CN114292659B - Deep processing method of coal tar - Google Patents
Deep processing method of coal tar Download PDFInfo
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- CN114292659B CN114292659B CN202210082892.9A CN202210082892A CN114292659B CN 114292659 B CN114292659 B CN 114292659B CN 202210082892 A CN202210082892 A CN 202210082892A CN 114292659 B CN114292659 B CN 114292659B
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Abstract
The application discloses a coal tar deep processing method, which comprises the steps of conveying oil gas obtained by decompressing soft asphalt in a decompressing 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 after acid removal into a liquid seal tank for circulation by a vacuum pump; meanwhile, the structure of the acid removal reaction tower device is disclosed. The application has simple process flow and good acid removal effect, saves maintenance time and cost and ensures continuous and stable operation of production.
Description
Technical Field
The application belongs to the technical field of chemical industry, and particularly relates to a coal tar deep processing method.
Background
At present, the deep processing process of coal tar comprises atmospheric distillation, reduced pressure distillation and industrial naphthalene distillation. And heating the soft asphalt pumped from the bottom of the atmospheric distillation tower to 370 ℃ through a decompression heating furnace, entering the decompression tower, forming negative pressure in the tower under the action of a vacuum system, extracting products, and enabling top oil gas to enter the vacuum system. The oil gas at the top of the vacuum tower enters a vacuum tank under the action of a vacuum pump, wash oil (the absorption oil for washing benzene or naphthalene compounds from coal gas is used for washing gas generated in the fractionation process by utilizing the characteristic that the absorption oil is similar to other components in coal tar and petroleum, and is used for washing the gas to absorb substances such as benzene and naphthalene in the gas) is sprayed, then the wash oil enters a liquid seal tank, and the wash oil is mixed with the washed oil gas by a wash oil circulating pump to enter the vacuum pump and continuously circulate (the circulation effect is that the wash oil is used for cooling the oil gas, and 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; in the reduced pressure distillation process, a stable vacuum system is required to be established through a vacuum pump to carry out continuous material extraction, but the vacuum pump has strict requirements on the temperature of an air medium, if the temperature is too high, the vacuum pump cannot work, therefore, for the air medium with higher temperature, the temperature of the air medium is reduced to be suitable for the operation of the vacuum pump by using the wash oil before the air medium enters the vacuum pump, a vacuum system is established through the pumping action of the vacuum pump, the wash oil flows into the liquid seal tank through a pipeline under the action of gravity, and the tail end of the pipeline is inserted below the liquid level so as to avoid air from entering and damage the vacuum state of the system, that is, the vacuum system is not destroyed, and the tail gas at the top of the liquid seal tank enters the tail gas system. However, because the oil gas pumped from the top of the vacuum tower contains more acid gas hydrogen sulfide with strong corrosiveness, the oil gas containing hydrogen sulfide can seriously corrode parts such as impellers and discs in the vacuum pump when circulating through the vacuum pump, such as a mechanical seal sealing cavity, an inner cavity, a mechanical seal, a baffle, a gauge bolt, a pump cover, a bearing seat, a bearing cover, a bearing and the like, thereby causing mechanical seal leakage, reducing the vacuum degree, seriously influencing normal production, having great labor intensity of maintenance personnel and high maintenance cost, and seriously influencing equipment in the subsequent production process. Therefore, this problem is urgently needed to be solved.
Disclosure of Invention
The technical problems to be solved by the application are as follows: the coal tar deep processing method overcomes the defects of the prior art, has simple process flow and good acid removal effect, saves maintenance time and cost, and ensures continuous and stable operation of production.
