CN107057776B - Benzene washing process for cooling washing oil in tower - Google Patents
Benzene washing process for cooling washing oil in tower Download PDFInfo
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- CN107057776B CN107057776B CN201611206831.XA CN201611206831A CN107057776B CN 107057776 B CN107057776 B CN 107057776B CN 201611206831 A CN201611206831 A CN 201611206831A CN 107057776 B CN107057776 B CN 107057776B
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- oil
- benzene
- washing
- heat exchanger
- tower
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
- C10K1/00—Purifying combustible gases containing carbon monoxide
- C10K1/002—Removal of contaminants
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
- C10K1/00—Purifying combustible gases containing carbon monoxide
- C10K1/08—Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors
- C10K1/16—Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors with non-aqueous liquids
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
- C10K1/00—Purifying combustible gases containing carbon monoxide
- C10K1/08—Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors
- C10K1/16—Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors with non-aqueous liquids
- C10K1/18—Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors with non-aqueous liquids hydrocarbon oils
Abstract
A benzene washing process for cooling washing oil in a tower comprises the following steps: introducing coke oven gas into the lower end of a benzene washing tower, and spraying washing oil from the top of the benzene washing tower; mixing the washing oil and the coke oven gas in a tube pass of a heat exchanger, and controlling the temperature in the tube pass of the heat exchanger to be within the range of 22-26 ℃; the shell side of the heat exchanger is filled with a heat absorption solution, and the heat absorption solution exchanges heat with a mixture of the wash oil and the coke oven gas to control the temperature rise of the wash oil caused by absorbing heat released by benzene hydrocarbon in the coke oven gas; a pressure sensor, a vacuum pump and a liquid level meter are arranged on the shell tube side of the heat exchanger, and the pressure sensor controls the starting and stopping of the vacuum pump so as to keep the micro-vacuum of which the pressure in the shell side is in the range of 2000-3000 Pa; heating the rich oil, sending the rich oil into a debenzolization tower, treating to obtain lean oil, and adding the lean oil into the wash oil for recycling to the benzene washing tower. Compared with the prior art that the recycle quantity of the washing oil is increased to improve the recovery rate of the crude benzene, the invention can improve the recovery rate of the crude benzene by at least 20 percent under the same consumption of the washing oil, and the increase of the overall energy consumption is small.
Description
Technical Field
The invention relates to the field of coal coking benzene washing, in particular to a benzene washing process for cooling washing oil in a benzene washing tower.
Background
In the chemical industry, each component in a gas mixture is often required to be separated, useful substances in the gas mixture are recovered, and economic benefits are increased; or removing harmful substances therein to prevent environmental pollution.
In the existing coke oven gas purification equipment and process, the wash oil is usually used as an absorbent to recycle the benzene hydrocarbon therein, the wash oil can release solution heat in the process of absorbing the benzene hydrocarbon, the wash oil absorption temperature and the benzene hydrocarbon recovery rate have very large correlation, the wash oil temperature is about 25 ℃, the temperature is optimum, and the crude benzene recovery rate is high. However, the temperature of the wash oil is continuously increased due to the release of the heat of solution, so that the temperature of the wash oil in the benzene washing tower is far higher than the proper absorption temperature, and the crude benzene absorption efficiency is low. In order to control the benzene content behind the tower, the conventional benzene washing process only uses a mode of improving the recycle volume of the washing oil, and overcomes the influence of the reduction of the absorption rate of crude benzene by increasing the supply volume of the washing oil, so that the consumption of the washing oil is increased, the corresponding treatment capacity of subsequent rich oil is increased, the operation cost and the power consumption are increased, and the improvement of the overall performance of the process is not facilitated.
Disclosure of Invention
The invention provides a benzene washing process for cooling washing oil in a tower, which is used for solving the problems in the prior art.
