CN114292659A - Coal tar deep processing method - Google Patents
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Abstract
The invention discloses a coal tar deep processing method, which comprises the steps of conveying oil gas obtained by the pressure reduction treatment of soft asphalt in a pressure reduction tower into a vacuum tank, washing the oil gas by washing oil, then conveying the oil gas into an acid removal reaction tower for acid removal, and conveying the oil gas subjected to acid removal into a liquid seal tank for circulation through a vacuum pump; simultaneously discloses the structure of the deacidification reaction tower device. The method has the advantages of simple process flow, good acid removal effect, maintenance time and cost saving, and continuous and stable production operation guarantee.
Description
Technical Field
The invention belongs to the technical field of chemical industry, and particularly relates to a deep processing method of coal tar.
Background
At present, the deep processing process of coal tar comprises atmospheric distillation, reduced pressure distillation and industrial naphthalene distillation. The soft asphalt extracted from the bottom of the atmospheric distillation tower is heated to 370 ℃ by a decompression heating furnace and enters a decompression tower, negative pressure is formed in the tower under the action of a vacuum system to extract products, and top oil gas enters the vacuum system. The method comprises the steps of enabling oil gas at the top of a decompression tower to enter a vacuum tank under the action of a vacuum pump, washing oil (absorbing oil for washing benzene or naphthalene compounds from coal gas by utilizing the characteristic that the absorbing oil is similar to and soluble with other components in coal tar and petroleum and used for washing gas generated in the fractionation process so as to enable the gas to absorb benzene, naphthalene and other substances in the gas) to wash the oil gas in a spraying mode, enabling the washing oil to enter a liquid seal tank, enabling the washing oil to be mixed with the washed oil gas by a washing oil circulating pump to enter a vacuum pump, and continuously circulating (the circulating function is to cool the oil gas by using the washing oil, because the vacuum pump has strict requirements on the temperature of an air medium, if the temperature is too high, the vacuum pump cannot work, wherein if the same part of washing oil is continuously circulated in the circulating process, the cooling effect is poor, so that a part of the washing oil is extracted to a non-washed three-mixed oil tank to serve as an industrial naphthalene distillation raw material after being circulated through the liquid seal tank, the reduced production is used to maintain the oil gas cooling effect by replenishing new wash oil. In the process of reduced pressure distillation, a stable vacuum system needs to be established by a vacuum pump to continuously extract materials, but because the vacuum pump has strict requirements on the temperature of an air medium, if the temperature is too high, the vacuum pump cannot work, so that for the air medium with higher temperature, before the air medium enters the vacuum pump, the temperature of the air medium is reduced to be suitable for the operation of the vacuum pump by using wash oil; the vacuum system is established through the pumping action of the vacuum pump, the washing oil flows into the liquid seal tank through the pipeline under the action of gravity, and the tail end of the pipeline is inserted below the liquid level so as to avoid air entering and damage the vacuum state of the system. Under the normal condition of the business turn over volume of wash oil, the liquid seal groove can maintain the stability of original liquid level, also can guarantee that vacuum system is not destroyed), liquid seal groove top tail gas gets into tail gas system. However, the oil gas extracted from the top of the vacuum tower contains more highly corrosive acidic gas hydrogen sulfide, and the oil gas containing hydrogen sulfide can seriously corrode parts such as an impeller and a disc in the vacuum pump, a machine seal sealing cavity, an inner cavity, a machine seal, a baffle, a spacer bolt, a pump cover, a bearing seat, a bearing cover, a bearing and the like when circulating through the vacuum pump, so that the machine seal leakage is caused, the vacuum degree is reduced, the normal production is seriously influenced, the labor intensity of maintenance personnel is high, the maintenance cost is high, and equipment in the subsequent production process is also seriously influenced. Therefore, this problem is urgently needed to be solved.
Disclosure of Invention
The technical problem to be solved by the invention is as follows: the method for deeply processing the coal tar overcomes the defects of the prior art, has simple process flow and good acid removal effect, saves the maintenance time and cost, and ensures continuous and stable operation of production.
