CN215250663U - Negative pressure benzene removal system for preparing superheated steam through electric heating - Google Patents
Negative pressure benzene removal system for preparing superheated steam through electric heating Download PDFInfo
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- CN215250663U CN215250663U CN202121086752.6U CN202121086752U CN215250663U CN 215250663 U CN215250663 U CN 215250663U CN 202121086752 U CN202121086752 U CN 202121086752U CN 215250663 U CN215250663 U CN 215250663U
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Abstract
The utility model relates to a negative pressure debenzolization system for preparing superheated steam by electric heating, which comprises a debenzolization tower, a regenerator, a crude benzene condensation cooler, a gas-liquid separator, a vacuum device, an oil-water separation device, a crude benzene reflux pump, a hot lean oil pump, an electric heater, a lean-rich oil heat exchanger, a rich oil heater, a first-stage lean oil cooler and a second-stage lean oil cooler; the utility model has the advantages of less fixed investment, lower energy consumption, simple flow and good environmental protection.
Description
Technical Field
The utility model relates to a coking product retrieves technical field, especially relates to a superheated steam's negative pressure debenzolization system is prepared to electrical heating.
Background
Benzene series in the coke oven gas belongs to high-value byproducts, and generally coking wash oil is adopted to absorb the benzene series in the coke oven gas to form rich oil, and the rich oil is subjected to a debenzolization process to obtain high-value byproducts such as crude benzene or light benzene.
At present, the benzene removal process in the coking industry generally comprises a normal-pressure superheated steam stripping benzene removal process, a negative-pressure superheated steam stripping benzene removal process and a tubular furnace heating wash oil steam-free benzene removal process, wherein:
the technology of the normal pressure superheated steam stripping method debenzolization process is mature and the operation is stable, but the process consumes a large amount of steam, and about 1.5 tons of 400 ℃ superheated steam is consumed for every 1 ton of crude benzene.
The benzene removal by the negative pressure superheated steam stripping method is a process which is gradually popularized in the coking industry in recent years. The noncondensable gas which is not condensed behind the crude benzene condensing cooler is extracted by utilizing vacuum equipment, so that the debenzolization system is in a negative pressure state. Compared with the benzene removal process by the normal-pressure superheated steam stripping method, the process increases a small amount of investment of vacuum equipment and the like, but can greatly reduce the consumption of superheated steam, and about 0.75 ton of superheated steam is consumed for each 1 ton of crude benzene. At present, most of newly built coking plants at home and abroad adopt a negative pressure superheated steam stripping method for benzene removal.
Both of the above-mentioned two debenzolization processes require the use of superheated steam for debenzolization. At present, methods for generating superheated steam include: (1) the tubular furnace heats the low-pressure saturated steam to generate low-pressure superheated steam; (2) and (4) carrying out temperature reduction and pressure reduction on the high-pressure superheated steam of the dry quenching to generate medium-pressure superheated steam. The method for producing the low-pressure superheated steam by heating the low-pressure saturated steam by the tubular furnace is simple and easy to implement, and most coking enterprises still adopt the method to produce the superheated steam at present. However, the tube furnace generally consumes coking self-produced gas and SO in the produced flue gas2The requirements of coking environmental protection standard can not be easily met. In addition, the first and second substrates are,the tubular furnace has low heat efficiency, high fuel consumption and high operation cost. And because of the industrial safety requirement, the tube furnace and other equipment have the spacing requirement, so the occupied area is larger, and the newly-built crude benzene distillation unit generally adopts the method less. The method for producing medium-pressure superheated steam by reducing temperature and pressure of high-pressure superheated steam produced by dry quenching coke is a method for replacing a tubular furnace method, but the method needs a dry quenching coke device in a plant area and needs additional equipment for reducing temperature and pressure and the like. The method can be implemented by the dry quenching device which is commonly arranged in the newly built factory, but the method is difficult to be applied to the improvement of the debenzolization process of the old factory due to the limited conditions of the old factory.
The steam-free debenzolization process of the heating wash oil of the tubular furnace is different from the two debenzolization processes, and the steam of the wash oil formed after the wash oil is heated and flashed by the tubular furnace is utilized to strip crude benzene. Compared with the two debenzolization processes, the process system needs higher vacuum degree, and increases the investment of equipment such as a vacuum pump, a tubular furnace for heating the circulating lean oil at the bottom of the tower, a lean oil circulating pump and the like; compared with the method that the temperature of the lean oil at the bottom of the debenzolization tower in the steam stripping method debenzolization process is 175-180 ℃, the temperature of the lean oil at the bottom of the debenzolization tower in the steam-free method debenzolization process is generally controlled to be 220-240 ℃, the temperature of the lean oil at the bottom of the debenzolization tower is higher, the deterioration degree of the wash oil is increased, and the consumption of the wash oil is inevitably increased. However, no external steam enters the debenzolization system in the process, the generation of waste water cannot be increased, and comprehensively, compared with the debenzolization by the two superheated steam stripping methods, the debenzolization method has higher operation cost, and the method is less applied at home and abroad at present.
