas.
Separated in rich solution is except heavy oil scummer from 90 in the rich solution of ammonia absorber～96wt% heavy oil and slag；When
In rich solution, slag inclusion or dregginess be not little, and time such as less than equal to 0.5wt%, rich solution removes slag-drip opening and the oil drain out of heavy oil scummer
Can merge and become an outlet；This step can remove 90～96wt% heavy oil and slag in rich solution.
Rich solution removes light oil device from rich solution except heavy oil scummer top exit enters rich solution, and the light oil in rich solution removes light at rich solution
Oil device is separated；This step can remove 85～95wt% light oil in rich solution.
The rich solution that rich solution is discharged except light oil device top exit enters light oil separator, and the rich solution after being separated by light oil returns ammonia
Absorption tower；This step can will isolate the rich solution of 85～95wt% light oil, returns ammonia absorber.
Residue in 30 in ammonia and anhydrous ammonia～300ppm oil, remove at product ammonia grease trap and product anhydrous ammonia respectively
The adsorbed removing of oil device.This step can be the oil content adsorbing and removing in product ammonia and product anhydrous ammonia to below 20ppm.
Phosphorus ammonium of the present invention wash ammonia produce the oil removing deslagging process of anhydrous ammonia and system is simple, rationally, its craft science, effect
Good, have the following advantages compared with current art.
In conventional anhydrous ammonia technique, earthenware filter deoiling effect is limited, diameter less than pottery aperture oils and
Slag enters desorber with rich solution, and oils makes desorber operate pressure oscillation, unstable, and eventually enters into ammonia and anhydrous ammonia
In, cause product to contain innage, defective；Slag is accumulated in system, occluding device；Earthenware filter, when routine cleaning, produces
Raw a large amount of waste water (flushing water).
Phosphorus ammonium of the present invention is washed ammonia and is produced oil removing deslagging process and system, the adaptation to oil-containing slag inclusion unstripped gas of anhydrous ammonia
By force, according in unstripped gas containing light, heavy oil and the content situation of slag, take single and/or compound mode, finally product ammonia and
Oil content in product anhydrous ammonia is removed to below 20ppm, system and technique and runs continuously, it is not necessary to clean.
To sum up, phosphorus ammonium of the present invention wash ammonia produce the oil removing deslagging process of anhydrous ammonia and system respectively to unstripped gas, rich solution and
Product carries out oil removing slagging-off, uses progressive manner step by step, progressively clean for dregs of fat removing, stablizes the operation of desorbing and guarantees to produce
Quality, and the totally-enclosed environmental protection of system is good.
Accompanying drawing explanation
Fig. 1 is the connection diagram that embodiment 1 phosphorus ammonium washes that ammonia produces the oil removing slag removing system of anhydrous ammonia；
Fig. 2 is the connection diagram that embodiment 2 phosphorus ammonium washes that ammonia produces the oil removing slag removing system of anhydrous ammonia；
Fig. 3 is the connection diagram that embodiment 3 phosphorus ammonium washes that ammonia produces the oil removing slag removing system of anhydrous ammonia；
Fig. 4 is the connection diagram that embodiment 4 phosphorus ammonium washes that ammonia produces the oil removing slag removing system of anhydrous ammonia.
Wherein reference is respectively as follows:
1-ammonia absorber；2-desorber；3-rectifying column；4-unstripped gas oil removing scummer；5-rich solution removes heavy oil scummer；6-
Rich solution removes light oil device；7-light oil separator；8-product ammonia grease trap；9-product anhydrous ammonia grease trap；10-ammonia absorber circulates
Pump；11-poor rich liquid heat exchanger；12-deacidification device；13-desorber feed pump；14-desorber cooler (on)；15-desorber is but
Device (under)；16-ammonia feeder trough；17-rectifying column feed pump；18-rectifying column condenser；19-return tank；20-product and backflow
Pump；21-lean solution cooler；22-rich solution pump.
Detailed description of the invention
Below in conjunction with embodiment, the present invention is further described:
The present embodiment also discloses a kind of phosphorus ammonium and washes ammonia production anhydrous ammonia system, and this phosphorus ammonium is washed ammonia and produced anhydrous ammonia system
Connection figure is as it is shown in figure 1, include 1-ammonia absorber；2-desorber；3-rectifying column；10-ammonia absorber circulating pump；The lean rich solution of 11-
Heat exchanger；12-deacidification device；13-desorber feed pump；14-desorber cooler (on)；15-desorber but device (under)；16-ammonia
Water feeder trough；17-rectifying column feed pump；18-rectifying column condenser；19-return tank；20-product and reflux pump；21-lean solution is cold
But device；22-rich solution pump.
External from battery limit (BL) enter ammonia absorber 1 bottom containing ammonia coal gas (containing ammonia unstripped gas), spray with middle part respectively in tower
The phosphorus ammonium barren liquor that the circulation phosphorus ammonium pregnant liquor spilt and top are sprayed carries out counter current contacting.Coal gas (gas after deamination) ammonia after washing contains
Amount is at 100mg/m3Hereinafter, leave battery limit (BL) from ammonia absorber 1 top.Phosphorus ammonium pregnant liquor ammonia bottom ammonia absorber 1 absorbs
Tower circulating pump 10 is extracted out, and major part is delivered to circulation in the middle part of ammonia absorber 1 and sprayed coal gas, small part rich solution earthenware filter.
Rich solution after filtration enters deacidification device 12 after entering poor rich liquid heat exchanger 11, with phosphorus ammonium barren liquor heat exchange.Phosphorus ammonium pregnant liquor
Flashing off sour gas in deacidification device 12, sour gas goes to ammonia absorber 1 bottom.Phosphorus ammonium pregnant liquor is again with desorber feed pump 13
Pump to desorber cooler (on) enter desorber 2 top behind 14, with ammonia vapour heat exchange.Phosphorus ammonium pregnant liquor desorbs wherein in tower
Contained ammonia also makes it be regenerated.Desorber 2 bottom is passed through steam as heat source.
