CN110342717A - Gasification energy couples ammonia recovery system and method - Google Patents
Gasification energy couples ammonia recovery system and method Download PDFInfo
- Publication number
- CN110342717A CN110342717A CN201910670147.4A CN201910670147A CN110342717A CN 110342717 A CN110342717 A CN 110342717A CN 201910670147 A CN201910670147 A CN 201910670147A CN 110342717 A CN110342717 A CN 110342717A
- Authority
- CN
- China
- Prior art keywords
- ammonia
- gasification
- condensate liquid
- buck
- stripping
- 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.)
- Pending
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
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F9/00—Multistage treatment of water, waste water or sewage
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/02—Treatment of water, waste water, or sewage by heating
- C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
- C02F1/048—Purification of waste water by evaporation
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/02—Treatment of water, waste water, or sewage by heating
- C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
- C02F1/06—Flash evaporation
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/20—Treatment of water, waste water, or sewage by degassing, i.e. liberation of dissolved gases
-
- C—CHEMISTRY; METALLURGY
- 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
- C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
- C02F2101/10—Inorganic compounds
- C02F2101/16—Nitrogen compounds, e.g. ammonia
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2301/00—General aspects of water treatment
- C02F2301/06—Pressure conditions
- C02F2301/063—Underpressure, vacuum
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F5/00—Softening water; Preventing scale; Adding scale preventatives or scale removers to water, e.g. adding sequestering agents
- C02F5/02—Softening water by precipitation of the hardness
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Analytical Chemistry (AREA)
- Inorganic Chemistry (AREA)
- Life Sciences & Earth Sciences (AREA)
- Hydrology & Water Resources (AREA)
- Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Water Supply & Treatment (AREA)
- Physical Water Treatments (AREA)
Abstract
The invention discloses a kind of gasification energies to utilize coupling ammonia recovery system, including gasification flash system, grey water pretreatment system, condensate liquid stripping and ammonia recovery system；The flash system that gasifies carries out vacuum flashing to temperature gasification and high Heisui River, gasification flashed vapour is obtained after cooling down and Heisui River of gasifying；Grey water pretreatment system includes hard-off to be obtained buck and strips rich ammonia logistics entering condensate liquid stripping and ammonia recovery system except being fixedly mounted with to set with buck stripper plant to gasification ash water hard-off except sending to buck stripper plant to remove ammonia after solid；Condensate liquid stripping and ammonia recovery system realize the separation of ammonia and sour gas, obtain the high ammonolysis product of ammonia content.Invention additionally discloses a kind of gasification energies to utilize coupling ammonia recovery method.The present invention improves gasification installation energy utilization efficiency, has both recycled the ammonia in buck and condensate liquid, also effectively reduces the NH_3-N treating difficulty and operating cost of waste water downstream processing unit, helps to reduce fouling existing for current system, abrasion and etching problem.
Description
Technical field
The present invention relates to recovery ammonia comprehensive treatment technique fields, more particularly to a kind of relevant gas of gas-flow bed gasifying apparatus
Change energy coupling ammonia recovery system and method.
Background technique
Entrained flow gasification reaction is being gasified by slurry or pneumatic conveying with oxygen by coal or other hydrocarbons
The partial oxidation reaction that high temperature and pressure occurs in furnace, generates product crude synthesis gas.
During coal gasification, the nitrogen in coal has sub-fraction to be converted into ammonia, and the ammonia of generation largely exists
In the synthesis gas and gasification ash water that gasification unit is sent out.Ammonia in synthesis gas enters the transformation list in downstream with synthesis gas
Member (including synthesis air cooling device), is present in condensate liquid, high temperature condensate liquid returns to gas after gradually cooling and wash
Makeup is set, and returns to gasification installation after the stripping system deamination of the transformed unit of low temperature cold lime set, and the sour gas stripped contains two
Carbonoxide, hydrogen sulfide, ammonia sour gas.Then there are ammonia nitrogen, calcium, magnesium and the silicon ion etc. of high level in gasification ash water.
