Tar distillation process for customized production

Abstract

The invention discloses a tar distillation process for customized production. A device for the tar distillation process comprises a raw material tar tank, a dehydrating tower, a heating furnace, a main tower, an extraction valve, an extraction pipeline, a purging valve, a purging pipeline, a dephenolization oil tank, a naphthalene oil tank, an oil washing tank, an anthracene oil tank, a carbon black oil tank, an oil distribution tank and a configuration pipeline. The tar distillation process comprises the following steps: carrying out production adjustment by controlling start-stop combination of side-line naphthalene oil, washing oil and anthracene oil extraction, and customizing oil products by configuring pipelines. In the normal production period of the side line of the tar distillation process, flexible adjustment of extraction and extraction stopping aiming at a single component can be realized, and meanwhile, final products of other extracted components are not influenced; according to the requirements of markets or customers, oil is debugged and distributed in proportion, customized production of various oil products is flexibly achieved, and benefit maximization is achieved on the premise that the quality is met.

Description

TECHNICAL FIELD

[0001] The present application relates to a tar distillation production process, in particular to a customized tar distillation production process. BACKGROUND

[0002] The production and processing technology of coal tar in coal chemical industry is relatively mature and stable. Mainly according to the actual demand of each manufacturer, the details such as distillation column atmospheric pressure or adding or not adding alkali are changed. The process is continuous production and stable, and the product quality is also relatively stable. In recent years, the main improvement direction is the upgrading of equipment, such as using more energy-saving heating furnace burner or more energy-saving frequency conversion fan to achieve cost reduction and efficiency increase. In the product tapping design, the two ways of tapping three mixed oil at the top of the tower and tapping fractions at the side line of the tower are relatively fixed. After tapping to the storage tank, it is ended. The present application mainly improves the design of the process of tapping fractions at the side line.

[0003] In the tar distillation process, light oil is tapped from the top of the dehydration tower, phenol oil is tapped from the top of the main tower, naphthalene oil, washing oil and anthracene oil are tapped from the side line, and medium temperature pitch is tapped from the bottom. The design may be aimed at the user's demand. The washing oil and anthracene oil will not be tapped, and the bottom output will be changed to carbon black oil.

[0004] Disadvantages of the prior art: 1. In the design, each product tapping is only one line to the tank, and the components in the production process are basically fixed in the design, which cannot be flexibly adjusted.

[0005] 2. After the product is tapped to the storage tank, it can only be delivered according to the product category, and there is no corresponding blending design. When the product is raised due to market or other factors, it will be empty back to the system, causing repeated production cost and affecting the normal operation of the system. SUMMARY

[0006] The purpose of the present application is to overcome the shortcomings of the prior art and provide a customized tar distillation production process.

[0007] In order to achieve the above purpose, the technical scheme adopted by the present application is: A customized tar distillation production process, the device of the tar distillation production process comprises: a raw material tar tank, a dehydration tower, a heating furnace and a main tower; the main tower is provided with a side line tapping valve and a tapping pipeline, a dephenol oil tank, a naphthalene oil tank, a washing oil tank, an anthracene oil tank, a carbon black oil tank, an oil distribution tank and a distribution pipeline; the tapping pipeline is additionally provided with a purging valve and a purging pipeline for purging and emptying; the distribution pipeline is additionally provided with a distribution pipeline from the dephenol oil tank to the anthracene oil tank and a distribution pipeline from the anthracene oil tank to the carbon black oil tank; The tar distillation process is: production adjustment is carried out by independently controlling the opening and stopping combination of side line naphthalene oil, washing oil and anthracene oil extraction, and customized production of oil products is carried out by configuring pipelines; The method for controlling the opening and stopping of side line naphthalene oil, washing oil and anthracene oil extraction is: when stopping extraction, closing the extraction valve and opening the purge valve to purge the pipeline, and after purging is completed, closing the purge valve; when the next production adjustment is carried out, first opening the purge valve, closing the purge valve after purging is completed, and then opening the extraction valve for extraction.