In order to solve the technical problems, the technical scheme of the invention is as follows:
a deep processing method of coal tar comprises the following steps:
a. carrying out reduced pressure treatment on the maltha in the reduced pressure tower, wherein oil gas at the top is conveyed to a vacuum tank through a vacuum pump and washed through washing oil, and the rest materials are heavy oil B, heavy oil A and asphalt respectively, and are extracted in a grading manner to enter other processing procedures;
b. conveying the washing oil to a vacuum tank for spraying to absorb substances such as benzene, naphthalene and the like in the oil gas; the washing oil falling into the bottom of the vacuum tank after being sprayed is conveyed into a liquid seal tank through a pump to be prepared for recycling, and the oil gas enters an acid removal reaction tower for acid removal or directly enters the liquid seal tank through a vacuum pump for recycling;
c. neutralizing and deacidifying the oil gas in a deacidification reaction tower by using dilute alkali, feeding the deacidified oil gas into a vacuum pump, and feeding the deacidified oil gas into a liquid seal tank for circulation by using the vacuum pump; introducing the liquid subjected to deacidification into a liquid collecting tank for temporary storage;
the deacidification reaction tower comprises a hollow cylindrical tower body, the top of the tower body is provided with an air outlet, the two sides of the bottom of the tower body are respectively provided with an oil gas inlet and an alkali liquor inlet, and the middle of the bottom of the tower body is provided with a discharge hole; the middle part in the tower body is provided with a lye tank, the lye tank is formed by two hollow cylinders with sealed ends at the bottom, wherein, the cylinder positioned at the outer side is an outer cylinder, the cylinder positioned at the inner side is an inner cylinder, the circle center lines of the outer cylinder and the inner cylinder are overlapped, the outer cylinder and the inner cylinder have the same height, the tops of the outer cylinder and the inner cylinder are provided with a plurality of overflow teeth, and the tooth forms of the inner overflow teeth and the outer overflow teeth are distributed in a staggered way; the alkali liquor inlet is communicated with an alkali liquor pipeline, the alkali liquor pipeline penetrates through the side wall of the tower body, is inserted into the middle of the inner column body from the bottom of the hollow inner column body and is branched and connected to the side wall of the inner column body respectively, and an opening is formed in the side wall of the inner column body at the joint of one side or two sides; the alkali liquor is conveyed into the alkali liquor tank through an opening on the side wall of the inner column body. The alkali liquor pipeline also plays a role in supporting the alkali liquor tank; thus, the overflowed alkali liquor forms an inner annular waterfall and an outer annular waterfall, and acid in the oil gas to be treated is neutralized by the alkali liquor when the oil gas passes through the annular waterfalls. The upper part of the lye tank is provided with a plurality of layers of baffle plates, and the baffle plates at different layers extend downwards from two sides of the inner wall of the tower body to the middle part of the tower body and penetrate through the center line of the tower body to form intersection.
Through the treatment, the oil gas on the top of the tower is pumped into the vacuum tank through the vacuum pump, the oil gas is sprayed and washed for the first time in the vacuum tank through the washing oil, then the washed oil gas enters the deacidification reaction tower for secondary washing, and finally the oil gas entering the vacuum pump is the oil gas which is washed for two times and has removed corrosive substances, so that the oil gas has no corrosive effect on the vacuum pump.
d. And (3) the gas in the liquid seal tank enters a tail gas system for treatment, and the liquid enters a vacuum pump for circulation through a wash oil circulating pump or enters an unwashed three-oil mixing tank to be temporarily stored as an industrial naphthalene distillation raw material for further treatment in a subsequent process.
Preferably, in the step a, the temperature of the bottom of the decompression tower is controlled to be 370-390 ℃, the temperature of the middle part of the decompression tower is controlled to be 252-265 ℃, and the temperature of the top of the decompression tower is controlled to be 80-85 ℃; the pressure of the tower bottom is-18 Kpa to-19 Kpa, the pressure in the tower is-20 Kpa to-22 Kpa, the pressure of the tower top is-32 Kpa to-35 Kpa, and the reaction time is controlled to be 10-12 hr.
Further, in the step a, the temperature of the bottom of the decompression tower is controlled to be 370 ℃, the temperature of the middle of the decompression tower is controlled to be 265 ℃, and the temperature of the top of the decompression tower is controlled to be 85 ℃; the pressure is controlled at-18 Kpa at the bottom of the column, -20Kpa at the top of the column, and-35 Kpa at the top of the column, and the reaction time is controlled at 12 hr.
Preferably, the reaction temperature in the step b is 50-55 ℃, the pressure is controlled to be-35-40 KPa, and the flow rate of the washing oil is controlled to be 600-700 kg/h.
