阅读说明：本技术 一种焦化乳化液制备装置及工艺 (Coking emulsion preparation device and process ) 是由 董少英 赵佳顺 孙晓然 孔德文 张平存 谷毅 何小锴 赵峥 王小琼 于 2021-01-26 设计创作，主要内容包括：一种焦化乳化液制备装置及工艺,属于焦化乳化液制备设备及工艺技术领域,用于制备焦化乳液。其技术方案为：本发明通过焦油输送泵、循环氨水泵将一定比例的焦油、氨水引入初冷器冷凝液槽,复配乳化剂加入初冷器冷凝液槽后由搅拌器搅拌；然后通过初冷器冷凝液喷洒泵将乳化液送入初冷器进行喷淋洗涤；喷淋后乳化液进入初冷器冷凝液送出槽,向初冷器冷凝液送出槽连续均匀加入破乳剂后进行搅拌,搅拌后的乳化液进入机械刮渣槽。本发明可自行控制焦油与氨水的比例,所制备的乳化液可提高初冷器的洗涤效果,清除附着在初冷器列管壁上的焦油、萘等物质,降低初冷器运行阻力、提升初冷器换热效果、改善煤气质量,保证了焦油、氨水分离效果。(A coking emulsion preparation device and a coking emulsion preparation process belong to the technical field of coking emulsion preparation equipment and coking emulsion preparation processes and are used for preparing coking emulsion. The technical scheme is as follows: according to the invention, a tar delivery pump and a circulating ammonia water pump are used for introducing tar and ammonia water in a certain proportion into a primary cooler condensate tank, and a compound emulsifier is added into the primary cooler condensate tank and then stirred by a stirrer; then the emulsion is sent into a primary cooler through a primary cooler condensate spraying pump for spraying and washing; and (3) the sprayed emulsion enters a primary cooler condensate liquid delivery tank, a demulsifier is continuously and uniformly added into the primary cooler condensate liquid delivery tank and then stirred, and the stirred emulsion enters a mechanical slag scraping tank. The invention can automatically control the ratio of tar to ammonia water, the prepared emulsion can improve the washing effect of the primary cooler, remove tar, naphthalene and other substances attached to the tube wall of the primary cooler, reduce the running resistance of the primary cooler, improve the heat exchange effect of the primary cooler, improve the gas quality and ensure the separation effect of the tar and the ammonia water.)

1. A coking emulsion preparation device is characterized in that: it comprises a tar and ammonia water separation tank (1), a tar delivery pump (2), a circulating ammonia water pump (3), a primary cooler condensate tank (4), a primary cooler condensate spraying pump (7), a primary cooler (10), a primary cooler condensate delivery tank (11), a condensate delivery pump (14) and a mechanical slag scraping tank (15), wherein a tar output pipeline of the tar and ammonia water separation tank (1) is connected with a tar input pipeline of the primary cooler condensate tank (4) through the tar delivery pump (2), an ammonia water output pipeline of the tar and ammonia water separation tank (1) is connected with an ammonia water input pipeline of the primary cooler condensate tank (4) through the circulating ammonia water pump (3), an output pipeline of the primary cooler condensate tank (4) is connected with an input pipeline of the primary cooler (10) through the primary cooler condensate spraying pump (7), an output pipeline of the primary cooler (10) is connected with the primary cooler condensate delivery tank (11), an output pipeline of the primary cooler condensate delivery tank (11) is connected with a mechanical slag scraping tank (15) through a condensate delivery pump (14), a compound emulsifier adding port (6) is arranged in the primary cooler condensate tank (4), and a demulsifier adding port (13) is arranged in the primary cooler condensate delivery tank (11).

2. The apparatus of claim 1, wherein: a primary cooler condensate tank stirrer (5) is arranged in the primary cooler condensate tank (4), and a primary cooler condensate conveying tank stirrer (12) is arranged in the primary cooler condensate conveying tank (11).

3. The apparatus of claim 1, wherein: the primary cooler (10) is respectively provided with a primary cooler upper-section spray pipe (8) and a primary cooler lower-section spray pipe (9), and the output end of the primary cooler condensate spray pump (7) is respectively connected with the primary cooler upper-section spray pipe (8) and the primary cooler lower-section spray pipe (9).