[0008] Further, the opening and stopping combination of side line naphthalene oil, washing oil and anthracene oil extraction for production adjustment includes: adjusting production of carbon black oil, stopping washing oil side line extraction and producing low softening point pitch; The process for adjusting production of carbon black oil is: first stopping washing oil extraction and then stopping anthracene oil extraction, simultaneously reducing the main tower bottom temperature of the tar, sampling and analyzing naphthalene oil and bottom carbon black oil, continuously adjusting the tower bottom temperature and side line naphthalene oil and bottom carbon black oil extraction according to the analysis results until the carbon black oil quality meets the standard, the tower bottom temperature is controlled and adjusted to 265℃, the naphthalene oil extraction is increased by 5%, and the remaining proportion is balanced by the carbon black oil extraction from the tower bottom; The process for stopping washing oil side line extraction is: stopping washing oil extraction from the side line, simultaneously reducing the main tower bottom temperature of the tar, sampling and analyzing naphthalene oil, anthracene oil and medium temperature pitch, continuously adjusting the tower bottom temperature and side line extraction according to the analysis results until the naphthalene oil, anthracene oil and medium temperature pitch quality meets the standard, the tower bottom temperature is adjusted to 275℃, the anthracene oil extraction proportion is increased by 1%, and the naphthalene oil and medium temperature pitch do not need to be adjusted; The process for producing low softening point pitch is: stopping anthracene oil extraction from the side line, simultaneously reducing the main tower bottom temperature of the tar, sampling and analyzing naphthalene oil, washing oil and medium temperature pitch, continuously adjusting the tower bottom temperature and side line extraction according to the analysis results until the product quality meets the standard, the tower bottom temperature is adjusted to 270℃, the medium temperature pitch extraction proportion is increased by 4%, and the naphthalene oil and washing oil do not need to be adjusted.

[0009] Further, the customized production of oil products includes customized production of mud gun oil, anthracene oil and carbon black oil; The process for customized production of mud gun oil is: carbon black oil and washing oil are delivered to the oil blending tank in a ratio of 4.39:1 through a pump and pipelines, carbon black oil is delivered first, washing oil is delivered after purging the pipeline, the oil blending tank agitator is started after purging the pipeline, the tank temperature is controlled and increased to 90-100℃, the agitator is stopped after blending for 12 hours, and carbon black oil or washing oil is added separately according to the sampling and analysis results until the customized softening point index is reached; The process for customized production of anthracene oil is: after the dephenol oil tank position reaches 60%, the theoretical proportion of dephenol oil is delivered to the anthracene oil tank through a pump and the configuration pipeline from the dephenol oil tank to the anthracene oil tank, the addition proportion of dephenol oil is adjusted according to the analysis results of the anthracene oil, and the customized requirements are met until the customized requirements are met. The process of customizing the production of carbon black oil is that when the softening point of the carbon black oil needs to be reduced according to the customization requirements, anthracene oil is transported to the carbon black oil tank through a pump and a configuration pipeline of the anthracene oil tank to the carbon black oil tank, and the addition proportion of the anthracene oil is adjusted according to the test analysis results of the carbon black oil until the customization requirements are met.

[0010] The beneficial effects of the present application are that the present application can realize flexible adjustment of extraction and stop of extraction of single components during normal production in the side line of the tar distillation process, and meanwhile, the final products of the remaining extracted components are not affected; according to the market or customer demand, the oil is adjusted in proportion, and the customized production of various oil products is realized flexibly, so that the maximization of benefits is realized under the premise of meeting the quality. BRIEF DESCRIPTION OF DRAWINGS

[0011] Figure 1 is a schematic diagram of the customized extraction structure of the tar distillation production process side line of the embodiment of the present application; The label in the figure is: 1-naphthalene oil extraction valve, 2-washing oil extraction valve, 3-anthracene oil extraction valve, 4-naphthalene oil purge valve, 5-washing oil purge valve, 6-anthracene oil purge valve. DETAILED DESCRIPTION

[0012] The present application will be further described in detail below in combination with embodiments, as shown in the following. Figure 1

[0013] The tar distillation production process is a conventional vacuum distillation process, the raw material is coal tar, which is transported through a raw material pump, heated, and then enters a dehydration tower, the bottom of the dehydration tower is controlled at 190 DEG C, the light oil is extracted at the top at 100 DEG C, and the water-free tar at the bottom is heated by a heating furnace and then sent to a main tar tower for distillation, the main tower is operated under negative pressure, the pressure is controlled above-76 kpa, and the bottom is controlled above 270 DEG C to meet the distillation requirements of the main tower, the phenolic oil is extracted at the top, the naphthalene oil, washing oil and anthracene oil can be extracted at the side line, and the medium temperature pitch is extracted at the bottom, the product quality and yield are adjusted by the main tower reflux, side line temperature and extraction amount.