In existing old process, the low temperature cold lime set of converter unit uses the steam stripped processing method of direct flashed vapour, by vapour
The gas containing ammonia and sour gas put forward is sent to sulfur recovery unit processing；Flash system generates a large amount of gasification flash distillation simultaneously
Gas, main component are water vapour, are rich in law level energy, the law level energy, except part is remainder in addition to gasification unit is personal
Condensed or be routed directly to converter unit stripping system.Gasification ash water is then sent to waste water downstream processing unit and carries out biochemical treatment.
Therefore, existing procedure has the disadvantage that
It 1. ammonia and sour gas do not separate in low temperature cold lime set, that is, cannot achieve the recycling of ammonia, while also causing to transport
Easily occur corroding in row process and scale problems, increases the operation difficulty and operating cost of sulfur recovery unit；
2. the ammonia-nitrogen content in gasification ash water is high, lead to the difficulty and increased costs of waste water downstream biochemical treatment, and gasify
The calcium of high-content, magnesium and silicon ion easily lead to scaling blocking in buck and next step advanced treating is difficult；
3. the energy of gasification flashed vapour is not fully used, and generally requires cooling treatment, consume a large amount of cooling
Water.
Summary of the invention
Technical problem to be solved by the present invention lies in improve gasification installation energy utilization efficiency, realize the recycling of ammonia
It utilizes, reduces the processing difficulty and operating cost of waste water downstream processing unit.
For up to foregoing purpose, the present invention provides a kind of gasification energy coupling ammonia recovery system, by gasification flash system, buck
Pretreatment system, condensate liquid stripping and ammonia recovery system composition.
The gasification flash system includes vacuum flashing device, and the vacuum flashing device is used for single from upstream gasification
The synthesis gas of member carries out Quench, and carries out vacuum flashing to the high temperature Heisui River from upstream washing unit, is dodged with generating gasification
Steam；The gasification flash system connects the grey water pretreatment system and condensate liquid stripping and ammonia recovery system；
The grey water pretreatment system, which includes hard-off, to be set and buck stripper plant except being fixedly mounted with；The hard-off is removed to be fixedly mounted with to set and is used for
Removing hardness and solids treatment are carried out to the gasification ash water from upstream gasification unit；The buck stripper plant is used for removing
Buck after hardness and solids treatment carries out deamination and handles to obtain rich ammonia logistics, and the grey water pretreatment system connects the condensation
Liquid stripping and ammonia recovery system, the richness ammonia logistics delivery is stripped to the condensate liquid and ammonia recovery system；
The condensate liquid stripping and ammonia recovery system include condensate liquid stripper plant and ammonia recovery unit, the condensate liquid vapour
It mentions device and connects the ammonia recovery unit；Locate in advance from the condensate liquid of upstream units and other logistics and from the buck
The rich ammonia logistics of reason system enters the condensate liquid stripper plant and is separated, and is subsequently transmitted to the ammonia recovery unit and carries out ammonia
Recycling.
For the gasification flash distillation atmospheric pressure in 0.2-3.0Mpa, main component is vapor, is rich in low-grade heat, can be described
Grey water pretreatment system and condensate liquid stripping and ammonia recovery system provide heat source；Preferably, the gasification flashes atmospheric pressure
For 0.5-1.2MPA.
The hard-off is set by under the pharmacy effects such as lye and flocculant except being fixedly mounted with, using reaction, clarification and filtering etc.
Means remove the hardness ions such as the calcium in buck, magnesium, silicon.
The buck stripper plant capital equipment is grey water stripper, utilizes the heat indirect heating vapour of gasification flashed vapour
It mentions to remove the ammonia in buck；The buck stripper plant further includes the equipment such as other relevant pump, heat exchanger and pans.
The condensate liquid stripper plant capital equipment is condensate liquid stripper, and the gasification flashed vapour is directly entered condensate liquid
Stripper is stripped using the heat of gasification flashed vapour, to remove the ammonia of liquid containing ammonia condensing or other logistics；Contained ammonia condensing liquid or
Other logistics further include torch condensate liquid and other wash ammoniacal liquor；The condensate liquid stripper plant further includes other relevant pumps, changes
The equipment such as hot device and pans.
The ammonia recovery unit includes ammonia condensing device and ammonia purification recovery device.
The ammonia condensing device is multistage fractional condensation system, and series is 2-4 grades；By multistage fractional condensation system, from aminoacid stripping tower
The rich ammonia logistics of middle part extraction cools, while the impurity such as the water of separating most and hydrogen sulfide.