In order to solve the technical problems, the technical scheme of the application is as follows:
a coal tar deep processing method comprises the following steps:
a. carrying out decompression treatment on soft asphalt in a decompression tower, wherein oil gas at the top is conveyed into a vacuum tank through a vacuum pump and is washed through washing oil, and the residual materials are heavy oil B, heavy oil A and asphalt respectively, and are extracted in stages to enter other processing procedures;
b. conveying the washing oil into a vacuum tank for spraying, and absorbing substances such as benzene, naphthalene and the like in the oil gas; the washing oil which falls into the bottom of the vacuum tank after spraying is conveyed into the liquid seal tank through a pump for recycling, and the oil gas enters an acid removal reaction tower for acid removal or directly enters the liquid seal tank through the vacuum pump for recycling;
c. neutralizing and acid removing the oil gas in an acid removing reaction tower through dilute alkali, and enabling the oil gas after acid removal to enter a vacuum pump and enter a liquid seal tank for circulation through the vacuum pump; introducing the liquid after acid removal into a liquid collecting tank for temporary storage;
the deacidification reaction tower comprises a hollow cylindrical tower body, wherein the top of the tower body is provided with an air outlet, the two sides of the bottom are respectively provided with an oil gas inlet and an alkali liquor inlet, and the middle of the bottom is provided with a discharge hole; the middle part in the tower body is provided with an alkali liquid tank, the alkali liquid tank is formed by two hollow cylinders with end-capped bottoms, 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 are equal in height, the top parts of the outer cylinder and the inner cylinder are provided with a plurality of overflow teeth, and the tooth shapes of the inner overflow teeth and the overflow teeth are distributed in a staggered mode; the alkali liquor inlet is communicated with an alkali liquor pipeline, the alkali liquor pipeline passes 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 bifurcated to be respectively connected to the side wall of the inner column body, and the side wall of the inner column body at the joint of one side or two sides is provided with an opening; the alkali liquor is conveyed into the alkali liquor tank through the 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 waterfall. The upper part of the alkali liquid 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 cross through the central line of the tower body;
through the treatment, the oil gas at the top of the tower is pumped into the vacuum tank by the vacuum pump, is sprayed into the vacuum tank by the washing oil for the first time, then enters the acid removal reaction tower for secondary washing, and finally enters the vacuum pump, and the oil gas after the two washing is the oil gas from which corrosive substances are removed, so that the oil gas has no corrosion effect on the vacuum pump.
d. The gas in the liquid seal tank enters into the tail gas system for treatment, and the liquid enters into the vacuum pump for circulation through the wash oil circulating pump, or enters into the unwashed three-mixed oil tank to serve as industrial naphthalene distillation raw material for temporary storage, so that the subsequent process is continued for treatment.
Preferably, in the step a, the temperature of the bottom of the vacuum tower is controlled to be 370-390 ℃, 252-265 ℃ in the tower and 80-85 ℃ at the top of the tower; the pressure at the bottom of the tower is-18 to-19 KPa, the pressure in the tower is-20 to-22 KPa, the pressure at the top of the tower is-32 to-35 KPa, and the reaction time is controlled to be 10 to 12 hours.
Further, in the step a, the temperature of the bottom of the vacuum tower is controlled at 370 ℃, the temperature in the tower is 265 ℃, and the temperature of the top of the tower is 85 ℃; the pressure is controlled at the bottom pressure of-18 KPa, the pressure in the tower of-20 KPa and the pressure at the top of the tower of-35 KPa, and the reaction time is controlled at 12h.
Preferably, the reaction temperature in the vacuum tank in the step b is 50-55 ℃, the pressure is controlled to be minus 35 to minus 40KPa, and the wash oil flow is controlled to be 600 kg/h-700 kg/h.
Further, the reaction temperature in the vacuum tank in the step b is 50 ℃, the pressure is controlled at-40 KPa, and the wash oil flow is controlled at 650kg/h.
Preferably, the reaction temperature in the acid removal reaction tower in the step c is 42-47 ℃, the pressure is controlled to be minus 35 to minus 40KPa, and the oil gas flow is controlled to be 720-750 m 3 And/h, controlling the flow rate of the dilute alkali at 1000 kg/h-1500 kg/h.