In order to realize the purpose of the invention, the following technical scheme is adopted:
a benzene washing process for cooling washing oil in a tower comprises the following steps:
introducing the coke oven gas into the lower end of a benzene washing tower, spraying washing oil from the top of the benzene washing tower to absorb benzene substances in the coke oven gas, obtaining purified coke oven gas at the upper end of the benzene washing tower, and obtaining rich oil at the bottom of the benzene washing tower;
secondly, mixing the washing oil and the coke oven gas in a tube pass of a closed tube type heat exchanger in a benzene washing tower, and controlling the temperature in the tube pass of the heat exchanger to be within the range of 22-26 ℃; the shell side of the heat exchanger is filled with heat absorption solution conveyed by an external solution pump, and the heat absorption solution exchanges heat with the mixture of the washing oil and the coke oven gas to control the temperature rise caused by absorbing the heat released by the benzene hydrocarbon in the coke oven gas by the washing oil;
thirdly, a pressure sensor, a vacuum pump and a liquid level meter are arranged on the shell tube side of the heat exchanger, the pressure sensor controls the starting and stopping of the vacuum pump so as to keep the micro vacuum of which the pressure in the shell side of the heat exchanger is in the range of 2000-3000 Pa, and the liquid level meter controls an external solution pump so as to ensure that the solution amount of which the total volume is 1/2-3/4 times is filled in the shell tube of the heat exchanger; an automatic exhaust valve is arranged at the top end of the shell pass of the heat exchanger, and an outlet of the automatic exhaust valve is communicated with an external steam collecting tank.
And fourthly, heating the rich oil, sending the rich oil into a debenzolization tower, treating the rich oil to obtain lean oil, and adding the lean oil into the wash oil for recycling to the benzene washing tower.
In order to further realize the purpose of the invention, the following technical scheme can be adopted:
in the benzene washing process for cooling and washing oil in the tower, the endothermic solution is one or a mixture of lithium bromide, lithium nitrate and lithium chloride;
in the benzene washing process of cooling and washing oil in the tower, the heat exchanger is a falling film absorber consisting of falling film tubes,
according to the benzene washing process for cooling washing oil in the tower, the heat absorption solution inlet and the heat absorption solution outlet of the shell side of the heat exchanger are respectively communicated with the outlet and the inlet of the low-temperature solution tank, the solution pump is installed on the outlet of the low-temperature solution tank, the steam collection tank is arranged above the low-temperature solution tank, and the cooling liquid outlet of the steam collection tank is communicated with the low-temperature solution tank.
The invention has the beneficial effects that:
1. the heat exchanger is arranged in the benzene washing tower, the coke oven gas is sprayed from the lower part and the washing oil is sprayed from the upper part and is mixed in the tube pass of the heat exchanger to absorb the benzene hydrocarbon in the coke oven gas, the shell pass of the heat exchanger is filled with the heat absorption solution, and the heat absorption solution exchanges heat with the mixture of the washing oil and the coke oven gas, so that the washing oil can be well controlled to be at a proper absorption temperature, and the washing oil is ensured to have a good crude benzene recovery rate.
2. The heat absorption solution in the shell pass of the heat exchanger is kept under a micro vacuum condition, so that water in the heat exchanger can form steam in time and take away heat, thereby improving the heat exchange effect, quickly taking away heat released by absorbing benzene hydrocarbon by the wash oil, and effectively controlling the temperature change range of the wash oil to be 22-26 ℃. And steam formed by the heat absorption solution is sent into the steam collecting tank through the automatic steam valve and then sent into the external low-temperature solution tank again through natural cooling to supplement the heat absorption solution.
3. Compared with the prior art that the recycle amount of the washing oil is increased to improve the recovery rate of the crude benzene, the process can improve the recovery rate of the crude benzene by at least 20 percent under the same consumption of the washing oil, and meanwhile, no harmful and toxic substances are newly added due to the adoption of a heat absorption solution recycling mode; the pressure sensor is adopted to control the intermittent start and stop of the vacuum pump, so that the increase of the overall energy consumption is small, and the treatment energy consumption required by the increase of the oil washing quantity is correspondingly saved.
Detailed Description
In order to make the objects, technical solutions and advantages of the embodiments of the present invention clearer, the technical solutions of the present invention will be clearly and completely described below with reference to the embodiments of the present invention, and it is obvious that the described embodiments are some embodiments of the present invention, but not all embodiments.