The patent of the utility model discloses a chinese utility model with the publication number of CN 103555377B discloses a method for debenzolizing under reduced pressure, which adopts the steam-free debenzolizing process, and the heat source at the bottom of the debenzolizing tower and the heat source for the regenerated wash oil all adopt the electric heating mode to supply heat, replace the heating mode of the tube furnace, and reduce the emission of the combustion tail gas pollutants. Compared with the existing negative pressure superheated steam stripping debenzolization process, the debenzolization method has the advantages that the operation energy consumption is still higher, the operation temperature is higher than that of the negative pressure superheated steam stripping debenzolization process, the washing oil consumption is still higher than that of the pressure steaming superheated steam stripping debenzolization process, and the whole operation cost is higher although the characteristics of high washing oil deterioration degree and high washing oil consumption caused by high wall temperature of a heating pipe of a tubular furnace are avoided.
Disclosure of Invention
The utility model provides a negative pressure benzene removal system for superheated steam preparation through electric heating, which has the advantages of less fixed investment, lower energy consumption, simple flow and good environmental protection.
In order to achieve the above purpose, the utility model adopts the following technical scheme:
a negative pressure debenzolization system for preparing superheated steam by electric heating comprises a debenzolization tower, a regenerator, a crude benzene condensation cooler, a gas-liquid separator, a vacuum device, an oil-water separation device, a crude benzene reflux pump, a hot lean oil pump, an electric heater, a lean rich oil heat exchanger, a rich oil heater, a first-stage lean oil cooler and a second-stage lean oil cooler; the upper part of the debenzolization tower is provided with a rich oil inlet which is connected with a rich oil outlet of the final cooling benzene washing unit through a rich oil pipeline, and the rich oil pipeline is sequentially provided with a lean rich oil heat exchanger and a rich oil heater along the flow direction of rich oil; the bottom of the debenzolization tower is provided with a hot lean oil outlet which is connected with a lean oil inlet of a lean-rich oil heat exchanger through a hot lean oil pipeline, and the hot lean oil pipeline is provided with a hot lean oil pump; a lean oil outlet of the lean-rich oil heat exchanger is sequentially connected with a first-section lean oil cooler and a second-section lean oil cooler; a crude benzene outlet is arranged at the top of the debenzolization tower and is sequentially connected with a crude benzene condensation cooler and a gas-liquid separator through a crude benzene pipeline; the gas outlet of the gas-liquid separator is connected with a gas pipeline at the upstream of the final cooling benzene washing unit through a vacuum device; the liquid phase outlet of the gas-liquid separator is connected with the oil-water mixed liquid inlet in the oil-water separating device; an oil phase outlet of the oil-water separation device is connected with a reflux crude benzene inlet at the upper part of the debenzolization tower through a crude benzene reflux pump; the top of the regenerator is provided with a steam outlet which is connected with a steam inlet at the lower part of the debenzolization tower; the saturated steam pipeline is connected with a superheated steam inlet at the lower part of the regenerator and a steam inlet at the lower part of the debenzolization tower through an electric heater, and the medium-pressure saturated steam pipeline is connected with a steam inlet of the rich oil heater.
The debenzolization tower is a packing type or plate type debenzolization tower or a combination of packing and plate type debenzolization towers.
The regenerator has a plate tray configuration.
Compared with the prior art, the beneficial effects of the utility model are that:
1) the electric heater is adopted to heat the steam into superheated steam which is used as a steam source for lean oil regeneration and debenzolization operation, compared with a mode of heating the steam by adopting a tubular heating furnace, the method avoids the environmental protection problem caused by tail gas combustion, and further reduces the occupied area and equipment investment;
2) the steam is heated into superheated steam by an electric heater to be used as a steam source for lean oil regeneration and debenzolization, so that the problems that no superheated steam source exists in a plant area and the debenzolization steam of a tubular furnace cannot be adopted can be solved;
3) compared with the existing superheated steam stripping debenzolization process, the process of the utility model can release the dependence of debenzolization on the superheated steam source in the factory; and the mode of preparing superheated steam by adopting the electric heater has lower requirement on a steam source and is generally suitable for various coking plants.
Drawings
Fig. 1 is a schematic structural diagram of a negative pressure benzene removal system for preparing superheated steam by electric heating.