The ammonia vapour of desorber 2 top effusion respectively desorber cooler (on) 14 and desorbing tower cooler device (under) in 15, add
After hot phosphorus ammonium pregnant liquor and cooled water cooling, form ammonia and flow into ammonia feeder trough 16.
Desorber 2 end phosphorus ammonium barren liquor respectively in poor rich liquid heat exchanger 11 and lean solution cooler 21, heating phosphorus ammonium pregnant liquor and
After cooled water cooling, enter ammonia absorber 1 top and spray.
Ammonia rectifying column feed pump 17 in ammonia feeder trough 16 is pumped to rectifying column 3.Rectifying column 3 pushes up anhydrous ammonia gas
In rectifying column condenser 18, cooled water becomes liquid anhydrous ammonia inflow return tank 19.In return tank anhydrous ammonia product and return
Stream pump 20 is extracted out, and part is delivered to rectifying column 3 as backflow and pushed up, and part is sent outside battery limit (BL) as product.The waste water at rectifying column 3 end send
Outside battery limit (BL).Rectifying column bottom is passed through steam as heat source
Embodiment 1
Present embodiment discloses a kind of phosphorus ammonium and wash the oil removing slag removing system of ammonia production anhydrous ammonia, as shown in Figure 1: include raw material
Gas oil removing scummer 4, rich solution are except heavy oil scummer 5, rich solution are except light oil device 6, light oil separator 7, product ammonia grease trap 8 and product
Product anhydrous ammonia grease trap 9；
Described unstripped gas oil removing scummer 4 import is connected with unstripped gas pipeline, and described unstripped gas oil removing scummer 4 top goes out
Mouth is connected with ammonia absorber 1；It is unstripped gas oil removing scummer slag-drip opening bottom described unstripped gas oil removing scummer 4, described former
Material gas oil removing scummer 4 oil drain out is positioned at unstripped gas oil removing scummer slag-drip opening top；Described rich solution removes heavy oil scummer 5 and richness
Liquid is used in series except light oil device 6, and rich solution is preposition except heavy oil scummer 5, absorbs with ammonia except heavy oil scummer 5 import when described rich solution
Tower circulating-pump outlet connects, and described rich solution is connected except light oil device import with rich solution except heavy oil scummer 5 top exit, described rich solution
Except being slag-drip opening bottom heavy oil scummer 5, described rich solution is positioned at slag-drip opening top except heavy oil scummer 5 re-scheduling hydraulic fluid port；Described
Rich solution is connected except heavy oil scummer 5 top exit with rich solution except light oil device import, and described rich solution is except light oil device top exit is with light
Oil eliminator 7 import connects, and described rich solution is connected with poor rich liquid heat exchanger 11 import except light oil device 6 outlet at bottom；Described is light
Oil eliminator 7 import is connected except light oil device 6 outlet with rich solution, and the outlet of described light oil separator 7 light oil is connected with oil trap, described
The outlet of light oil separator 7 rich solution is connected with ammonia absorber bottom.Described product ammonia grease trap 8 import is with ammonia feeder trough 16 even
Connecing, described product ammonia grease trap 8 outlet material is the product ammonia that oil content is less than 10ppm.Described product anhydrous ammonia removes
Oil device 9 import exports with product and reflux pump 20 and is connected, and described product anhydrous ammonia grease trap 9 outlet material is that oil content is less than
The product ammonia of 2ppm.
The present embodiment also discloses a kind of phosphorus ammonium and washes ammonia production anhydrous ammonia system, and this system uses above-mentioned phosphorus ammonium to wash ammonia and produces
The oil removing slag removing system of anhydrous ammonia, this phosphorus ammonium is washed ammonia and is produced the connection figure of anhydrous ammonia system as it is shown in figure 1, include that 1-ammonia absorbs
Tower；2-desorber；3-rectifying column；4-unstripped gas oil removing scummer；5-rich solution removes heavy oil scummer；6-rich solution removes light oil device；7-
Light oil separator；8-product ammonia grease trap；9-product anhydrous ammonia grease trap；10-ammonia absorber circulating pump；11-is lean, and rich solution changes
Hot device；12-deacidification device；13-desorber feed pump；14-desorber cooler (on)；15-desorber but device (under)；16-ammonia
Feeder trough；17-rectifying column feed pump；18-rectifying column condenser；19-return tank；20-product and reflux pump；21-lean solution cools down
Device；22-rich solution pump.
Phosphorus ammonium of the present invention is washed ammonia and is produced oil removing deslagging process and the system of anhydrous ammonia, according to the oil-containing slag inclusion feelings of unstripped gas
Condition, uses the most progressive oil removing slagging-off mode, it is ensured that the oil content of product ammonia and anhydrous ammonia conforms to quality requirements, Er Qiehuan
Border protects.Phosphorus ammonium of the present invention is washed ammonia and is produced the oil removing deslagging process of anhydrous ammonia and system can be widely used for containing ammonia unstripped gas
Ammonia separation field.
Use phosphorus ammonium to wash ammonia by semi-coke coal gas to produce as a example by anhydrous ammonia, and combine Fig. 1 and the present embodiment phosphorus ammonium is washed ammonia produce
The oil removing slag removing system of anhydrous ammonia and technique illustrate.