The embodiment discloses a benzene washing process for cooling washing oil in a tower, which comprises the following steps:
introducing the coke oven gas into the lower end of a benzene washing tower, spraying washing oil from the top of the benzene washing tower to absorb benzene substances in the coke oven gas, obtaining purified coke oven gas at the upper end of the benzene washing tower, and obtaining rich oil at the bottom of the benzene washing tower;
secondly, mixing the washing oil and the coke oven gas in a tube pass of a closed tube type heat exchanger in a benzene washing tower, and controlling the temperature in the tube pass of the heat exchanger to be within the range of 22-26 ℃; the shell side of the heat exchanger is filled with heat absorption solution conveyed by an external solution pump, and the heat absorption solution exchanges heat with the mixture of the washing oil and the coke oven gas to control the temperature rise caused by absorbing the heat released by the benzene hydrocarbon in the coke oven gas by the washing oil;
thirdly, a pressure sensor, a vacuum pump and a liquid level meter are arranged on the shell tube side of the heat exchanger, the pressure sensor controls the starting and stopping of the vacuum pump so as to keep the micro vacuum of which the pressure in the shell side of the heat exchanger is in the range of 2000-3000 Pa, and the liquid level meter controls an external solution pump so as to ensure that the solution amount of which the total volume is 1/2-3/4 times is filled in the shell tube of the heat exchanger; an automatic exhaust valve is arranged at the top end of the shell pass of the heat exchanger, and an outlet of the automatic exhaust valve is communicated with an external steam collecting tank.
And fourthly, heating the rich oil, sending the rich oil into a debenzolization tower, treating the rich oil to obtain lean oil, and adding the lean oil into the wash oil for recycling to the benzene washing tower.
Specifically, the benzene washing process for cooling washing oil in the tower provided by the invention has the advantages that the heat exchanger is arranged in the benzene washing tower, coke oven gas is sprayed from the lower part and the washing oil is sprayed from the upper part and is mixed in the tube pass of the heat exchanger to absorb the benzene hydrocarbon in the coke oven gas, the shell pass of the heat exchanger is filled with the heat absorption solution, and the heat absorption solution exchanges heat with the mixture of the washing oil and the coke oven gas, so that the temperature of the washing oil can be well controlled, and the good crude benzene recovery rate of the washing oil is ensured. The heat absorption solution in the shell pass of the heat exchanger is kept under the micro vacuum condition, so that water in the heat exchanger can form steam in time to take away heat, thereby improving the heat exchange effect, quickly taking away heat released by absorbing benzene hydrocarbon by the wash oil, and effectively controlling the temperature change range of the wash oil.
Further, the endothermic solution used in this embodiment is one or a mixture of a plurality of lithium bromide, lithium nitrate, and lithium chloride. During use, the heat absorption solution can be prepared by proportioning, mixing and stirring according to the components and characteristics of the coke oven gas and the content of the benzene hydrocarbon and the recovery requirement, the water weight ratio is generally controlled not to exceed 30 percent of the heat absorption solution, and the range of 20 to 25 percent is preferably adopted, so that the heat absorption solution can still have good fluidity after being evaporated.
Furthermore, the heat exchanger in this embodiment is a falling film absorber composed of falling film tubes. Because the heat absorption solution has certain corrosivity, the falling film tube absorber can ensure the use safety and the heat exchange effect, and has convenient maintenance and use and low investment cost.
Furthermore, in this embodiment, the heat absorbing solution inlet and outlet of the shell side of the heat exchanger are respectively communicated with the outlet and inlet of the cryogenic solution tank, the solution pump is installed at the outlet of the cryogenic solution tank, the vapor collection tank is disposed above the cryogenic solution tank, and the coolant outlet is communicated with the cryogenic solution tank. And steam formed by the heat absorption solution is sent into the steam collecting tank through the automatic steam valve and then sent into the external low-temperature solution tank again through natural cooling to supplement the heat absorption solution.