The ammonia purification recovery device further removes impurity contained by ammonia condensing device, obtains the ammon amount of required specification
High liquid or gaseous state ammonolysis product, such as product can be gas ammonia, ammonium hydroxide and liquefied ammonia.The technique of the ammonia purification recovery device
Route can be adjusted according to the specification of ammonolysis product, for example, such as using weak aqua ammonia as product, then can be used washing process (with alkali or
Ammonia is solvent) impurities are first removed, then wash to obtain weak aqua ammonia；Such as using pure liquefied ammonia as product, then hydrogen sulfide in liquefied ammonia is required
The content of equal impurity is very low, therefore in addition to washing process, also needs to consider that absorption crystallization even depth processing method further removes sulphur
Change the impurity such as hydrogen, recompression cooling obtains liquefied ammonia.
The present invention also provides a kind of gasification energies using coupling ammonia recovery method, comprising steps of
1) the high temperature Heisui River from upstream units, which is passed through, carries out vacuum flashing and cooling in gasification flash system, generates gas
Change flashed vapour；
2) from upstream gasification unit generate gasification ash water enter grey water pretreatment system, hard-off except be fixedly mounted with set in
Alkali, flocculant hybrid reaction generate solid, remove solid after clarification and filtering；Buck after removing solid enters buck stripping dress
Set, 1) described in gasification flash vaporization air lift supplying heat source strip the ammonia in buck, the rich ammonia logistics delivery extracted to condensate liquid vapour
Refer to ammonia recovery system；Buck heat exchange after stripping is further processed with quenched rear discharge system or Returning utilization；
3) condensate liquid stripping and ammonia recovery system in, 1) described in gasification flash vaporization air lift supplying heat source, condensate liquid strip
The buck containing the condensate liquid of ammonia or other logistics and from grey water pretreatment system from upstream units is stripped in device rich
Ammonia logistics is separated, and rich ammonia logistics is sent to ammonia recovery system after obtained stripping, utilizes the ammonia condensing of ammonia recovery unit and net
Change recyclable device, after which is further processed removal sour gas, obtains the ammonolysis product of high ammon amount；Condensate liquid stripping
Condensate liquid or other logistics discharge systems are recycled or are further processed after the stripping generated after separation in device, are generated
Sour gas be sent into downstream units be further processed.
Gasification energy coupling ammonia recovery system provided by the invention and method, have the advantage that compared with the prior art
Using gasification flashed vapour heat, the buck after removing admittedly to hard-off strips the present invention, obtains the lower stripping of ammonia content
Buck and buck strip rich ammonia logistics, realize the recycling of ammonia and can obtain the high product of ammon amount, facilitate under reduction
Swim grey cost of water treatment and difficulty；Flashed vapour heat is recycled, it is real for being stripped to containing the condensate liquid of ammonia or other logistics
Existing sour gas separation and recycling, help to solve current system generally existing corrosion and scale problems, and obtained ammonia produces
The very high problem of product ammon amount；And the heat for the flashed vapour that gasifies also is fully utilized, that is, improves gasification installation energy
Utilization efficiency also avoids the consumption of recirculated cooling water.
Detailed description of the invention
Fig. 1 is the schematic diagram of gasification energy coupling ammonia recovery system of the invention.
Fig. 2 is a specific embodiment of the condensate liquid stripping and ammonia recovery system in the present invention.