From battery limit (BL) external containing ammonia less than or equal to 20g/m3, heavy oil drips less than or equal to 2g/m3, light oil drips less than or equal to 5g/
m3, slag is less than or equal to 2g/m3Coal gas (containing ammonia unstripped gas) enters unstripped gas oil removing scummer 4, and isolated slag is discharged from bottom,
Isolated oil is discharged from slag-drip opening top, and top ammon amount out is less than or equal to 20g/m3, heavy oil drips less than or equal to 0.2g/
m3, light oil drips less than or equal to 0.5g/m3, slag is less than or equal to 0.2g/m3Coal gas enter ammonia absorber 1 bottom, in tower respectively with in
Circulation phosphorus ammonium pregnant liquor and the phosphorus ammonium barren liquor of top sprinkling that portion sprays carry out counter current contacting.Coal gas (gas after deamination) after washing
Ammonia content is at 100mg/m3Hereinafter, leave battery limit (BL) from ammonia absorber 1 top.Phosphorus ammonium pregnant liquor ammonia bottom ammonia absorber 1
Absorption tower circulating pump 10 is extracted out, and major part is delivered to circulation in the middle part of ammonia absorber 1 and sprayed coal gas, and small part rich solution sends into rich solution except weight
Oil scummer 5.
Remove except heavy oil at rich solution less than or equal to 1g/l rich solution less than or equal to 5g/l, slag less than or equal to 1g/l, light oil containing heavy oil
Separating in slag device 5, isolated slag is discharged from bottom, and isolated heavy oil is discharged from slag-drip opening top, top rich solution out
Send into rich solution except light oil device 6.
At rich solution remove light less than or equal to 5g/l, slag less than or equal to 0.1g/l rich solution less than or equal to 0.1g/l, light oil containing heavy oil
Separating in oil device 6, bottom is discharged and is less than or equal to 0.1g/l, light oil less than or equal to 0.4g/l, slag less than or equal to 0.1g/l containing heavy oil
Rich solution enters deacidification device 12 after entering poor rich liquid heat exchanger 11, with phosphorus ammonium barren liquor heat exchange.Top rich solution out enters light oil and divides
From device 7.
Separating in light oil separator 7 less than or equal to 50g/l rich solution containing light oil, isolated light oil is delivered to outside battery limit (BL), rich
Liquid returns to ammonia absorber 1 bottom.
In deacidification device 12, flash off sour gas containing light oil less than or equal to 0.4g/l phosphorus ammonium pregnant liquor and (comprise 80～90wt%
Light oil), sour gas goes to ammonia absorber 1 bottom.Phosphorus ammonium pregnant liquor is pumped to desorber cooler with desorber feed pump 13 again
On () enter desorber 2 top behind 14, with ammonia vapour heat exchange.Phosphorus ammonium pregnant liquor desorbs ammonia contained therein in tower and makes it obtain
With regeneration.Desorber 2 bottom is passed through steam as heat source.
The ammonia vapour of desorber 2 top effusion respectively desorber cooler (on) 14 and desorbing tower cooler device (under) in 15, add
After hot phosphorus ammonium pregnant liquor and cooled water cooling, form ammonia and flow into ammonia feeder trough 16.
Desorber 2 end phosphorus ammonium barren liquor respectively in poor rich liquid heat exchanger 11 and lean solution cooler 21, heating phosphorus ammonium pregnant liquor and
After cooled water cooling, enter ammonia absorber 1 top and spray.
Partial ammonia water in ammonia feeder trough 16 enters product ammonia grease trap 8, and the oil content in ammonia is removed to
Deliver to outside battery limit (BL) after below 10ppm.
Remained ammonia rectifying column feed pump 17 in ammonia feeder trough 16 is pumped to rectifying column 3.Rectifying column 3 pushes up anhydrous ammonia
Gas cooled water in rectifying column condenser 18 becomes liquid anhydrous ammonia and flows into return tank 19.Anhydrous ammonia product in return tank
Extracting out with reflux pump 20, part is delivered to rectifying column 3 as backflow and is pushed up, and part sends into product anhydrous ammonia grease trap 9 as product.Essence
The waste water evaporating tower 3 end is delivered to outside battery limit (BL).Rectifying column bottom is passed through steam as heat source.
In product anhydrous ammonia grease trap 9, deliver to outside battery limit (BL) after the oil content in anhydrous ammonia is removed to below 2ppm.
To sum up, the present embodiment phosphorus ammonium wash ammonia produce anhydrous ammonia oil removing deslagging process comprise the following steps: to enter ammonia inhale
The unstripped gas receiving tower carries out first oil removing slagging-off, then carries out the rich solution absorbing ammonia, except heavy oil slagging-off with except light oil, finally dividing
Other product ammonia and product anhydrous ammonia are carried out oil removing.This system and the technique unstripped gas adaptability to various oil-containings and slag inclusion
By force, it is ensured that desorption operations is stable, and product ammonia and product anhydrous ammonia not oil-containing, the totally-enclosed environmental protection of system is good.
Embodiment 2:
Present embodiment discloses a kind of phosphorus ammonium and wash the oil removing slag removing system of ammonia production anhydrous ammonia, as shown in Figure 2: include raw material
Gas oil removing scummer 4, rich solution are except heavy oil scummer 5, rich solution are except light oil device 6, light oil separator 7, product ammonia grease trap 8 and product
Product anhydrous ammonia grease trap 9；
Described unstripped gas oil removing scummer 4 import is connected with unstripped gas pipeline, and described unstripped gas oil removing scummer 4 top goes out
Mouth is connected with ammonia absorber 1；It is unstripped gas oil removing scummer slag-drip opening bottom described unstripped gas oil removing scummer 4, described former
Material gas oil removing scummer 4 oil drain out is positioned at unstripped gas oil removing scummer slag-drip opening top；Described rich solution removes light oil device 6 top exit
Being connected with light oil separator 7 import, described rich solution is except light oil device 6 outlet at bottom with described rich solution except heavy oil scummer 5 import even
Connecing, described except rich solution heavy oil scummer 5 top exit is for being connected with poor rich liquid heat exchanger 11 import, described rich solution removes except heavy oil
It is positioned at rich solution except heavy oil except heavy oil scummer slag-drip opening, described rich solution except heavy oil scummer 5 re-scheduling hydraulic fluid port for rich solution bottom slag device 5
Scummer slag-drip opening top.Described light oil separator 7 import is connected except the outlet of light oil device with rich solution, described light oil separator 7
Light oil outlet is connected with oil trap, and the outlet of described light oil separator 7 rich solution is connected with ammonia absorber bottom.Described product ammonia removes
Oil device 8 import is connected with ammonia feeder trough 16, and described product ammonia grease trap 8 outlet material is the product that oil content is less than 5ppm
Product ammonia.Described product anhydrous ammonia grease trap 9 import exports with product and reflux pump 20 and is connected, described product anhydrous ammonia oil removing
Device 9 outlet material is the product ammonia that oil content is less than 1ppm.
