CN111253203A - Heat exchange optimization process for crude benzene distillation section - Google Patents
Heat exchange optimization process for crude benzene distillation section Download PDFInfo
- Publication number
- CN111253203A CN111253203A CN202010184796.6A CN202010184796A CN111253203A CN 111253203 A CN111253203 A CN 111253203A CN 202010184796 A CN202010184796 A CN 202010184796A CN 111253203 A CN111253203 A CN 111253203A
- Authority
- CN
- China
- Prior art keywords
- oil
- lean
- rich
- heat exchanger
- benzene
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 title claims abstract description 129
- 238000000034 method Methods 0.000 title claims abstract description 16
- 238000004821 distillation Methods 0.000 title claims abstract description 15
- 238000005457 optimization Methods 0.000 title claims abstract description 8
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 45
- 239000000203 mixture Substances 0.000 claims abstract description 17
- VEFXTGTZJOWDOF-UHFFFAOYSA-N benzene;hydrate Chemical compound O.C1=CC=CC=C1 VEFXTGTZJOWDOF-UHFFFAOYSA-N 0.000 claims abstract description 8
- 238000005406 washing Methods 0.000 claims description 12
- 238000009833 condensation Methods 0.000 claims description 5
- 230000005494 condensation Effects 0.000 claims description 5
- 238000001816 cooling Methods 0.000 claims description 3
- 230000000694 effects Effects 0.000 abstract description 10
- 238000010586 diagram Methods 0.000 description 2
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000004939 coking Methods 0.000 description 1
Images
Classifications
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C7/00—Purification; Separation; Use of additives
- C07C7/04—Purification; Separation; Use of additives by distillation
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Engineering & Computer Science (AREA)
- Analytical Chemistry (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Water Supply & Treatment (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The invention relates to the technical field of crude benzene distillation heat exchange, in particular to a heat exchange optimization process for a crude benzene distillation working section. The temperature of the mixture of oil gas and water vapor is reduced by circulating water at the temperature lower than 32 ℃ in a benzene-water heat exchanger, and the temperature of the hot lean oil is improved from the temperature reduction by heat exchange with rich oil at the temperature of about 70 ℃ to the temperature reduction by heat exchange with rich oil at the temperature of about 30 ℃; the heat transfer coefficient of the lean-rich heat exchanger is increased by changing the heat lean oil pump to the front of the lean-rich heat exchanger. The invention solves the problem of poor heat exchange effect of the mixture of oil gas and water vapor and rich oil at about 30 ℃ in the oil gas heat exchanger, and solves the problem that the quality and yield of crude benzene are influenced when the rich oil leaked from the oil gas heat exchanger enters the benzene-water mixture; the problem of poor heat exchange and temperature reduction effects of hot lean oil and rich oil at about 70 ℃ is solved; the problem of low heat transfer coefficient when the hot lean oil automatically flows into the lean rich oil heat exchanger is solved; the problem that the benzene content of lean oil is influenced when the lean oil enters the lean oil due to the leakage of the rich oil from the lean-rich oil heat exchanger is solved.
Description
Technical Field
The invention relates to the technical field of crude benzene distillation heat exchange, in particular to a heat exchange optimization process for a crude benzene distillation working section.
Background
The crude benzene distillation process flow of the coking plant at present is as follows:
the rich oil at about 30 ℃ from the benzene washing procedure firstly enters an oil-gas heat exchanger, exchanges heat with the mixture of oil gas and water vapor from the top of the benzene removal tower, then is heated to about 70 ℃, then enters a lean-rich oil heat exchanger, is heated to 150-160 ℃ by hot lean oil discharged from the bottom of the benzene removal tower, and then enters a tubular furnace.
The mixture of oil gas and water vapor with the temperature of 90-93 ℃ escaping from the top of the debenzolization tower enters an oil gas heat exchanger to exchange heat with rich oil, then enters a condensing cooler to be condensed and cooled by low-temperature water, and condensate enters an oil-water separator.
And the hot lean oil discharged from the bottom of the debenzolization tower flows to a lean-rich oil heat exchanger to exchange heat with rich oil, and then is cooled by circulating water and low-temperature water respectively by a lean oil first-stage cooler and a lean oil second-stage cooler by a hot lean oil pump, and then is recycled in the benzene washing process.
However, the problems of the heat exchange method are as follows:
1. the mixture of oil and gas and water in the oil-gas heat exchanger exchanges heat with rich oil at about 30 ℃ in the oil-gas heat exchanger, the heat exchange effect is poor, and if the oil-gas heat exchanger leaks, the rich oil is mixed into the mixture of benzene and water, and the benzene needs to be returned to the system again, so that the quality and the yield of crude benzene are influenced.
