CN205328783U - A desulfurization deamination system for direct liquefaction of coal sewage treatment - Google Patents
A desulfurization deamination system for direct liquefaction of coal sewage treatment Download PDFInfo
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- CN205328783U CN205328783U CN201521009599.1U CN201521009599U CN205328783U CN 205328783 U CN205328783 U CN 205328783U CN 201521009599 U CN201521009599 U CN 201521009599U CN 205328783 U CN205328783 U CN 205328783U
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Abstract
The utility model discloses a desulfurization deamination system for direct liquefaction of coal sewage treatment, including conveying unit, hydrogen sulfide strip unit, first heat exchanger, ammonia strip unit, second heat exchanger and first cooler. The utility model discloses hydrogen sulfide and ammonia in the desorption direct liquefaction of coal sewage make the dirty water purification of whole direct liquefaction of coal high -efficiently go on smoothly.
Description
Technical field
This utility model relates to sewage treatment area, particularly relates to a kind of desulfurization deamination system for DCL/Direct coal liquefaction sewage disposal。
Background technology
Increasingly serious along with China's water scarcity situation, Green GDP construction that especially country advocates energetically and the proposition of recycling economy, make industrial water saving reduce discharging particularly important with utilization of wastewater resource。Therefore how economical, improve enterprise's water resources comprehensive utilization rate even up to " zero-emission " standard efficiently, reliably, be that enterprise meets country, local government's environmental requirement, establish the important process of the responsible image of enterprise。
Firing Shenhua Coal direct liquefaction project is China is also first coal direct liquefaction commerciality construction project in the world, DCL/Direct coal liquefaction, stabilized hydrogenation, hydro-upgrading process are reacted the hydrogen sulfide of generation, ammonia, aldehydes matter after water filling is rinsed, produces high-concentration sewage, hydrogen sulfide in water, ammonia content up to 16000mg/L, aldehydes matter content more than 5000mg/L, in addition, the part oil that coal liquefaction hydrogenation process produces is present in high-concentration sewage with emulsifying state。Sulfur, ammonia contaminant content are high and contain the aldehydes matter of higher concentration simultaneously, oil in sewage is difficult to elimination, these unfavorable factors are processed all to DCL/Direct coal liquefaction high-concentration sewage and bring huge challenge, in addition the requirement of " zero " discharge and reusing sewage, further increases difficulty and the requirement of sewage disposal。Therefore, generally speaking, these quantity of wastewater effluent are big, and complicated component, and impurity content is high, when at home and abroad not having similar sewage disposal experience to be available for using for reference, deal with difficulty very big。
To sum up, in order to make sulfur in DCL/Direct coal liquefaction sewage and ammonia remove smoothly, in order to whole DCL/Direct coal liquefaction dirt water purification, it is necessary to provide a kind of desulfurization deamination system for DCL/Direct coal liquefaction sewage disposal。
Utility model content
The purpose of this utility model is in that to provide a kind of desulfurization deamination system for DCL/Direct coal liquefaction sewage disposal, to remove hydrogen sulfide in DCL/Direct coal liquefaction sewage and ammonia smoothly, makes whole DCL/Direct coal liquefaction dirt water purification efficiently to carry out。
For achieving the above object, this utility model is by the following technical solutions:
A kind of desulfurization deamination system for DCL/Direct coal liquefaction sewage disposal, described desulfurization deamination system includes:
Supply unit, for sending DCL/Direct coal liquefaction sewage into hydrogen sulfide steam stripping unit；
Hydrogen sulfide steam stripping unit, described hydrogen sulfide steam stripping unit includes de-hydrogen sulfide column and the first reboiler with the supporting setting of described de-hydrogen sulfide column, wherein, described de-hydrogen sulfide column includes column plate section and packing section, is provided with first paragraph filler and is positioned at the second segment filler below described first paragraph filler in described packing section；Described de-hydrogen sulfide column is arranged over overhead reflux mouth at first paragraph filler, and described de-hydrogen sulfide column is provided with the first sewage inlet between first paragraph filler and second segment filler, for receiving the part of coal direct liquefaction sewage from described supply unit；Described de-hydrogen sulfide column is provided with the second sewage inlet in the bottom of described column plate section；Described hydrogen sulfide steam stripping unit, for DCL/Direct coal liquefaction sewage is stripped, to obtain hydrogen sulfide gas at tower top, is obtaining Waste Water Containing Sulfur at the bottom of tower；