4. A coking emulsion preparation process using the coking emulsion preparation device is characterized in that: the method comprises the following steps:

a. tar delivery pump (2), circulation ammonia water pump (3) are sent into primary cooler condensate tank (4) with tar, aqueous ammonia respectively from tar aqueous ammonia separating tank (1) in, wherein the proportion of tar and aqueous ammonia is 15: 100-35:100, wherein the conveying mode is continuous conveying, and a primary cooler condensate tank stirrer (5) is used for stirring tar and ammonia water in a primary cooler condensate tank (4);

b. continuously adding the compound emulsifier into the primary cooler condensate tank (4) through a compound emulsifier adding port (6), wherein the proportion of the compound emulsifier to the mixture of tar and ammonia water is 1: 100-3:100, wherein the compound emulsifier consists of sodium dodecyl benzene sulfonate and octadecane, and the mass ratio of the sodium dodecyl benzene sulfonate to the octadecane is 30: 100-45: 100) adding the compound emulsifier into the primary cooler condensate liquid, and stirring and emulsifying in the primary cooler condensate liquid tank (4);

c. the emulsified primary cooler condensate enters a primary cooler (10) through a primary cooler condensate spraying pump (7), a primary cooler upper section spraying pipe (8) and a primary cooler lower section spraying pipe (9) and then is sprayed and washed on the primary cooler (10);

d. the condensate after the washing gets into primary cooler condensate and sends out groove (11), sends out groove (11) to primary cooler condensate through demulsifier interpolation mouth (13) and evenly adds demulsifier polyoxyethylene polyoxypropylene polyether in succession, and demulsifier polyoxyethylene polyoxypropylene polyether is 0.2 with the condensate proportion of sending out: 100-0.6:1000, the primary cooler condensate is sent out of the tank stirrer (12), and the condensate added with the demulsifier is stirred in the primary cooler condensate is sent out of the tank (11);

e. the condensate of the primary cooler is sent out of the tank (11) by a condensate sending pump (14) and the demulsified condensate is sent into a mechanized slag scraping tank (15).

Technical Field

The invention relates to a coking emulsion preparation device and a coking emulsion preparation process, and belongs to the technical field of coking emulsion preparation equipment and coking emulsion preparation processes.

Background

The separation of tar and ammonia water is one of the key links in the production process of tar and is also a difficult point in production. How to improve the separation of tar and ammonia water and improve the quality of emulsion is a key process factor influencing coking recovery. The used emulsion of traditional primary cooler spray washing adopts in tar aqueous ammonia separating tank, because coke oven operating mode complexity, tar and aqueous ammonia interface fluctuation of tar aqueous ammonia separating tank cause the difficult control of emulsion tar aqueous ammonia proportion of adopting, tar content is low then can not reach impurity such as primary cooler washing tubulation adhesion naphthalene, and tar content too high can cause tar adhesion on primary cooler tubulation wall, cause the primary cooler resistance too high, influence primary cooler cooling effect, influence follow-up coal gas quality. And because the tar and the ammonia water belong to lipophilic and hydrophilic substances respectively, the single tar ammonia water emulsion is heterogeneous, and the spraying and washing effect cannot be achieved. Therefore, the traditional coking emulsion preparation technology cannot meet the production process requirements, and the traditional emulsion preparation method needs to be improved to improve the controllability of the coking recovery process.

Disclosure of Invention

The technical problem to be solved by the invention is to provide a coking emulsion preparation device and a coking emulsion preparation process, which can control the ratio of tar to ammonia water, and the prepared emulsion can improve the washing effect of a primary cooler, remove substances such as tar, naphthalene and the like attached to the tube wall of the primary cooler, reduce the running resistance of the primary cooler, improve the heat exchange effect of the primary cooler and improve the quality of coal gas.

The technical scheme for solving the technical problems is as follows:

a coking emulsion preparation device comprises a tar-ammonia water separation tank, a tar delivery pump, a circulating ammonia water pump, a primary cooler condensate tank, a primary cooler condensate spraying pump, a primary cooler condensate delivery tank, a condensate delivery pump and a mechanized scum scraping tank, wherein a tar output pipeline of the tar-ammonia water separation tank is connected with a tar input pipeline of the primary cooler condensate tank through the tar delivery pump, an ammonia output pipeline of the tar-ammonia water separation tank is connected with an ammonia input pipeline of the primary cooler condensate tank through the circulating ammonia water pump, an output pipeline of the primary cooler condensate tank is connected with an input pipeline of a primary cooler through the primary cooler condensate spraying pump, an output pipeline of the primary cooler is connected with the primary cooler condensate delivery tank, an output pipeline of the primary cooler condensate delivery tank is connected with the mechanized scum scraping tank through the condensate delivery pump, a compound emulsifier adding port is arranged in the primary cooler condensate tank, the condensate of the primary cooler is sent out of the tank and is provided with a demulsifier adding port.