Sign flag illustrates in attached drawing:
Gasify 1 grey water pretreatment system 2 of flash system
De- be fixedly mounted with of hard-off sets 21 buck stripper plants 22
Condensate liquid stripping and 3 condensate liquid stripper plant 31 of ammonia recovery system
32 ammonia purification recovery device 33 of ammonia condensing device
Ammonia condensing liquid stripper plant:
Condensate liquid stripper 3E01 condensate liquid cooler 3E02
Condensate liquid stripper bottom pump 3E03 stripper bottom 1# heat exchanger 3E04
Stripper bottom 2# heat exchanger 3E05
Ammonia condensing device:
1# ammonia cooler 3E07 1# ammonia refrigerated separation tank 3E08
2# ammonia cooler 3E09 2# ammonia refrigerated separation tank 3E10
3# ammonia cooler 3E11 3# ammonia refrigerated separation tank 3E12
Ammonia condensing separating liquid cooler 3E15 ammonia condensing separates flow container 3E16
Ammonia condensing separates liquid pump 3E17
Ammonia purification recovery device:
Caustic wash tower 3E13 water scrubber 3E14
Temperature gasification and high Heisui River 101 (it is steam stripped to lead to gasification ash water) gasification flashed vapour 102
(it is steam stripped to lead to condensation liquefied ammonia) gasification flashed vapour 102A gasification ash water 201
Buck stripping gasification 203 buck of flashed vapour condensate liquid strips rich ammonia logistics 202
The de- solid rear buck 206 of 204 hard-off of buck after stripping
Grey 207 lye 208 of water solid
209 ammonolysis product 301 of flocculant
Condensate liquid 303 after sour gas 302 strips
Rich ammonia logistics 305 after liquid containing ammonia condensing or other logistics 304 stripping
Rich 306 water scrubber on-condensible gas 307 of ammonia logistics after condensation
308 process water 309 of lye
310 low temperature cold lime set 311 of high temperature condensate liquid
312 aminoacid stripping tower bottoms 313 of caustic wash tower bottom liquid
Gasification flashes not condensing 314
Specific embodiment
Clear, complete description will be carried out to technical solution of the present invention below, it is clear that described embodiment is this hair
Bright a part of the embodiment, instead of all the embodiments.Based on the embodiments of the present invention, those of ordinary skill in the art exist
Every other embodiment obtained under the premise of creative work is not made, shall fall within the protection scope of the present invention.
As shown in Figure 1, the present invention provides a kind of gasification energy coupling ammonia recovery system, comprising: gasification flash system 1, ash
Water pretreatment system 2 and condensate liquid stripping and ammonia recovery system 3.
Gasification flash system 1 is separately connected grey water pretreatment system 2 and condensate liquid stripping and ammonia recovery system 3；Gasification is dodged
Steaming system 1 mainly includes vacuum flashing device, and the temperature gasification and high Heisui River 101 from upstream device enters vacuum flashing device and carries out
Evaporation and cooling generate a large amount of gasification flashed vapour, wherein one gasification flashed vapour 102A is sent to condensate liquid stripping and recovery ammonia
System 3, in addition one gasification flashed vapour 102, provides stripping heat source for the buck stripper plant 22 of grey water pretreatment system 2, changes
Heat obtains buck stripping gasification flashed vapour condensate liquid 203 and is back to the gasification utilization of flash system 1.
Grey water pretreatment system 2 connects condensate liquid stripping and ammonia recovery system 3；Grey water pretreatment system 2 is removed including hard-off
It is fixedly mounted with and sets 21 and buck stripper plant 22；
Gasification ash water 201 is delivered to hard-off and sets 21 and carry out removing hardness and solids treatment except being fixedly mounted with, and sets in hard-off except being fixedly mounted with
In 21, gasification ash water 201 makes calcium, magnesium and silicon plasma in gasification ash water 201 heavy with lye 208,209 hybrid reaction of flocculant
Drop, buck 206 is delivered to the progress deamination processing of buck stripper plant 22 after being taken off admittedly by the hard-off after clarification and filtration treatment, and
The grey water solid 207 of removing is discharged from gasification energy coupling ammonia recovery system；
Deamination processing is carried out in buck stripper plant 22, is obtained buck and is stripped rich ammonia logistics 202, buck strips rich ammonia logistics
202 convey toward condensate liquid stripping and ammonia recovery system 3；Buck 204 is delivered to downstream after the stripping that buck stripper plant 22 is discharged
Wastewater treatment equipment, can also partially back to upstream gasification unit water system be recycled.Carry out autopneumatolysis flash system 1
Gasification flashed vapour 102 is that buck stripper plant 22 provides stripping heat source, and heat exchange obtains buck stripping gasification flashed vapour condensate liquid
203, which are back to gasification flash system 1, utilizes.
