CN110585861A - Coking waste gas treatment system and treatment method - Google Patents
Coking waste gas treatment system and treatment method Download PDFInfo
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- CN110585861A CN110585861A CN201910965275.1A CN201910965275A CN110585861A CN 110585861 A CN110585861 A CN 110585861A CN 201910965275 A CN201910965275 A CN 201910965275A CN 110585861 A CN110585861 A CN 110585861A
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- B01D53/02—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography
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Abstract
The invention discloses a coking waste gas treatment system and a coking waste gas treatment method, and solves the problem that naphthalene crystals block a pipeline in a coking waste gas recovery process, so that the waste gas treatment efficiency of equipment is greatly influenced. The invention comprises a naphthalene recovery system, wherein the naphthalene recovery system is connected with a wash oil absorption tower, the wash oil absorption tower is connected with a dynamic wave alkali absorption tower through an oil-water separator, the dynamic wave alkali absorption tower is connected with a three-phase adsorption oxidation tower through a conveying pipeline, and the three-phase adsorption oxidation tower is connected with an adsorption/desorption system through a gas-water separation device. The invention is provided with the naphthalene recovery system to remove naphthalene, prevents the crystallization of naphthalene in the subsequent waste gas treatment process, blocks pipelines or active carbon pores, and greatly improves the treatment efficiency in the subsequent waste gas treatment process. And the waste gas treatment effect after passing through a series of subsequent waste gas treatment devices is good, and the pipelines do not need to be cleaned frequently, the active carbon does not need to be replaced frequently, and the waste gas treatment cost is greatly reduced.
Description
Technical Field
The invention relates to the field of waste gas treatment, in particular to a coking waste gas treatment system and method in a coking plant.
Background
In a coke plant, the large quantities of hazardous process off-gases produced originate primarily from chemical recovery plants. The chemical product recovery workshop not only plays a role in conveying coke oven gas, but also needs to purify the gas. During the production process, a large amount of volatile gases are generated in various chemical tower, tank and tank areas, the volatile gases contain a large amount of organic waste gases such as benzene, naphthalene, toluene, xylene, oil gas and the like, and inorganic waste gases such as water vapor and H2S、HCN、NH3Etc. these gases are simply treated for unorganized emission.
On the one hand, the gases generally have single or multiple hazards of flammability, explosiveness, poisoning and the like, and most of the gases have irritation and corrosiveness due to different impurities. In addition, the composition of the gas is complex, and the gas can cause serious pollution to the atmospheric environment, aggravate the corrosion of equipment, and easily cause safety accidents such as combustion, explosion and the like when being improperly handled.
On the other hand, benzene, naphthalene, oil and gas, etc. are important chemical industrial raw materials. With the improvement of environmental protection requirements, the unorganized exhaust gas is required to be purified and then is discharged up to the standard, which is also called VOC treatment, otherwise, production is not allowed. Along with the improvement of the environmental protection requirement and the promotion of the chemical utilization after the coke oven gas is purified in recent years, the requirement of purifying aromatic hydrocarbon in the coke oven gas is more urgent.
Methods for purifying aromatic hydrocarbons from gases commonly used in industry at present include absorption (wet), adsorption (dry), cryogenic treatment, etc. These methods are not completely suitable for coking waste gas because the coking waste gas contains a large amount of naphthalene, which is a condensed ring aromatic hydrocarbon, is an organic compound, colorless and toxic, and has a pure white crystal with camphorwood smell and a melting point of 80.5 ℃. The crystallization takes place for the naphthalene precooling in the waste gas, blocks up in the waste gas recovery treatment pipeline after the naphthalene crystallization, causes the pipeline to block up, influences the waste gas treatment efficiency of equipment greatly, is difficult to realize the discharge to reach standard of coking waste gas. The problem that how to solve the problem that the naphthalene crystal blocks the pipeline in the coking waste gas treatment process is a key problem to be solved in a coking plant.
Disclosure of Invention
The invention solves the technical problem that naphthalene crystals block a pipeline in the recovery process of coking waste gas, greatly influences the waste gas treatment efficiency of equipment, and provides a coking waste gas treatment system and a coking waste gas treatment method which can effectively control the unorganized emission of the naphthalene-containing waste gas and prevent atmosphere pollution.