2. The hot lean oil exchanges heat with rich oil at about 70 ℃, the temperature reduction amplitude of the hot lean oil is small, the temperature is difficult to reach below 30 ℃ after the heat exchange of circulating water and low-temperature water, the benzene washing effect is poor, the hot lean oil automatically flows into a lean-rich heat exchanger, the heat transfer coefficient is low, and if the lean-rich heat exchanger leaks, the rich oil leaks into the lean oil due to high rich pressure, so that the benzene content of the lean oil is increased, the benzene washing effect is influenced, and the crude benzene yield is further influenced.
Disclosure of Invention
In order to solve the technical problem, the invention provides a heat exchange optimization process for a crude benzene distillation section. The problem of poor heat exchange effect of the mixture of oil gas and water vapor and rich oil at about 30 ℃ in the oil-gas heat exchanger is solved, and the problem that the quality and yield of crude benzene are influenced when the rich oil leaked from the oil-gas heat exchanger enters the benzene-water mixture is solved; the problem of poor heat exchange and temperature reduction effects of hot lean oil and rich oil at about 70 ℃ is solved; the problem of low heat transfer coefficient when the hot lean oil automatically flows into the lean rich oil heat exchanger is solved; the problem that the benzene content of lean oil is influenced when the lean oil enters the lean oil due to the leakage of the rich oil from the lean-rich oil heat exchanger is solved.
The specific technical scheme is as follows:
a heat exchange optimization process for a crude benzene distillation section is characterized by comprising the following steps: the mixture of oil gas and water vapor with the temperature of 90-93 ℃ escaping from the top of the debenzolization tower is cooled by circulating water with the temperature lower than 32 ℃ in a benzene-water heat exchanger and then enters a condensation cooler for condensation and cooling by low-temperature water, and the condensate enters an oil-water separator; the hot lean oil discharged from the bottom of the debenzolization tower is pressurized by a hot lean oil pump, enters a lean rich oil heat exchanger, is cooled by rich oil at about 30 ℃ from a benzene washing process, is cooled by circulating water and low-temperature water through a lean oil first-stage cooler and a lean oil second-stage cooler respectively, and then is recycled in the benzene washing process; the rich oil heated by the hot lean oil enters a tube furnace; the heat transfer coefficient of the lean-rich heat exchanger is increased by changing the heat lean oil pump to the front of the lean-rich heat exchanger.
Compared with the prior art, the invention has the following beneficial technical effects:
1. the mixture of oil gas and water vapor is cooled by circulating water at a temperature lower than 32 ℃ in a benzene-water heat exchanger, and the specific heat capacity of water is larger than that of rich oil, so that the heat exchange effect is better than that of the rich oil at a temperature of about 30 ℃.
2. The leakage of the oil-gas heat exchanger is high due to the high pressure of the circulating water, so that the circulating water enters the benzene-water mixture, the quality and the yield of crude benzene are not influenced, and water can be separated from benzene in an oil-water separator.
3. The heat exchange and temperature reduction effect of the hot lean oil and the rich oil at about 30 ℃ is better than that of the hot lean oil and the rich oil at about 70 ℃.
4. The heat transfer coefficient of the lean-rich heat exchanger is increased by changing the heat lean oil pump to the front of the lean-rich heat exchanger.
5. If the lean-rich heat exchanger leaks, the lean oil pressure is higher than the rich oil pressure, so that the lean oil enters the rich oil, and the benzene content of the lean oil cannot be influenced.
Drawings
FIG. 1 is a flow diagram of a prior art heat exchange process;
FIG. 2 is a flow chart of the heat exchange process after the crude benzene distillation section is improved and optimized.
Detailed Description
The present invention is described in detail below with reference to the drawings and the embodiments, but the scope of the present invention is not limited by the drawings and the embodiments.
FIG. 1 is a heat exchange process flow diagram of the prior art, and as shown in the figure, the crude benzene distillation process flow of the current coke-oven plant is as follows:
the rich oil at about 30 ℃ from the benzene washing procedure firstly enters an oil-gas heat exchanger, exchanges heat with the mixture of oil gas and water vapor from the top of the benzene removal tower, then is heated to about 70 ℃, then enters a lean-rich oil heat exchanger, is heated to 150-160 ℃ by hot lean oil discharged from the bottom of the benzene removal tower, and then enters a tubular furnace.
The mixture of oil gas and water vapor with the temperature of 90-93 ℃ escaping from the top of the debenzolization tower enters an oil gas heat exchanger to exchange heat with rich oil, then enters a condensing cooler to be condensed and cooled by low-temperature water, and condensate enters an oil-water separator.
And the hot lean oil discharged from the bottom of the debenzolization tower flows to a lean-rich oil heat exchanger to exchange heat with rich oil, and then is cooled by circulating water and low-temperature water respectively by a lean oil first-stage cooler and a lean oil second-stage cooler by a hot lean oil pump, and then is recycled in the benzene washing process.