Condensate liquid stripping and ammonia recovery system 3 include condensate liquid stripper plant 31, ammonia condensing device 32 and ammonia Recovery Purifying
Device 33；Upstream units are stripped containing the condensate liquid of ammonia or other logistics 304 in condensate liquid stripper plant 31, obtained acid
Property gas 302 gasification energy coupling ammonia recovery system be discharged be further processed；Condensate liquid 303 is discharged after obtained stripping
The gasification energy coupling ammonia recovery system is recycled or is further processed；After obtained stripping rich ammonia logistics 305 into
Enter ammonia condensing device 32, rich ammonia logistics 306 after being condensed after removing most of moisture and impurity, into ammonia purification recovery device
33, after the process for refining such as washing absorption or absorption, obtains the high ammonolysis product 301 of ammonia content and send out the gasification energy coupling
Ammonia recovery system.Wherein, a part gasification flashed vapour 102A for carrying out autopneumatolysis flash system 1 enters condensate liquid stripper plant 31,
Stripping heat source is provided.
As shown in Fig. 2, preparing a specific embodiment of weak aqua ammonia for condensate liquid stripping and 3 operation of ammonia recovery system.
Condensate liquid stripping and ammonia recovery system 3 include condensate liquid stripper plant 31, ammonia condensing device 32 and ammonia Recovery Purifying
Device 33；Wherein, the fractional condensation device that ammonia condensing device 32 is one 2-4 grades, generally three-level, wherein level-one is cooling using cold
Lime set, second level is cooling to use cooling water, and cooling water or other low-temperature cooling medias, such as liquefied ammonia etc. can be used in three-level cooling.
The gasification flashed vapour 102A for carrying out autopneumatolysis flash system 1 enters condensate liquid stripper 3E01 and provides heat source；
Divide from the condensate liquid of upstream units and other logistics 304 for two-way: cooling through condensate liquid cooler 3E02 all the way
Low temperature cold lime set 311 is formed, the top condensate liquid stripper 3E01 is sent into；The titanium dioxide that the top condensate liquid stripper 3E01 is rich in
The sour gas such as carbon, hydrogen sulfide 302 are sent to downstream sulfur recovery unit processing；
Another way and aminoacid stripping tower bottoms 313 after stripper bottom 2# heat exchanger 3E05 mixing, respectively with 1# ammonia
Cooler 3E07 and stripper bottom 1# heat exchanger 3E04 heat exchange heating, obtained high temperature condensate liquid 310 enter condensate liquid and strip
The middle and upper part tower 3E01.
Aminoacid stripping tower bottoms 313 respectively with stripper bottom 1# heat exchanger 3E04 and stripper bottom 2# heat exchanger
3E05 exchanges heat, and condensate liquid 303 is sent gasification unit back to and recycled after stripping after cooling；
The condensate liquid middle and lower part stripper 3E01 side extraction stripping richness ammonia logistics 305 successively respectively with 1# ammonia cooler
3E07,1# ammonia refrigerated separation tank 3E08,2# ammonia cooler 3E092,2# ammonia refrigerated separation tank 3E10 and 3# ammonia cooler 3E11,3#
Ammonia refrigerated separation tank 3E12 heat exchange cooling, rich ammonia logistics 306 enters after gas-liquid separation obtains the condensation obtained after most of liquid phase
Ammonia purification recovery device 33.Wherein, the ammonia refrigerated separation bottom tank 3E10 1# ammonia refrigerated separation tank 3E08 and 2# discharge temperature compared with
High liquid phase enters after ammonia condensing separating liquid cooler 3E15 cooling with the liquid phase of the 3# ammonia refrigerated separation bottom tank 3E12 discharge
Ammonia condensing separates flow container 3E16, and the liquid of the ammonia condensing separation bottom flow container 3E16 discharge separates liquid pump 3E17 by ammonia condensing again and adds
Condensate liquid feeding line is returned to after pressure, imports 310 high temperature condensate liquids.
It is cold that the 3# ammonia that rich ammonia logistics 202 enters ammonia condensing device 32 is stripped from the buck of grey water pretreatment system 2 simultaneously
But device 3E11 suction line and knockout drum 3E12 heat exchange cooling import rich ammonia logistics 306 after condensation.
Carry out the gasification flash distillation fixed gas 314 of autopneumatolysis flash system 1 also containing a small amount of ammonia, processing need to comprehensively consider gas
Water system and nitrogen balance situation are set in makeup.In the present embodiment, the gasification flash distillation fixed gas 314 that the flash system 1 that gasifies generates is sent
Enter the entrance of the 1# ammonia cooler 3E07 of ammonia condensing device 32.