In the figure: 1. a debenzolization tower 2, a regenerator 3, a crude benzene condensation cooler 4, a gas-liquid separator 5, a vacuum device 6, an oil-water separation device 7, a crude benzene reflux pump 8, a hot lean oil pump 9, an electric heater 10, a lean rich oil heat exchanger 11, a rich oil heater 12, a first-stage lean oil cooler 13, a second-stage lean oil cooler
Detailed Description
The following description of the embodiments of the present invention will be made with reference to the accompanying drawings:
as shown in fig. 1, the utility model relates to a negative pressure debenzolization system for preparing superheated steam by electric heating, which comprises a debenzolization tower 1, a regenerator 2, a crude benzene condensation cooler 3, a gas-liquid separator 4, a vacuum device 5, an oil-water separation device 6, a crude benzene reflux pump 7, a hot lean oil pump 8, an electric heater 9, a lean-rich oil heat exchanger 10, a rich oil heater 11, a first-stage lean oil cooler 12 and a second-stage lean oil cooler 13; an oil-rich inlet is formed in the upper part of the debenzolization tower 1 and is connected with an oil-rich outlet of the final-cooling benzene washing unit through an oil-rich pipeline, and a lean-rich heat exchanger 10 and a rich heater 11 are sequentially arranged on the oil-rich pipeline along the flow direction of rich oil; the bottom of the debenzolization tower 1 is provided with a hot lean oil outlet which is connected with a lean oil inlet of a lean rich oil heat exchanger 10 through a hot lean oil pipeline, and the hot lean oil pipeline is provided with a hot lean oil pump 8; a lean oil outlet of the lean-rich oil heat exchanger 10 is sequentially connected with a first-stage lean oil cooler 12 and a second-stage lean oil cooler 13; a crude benzene outlet arranged at the top of the debenzolization tower 1 is sequentially connected with a crude benzene condensation cooler 3 and a gas-liquid separator 4 through a crude benzene pipeline; a gas phase outlet of the gas-liquid separator 4 is connected with a gas pipeline at the upstream of the final cooling benzene washing unit through a vacuum device 5; the liquid phase outlet of the gas-liquid separator 4 is connected with the oil-water mixed liquid inlet of the oil-water separator 6; an oil phase outlet of the oil-water separation device 6 is connected with a reflux crude benzene inlet at the upper part of the debenzolization tower 1 through a crude benzene reflux pump 7; the top of the regenerator 2 is provided with a steam outlet which is connected with a steam inlet at the lower part of the debenzolization tower 1; the saturated steam pipeline is connected with a superheated steam inlet at the lower part of the regenerator 2 and a steam inlet at the lower part of the debenzolization tower 1 through an electric heater 9, and the medium-pressure saturated steam pipeline is connected with a steam inlet of the rich oil heater 11.
The debenzolization tower 1 is a packing type or plate type debenzolization tower or a combination of packing and plate type debenzolization towers.
The regenerator 2 has a plate tray configuration.
The technical process of the negative pressure debenzolization system for preparing superheated steam by electric heating is as follows:
1) rich oil sent by the final cooling benzene washing unit exchanges heat with hot lean oil pumped out from the bottom of the debenzolization tower 1 through a lean rich oil heat exchanger 10 to 175-185 ℃, enters a rich oil heater 11 for heating, and enters the debenzolization tower 1 for debenzolization after heating;
2) the operation vacuum degree at the top of the debenzolization tower 1 is-40 kPa to-80 kPa, crude benzene steam and water steam from the top of the debenzolization tower enter a crude benzene condensation cooler 3 for condensation and cooling, and a gas-liquid mixture after condensation and cooling enters a gas-liquid separator 4 for gas-liquid two-phase separation;
3) the liquid phase part separated by the gas-liquid separator 4 enters an oil-water separation device 6 for oil-water two-phase separation operation, one part of the crude benzene oil phase after two-phase separation is sent to the top of the debenzolization tower by a crude benzene reflux pump 7 to be used as tower top reflux, and the other part is directly sent to an oil depot for storage; the separated water phase part is sent to a final cooling benzene washing unit or a tar ammonia water separation unit;
4) the noncondensable gas phase part separated by the gas-liquid separator 4 is sucked by a vacuum device 5 to generate negative pressure, so that the benzene removal system maintains the negative pressure state; the pumped noncondensable gas phase is discharged into a gas pipeline before benzene washing after passing through a vacuum device 5;
5) medium-pressure saturated steam or superheated steam with the pressure of 1.2MPa to 4.0MPa enters the rich oil heater 11 to be used as a heat source for heating the rich oil; saturated steam with the pressure of 0.2 MPa-2.0 MPa enters an electric heater 9, superheated steam with the temperature of 300-420 ℃ is heated by electric heating and then enters a regenerator 2 to be used as ascending stripping steam during the regeneration of lean oil;
6) the operation vacuum degree at the top of the regenerator 2 is-30 kPa to-70 kPa, and the wash oil steam and the water steam coming out from the top of the regenerator 2 enter the bottom of the debenzolization tower 1 to be used as ascending stripping steam during the debenzolization operation;
7) the temperature of hot lean oil at the bottom of the debenzolization tower is 170-190 ℃, the hot lean oil is sent to a lean rich oil heat exchanger 10 by a hot lean oil pump 8 to exchange heat with rich oil sent by a final cooling benzene washing unit, and then the hot lean oil enters a first-stage lean oil cooler 12 and a second-stage lean oil cooler 13 to be cooled, and the cooled lean oil is sent to a benzene washing tower in the final cooling benzene washing unit to be subjected to benzene washing operation.