Further, the reaction temperature in the acid removal reaction tower in the step c is 42-47 ℃ and the pressure is highThe force is controlled to be minus 35 to minus 40KPa, and the oil gas flow is controlled to be 720 to 750m 3 And/h, controlling the flow rate of the dilute alkali at 1000kg/h.
Preferably, the dilute alkali in the step c is sodium hydroxide with a concentration of 21%, potassium hydroxide with a concentration of 19%, barium hydroxide with a concentration of 20% or calcium hydroxide with a concentration of 21%.
Further, in the step c, the dilute alkali 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 the tail gas system, and the lower part of the liquid collecting tank is provided with a discharge outlet communicated with the dilute alkali supply system, so that the dilute alkali is recycled.
Preferably, the oil gas inlet is connected with an oil gas pipeline, the gas outlet of the oil gas pipeline is arranged close to the wall of the tower body, or the oil gas pipeline extends into the bottom of the alkali liquor tank, the bottom corresponding to the end closure of the alkali liquor tank is arranged in a ring shape, and a plurality of gas outlets are formed in the upper part of the ring-shaped pipeline.
Preferably, the distance between the outer side of the outer column and the inner wall of the column 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.
Further, the distance between the outer side of the outer column body and the inner wall of the column body is 5 cm, and the distance between the outer column body and the inner column body is 6.2 cm.
Because the distance between the outer column body and the inner wall of the tower body is relatively short, when the gas outlet of the oil gas pipeline is arranged on the wall of the tower body, the oil gas also needs to pass through the alkali lye waterfall when being conveyed upwards through vacuum after entering; when the gas outlet of the oil gas pipeline is arranged between the two alkali lye waterfalls formed by the outer column body and the inner column body, the oil gas is conveyed upwards to more necessarily pass through the alkali lye waterfall, so that acid in the oil gas can be fully neutralized by alkali lye.
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 inner cylinder are staggered from each other when seen from the outside view angle of the circle center line, namely, the tooth peaks of the overflow teeth of the outer cylinder at the position of the circle center to the circumference connecting line correspond to the tooth valleys of the overflow teeth of the inner cylinder.
Preferably, the length of the crossing part between the two layers of the baffle plate is one fifth to one fourth of the maximum length of the baffle plate.
Further, the length of the crossing part between the two layers of the baffle plates is one fifth of the maximum length of the baffle plates.
Preferably, the baffle is inclined downwardly at an angle of 15 to 18.
Further, the baffle plate is inclined downward by 15 degrees.
Preferably, the interval between the baffle plates on the same side is 15-20 cm.
Further, the interval between the baffle plates on the same side is 20 cm.
Due to the adoption of the technical scheme, the application has the beneficial effects that:
1. the application has the advantages that the alkali liquid tank is arranged in the tower body of the acid removal reaction tower, the alkali liquid tank is a zigzag overflow device, dilute alkali liquid firstly enters a cavity formed by the inner column body from the bottom and then enters the alkali liquid tank through the side wall of the inner column body, overflow is generated after the dilute alkali liquid is filled in the alkali liquid tank to form an inner alkali liquid waterfall and an outer alkali liquid waterfall, and acidic substances (mainly hydrogen sulfide gas) in oil gas are positively subjected to waterfall formed by the dilute alkali liquid when flowing upwards, so that the acidic substances are neutralized, the concentration of the acidic gas is reduced, and the acidic gas is prevented from flowing upwards to enter a vacuum pump and subsequent equipment to be corroded.
2. The application designs a baffle plate at the upper part of an alkali liquid tank in the acid removal reaction tower, when the liquid and the gas are mixed together for flowing due to different specific gravities of the gas and the liquid, if the gas is blocked, the gas is baffled and the liquid is moved away due to inertia, the forward speed is continued, the forward liquid is attached to the blocking wall surface and is downwards collected to the bottom of the acid removal reaction tower due to the action of gravity, and is discharged through a discharge hole; thus, the baffle plate can separate the oil, gas and water, so that the oil, gas and water entering the vacuum pump are reduced.