As a example by coordinating phosphorus ammonium to wash ammonia production anhydrous ammonia containing ammonia, hydrogen sulfide, dregs of fat submarine discharge, and combine Fig. 2 to this reality
Execute example phosphorus ammonium to wash ammonia and produce the oil removing slag removing system of anhydrous ammonia and technique illustrates.
From battery limit (BL) external containing ammonia less than or equal to 1kg/m3, hydrogen sulfide is less than or equal to 2kg/m3, carbon dioxide is less than or equal to
2.6kg/m3, heavy oil drips less than or equal to 1g/m3, light oil drips less than or equal to 3g/m3, slag is less than or equal to 1g/m3Unstripped gas is (former containing ammonia
Material gas) enter unstripped gas oil removing scummer 4, isolated slag is discharged from bottom, and isolated oil is discharged from slag-drip opening top, top
Portion out containing ammonia less than or equal to 1kg/m3, hydrogen sulfide is less than or equal to 2kg/m3, carbon dioxide is less than or equal to 2.6kg/m3, heavy oil
Drip less than or equal to 0.1g/m3, light oil drips less than or equal to 0.2g/m3, slag is less than or equal to 0.1g/m3Coal gas enters ammonia absorber 1 time
Portion, the phosphorus ammonium barren liquor that the circulation phosphorus ammonium pregnant liquor sprayed with middle part respectively in tower and top are sprayed carries out counter current contacting.After washing
Tail gas (tail gas after deamination) ammonia content at 10g/m3Hereinafter, leave battery limit (BL) from ammonia absorber 1 top.Ammonia absorber 1 end
The phosphorus ammonium pregnant liquor ammonia absorber circulating pump 10 in portion is extracted out, and major part is delivered to circulation in the middle part of ammonia absorber 1 and sprayed coal gas, small part
Rich solution sends into rich solution except light oil device 6.
At rich solution remove light less than or equal to 3g/l, slag less than or equal to 0.8g/l rich solution less than or equal to 0.8g/l, light oil containing heavy oil
Separating in oil device 6, bottom is discharged rich solution entrance rich solution and is gone out heavy oil scummer 5.Top out containing heavy oil less than or equal to 0.01g/l,
Light oil enters light oil separator 7 less than or equal to 30g/l, slag less than or equal to 0.01g/l rich solution.
Remove at rich solution less than or equal to 0.8g/l rich solution less than or equal to 0.3g/l, slag less than or equal to 0.8g/l, light oil containing heavy oil
Separating in heavy oil scummer 5, isolated slag is discharged from bottom, and isolated heavy oil is discharged from slag-drip opening top, and top is out
Rich solution enter and enter deacidification device 12 after poor rich liquid heat exchanger 11, with phosphorus ammonium barren liquor heat exchange.
Separating in light oil separator 7 less than or equal to 30g/l rich solution containing light oil, isolated light oil and heavy oil and slag are delivered to
Outside battery limit (BL), rich solution returns to ammonia absorber 1 bottom.
Phosphorus ammonium pregnant liquor flashes off sour gas (comprising 80～90wt% light oil) in deacidification device 12, and sour gas deammoniation is inhaled
Receive tower 1 bottom.Phosphorus ammonium pregnant liquor again with desorber feed pump 13 pump to desorber cooler (on) enter behind 14, with ammonia vapour heat exchange
Desorber 2 top.Phosphorus ammonium pregnant liquor desorbs ammonia contained therein in tower and makes it be regenerated.Desorber 2 bottom is passed through
Steam is as heat source.
The ammonia vapour of desorber 2 top effusion respectively desorber cooler (on) 14 and desorbing tower cooler device (under) in 15, add
After hot phosphorus ammonium pregnant liquor and cooled water cooling, form ammonia and flow into ammonia feeder trough 16.
Desorber 2 end phosphorus ammonium barren liquor respectively in poor rich liquid heat exchanger 11 and lean solution cooler 21, heating phosphorus ammonium pregnant liquor and
After cooled water cooling, enter ammonia absorber 1 top and spray.
Partial ammonia water in ammonia feeder trough 16 enters product ammonia grease trap 8, and the oil content in ammonia is removed to
Deliver to outside battery limit (BL) after below 5ppm.
Remained ammonia rectifying column feed pump 17 in ammonia feeder trough 16 is pumped to rectifying column 3.Rectifying column 3 pushes up anhydrous ammonia
Gas cooled water in rectifying column condenser 18 becomes liquid anhydrous ammonia and flows into return tank 19.Anhydrous ammonia product in return tank
Extracting out with reflux pump 20, part is delivered to rectifying column 3 as backflow and is pushed up, and part sends into product anhydrous ammonia grease trap 9 as product.Essence
The waste water evaporating tower 3 end is delivered to outside battery limit (BL).Rectifying column bottom is passed through steam as heat source.
In product anhydrous ammonia grease trap 9, deliver to outside battery limit (BL) after the oil content in anhydrous ammonia is removed to below 1ppm.