Above-mentioned coking emulsion preparation facilities, there is primary cooler condensate tank agitator in the primary cooler condensate tank, has primary cooler condensate to send out the groove agitator in the primary cooler condensate sends out the inslot.

Above-mentioned coking emulsion preparation facilities, there are primary cooler upper segment spray pipe, primary cooler hypomere spray pipe respectively on the primary cooler, primary cooler condensate spray pump output end is connected with primary cooler upper segment spray pipe, primary cooler hypomere spray pipe respectively.

A coking emulsion preparation process using the coking emulsion preparation device comprises the following steps:

a. tar delivery pump, circulation ammonia water pump send into tar, aqueous ammonia into the primary cooler condensate tank from tar aqueous ammonia separating tank respectively, and wherein the ratio of tar and aqueous ammonia is 15: 100-35:100, wherein the conveying mode is continuous conveying, and a primary cooler condensate tank stirrer is used for stirring tar and ammonia water in the primary cooler condensate tank;

b. continuously adding the compound emulsifier into the condensate tank of the primary cooler through a compound emulsifier adding port, wherein the ratio of the compound emulsifier to the mixture of tar and ammonia water is 1: 100-3:100, wherein the compound emulsifier consists of sodium dodecyl benzene sulfonate and octadecane, and the mass ratio of the sodium dodecyl benzene sulfonate to the octadecane is 30: 100-45:100, stirring and emulsifying the primary cooler condensate added with the compound emulsifier in a primary cooler condensate tank;

c. after passing through a primary cooler condensate spray pump, a primary cooler upper section spray pipe and a primary cooler lower section spray pipe, the emulsified primary cooler condensate enters a primary cooler and then is sprayed and washed;

d. the condensate after washing gets into primary cooler condensate and sends out the groove, sends out the groove to primary cooler condensate through the demulsifier interpolation mouth and evenly adds demulsifier polyoxyethylene polyoxypropylene polyether in succession, and demulsifier polyoxyethylene polyoxypropylene polyether and the condensate proportion of sending out are 0.2: 100-0.6:100, feeding the primary cooler condensate out of the tank stirrer, and stirring the condensate added with the demulsifier in the primary cooler condensate feeding out tank;

e. the condensate liquid of the primary cooler is conveyed out of the tank by a condensate liquid conveying pump, and the condensate liquid after demulsification is conveyed into a mechanized slag scraping tank.

The invention has the beneficial effects that:

according to the invention, by using the compound emulsifier and automatically controlling the ratio of tar to ammonia water, the prepared emulsion can improve the washing effect of the primary cooler, remove substances such as tar and naphthalene attached to the wall of the tubular shell of the primary cooler, reduce the running resistance of the primary cooler, improve the heat exchange effect of the primary cooler and improve the quality of coal gas, and the spray liquid after emulsion breaking is sent to a mechanized slag scraping tank, so that the separation effect of tar and ammonia water is ensured.

The invention is the initiative of tar ammonia water separation equipment and process, provides new good-effect tar ammonia water emulsification equipment and process for separating coking ammonia water, solves the technical problems of poor cleaning effect and unstable operation of a primary cooler caused by oil-water insolubility between tar and ammonia water, provides technical support for the separation of tar and ammonia water, and is worthy of popularization and application.

Drawings

FIG. 1 is a schematic diagram of the structure of a coker emulsion production unit of the present invention.

The figures are labeled as follows: the system comprises a tar and ammonia water separation tank 1, a tar delivery pump 2, a circulating ammonia water pump 3, a primary cooler condensate tank 4, a primary cooler condensate tank stirrer 5, a compound emulsifier adding port 6, a primary cooler condensate spraying pump 7, a primary cooler upper section spraying pipe 8, a primary cooler lower section spraying pipe 9, a primary cooler 10, a primary cooler condensate sending tank 11, a primary cooler condensate sending tank stirrer 12, a demulsifier adding port 13, a condensate sending pump 14 and a mechanical slag scraping tank 15.