Furthermore, in the step b, the reaction temperature is 50 ℃, the pressure is controlled to be-40 KPa, and the flow rate of the washing oil is controlled to be 650 kg/h.
Preferably, in the step c, the reaction temperature is 42-47 ℃, the pressure is controlled to be-35-40 KPa, and the oil-gas flow is controlled to be 720-750 m3The flow rate of the dilute alkali is controlled between 1000kg/h and 1500 kg/h.
Further, in the step c, the reaction temperature is 42-47 ℃, the pressure is controlled to be-35-40 KPa, and the oil-gas flow is controlled to be 720-750 m3The flow rate of the dilute alkali is controlled at 1000 kg/h.
Preferably, the dilute alkali in step c is 21% sodium hydroxide, 19% potassium hydroxide, 20% barium hydroxide or 21% calcium hydroxide.
Further, the dilute alkali in the step c is 21% sodium hydroxide.
Preferably, the upper part of the liquid collecting tank in the step c is provided with a gas outlet communicated with a tail gas system, and the lower part of the liquid collecting tank is provided with a discharge hole communicated with a dilute alkali supply system, so that the dilute alkali can be recycled.
Preferably, the oil gas inlet is connected with an oil gas pipeline, the gas outlet of the oil gas pipeline is arranged by being attached to the tower body wall, or the oil gas pipeline extends into the bottom of the lye tank, the bottom corresponding to the end sealing of the lye tank is arranged in an annular mode, and the upper part of the annular pipeline is provided with a plurality of gas outlets.
Preferably, the distance between the outer side of the outer column body and the inner wall of the tower body is 4.5-5 cm, and the distance between the outer column body and the inner column body is 5.5-6.5 cm.
Furthermore, the distance between the outer side of the outer column body and the inner wall of the tower body is 5 cm, and the distance between the outer column body and the inner column body is 6.2 cm.
Because the outer column body is closer to the inner wall of the tower body, when the air outlet of the oil gas pipeline is arranged close to the wall of the tower body, oil gas enters and then is conveyed upwards through vacuum and must pass through the alkali liquor waterfall; when the gas outlet of the oil gas pipeline is arranged between two layers of alkali liquid waterfalls formed by the outer column body and the inner column body, the oil gas is conveyed upwards and must penetrate through the alkali liquid waterfalls, and thus, acid in the oil gas can be fully neutralized by the alkali liquid.
Preferably, the overflow teeth of the outer cylinder and the inner cylinder have the same structure, and the overflow teeth of the outer cylinder and the overflow teeth of the inner cylinder are arranged in a staggered manner when viewed from the circle center line to the external view angle, namely, the tooth crest of the overflow teeth of the outer cylinder at the position from the circle center to the circumferential connecting line corresponds to the tooth trough of the overflow teeth of the inner cylinder.
Preferably, the length of the crossing part between two layers of the baffle plate is one fifth to one fourth of the maximum length of the baffle plate.
Furthermore, the length of the cross part between two layers of the baffle plate is one fifth of the maximum length of the baffle plate.
Preferably, the baffle plate inclines downwards 15-18 degrees.
Further, the baffle plate is inclined downwards by 15 degrees.
Preferably, the distance between the baffle plates on the same side is 15-20 cm.
Furthermore, the distance between the baffle plates on the same side is 20 cm.
Due to the adoption of the technical scheme, the invention has the beneficial effects that:
1. the tower body of the deacidification reaction tower is internally provided with an alkali liquor tank which is a zigzag overflow device, dilute alkali liquor firstly enters a cavity formed by the inner cylinder body from the bottom, then branches enter the alkali liquor tank through the side wall of the inner cylinder body, overflow is generated after the dilute alkali liquor is filled in the alkali liquor tank to form inner and outer alkali liquor waterfalls, and acid substances (mainly hydrogen sulfide gas) in oil gas positively pass through the waterfalls formed by the dilute alkali liquor when flowing upwards, so that the acid substances are neutralized, the concentration of acid gas is reduced, and the acid gas is prevented from flowing upwards to enter a vacuum pump and follow-up equipment to be corroded.
