CN108096999B - Reboiler method negative pressure crude benzene distillation process - Google Patents
Reboiler method negative pressure crude benzene distillation process Download PDFInfo
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- CN108096999B CN108096999B CN201711401506.3A CN201711401506A CN108096999B CN 108096999 B CN108096999 B CN 108096999B CN 201711401506 A CN201711401506 A CN 201711401506A CN 108096999 B CN108096999 B CN 108096999B
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- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
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- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
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- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1425—Regeneration of liquid absorbents
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
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- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
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- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/18—Absorbing units; Liquid distributors therefor
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Abstract
The invention relates to a reboiler method negative pressure crude benzene distillation process, which uses superheated steam to heat tower bottom circulating wash oil to provide a heat source for a benzene removal tower, and distills crude benzene or light benzene in the wash oil in the benzene removal tower under a certain vacuum degree. In order to maintain the quality of the circulating wash oil, 1 to 1.5 percent of the circulating wash oil is led out and sent into a regenerator with a certain vacuum degree, and superheated steam is used for heating and regenerating; and (3) leading out a naphthalene oil fraction from the side line of the debenzolization tower to reduce the naphthalene content of lean oil. Compared with the existing crude benzene distillation process, the method has the remarkable advantages of low operation cost, good environmental protection effect and the like.
Description
Technical Field
The invention relates to the technical field of coking chemical product recovery, in particular to a negative pressure crude benzene distillation process by a reboiler method.
Background
In order to reduce the emission of waste water, a steam-free crude benzene distillation process (steam does not directly participate in the distillation process) appears in the recent coking industry, and the process is a process for heating rich oil and circulating hot lean oil by using a tube furnace to provide heat for a benzene removal tower, and the crude benzene separation water amount in the process is small, so that the emission of waste water is greatly reduced. However, the tube furnace produces a large amount of exhaust gas, which causes a certain exhaust emission; meanwhile, the waste gas of the tubular furnace heated by the coke oven gas hardly meets the pollutant emission standard of coking chemical industry, a matched waste gas treatment device is necessary, and the investment cost is high; although the SO in the waste gas can be reduced by using the tube furnace heated by blast furnace gas 2 The content of the waste gas is large, the equipment is large in amount of waste gas, and the environmental protection effect is poor. Meanwhile, the tube furnace is used for heating the rich oil and the wash oil, so that a large amount of the rich oil and the wash oil are condensed and coked, a large amount of residual oil is generated, the wash oil is wasted, and the operation cost is high.
In conclusion, the steam-free crude benzene distillation process at the present stage has the defects of running cost, environmental protection and the like, and is urgently needed to be solved.
At present, a dry quenching process is mostly adopted in the coke quenching process in the coking industry, and a large amount of high-pressure superheated steam is generated in the process, and the steam is commonly used for power generation or in a coal gas purification process. The invention relates to a negative pressure crude benzene distillation process for heating rich oil and wash oil by using high-temperature superheated steam generated by dry quenching.
Disclosure of Invention
Compared with the existing crude benzene distillation process, the reboiler-method negative pressure crude benzene distillation process has the remarkable advantages of low operation cost, good environmental protection effect and the like.
In order to achieve the above purpose, the invention is realized by adopting the following technical scheme:
a reboiler process negative pressure crude benzene distillation process comprising:
1) Sending the wash oil after absorbing benzene substances in the coal gas from the benzene washing tower into a lean-rich oil heat exchanger, exchanging heat with 210-245 ℃ hot lean oil led out from a hot lean oil pump at the bottom of the benzene removal tower, sending the heat into an oil-rich heater, heating to 190-220 ℃ and sending the heat into the benzene removal tower; the lean oil after heat exchange is sent to a final cooling section for benzene washing after being cooled by a lean oil primary cooler and a lean oil cooler secondary cooling;
2) In the benzene removal tower, stripping and distilling are carried out under the vacuum degree of minus 40 to minus 70KPa, part of circulating wash oil is extracted from the bottom of the benzene removal tower and is sent to a reboiler, and after being heated by high-pressure superheated steam at 300-550 ℃ from a dry quenching system, the wash oil is returned to the benzene removal tower to be used as a heat source and a stripping component for crude benzene distillation;
3) Crude benzene steam or light benzene steam with the temperature of 55-70 ℃ escaping from the top of the debenzolization tower enters a crude benzene or light benzene reflux tank for separation after passing through a crude benzene or light benzene condensation cooler, and the separated non-condensable gas is fed into a gas system by a debenzolization vacuum pump or an ejector after being further cooled by a benzene vapor cooler; oil-water separation is carried out on the separated liquid in a crude benzene or light benzene reflux tank, a part of the separated crude benzene or light benzene is sent to the top of a benzene removal tower by a crude benzene or light benzene pump to be used as reflux, and the rest is sent out as a product;
4) Leading out a naphthalene oil fraction from the side line of the debenzolization tower to reduce the naphthalene content of lean oil; leading out the naphthalene oil fraction to enter a residue tank, and periodically pumping the naphthalene oil fraction;
5) In order to maintain the quality of the circulating wash oil, 1 to 1.5 percent of the circulating wash oil is led out and sent into a regenerator, distillation regeneration is carried out under the vacuum degree of 200 to 230 ℃ and 75 to 95KPa below zero, and the regeneration heat source is high-temperature superheated steam from a dry quenching system;
6) Discharging the regenerated residues at the bottom of the benzene removal tower into a residue tank, and periodically pumping the regenerated residues out; the non-condensable gas at the bottom of the debenzolization tower is cooled by a wash oil condensation cooler, an oil-gas separator and an oil-gas cooler and then is sent to a gas system by a regenerative vacuum pump or an ejector;
during operation of the system, the operating pressure of the debenzolization tower and the regenerator is below atmospheric pressure, i.e., at negative pressure.