Rich ammonia logistics 306 enters the caustic wash tower of ammonia purification recovery device 33 after the condensation of the processing of ammonia condensing device 32
3E13, the sulphur with lye 308 (liquefied ammonia or sodium hydroxide solution etc.) for solvent, after absorbing and removing condensation in rich ammonia logistics 306
Water scrubber 3E14 is entered back into after changing the impurity such as hydrogen；Caustic wash tower 3E13 bottom liquid 312 is discharged to outside device, also can return to ammonia condensing point
Chaotropic tank 3E16 directly returns to condensate liquid stripper 3E01 re-using；It is (de- using process water 309 in water scrubber 3E14
Salt water or boiler feedwater) it is used as lyosoption to obtain 301 weak aqua ammonia of ammonolysis product, it is discharged from tower bottom, at the top of water scrubber 3E14
On-condensible gas 307 leaves system at the top of water scrubber 3E14.
In other embodiments, can comprehensively consider as needed in conjunction with system configuration in condensate liquid stripping and ammonia recovery system 3
Interior setting condensate liquid head tank.
The above is the explanation of each chief component of the embodiment of the present invention, below with 1,800,000 tons of methanol of an annual output
Coal Coal-water Slurry Pressurized Gasification Unit for for, illustrate the embodiment of the present invention condensate liquid stripping and ammonia recovery system 3 master
Want flow stream parameters and effect.
Table 1 is the condensate liquid stripping of the embodiment of the present invention and the main streams parameter of ammonia recovery system 3:
| Logistics number | Unit | 304 | 102A | 202 | 314 | 302 | 303 | 312 | 301 |
| Temperature | ℃ | 40 | 176.65 | 87.78 | 153.9 | 74.08 | 74.21 | 55.57 | 50.91 |
| Pressure | MPa(A) | 6.1 | 0.965 | 0.265 | 0.964 | 0.43 | 0.436 | 0.5 | 0.5 |
| Composition flow rate | |||||||||
| NH3 | Kilomol/hour | 30.4 | 1.5 | 6.55 | 0.254 | 0.617 | 1.24 | 3.71 | 31.8 |
From above table it is found that the embodiment of the present invention can bring it is following the utility model has the advantages that
1. stripping rich 202 band of ammonia logistics from condensate liquid 304, gasification flashed vapour 102A and buck in the system of this method
The ammonia total amount entered is 30.4+1.5+6.55=38.45 kilomol/hour, and the ammonia of output is primarily present in ammonolysis product 301,
His ammonia is mainly discharged in liquid 312 in sour gas 302, not condensing 314 and caustic wash tower, overall recovery 31.8/38.45=
82.7%, it can produce 2.7 ton/hours of ammonium hydroxide (mass concentration 20%), the use of boiler plant desulphurization denitration can be sent to.
2. stripping the ammonia for passing through in richness ammonia logistics 202 and stripping and recycling from buck is 6.55x 17=111.4 kg/hr,
Ammonia content in gasification ash water can be reduced to 100ppm or less；Ammonia has not only been recycled, waste water downstream processing is also significantly reduced
The cost and difficulty of device.
3. the ammonia flow for the gasification flash distillation tolerance 102A entrainment for needing to consume in the present embodiment is 1.5x 17=25.5 thousand
Grams Per Hour.Through this embodiment, this part ammonia amount can be not only recycled, this cooling part gas in old process can also be reduced
Cooling water consumption needed for changing flashed vapour 102A；
4. from system be discharged sour gas 302 and water scrubber on-condensible gas 307 in ammonia content it is very low, facilitate downstream into
The processing of one step.
In conclusion the various embodiments described above are only presently preferred embodiments of the present invention, it is not of the invention to limit
Protection scope, all within the spirits and principles of the present invention, any modification, equivalent substitution, improvement and etc. done should be all included in
In protection scope of the present invention.