In order to solve the technical problems, the invention adopts the following technical scheme: the utility model provides a coking waste gas treatment system, includes naphthalene recovery system, naphthalene recovery system be connected with wash oil absorption tower, wash oil absorption tower passes through oil water separator and is connected with power ripples alkali absorption tower, power ripples alkali absorption tower passes through pipeline and is connected with the three-phase adsorption oxidation tower, the three-phase adsorption oxidation tower passes through gas-water separation device and adsorbs/desorption headtotail.
The naphthalene recovery system comprises a naphthalene recovery tower, a gas-liquid separation tower and a waste liquid pool, wherein the middle part of the naphthalene recovery tower is provided with a waste gas inlet I, the upper part of the naphthalene recovery tower is provided with a waste gas outlet I, and the lower part of the naphthalene recovery tower is provided with a liquid outlet I; gas-liquid separation tower upper portion be equipped with waste gas entry II and waste gas outlet II, the gas-liquid separation tower lower part is equipped with leakage fluid dram II, waste gas entry II and waste gas collecting pipe connection, waste gas outlet II is linked together with waste gas entry I, leakage fluid dram II all are linked together with the waste liquid pond.
The naphthalene recovery tower is also provided with a circulating liquid outlet, a spray pipe is arranged in the naphthalene recovery tower, and a circulating pump is arranged between the circulating liquid outlet and the spray pipe; a grating layer is arranged above the waste gas inlet I, and a demister is arranged below the waste gas outlet I.
The circulating liquid outlet is communicated with a liquid inlet of the circulating pump, the spraying pipe is communicated with a liquid outlet of the circulating pump, a waste liquid pipe is also arranged and is communicated with the liquid outlet of the circulating pump, and the waste liquid pipe is communicated with a waste liquid pool.
An atomizing spray head is arranged on the outer side of a gas inlet II of the wash oil absorption tower, the gas inlet II is arranged below a gas distributor II, a two-stage wash oil spraying system is arranged in the wash oil absorption tower, the wash oil spraying system of each stage comprises the gas distributor II, a packing layer II is arranged above the gas distributor II, a wash oil spraying pipe is arranged above the packing layer II, and a gas outlet II is arranged at the upper part of the wash oil absorption tower; gas outlet II be connected with oil water separator, oil water separator from the bottom up include gas distributor III, gas distributor III top is equipped with packing layer III.
A dynamic wave spray head is arranged in front of an air inlet IV of the dynamic wave alkali absorption tower, and the air inlet IV is arranged below the dynamic wave alkali absorption tower; the dynamic wave alkali absorption tower is internally provided with two stages of alkali spraying systems, each alkali spraying system sequentially comprises a gas distributor IV, a packing layer IV and an alkali spraying pipe from bottom to top, and the upper part of the dynamic wave alkali absorption tower is provided with a gas outlet IV.
The lower part of the three-phase adsorption oxidation tower is provided with a gas inlet VI, the interior of the three-phase adsorption oxidation tower is provided with a two-stage oxidant spraying system, the oxidant spraying system comprises a gas distributor VI, a packing layer VI and an oxidant spraying pipe from bottom to top in sequence, and the upper part of the three-phase adsorption oxidation tower is provided with a gas outlet VI; and a gas-water separation device is connected with the gas outlet VI and comprises a gas distributor VII and a packing layer VII.
The adsorption/desorption system comprises a longitudinal gas distributor, a plurality of layers of adsorption beds are arranged behind the longitudinal gas distributor, a steam branch pipe is arranged above each layer of adsorption bed, and the plurality of steam branch pipes are connected in parallel; an air blower is arranged on an air inlet pipeline of the adsorption/desorption system, and a condensation recovery pipeline is arranged on an exhaust pipeline of the adsorption/desorption system.
A method of treating a coking exhaust gas treatment system, comprising the steps of: firstly, carrying out primary treatment on naphthalene toluene, benzene and xylene in waste gas by a naphthalene recovery system; secondly, the waste gas after primary treatment enters an oil washing absorption tower to remove naphthalene, toluene, benzene and xylene in the waste gas again; step three, the waste gas discharged from the oil washing absorption tower enters a dynamic wave alkali absorption tower to remove acidic substances in the waste gas; fourthly, the waste gas from which the acidic substances are removed enters a three-phase adsorption oxidation tower, and organic matters in the waste gas in the three-phase adsorption oxidation tower are oxidized into inorganic matters and are discharged along with the waste gas; fifthly, the waste gas containing inorganic matters discharged in the step IV enters an adsorption/desorption system to adsorb the inorganic matters and the residual organic matters in the waste gas again in a heating state and then is discharged.