In a word, the application overcomes the defects of the prior art, has simple process flow and good acid removal effect, saves maintenance time and cost, and ensures continuous and stable operation of production.
Drawings
The application will be further described with reference to the drawings and examples.
FIG. 1 is a process flow diagram of the present application;
FIG. 2 is a schematic structural view of the acid removal reaction tower of the present application;
FIG. 3 is a schematic cross-sectional view of the lye tank and lye piping in the deacidification reaction tower of the present application;
in the figure, 1, a decompression tower; 2. a vacuum pump; 3. a vacuum tank; 4. an acid removal reaction tower; 41. a tower body; 42. an air outlet; 43. a discharge port; 44. a base tank; 441. an outer cylinder; 442. an inner cylinder; 443. overflow teeth; 45. an alkali liquor pipeline; 46. a baffle plate; 47. an oil and gas pipeline; 5. a liquid seal groove; 6. a wash oil circulation pump; 7. a liquid collecting tank.
Detailed Description
The application is further illustrated by the following examples.
The experimental parameters not indicated in the embodiments are all preferred parameters in the foregoing technical solutions, and are not described in detail in specific embodiments.
Example 1 brief description of the process flow of the application
In the deep processing process of coal tar, soft asphalt pumped 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 carry out product extraction, oil gas at the top of the decompression tower 1 enters a vacuum tank 3 under the action of a vacuum pump 2, oil gas in the vacuum tank 3 is washed by wash 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, gas in the liquid seal tank 5 is conveyed to a tail gas system (not marked) for treatment and then is discharged, and the liquid in the liquid seal tank 5 is conveyed to the vacuum pump 2 for circulation to the liquid seal tank 5 by a wash oil circulation pump 6 or is conveyed to a three-mixing tank (not marked) for treatment; the acid-removing reaction tower 4 is introduced with external dilute alkali solution for acid neutralization, wherein the treated gas is conveyed to the vacuum pump 2 and then conveyed to the liquid seal tank 5 for circulation, the treated liquid is conveyed to the liquid collecting tank 7, the gas in the liquid collecting tank 7 is conveyed to the tail gas system for treatment, and the liquid is conveyed to the dilute alkali solution supply system (not shown) for circulation.
The acid removal reaction tower 4 comprises a hollow cylindrical tower body 41, wherein an air outlet 42 is formed in the top of the tower body 41, an oil gas inlet (not shown) and an alkali liquor inlet (not shown) are respectively formed in two sides of the bottom, and a discharge hole 43 is formed in the middle of the bottom; the middle part in the tower body is provided with an alkali liquor tank 44, the alkali liquor tank 44 is formed by two hollow cylinders with end-capped bottoms, 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 center lines of the outer cylinder 441 and the inner cylinder 442 are overlapped, the outer cylinder 441 and the inner cylinder 442 are equal in height, and a plurality of overflow teeth 443 are arranged at the top; the alkali liquor inlet is communicated with an alkali liquor pipeline 45, the alkali liquor pipeline 45 passes through the side wall of the tower body 41, is inserted into the middle of the inner column 442 from the bottom of the hollow inner column 442 to be separated to two sides, is respectively communicated with the side wall of the inner column 442, and conveys alkali liquor into the alkali liquor tank 44 through openings on the side walls on two sides of the inner column 442. The upper part of the alkali liquid tank 44 is provided with a plurality of layers of baffle plates 46, and the baffle plates 46 of 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 cross through the central line of the tower body 41. The oil gas inlet is connected with an oil gas pipeline 47, the oil gas pipeline 47 stretches into the bottom of the alkali liquor tank 44, the bottom corresponding to the end closure of the alkali liquor tank 44 is arranged in a ring shape, and a plurality of air outlets (not shown) are formed in the upper portion of the ring-shaped pipeline.