2. The invention designs the baffle plate on the upper part of the lye tank in the deacidification reaction tower, because the specific gravity of the gas is different from that of the liquid, when the liquid and the gas are mixed and flow together, if the liquid meets the blockage, the gas can be baffled and moved away, and the liquid continues to have a forward speed because of inertia, the forward liquid is attached to the wall surface of the blockage, and is downwards converged to the bottom of the deacidification reaction tower under the action of the gravity, and is discharged through a discharge hole; therefore, the oil-gas moisture can be separated through the baffle plate, so that the oil-gas moisture entering the vacuum pump is reduced.
In a word, the invention overcomes the defects of the prior art, has simple process flow and good acid removal effect, saves the maintenance time and the maintenance cost, and ensures the continuous and stable operation of production.
Drawings
The invention is further illustrated with reference to the following figures and examples.
FIG. 1 is a process flow diagram of the present invention;
FIG. 2 is a schematic diagram of the acid removal reaction tower according to the present invention;
FIG. 3 is a schematic sectional view of an alkali solution tank and an alkali solution pipeline in the deacidification reaction tower according to the present invention;
in the figure, 1, a vacuum tower; 2. a vacuum pump; 3. a vacuum tank; 4. a deacidification reaction tower; 41. a tower body; 42. an air outlet; 43. a discharge port; 44. a lye tank; 441. an outer cylinder; 442. an inner cylinder; 443. an overflow tooth; 45. an alkali liquor pipeline; 46. a baffle plate; 47. an oil and gas pipeline; 5. liquid seal groove; 6. a washing oil circulating pump; 7. a liquid collecting tank.
Detailed Description
The invention is further illustrated by the following examples.
The experimental parameters which are not specified in the embodiments are all the preferable parameters in the foregoing technical solutions, and are not described in detail in the specific embodiments.
Example 1 brief description of the process of the invention
In the deep processing process of coal tar, soft pitch extracted from the bottom of an atmospheric distillation tower is heated to 370 ℃ by a decompression heating furnace and enters a decompression tower 1, negative pressure is formed in the tower under the action of a vacuum system to extract products, oil gas at the top of the decompression tower 1 enters a vacuum tank 3 under the action of a vacuum pump 2, the oil gas in the vacuum tank 3 is washed by washing oil input from the outside of the vacuum tank 3, the washed oil gas enters an acid removal reaction tower 4, the washed liquid is conveyed to a liquid seal tank 5, the gas in the liquid seal tank 5 is conveyed to a tail gas system (not marked) for treatment and then discharged, and the liquid in the liquid seal tank 5 is conveyed to the vacuum pump 2 by a washing oil circulating pump 6 and circulated to the liquid seal tank 5 or conveyed to a three-component oil mixing tank (not marked) for treatment; an external dilute alkali solution is introduced into the deacidification reaction tower 4 for acid neutralization, wherein the treated gas is conveyed into the vacuum pump 2 and then conveyed into the liquid seal tank 5 for circulation, the treated liquid is conveyed into the liquid collecting tank 7, the gas in the liquid collecting tank 7 is conveyed into the tail gas system for treatment, and the liquid is conveyed into a dilute alkali solution supply system (not shown) for recycling.
Wherein, the deacidification reaction tower 4 comprises a hollow cylindrical tower body 41, the top of the tower body 41 is provided with an air outlet 42, the two sides of the bottom are respectively provided with an oil gas inlet (not marked) and an alkali liquor inlet (not marked), and the middle of the bottom is provided with a discharge hole 43; the middle part in the tower body is provided with a lye tank 44, the lye tank 44 is composed of two hollow cylinders with sealed ends at the bottom, wherein the cylinder positioned at the outer side is an outer cylinder 441, the cylinder positioned at the inner side is an inner cylinder 442, the circle center lines of the outer cylinder 441 and the inner cylinder 442 are overlapped, the outer cylinder 441 and the inner cylinder 442 have the same height, and the tops of the outer cylinder 441 and the inner cylinder 442 are provided with a plurality of overflow teeth 443; the alkali liquor inlet is communicated with an alkali liquor pipeline 45, the alkali liquor pipeline 45 penetrates through the side wall of the tower body 41, is inserted into the middle of the inner column body 442 from the bottom of the hollow inner column body 442, is separated towards two sides, is respectively communicated with the side wall of the inner column body 442, and conveys alkali liquor to the alkali liquor tank 44 through openings in the side walls on two sides of the inner column body 442. The upper part of the lye tank 44 is provided with a plurality of layers of baffle plates 46, and the baffle plates 46 at different layers extend downwards from two sides of the inner wall of the tower body 41 to the middle part of the tower body 41 and penetrate through the central line of the tower body 41 to form intersection. The oil gas inlet is connected with an oil gas pipeline 47, the oil gas pipeline 47 extends into the bottom of the lye tank 44, the bottom of the sealed end of the lye tank 44 is arranged in an annular mode, and the upper portion of the annular pipeline is provided with a plurality of gas outlets (not shown).