The naphthalene recovery system comprises the following steps when carrying out primary treatment on naphthalene, toluene, benzene and xylene in waste gas: a. naphthalene-containing waste gas from a coking plant is converged in a waste gas collecting pipeline and enters a gas-liquid separation tower from a waste gas inlet II, the naphthalene-containing waste gas is condensed in the gas-liquid separation tower, waste liquid generated by condensation is discharged into a waste liquid pool through a liquid outlet II, and the residual condensed waste gas is discharged from a waste gas outlet II and enters a naphthalene recovery tower through a waste gas inlet I; b. the method comprises the following steps that firstly, the waste gas entering a naphthalene recovery tower is discharged from a waste gas outlet I after the naphthalene is recovered in the naphthalene recovery tower, and the specific process is as follows: pumping the light tar into a spray pipe by a circulating pump to be sprayed down, absorbing naphthalene in the waste gas by the light tar in the spraying process, and then dropping to the bottom of a naphthalene recovery tower; when the naphthalene content in the light tar is saturated, the light tar is discharged to a waste liquid pool through a liquid outlet I. Realizing the recovery of naphthalene in the waste gas.
The naphthalene recovery system is arranged to primarily remove organic matters such as naphthalene, toluene, benzene, xylene and the like from naphthalene-containing waste gas collected from production workshops of a coking plant, particularly remove naphthalene, so that naphthalene is prevented from crystallizing and blocking pipelines or activated carbon pores in the subsequent waste gas treatment process, and the treatment efficiency in the subsequent waste gas treatment process is greatly improved. And the content of each component in the waste gas after passing through a series of subsequent waste gas treatment devices reaches the standard of table 6 of emission standard of pollutants for coking chemical industry (GB 167171-2012), the treatment effect is good, the pipelines do not need to be cleaned frequently, the activated carbon does not need to be replaced frequently, and the waste gas treatment cost is greatly reduced.
Drawings
FIG. 1 is a system diagram of the present invention;
FIG. 2 is a schematic diagram of the naphthalene recovery system of the present invention;
FIG. 3 is a schematic view of the structure of a naphthalene recovery column of the present invention.
Detailed Description
The technical solutions in the embodiments of the present invention will be clearly and completely described below with reference to the drawings in the embodiments of the present invention, and it is obvious that the described embodiments are only a part of the embodiments of the present invention, and not all of the embodiments. All other embodiments, which can be obtained by a person skilled in the art without inventive effort based on the embodiments of the present invention, are within the scope of the present invention.
As shown in fig. 1 to 3, a coking waste gas treatment system comprises a naphthalene recovery system 1, wherein the naphthalene recovery system 1 is connected with a wash oil absorption tower 2, the wash oil absorption tower 2 is connected with a dynamic wave alkali absorption tower 4 through an oil-water separator 3, the dynamic wave alkali absorption tower 4 is connected with a three-phase adsorption oxidation tower 6 through a conveying pipeline 5, and the three-phase adsorption oxidation tower 6 is connected with an adsorption/desorption system 8 through a gas-water separation device 7.