First Heat Exchanger, for making another part DCL/Direct coal liquefaction sewage from described supply unit heat up with the Waste Water Containing Sulfur heat exchange from described de-hydrogen sulfide column, and DCL/Direct coal liquefaction sewage described second sewage inlet of feeding after will heat up；
Ammonia steam stripping unit, described ammonia steam stripping unit includes deammoniation tower, and described ammonia steam stripping unit, for the Waste Water Containing Sulfur from described First Heat Exchanger is stripped, to obtain thick ammonia at tower top, is obtaining deamination sewage at the bottom of tower；
Second heat exchanger, for making the DCL/Direct coal liquefaction sewage waiting to enter described First Heat Exchanger heat up with the deamination sewage heat change from described deammoniation tower；With
First cooler, for cooling down deamination sewage from described two heat exchangers, and sends into described overhead reflux mouth using the deamination sewage after part cooling as the overhead reflux of described hydrogen sulfide stripping tower。
According to desulfurization deamination system of the present utility model, it is preferable that described desulfurization deamination system also includes oil-water separation unit, carry out oil-water separation with the DCL/Direct coal liquefaction sewage that pending desulfurization deamination is processed。
According to desulfurization deamination system of the present utility model, it is preferable that described oil-water separation unit includes:
Degrease water pot, for making the DCL/Direct coal liquefaction sewage stratification of oil-containing and separating oil phase；With
Grease trap, for removing from the oil phase in the DCL/Direct coal liquefaction sewage of the described water pot that degreases further。
According to desulfurization deamination system of the present utility model, it is preferable that described ammonia steam stripping unit includes:
Deammoniation tower, for the Waste Water Containing Sulfur from described First Heat Exchanger is stripped, to obtain thick ammonia at tower top, is obtaining deamination sewage at the bottom of tower；
The second reboiler with the supporting setting of described deammoniation tower；
Second cooler, for cooling down the thick ammonia from described deammoniation tower tower top；With
Return tank of top of the tower, for receiving from the thick ammonia of described first cooler and as overhead reflux, wherein isolated condensed fluid being sent into described deammoniation tower。
According to desulfurization deamination system of the present utility model, it is preferable that described desulfurization deamination system also includes ammonia recovery unit, and described ammonia recovery unit includes:
3rd cooler, for cooling down the thick ammonia from described return tank of top of the tower；
Rich ammonia fractional condensation tank, for separating the condensed fluid in the thick ammonia of described 3rd cooler, and will obtain richness ammonia and send from tank deck；
Rich ammonia washing tank, is provided with filler in described rich ammonia washing tank, for the rich ammonia from described rich ammonia fractional condensation tank carries out the spray washing of rich ammoniacal liquor, the rich ammonia after being washed；
Ammonia crystallizer, is used for the crystallization impurity under liquefied ammonia freezes of the rich ammonia after making washing；
Ammonia refining tank, for making the rich ammonia from described ammonia crystallizer carry out desulfurization adsorption treatment under the effect of desulfuration adsorbent；
Ammonia absorber, for utilizing the weak ammonia from ammonia distillation column that the rich ammonia from described ammonia refining tank is absorbed, in order to obtaining strong aqua ammonia at the bottom of tower；
Ammonia distillation column, for being heated from the strong aqua ammonia at the bottom of described ammonia absorber tower, to evaporate ammonia, and is obtaining weak ammonia at the bottom of tower；With
3rd heat exchanger, for by the weak ammonia from ammonia distillation column and the strong aqua ammonia heat exchange from ammonia absorber。
According to desulfurization deamination system of the present utility model, it is preferable that be provided with cooling tube bundle in described ammonia distillation column, described cooling tube bundle is arranged at described ammonia distillation column top, cools down for treating the ammonia drawing described ammonia distillation column。