Example 2
a. And (3) carrying out reduced pressure treatment on the maltha in the reduced pressure tower 1: the soft asphalt pumped by a pump (P84004A/B) is pumped out of an atmospheric distillation tower, sent to a reduced pressure heating furnace to be heated until the temperature of the tower bottom is 370 ℃, the pressure is controlled to be-18 Kpa, the temperature in the tower is 265 ℃ and the pressure is controlled to be-20 Kpa under the action of a vacuum system, heavy oil B is extracted from the tower, pumped out by a heavy oil B pump (P84102A/B) and passes through a heavy oil B waste boiler, and part of the heavy oil B is refluxed and extracted into a CB oil heavy oil tank. The upper temperature of the tower is 85 ℃, the pressure is controlled to be-35 Kpa, heavy oil A is extracted from the tower, the heavy oil A is extracted by a heavy oil A extraction pump (P84103A/B) and passes through a waste boiler of the heavy oil A and a heavy oil A2# cooler, a part of the heavy oil A flows back, and a part of the heavy oil A is extracted and merged with the heavy oil B to a CB oil heavy oil tank. And (4) after the oil gas at the top of the tower enters a vacuum system. The asphalt at the bottom of the tower enters a first-stage asphalt retention tank (V84101), then a part of the asphalt is circulated to the retention tank by a first-stage asphalt circulating pump (P84104A/B), a part of the asphalt is extracted to a second-stage asphalt retention tank (V84102), a part of the asphalt is circulated to the retention tank by a second-stage asphalt circulating pump (P84108A/B), a part of the asphalt is mixed with soft asphalt and then enters a vacuum furnace, and the other part of the asphalt is extracted to a finished product by an asphalt extraction pump (P84101A/B) through an asphalt waste pot; the reaction is carried out for 12 hours in total, wherein the top oil gas (the content of the detected hydrogen sulfide is 153000 mu mol/mol) is conveyed into a vacuum tank 3 through a vacuum pump 2 for washing;
b. conveying the washing oil into a vacuum tank 3 for spraying, wherein the reaction temperature in the vacuum tank 3 is 50 ℃, the pressure is controlled at-40 KPa, the washing oil flow is controlled at 650kg/h, and substances such as benzene, naphthalene and the like in oil gas are absorbed; the liquid which falls into the bottom of the vacuum tank 3 after being sprayed is conveyed into a liquid seal tank 5 through a pump to be prepared for recycling, and the oil gas enters an acid removal reaction tower 4 for acid removal or directly enters the liquid seal tank 5 through a vacuum pump 2 for circulation;
c. neutralizing and deacidifying the oil gas in a deacidification reaction tower 4 by 21 percent sodium hydroxide, controlling the reaction temperature in the deacidification reaction tower 4 at 45 ℃, the pressure at-40 KPa and the oil gas flow at 720m3The flow rate of 21 percent sodium hydroxide is controlled to be 1200 kg/h; the oil gas after acid removal enters a vacuum pump 2 and enters a liquid seal tank 5 through the vacuum pump 2 for circulation; detecting the content of hydrogen sulfide of the oil gas after deacidification by 30 mu mol/mol, and introducing the liquid after deacidification into a liquid collecting tank 7 for temporary storage;
d. and the gas in the liquid seal tank 5 enters a tail gas system for treatment, and the liquid enters the vacuum pump 2 for circulation through the oil washing circulating pump 6.
