CN102634381A - System and method for treating benzene-contained separating water of coking benzol - Google Patents
System and method for treating benzene-contained separating water of coking benzol Download PDFInfo
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- CN102634381A CN102634381A CN2012101042144A CN201210104214A CN102634381A CN 102634381 A CN102634381 A CN 102634381A CN 2012101042144 A CN2012101042144 A CN 2012101042144A CN 201210104214 A CN201210104214 A CN 201210104214A CN 102634381 A CN102634381 A CN 102634381A
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- gas
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- oil
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- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 title claims abstract description 470
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 title claims abstract description 43
- 238000004939 coking Methods 0.000 title claims abstract description 19
- 238000000034 method Methods 0.000 title claims abstract description 18
- 238000005406 washing Methods 0.000 claims abstract description 47
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims abstract description 46
- 239000000571 coke Substances 0.000 claims abstract description 27
- 229910021529 ammonia Inorganic materials 0.000 claims abstract description 23
- 238000004519 manufacturing process Methods 0.000 claims abstract description 9
- 238000010438 heat treatment Methods 0.000 claims abstract description 5
- 235000011114 ammonium hydroxide Nutrition 0.000 claims description 90
- UFWIBTONFRDIAS-UHFFFAOYSA-N Naphthalene Chemical compound C1=CC=CC2=CC=CC=C21 UFWIBTONFRDIAS-UHFFFAOYSA-N 0.000 claims description 84
- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 claims description 64
- 239000003921 oil Substances 0.000 claims description 62
- 125000004122 cyclic group Chemical group 0.000 claims description 54
- 239000003034 coal gas Substances 0.000 claims description 37
- YXFVVABEGXRONW-UHFFFAOYSA-N Toluene Chemical compound CC1=CC=CC=C1 YXFVVABEGXRONW-UHFFFAOYSA-N 0.000 claims description 27
- 238000001816 cooling Methods 0.000 claims description 21
- 239000007788 liquid Substances 0.000 claims description 16
- 235000008733 Citrus aurantifolia Nutrition 0.000 claims description 12
- 235000011941 Tilia x europaea Nutrition 0.000 claims description 12
- HIVLDXAAFGCOFU-UHFFFAOYSA-N ammonium hydrosulfide Chemical compound [NH4+].[SH-] HIVLDXAAFGCOFU-UHFFFAOYSA-N 0.000 claims description 12
- 239000004571 lime Substances 0.000 claims description 12
- 238000012546 transfer Methods 0.000 claims description 12
- 239000012530 fluid Substances 0.000 claims description 7
- 230000003068 static effect Effects 0.000 claims description 7
- 239000011259 mixed solution Substances 0.000 claims description 6
- 238000000926 separation method Methods 0.000 claims description 6
- 239000007921 spray Substances 0.000 claims description 6
- 230000005484 gravity Effects 0.000 claims description 5
- 238000009835 boiling Methods 0.000 claims description 4
- 230000008676 import Effects 0.000 claims description 3
- 239000000203 mixture Substances 0.000 claims description 3
- 238000012856 packing Methods 0.000 claims description 3
- 238000004064 recycling Methods 0.000 claims description 3
- 238000013022 venting Methods 0.000 claims description 2
- 230000000694 effects Effects 0.000 abstract description 5
- 239000000126 substance Substances 0.000 abstract description 2
- 230000008016 vaporization Effects 0.000 abstract description 2
- 238000005507 spraying Methods 0.000 abstract 1
- 239000011269 tar Substances 0.000 description 16
- 238000005516 engineering process Methods 0.000 description 9
- 238000011010 flushing procedure Methods 0.000 description 8
- 239000002253 acid Substances 0.000 description 4
- BFNBIHQBYMNNAN-UHFFFAOYSA-N ammonium sulfate Chemical compound N.N.OS(O)(=O)=O BFNBIHQBYMNNAN-UHFFFAOYSA-N 0.000 description 4