Example 2
a. The soft asphalt in the decompression tower 1 is decompressed: the soft asphalt pumped out by the pump (P84004A/B) of the atmospheric distillation tower is sent to a decompression heating furnace to be heated to the bottom temperature of 370 ℃, the control pressure is-18 Kpa, the temperature in the tower is 265 ℃ under the action of a vacuum system, the control pressure is-20 Kpa, heavy oil B is extracted from the tower, the heavy oil B is pumped out by the pump (P84102A/B) of the heavy oil B, and part of the heavy oil B flows back and the rest of the heavy oil is extracted to a CB oil heavy oil tank. The upper temperature of the tower is 85 ℃, the control pressure is-35 Kpa, heavy oil A is extracted from the tower, the heavy oil A is extracted through a heavy oil A extraction pump (P84103A/B) and passes through a heavy oil A waste pot and a heavy oil A2# cooler, a part of the heavy oil A waste pot and the heavy oil A2# cooler are refluxed, and a part of the heavy oil A waste pot and the heavy oil A2# cooler are extracted and are converged with heavy oil B to a CB oil heavy oil tank. And (3) after the oil gas at the top of the tower enters a vacuum system. After entering a primary asphalt detention tank (V84101), part of the asphalt at the bottom is recirculated to the detention tank by a primary asphalt circulating pump (P84104A/B), part of the asphalt is extracted to a secondary asphalt detention tank (V84102), part of the asphalt is recirculated to the detention tank by a secondary asphalt circulating pump (P84108A/B), part of the asphalt is mixed with soft asphalt, and then enters a decompression furnace, and the other part of the asphalt is extracted to a finished product by an asphalt extracting pump (P84101A/B) through an asphalt waste pot; the reaction is carried out for 12 hours, wherein oil gas at the top (the content of hydrogen sulfide is 153000 mu mol/mol through detection) is conveyed into a vacuum tank 3 through a vacuum pump 2 for washing;
b. conveying the wash 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 flow rate of the wash oil is controlled at 650kg/h, and substances such as benzene, naphthalene and the like in the oil gas are absorbed; the liquid which falls into the bottom of the vacuum tank 3 after spraying is conveyed into the liquid seal tank 5 through a pump for recycling, and the oil gas enters the acid removal reaction tower 4 for acid removal or directly enters the liquid seal tank 5 through the vacuum pump 2 for recycling;
c. neutralizing and deacidifying oil gas in an acid removal reaction tower 4 by 21% sodium hydroxide, controlling the reaction temperature in the acid removal reaction tower 4 to be 45 ℃, controlling the pressure to be-40 KPa, and controlling the oil gas flow to be 720m 3 Controlling the flow rate of 21% sodium hydroxide at 1200kg/h; the oil gas after acid removal enters a vacuum pump 2, and enters a liquid seal tank 5 for circulation through the vacuum pump 2; detecting the content of 30 mu mol/mol of hydrogen sulfide in the oil gas subjected to acid removal, and introducing the liquid subjected to acid removal into a liquid collecting tank 7 for temporary storage;
d. the gas in the liquid seal tank 5 enters the tail gas system for treatment, and the liquid enters the vacuum pump 2 for circulation through the wash oil circulating pump 6.