Example 3
a. And (3) carrying out reduced pressure treatment on the maltha in the reduced pressure tower 1: the soft asphalt pumped by a pump (P84004A/B) is pumped out of an atmospheric distillation tower, sent to a reduced pressure heating furnace to be heated until the temperature of the bottom of the tower is 390 ℃, the pressure is controlled to be-19 Kpa, the temperature in the tower is 252 ℃ and the pressure is controlled to be-22 Kpa under the action of a vacuum system, heavy oil B is extracted from the tower, pumped out by a heavy oil B pump (P84102A/B) and passes through a heavy oil B waste boiler, and part of the heavy oil B is refluxed and extracted into a CB oil heavy oil tank. The upper temperature of the tower is 80 ℃, the pressure is controlled to be-32 Kpa, heavy oil A is extracted from the tower, the heavy oil A is extracted by a heavy oil A extraction pump (P84103A/B) and passes through a waste boiler of the heavy oil A and a heavy oil A2# cooler, a part of the heavy oil A flows back, and a part of the heavy oil A is extracted and merged with the heavy oil B to a CB oil heavy oil tank. And (4) after the oil gas at the top of the tower enters a vacuum system. The asphalt at the bottom of the tower enters a first-stage asphalt retention tank (V84101), then a part of the asphalt is circulated to the retention tank by a first-stage asphalt circulating pump (P84104A/B), a part of the asphalt is extracted to a second-stage asphalt retention tank (V84102), a part of the asphalt is circulated to the retention tank by a second-stage asphalt circulating pump (P84108A/B), a part of the asphalt is mixed with soft asphalt and then enters a vacuum furnace, and the other part of the asphalt is extracted to a finished product by an asphalt extraction pump (P84101A/B) through an asphalt waste pot; the reaction is carried out for 10 hours in total, wherein the top oil gas (the content of the detected hydrogen sulfide is 153400 mu mol/mol) is conveyed into a vacuum tank 3 through a vacuum pump 2 for washing;
b. conveying the washing oil into a vacuum tank 3 for spraying, wherein the reaction temperature in the vacuum tank 3 is 55 ℃, the pressure is controlled at-35 KPa, the washing oil flow is controlled at 700kg/h, and substances such as benzene, naphthalene and the like in oil gas are absorbed; the liquid which falls into the bottom of the vacuum tank 3 after being sprayed is conveyed into a liquid seal tank 5 through a pump to be prepared for recycling, and the oil gas enters an acid removal reaction tower 4 for acid removal or directly enters the liquid seal tank 5 through a vacuum pump 2 for circulation;
c. oil gas is neutralized and deacidified in a deacidification reaction tower 4 by 19 percent of potassium hydroxide, the reaction temperature in the deacidification reaction tower 4 is 42 ℃, the pressure is controlled to be-35 KPa, and the oil gas flow is controlled to be 750m3The flow rate of 19 percent potassium hydroxide is controlled to be 1000 kg/h; the oil gas after acid removal enters a vacuum pump 2 and enters a liquid seal tank 5 through the vacuum pump 2 for circulation; the content of hydrogen sulfide of the oil gas after acid removal is 45 mu mol through detectionAnd/mol, introducing the liquid after deacidification into a liquid collecting tank 7 for temporary storage;
d. and the gas in the liquid seal tank 5 enters a tail gas system for treatment, and the liquid enters the vacuum pump 2 for circulation through the oil washing circulating pump 6.
Example 4
a. And (3) carrying out reduced pressure treatment on the maltha in the reduced pressure tower 1: the soft asphalt pumped by a pump (P84004A/B) is pumped out of an atmospheric distillation tower, sent to a reduced pressure heating furnace to be heated until the temperature of the bottom of the tower is 390 ℃, the pressure is controlled to be-19 Kpa, the temperature in the tower is 265 ℃ and the pressure is controlled to be-20 Kpa under the action of a vacuum system, heavy oil B is extracted from the tower, pumped out by a heavy oil B pump (P84102A/B), passes through a heavy oil B waste boiler, part of the heavy oil B is refluxed, and part of the heavy oil B is extracted to a CB oil heavy oil tank. The upper temperature of the tower is 80 ℃, the pressure is controlled to be-35 Kpa, heavy oil A is extracted from the tower, the heavy oil A is