According to desulfurization deamination system of the present utility model, it is preferable that described ammonia refining tank is provided with two, respectively the first ammonia refining tank and the second ammonia refining tank, described first ammonia refining tank and the second ammonia refining tank are arranged in series。
According to desulfurization deamination system of the present utility model, it is preferable that described ammonia recovery unit also includes:
4th cooler, for making the ammonia condensation of the described ammonia distillation column of extraction；
Ammonia tank, is provided with Fen Shuibao in described ammonia tank, for receiving the liquefied ammonia from described 4th cooler, and isolates the water in liquefied ammonia；
Liquid ammonia storage tank, for receiving the liquefied ammonia from described ammonia tank；With
Pressure-equalizing line, one end of described pressure-equalizing line is connected to ammonia distillation column top, and the other end is connected to the top of described liquid ammonia storage tank, is used for making described ammonia distillation column keep gas phase to connect with liquid ammonia storage tank。
Desulfurization deamination system of the present utility model, has the advantage that
1, in DCL/Direct coal liquefaction, stabilized hydrogenation, hydro-upgrading process, react the hydrogen sulfide of generation, ammonia, aldehydes matter after water filling is rinsed, produce high-concentration sewage, hydrogen sulfide in water, ammonia content up to 16000mg/L, aldehydes matter content more than 5000mg/L, in addition, the part oil that coal liquefaction hydrogenation process produces is present in high-concentration sewage with emulsifying state, sewage complicated component。For this, this utility model takes into full account the impact of Oil in Sewage Water and aldehydes matter, have selected double tower stripping process and sewage is processed。Additionally, the existence of sulfur is bigger on follow-up dephenolize impact, it is therefore desirable to preferential desulfurization, although the sewage elder generation deamination after desulfurization or first dephenolize have feasibility in theory, but take into full account that too high ammonia content is very easily in problems such as the ether gassy system of extracting and dephenolizing device result in blockage, in addition to process system higher to the requirement of pollutant extrusion rate for downstream wastewater, therefore selects to carry out phenol removal after deamination, thus the complicated sewage of mentioned component can obtain reasonable, effectively process。
2, in this utility model, thick ammonia circulates washing process and low temperature crystallization technique and two-step desulfurization agent absorption, the ammonia being purified through strong aqua ammonia。Gas ammonia after refining enters back into be absorbed by weak ammonia in absorption tower and obtains strong aqua ammonia, is sent into by strong aqua ammonia and carries out distilation in ammonia distillation column, such that it is able to obtain the liquefied ammonia that purity is more than 99.5% (wt%)。
Accompanying drawing explanation
Fig. 1 is the schematic diagram of a kind of embodiment of desulfurization deamination system of the present utility model；
Fig. 2 is the schematic diagram of ammonia recovery unit of the present utility model。
Detailed description of the invention
Below in conjunction with accompanying drawing, this utility model is described in detail, it is understood that, this utility model is not limited to that。
Fig. 1 illustrates a kind of desulfurization deamination system for DCL/Direct coal liquefaction sewage disposal that this utility model provides, and described desulfurization deamination system includes supply unit (not shown), hydrogen sulfide steam stripping unit 1, First Heat Exchanger 2, ammonia steam stripping unit the 3, second heat exchanger 4 and the first cooler 5。
Wherein, described supply unit is for sending DCL/Direct coal liquefaction sewage into hydrogen sulfide steam stripping unit 1, and described supply unit can be liquid transporting apparatus commonly used in the art, for instance centrifugal pump etc., for known in the art, repeats no more here。