- 229910052921 ammonium sulfate Inorganic materials 0.000 description 4
- 235000011130 ammonium sulphate Nutrition 0.000 description 4
- 239000002641 tar oil Substances 0.000 description 4
- 238000010790 dilution Methods 0.000 description 3
- 239000012895 dilution Substances 0.000 description 3
- 238000005086 pumping Methods 0.000 description 3
- 238000000746 purification Methods 0.000 description 3
- 238000004140 cleaning Methods 0.000 description 2
- 238000009833 condensation Methods 0.000 description 2
- 230000005494 condensation Effects 0.000 description 2
- 230000003628 erosive effect Effects 0.000 description 2
- 238000012545 processing Methods 0.000 description 2
- 239000000243 solution Substances 0.000 description 2
- 239000002699 waste material Substances 0.000 description 2
- 238000010521 absorption reaction Methods 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 150000001555 benzenes Chemical class 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 238000005352 clarification Methods 0.000 description 1
- 238000011109 contamination Methods 0.000 description 1
- 235000019628 coolness Nutrition 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 230000007797 corrosion Effects 0.000 description 1
- 230000018044 dehydration Effects 0.000 description 1
- 238000006297 dehydration reaction Methods 0.000 description 1
- 238000006477 desulfuration reaction Methods 0.000 description 1
- 230000023556 desulfurization Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000004134 energy conservation Methods 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 239000012452 mother liquor Substances 0.000 description 1
- 239000005416 organic matter Substances 0.000 description 1
- 238000010025 steaming Methods 0.000 description 1
- 238000003860 storage Methods 0.000 description 1
- 230000009466 transformation Effects 0.000 description 1
- 238000005292 vacuum distillation Methods 0.000 description 1
- 238000009834 vaporization Methods 0.000 description 1
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- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
- Industrial Gases (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The invention belongs to the technical field of purifying coke oven gas, and relates to a system and method for treating benzene-contained separating water of coking benzol. The method comprises the following steps that: benzene-contained and oil-contained separating water which is separated in a benzol production process is fed to an inlet pipeline of a circulating ammonia pump through a pipeline; the benzene-contained and oil-contained separating water reaches the circulating ammonia pump through an inlet of the circulating ammonia pump; raw coke oven gas reaches a gas collecting pipe of a coke oven for spraying by pressurizing the circulating ammonia pump; heat exchange is carried out on the raw coke oven gas in the gas collecting pipe at a temperature of 780-850 DEG C; benzene matter is separated from water so as to rapidly volatilize to mix with gas due to heating effects of the raw coke oven gas at a high temperature, and enters a next benzene washing process with gas; the separating water in which the benzene is removed is mixed with an ammonia tar system; and finally, ammonia enters an ammonia vaporizing system for treatment and oil matter enters a tar system. According to the invention, the treatment efficiency of the benzene-contained separating water is high and the treatment speed of the benzene-contained separating water is high. Meanwhile, the conventional equipment and device in coking can be sufficiently used, so that the operation cost is low, the operation field conditions is improved, and the yield of chemical product of benzol is increased.
Description
Technical field
The invention belongs to the coke oven gas purification technical field, a kind of specifically coking crude benzene contains benzene and separates water treatment system and method.