The naphthalene recovery system 1 comprises a naphthalene recovery tower 11, a gas-liquid separation tower 12 and a waste liquid pool 13, wherein the middle part of the naphthalene recovery tower 11 is provided with a waste gas inlet I113, the upper part of the naphthalene recovery tower is provided with a waste gas outlet I114, and the lower part of the naphthalene recovery tower is provided with a liquid discharge port I115; the upper part of the gas-liquid separation tower 12 is provided with a waste gas inlet II121 and a waste gas outlet II122, the lower part of the gas-liquid separation tower 12 is provided with a liquid outlet II123, the waste gas inlet II121 is connected with a waste gas collecting pipeline 124, the waste gas outlet II122 is communicated with a waste gas inlet I113, and the liquid outlet I115 and the liquid outlet II123 are both communicated with a waste liquid pool 13. When the naphthalene recovery system 1 works, the naphthalene-containing waste gas formed by the waste gas collected from each production workshop of a coke-oven plant is collected in a waste gas collecting pipeline 124 and enters a gas-liquid separation tower 12 from a waste gas inlet II121, the naphthalene-containing waste gas is condensed in the gas-liquid separation tower 12, the condensed waste liquid is discharged into a waste liquid pool 13 through a liquid discharge port II123, and the condensed residual waste gas is discharged from a waste gas outlet II122 and enters a naphthalene recovery tower 11 through a waste gas inlet I113; the waste gas is discharged to the wash oil absorption tower from a waste gas outlet I114 after the naphthalene is recovered in the naphthalene recovery tower 11.
The naphthalene recovery tower 11 is also provided with a circulating liquid outlet 116, the naphthalene recovery tower 11 is internally provided with a spray pipe 117, and a circulating pump 14 is arranged between the circulating liquid outlet 116 and the spray pipe 117; a grid layer 118 is arranged above the waste gas inlet I113, and a demister 119 is arranged below the waste gas outlet I114. The naphthalene recovery tower 11 is filled with light tar, the light tar is tar condensed from a primary cooler of a coking plant, the light tar is pumped into a spray pipe 117 by a circulating pump 14 to be sprayed, and the light tar is dropped to the bottom of the naphthalene recovery tower 11 after absorbing organic matters such as naphthalene in waste gas; the light tar is circularly pumped by the circulating pump to remove the naphthalene in the waste gas, and when the naphthalene content in the light tar is higher, the light tar is discharged to the waste liquid pool 13 through the liquid outlet I115. The naphthalene recovery tower 11 is a Venturi recovery tower, the lower part of the naphthalene recovery tower 11 is a light tar storage area, two layers of spray pipes 117 are arranged in the naphthalene recovery tower 11, a grid layer 118 is arranged below each layer of spray pipes, and the naphthalene removal effect is good when waste gas is sprayed in the naphthalene recovery tower 11 in two stages. The naphthalene-containing waste gas enters the naphthalene recovery tower 11 from the waste gas inlet I113, the waste gas is uniformly distributed through the grid layer 118, then the light tar sprayed by the spray pipe absorbs the naphthalene in the waste gas, and the naphthalene is dehydrated by the demister and then is discharged from the waste gas outlet I114. The venturi effect formed by the grid layer 118 strengthens the mass transfer process between gas and liquid in the tower, increases the gas-liquid contact time and the contact area, ensures uniform distribution of gas flow in the tower and greatly improves the naphthalene removal efficiency.
The circulation liquid outlet 116 is communicated with a liquid inlet of the circulation pump 14, the spray pipe 117 is communicated with a liquid outlet of the circulation pump 14, a waste liquid pipe 141 is also arranged and communicated with the liquid outlet of the circulation pump 14, and the waste liquid pipe 141 is communicated with the waste liquid pool 13. When the naphthalene content in the light tar is high, the valve on the spray pipe 117 can be closed, and the light tar is pumped by the circulating pump 14 and discharged to the waste liquid tank 13 through the waste liquid pipe 141.
Naphthalene recovery system 1 adopts light tar to carry out the collection from each workshop of coke-oven plant to contain organic matters such as naphthalene, toluene, benzene, xylol to the naphthalene waste gas of removing preliminarily, especially to the getting rid of naphthalene, prevents that follow-up waste gas treatment in-process naphthalene from taking place the crystallization, blocks up pipeline or active carbon hole, improves the treatment effeciency in the follow-up waste gas treatment process greatly.