Embodiment 3:
Present embodiment discloses a kind of phosphorus ammonium and wash the oil removing slag removing system of ammonia production anhydrous ammonia, as shown in Figure 3: include rich solution
Except heavy oil scummer 5, rich solution are except light oil device 6, light oil separator 7, product ammonia grease trap 8 and product anhydrous ammonia grease trap 9；
Described rich solution is used in series except heavy oil scummer 5 and rich solution remove light oil device 6, and rich solution is preposition except heavy oil scummer 5, when
Described rich solution is connected with ammonia absorber circulating-pump outlet except heavy oil scummer 5 import, and described rich solution goes out except heavy oil scummer 5 top
Mouth is connected except light oil device import with rich solution, and described rich solution is except being slag-drip opening bottom heavy oil scummer 5, and described rich solution removes the gred except heavy oil
Device 5 re-scheduling hydraulic fluid port is positioned at slag-drip opening top；Described rich solution is except light oil device import with rich solution except heavy oil scummer 5 top exit even
Connecing, described rich solution is connected with light oil separator 7 import except light oil device top exit, described rich solution remove light oil device 6 outlet at bottom and
Poor rich liquid heat exchanger 11 import connects；Described light oil separator 7 import is connected except light oil device 6 outlet with rich solution, described light oil
The outlet of separator 7 light oil is connected with oil trap, and the outlet of described light oil separator 7 rich solution is connected with ammonia absorber bottom.Described product
Product ammonia grease trap 8 import is connected with ammonia feeder trough 16, and described product ammonia grease trap 8 outlet material is that oil content is less than
The product ammonia of 2ppm.Described product anhydrous ammonia grease trap 9 import exports with product and reflux pump 20 and is connected, and described product is anhydrous
Ammonia grease trap 9 outlet material is the product ammonia that oil content is less than 2ppm.
Use phosphorus ammonium to wash ammonia by coke gas to produce as a example by anhydrous ammonia, and combine Fig. 3 and the present embodiment phosphorus ammonium is washed ammonia produce
The oil removing slag removing system of anhydrous ammonia and technique illustrate.
From battery limit (BL) external containing ammonia less than or equal to 10g/m3, heavy oil drips less than or equal to 0.1g/m3, light oil drips less than or equal to 3g/
m3, slag is less than or equal to 0.1g/m3Coal gas (containing ammonia unstripped gas) enter ammonia absorber 1 bottom, in tower respectively with middle part spray follow
The phosphorus ammonium barren liquor that ring phosphorus ammonium pregnant liquor and top are sprayed carries out counter current contacting.Coal gas (gas after deamination) ammonia content after washing exists
100mg/m3Hereinafter, leave battery limit (BL) from ammonia absorber 1 top.Phosphorus ammonium pregnant liquor ammonia absorber bottom ammonia absorber 1 follows
Ring pump 10 is extracted out, and major part is delivered to circulation in the middle part of ammonia absorber 1 and sprayed coal gas, and small part rich solution sends into rich solution except heavy oil scummer
5。
Weight is removed less than or equal to 0.5g/l rich solution at rich solution less than or equal to 3g/l, slag less than or equal to 0.5g/l, light oil containing heavy oil
Separating in oil scummer 5, isolated slag is discharged from bottom, and isolated heavy oil is discharged from slag-drip opening top, and top is out
Rich solution sends into rich solution except light oil device 6.
Remove at rich solution less than or equal to 0.05g/l rich solution less than or equal to 3g/l, slag less than or equal to 0.05g/l, light oil containing heavy oil
Separating in light oil device 6, bottom is discharged and is less than or equal to less than or equal to 0.03g/l, slag less than or equal to 0.05g/l, light oil containing heavy oil
0.05g/l rich solution enters deacidification device 12 after entering poor rich liquid heat exchanger 11, with phosphorus ammonium barren liquor heat exchange.Top rich solution out enters
Light oil separator 7.
Separating in light oil separator 7 less than or equal to 30g/l rich solution containing light oil, isolated light oil is delivered to outside battery limit (BL), rich
Liquid returns to ammonia absorber 1 bottom.
Phosphorus ammonium pregnant liquor flashes off sour gas (comprising 80～90wt% light oil) in deacidification device 12, and sour gas deammoniation is inhaled
Receive tower 1 bottom.Phosphorus ammonium pregnant liquor again with desorber feed pump 13 pump to desorber cooler (on) enter behind 14, with ammonia vapour heat exchange
Desorber 2 top.Phosphorus ammonium pregnant liquor desorbs ammonia contained therein in tower and makes it be regenerated.Desorber 2 bottom is passed through
Steam is as heat source.
The ammonia vapour of desorber 2 top effusion respectively desorber cooler (on) 14 and desorbing tower cooler device (under) in 15, add
After hot phosphorus ammonium pregnant liquor and cooled water cooling, form ammonia and flow into ammonia feeder trough 16.
Desorber 2 end phosphorus ammonium barren liquor respectively in poor rich liquid heat exchanger 11 and lean solution cooler 21, heating phosphorus ammonium pregnant liquor and
After cooled water cooling, enter ammonia absorber 1 top and spray.
Partial ammonia water in ammonia feeder trough 16 enters product ammonia grease trap 8, and the oil content in ammonia is removed to
Deliver to outside battery limit (BL) after below 2ppm.
Remained ammonia rectifying column feed pump 17 in ammonia feeder trough 16 is pumped to rectifying column 3.Rectifying column 3 pushes up anhydrous ammonia
Gas cooled water in rectifying column condenser 18 becomes liquid anhydrous ammonia and flows into return tank 19.Anhydrous ammonia product in return tank
Extracting out with reflux pump 20, part is delivered to rectifying column 3 as backflow and is pushed up, and part sends into product anhydrous ammonia grease trap 9 as product.Essence
The waste water evaporating tower 3 end is delivered to outside battery limit (BL).Rectifying column bottom is passed through steam as heat source.