Background technology
The coke-oven plant is in gas purification crude benzol production process; Owing to adopt washing oil that organism such as the benzene in the coal gas, toluene and naphthalene are sprayed absorption, absorbed and be sent to debenzolizing tower after the organic washing oil heating such as benzene, methylbenzene and naphthalene and take off benzene, take off naphthalene and handle.Domestic de-benzene process at debenzolizing tower mainly contains two kinds at present, and a kind of is to adopt steam to carry out malleation to distill, and feeds direct steaming of steam from tower bottom and blows, and the last branch of this technology is dried up more; Another kind is a vacuum distillation, adopts vacuum pump to extract certain vacuum tightness from top of tower, and benzene, naphthalene are separated from washing oil, and the water phase separated that this kind technology is separated at last is to few.But no matter be to adopt which kind of technology, it is dried up all can to produce branch at last.In addition, owing to adopt washing oil to wash benzene, wash that the oil-containing water of condensation of coal gas condensation gets into sloptank behind the benzene tower, be sent to the washing oil groove after the collection and carry out static dehydration, this part divides dried up when containing benzene, also contains the washing oil of part.Crude benzol production at present produces contains benzene to divide dried up all is to adopt pumping toward the suction gas line (after being effuser; One section gas line before the gas-liquid separator) or mechanizeding ammonia clarifying groove sneak in the ammonia water and tar oil system; Gas temperature is at 78-82 ℃ in the gas line owing to inhale, and the ammonia water and tar oil mixeding liquid temperature is at 75-80 ℃, and temperature is relatively all lower; Be lower than the boiling point of benzene, methylbenzene, contain benzene and divide dried up entering back volatilization slower.And it is nearer to inhale gas line distance Mechanical ammoniacal liquor clarifying tank (ammonia water and tar oil separator tank); Contain benzene divide benzene in dried up, methylbenzene also fully volatilization just arrive mechanizeding ammonia clarifying groove with ammonia water and tar oil, in the long-time static sepn process of clarifying tank, divide dried up in volatile matter such as remaining benzene volatilize in a large number; With exhaust emissions in atmosphere; Environment is on every side caused severe contamination, and the volatilization of a large amount of benzene gas, cause valuable benzene to waste.Overflow to the cyclic ammonia water medial launder again through the static ammoniacal liquor of separating of clarifying tank at last, again by the past effuser of cyclic ammonia water pumping.
Chinese patent " a kind of water saving, energy-conservation and reduce the coke oven gas purification novel process and the device of the equipment corrosion " patent No. is: 200910248854.0; This technology and device adopt the crude benzol in the crude benzol water distilling apparatus to divide the dried up final cooling tower of washing before the benzene that is sent to use as the circulation flushing liquor; Cold circulation fluid at end in the dilution final cooling tower, this process using crude benzol divides the end in the dried up dilution final cooling tower cold circulation fluid.Because the effect of dilution has reduced the concentration of acid in the whole cold circulation fluid to a certain extent, the last unnecessary circulation fluid in back that in final cooling tower, circulates is sent to complex acid and the spray saturex wash water of sulphur ammonium operation as ammonium sulfate device.This technology is to adopt crude benzol to divide dried up as the final cooling tower flushing liquor; Because crude benzol divides the dried up oil greatly that contains, and after getting into the final cooling tower circulation, is sent to sulphur ammonium operation; Make a large amount of washing oil to sulphur ammonium saturex; Make ammonium sulfate liquor band oil serious, influence the quality of sulphur ammonium, serious meeting makes finished product ammonium sulfate products blackout.In addition since at final cooling tower as flushing liquor, temperature is at 25-27 ℃; Temperature almost is in the normal temperature state, divides a large amount of benzene classes, oily substance in dried up to stay all the time in the flushing liquor, is sent to sulphur ammonium complex acid and uses; In the complex acid process, tank solution is stored in the ammonium sulfate liquor storage tank, under 50-55 ℃ mother liquor effect; The effusion of volatilizing easily of volatile matter such as benzene, the environment around polluting.
Chinese patent " the indirect final cooling tower circulation cleaning of a kind of coking technology " patent No. is: 200910067457.3, and this invention relates to the indirect final cooling tower circulation cleaning of a kind of coking technology, divides dried up and tar to spray in final cooling tower as mixing, washing liquid crude benzol; Flushing liquor after the circulation flows into the solution circulated groove at last; Unnecessary flushing liquor again through pumping toward the cold mechanizeding ammonia clarifying groove of drum, this technology is because flushing liquor gets into mechanizeding ammonia clarifying groove at last, in mechanizeding ammonia clarifying groove owing to stop; Rest time is longer; In groove, receive temperature 75-80 ℃ ammoniacal liquor effect, the benzene class material in the flushing liquor evaporate in the atmosphere easily, the environment around polluting; Waste a large amount of resources, cause crude benzol to divide dried up effective processing that can not get.