An atomizing spray head 29 is arranged on the outer side of a gas inlet II28 of the wash oil absorption tower 2, a gas inlet II28 is arranged below a gas distributor II21, a two-stage wash oil spraying system is arranged in the wash oil absorption tower 2, the wash oil spraying system at each stage comprises a gas distributor II21, a packing layer II22 is arranged above the gas distributor II21, a wash oil spraying pipe 23 is arranged above a packing layer II22, and a gas outlet II24 is arranged at the upper part of the wash oil absorption tower 2; the gas outlet II24 is connected with the oil-water separator 3, the oil-water separator 3 comprises a gas distributor III31 from bottom to top, and a filler layer III32 is arranged above the gas distributor III 31. The atomizing nozzle 29 sprays water vapor, and the sprayed water vapor primarily separates ammonia, which is easily dissolved in water, in the exhaust gas, and substances such as dust, sand, and the like in the exhaust gas. The washing oil absorption tower 2 removes organic matters through a two-stage washing oil spraying system: gas enters from a gas inlet I28 at the lower part of the washing oil absorption tower and then diffuses upwards to sequentially enter two-stage washing oil spraying systems, the waste gas passes through a gas distributor I21 in the first-stage washing oil spraying system and then is uniformly distributed, the waste gas enters a packing layer I22, oily substances in the waste gas are adsorbed by the packing layer I22, the waste gas continuously rises after passing through the packing layer I22, meanwhile, a washing oil spraying pipe 23 sprays the waste gas, and organic matters such as naphthalene, toluene, benzene, xylene and the like in the waste gas are dissolved in the washing oil by the sprayed washing oil and then are removed; the residual waste gas continuously rises and is discharged after passing through a second-stage oil washing spraying system, and passes through a gas distributor III31 and a filler layer III32 of the oil-water separator 3 at the gas outlet 24, and the washing oil possibly carried in the waste gas is adsorbed and removed again. The exhaust gas from gas distributor III31 enters dynamic wave alkali absorption tower 4 through dynamic wave spray head 42.
A dynamic wave spray head 42 is arranged in front of an air inlet IV41 of the dynamic wave alkali absorption tower 4, and an air inlet IV41 is arranged below the dynamic wave alkali absorption tower 4; the dynamic wave alkali absorption tower 4 is internally provided with two stages of alkali spraying systems, the alkali spraying systems sequentially comprise a gas distributor IV43, a packing layer IV44 and an alkali spraying pipe 45 from bottom to top, and the upper part of the dynamic wave alkali absorption tower 4 is provided with a gas outlet IV 46. The dynamic wave nozzle 42 sprays alkaline solution, the alkaline solution is baking soda solution or caustic soda solution, acidic substances such as hydrogen sulfide in waste gas are primarily absorbed, the waste gas after primary absorption of the acidic substances enters the dynamic wave alkaline absorption tower 4 through the gas distributor IV43, the dynamic wave alkaline absorption tower 4 enables the waste gas to be uniformly distributed, the waste gas uniformly enters the packing layer IV44, and the packing layer IV44 is active carbon or a multi-surface hollow sphere and is used for absorbing the alkaline solution and other substances in the waste gas; and (4) spraying the alkaline solution again from the alkaline spraying pipe 45, spraying the waste gas by the alkaline solution from top to bottom, neutralizing the acidic substances in the waste gas, and removing the acidic substances in the waste gas again. The waste gas is sprayed by a two-stage alkali spraying system in the dynamic wave alkali absorption tower 4 and then enters the three-phase adsorption oxidation tower 6 through a gas outlet IV 46.
The lower part of the three-phase adsorption oxidation tower 6 is provided with a gas inlet VI61, the interior of the three-phase adsorption oxidation tower 6 is provided with a two-stage oxidant spraying system, the oxidant spraying system comprises a gas distributor VI63, a packing layer VI64 and an oxidant spraying pipe 65 from bottom to top, and the upper part of the three-phase adsorption oxidation tower 6 is provided with a gas outlet VI 66; the gas-water separation device 7 is connected with the gas outlet VI66, and the gas-water separation device 7 comprises a gas distributor VII71 and a packing layer VII 72. The gas distributor VI63 redistributes the waste gas entering the three-phase adsorption oxidation tower 6, so that the waste gas uniformly enters the packing layer VI64, and the packing layer VI64 is activated carbon or a multi-surface hollow sphere and absorbs liquid substances in the waste gas; the substance sprayed from the oxidant spraying pipe 65 is hydrogen peroxide aqueous solution, ferrous sulfate is added as an active agent, the hydrogen peroxide and the ferrous sulfate generate hydroxyl, the hydroxyl has strong oxidation effect, and organic matter macromolecules in the waste gas such as carboxylic acid, alcohol, esters and the like can be oxidized into inorganic matter micromolecules; the hydrogen peroxide aqueous solution sprays the waste gas from top to bottom, and neutralizes the alkaline substances in the waste gas to remove the alkaline substances in the waste gas; the waste gas is sprayed by a two-stage oxidant spraying system in the three-phase adsorption oxidation tower 6 and then enters the gas-water separation device 7 through a gas outlet VI66, and the moisture contained in the waste gas is separated out after the waste gas passes through the gas-water separation device 7 and then enters the adsorption/desorption system 8.