In order to ensure the distillation efficiency of crude benzene in the benzene removal tower, the operating pressure of the benzene removal tower is pumped to 30-60 KPa absolute pressure by a benzene removal vacuum pump or an ejector, and the operating temperature of the benzene removal tower bottom is maintained at 190-245 ℃.
In order to ensure the efficiency of the regeneration of the wash oil in the regenerator, the operation pressure of the regenerator is pumped by a regenerating vacuum pump or an ejector to have an absolute pressure of 5 to 25KPa, and the operation temperature is maintained at 200 to 230 ℃.
In order to reduce the resistance of the debenzolization tower, a rectifying section of the debenzolization tower adopts a tray structure, and a stripping section adopts a filler structure.
The condensation water generated after the heat exchange of the high-pressure superheated steam is subjected to flash evaporation to generate low-pressure steam, the low-pressure steam is sent to a low-pressure steam pipe network for recycling, and the residual condensation water is returned to the boiler for recycling.
Compared with the prior art, the invention has the beneficial effects that:
1) The operation cost is low: compared with the existing negative pressure crude benzene distillation process without steam, the invention uses steam to heat the rich oil and the wash oil, has low operation temperature, effectively inhibits the slagging of the wash oil, reduces the production quantity of the residual oil and the update quantity of the wash oil, and reduces the operation cost;
2) The environmental protection effect is good: compared with the prior crude benzene distillation process, the invention does not have a tube furnace, does not generate tube furnace waste gas, and reduces the discharge amount of the waste gas; meanwhile, the crude benzene separation water is less in generation amount, so that the wastewater discharge capacity is greatly reduced;
3) The benzene gas, oil gas and the like separated from the top of the benzene removal tower and the regenerator are sent to a gas system, so that the environmental protection of the process and the effective recovery of benzene substances are ensured.
Drawings
FIG. 1 is a flow chart of a reboiler process negative pressure crude benzene distillation process according to the present invention.
In the figure: 1. the benzene removal column 2, the regenerator 3, the reboiler 4, the crude benzene or light benzene condensate cooler 5, the crude benzene or light benzene reflux drum 6, the benzene vapor cooler 7, the benzene removal vacuum pump or ejector 8, the wash oil condensate cooler 9, the oil vapor separator 10, the oil vapor cooler 11, the regenerative vacuum pump or ejector 12, the crude benzene or light benzene pump 13, the hot lean oil pump 14, the lean oil-rich heat exchanger 15, the lean oil first-stage cooler 16, the lean oil second-stage cooler 17, the rich oil heater
Detailed Description
The following is a further description of embodiments of the invention, taken in conjunction with the accompanying drawings:
as shown in fig. 1, the negative pressure crude benzene distillation process by the reboiler method of the invention comprises the following steps:
1) Sending wash oil after absorbing benzene substances in the coal gas from the benzene washing tower into a lean-rich oil heat exchanger 14, exchanging heat with 210-245 ℃ hot lean oil led out from a hot lean oil pump 13 at the bottom of the benzene removal tower, sending the heat into an oil-rich heater 17, heating to 190-220 ℃ and sending the heat into the benzene removal tower 1; the lean oil after heat exchange is cooled by a lean oil primary cooler 15 and a lean oil secondary cooler 16 and then sent to a final cooling section for benzene washing;
2) In the debenzolization tower 1, stripping and distilling are carried out under the vacuum degree of minus 40 to minus 70KPa, part of circulating wash oil is extracted from the bottom of the debenzolization tower and is sent to the reboiler 3, and after being heated by using 300-550 ℃ high-pressure superheated steam from a dry quenching system, the steam returns to the debenzolization tower 1 to be used as a heat source and a stripping component for crude benzene distillation;