extracted by a heavy oil A extraction pump (P84103A/B) and passes through a waste boiler of the heavy oil A and a heavy oil A2# cooler, a part of the heavy oil A flows back, and a part of the heavy oil A is extracted and merged with the heavy oil B to a CB oil heavy oil tank. And (4) after the oil gas at the top of the tower enters a vacuum system. The asphalt at the bottom of the tower enters a first-stage asphalt retention tank (V84101), then a part of the asphalt is circulated to the retention tank by a first-stage asphalt circulating pump (P84104A/B), a part of the asphalt is extracted to a second-stage asphalt retention tank (V84102), a part of the asphalt is circulated to the retention tank by a second-stage asphalt circulating pump (P84108A/B), a part of the asphalt is mixed with soft asphalt and then enters a vacuum furnace, and the other part of the asphalt is extracted to a finished product by an asphalt extraction pump (P84101A/B) through an asphalt waste pot; the reaction is carried out for 12 hours in total, wherein the top oil gas (the content of the detected hydrogen sulfide is 153100 mu mol/mol) is conveyed into a vacuum tank 3 through a vacuum pump 2 for washing;
b. conveying the washing oil into a vacuum tank 3 for spraying, wherein the reaction temperature in the vacuum tank 3 is 50 ℃, the pressure is controlled at-40 KPa, the washing oil flow is controlled at 650kg/h, and substances such as benzene, naphthalene and the like in oil gas are absorbed; the liquid which falls into the bottom of the vacuum tank 3 after being sprayed is conveyed into a liquid seal tank 5 through a pump to be prepared for recycling, and the oil gas enters an acid removal reaction tower 4 for acid removal or directly enters the liquid seal tank 5 through a vacuum pump 2 for circulation;
c. oil gas is neutralized and deacidified in a deacidification reaction tower 4 by 20 percent of barium hydroxide, and the reaction temperature in the deacidification reaction tower 4 isThe pressure is controlled to be-35 KPa at 47 ℃, and the oil-gas flow is controlled to be 720m3The flow rate of 20 percent barium hydroxide is controlled to be 1500 kg/h; the oil gas after acid removal enters a vacuum pump 2 and enters a liquid seal tank 5 through the vacuum pump 2 for circulation; detecting the content of hydrogen sulfide in the deacidified oil gas by 38 mu mol/mol, and introducing the deacidified liquid into a liquid collecting tank 7 for temporary storage;
d. and the gas in the liquid seal tank 5 enters a tail gas system for treatment, and the liquid enters the vacuum pump 2 for circulation through the oil washing circulating pump 6.
Example 5
The 21 percent sodium hydroxide in the example 2 is replaced by 21 percent calcium hydroxide, other process conditions are not changed, and the content of the hydrogen sulfide in the treated oil gas is changed from 153000 mu mol/mol to 35 mu mol/mol.
To summarize:
by comparing the processes of examples 2 to 5, the following conclusions can be drawn: the best treatment effect of the embodiment 2 is achieved, the content of hydrogen sulfide is greatly reduced after treatment, a vacuum pump disc, an end cover, an impeller, a pump body, a pump shaft, a sealing cavity and other corroded parts need to be replaced every year before the method is implemented, the maintenance cost of 71.72 ten thousand yuan is added, the vacuum pump and other corresponding parts are not replaced within 12 months after the method is implemented, the maintenance cost is saved by seventy hundred thousand, the downtime is reduced by five hundred to four hours, the labor is saved by sixty three parts, meanwhile, the peculiar smell generated due to leakage on site is obviously reduced, and the working environment of operators is improved. Therefore, the acid removal effect is good, the maintenance time and the maintenance cost are saved, and the production benefit is indirectly increased.
It should be understood that these examples are for illustrative purposes only and are not intended to limit the scope of the present invention. Further, it should be understood that various changes or modifications of the present invention may be made by those skilled in the art after reading the teaching of the present invention, and such equivalents may fall within the scope of the present invention as defined in the appended claims.