Detailed Description

The tar and ammonia water separation equipment comprises a tar and ammonia water separation tank 1, a tar delivery pump 2, a circulating ammonia water pump 3, a primary cooler condensate tank 4, a primary cooler condensate spraying pump 7, a primary cooler 10, a primary cooler condensate discharge tank 11, a condensate discharge pump 14 and a mechanized slag scraping tank 15.

The figure shows that the tar output pipeline of the tar-ammonia water separation tank 1 is connected with the tar input pipeline of the primary cooler condensate tank 4 through a tar delivery pump 2, the ammonia water output pipeline of the tar-ammonia water separation tank 1 is connected with the ammonia water input pipeline of the primary cooler condensate tank 4 through a circulating ammonia water pump 3, and tar and ammonia water are respectively delivered to the primary cooler condensate tank 4. The ratio of tar to ammonia was 15: 100-35:100, and the conveying mode is continuous conveying.

The figure shows that a compound emulsifier adding port 6 and a compound emulsifier stirrer 5 are respectively arranged in a primary cooler condensate tank 4, the compound emulsifier is added into the primary cooler condensate tank 4 through the compound emulsifier adding port 6, and the tar, ammonia water and the compound emulsifier in the primary cooler condensate tank 4 are stirred by the primary cooler condensate tank stirrer 5. The proportion of the compound emulsifier to the mixture of tar and ammonia water is 1: 100-3:100, wherein the compound emulsifier consists of sodium dodecyl benzene sulfonate and octadecane, and the mass ratio of the sodium dodecyl benzene sulfonate to the octadecane is 30: 100-45:100.

The figure shows that the output pipeline of the primary cooler condensate tank 4 is connected with the primary cooler upper section spray pipe 8 and the primary cooler lower section spray pipe 9 of the primary cooler 10 through the primary cooler condensate spray pump 7, and the emulsified condensate is conveyed into the primary cooler 10. The upper spraying pipe 8 of the primary cooler is corresponding to the spraying and washing of the upper section of the primary cooler 10, and the lower spraying pipe 9 of the primary cooler is corresponding to the spraying and washing of the lower section of the primary cooler 10.

The figure shows that the outlet pipe of the primary cooler 10 is connected to a primary cooler condensate feed tank 11, and a primary cooler condensate feed tank stirrer 12 and a demulsifier addition port 13 are provided in the primary cooler condensate feed tank 11. The washed condensate enters a primary cooler condensate discharging tank 11, a demulsifier adding port 13 continuously and uniformly adds a demulsifier to the primary cooler condensate discharging tank 11, wherein the demulsifier is polyoxyethylene polyoxypropylene polyether (molecular structural formula: D (PO) x (EO) y (PO) z H, in the formula, EO-polyoxyethylene, PO-polyoxypropylene, R-fatty alcohol, D-polyethylene polyamine, x, y and z-polymerization degrees, the proportion of the demulsifier polyoxyethylene polyoxypropylene polyether to the discharged condensate is 0.2: 100-0.6:100, and the primary cooler condensate discharging tank stirrer 12 stirs the condensate added with the demulsifier in the primary cooler condensate discharging tank 11.

The outlet line of the primary cooler condensate discharge tank 11 is connected to a mechanical slag scraping tank 15 via a condensate discharge pump 14, and the condensate after demulsification of the primary cooler condensate discharge tank 11 is discharged into the mechanical slag scraping tank 15 by the condensate discharge pump 14.

The preparation process of the coking emulsion is carried out by the following steps:

a. tar delivery pump 2, circulation ammonia water pump 3 send tar, aqueous ammonia into primary cooler condensate tank 4 from tar aqueous ammonia separating tank 1 respectively, and wherein the proportion of tar and aqueous ammonia is 15: 100-35, 100, wherein the conveying mode is continuous conveying, and a primary cooler condensate tank stirrer 5 is used for stirring tar and ammonia water in a primary cooler condensate tank 4;

b. continuously adding the compound emulsifier into the primary cooler condensate tank 4 through a compound emulsifier adding port 6, wherein the proportion of the compound emulsifier to the mixture of tar and ammonia water is 1: 100-3:100, wherein the compound emulsifier consists of sodium dodecyl benzene sulfonate and octadecane, and the mass ratio of the sodium dodecyl benzene sulfonate to the octadecane is 30: 100-45:100, stirring and emulsifying the primary cooler condensate added with the compound emulsifier in a primary cooler condensate tank 4;