The adsorption/desorption system 8 comprises a longitudinal gas distributor 84, a plurality of layers of adsorption beds 85 are arranged behind the longitudinal gas distributor 84, a steam branch pipe 86 is arranged above each layer of adsorption bed 85, and the plurality of steam branch pipes are connected in parallel; an air blower 81 is arranged on an air inlet pipeline 83 of the adsorption/desorption system 8, and a condensation recovery pipeline 87 is arranged on an exhaust pipeline 88 of the adsorption/desorption system 8. The adsorption bed 85 is honeycomb-shaped activated carbon with a large specific surface area, organic matters are adsorbed on the surface of the activated carbon, the activated carbon is saturated after adsorption operation for a period of time, desorption of the system is started, the organic matters which are originally adsorbed on the surface of the activated carbon are desorbed through steam heating, and the organic matters are converted into CO2 and water through catalytic reaction. When the adsorption process of the adsorption bed 85 is carried out, the waste gas enters the adsorption/desorption system 8 through the gas inlet pipeline 83, the gas is uniformly distributed by the longitudinal gas distributor 84 and then flows through the adsorption bed 85, meanwhile, the high-temperature steam in the steam branch pipe 86 heats the waste gas, the organic matters and other substances in the waste gas are adsorbed onto the adsorption bed in the heated state, and the waste gas passing through the adsorption bed is finally discharged through the exhaust pipeline 88; when the desorption process of the adsorption bed 85 is carried out, the valve of the steam branch pipe 86 is closed, the input of high-temperature steam is stopped, and meanwhile, the air blower is opened to introduce air to the direction of the adsorption bed to cool the adsorption bed, so that the absorbed organic matters are released when the adsorption bed is at high temperature, and are recovered through the condensation recovery pipeline 87.
The adsorption/desorption system 8 adopts an activated carbon adsorption/steam desorption mode, and utilizes the adsorption and desorption capacities of activated carbon at different temperatures to carry out adsorption and desorption operations on organic matters.
A method of treating a coking exhaust gas treatment system, comprising the steps of: firstly, the waste gas is subjected to primary treatment on naphthalene toluene, benzene and xylene in the waste gas through a naphthalene recovery system 1; secondly, the waste gas after primary treatment enters an oil washing absorption tower 2 to remove naphthalene, toluene, benzene and xylene in the waste gas again; step three, the waste gas discharged from the oil washing absorption tower 2 enters a dynamic wave alkali absorption tower 4 to remove acidic substances in the waste gas; fourthly, the waste gas from which the acidic substances are removed enters a three-phase adsorption oxidation tower 6, and organic matters in the waste gas in the three-phase adsorption oxidation tower 6 are oxidized into inorganic matters and are discharged along with the waste gas; fifthly, the waste gas containing inorganic matters discharged in the step (iv) enters an adsorption/desorption system 8, and the inorganic matters and the residual organic matters in the waste gas are adsorbed again in a heated state and then discharged.
The substance sprayed out of the three-phase adsorption oxidation tower 6 is hydrogen peroxide aqueous solution, and the active agent ferrous sulfate is added into the hydrogen peroxide aqueous solution.