In product anhydrous ammonia grease trap 9, deliver to outside battery limit (BL) after the oil content in anhydrous ammonia is removed to below 2ppm.
Embodiment 4:
Present embodiment discloses a kind of phosphorus ammonium and wash the oil removing slag removing system of ammonia production anhydrous ammonia, as shown in Figure 4: include rich solution
Except light oil device 6, light oil separator 7, product ammonia grease trap 8 and product anhydrous ammonia grease trap 9；
Described rich solution is connected with ammonia absorber 1 except light oil device 6 import, and described rich solution removes light oil device 6 top exit and light oil
Separator 7 import connects, and described rich solution is connected with poor rich liquid heat exchanger 11 import except light oil device 6 outlet at bottom；Described light oil
Separator 7 import and rich solution are connected except light oil device 6 outlet, and described light oil separator 7 light oil exports and is connected with oil trap, described gently
The outlet of oil eliminator 7 rich solution is connected with ammonia absorber bottom.Described product ammonia grease trap 8 import is with ammonia feeder trough 16 even
Connecing, described product ammonia grease trap 8 outlet material is the product ammonia that oil content is less than 1ppm.Described product anhydrous ammonia oil removing
Device 9 import exports with product and reflux pump 20 and is connected, and described product anhydrous ammonia grease trap 9 outlet material is that oil content is less than 1ppm
Product ammonia.
As a example by coking propylhomoserin mixing unstripped gas coordinates phosphorus ammonium to wash ammonia production anhydrous ammonia, and combine Fig. 4 to the present embodiment phosphorus
Ammonium is washed ammonia and is produced the oil removing slag removing system of anhydrous ammonia and technique illustrates.
From battery limit (BL) external containing ammonia less than or equal to 1kg/m3, hydrogen sulfide is less than or equal to 2kg/m3, carbon dioxide is less than or equal to
2.6kg/m3, light oil drips less than or equal to 2g/m3Unstripped gas (containing ammonia unstripped gas) enters ammonia absorber 1 bottom, in tower respectively
The phosphorus ammonium barren liquor that the circulation phosphorus ammonium pregnant liquor sprayed with middle part and top are sprayed carries out counter current contacting.Tail gas after washing is (after deamination
Tail gas) ammonia content is at 9g/m3Hereinafter, leave battery limit (BL) from ammonia absorber 1 top.Phosphorus ammonium pregnant liquor bottom ammonia absorber 1 is used
Ammonia absorber circulating pump 10 is extracted out, delivers to circulation in the middle part of ammonia absorber 1 and sprays coal gas, and small part rich solution is sent into richness by rich solution pump 22
Liquid removes light oil device 6.
Separating in rich solution is except light oil device 6 less than or equal to 3g/l rich solution containing light oil, bottom is discharged and is less than or equal to containing light oil
0.2g/l rich solution enters deacidification device 12 after entering poor rich liquid heat exchanger 11, with phosphorus ammonium barren liquor heat exchange.Top rich solution out enters
Light oil separator 7.
Separating in light oil separator 7 less than or equal to 30g/l rich solution containing light oil, isolated light oil is delivered to outside battery limit (BL), rich
Liquid returns to ammonia absorber 1 bottom.
Phosphorus ammonium pregnant liquor flashes off sour gas (comprising 80～90wt% light oil) in deacidification device 12, and sour gas deammoniation is inhaled
Receive tower 1 bottom.Phosphorus ammonium pregnant liquor again with desorber feed pump 13 pump to desorber cooler (on) enter behind 14, with ammonia vapour heat exchange
Desorber 2 top.Phosphorus ammonium pregnant liquor desorbs ammonia contained therein in tower and makes it be regenerated.Desorber 2 bottom is passed through
Steam is as heat source.
The ammonia vapour of desorber 2 top effusion respectively desorber cooler (on) 14 and desorbing tower cooler device (under) in 15, add
After hot phosphorus ammonium pregnant liquor and cooled water cooling, form ammonia and flow into ammonia feeder trough 16.
Desorber 2 end phosphorus ammonium barren liquor respectively in poor rich liquid heat exchanger 11 and lean solution cooler 21, heating phosphorus ammonium pregnant liquor and
After cooled water cooling, enter ammonia absorber 1 top and spray.
Partial ammonia water in ammonia feeder trough 16 enters product ammonia grease trap 8, and the oil content in ammonia is removed to
Deliver to outside battery limit (BL) after below 1ppm.
Remained ammonia rectifying column feed pump 17 in ammonia feeder trough 16 is pumped to rectifying column 3.Rectifying column 3 pushes up anhydrous ammonia
Gas cooled water in rectifying column condenser 18 becomes liquid anhydrous ammonia and flows into return tank 19.Anhydrous ammonia product in return tank
Extracting out with reflux pump 20, part is delivered to rectifying column 3 as backflow and is pushed up, and part sends into product anhydrous ammonia grease trap 9 as product.Essence
The waste water evaporating tower 3 end is delivered to outside battery limit (BL).Rectifying column bottom is passed through steam as heat source.
In product anhydrous ammonia grease trap 9, deliver to outside battery limit (BL) after the oil content in anhydrous ammonia is removed to below 1ppm.
Last it is noted that various embodiments above is only in order to illustrate technical scheme, it is not intended to limit；To the greatest extent
The present invention has been described in detail by pipe with reference to foregoing embodiments, it will be understood by those within the art that: it depends on
So the technical scheme described in foregoing embodiments can be modified, or the most some or all of technical characteristic is entered
Row equivalent；And these amendments or replacement, do not make the essence of appropriate technical solution depart from various embodiments of the present invention technology
The scope of scheme.