The following examples are carried out on the premise of the technical solution of the present invention, and detailed embodiments and specific operation procedures are given, but the scope of the present invention is not limited to the following examples. The methods used in the following examples are conventional methods unless otherwise specified.
[ examples ] A method for producing a compound
In this example, the coke production capacity is 250 ten thousand tons/year, and the washing oil circulation amount is 300m3The crude benzene yield is 5.5t/h, and the energy consumption comparison of four different debenzolization processes is detailed in Table 1.
TABLE 1
As can be seen from the above table, the operating costs of the four debenzolization processes are as follows: the negative pressure electric heating benzene removal process without steam is more than the normal pressure superheated steam stripping benzene removal process, the negative pressure electric heating superheated steam preparation stripping process and the negative pressure superheated steam stripping benzene removal process.
Therefore, the utility model is particularly suitable for the coking enterprises that the factory does not have superheated steam vapour source, can not adopt the tube furnace moreover.
The above, only be the concrete implementation of the preferred embodiment of the present invention, but the protection scope of the present invention is not limited thereto, and any person skilled in the art is in the technical scope of the present invention, according to the technical solution of the present invention and the utility model, the concept of which is equivalent to replace or change, should be covered within the protection scope of the present invention.
Claims (3)
1. A negative pressure debenzolization system for preparing superheated steam by electric heating is characterized by comprising a debenzolization tower, a regenerator, a crude benzene condensation cooler, a gas-liquid separator, a vacuum device, an oil-water separation device, a crude benzene reflux pump, a hot lean oil pump, an electric heater, a lean-rich oil heat exchanger, a rich oil heater, a first-stage lean oil cooler and a second-stage lean oil cooler; the upper part of the debenzolization tower is provided with a rich oil inlet which is connected with a rich oil outlet of the final cooling benzene washing unit through a rich oil pipeline, and the rich oil pipeline is sequentially provided with a lean rich oil heat exchanger and a rich oil heater along the flow direction of rich oil; the bottom of the debenzolization tower is provided with a hot lean oil outlet which is connected with a lean oil inlet of a lean-rich oil heat exchanger through a hot lean oil pipeline, and the hot lean oil pipeline is provided with a hot lean oil pump; a lean oil outlet of the lean-rich oil heat exchanger is sequentially connected with a first-section lean oil cooler and a second-section lean oil cooler; a crude benzene outlet is arranged at the top of the debenzolization tower and is sequentially connected with a crude benzene condensation cooler and a gas-liquid separator through a crude benzene pipeline; the gas outlet of the gas-liquid separator is connected with a gas pipeline at the upstream of the final cooling benzene washing unit through a vacuum device; the liquid phase outlet of the gas-liquid separator is connected with the oil-water mixed liquid inlet in the oil-water separating device; an oil phase outlet of the oil-water separation device is connected with a reflux crude benzene inlet at the upper part of the debenzolization tower through a crude benzene reflux pump; the top of the regenerator is provided with a steam outlet which is connected with a steam inlet at the lower part of the debenzolization tower; the saturated steam pipeline is connected with a superheated steam inlet at the lower part of the regenerator and a steam inlet at the lower part of the debenzolization tower through an electric heater, and the medium-pressure saturated steam pipeline is connected with a steam inlet of the rich oil heater.
2. The negative-pressure debenzolization system for producing superheated steam through electric heating as claimed in claim 1, wherein the debenzolization tower is a packed type, a plate type or a combination of packed and plate type debenzolization towers.
3. An electrically heated superheated steam generating negative pressure debenzolization system as claimed in claim 1 wherein said regenerator has a tray-in-tray configuration.
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| CN113201370A (en) * | 2021-05-20 | 2021-08-03 | 中冶焦耐(大连)工程技术有限公司 | Negative pressure debenzolization process and system for preparing superheated steam through electric heating |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN113201370A (en) * | 2021-05-20 | 2021-08-03 | 中冶焦耐(大连)工程技术有限公司 | Negative pressure debenzolization process and system for preparing superheated steam through electric heating |
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