Claims (10)
1. The deep processing method of the coal tar is characterized by comprising the following steps:
a. carrying out reduced pressure treatment on the maltha in the reduced pressure tower, wherein oil gas at the top is conveyed to a vacuum tank through a vacuum pump and washed through washing oil, and the rest materials are heavy oil B, heavy oil A and asphalt respectively, and are extracted in a grading manner to enter other processing procedures;
b. conveying the washing oil into a vacuum tank for spraying, conveying the washing oil falling into the bottom of the vacuum tank after spraying into a liquid seal tank through a pump for preparation for recycling, and conveying oil gas into an acid removal reaction tower for removing acid or directly into the liquid seal tank through a vacuum pump for recycling;
c. neutralizing and deacidifying the oil gas in a deacidification reaction tower by using dilute alkali, feeding the deacidified oil gas into a vacuum pump, and feeding the deacidified oil gas into a liquid seal tank for circulation by using the vacuum pump; introducing the liquid subjected to deacidification into a liquid collecting tank for temporary storage;
the deacidification reaction tower comprises a hollow cylindrical tower body, the top of the tower body is provided with an air outlet, the two sides of the bottom of the tower body are respectively provided with an oil gas inlet and an alkali liquor inlet, and the middle of the bottom of the tower body is provided with a discharge hole; the middle part in the tower body is provided with a lye tank, the lye tank is formed by two hollow cylinders with sealed ends at the bottom, wherein the cylinder positioned at the outer side is an outer cylinder, the cylinder positioned at the inner side is an inner cylinder, the circle center lines of the outer cylinder and the inner cylinder are overlapped, the outer cylinder and the inner cylinder have the same height, the tops of the outer cylinder and the inner cylinder are provided with a plurality of overflow teeth, and the tooth forms of the inner overflow teeth and the outer overflow teeth are distributed in a staggered manner; the alkali liquor inlet is communicated with an alkali liquor pipeline, the alkali liquor pipeline penetrates through the side wall of the tower body, is inserted into the middle of the inner column body from the bottom of the hollow inner column body and is branched and connected to the side wall of the inner column body respectively, and an opening is formed in the side wall of the inner column body at the joint of one side or two sides; the upper part of the lye tank is provided with a plurality of layers of baffle plates, and the baffle plates at different layers extend downwards from two sides of the inner wall of the tower body to the middle part of the tower body and penetrate through the center line of the tower body to form intersection.
d. And (3) the gas in the liquid seal tank enters a tail gas system for treatment, and the liquid enters a vacuum pump for circulation through a wash oil circulating pump or enters an unwashed three-oil mixing tank to be temporarily stored as an industrial naphthalene distillation raw material for further treatment in a subsequent process.
2. The method for further processing the coal tar according to claim 1, characterized in that: in the step a, the temperature of the bottom of the pressure reducing tower is controlled to be 370-390 ℃, the temperature of the middle tower is controlled to be 252-265 ℃, and the temperature of the top of the tower is controlled to be 80-85 ℃; the pressure of the tower bottom is-18 Kpa to-19 Kpa, the pressure in the tower is-20 Kpa to-22 Kpa, the pressure of the tower top is-32 Kpa to-35 Kpa, and the reaction time is controlled to be 10-12 hr.
3. The method for further processing the coal tar according to claim 1, characterized in that: in the step b, the reaction temperature is 50-55 ℃, the pressure is controlled to be-35-40 KPa, and the oil washing flow is controlled to be 600-700 kg/h.
4. The method for further processing the coal tar according to claim 1, characterized in that: in the step c, the reaction temperature is 42-47 ℃, the pressure is controlled to be-35 to-40 KPa, and the oil-gas flow is controlled to be 720-750 m3The flow rate of the dilute alkali is controlled between 1000kg/h and 1500 kg/h.
5. The method for further processing the coal tar according to claim 1, characterized in that: and the dilute alkali in the step c is 21% of sodium hydroxide, 19% of potassium hydroxide, 20% of barium hydroxide or 21% of calcium hydroxide.
6. The method for further processing the coal tar according to claim 1, characterized in that: and c, arranging a gas outlet at the upper part of the liquid collecting tank in the step c to be communicated with a tail gas system, arranging a discharge hole at the lower part of the liquid collecting tank to be communicated with a dilute alkali supply system, and recycling the dilute alkali.
7. The method for further processing the coal tar according to claim 1, characterized in that: the oil gas inlet is connected with an oil gas pipeline, the gas outlet of the oil gas pipeline is arranged close to the tower body wall, or the oil gas pipeline extends into the bottom of the lye tank, the bottom corresponding to the end sealing of the lye tank is arranged in an annular mode, and the upper portion of the annular pipeline is provided with a plurality of gas outlets.
8. The method for further processing the coal tar according to claim 1, characterized in that: the distance between the outer side of the outer column body and the inner wall of the tower body is 4.5-5 cm, and the distance between the outer column body and the inner column body is 5.5-6.5 cm.
9. The method for further processing the coal tar according to claim 1, characterized in that: the baffle plates incline downwards 15-18 degrees, and the distance between baffle plates on the same side is 15-20 cm.
10. The method for further processing the coal tar according to claim 1, characterized in that: the length of the crossing part between two layers of the baffle plate is one fifth to one fourth of the maximum length of the baffle plate.
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| CN114292659B (en) | 2023-09-01 |
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