Summary of the invention
Technical problem to be solved by this invention is; Overcome the shortcoming of prior art; Provide a kind of coking crude benzene to contain benzene and separate water treatment system and method; The efficient of removing benzene, naphthalene is high, can not produce secondary pollution, solved simultaneously divide in the past dried up to the suction benzene gas pollution problem that gas line or mechanizeding ammonia clarifying groove produced.
The technical scheme that the present invention solves above technical problem is:
A kind of coking crude benzene contains benzene and separates water treatment system; Comprise underground emptying groove, cyclic ammonia water groove, coke oven collecting main and cyclic ammonia water pump; The cyclic ammonia water pump is arranged on the cyclic ammonia water pipe that the cyclic ammonia water groove is connected to coke oven collecting main; The front and back of cyclic ammonia water pipe cocycle aqua ammonia pump all are provided with valve, and the fluid inlet that underground emptying groove has connects crude benzol and divides dried up blow-down pipe, and the benzene butyraceous crude benzol that contains that crude benzol divides dried up blow-down pipe to carry the crude benzol production process to separate divides dried up to underground emptying groove; The crude benzol that is connected to underground emptying groove inner bottom part divides dried up transfer lime to be connected to the import of cyclic ammonia water pump; Crude benzol divides dried up transfer lime to be provided with vacuum primingpump; Crude benzol between vacuum primingpump and the cyclic ammonia water pump divides dried up transfer lime to be provided with valve, and the cyclic ammonia water pump divides crude benzol and dried uply is delivered to coke oven collecting main with ammoniacal liquor; The outlet of coke oven collecting main connects gas-liquid separator; The outlet at bottom of gas-liquid separator connects the ammoniacal liquor clarifying tank through the mixed solution pipeline; The top outlet of gas-liquid separator connects gas blower through the cooling oil eliminator; The outlet at bottom of ammoniacal liquor clarifying tank is connected to the tar medial launder, and the top outlet of ammoniacal liquor clarifying tank is connected to the cyclic ammonia water groove; The gas blower outlet connects thionizer, sulphur ammonium tower successively and washes the benzene tower; The outlet at bottom of washing the benzene tower is connected to debenzolizing tower through rich oil pump and oil gas interchanger successively; The top exit of debenzolizing tower is connected to the light benzene condensate cooler through the light benzene pipeline; The condensate cooler outlet is connected to the light benzene medial launder, washes benzene tower side line and connects the naphthalene fairlead.
Coking crude benzene contains benzene and separates water treatment method, carries out according to the following steps:
(1) divides dried up to underground emptying groove through the benzene butyraceous crude benzol that contains that crude benzol divides dried up blow-down pipe to carry the crude benzol production process to separate;
(2) opens the valve that crude benzol divides dried up transfer lime to be provided with, and opens the valve before and after the cyclic ammonia water pipe cocycle aqua ammonia pump, opens vacuum primingpump and cyclic ammonia water pump, crude benzol is divided dried uply be sent to coke oven collecting main cooling down high-temperature coal gas with ammoniacal liquor;
(3) relies on pyritous coal gas to divide dried up the heating to the crude benzol that contains benzene and naphthalene in cooling coal gas, sneaks into benzene and naphthalene heated volatile in the coal gas; Wherein volatilization is sneaked into the benzene gas that gets in the coal gas and is directly arrived behind thionizer and sulphur ammonium tower by the gas blower positive delivery with coke-oven gas with naphthalene gas and wash the benzene operation, washes the benzene tower washing benzene operation employing packing type, and adopts 25～28 ℃ washing oil that coal gas is washed; Coal gas gets into from the bottom in washing the benzene tower, comes out in top, and washing oil sprays coal gas in washing the benzene tower from top to bottom; The principle of utilizing washing oil and benzene, toluene and naphthalene to dissolve each other; Absorb the benzene in the coal gas, toluene and naphthalene get off, dissolve in the washing oil, the washing oil (being called rich oil) that has absorbed benzene, naphthalene is again through the rich oil pump delivery; After preheating, get into from the debenzolizing tower middle and lower part; And use steam that rich oil is steamed in the debenzolizing tower bottom and blow, from washing oil, steam benzene, naphthalene and produce by boasting, adopt water cooler the benzene condensing and recycling again; Simultaneously according to the boiling point of naphthalene on the top of debenzolizing tower tower tray draw collection, reach the purpose that reclaims benzene, naphthalene; Water and oils are then sneaked into the tar system, with tar ammonia mixture ammoniacal liquor clarifying tank, carry out static layering with oil according to immiscible principle at ammoniacal liquor clarification trough inner water; Water continuously flows into the cyclic ammonia water groove because light specific gravity floats over top; Tar is then because than great; Sink to the bottom, regularly, realize oily water separation through the past tar medial launder of row of conduits.
The technical scheme that the present invention further limits is:
Aforesaid coking crude benzene contains benzene and separates water treatment system, and the venting port that the cyclic ammonia water pump has connects one road pipeline to the cyclic ammonia water groove, and vent valve is installed on pipeline, regularly the cyclic ammonia water pump is carried out exhaust.In order to prevent that benzene gas from producing cavitation erosion at the cyclic ammonia water pump, is discharged into the cyclic ammonia water pump to a small amount of benzene gas that accumulates in pump.
Aforesaid coking crude benzene contains benzene and separates water treatment method, and gas temperature is 780～850 ℃ in the coke oven collecting main.
The invention has the beneficial effects as follows: the present invention is through existing equipment in coke-oven plant and condition; Make full use of original equipment and divide the dried up purifying treatment of carrying out crude benzol; Crude benzol of the present invention divides dried up processing owing to make dried up middle benzene of branch and naphthalene vaporization through coal gas of high temperature as carrier, and the efficient of removing benzene, naphthalene is high.Removing benzene, naphthalene and oil separating water simultaneously directly handles to ammonia still process with ammoniacal liquor; Can not produce secondary pollution; Solved simultaneously and divided dried uply in the past, the environment that improves operation site has been played an important role to inhaling the benzene gas pollution problem that gas line or mechanizeding ammonia clarifying groove produced.
Description of drawings
Fig. 1 is a connection synoptic diagram of the present invention.
Embodiment
Embodiment 1
A kind of coking crude benzene of present embodiment contains benzene and separates water treatment system; Connect as shown in Figure 1; A kind of coking crude benzene contains benzene and separates water treatment system, comprises underground emptying groove 22, cyclic ammonia water groove 28, coke oven collecting main 2 and cyclic ammonia water pump 25, and coke oven collecting main 2 connects coke oven 1; Cyclic ammonia water pump 25 is arranged on the cyclic ammonia water pipe 3 that cyclic ammonia water groove 28 is connected to coke oven collecting main 2; The front and back of cyclic ammonia water pipe 3 cocycle aqua ammonia pumps 25 all are provided with valve, and the fluid inlet that underground emptying groove 22 has connects crude benzol and divides dried up blow-down pipe 21, and the benzene butyraceous crude benzol that contains that crude benzol divides dried up blow-down pipe 21 to carry the crude benzol production process to separate divides dried up to underground emptying groove 22; The crude benzol that is connected to underground emptying groove 22 inner bottom parts divides dried up transfer lime 24 to be connected to the import of cyclic ammonia water pump 25; Crude benzol divides dried up transfer lime 24 to be provided with vacuum primingpump 23; Crude benzol between vacuum primingpump 23 and the cyclic ammonia water pump 25 divides dried up transfer lime 24 to be provided with valve 27, and cyclic ammonia water pump 25 divides crude benzol and dried uply is delivered to coke oven collecting main 2 with ammoniacal liquor; The outlet of coke oven collecting main 2 connects gas-liquid separator 4; The outlet at bottom of gas-liquid separator 4 connects ammoniacal liquor clarifying tank 30 through mixed solution pipeline 5; The top outlet of gas-liquid separator 4 connects gas blower 7 through cooling oil eliminator 6; The outlet at bottom of ammoniacal liquor clarifying tank 30 is connected to tar medial launder 29, and the top outlet of ammoniacal liquor clarifying tank 30 is connected to cyclic ammonia water groove 28; Gas blower 7 outlets connect thionizer 8, sulphur ammonium tower 9 successively and wash benzene tower 11; The outlet at bottom of washing benzene tower 11 is connected to debenzolizing tower 13 through rich oil pump 20 and oil gas interchanger 19 successively; The top exit of debenzolizing tower 13 is connected to light benzene condensate cooler 15 through light benzene pipeline 14; Condensate cooler 15 outlets are connected to light benzene medial launder 17, wash benzene tower 11) side line connection naphthalene fairlead 18.
Crude benzol divides and dried uply directly sprays through shower nozzle, contacts with coal gas of high temperature, benzene, how to wait volatile organic matter in effuser 2, directly to sneak into coke-oven gas; Coal gas and ammoniacal liquor, the tar mixed solution pipeline that exists together in effuser 2, wherein coal gas flows to gas blower 7 under the suction of gas blower 7 on pipeline; Mixed solution such as ammoniacal liquor, tar relies on the effect of gravity flow to flow to mechanizeding ammonia clarifying groove 30 in the bottom of pipeline, and 4 places carry out gas-liquid separation at gas-liquid separator; Coal gas gets into gas line, after cooling, oil removing, is sent to thionizer 8 and sulphur ammonium tower 9 by gas blower 7, reaches at last and washes the benzene operation; Adopt washing oil that coal gas is sprayed washing washing in the benzene tower 11 of benzene operation, absorb the organism such as benzene and naphthalene in the coal gas, absorbed benzene and how to have waited organic washing oil (title rich oil) by 20 conveyings of rich oil pump; Be heated to 180～185 ℃ through oil gas interchanger, poor oil-rich heat exchanger and tube furnace and get into debenzolizing tower 13; In debenzolizing tower 13, adopt steam that rich oil is steamed and blow, washing oil is separated with benzene, naphthalene, benzene steams from debenzolizing tower 13 tops; After 15 coolings of light benzene condensate cooler, collect with light benzene medial launder 17; Naphthalene is drawn from the tower tray of debenzolizing tower side line, collects with groove, directly diffuses after the incoagulability dispersing gas on groove top gets into the washing tail gas system handles.Ammoniacal liquor, tar mixed solution along pipeline self to mechanizeding ammonia clarifying groove 30, carry out static layering with oil according to immiscible principle at mechanizeding ammonia clarifying groove 30 Nei Shui after gas-liquid separator 4 places carry out gas-liquid separation, water is because light specific gravity; Float over top; Continuously flow into cyclic ammonia water groove 28, tar is then owing to than great, sink to the bottom; Regularly, realize oily water separation through the past tar medial launder 29 of row of conduits.
In order to prevent that benzene gas from producing cavitation erosion at centrifugal pump of horizontal axis; Upper air vent at cyclic ammonia water pump 25 connects one road pipeline to cyclic ammonia water groove 28; And vent valve 26 is installed, and regularly cyclic ammonia water pump 25 is carried out exhaust, be discharged into cyclic ammonia water groove 28 to a small amount of benzene gas that accumulates in pump.
Coking crude benzene contains benzene and separates water treatment method, carries out according to the following steps:
(1) divides dried up to underground emptying groove 22 through the benzene butyraceous crude benzol that contains that crude benzol divides dried up blow-down pipe 21 to carry the crude benzol production process to separate;
(2) opens the valve 26 that crude benzol divides dried up transfer lime 24 to be provided with, and opens the valve of cyclic ammonia water pipe 3 cocycle aqua ammonia pumps 25 front and back, opens vacuum primingpump 23 and cyclic ammonia water pump 25, crude benzol is divided dried uply be sent to coke oven collecting main 2 cooling down high-temperature coal gas with ammoniacal liquor;
(3) relies on pyritous coal gas to divide dried up the heating to the crude benzol that contains benzene and naphthalene in cooling coal gas, and gas temperature is 780～850 ℃ in the coke oven collecting main 2; Sneak into benzene and naphthalene heated volatile in the coal gas; With coal gas to the road, back wash the benzene operation, reclaim organism such as benzene and naphthalene wherein, wherein volatilization is sneaked into benzene gas in the entering coal gas and is directly arrived after desulfurization process 8, sulphur ammonium operation 9 by gas blower 7 positive delivery with coke-oven gas with naphthalene gas and wash the benzene operation; Adopt packing type to wash benzene tower 11 washing the benzene operation; And adopt 25～28 ℃ washing oil that coal gas is washed, and coal gas gets into from the bottom in washing the benzene tower, and come out in top; Washing oil sprays coal gas in washing the benzene tower from top to bottom; The principle of utilizing organism such as washing oil and benzene, toluene and naphthalene to dissolve each other absorbs the benzene in the coal gas, toluene and naphthalene get off, and dissolves in the washing oil.The washing oil (being called rich oil) that has absorbed benzene, naphthalene is through carry through rich oil pump 20 again; After preheating, get into from debenzolizing tower 13 middle and lower parts; And use steam that rich oil is steamed in debenzolizing tower 13 bottoms and blow, from washing oil, steam benzene, naphthalene and produce by boasting, adopt water cooler 15 the benzene condensing and recycling again; Simultaneously according to the boiling point of naphthalene on the top of debenzolizing tower 13 tower tray draw collection, reach the purpose that reclaims benzene, naphthalene.Water and oils are then sneaked into the tar system, with tar ammonia mixture mechanizeding ammonia clarifying groove 30, carry out static layering with oil according to immiscible principle at mechanizeding ammonia clarifying groove 30 Nei Shui; Water continuously flows into cyclic ammonia water groove 28 because light specific gravity floats over top; Tar is then because than great; Sink to the bottom, regularly, realize oily water separation through the past tar medial launder 29 of row of conduits.
Except that the foregoing description, the present invention can also have other embodiments.All employings are equal to the technical scheme of replacement or equivalent transformation formation, all drop on the protection domain of requirement of the present invention.
Claims (4)
1. a coking crude benzene contains benzene and separates water treatment system; Comprise underground emptying groove (22), cyclic ammonia water groove (28), coke oven collecting main (2) and cyclic ammonia water pump (25); Said cyclic ammonia water pump (25) is arranged on the cyclic ammonia water pipe (3) that cyclic ammonia water groove (28) is connected to coke oven collecting main (2); The front and back of said cyclic ammonia water pipe (3) cocycle aqua ammonia pump (25) all are provided with valve; It is characterized in that: the fluid inlet that said underground emptying groove (22) has connects crude benzol and divides dried up blow-down pipe (21), and the benzene butyraceous crude benzol that contains that said crude benzol divides dried up blow-down pipe (21) to carry the crude benzol production process to separate divides dried up to underground emptying groove (22); The crude benzol that is connected to said underground emptying groove (22) inner bottom part divides dried up transfer lime (24) to be connected to the import of cyclic ammonia water pump (25); Said crude benzol divides dried up transfer lime (24) to be provided with vacuum primingpump (23); Crude benzol between vacuum primingpump (23) and the cyclic ammonia water pump (25) divides dried up transfer lime (24) to be provided with valve (27), and cyclic ammonia water pump (25) divides crude benzol and dried uply is delivered to coke oven collecting main (2) with ammoniacal liquor; The outlet of said coke oven collecting main (2) connects gas-liquid separator (4); The outlet at bottom of said gas-liquid separator (4) connects ammoniacal liquor clarifying tank (30) through mixed solution pipeline (5); The top outlet of gas-liquid separator (4) connects gas blower (7) through cooling oil eliminator (6); The outlet at bottom of said ammoniacal liquor clarifying tank (30) is connected to tar medial launder (29), and the top outlet of ammoniacal liquor clarifying tank (30) is connected to cyclic ammonia water groove (28); Said gas blower (7) outlet connects thionizer (8), sulphur ammonium tower (9) successively and washes benzene tower (11); The said outlet at bottom of washing benzene tower (11) is connected to debenzolizing tower (13) through rich oil pump (20) and oil gas interchanger (19) successively; The top exit of debenzolizing tower (13) is connected to light benzene condensate cooler (15) through light benzene pipeline (14); Condensate cooler (15) outlet is connected to light benzene medial launder (17), and said benzene tower (11) side line of washing connects naphthalene fairlead (18).
2. coking crude benzene as claimed in claim 1 contains benzene and separates water treatment system; It is characterized in that: the venting port that cyclic ammonia water pump (25) has connects one road pipeline to cyclic ammonia water groove (28); And vent valve (26) is installed on pipeline, regularly cyclic ammonia water pump (25) is carried out exhaust.
3. the coking crude benzene that is used for the said system of claim 1 contains benzene and separates water treatment method, it is characterized in that: carry out according to the following steps:
(1) divides dried up to underground emptying groove (22) through the benzene butyraceous crude benzol that contains that crude benzol divides dried up blow-down pipe (21) to carry the crude benzol production process to separate;
(2) opens crude benzol and divides the dried up transfer lime valve that (24) are provided with (27); Open the valve of cyclic ammonia water pipe (3) cocycle aqua ammonia pump (25) front and back; Open vacuum primingpump (23) and cyclic ammonia water pump (25), crude benzol is divided dried uply be sent to coke oven collecting main (2) cooling down high-temperature coal gas with ammoniacal liquor;
(3) relies on pyritous coal gas to divide dried up the heating to the crude benzol that contains benzene and naphthalene in cooling coal gas, sneaks into benzene and naphthalene heated volatile in the coal gas; Wherein volatilization is sneaked into the benzene gas that gets in the coal gas and is directly arrived behind thionizer (8) and sulphur ammonium tower (9) by gas blower (7) positive delivery with coke-oven gas with naphthalene gas and wash the benzene operation, washes benzene tower (11) washing benzene operation employing packing type, and adopts 25～28 ℃ washing oil that coal gas is washed; Coal gas gets into from the bottom in washing the benzene tower, comes out in top, and washing oil sprays coal gas in washing the benzene tower from top to bottom; The principle of utilizing washing oil and benzene, toluene and naphthalene to dissolve each other; Absorb the benzene in the coal gas, toluene and naphthalene get off, dissolve in the washing oil, the washing oil that has absorbed benzene, naphthalene is carried through rich oil pump (20) again; After preheating, get into from debenzolizing tower (13) middle and lower part; And use steam that rich oil is steamed in debenzolizing tower (13) bottom and blow, from washing oil, steam benzene, naphthalene and produce by boasting, adopt water cooler (15) the benzene condensing and recycling again; Simultaneously draw collection at the top tower tray of debenzolizing tower (13), reach the purpose that reclaims benzene, naphthalene according to the boiling point of naphthalene; Water and oils are then sneaked into the tar system, with tar ammonia mixture ammoniacal liquor clarifying tank (30), carry out static layering with oil according to immiscible principle at ammoniacal liquor clarifying tank (30) Nei Shui; Water continuously flows into cyclic ammonia water groove (28) because light specific gravity floats over top; Tar is then because than great; Sink to the bottom, regularly, realize oily water separation through the past tar medial launder (29) of row of conduits.
4. coking crude benzene as claimed in claim 2 contains benzene and separates water treatment method, and it is characterized in that: the interior gas temperature of said coke oven collecting main (2) is 780～850 ℃.
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| CN104232133A (en) * | 2013-06-21 | 2014-12-24 | 上海宝钢化工有限公司 | Method and device for reducing potassium and sodium ion content of coal tar |
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| CN107021590B (en) * | 2017-04-24 | 2020-02-21 | 莱芜市泰山焦化有限公司 | Method for reducing harmful components in ammonia distillation wastewater through step-by-step separation based on high dry distillation of coal cakes |
| CN116376605A (en) * | 2021-12-24 | 2023-07-04 | 江苏集萃冶金技术研究院有限公司 | Coke oven waste gas denaphthalene dehydration detar recovery method |
| CN116392933A (en) * | 2023-05-24 | 2023-07-07 | 广东中南钢铁股份有限公司 | Purifying device and purifying method for crude benzene system tail gas |
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