Claims (9)
1. a phosphorus ammonium is washed ammonia and is produced the oil removing slag removing system of anhydrous ammonia, it is characterised in that including: rich solution is except light oil device (6), light
Oil eliminator (7), product ammonia grease trap (8) and product anhydrous ammonia grease trap (9)；
Described rich solution is connected with ammonia absorber (1) circulating pump or rich solution pump discharge except light oil device (6) import, and described rich solution removes light oil
Device (6) top exit is connected with light oil separator (7) import, and described rich solution is except light oil device (6) outlet at bottom and lean rich solution heat exchange
Device (11) import connects；
The outlet of described light oil separator (7) light oil is connected with oil groove, the outlet of described light oil separator (7) rich solution and ammonia absorber
(1) bottom connects；
Described product ammonia grease trap (8) import is connected with ammonia feeder trough (16)；
Described product anhydrous ammonia grease trap (9) import exports with product and reflux pump and is connected.
The most according to claim 1, phosphorus ammonium is washed ammonia and is produced the oil removing slag removing system of anhydrous ammonia, it is characterised in that include unstripped gas
Oil removing scummer (4), described unstripped gas oil removing scummer (4) import is connected with unstripped gas pipeline, and described unstripped gas oil removing removes the gred
Device (4) top exit is connected with ammonia absorber (1)；Described unstripped gas oil removing scummer (4) bottom is unstripped gas oil removing scummer
(4) slag-drip opening, described unstripped gas oil removing scummer (4) oil drain out is positioned at unstripped gas oil removing scummer (4) slag-drip opening top.
Phosphorus ammonium the most according to claim 1 or claim 2 is washed ammonia and is produced the oil removing slag removing system of anhydrous ammonia, it is characterised in that include richness
Liquid removes heavy oil scummer (5), and described rich solution is except heavy oil scummer (5) import and ammonia absorber (1) circulating pump or rich solution pump discharge
Connecting, described rich solution is connected except light oil device (6) import with rich solution except heavy oil scummer (5) top exit, and described rich solution removes heavy oil
Scummer (5) bottom is positioned at except heavy oil scummer (5) re-scheduling hydraulic fluid port except heavy oil scummer (5) slag-drip opening, described rich solution for rich solution
Rich solution removes heavy oil scummer (5) slag-drip opening top.
Phosphorus ammonium the most according to claim 1 or claim 2 is washed ammonia and is produced the oil removing slag removing system of anhydrous ammonia, it is characterised in that include richness
Liquid removes heavy oil scummer (5), and described rich solution is connected except light oil device (6) outlet at bottom with rich solution except heavy oil scummer (5) import, institute
Stating rich solution and be connected with poor rich liquid heat exchanger (11) import except heavy oil scummer (5) top exit, described rich solution is except heavy oil scummer
(5) bottom is removed except heavy oil scummer (5) re-scheduling hydraulic fluid port is positioned at rich solution except heavy oil scummer (5) slag-drip opening, described rich solution for rich solution
Heavy oil scummer (5) slag-drip opening top.
5. a phosphorus ammonium with oil removing slag removing function is washed ammonia and is produced anhydrous ammonia system, it is characterised in that include claim 1-4
Phosphorus ammonium described in any one is washed ammonia and is produced the oil removing slag removing system of anhydrous ammonia.
6. a phosphorus ammonium is washed ammonia and is produced the oil removing deslagging process of anhydrous ammonia, it is characterised in that comprise the steps:
Rich solution from ammonia absorber (1) enters rich solution and removes light oil device (6), and light oil, trace heavy oil and slag in rich solution are at rich solution
Except light oil device (6) is separated；
The rich solution that rich solution is discharged except light oil device (6) top exit enters light oil separator (7), and light oil separator (7) divides further
Light oil in rich solution, the rich solution after being separated by light oil returns ammonia absorber (1)；
Residue in the trace amount in ammonia and anhydrous ammonia, respectively at product ammonia grease trap (8) and product anhydrous ammonia grease trap (9)
In adsorbed removing.
The most according to claim 1, phosphorus ammonium is washed ammonia and is produced the oil removing deslagging process of anhydrous ammonia, it is characterised in that include walking as follows
Rapid:
Rich solution from ammonia absorber (1) enters rich solution and removes heavy oil scummer (5), and heavy oil and slag in rich solution remove heavy oil at rich solution
Scummer is separated in (5)；
Rich solution enters rich solution except light oil device (6), the light oil in rich solution, residual weight from rich solution except heavy oil scummer (5) top exit
Oil and slag are separated in rich solution is except light oil device (6).
The most according to claim 1, phosphorus ammonium is washed ammonia and is produced the oil removing deslagging process of anhydrous ammonia, it is characterised in that include walking as follows
Rapid:
90～95wt% oil droplets and slag in unstripped gas are separated in unstripped gas oil removing scummer (4)；
Rich solution from ammonia absorber (1) enters rich solution except light oil device (6), 85～95wt% light oil in rich solution, trace heavy oil
And slag is separated in rich solution is except light oil device (6)；
The rich solution that rich solution is discharged except light oil device (6) top exit enters light oil separator (7), and the rich solution after being separated by light oil returns
Ammonia absorber (1)；
Rich solution enters except heavy oil scummer (5), 90～96wt% weights in rich solution except the rich solution that light oil device (6) outlet at bottom is discharged
Oil and slag are separated except heavy oil scummer (5) at rich solution；
Residue in 30 in ammonia and anhydrous ammonia～300ppm oil, remove at product ammonia grease trap (8) and product anhydrous ammonia respectively
Oil device (9) is adsorbed be removed to 1～20ppm.