c. the emulsified primary cooler condensate enters a primary cooler 10 through a primary cooler condensate spraying pump 7, a primary cooler upper section spraying pipe 8 and a primary cooler lower section spraying pipe 9, and then is sprayed and washed on the primary cooler 10;

d. the condensate after washing gets into primary cooler condensate and sends out groove 11, sends out groove 11 to primary cooler condensate through demulsifier interpolation mouth 13 and evenly adds demulsifier polyoxyethylene polyoxypropylene polyether in succession, and demulsifier polyoxyethylene polyoxypropylene polyether and the condensate proportion of sending out are 0.2: 100-0.6:100, the primary cooler condensate is sent out of the tank stirrer 12, and the condensate added with the demulsifier is stirred in the primary cooler condensate is sent out of the tank 11;

e. the condensate of the primary cooler is sent out of the tank 11 by a condensate sending pump 14, and the condensate after demulsification is sent into a mechanized slag scraping tank 15.

The examples of the invention are as follows:

example 1

Carry tar, carry the aqueous ammonia by circulating ammonia water pump 3 to primary cooler condensate tank 4 by tar delivery pump 2 to primary cooler condensate tank 4, wherein the quality proportion of tar and aqueous ammonia is 15: 100, emulsifier added in the primary cooler condensate tank 4: the mass ratio of the sodium dodecyl benzene sulfonate to the octadecane is 30: 100, the proportion of the compound emulsifier to the mixture of tar and ammonia water is 1: 100, the proportion of demulsifier polyoxyethylene polyoxypropylene polyether added into the primary cooler condensate delivery tank 11 to the delivered condensate is 0.2: 100, and the resistance of the primary cooler is 1650 Pa.

Example 2:

carry tar, carry the aqueous ammonia by circulating ammonia water pump 3 to primary cooler condensate tank 4 by tar delivery pump 2 to primary cooler condensate tank 4, wherein the quality proportion of tar and aqueous ammonia is 20: 100, emulsifier added in the primary cooler condensate tank 4: the mass ratio of the sodium dodecyl benzene sulfonate to the octadecane is 34: 100, the proportion of the compound emulsifier to the mixture of tar and ammonia water is 1.5: 100, the proportion of demulsifier polyoxyethylene polyoxypropylene polyether added into the primary cooler condensate delivery tank 11 to the delivered condensate is 0.3: 100, and the resistance of the primary cooler is 1470 Pa.

Example 3:

carry tar, carry the aqueous ammonia by circulating ammonia water pump 3 to primary cooler condensate tank 4 by tar delivery pump 2 to primary cooler condensate tank 4, wherein the quality proportion of tar and aqueous ammonia is 25: 100, emulsifier added in the primary cooler condensate tank 4: the mass ratio of the sodium dodecyl benzene sulfonate to the octadecane is 38: 100, the proportion of the compound emulsifier to the mixture of tar and ammonia water is 2: 100, the proportion of demulsifier polyoxyethylene polyoxypropylene polyether added into the primary cooler condensate delivery tank 11 to the delivered condensate is 0.4: 100, and the resistance of the primary cooler is 1310 Pa.

Example 4:

carry tar, carry the aqueous ammonia by circulating ammonia water pump 3 to primary cooler condensate tank 4 by tar delivery pump 2 to primary cooler condensate tank 4, wherein the quality proportion of tar and aqueous ammonia is 30: 100, emulsifier added in the primary cooler condensate tank 4: the mass ratio of the sodium dodecyl benzene sulfonate to the octadecane is 42: 100, the proportion of the compound emulsifier to the mixture of tar and ammonia water is 2.5: 100, the proportion of demulsifier polyoxyethylene polyoxypropylene polyether added into the primary cooler condensate delivery tank 11 to the delivered condensate is 0.5: 100, and the resistance of the primary cooler is 1220 Pa.

Example 5:

carry tar, carry the aqueous ammonia by circulating ammonia water pump 3 to primary cooler condensate tank 4 by tar delivery pump 2 to primary cooler condensate tank 4, wherein the quality proportion of tar and aqueous ammonia is 35:100, emulsifier added in the primary cooler condensate tank 4: the mass ratio of the sodium dodecyl benzene sulfonate to the octadecane is 45:100, the proportion of the compound emulsifier to the mixture of tar and ammonia water is 3:100, the proportion of demulsifier polyoxyethylene polyoxypropylene polyether added into the primary cooler condensate delivery tank 11 to the delivered condensate is 0.5: 100 and the resistance of the primary cooler is 1370 Pa.