The naphthalene recovery system 1 comprises the following steps when carrying out primary treatment on naphthalene, toluene, benzene and xylene in waste gas: a. naphthalene-containing waste gas from a coking plant is converged in a waste gas collecting pipeline 124 and enters a gas-liquid separation tower 12 from a waste gas inlet II121, the naphthalene-containing waste gas is condensed in the gas-liquid separation tower 12, waste liquid generated by condensation is discharged into a waste liquid pool 13 through a liquid outlet II123, and the residual condensed waste gas is discharged from a waste gas outlet II122 and enters a naphthalene recovery tower 11 through a waste gas inlet I113; b. the method comprises the following steps that firstly, the waste gas entering the naphthalene recovery tower 11 is discharged from a waste gas outlet I114 after the naphthalene is recovered in the naphthalene recovery tower 11, and the specific process is as follows: the light tar is pumped into the spray pipe 117 by the circulating pump 14 to be sprayed down, and the light tar falls to the bottom of the naphthalene recovery tower 11 after absorbing naphthalene in the waste gas in the spraying process; when the naphthalene content in the light tar is saturated, the light tar is discharged to the waste liquid tank 13 through the liquid discharge port I115. Realizing the recovery of naphthalene in the waste gas. The light tar at the bottom of the naphthalene recovery tower 11 is pumped by a circulating pump in a circulating way, and the naphthalene in the waste gas is removed by spraying for many times until the naphthalene content in the light tar is saturated, and the light tar is discharged through a liquid outlet I115.
The content of each component in the waste gas passing through the waste gas treatment device reaches the standard of table 6 of emission standard of pollutants for coking chemical industry (GB 167171-2012), the treatment effect is good, each pipeline does not need to be cleaned frequently, the activated carbon does not need to be replaced frequently, and the waste gas treatment cost is greatly reduced.
Claims (10)
1. A coking waste gas treatment system is characterized in that: including naphthalene recovery system (1), naphthalene recovery system (1) be connected with wash oil absorption tower (2), wash oil absorption tower (2) are connected with power ripples alkali absorption tower (4) through oil water separator (3), power ripples alkali absorption tower (4) are connected with three-phase adsorption oxidation tower (6) through pipeline (5), three-phase adsorption oxidation tower (6) are connected with adsorption/desorption system (8) through gas-water separation device (7).
2. The coking exhaust gas treatment system of claim 1, characterized in that: the naphthalene recovery system (1) comprises a naphthalene recovery tower (11), a gas-liquid separation tower (12) and a waste liquid pool (13), wherein the middle part of the naphthalene recovery tower (11) is provided with a waste gas inlet I (113), the upper part of the naphthalene recovery tower is provided with a waste gas outlet I (114), and the lower part of the naphthalene recovery tower is provided with a liquid outlet I (115); the waste gas recovery device is characterized in that a waste gas inlet II (121) and a waste gas outlet II (122) are arranged on the upper portion of the gas-liquid separation tower (12), a liquid discharge port II (123) is arranged on the lower portion of the gas-liquid separation tower (12), the waste gas inlet II (121) is connected with a waste gas collecting pipeline (124), the waste gas outlet II (122) is communicated with a waste gas inlet I (113), and the liquid discharge port I (115) and the liquid discharge port II (123) are communicated with a waste liquid pool (13).
3. The coking exhaust gas treatment system of claim 2, characterized in that: a circulating liquid outlet (116) is also arranged on the naphthalene recovery tower (11), a spray pipe (117) is arranged in the naphthalene recovery tower (11), and a circulating pump (14) is arranged between the circulating liquid outlet (116) and the spray pipe (117); a grating layer (118) is arranged above the waste gas inlet I (113), and a demister (119) is arranged below the waste gas outlet I (114).
4. A coking exhaust gas treatment system according to claim 3, in which: the circulating liquid outlet (116) is communicated with a liquid inlet of the circulating pump (14), the spraying pipe (117) is communicated with a liquid outlet of the circulating pump (14), a waste liquid pipe (141) is also communicated with the liquid outlet of the circulating pump (14), and the waste liquid pipe (141) is communicated with the waste liquid pool (13).
5. The coking exhaust gas treatment system of claim 1, characterized in that: an atomizing spray head (29) is arranged on the outer side of a gas inlet II (28) of the washing oil absorption tower (2), the gas inlet II (28) is arranged below a gas distributor II (21), a two-stage washing oil spraying system is arranged in the washing oil absorption tower (2), each stage of washing oil spraying system comprises a gas distributor II (21), a packing layer II (22) is arranged above the gas distributor II (21), a washing oil spraying pipe (23) is arranged above the packing layer II (22), and a gas outlet II (24) is arranged at the upper part of the washing oil absorption tower (2); gas outlet II (24) be connected with oil water separator (3), oil water separator (3) from the bottom up include gas distributor III (31), gas distributor III (31) top is equipped with packing layer III (32).