Example 3
a. The soft asphalt in the decompression tower 1 is decompressed: the soft asphalt pumped out by the pump (P84004A/B) is sent to a decompression heating furnace to be heated to the bottom temperature of 390 ℃, the control pressure is minus 19Kpa, the temperature in the tower is 252 ℃ under the action of a vacuum system, the control pressure is minus 22Kpa, heavy oil B is extracted from the tower, the heavy oil B is pumped out by the pump (P84102A/B) for pumping out the heavy oil B, and part of the heavy oil B flows back and the other part of the heavy oil B is extracted to a CB oil heavy oil tank. The upper temperature of the tower was 80 ℃, the control pressure was-32 Kpa, and heavy oil a was extracted therefrom, and was extracted through a heavy oil a extraction pump (P84103A/B) and passed through a heavy oil a waste pan, a heavy oil a2# cooler, with a part of the reflux, and a part of the extraction was merged with heavy oil B and then to a CB oil heavy oil tank. And (3) after the oil gas at the top of the tower enters a vacuum system. After entering a primary asphalt detention tank (V84101), part of the asphalt at the bottom is recirculated to the detention tank by a primary asphalt circulating pump (P84104A/B), part of the asphalt is extracted to a secondary asphalt detention tank (V84102), part of the asphalt is recirculated to the detention tank by a secondary asphalt circulating pump (P84108A/B), part of the asphalt is mixed with soft asphalt, and then enters a decompression furnace, and the other part of the asphalt is extracted to a finished product by an asphalt extracting pump (P84101A/B) through an asphalt waste pot; the reaction is carried out for 10 hours, wherein oil gas at the top (the content of hydrogen sulfide is 153400 mu mol/mol through detection) is conveyed into a vacuum tank 3 through a vacuum pump 2 for washing;
b. conveying the wash 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 flow rate of the wash oil is controlled at 700kg/h, and substances such as benzene, naphthalene and the like in the oil gas are absorbed; the liquid which falls into the bottom of the vacuum tank 3 after spraying is conveyed into the liquid seal tank 5 through a pump for recycling, and the oil gas enters the acid removal reaction tower 4 for acid removal or directly enters the liquid seal tank 5 through the vacuum pump 2 for recycling;
c. neutralizing oil gas in an acid removal reaction tower 4 by 19% potassium hydroxide to remove acid, wherein the reaction temperature in the acid removal reaction tower 4 is 42 ℃, the pressure is controlled at-35 KPa, and the oil gas flow is controlled at 750m 3 Controlling the flow rate of 19% potassium hydroxide at 1000kg/h; the oil gas after acid removal enters a vacuum pump 2, and enters a liquid seal tank 5 for circulation through the vacuum pump 2; detecting the content of hydrogen sulfide in the oil gas subjected to acid removal by 45 mu mol/mol, and introducing the liquid subjected to acid removal into a liquid collecting tank 7 for temporary storage;
d. the gas in the liquid seal tank 5 enters the tail gas system for treatment, and the liquid enters the vacuum pump 2 for circulation through the wash oil circulating pump 6.
Example 4
a. The soft asphalt in the decompression tower 1 is decompressed: the soft asphalt pumped out by the pump (P84004A/B) of the atmospheric distillation tower is sent to a decompression heating furnace to be heated to the bottom temperature of 390 ℃, the control pressure is minus 19Kpa, the temperature in the tower is 265 ℃ under the action of a vacuum system, the control pressure is minus 20Kpa, the heavy oil B is extracted from the tower, the heavy oil B is pumped out by the pump (P84102A/B) of the heavy oil B, and part of the heavy oil B flows back and the rest is extracted to a CB oil heavy oil tank. The upper temperature of the tower is 80 ℃, the control pressure is-35 Kpa, heavy oil A is extracted from the tower, the heavy oil A is extracted through a heavy oil A extraction pump (P84103A/B) and passes through a heavy oil A waste pot and a heavy oil A2# cooler, a part of the heavy oil A waste pot and the heavy oil A2# cooler are refluxed, and a part of the heavy oil A waste pot and the heavy oil A2# cooler are extracted and are converged with heavy oil B to a CB oil heavy oil tank. And (3) after the oil gas at the top of the tower enters a vacuum system. After entering a primary asphalt detention tank (V84101), part of the asphalt at the bottom is recirculated to the detention tank by a primary asphalt circulating pump (P84104A/B), part of the asphalt is extracted to a secondary asphalt detention tank (V84102), part of the asphalt is recirculated to the detention tank by a secondary asphalt circulating pump (P84108A/B), part of the asphalt is mixed with soft asphalt, and then enters a decompression furnace, and the other part of the asphalt is extracted to a finished product by an asphalt extracting pump (P84101A/B) through an asphalt waste pot; the reaction is carried out for 12 hours, wherein oil gas at the top (the content of hydrogen sulfide is 153100 mu mol/mol through detection) is conveyed into a vacuum tank 3 through a vacuum pump 2 for washing;