Compared with the prior art that the recycle amount of the washing oil is increased to improve the recovery rate of the crude benzene, the process can improve the recovery rate of the crude benzene by at least 20 percent under the same consumption of the washing oil, and meanwhile, no harmful and toxic substances are newly added due to the adoption of a heat absorption solution recycling mode; the pressure sensor is adopted to control the intermittent start and stop of the vacuum pump, so that the increase of the overall energy consumption is small, and the treatment energy consumption required by the increase of the oil washing quantity is correspondingly saved.
The technical contents not described in detail in the present invention are all known techniques.
Claims (3)
1. The benzene washing process for cooling washing oil in the tower is characterized by comprising the following steps of:
introducing the coke oven gas into the lower end of a benzene washing tower, spraying washing oil from the top of the benzene washing tower to absorb benzene substances in the coke oven gas, obtaining purified coke oven gas at the upper end of the benzene washing tower, and obtaining rich oil at the bottom of the benzene washing tower;
secondly, mixing the washing oil and the coke oven gas in a tube pass of a closed tube type heat exchanger in a benzene washing tower, and controlling the temperature in the tube pass of the heat exchanger to be within the range of 22-26 ℃; the shell side of the heat exchanger is filled with heat absorption solution conveyed by an external solution pump, and the heat absorption solution exchanges heat with the mixture of the washing oil and the coke oven gas to control the temperature rise caused by absorbing the heat released by the benzene hydrocarbon in the coke oven gas by the washing oil;
thirdly, a pressure sensor, a vacuum pump and a liquid level meter are arranged on the shell tube side of the heat exchanger, the pressure sensor controls the starting and stopping of the vacuum pump so as to keep the micro vacuum of which the pressure in the shell side of the heat exchanger is in the range of 2000-3000 Pa, and the liquid level meter controls an external solution pump so as to ensure that the solution amount of which the total volume is 1/2-3/4 times is filled in the shell tube of the heat exchanger; an automatic exhaust valve is arranged at the top end of the shell pass of the heat exchanger, and an outlet of the automatic exhaust valve is communicated with an external steam collecting tank;
heating the rich oil, sending the rich oil into a debenzolization tower, treating the rich oil to obtain lean oil, and adding the lean oil into the wash oil for recycling to the benzene washing tower;
the endothermic solution is one or a mixture of a plurality of lithium bromide, lithium nitrate and lithium chloride.
2. The benzene washing process of claim 1, wherein the heat exchanger is a falling film absorber comprising falling film tubes.
3. The benzene washing process for cooling washing oil in the tower according to claim 1, wherein the heat absorption solution inlet and outlet of the shell side of the heat exchanger are respectively communicated with the outlet and inlet of the cryogenic solution tank, the solution pump is installed on the outlet of the cryogenic solution tank, the vapor collection tank is arranged above the cryogenic solution tank, and the cooling liquid outlet of the vapor collection tank is communicated with the cryogenic solution tank.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201611206831.XA CN107057776B (en) | 2016-12-23 | 2016-12-23 | Benzene washing process for cooling washing oil in tower |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201611206831.XA CN107057776B (en) | 2016-12-23 | 2016-12-23 | Benzene washing process for cooling washing oil in tower |
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| CN107057776A CN107057776A (en) | 2017-08-18 |
| CN107057776B true CN107057776B (en) | 2020-10-23 |
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| CN201611206831.XA Active CN107057776B (en) | 2016-12-23 | 2016-12-23 | Benzene washing process for cooling washing oil in tower |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN109438161A (en) * | 2018-12-07 | 2019-03-08 | 山东齐鲁石化工程有限公司 | Residual neat recovering system in alkene production |
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Patent Citations (8)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN101016485A (en) * | 2007-03-13 | 2007-08-15 | 中冶焦耐工程技术有限公司 | Vacuum carbonate method coal gas desulfurization processes and apparatus thereof directly utilizing deserted coal gas residual heat as desorption heat source |
| CN201978659U (en) * | 2010-12-29 | 2011-09-21 | 北京国电龙源环保工程有限公司 | Overhead type smoke gas desulphurization absorption tower for smoke gas heat exchanger |
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