3) Crude benzene steam or light benzene steam with the temperature of 55-70 ℃ escaping from the top of the benzene removal tower 1 enters a crude benzene or light benzene reflux tank 5 for separation after passing through a crude benzene or light benzene condensation cooler 4, and the separated non-condensable gas is sent into a gas system by a benzene vapor cooler 6 after being further cooled by a benzene removal vacuum pump or an ejector 7; the separated liquid is subjected to oil-water separation in a crude benzene or light benzene reflux tank 5, a part of the separated crude benzene or light benzene is sent to the top of a benzene removal tower 1 by a crude benzene or light benzene pump 12 to be used as reflux, and the rest is sent out as a product;
4) Leading out a naphthalene oil fraction from the side line of the debenzolization tower to reduce the naphthalene content of lean oil; leading out the naphthalene oil fraction to enter a residue tank, and periodically pumping the naphthalene oil fraction;
5) In order to maintain the quality of the circulating wash oil, 1 to 1.5 percent of the circulating wash oil is led out and sent into a regenerator 2 for distillation and regeneration at the temperature of 200 to 230 ℃ and the vacuum degree of minus 75 to minus 95KPa, and the regeneration heat source is high-temperature superheated steam from a dry quenching system;
6) Discharging the regenerated residues at the bottom of the benzene removal tower into a residue tank, and periodically pumping the regenerated residues out; the non-condensable gas at the bottom of the debenzolization tower is cooled by a wash oil condensation cooler 8, an oil-gas separator 9 and an oil-gas cooler 10 and then is sent to a gas system by a regenerative vacuum pump or an ejector 11;
during operation of the system, the operating pressure of the debenzolization tower 1 and the regenerator 2 is below atmospheric pressure, i.e., at a negative pressure.
In order to ensure the distillation efficiency of crude benzene in the debenzolization tower 1, the operating pressure of the debenzolization tower is pumped to 30-60 KPa absolute pressure by a debenzolization vacuum pump or an ejector 7, and the operating temperature of the bottom of the debenzolization tower is maintained at 190-245 ℃.
In order to ensure the efficiency of the regeneration of the wash oil in the regenerator 2, the operating pressure of the regenerator is pumped with a regenerating vacuum pump or the absolute pressure of the ejector 11 is 5 to 25KPa, and the operating temperature is maintained at 200 to 230 ℃.
In order to reduce the resistance of the debenzolization tower 1, a rectifying section of the debenzolization tower 1 adopts a tray structure, and a stripping section adopts a filler structure.
The condensation water generated after the heat exchange of the high-pressure superheated steam is subjected to flash evaporation to generate low-pressure steam, the low-pressure steam is sent to a low-pressure steam pipe network for recycling, and the residual condensation water is returned to the boiler for recycling.
The invention relates to a reboiler method negative pressure crude benzene distillation process, which adopts the working principle that superheated steam is used for heating circulating wash oil at the bottom of a tower to provide a heat source for a benzene removal tower 1, and crude benzene or light benzene in the wash oil is distilled out from the benzene removal tower 1 under a certain vacuum degree. In order to maintain the quality of the circulating wash oil, 1 to 1.5 percent of the circulating wash oil is led out and sent into a regenerator 2 with a certain vacuum degree, and superheated steam is used for heating and regenerating; and (3) leading out a naphthalene oil fraction from the side line of the debenzolization tower to reduce the naphthalene content of lean oil. The process has the remarkable advantages of low running cost, good environmental protection effect and the like.
The foregoing is only a preferred embodiment of the present invention, but the scope of the present invention is not limited thereto, and any person skilled in the art, who is within the scope of the present invention, should make equivalent substitutions or modifications according to the technical scheme of the present invention and the inventive concept thereof, and should be covered by the scope of the present invention.