[0014] The light oil and naphthalene oil are transported to a dephenolization device after being extracted into an intermediate tank, the washing oil, anthracene oil and medium temperature pitch can be produced as products to a finished product warehouse. The medium temperature pitch can also be used as a raw material of a downstream modified pitch device, and is transported from the finished product warehouse to the modified device. The main control points of the present application are the control of the main tower and the adjustment and change of the rear-end products, and the front-end heat exchange and other auxiliary processes are not described in detail.

[0015] The improvement points of the present application are as follows: 1. Side line extraction modification and use.

[0016] ​The naphthalene oil, wash oil, and anthracene oil extracted from the side line are modified, and new pipelines and valves are added for blowing and emptying when the online production is stopped and a single product is extracted, to meet the blowing and emptying requirements when the extraction is stopped. The functions are realized according to the following operations: (1) When the naphthalene oil is stopped for extraction alone, close the naphthalene oil extraction valve 1, open the naphthalene oil blowing valve 4 to blow the naphthalene oil pipeline alone, close the naphthalene oil blowing valve 4 after blowing is completed, and wait for the next production adjustment. Open the naphthalene oil blowing valve 4 again before blowing, and then close the naphthalene oil blowing valve 4. Open the naphthalene oil extraction valve 1 for extraction.

[0017] (2) When the wash oil is stopped for extraction alone, close the wash oil extraction valve 2, open the wash oil blowing valve 5 to blow the naphthalene oil pipeline alone, close the wash oil blowing valve 5 after blowing is completed, and wait for the next production adjustment. Open the wash oil blowing valve 5 again before blowing, and then close the wash oil blowing valve 5. Open the wash oil extraction valve 2 for extraction.

[0018] (3) When the anthracene oil is stopped for extraction alone, close the anthracene oil extraction valve 3, open the anthracene oil blowing valve 6 to blow the naphthalene oil pipeline alone, close the anthracene oil blowing valve 6 after blowing is completed, and wait for the next production adjustment. Open the anthracene oil blowing valve 6 again before blowing, and then close the anthracene oil blowing valve 6. Open the anthracene oil extraction valve 3 for extraction.

[0019] (4) When multiple materials need to be stopped, follow the steps for stopping naphthalene oil, wash oil, and anthracene oil alone.

[0020] 2. Through production debugging, a production adjustment model for the opening and closing of the three oil products in the side line is formed.

[0021] In the case of regular production with all side lines extracted, the tower bottom temperature is controlled at 280℃, and each extraction is adjusted according to the normal yield. According to the actual production needs, the production debugging and solidification of the side line combination shutdown model are carried out.

[0022] (1) When the modification device is stopped, do not supply the medium temperature pitch, and the tower bottom of the tar main tower can be adjusted to produce carbon black oil, which can reduce energy costs, and the stop of the wash oil and anthracene oil side lines is required.

[0023] According to the steps for stopping naphthalene oil and anthracene oil, stop the wash oil first, then stop the anthracene oil, and simultaneously adjust the tower bottom temperature of the tar main tower. Sample and analyze the naphthalene oil and bottom carbon black oil, and continuously adjust the tower bottom temperature and the extraction of naphthalene oil and bottom carbon black oil based on the analysis results, After multiple rounds of production adjustment, the product quality meets the standard, the tower bottom temperature is controlled and adjusted to 265℃, the naphthalene oil extraction is adjusted to increase by 5%, and the remaining proportion is extracted by the bottom carbon black oil.

[0024] (2) When the wash oil product is in short supply, the wash oil side line extraction needs to be stopped.