b. conveying the wash 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 flow rate of the wash oil is controlled at 650kg/h, and substances such as benzene, naphthalene and the like in the oil gas are absorbed; the liquid which falls into the bottom of the vacuum tank 3 after spraying is conveyed into the liquid seal tank 5 through a pump for recycling, and the oil gas enters the acid removal reaction tower 4 for acid removal or directly enters the liquid seal tank 5 through the vacuum pump 2 for recycling;
c. neutralizing and deacidifying oil gas in an deacidification reaction tower 4 by using 20% barium hydroxide, controlling the reaction temperature in the deacidification reaction tower 4 to be 47 ℃, controlling the pressure to be-35 KPa, and controlling the oil gas flow to be 720m 3 Controlling the flow rate of 20% barium hydroxide at 1500kg/h; the oil gas after acid removal enters a vacuum pump 2, and enters a liquid seal tank 5 for circulation through the vacuum pump 2; detecting the content of 38 mu mol/mol of hydrogen sulfide in the oil gas subjected to acid removal, and introducing the liquid subjected to acid removal into a liquid collecting tank 7 for temporary storage;
d. the gas in the liquid seal tank 5 enters the tail gas system for treatment, and the liquid enters the vacuum pump 2 for circulation through the wash oil circulating pump 6.
Example 5
The 21% sodium hydroxide in example 2 was replaced by 21% calcium hydroxide, the other process conditions were unchanged, and the hydrogen sulfide content in the treated oil gas was changed from 153000. Mu. Mol/mol to 35. Mu. Mol/mol.
Summarizing:
by comparison of the processes of examples 2-5, the following can be concluded: the treatment effect of the embodiment 2 is best, the content of hydrogen sulfide is greatly reduced after treatment, before the application is not implemented, the disc, the end cover, the impeller, the pump body, the pump shaft and the sealing cavity of the vacuum pump are required to be replaced every year, and the maintenance cost generated by other corroded parts is 71.72 ten thousand yuan. Therefore, the application has good acid removal effect, saves maintenance time and cost and indirectly increases production benefit.
It is to be understood that these examples are illustrative of the present application and are not intended to limit the scope of the present application. Furthermore, it should be understood that various changes and modifications can be made by one skilled in the art after reading the teachings of the present application, and such equivalents are intended to fall within the scope of the application as defined in the appended claims.
Claims (10)
1. The coal tar deep processing method is characterized by comprising the following steps of:
a. carrying out decompression treatment on soft asphalt in a decompression tower, wherein oil gas at the top is conveyed into a vacuum tank through a vacuum pump and is washed through washing oil, and the residual materials are heavy oil B, heavy oil A and asphalt respectively, and are extracted in stages to enter other processing procedures;
b. the washing oil is conveyed into a vacuum tank for spraying, the washing oil which falls into the bottom of the vacuum tank after spraying is conveyed into a liquid seal tank through a pump for recycling, and the oil gas enters an acid removal reaction tower for acid removal or directly enters the liquid seal tank for recycling through a vacuum pump;
c. neutralizing and acid removing the oil gas in an acid removing reaction tower through dilute alkali, and enabling the oil gas after acid removal to enter a vacuum pump and enter a liquid seal tank for circulation through the vacuum pump; introducing the liquid after acid removal into a liquid collecting tank for temporary storage;