Described hydrogen sulfide steam stripping unit 1 includes de-hydrogen sulfide column 11 and boils 15 devices with the first of the supporting setting of described de-hydrogen sulfide column again, wherein, described de-hydrogen sulfide column 11 includes column plate section 14 and is positioned at the packing section above described column plate section 14, is provided with first paragraph filler 12 and is positioned at the second segment filler 13 below described first paragraph filler 12 in described packing section；Described de-hydrogen sulfide column 11 is arranged over overhead reflux mouth (not marking in figure) at first paragraph filler 12, thus receiving the deamination water from described ammonia steam stripping unit 3, as overhead reflux liquid；Described de-hydrogen sulfide column 11 is provided with the first sewage inlet (not marking in figure) between first paragraph filler 12 and second segment filler 13, for receiving the part of coal direct liquefaction sewage from described supply unit；Described de-hydrogen sulfide column 11 is provided with the second sewage inlet (not marking in figure) in the bottom of described column plate section 14；Described hydrogen sulfide steam stripping unit 1, for DCL/Direct coal liquefaction sewage is stripped, to obtain hydrogen sulfide gas at tower top, is obtaining Waste Water Containing Sulfur at the bottom of tower。Preferably, the tower tray of described column plate section 14 is the three-dimensional tower tray of film injection, to overcome tradition float valve tray to be affected, by oil, aldehydes matter and coal dust comprehensive function, the problem that cannot meet sewage disposal requirement。
During operation, sewage enters de-hydrogen sulfide column respectively through first, second sewage inlet, utilizes H2S and NH3Dissolubility in water is different with volatility, first removes the hydrogen sulfide in sewage, obtain Waste Water Containing Sulfur under heating and stripping effect。Owing to whole stripping operation is based on volatile weak electrolyte aqueous solution vapour-liquid equilibrium at different conditions, thus the selection of de-hydrogen sulfide column and deammoniation tower operating condition is most important。It is said that in general, de-hydrogen sulfide column operates under a certain pressure, be conducive to NH3It is dissolved in water, and to H2The impact of S is less, therefore for obtaining the H of high concentration2S-acid gas, it is necessary in de-hydrogen sulfide column, top set up the condition of elevated pressures and low temperature, carry out the process based on absorption distillation, make the NH in rising steam flow in tower3After being washed entrance liquid phase, with NH4HS、(NH4)2S form is " fixed ", for this, two sections of fillers are set on de-hydrogen sulfide column top, and the sewage inlet that temperature is relatively low are set between two sections of fillers, thus being conducive to the carrying out of above-mentioned absorption-distillation process。Due to higher containing ammonia in DCL/Direct coal liquefaction sewage, the H being stripped off2S still contains part NH3, in order to ensure NH3Removal effect and the operation temperature of tower top sour gas, adopt, at hydrogen sulfide stripping tower absorber portion, the packing section that contact area is bigger for this, to improve the absorption efficiency of washings, it is ensured that in sour gas, ammonia content does not exceed standard。Hypomere at tower is then resolve the above-mentioned ammonium salt being " fixed " the H that will parse2S and NH3Stripping and on, thus obtaining Waste Water Containing Sulfur at the bottom of de-hydrogen sulfide column, for this, column plate section is set in de-hydrogen sulfide column bottom, and the sewage inlet that temperature is higher is set at column plate pars infrasegmentalis, thus being conducive to the carrying out of above-mentioned resolving。
Described First Heat Exchanger 2 is for making another part DCL/Direct coal liquefaction sewage from described supply unit heat up with the Waste Water Containing Sulfur heat exchange from described de-hydrogen sulfide column 11, and DCL/Direct coal liquefaction sewage described second sewage inlet of feeding after will heat up；Described second heat exchanger 4, for making to wait that the DCL/Direct coal liquefaction sewage entering described First Heat Exchanger 2 heats up with the deamination sewage heat change from described ammonia steam stripping unit 3, by twice heat exchange, saves energy consumption。Described first, second heat exchanger can be the liquid-liquid heat exchanger that this area is conventional, for known in the art, repeats no more here。
Described first cooler 5 is for cooling down the deamination sewage from described second heat exchanger 4, and using part cooling after deamination sewage as described hydrogen sulfide stripping tower 11 overhead reflux send into described overhead reflux mouth, forming the overhead reflux of de-hydrogen sulfide column 11, all the other sewage are sent to subsequent processing units。