Claims (3)
1. The reboiler method negative pressure crude benzene distillation process is characterized by comprising the following steps:
1) Sending the wash oil after absorbing benzene substances in the coal gas from the benzene washing tower into a lean-rich oil heat exchanger, exchanging heat with 210-245 ℃ hot lean oil led out from a hot lean oil pump at the bottom of the benzene removal tower, sending the heat into an oil-rich heater, heating to 190-220 ℃ and sending the heat into the benzene removal tower; the lean oil after heat exchange is cooled by a lean oil first-stage cooler and a lean oil second-stage cooler and then is sent to a final cooling section for benzene washing;
2) In the benzene removal tower, stripping and distilling are carried out under the vacuum degree of minus 40 to minus 70KPa, part of circulating wash oil is extracted from the bottom of the benzene removal tower and is sent to a reboiler, and after being heated by high-pressure superheated steam at 300-550 ℃ from a dry quenching system, the wash oil is returned to the benzene removal tower to be used as a heat source and a stripping component for crude benzene distillation;
3) Crude benzene steam or light benzene steam with the temperature of 55-70 ℃ escaping from the top of the debenzolization tower enters a crude benzene or light benzene reflux tank for separation after passing through a crude benzene or light benzene condensation cooler, and the separated non-condensable gas is fed into a gas system by a debenzolization vacuum pump or an ejector after being further cooled by a benzene vapor cooler; oil-water separation is carried out on the separated liquid in a crude benzene or light benzene reflux tank, a part of the separated crude benzene or light benzene is sent to the top of a benzene removal tower by a crude benzene or light benzene pump to be used as reflux, and the rest is sent out as a product;
4) Leading out a naphthalene oil fraction from the side line of the debenzolization tower to reduce the naphthalene content of lean oil; leading out the naphthalene oil fraction to enter a residue tank, and periodically pumping the naphthalene oil fraction;
5) In order to maintain the quality of the circulating wash oil, leading out 1 to 1.5 percent of hot lean oil as the circulating wash oil to be sent into a regenerator, and carrying out distillation regeneration at the vacuum degree of between 200 and 230 ℃ and between 75 and 95KPa below zero, wherein the regeneration heat source is high-temperature superheated steam from a dry quenching system;
6) Discharging the regenerated residues at the bottom of the benzene removal tower into a residue tank, and periodically pumping the regenerated residues out; the non-condensable gas at the bottom of the debenzolization tower is cooled by a wash oil condensation cooler, an oil-gas separator and an oil-gas cooler and then is sent to a gas system by a regenerative vacuum pump or an ejector;
during the operation of the system, the operating pressure of the debenzolization tower and the regenerator is lower than the atmospheric pressure, namely in a negative pressure state;
in order to ensure the distillation efficiency of crude benzene in the benzene removal tower, the operating pressure of the benzene removal tower is pumped to 30-60 KPa absolute pressure by a benzene removal vacuum pump or an ejector, and the operating temperature of the benzene removal tower bottom is maintained at 190-245 ℃;
in order to ensure the efficiency of the regeneration of the wash oil in the regenerator, the operating pressure of the regenerator is pumped to 5-25 KPa absolute pressure by a regenerating vacuum pump or an ejector, and the operating temperature is maintained at 200-230 ℃.
2. The process according to claim 1, wherein the rectifying section of the debenzolization tower is tray structure and the stripping section is packing structure.
3. The reboiler-method negative pressure crude benzene distillation process according to claim 1, wherein the condensate water generated after heat exchange of the high-pressure superheated steam is flashed to generate low-pressure steam, and the low-pressure steam is sent to a low-pressure steam pipe network for reuse, and the residual condensate water is returned to the boiler for recycling.
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| CN108911938B (en) * | 2018-08-22 | 2024-01-23 | 樊晓光 | Middle-low pressure steam heating process and device in crude benzene distillation system |
| CN111253203A (en) * | 2020-03-17 | 2020-06-09 | 本钢板材股份有限公司 | Heat exchange optimization process for crude benzene distillation section |
| CN111939584B (en) * | 2020-09-04 | 2023-09-15 | 中冶焦耐(大连)工程技术有限公司 | Crude benzene evaporation process and system in benzene hydrogenation reaction system |
| CN113521965A (en) * | 2021-01-29 | 2021-10-22 | 乌海宝杰新能源材料有限公司 | Efficient and energy-saving granulation tail gas treatment system and treatment process thereof |
| CN113150840B (en) * | 2021-04-23 | 2023-03-28 | 济南冶金化工设备有限公司 | Self-azeotropic negative pressure debenzolization process |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101289633A (en) * | 2007-04-20 | 2008-10-22 | 宝山钢铁股份有限公司 | Novel regeneration process for circulation oil of crude benzol device |
| CN103382404A (en) * | 2013-04-15 | 2013-11-06 | 北京中亿孚佑科技有限公司 | New method for benzene elution of coke-oven gas |
| CN103555377A (en) * | 2013-10-24 | 2014-02-05 | 天津市创举科技有限公司 | Method and equipment for reduced-pressure benzene removal |
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Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101289633A (en) * | 2007-04-20 | 2008-10-22 | 宝山钢铁股份有限公司 | Novel regeneration process for circulation oil of crude benzol device |
| CN103382404A (en) * | 2013-04-15 | 2013-11-06 | 北京中亿孚佑科技有限公司 | New method for benzene elution of coke-oven gas |
| CN103555377A (en) * | 2013-10-24 | 2014-02-05 | 天津市创举科技有限公司 | Method and equipment for reduced-pressure benzene removal |
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