the acid removal reaction tower comprises a hollow cylindrical tower body, wherein the top of the tower body is provided with an air outlet, the two sides of the bottom are respectively provided with an oil gas inlet and an alkali liquor inlet, and the middle of the bottom is provided with a discharge hole; the middle part in the tower body is provided with an alkali liquid tank, the alkali liquid tank is formed by two hollow cylinders with end-capped bottoms, wherein the cylinder positioned at the outer side is an outer cylinder, the cylinder positioned at the inner side is an inner cylinder, the center lines of the outer cylinder and the inner cylinder are overlapped, the outer cylinder and the inner cylinder are equal in height, the top parts of the outer cylinder and the inner cylinder are provided with a plurality of overflow teeth, and the tooth shapes of the inner overflow teeth and the overflow teeth are distributed in a staggered manner; the alkali liquor inlet is communicated with an alkali liquor pipeline, the alkali liquor pipeline passes 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, is bifurcated and is respectively connected to the side wall of the inner column body, and the side wall of the inner column body at the joint of one side or two sides is provided with an opening; the upper part of the alkali liquid 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 cross through the central line of the tower body;
d. the gas in the liquid seal tank enters into the tail gas system for treatment, and the liquid enters into the vacuum pump for circulation through the wash oil circulating pump, or enters into the unwashed three-mixed oil tank to serve as industrial naphthalene distillation raw material for temporary storage, so that the subsequent process is continued for treatment.
2. The method for further processing coal tar as recited in claim 1, wherein: in the step a, the temperature of the bottom of the vacuum tower is controlled to be 370-390 ℃, the temperature in the vacuum tower is 252-265 ℃, and the temperature of the top of the vacuum tower is 80-85 ℃; the pressure at the bottom of the tower is-18 to-19 KPa, the pressure in the tower is-20 to-22 KPa, the pressure at the top of the tower is-32 to-35 KPa, and the reaction time is controlled to be 10 to 12 hours.
3. The method for further processing coal tar as recited in claim 1, wherein: the reaction temperature in the vacuum tank in the step b is 50-55 ℃, the pressure is controlled to be minus 35-minus 40KPa, and the wash oil flow is controlled to be 600 kg/h-700 kg/h.
4. As claimed inThe coal tar deep processing method is characterized by comprising the following steps: the reaction temperature in the deacidification reaction tower in the step c is 42-47 ℃, the pressure is controlled to be minus 35 to minus 40KPa, and the oil gas flow is controlled to be 720-750 m 3 And/h, controlling the flow rate of the dilute alkali at 1000 kg/h-1500 kg/h.
5. The method for further processing coal tar as recited in claim 1, wherein: the dilute alkali in the step c is sodium hydroxide with the concentration of 21%, potassium hydroxide with the concentration of 19%, barium hydroxide with the concentration of 20% or calcium hydroxide with the concentration of 21%.
6. The method for further processing coal tar as recited in claim 1, wherein: and c, the upper part of the liquid collecting tank is provided with a gas outlet communicated with the tail gas system, and the lower part of the liquid collecting tank is provided with a discharge outlet communicated with the dilute alkali supply system, so that the dilute alkali is recycled.
7. The method for further processing coal tar as recited in claim 1, wherein: the oil gas inlet is connected with an oil gas pipeline, the gas outlet of the oil gas pipeline is arranged close to the wall of the tower body, or the oil gas pipeline extends into the bottom of the alkali liquor tank, the bottom corresponding to the end closure of the alkali liquor tank is arranged in a ring shape, and a plurality of gas outlets are formed in the upper part of the ring-shaped pipeline.
8. The method for further processing coal tar as recited in claim 1, wherein: the distance between the outer side of the outer column body and the inner wall of the column 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 coal tar as recited in claim 1, wherein: the baffle plates are inclined downwards by 15-18 degrees, and the interval between the baffle plates on the same side is 15-20 cm.
10. The method for further processing coal tar as recited in claim 1, wherein: the length of the crossing part between the two layers of the baffle plates is one fifth to one fourth of the maximum length of the baffle plates.
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| CN114292659A (en) | 2022-04-08 |
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