[0025] Following the procedure of stopping the side stream oil washing, the washing oil production was stopped, and the temperature at the bottom of the tar tower was simultaneously lowered and adjusted. Naphthalene oil, anthracene oil, and medium-temperature pitch were sampled and analyzed. The bottom temperature of the tower and the side stream production were continuously adjusted based on the analysis results.

[0026] After several rounds of production adjustments, and with product quality meeting standards, the bottom temperature of the tower was reduced to 275℃, increasing the anthracene extraction ratio by 1%. Naphthalene oil and medium-temperature pitch did not require adjustment.

[0027] (3) When the modification unit produces low softening point asphalt, the side-stream anthracene oil extraction is stopped.

[0028] Following the procedure for stopping anthracene oil production via the side stream, anthracene oil production was stopped, and the temperature at the bottom of the tar tower was simultaneously lowered. Naphthalene oil, wash oil, and medium-temperature pitch were sampled and analyzed. The bottom temperature and side stream production were continuously adjusted based on the analysis results.

[0029] After several rounds of production adjustments, and with product quality meeting standards, the bottom temperature of the tower was reduced to 270℃, increasing the proportion of Chinese bitumen extracted by 4%. Naphthalene oil and wash oil did not require adjustment.

[0030] 3. Establishment of a refined oil depot oil product allocation system.

[0031] (1) Line 1 meets the needs of downstream customers. Currently, existing oil mixing tanks can be used to develop a mud gun oil system that uses wash oil and carbon black oil.

[0032] Add carbon black oil and wash oil to the mixing tank in a ratio of 4.39:1 (carbon black oil: wash oil) based on the theoretical data from the laboratory small-scale test. The order of addition is to add carbon black oil first, purge the pipeline, and then add wash oil. After purging the pipeline, turn on the mixing tank agitator and control the tank temperature to rise to 90-100℃. After mixing for 12 hours, stop the agitator, take a sample for analysis, and add carbon black oil or wash oil separately according to the analysis results until the softening point index required by the customer is reached.

[0033] (2) Line 2: By modifying and adding a configuration pipeline from the dephenolized oil to the anthracene oil tank, the existing storage tank is used to configure anthracene oil. The configuration requirements are based on the quality requirements of the anthracene oil demanded by the downstream customers.

[0034] After the dephenolized oil tank reaches 60%, confirm the current quality requirements of anthracene oil with the sales department. Based on the requirements, add the theoretical proportion to the anthracene oil tank and then conduct laboratory analysis of the anthracene oil. Based on the test results, confirm whether to add more. Since the quality requirements of anthracene oil are not clear, this invention does not provide a fixed theoretical addition ratio. It is based on the actual anthracene oil requirements. If there is no requirement, the dephenolized oil can also be sold separately as a normal dephenolized oil product.

[0035] (3) Line 3: By modifying and adding a configuration pipeline from anthracene oil to carbon black oil tank, the existing storage tank is used to configure carbon black oil. The configuration requirements are the same as the carbon black oil quality required by downstream customers.

[0036] The preparation of carbon black oil is related to the start-up and shutdown of the equipment. When the softening point of carbon black oil needs to be lowered and adjusted, anthracene oil is transported to the carbon black oil tank and added according to the actual required ratio. Adjustments are made based on the test analysis results. Therefore, the quality requirements are intermittent and occasional. This invention does not provide a fixed addition ratio. Anthracene oil and carbon black oil also have their own quality and requirements for separate external sales.

[0037] The above content is only used to illustrate the technical solution of the present invention. Simple modifications or equivalent substitutions made by those skilled in the art to the technical solution of the present invention do not depart from the essence and scope of the technical solution of the present invention.