6. The coking exhaust gas treatment system of claim 1, characterized in that: a dynamic wave spray head (42) is arranged in front of an air inlet IV (41) of the dynamic wave alkali absorption tower (4), and the air inlet IV (41) is arranged below the dynamic wave alkali absorption tower (4); the dynamic wave alkali absorption tower (4) is internally provided with two stages of alkali spraying systems, the alkali spraying systems sequentially comprise a gas distributor IV (43), a packing layer IV (44) and an alkali spraying pipe (45) from bottom to top, and the upper part of the dynamic wave alkali absorption tower (4) is provided with a gas outlet IV (46).
7. The coking exhaust gas treatment system of claim 1, characterized in that: the lower part of the three-phase adsorption oxidation tower (6) is provided with an air inlet VI (61), a two-stage oxidant spraying system is arranged in the three-phase adsorption oxidation tower (6), the oxidant spraying system comprises a gas distributor VI (63), a packing layer VI (64) and an oxidant spraying pipe (65) from bottom to top, and the upper part of the three-phase adsorption oxidation tower (6) is provided with an air outlet VI (66); the gas-water separator is connected with the gas outlet VI (66) and is provided with a gas-water separator (7), and the gas-water separator (7) comprises a gas distributor VII (71) and a packing layer VII (72).
8. The coking exhaust gas treatment system of claim 1, characterized in that: the adsorption/desorption system (8) comprises a longitudinal gas distributor (84), a plurality of layers of adsorption beds (85) are arranged behind the longitudinal gas distributor (84), a steam branch pipe (86) is arranged above each layer of adsorption bed (85), and the plurality of steam branch pipes are connected in parallel and then connected with a steam main pipe (89); an air blower (81) is arranged on an air inlet pipeline (83) of the adsorption/desorption system (8), and a condensation recovery pipeline (87) is arranged on an exhaust pipeline (88) of the adsorption/desorption system (8).
9. The method of treating a coking exhaust gas treatment system according to claims 1 to 8, characterized in that: the method comprises the following steps: firstly, carrying out primary treatment on naphthalene, toluene, benzene and xylene in waste gas by a naphthalene recovery system (1); secondly, the waste gas after primary treatment enters an oil washing absorption tower (2) to remove naphthalene, toluene, benzene and xylene in the waste gas again; step three, the waste gas discharged from the oil washing absorption tower (2) enters a dynamic wave alkali absorption tower (4) to remove acidic substances in the waste gas; fourthly, the waste gas from which the acidic substances are removed enters a three-phase adsorption oxidation tower (6), and organic substances in the waste gas in the three-phase adsorption oxidation tower (6) are oxidized into inorganic substances and are discharged along with the waste gas; fifthly, the waste gas containing inorganic matters discharged in the step (iv) enters an adsorption/desorption system (8) to adsorb the inorganic matters and the residual organic matters in the waste gas again in a heated state and then is discharged.
10. A method of treating a coking exhaust gas treatment system according to claim 9, characterised in that: the naphthalene recovery system (1) comprises the following steps when carrying out primary treatment on naphthalene, toluene, benzene and xylene in waste gas: a. naphthalene-containing waste gas from a coking plant is collected in a waste gas collecting pipeline (124) and enters a gas-liquid separation tower (12) from a waste gas inlet II (121), the naphthalene-containing waste gas is condensed in the gas-liquid separation tower (12), waste liquid generated by condensation is discharged into a waste liquid pool (13) through a liquid discharge port II (123), and the residual condensed waste gas is discharged from a waste gas outlet II (122) and enters a naphthalene recovery tower (11) through a waste gas inlet I (113); b. the method comprises the following steps that waste gas entering a naphthalene recovery tower (11) is discharged from a waste gas outlet I (114) after naphthalene is recovered in the naphthalene recovery tower (11), and the specific process is as follows: the light tar is pumped into a spray pipe (117) by a circulating pump (14) and sprayed down, and the light tar falls to the bottom of a naphthalene recovery tower (11) after absorbing naphthalene in waste gas in the spraying process; when the naphthalene content in the light tar is saturated, the light tar is discharged to a waste liquid pool (13) through a liquid discharge port I (115).
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