Claims (10)
1. a kind of gasification energy couples ammonia recovery system characterized by comprising gasification flash system, grey water pretreatment system,
Condensate liquid stripping and ammonia recovery system；
The gasification flash system includes vacuum flashing device, and the vacuum flashing device is used for from upstream gasification unit
Synthesis gas carries out Quench, and carries out vacuum flashing to the high temperature Heisui River from upstream washing unit, to generate gasification flashed vapour；
The gasification flash system connects the grey water pretreatment system and condensate liquid stripping and ammonia recovery system；
The grey water pretreatment system, which includes hard-off, to be set and buck stripper plant except being fixedly mounted with；The hard-off is removed to be fixedly mounted with and be set for next
Removing hardness and solids treatment are carried out from the gasification ash water of upstream gasification unit, the buck stripper plant is used for removing hardness
Deamination is carried out with the buck after solids treatment to handle to obtain rich ammonia logistics；The grey water pretreatment system connects the condensate liquid vapour
Refer to ammonia recovery system, the richness ammonia logistics delivery is stripped to the condensate liquid and ammonia recovery system；
The condensate liquid stripping and ammonia recovery system include condensate liquid stripper plant and ammonia recovery unit, the condensate liquid stripping dress
Set the connection ammonia recovery unit；Condensate liquid logistics from upstream units and the richness from the grey water pretreatment system
Ammonia logistics enters the condensate liquid stripper plant and is separated, and is subsequently transmitted to the recycling that the ammonia recovery unit carries out ammonia.
2. system according to claim 1, which is characterized in that the pressure of the gasification flashed vapour is in 0.2-3.0MPA, master
Will group be divided into vapor.
3. system according to claim 2, which is characterized in that the gasification flash distillation atmospheric pressure is 0.5-1.2MPA.
4. system as defined in claim 1, which is characterized in that the buck stripper plant includes for grey water stripper.
5. system as defined in claim 1, which is characterized in that the condensate liquid stripper plant includes condensate liquid stripping
Tower.
6. system according to claim 4 or 5, which is characterized in that the buck stripper plant and condensate liquid stripper plant
It further include pump, heat exchanger and pans.
7. system according to claim 1, which is characterized in that the ammonia recovery unit includes ammonia condensing device and ammonia purification
Recyclable device.
8. system according to claim 7, which is characterized in that the ammonia condensing device is multistage fractional condensation system, and series is
2-4 grades.
9. system according to claim 7, which is characterized in that the ammonia purification recovery device is miscellaneous for further removing
Matter obtains the ammon amount of required specification high liquid or gaseous state ammonolysis product.
10. a kind of gasification energy couples ammonia recovery method, which is characterized in that comprising steps of
1) the high temperature Heisui River from upstream units, which is passed through, carries out vacuum flashing and cooling in gasification flash system, generates gasification and dodges
Steam；
2) from upstream gasification unit generate gasification ash water enter grey water pretreatment system, hard-off except be fixedly mounted with set in first with
The solid of generation is removed after alkali, flocculant hybrid reaction, clarification and filtering；Buck after removing solid enters buck stripping dress
Set, 1) described in gasification flash vaporization air lift supplying heat source strip the ammonia in buck, the rich ammonia logistics delivery extracted to condensate liquid vapour
Refer to ammonia recovery system；Buck heat exchange after stripping is further processed with quenched rear discharge system or Returning utilization；
3) condensate liquid stripping and ammonia recovery system in, 1) described in gasification flash vaporization air lift supplying heat source, in condensate liquid stripper plant
In rich ammonia logistics stripped to the condensate liquid logistics from upstream units containing ammonia and the buck from grey water pretreatment system carry out
Separation, rich ammonia logistics is sent to ammonia recovery system after obtained stripping, using the ammonia condensing and purification recovery device of ammonia recovery unit,
After the richness ammonia logistics is further processed removal sour gas, the ammonolysis product of high ammon amount is obtained；Warp in condensate liquid stripper plant
Condensate liquid logistics discharge system is recycled or is further processed after the stripping generated after separation, and the sour gas of generation is sent into downstream