Described ammonia steam stripping unit 3 includes deammoniation tower 31, and described ammonia steam stripping unit 3, for the Waste Water Containing Sulfur from described First Heat Exchanger 2 is stripped, to obtain thick ammonia at tower top, is obtaining deamination sewage at the bottom of tower。In a kind of embodiment of the present utility model, described ammonia steam stripping unit 3 includes deammoniation tower the 31, second cooler 33, return tank of top of the tower 34 and the second reboiler 32 with the described supporting setting of deammoniation tower 31。Wherein, described deammoniation tower 31, for the Waste Water Containing Sulfur from described First Heat Exchanger 2 is stripped, to obtain thick ammonia at tower top, is obtaining deamination sewage at the bottom of tower；Described second cooler 33 is for cooling down the thick ammonia from described deammoniation tower 31 tower top, in order to condense moisture therein；Described return tank of top of the tower 34 is for receiving from the thick ammonia of described second cooler 33 and as overhead reflux, wherein isolated condensed fluid being sent into described deammoniation tower 31。For the operation logic of above-mentioned deammoniation tower 31, it should be readily apparent to one skilled in the art that and repeat no more here。
Oil-water separation unit
In a kind of embodiment of the present utility model, described desulfurization deamination unit also includes oil-water separation unit (not shown), carries out oil-water separation with the DCL/Direct coal liquefaction sewage that pending desulfurization deamination is processed。Described oil-water separation unit can be oily-water seperating equipment commonly used in the art, for instance carried out the device of oil-water separation by profit density contrast。In one embodiment, described oil-water separation unit includes degrease water pot and grease trap, described in degrease water pot for making the DCL/Direct coal liquefaction sewage stratification of oil-containing and separating oil phase；Described grease trap is for removing from the oil phase in the DCL/Direct coal liquefaction sewage of the described water pot that degreases further。Described degrease water pot and grease trap is known in the art, repeat no more here。Sewage handled by this utility model is DCL/Direct coal liquefaction sewage, by the pretreatment of oil-water separation unit, it is possible to effectively remove the oil phase in sewage so that follow-up process is got twice the result with half the effort。
Ammonia recovery unit
In a kind of embodiment of the present utility model, as shown in Figure 2, described desulfurization deamination unit also includes ammonia recovery unit, and described ammonia recovery unit includes the 3rd cooler 61, rich ammonia fractional condensation tank 62, rich ammonia washing tank 63, ammonia crystallizer 65, ammonia refining tank 66, ammonia absorber 67, ammonia distillation column 68 and the 3rd heat exchanger 69。
Wherein, described 3rd cooler 61 is for cooling down the thick ammonia from described return tank of top of the tower 34, thus reducing temperature further (for controlling the tower top temperature of deammoniation tower 31, it is too low that second condenser 33 should not make temperature be down to), so that moisture therein condenses further, part sulfur-containing compound can be dissolved simultaneously；Described rich ammonia fractional condensation tank 62 is for separating from the condensed fluid (condensed fluid under gravity, comes together in tank bottoms and discharges in rich ammonia fractional condensation tank 62) in the thick ammonia of described 3rd cooler 61, and will obtain richness ammonia and send from tank deck。
It is provided with filler 64, for the rich ammonia from described rich ammonia fractional condensation tank 62 being carried out the spray washing of rich ammoniacal liquor, the rich ammonia after being washed in described rich ammonia washing tank 63。Specifically, rich ammonia enters bottom washing tank 63, is fully contacted with rich ammoniacal liquor adverse current, completes mass transport process on filler 64 surface in uphill process。Transfer to the H in rich ammoniacal liquor2S and NH3Reaction generates NH4HS or (NH4)2S, is fixed in liquid phase, thus completing H in gas phase2The washing absorption of S。Wherein, described rich ammoniacal liquor is preferably the strong aqua ammonia from described ammonia absorber, and using the part richness ammoniacal liquor after washing as circulating cleaning solution。It will be understood by those skilled in the art that the utilization rich ammoniacal liquor rich ammonia of washing, it is possible to absorb more sulfur-containing compound, further ammonia removal when absorbing less ammonia；Simultaneously as arrange filler, favourable rich ammoniacal liquor is fully contacted with rich ammonia, improves assimilation effect。
Described ammonia crystallizer 65 is used for the crystallization impurity under liquefied ammonia freezes of the rich ammonia after making washing, for instance NH4HS、(NH4)2S；Described ammonia crystallizer 65 can be ammonia crystallizer commonly used in the art, for instance purchased from the ammonia crystallizer of Aerosun Corp。