Claims

1. A customized tar distillation process, characterized in that: The apparatus for the tar distillation process includes: a raw material tar tank, a dehydration tower, a heating furnace, and a main tower; the main tower is equipped with a side-line extraction valve and extraction pipeline, a phenol-removing oil tank, a naphthalene oil tank, a washing oil tank, an anthracene oil tank, a carbon black oil tank, a blending tank, and a configuration pipeline; the extraction pipeline is additionally equipped with a purging valve and purging pipeline for purging and venting; the configuration pipeline is additionally equipped with a configuration pipeline from the phenol-removing oil tank to the anthracene oil tank and a configuration pipeline from the anthracene oil tank to the carbon black oil tank; The tar distillation process involves adjusting production by independently controlling the start-stop combination of side-stream naphthalene oil, wash oil, and anthracene oil extraction, and customizing oil production through pipeline configuration. The start and stop methods for controlling the production of naphthalene oil, wash oil and anthracene oil from the control side are as follows: When production is stopped, close the production valve, open the purge valve to purge the pipeline, and close the purge valve after purging. When production is adjusted next time, first open the purge valve, close the purge valve after purging, and then open the production valve to produce.

2. The customized tar distillation process according to claim 1, characterized in that: The production adjustment based on the combination of starting and stopping the extraction of naphthalene oil, wash oil and anthracene oil from the control side line includes: adjusting the production of carbon black oil, stopping the extraction of wash oil from the side line and producing low softening point bitumen. The process of adjusting the production of carbon black oil is as follows: first stop the washing oil extraction from the side stream, then stop the anthracene oil extraction, and simultaneously reduce the bottom temperature of the tar main tower. Take samples of naphthalene oil and bottom carbon black oil for analysis. Based on the analysis results, continuously adjust the bottom temperature of the tower and the extraction of naphthalene oil from the side stream and bottom carbon black oil until the carbon black oil quality meets the standard. The bottom temperature of the tower is controlled and adjusted to 265℃, and the extraction of naphthalene oil is increased by 5%. The remaining proportion is balanced by the extraction of carbon black oil from the bottom of the tower. The process of stopping the side stream oil extraction is as follows: the side stream oil extraction is stopped, the temperature at the bottom of the tar main tower is reduced simultaneously, and naphthalene oil, anthracene oil and medium-temperature pitch are sampled and analyzed. Based on the analysis results, the bottom temperature and side stream extraction are continuously adjusted until the quality of naphthalene oil, anthracene oil and medium-temperature pitch meets the standards. The bottom temperature is adjusted to 275℃, and the extraction ratio of anthracene oil is increased by 1%. There is no need to adjust naphthalene oil and medium-temperature pitch. The process for producing low softening point asphalt is as follows: anthracene oil extraction is stopped from the side stream, the bottom temperature of the tar main tower is reduced simultaneously, naphthalene oil, wash oil and medium-temperature asphalt are sampled and analyzed, and the bottom temperature and side stream extraction are continuously adjusted according to the analysis results until the product quality meets the standards. The bottom temperature is adjusted to 270℃, and the extraction ratio of medium-temperature asphalt is increased by 4%. Naphthalene oil and wash oil do not need to be adjusted.

3. The customized tar distillation process according to claim 1, characterized in that: The customized production of oil products includes customized production of mud oil, anthracene oil, and carbon black oil; The customized production process of mud gun oil is as follows: carbon black oil and wash oil are delivered to the oil mixing tank through pumps and pipelines at a ratio of 4.39:

1. Carbon black oil is delivered first, the pipeline is purged, and then wash oil is delivered. After purging the pipeline, the mixing tank mixer is turned on, and the tank temperature is controlled to rise to 90-100℃. The mixer is stopped after mixing for 12 hours. Based on the sampling analysis results, carbon black oil or wash oil is added separately until the customized softening point index is reached. The customized production process of anthracene oil is as follows: after the dephenolized oil tank reaches 60%, the theoretical proportion of dephenolized oil is delivered to the anthracene oil tank through a pump and the pipeline from the dephenolized oil tank to the anthracene oil tank. Based on the analysis results of the anthracene oil, the addition ratio of dephenolized oil is adjusted according to the customized requirements until the customized requirements are met. The customized carbon black oil production process is as follows: when the softening point of the carbon black oil needs to be lowered according to the customized requirements, anthracene oil is transported to the carbon black oil tank through a pump and a pipeline connecting the anthracene oil tank to the carbon black oil tank. Based on the analysis results of the carbon black oil, the addition ratio of anthracene oil is adjusted according to the customized requirements until the customized requirements are met.

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