The most according to claim 1, phosphorus ammonium is washed ammonia and is produced the oil removing deslagging process of anhydrous ammonia, it is characterised in that include walking as follows
Rapid:
90～95wt% oil droplets and slag in unstripped gas are separated in unstripped gas oil removing scummer (4)；
Separated in rich solution is except heavy oil scummer (5) from 90 in the rich solution of ammonia absorber (1)～96wt% heavy oil and slag；
Rich solution enters rich solution except light oil device (6) from rich solution except heavy oil scummer (5) top exit, 85～95wt% light oil in rich solution and
Separated in rich solution is except light oil device (6)；
The rich solution that rich solution is discharged except light oil device (6) top exit enters light oil separator (7), and the rich solution after being separated by light oil returns
Ammonia absorber (1)；
Residue in 30 in ammonia and anhydrous ammonia～300ppm oil, remove at product ammonia grease trap (8) and product anhydrous ammonia respectively
Oil device (9) is adsorbed be removed to 1～20ppm.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201610515238.7A CN106185986B (en) | 2016-07-04 | 2016-07-04 | Phosphorus ammonium washes the oil removing slag removing system and technique of ammonia production anhydrous ammonia |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201610515238.7A CN106185986B (en) | 2016-07-04 | 2016-07-04 | Phosphorus ammonium washes the oil removing slag removing system and technique of ammonia production anhydrous ammonia |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN106185986A true CN106185986A (en) | 2016-12-07 |
| CN106185986B CN106185986B (en) | 2018-07-31 |
Family
ID=57465671
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201610515238.7A Active CN106185986B (en) | 2016-07-04 | 2016-07-04 | Phosphorus ammonium washes the oil removing slag removing system and technique of ammonia production anhydrous ammonia |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN106185986B (en) |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3985863A (en) * | 1973-07-02 | 1976-10-12 | United States Steel Corporation | Process for the separation and recovery of ammonia and acid gases |
| EP1157969A2 (en) * | 2000-05-23 | 2001-11-28 | Rohm And Haas Company | Process for recovery and recycle of ammonia from a reactor effluent stream |
| CN101531379A (en) * | 2009-04-17 | 2009-09-16 | 天津天达联合工程技术有限公司 | Method for producing anhydrous ammonia by absorbing ammonium phosphate |
| CN104689703A (en) * | 2015-03-30 | 2015-06-10 | 攀钢集团西昌钢钒有限公司 | Ammonium phosphate ammonia-washing tail gas treatment technology and ammonium phosphate ammonia-washing system |
| CN105293524A (en) * | 2015-11-20 | 2016-02-03 | 薛斌 | Recovery system and process for waste heat in production of anhydrous ammonia from ammonium phosphate through ammonia washing |
-
2016
- 2016-07-04 CN CN201610515238.7A patent/CN106185986B/en active Active
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3985863A (en) * | 1973-07-02 | 1976-10-12 | United States Steel Corporation | Process for the separation and recovery of ammonia and acid gases |
| EP1157969A2 (en) * | 2000-05-23 | 2001-11-28 | Rohm And Haas Company | Process for recovery and recycle of ammonia from a reactor effluent stream |
| CN101531379A (en) * | 2009-04-17 | 2009-09-16 | 天津天达联合工程技术有限公司 | Method for producing anhydrous ammonia by absorbing ammonium phosphate |
| CN104689703A (en) * | 2015-03-30 | 2015-06-10 | 攀钢集团西昌钢钒有限公司 | Ammonium phosphate ammonia-washing tail gas treatment technology and ammonium phosphate ammonia-washing system |
| CN105293524A (en) * | 2015-11-20 | 2016-02-03 | 薛斌 | Recovery system and process for waste heat in production of anhydrous ammonia from ammonium phosphate through ammonia washing |
Also Published As
| Publication number | Publication date |
|---|---|
| CN106185986B (en) | 2018-07-31 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN104826472B (en) | Smoke carbon dioxide capture recovery system | |
| CN107413176A (en) | A kind of ammonia process of desulfurization dedusting flue gas minimum discharge system and application | |
| RU2015144714A (en) | Absorption of Phosphorus by Hydration and Reduction of Fluorine during Firing in a Furnace for the Production of Phosphoric Acid | |
| CN206553478U (en) | Coal oven dithio-gas purifier | |
| CN111729483A (en) | Carbon dioxide capture system and method | |
| CN102151470A (en) | Flue gas desulfurization method and device | |
| EP3006100B1 (en) | Gas-liquid contactor and co2-recovering apparatus provided therewith | |
| CN206652387U (en) | A kind of ammonia desulfuration equipment of resourcebility | |
| CN102120937A (en) | Purification method of coke oven gas matched with vacuum carbonate desulphurization | |
| CN106479578A (en) | A kind of acid gas removal technique of supporting coal gasification | |
| CN207958281U (en) | A kind of thick Straw Gas purification unit equipment | |
| CN103831003B (en) | A kind of regeneration tail gas purification combination tower | |
| US4086323A (en) | Process for removal of sulfur compounds from fuel gases | |
| CN106377968A (en) | Dust removing and recycling system for granulation column | |
| US2733054A (en) | Van ackeren | |
| CN106185986A (en) | Phosphorus ammonium is washed ammonia and is produced oil removing slag removing system and the technique of anhydrous ammonia | |
| CN105854478A (en) | Apparatus and method for treating exhaust gas in the production of PVC gloves | |
| KR20140042536A (en) | Apparatus for treating carbon dioxide | |
| KR101955782B1 (en) | Processing unit for a washing medium contaminated with sulphur oxides and/or nitrogen oxides | |
| CN205650085U (en) | Concentration circulating separator | |
| CN205258214U (en) | Phenyl amines midbody waste water's processing apparatus | |
| CN207042226U (en) | A kind of cold rolling acid mist absorbs automatic circulating system | |
| CN103224817A (en) | Coal gas dedusting decoking desulfurization system and method | |
| CN207845726U (en) | A kind of bastnaesite rare earth production technology system | |
| CN214780788U (en) | Device for twice recovering ammonia in ammonia-containing non-condensable gas in coal gasification process |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant |