CN105126380A - Coking exhaust gas treatment method - Google Patents
Coking exhaust gas treatment method Download PDFInfo
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- CN105126380A CN105126380A CN201510608866.5A CN201510608866A CN105126380A CN 105126380 A CN105126380 A CN 105126380A CN 201510608866 A CN201510608866 A CN 201510608866A CN 105126380 A CN105126380 A CN 105126380A
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Abstract
The invention relates to a coking exhaust gas treatment method which is characterized by comprising the following steps: coking exhaust gas enters a condensate separator; after liquid phases are separated, the separated coking exhaust gas enters a liquid-gas jet pump and is mixed with methanol which enters the liquid-gas jet pump from a liquid phase inlet; the mixture is conveyed into a stock solution in an absorption tower; part of sulfur components and benzene series in the gas phase are washed out from the stock solution, get out in bubbles from the stock solution and are in countercurrent contact with low-temperature washing methanol which enters the absorption tower from the middle part; the sulfur components and benzene series are dissolved in washing methanol and further washed out from the coking exhaust gas; the washed waste gas enters the activated carbon packing section at the top of the absorption tower, and is adsorbed and evacuated; the stock solution in the kettle of the absorption tower is extracted by a circulating pump and divided into two streams: a first stream is conveyed for regeneration, and a second stream is further divided into two parts: a first part is mixed with lean methanol, and the mixture is used as washing methanol and enters from the middle part of the absorption tower, and the second part is conveyed into the liquid-gas jet pump, wherein the flow amount of the second part is matched with the pressure of the liquid-gas jet pump.
Description
Technical field
The present invention relates to a kind of coking exhaust gas treating method, specifically refer to the coking exhaust gas treating method containing a large amount of steam, hydrocarbon and sulfide volatilized in a kind of, coke cutting water cold to oil plant delayed coking.
Background technology
At present, the decoking technology of China's delayed coking extensively adopts the mode of hydraulic decoking, coke is in cooling, sewage can be produced in excision process, coke powder, the pollutant such as sump oil and waste gas, especially give water-cooled burnt at device, bubble is burnt, in flooding process, large amount temperature can be produced at the oil-containing of about 100 DEG C, sulfur-bearing, containing the sewage of benzene homologues, the thing followed is organic exhaust gas and the coking tail gas of the pollutant such as a large amount of sulfur compound and hydro carbons evaporated under high temperature, these gas compositions are complicated, moisture accounts for more than 95%, there is stench, the feature such as poisonous, environment and personal safety are constituted a threat to, especially when device processing high-sulfur inferior raw material, air pollution is even more serious.
The cold-cut water treatment process that the production of coking tail gas and enterprise adopt has direct relation, treatment process both at home and abroad for cold-cut water has vented disposal technique, semi-open-type treatment process and closed treatment process three kinds, first two processing mode is owing to being all communicated with air, coking exhaust collection difficulty, just progressively made superseded by refining enterprises reform, pond is changed tank by closed technique, cooling column changes air cooler into, oil in coke cooling water is realized under completely airtight condition, Jiao is separated with water, the coking waste gas volatilized concentrates on the treated rear discharge air up to standard in coke cooling water hot-water cylinder top.Existing cold-cut water closed processes technique mainly contains liquefied ammonia and other alkali lye, the deodorization of amine liquid wet chemistry, IVP charcoal absorption and the deodorization of desulfurizing agent chemical dry etc. to coking waste gas processing method.The product (ferrous sulfide) of dry desulfurization contacts rear easily spontaneous combustion with air, very easily cause blast, there is serious potential safety hazard under the environment that exhaust is not smooth; The product reclaiming of alkali desulphurization is difficult, cost is high, and spent lye belongs to hazardous waste, difficult treatment, easily causes secondary pollution to environment; Amine desulfurization can the purifier of supporting plant area, but absorbent price is higher, with CO
2reaction speed is comparatively slow, and especially under low pressure deodorising effect is poor, unstable, easily occurs H in purified gas
2s content overproof, the phenomenon of liquid, degraded and organic amine mixed liquor ubiquity foams, blocks, bring considerable influence can to the stable operation of production system.
CN2808275Y discloses a kind of deodorizing equipment, and its core utilizes acid or alkali lye chemical absorbing hydrogen sulfide, the materials such as mercaptan, and utilize thixotropic activated carbon oxidation organic sulfur.The method flow process is too complicated, invests high, be acid or alkali liquor absorption sulfide after all there is the saturated problem of lyosoption, and easily cause secondary pollution, and in reality, with the hydrocarbons in addition of Stenchy sulfides, the method is to hydro carbons almost non-processor ability.
In the existing processing method of delayed coking waste gas, the technique adopted or itself there is defect, long flow path, investment is large, and energy consumption is high, and security is lower, cause secondary pollution, or only have desulfurizing function, or there is desulfurization take off hydrocarbon ability but middle hydrocarbon sulfur content of dropping a hint still exceeds standard.
Summary of the invention
The problem to be solved in the present invention provides a kind of coking exhaust gas treating method for existing technology, and low to solve security of the prior art, energy consumption is high, and lyosoption is unstable, and result is undesirable waits series of problems.
The present invention's adopted technical scheme that solves the problem is: this coking exhaust gas treating method, is characterized in that comprising the steps:
The coking tail gas of 90 ~ 100 DEG C enters condensation separator, be cooled to 30 ~ 35 DEG C, isolated liquid phase is extracted out and is sent coking plant back to bottom condenser, isolated coking tail gas enters liquid-gas jet pump from gas phase entrance, sends in the liquid storage of absorption tower bottom tower reactor together with after mixing with the methyl alcohol entering liquid-gas jet pump 3 from liquid phase entrance;
Described gas phase washs out part sulphur component and benzene homologues in liquid storage, bubbling from liquid storage and going out, with the washing methyl alcohol counter current contacting that the temperature entering absorption tower from middle part is-25 ~-30 DEG C, sulphur component and benzene homologues are dissolved in washing methyl alcohol, are washed out further by from coking tail gas;
The mol ratio of described washing methyl alcohol and described coking tail gas is 2:1 ~ 10:1;
Waste gas after washing enters the active carbon filler section at top, absorption tower, is adsorbed by small molecule hydrocarbon remaining in waste gas, the tail gas emptying after absorption;
The liquid storage of described absorption tower tower reactor is extracted out via circulating pump, two strands are divided into after being forced into 1.5-2.5MPa (G), wherein send to low-temp methanol cyclic regeneration device for first strand, the uninterrupted of first strand is controlled automatically by the liquid level of tower reactor Liquid level adjusting valve according to liquid storage section, the liquid level height 0.5m ~ 1m of liquid storage section; Second strand is divided into two parts again, wherein the ratio of Part I and the poor methanol from low temperature washing device for methanol 4:1 ~ 10:1 in molar ratio enters in the middle part of absorption tower as washing methyl alcohol after mixing, the addition of poor methanol can adjust according to sulfur content in coking tail gas, sulfur content is lower, the temperature rise of washing methyl alcohol is less, saturated velocity is slower, and poor methanol addition is less.Part II sends into liquid-gas jet pump; The flow of described Part II and the pressure of described liquid-gas jet pump suitable.
Preferably, the pressure of described liquid-gas jet pump gas phase entrance is-10Kpa ~-20Kpa negative pressure, and the pressure of described liquid-gas jet pump discharge is 100Kpa ~ 200Kpa malleation.The program take liquid-gas jet pump as boundary, and upstream forms tiny structure, and for coking tail gas provides power from coke cooling water hot-water cylinder to absorption tower, liquid-gas jet pump downstream is pressure-fired, is conducive to the washing absorption of methyl alcohol to sulfide and benzene homologues.
Described absorption tower comprises the packing section being positioned at top and the washing section being positioned at below, and wherein said packing section is filled with active carbon, and packed height is at 0.8m ~ 1.5m; Described absorber portion comprises superposed column plate and is positioned at the liquid storage section of bottom.
Described washing section top is provided with deflector-type separator, to reduce the methyl alcohol carried secretly when coking tail gas rises, reduces methanol loss.
Described column plate has 3-10 block, column plate form can be float valve or other types, the tower tray of coking tail gas in lower tower is recycled methyl alcohol washing absorption again from bottom to top, goes out the coking tail gas sulfur content of tower and the mol ratio of benzene homologues under Methanol Wash Column and all reaches 10 × 10
-6below tower on Methanol Wash Column is sent into afterwards.
Described liquid-gas jet pump discharge is provided with the straight length of 1 ~ 6 meter, fully mixes with methyl alcohol to make coking tail gas.
Liquid level adjusting valve for controlling described liquid storage section liquid level is provided with for carrying the pipeline of described first strand of low-temp methanol.
The liquid distributor be connected with described washing methanol inlet is provided with in described absorption tower.
Compared with existing coking exhaust gas treating method, tool of the present invention has the following advantages:
1, the present invention adopts the processing method of " condensation+methyl alcohol desulfurization deodorizing+charcoal absorption ", and water and large molecule hydrocarbon condensation separation, sulphur content low temperature absorption, all the other component adsorbing and removings, tertiary treatment, removes the harmful substance in coking tail gas to the full extent.Change the process only focusing on malodor source-sulfide in existing coking tail gas closed processes technique, and ignore the discharge beyond standards problem of organic hydrocarbon, reach the object that coking tail gas full constituent processes simultaneously.
2, using methyl alcohol as the sulfide lyosoption of coking tail gas, make full use of the feature of methyl alcohol to the effective easy regeneration of polar molecule Physical Absorption, overcome the degraded of other solution chemical processing modes, secondary pollution problems simultaneously.
3, liquid-gas jet pump is introduced, absorption tower repeats itself methyl alcohol is aspirated as power coking tail gas, form upstream negative pressure ventilation, downstream malleation absorbs, solving the problem that under normal pressure, efficiency is low, assimilation effect is undesirable, can avoiding additionally introducing steam and the energy consumption needing this some vapor of condensation and produce increase problem to increase suction power simultaneously.
4, take into full account that coking tail gas volatilization total amount is little, in component, more than 95% is steam, after condensation separatory, gas flow is little, methanol loop amount is little, the feature that temperature rise is slow, one low-temp methanol from low temperature washing device for methanol of direct introducing, without the need to additionally increasing cooler, circulation rich methanol is cooled, low-temperature rectisol is sent to regenerate as backflow a part of rich methanol, no matter pass in and out methyl alcohol for continuous or intermittent operation, on low temperature washing device for methanol original system almost without impact, investment more economizes, without the need to the cyclic processing device of special supporting lyosoption again.
5, the present invention is only provided with a condenser, and adopts repeats itself methyl alcohol as power of bleeding, and methanol absorber tower and active carbon absorption is united two into one, and flow process is shorter, and equipment investment is little compared with low floor space, and energy consumption is lower.
Accompanying drawing explanation
Fig. 1 is the process chart of the embodiment of the present invention.
Detailed description of the invention
Below in conjunction with accompanying drawing embodiment, the present invention is described in further detail.
Under the suction of liquid-gas jet pump 3, from coke cooling water hot-water cylinder temperature at 95-98 DEG C, the coking tail gas of absolute pressure 80KPa enters condensation separator 1, coking tail gas walks the shell side of condensation separator, liquid storage space 11 is provided with bottom condensation separator shell side, coking tail gas is water-cooled to 32 DEG C by the circulating cooling walking condensation separator tube side from public work, the steam of in coking tail gas 98% and macromolecule hydrocarbon, by the liquid storage space enrichment after precipitation of condensing bottom condensation separator, are sent delayed coking back to through lime set pump 2 and are processed further.
Be separated the coking tail gas after liquid phase from tail gas condensing separator 1 out after, aspirated by liquid-gas jet pump 3 and compress, the suction power source of liquid-gas jet pump is the Part II from second burst of recycle methanol on absorption tower.Temperature is recycled pump 6 the recycle methanol of-27 DEG C and is forced into 2.0MPa (G).
After coking tail gas fully mixes with Part II recycle methanol in liquid-gas jet pump 3 straight length outlet line, enter in the liquid storage section of tower 4 under absorption tower, be the methanol wash of-27 DEG C by the temperature in liquid storage section, wash out part sulphur component and benzene homologues; All the other tail gas overflow in bubbling mode, tower tray in lower tower flows from bottom to top, with the washing methyl alcohol counter current contacting sprayed from liquid distribution trough, sulfide in tail gas and benzene homologues are washed further, and the sulfur content in the waste gas obtained after washing and the mol ratio of benzene homologues all reach 10 × 10
-6below.
Under control absorption tower, the operating pressure of tower 4 is 0.1MPa (G), and washing methyl alcohol is 7:1 with the mol ratio of the coking tail gas entering liquid storage section.Coking tail gas can be selected in 2:1 ~ 10:1 according to the content of coking exhaust flow and sulphur and benzene homologues with the amount ratio of washing methyl alcohol, washs methyl alcohol and maintains certain surplus capacity, can meet the needs of intermittent operation under this ratio.
Waste gas overflows from lower tower and enters upper tower 5.On absorption tower, tower 5 is packed tower, inside be filled with active carbon, as the adsorbent of VOCs (organic exhaust gas), remove not by the low concentration small molecule hydrocarbon of methanol absorption and remaining benzene homologues further, after the absorption of active carbon reaches capacity, can regularly replace or pass into hot nitrogen and desorption and regeneration is carried out to charcoal bed.The Small molecular hydro carbons that absorbed by the 4 times towers in absorption tower and all the other harmful substances fail in coking tail gas by after the charcoal absorption of tower on absorption tower 5, and from absorption tower, tower 5 top directly enters air.Under absorption tower, on tower 4 and absorption tower, tower 5 is merged into a tower with the form of up-down structure and is arranged.
From absorption tower, rich methanol temperature out at the bottom of tower 4 still is-27 DEG C, is forced into after 2.0MPa (G), is divided into two strands, wherein first strand of transmitting system through circulating pump 6, enters low temperature washing device for methanol regeneration; The pipeline of sending of first strand is provided with fluid level control valve 7, regulates the flow of first strand to maintain 0.8m with the liquid level controlling liquid storage section by this fluid level control valve.
Second strand of rich methanol is divided into two parts, wherein Part I is mixed into washing methyl alcohol with-35 DEG C of poor methanols that out-of-bounds low temperature washing device for methanol is sent here, absorption tower Xia Ta is returned via liquid distribution trough from upper tower entrance, the mol ratio of Part I and poor methanol is 8:1, the addition of poor methanol can adjust according to sulfur content in coking tail gas, and sulfur content is lower, and the temperature rise of washing methyl alcohol is less, saturated velocity is slower, and poor methanol addition is less.Part II liquid phase enters liquid-gas jet pump 3 as suction power source, and flow is 150 ~ 200kmol/h about, and the flow of Part II is determined according to calculation of pressure required before and after the amount of coking tail gas and liquid-gas jet pump, and this is conventionally calculation, does not do burden and describes.
Claims (8)
1. a coking exhaust gas treating method, is characterized in that comprising the steps:
The coking tail gas of 90 ~ 100 DEG C enters condensation separator, be cooled to 30 ~ 35 DEG C, isolated liquid phase is extracted out and is sent coking plant back to bottom condenser, isolated coking tail gas enters liquid-gas jet pump from gas phase entrance, sends in the liquid storage on absorption tower together with after mixing with the methyl alcohol entering liquid-gas jet pump from liquid phase entrance;
Described gas phase washs out part sulphur component and benzene homologues in liquid storage, bubbling from liquid storage and going out, with the washing methyl alcohol counter current contacting that the temperature entering absorption tower from middle part is-25 ~-30 DEG C, sulphur component and benzene homologues are dissolved in washing methyl alcohol, are washed out further by from coking tail gas;
The mol ratio of described washing methyl alcohol and described coking tail gas is 2:1 ~ 10:1;
Waste gas after washing enters the active carbon filler section at top, absorption tower, is adsorbed by small molecule hydrocarbon remaining in waste gas, the tail gas emptying after absorption;
The liquid storage of described absorption tower tower reactor is extracted out via circulating pump, two strands are divided into after being forced into 1.5-2.5MPa (G), wherein send to low-temp methanol device circular regeneration for first strand, the uninterrupted of first strand is controlled automatically by the liquid level of tower reactor Liquid level adjusting valve according to liquid storage section, and liquid storage section at least keeps the liquid level of 0.5m ~ 1m; Second strand is divided into two parts again, and wherein the ratio of Part I and the poor methanol from low temperature washing device for methanol 4:1 ~ 10:1 in molar ratio enters in the middle part of absorption tower as washing methyl alcohol after mixing, and Part II sends into liquid-gas jet pump 3; The flow of described Part II and the pressure of described liquid-gas jet pump suitable.
2. coking exhaust gas treating method according to claim 1, it is characterized in that the pressure of described liquid-gas jet pump gas phase entrance is for-10Kpa ~-20Kpa negative pressure, the pressure of described liquid-gas jet pump discharge is 100Kpa ~ 200Kpa malleation.
3. coking exhaust gas treating method according to claim 1 and 2, it is characterized in that described absorption tower comprises the packing section being positioned at top and the washing section being positioned at below, wherein said packing section is filled with active carbon, and packed height is at 0.8 ~ 1.5 meter; Described absorber portion comprises superposed column plate and is positioned at the liquid storage section of bottom.
4. coking exhaust gas treating method according to claim 3, is characterized in that described washing section top is provided with deflector-type separator.
5. coking exhaust gas treating method according to claim 4, is characterized in that described column plate has 3-10 block.
6. coking exhaust gas treating method according to claim 1, is characterized in that described liquid-gas jet pump discharge is provided with the straight length of 1 meter ~ 6 meters.
7. coking exhaust gas treating method according to claim 6, is characterized in that for carrying the pipeline of described first strand of low-temp methanol to be provided with Liquid level adjusting valve for controlling described liquid storage section liquid level.
8. coking exhaust gas treating method according to claim 7, is characterized in that being provided with the liquid distributor be connected with described washing methanol inlet in described absorption tower.
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Cited By (7)
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| CN105505440A (en) * | 2015-12-16 | 2016-04-20 | 华南理工大学 | Re-absorbing unit and procedure for absorbing lean gas in stable system |
| CN106178903A (en) * | 2016-08-31 | 2016-12-07 | 南京中衡元环保设备有限公司 | A kind of coke cooling water tank waste gas treatment process and system |
| CN108949246A (en) * | 2018-08-06 | 2018-12-07 | 宁夏宝丰能源集团股份有限公司 | A kind of purification process of the sulfur method that low-temp methanol is washed and preparing methanol from coke oven gas |
| CN109603513A (en) * | 2018-12-17 | 2019-04-12 | 广州市致顺科技有限公司 | A kind of glue residue exhaust treatment system |
| CN109718635A (en) * | 2017-10-31 | 2019-05-07 | 中国石油化工股份有限公司 | A kind of process of flue gas desulfurization and denitrification |
| CN114525156A (en) * | 2022-02-23 | 2022-05-24 | 华南理工大学 | Energy-saving device and method for strengthening low-temperature methanol washing absorption based on Lurgi process |
| CN115591371A (en) * | 2022-11-30 | 2023-01-13 | 中化蓝天霍尼韦尔新材料有限公司（Cn） | Tail gas recovery system and method in trans-1-chloro-3, 3-trifluoropropene production process |
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| CN115591371A (en) * | 2022-11-30 | 2023-01-13 | 中化蓝天霍尼韦尔新材料有限公司（Cn） | Tail gas recovery system and method in trans-1-chloro-3, 3-trifluoropropene production process |
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