It is provided with desulfuration adsorbent, for making the rich ammonia from described ammonia crystallizer 65 carry out desulfurization adsorption treatment under the effect of desulfuration adsorbent, with further ammonia removal in described ammonia refining tank 66；Wherein, described desulfuration adsorbent is known in the art, for instance JX-4A type desulfuration adsorbent。Preferably, described ammonia refining tank 66 is provided with two, respectively the first ammonia refining tank and the second ammonia refining tank, and described first ammonia refining tank and the second ammonia refining tank are arranged in series, to improve desulfurized effect。
Described ammonia absorber 67 is for utilizing the weak ammonia from ammonia distillation column 68 that the rich ammonia from described ammonia refining tank 66 is absorbed, in order to obtaining strong aqua ammonia at the bottom of tower；This absorption tower is known in the art, for instance material filling type absorption tower or column plate type absorption tower, repeats no more here。
Described ammonia distillation column 68, for being heated from the strong aqua ammonia at the bottom of described ammonia absorber 67 tower, to evaporate ammonia, and is obtaining weak ammonia at the bottom of tower。In one embodiment, being additionally provided with cooling tube bundle 70 in described ammonia distillation column 68, described cooling tube bundle 70 is arranged at described ammonia distillation column 68 top, cools down for treating the ammonia drawing described ammonia distillation column 68, so that wherein condensate moisture, minimizing is carried secretly。
Described 3rd heat exchanger 69 is for by the weak ammonia from ammonia distillation column 68 and the strong aqua ammonia heat exchange from ammonia absorber 67, with energy-saving and cost-reducing。Described 3rd heat exchanger 69 can be the liquid-liquid heat exchanger that this area is conventional, repeats no more here。
In a preferred implementation of the present utility model, described ammonia recovery unit also includes the 4th cooler 72, ammonia tank 73, liquid ammonia storage tank 75 and pressure balance line 76。Wherein, described 4th cooler 72, for making the ammonia condensation of the described ammonia distillation column 68 of extraction, to obtain liquefied ammonia。Described 4th cooler 72 can be conventional water cooler, it will be understood by those skilled in the art that owing to operation temperature is high, can make ammonia condensation by water-cooled。
Being provided with a point oil bag 74 in described ammonia tank 73, for receiving the liquefied ammonia from described 4th cooler 72, and isolate the oil in liquefied ammonia, described point of oil bag 74 is known in the art, by settlement action, to isolate the oil in liquefied ammonia。
Described liquid ammonia storage tank 75 is for receiving and store the liquefied ammonia from described ammonia tank 73。
One end of described pressure-equalizing line 76 is connected to ammonia distillation column 68 top, and the other end is connected to the top of described liquid ammonia storage tank 75, is used for making described ammonia distillation column 68 keep gas phase to connect with liquid ammonia storage tank 75, to keep pressure balance, is conducive to liquefied ammonia to store。
As illustrated in fig. 1 and 2, during carrying out practically, when above-mentioned desulfurization deamination unit runs, DCL/Direct coal liquefaction sewage first passes through and degreases water pot and grease trap carries out oil-water separation, is then directly entered first sewage inlet on de-hydrogen sulfide column top through conveyer device rear portion as cold feed；Another part is warming up to 115 DEG C through First Heat Exchanger with deamination water (pressure 1.1MPa) heat exchange from described ammonia steam stripping unit, then further heat up to 137 DEG C with the desulfurization water heat exchange drawn from de-hydrogen sulfide column then through the second heat exchanger, enter de-hydrogen sulfide column from described second sewage inlet。In the middle part of the deamination water of First Heat Exchanger, lease making is crossed and is entered depriving hydrogen sulphide top of tower from overhead reflux mouth after the first cooler is cooled to 35 DEG C, forms backflow and controls tower top temperature；All the other send (being designated as sewage W1, leading indicator is in Table 2)。Sewage flows from top to bottom in de-hydrogen sulfide column, under the stripping effect that depriving hydrogen sulphide bottom reboiler provides thermal source to produce, rich in H2The sour gas of S composition draws (pressure 0.6MPa, sour gas index is in Table 2) from tower top, it is possible to be sent to sulfur recovery facility under voltage-controlled further。Deammoniation tower is entered from the desulfurization water of 162 DEG C drawn at the bottom of de-hydrogen sulfide column self-pressure after the second heat exchanger is cooled to 143 DEG C, under the stripping effect that deamination bottom reboiler provides thermal source to produce, thick ammonia is drawn from tower top, it is cooled to 80 DEG C of return tank of top of the tower entering deammoniation tower through deamination tower top the second cooler and carries out gas-liquid separation, liquid phase sends into deammoniation tower top as flowing backward through deamination overhead reflux pump under stream control, and isolated thick ammonia send ammonia recovery unit to reclaim ammonia。