Unit is further processed.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201910670147.4A CN110342717A (en) | 2019-07-24 | 2019-07-24 | Gasification energy couples ammonia recovery system and method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201910670147.4A CN110342717A (en) | 2019-07-24 | 2019-07-24 | Gasification energy couples ammonia recovery system and method |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN110342717A true CN110342717A (en) | 2019-10-18 |
Family
ID=68180000
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201910670147.4A Pending CN110342717A (en) | 2019-07-24 | 2019-07-24 | Gasification energy couples ammonia recovery system and method |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN110342717A (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111115734A (en) * | 2020-01-21 | 2020-05-08 | 恒力石化（大连）炼化有限公司 | Device and process for treating flash evaporation condensate of coal water slurry gasification system |
| CN114314977A (en) * | 2021-11-24 | 2022-04-12 | 国家能源集团煤焦化有限责任公司 | Method and system for recycling conversion condensate |
| CN116354480A (en) * | 2023-03-30 | 2023-06-30 | 实联化工(江苏)有限公司 | Torch sewage treatment device and process |
Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108911338A (en) * | 2018-08-17 | 2018-11-30 | 通用电气神华气化技术有限公司 | A kind of recovery ammonia total system and method |
-
2019
- 2019-07-24 CN CN201910670147.4A patent/CN110342717A/en active Pending
Patent Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108911338A (en) * | 2018-08-17 | 2018-11-30 | 通用电气神华气化技术有限公司 | A kind of recovery ammonia total system and method |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111115734A (en) * | 2020-01-21 | 2020-05-08 | 恒力石化（大连）炼化有限公司 | Device and process for treating flash evaporation condensate of coal water slurry gasification system |
| CN114314977A (en) * | 2021-11-24 | 2022-04-12 | 国家能源集团煤焦化有限责任公司 | Method and system for recycling conversion condensate |
| CN116354480A (en) * | 2023-03-30 | 2023-06-30 | 实联化工(江苏)有限公司 | Torch sewage treatment device and process |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN107434335B (en) | Comprehensive treatment method for recycling semi-coke wastewater phenol ammonia | |
| US4314077A (en) | Method for the production of urea and purification of water | |
| CN110342717A (en) | Gasification energy couples ammonia recovery system and method | |
| CN110740801A (en) | Method and device for cleaning gas with at least two injection phases and use | |
| CN105967425A (en) | Coal chemical industry grey water flashing treatment system capable of reducing ammonia accumulation and coal chemical industry grey water flashing treatment process capable of reducing ammonia accumulation | |
| KR100407370B1 (en) | METHOD AND APPARATUS FOR RECOVERING INTEGRATED VAPOR CONDENSATE FROM URGENT VACUUM EVAPORATOR | |
| CN111847478B (en) | Comprehensive treatment process for conversion condensate | |
| CN106000000A (en) | Device and method for performing multistage flash, resolution and separation on synthetic ammonia decarburization absorption tower bottom pregnant solution | |
| CN107823906B (en) | crude gas conversion process condensate steam stripping treatment system and method | |
| CN114634400A (en) | Method and production system for synthesizing methanol by using carbon dioxide | |
| CN109319736B (en) | Ammonia tank purge gas recovery device and process thereof | |
| CN214936766U (en) | Phenol ammonia sewage single tower processing system | |
| CN214114973U (en) | CO conversion condensate refining process system | |
| EA011378B1 (en) | Process for increasing the capacity of an urea plant | |
| US4102650A (en) | Process feed and effluent treatment systems | |
| CN108911338A (en) | A kind of recovery ammonia total system and method | |
| CN208995304U (en) | A kind of recovery ammonia total system | |
| CN112979516B (en) | Energy-saving methyl mercaptan synthesis device | |
| CN114409573A (en) | Improved low energy CO2Urea process by steam stripping method | |
| CN211159192U (en) | Processing apparatus of acid water is retrieved to claus sulphur | |
| CN104030316B (en) | The novel process of anhydrous ammonia produced by a kind of raw gas | |
| CN108249501B (en) | Coal gas water treatment system of Lurgi furnace gasification anthracite device | |
| RU2258063C2 (en) | Method for preparing urea (variants), device for preparing urea and method for device updating | |
| CN220467588U (en) | Change condensate ammonia resource recovery unit | |
| CN220951267U (en) | Double-tower efficient ammonia stripping device for changing condensate |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| WD01 | Invention patent application deemed withdrawn after publication |
Application publication date: 20191018 |
|
| WD01 | Invention patent application deemed withdrawn after publication |