When described ammonia recovery unit runs, isolated thick ammonia enters rich ammonia fractional condensation tank after the 3rd cooler is cooled to 40 DEG C, is removed H further2The rich ammonia of S, described rich ammonia delivers to rich ammonia washing tank through rich ammonia fractional condensation tank top under voltage-controlled。Rich ammonia washs through strong aqua ammonia in rich ammonia washing tank, after elimination partial vulcanization hydrogen, send into ammonia crystallizer, under liquefied ammonia sweat cooling so that it is in NH4HS and/or (NH4)2S crystallization, then removes H further through two-stage ammonia refining tank2Send into bottom ammonia absorber after S。Ammonia is absorbed by the weak ammonia come from ammonia distillation column in ammonia absorber, send under voltage-controlled for absorbed tower overhead gas, the strong aqua ammonia self-absorption tower bottom obtained boosts to 2.0MPa through pump, then ammonia distillation column is entered through the 3rd heat exchanger heat exchange to 165 DEG C, bottom reboiler heating evaporation through ammonia distillation column, ammonia distillation column top is provided with cooling tube bundle, and the gas that recirculated water evaporates in cooling tube bundle is by tower condenses to form backflow, and residue ammonia is drawn from ammonia overhead。
The ammonia distilling tower top from ammonia enters ammonia tank after the 4th cooler condensation, is further separated out the oil of remaining, then delivers to liquid ammonia storage tank under hydraulic control and store (pressure 11.6MPa) under the effect of Fen Youbao。Liquefied ammonia in liquid ammonia storage tank is sent (liquefied ammonia product index is in Table 2) mostly as product, and fraction controls its operation temperature after being sent to the gasification of ammonia crystallizer。
The character of table 1 DCL/Direct coal liquefaction sewage
The major product character of table 2 desulfurization deamination unit
(in table " ≯ " represent be not more than, " ≮ " represent be not less than)
Claims (8)
1., for a desulfurization deamination system for DCL/Direct coal liquefaction sewage disposal, described desulfurization deamination system includes:
Supply unit, for sending DCL/Direct coal liquefaction sewage into hydrogen sulfide steam stripping unit；
Hydrogen sulfide steam stripping unit, described hydrogen sulfide steam stripping unit includes de-hydrogen sulfide column and the first reboiler with the supporting setting of described de-hydrogen sulfide column, wherein, described de-hydrogen sulfide column includes column plate section and packing section, is provided with first paragraph filler and is positioned at the second segment filler below described first paragraph filler in described packing section；Described de-hydrogen sulfide column is arranged over overhead reflux mouth at first paragraph filler, and described de-hydrogen sulfide column is provided with the first sewage inlet between first paragraph filler and second segment filler, for receiving the part of coal direct liquefaction sewage from described supply unit；Described de-hydrogen sulfide column is provided with the second sewage inlet in the bottom of described column plate section；Described hydrogen sulfide steam stripping unit, for DCL/Direct coal liquefaction sewage is stripped, to obtain hydrogen sulfide gas at tower top, is obtaining Waste Water Containing Sulfur at the bottom of tower；
First Heat Exchanger, for making another part DCL/Direct coal liquefaction sewage from described supply unit heat up with the Waste Water Containing Sulfur heat exchange from described de-hydrogen sulfide column, and DCL/Direct coal liquefaction sewage described second sewage inlet of feeding after will heat up；
Ammonia steam stripping unit, described ammonia steam stripping unit includes deammoniation tower, and described ammonia steam stripping unit, for the Waste Water Containing Sulfur from described First Heat Exchanger is stripped, to obtain thick ammonia at tower top, is obtaining deamination sewage at the bottom of tower；
Second heat exchanger, for making the DCL/Direct coal liquefaction sewage waiting to enter described First Heat Exchanger heat up with the deamination sewage heat change from described deammoniation tower；With
First cooler, for cooling down deamination sewage from described two heat exchangers, and sends into described overhead reflux mouth using the deamination sewage after part cooling as the overhead reflux of described hydrogen sulfide stripping tower。
2. desulfurization deamination system according to claim 1, it is characterised in that described desulfurization deamination system also includes oil-water separation unit, carries out oil-water separation with the DCL/Direct coal liquefaction sewage that pending desulfurization deamination is processed。
3. desulfurization deamination system according to claim 2, it is characterised in that described oil-water separation unit includes:
Degrease water pot, for making the DCL/Direct coal liquefaction sewage stratification of oil-containing and separating oil phase；With
Grease trap, for removing from the oil phase in the DCL/Direct coal liquefaction sewage of the described water pot that degreases further。
4. the desulfurization deamination system according to any one of claim 1-3, it is characterised in that described ammonia steam stripping unit includes:
Deammoniation tower, for the Waste Water Containing Sulfur from described First Heat Exchanger is stripped, to obtain thick ammonia at tower top, is obtaining deamination sewage at the bottom of tower；
The second reboiler with the supporting setting of described deammoniation tower；
Second cooler, for cooling down the thick ammonia from described deammoniation tower tower top；With
Return tank of top of the tower, for receiving from the thick ammonia of described first cooler and as overhead reflux, wherein isolated condensed fluid being sent into described deammoniation tower。
5. desulfurization deamination system according to claim 4, it is characterised in that described desulfurization deamination system also includes ammonia recovery unit, and described ammonia recovery unit includes:
3rd cooler, for cooling down the thick ammonia from described return tank of top of the tower；
Rich ammonia fractional condensation tank, for separating the condensed fluid in the thick ammonia of described 3rd cooler, and will obtain richness ammonia and send from tank deck；
Rich ammonia washing tank, is provided with filler in described rich ammonia washing tank, for the rich ammonia from described rich ammonia fractional condensation tank carries out the spray washing of rich ammoniacal liquor, the rich ammonia after being washed；
Ammonia crystallizer, is used for the crystallization impurity under liquefied ammonia freezes of the rich ammonia after making washing；
Ammonia refining tank, for making the rich ammonia from described ammonia crystallizer carry out desulfurization adsorption treatment under the effect of desulfuration adsorbent；
Ammonia absorber, for utilizing the weak ammonia from ammonia distillation column that the rich ammonia from described ammonia refining tank is absorbed, in order to obtaining strong aqua ammonia at the bottom of tower；
Ammonia distillation column, for being heated from the strong aqua ammonia at the bottom of described ammonia absorber tower, to evaporate ammonia, and is obtaining weak ammonia at the bottom of tower；With
3rd heat exchanger, for by the weak ammonia from ammonia distillation column and the strong aqua ammonia heat exchange from ammonia absorber。
6. desulfurization deamination system according to claim 5, it is characterised in that be provided with cooling tube bundle in described ammonia distillation column, described cooling tube bundle is arranged at described ammonia distillation column top, cools down for treating the ammonia drawing described ammonia distillation column。
7. desulfurization deamination system according to claim 6, it is characterised in that described ammonia refining tank is provided with two, respectively the first ammonia refining tank and the second ammonia refining tank, described first ammonia refining tank and the second ammonia refining tank are arranged in series。
8. desulfurization deamination system according to claim 6, it is characterised in that described ammonia recovery unit also includes:
4th cooler, for making the ammonia condensation of the described ammonia distillation column of extraction；
Ammonia tank, is provided with Fen Shuibao in described ammonia tank, for receiving the liquefied ammonia from described 4th cooler, and isolates the water in liquefied ammonia；
Liquid ammonia storage tank, for receiving the liquefied ammonia from described ammonia tank；With
Pressure-equalizing line, one end of described pressure-equalizing line is connected to ammonia distillation column top, and the other end is connected to the top of described liquid ammonia storage tank, is used for making described ammonia distillation column keep gas phase to connect with liquid ammonia storage tank。
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| CN107235593A (en) * | 2017-07-03 | 2017-10-10 | 天津晟远环境有限公司 | The system and method that a kind of coal gasification water system recovery ammonia is removed with sulphur |
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