FIG. 2 is a flow chart of a heat exchange process after the crude benzene distillation section is improved and optimized, as shown in the figure, the heat exchange process of the crude benzene distillation section is optimized after the improvement, the temperature of a mixture of oil gas and water vapor with the temperature of 90-93 ℃ escaping from the top of a debenzolization tower is reduced by circulating water with the temperature lower than 32 ℃ in a benzene-water heat exchanger, then the mixture enters a condenser cooler for condensation and cooling by low-temperature water, and condensate enters an oil-water separator; the hot lean oil discharged from the bottom of the debenzolization tower is pressurized by a hot lean oil pump, enters a lean rich oil heat exchanger, is cooled by rich oil at about 30 ℃ from a benzene washing process, is cooled by circulating water and low-temperature water through a lean oil first-stage cooler and a lean oil second-stage cooler respectively, and then is recycled in the benzene washing process; the rich oil heated by the hot lean oil enters a tube furnace; the heat transfer coefficient of the lean-rich heat exchanger is increased by changing the heat lean oil pump to the front of the lean-rich heat exchanger.
Claims (2)
1. A heat exchange optimization process for a crude benzene distillation section is characterized by comprising the following steps: the mixture of oil gas and water vapor with the temperature of 90-93 ℃ escaping from the top of the debenzolization tower is cooled by circulating water with the temperature lower than 32 ℃ in a benzene-water heat exchanger and then enters a condensation cooler for condensation and cooling by low-temperature water, and the condensate enters an oil-water separator; the hot lean oil discharged from the bottom of the debenzolization tower is pressurized by a hot lean oil pump, enters a lean rich oil heat exchanger, is cooled by rich oil at about 30 ℃ from a benzene washing process, is cooled by circulating water and low-temperature water through a lean oil first-stage cooler and a lean oil second-stage cooler respectively, and then is recycled in the benzene washing process; the rich oil heated by the hot lean oil enters a tube furnace.
2. The heat exchange optimization process of the crude benzene distillation section according to claim 1, which is characterized in that: and the heat lean oil pump is arranged in front of the lean-rich oil heat exchanger, so that the heat transfer coefficient of the lean-rich oil heat exchanger is increased.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202010184796.6A CN111253203A (en) | 2020-03-17 | 2020-03-17 | Heat exchange optimization process for crude benzene distillation section |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202010184796.6A CN111253203A (en) | 2020-03-17 | 2020-03-17 | Heat exchange optimization process for crude benzene distillation section |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN111253203A true CN111253203A (en) | 2020-06-09 |
Family
ID=70943200
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202010184796.6A Pending CN111253203A (en) | 2020-03-17 | 2020-03-17 | Heat exchange optimization process for crude benzene distillation section |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN111253203A (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113790626A (en) * | 2021-09-08 | 2021-12-14 | 山东博宇重工科技有限公司 | Lean oil cooling process |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| 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 |
| CN103589462A (en) * | 2013-11-21 | 2014-02-19 | 王光华 | Technological method for purifying coal oven gas and recovering chemical products |
| CN104403704A (en) * | 2014-11-21 | 2015-03-11 | 中冶焦耐工程技术有限公司 | Negative-pressure crude benzene distillation process and equipment heating washing oil by steam |
| CN108096999A (en) * | 2017-12-22 | 2018-06-01 | 中冶焦耐(大连)工程技术有限公司 | A kind of reboiler method negative pressure crude benzol distillation technique |
-
2020
- 2020-03-17 CN CN202010184796.6A patent/CN111253203A/en active Pending
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| 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 |
| CN103589462A (en) * | 2013-11-21 | 2014-02-19 | 王光华 | Technological method for purifying coal oven gas and recovering chemical products |
| CN104403704A (en) * | 2014-11-21 | 2015-03-11 | 中冶焦耐工程技术有限公司 | Negative-pressure crude benzene distillation process and equipment heating washing oil by steam |
| CN108096999A (en) * | 2017-12-22 | 2018-06-01 | 中冶焦耐(大连)工程技术有限公司 | A kind of reboiler method negative pressure crude benzol distillation technique |
Non-Patent Citations (1)
| Title |
|---|
| 盛军波主编: "《苯加氢操作技术》", 31 January 2014, 冶金工业出版社 * |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113790626A (en) * | 2021-09-08 | 2021-12-14 | 山东博宇重工科技有限公司 | Lean oil cooling process |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN101597517B (en) | Rich oil de-benzene process | |
| CN102336415B (en) | Tubular furnace negative pressure ammonia distillation process | |
| CN109355083B (en) | Process and system for extracting three-mixed fraction by reduced pressure distillation of tar | |
| CN108096999B (en) | Reboiler method negative pressure crude benzene distillation process | |
| CN105154144B (en) | A kind of negative pressure benzene removal device and de- benzene method | |
| CN107628923A (en) | A kind of negative pressure benzene removal system and method for rich oil half | |
| CN110804486B (en) | Method and system for regenerating waste lubricating oil | |
| CN111253203A (en) | Heat exchange optimization process for crude benzene distillation section | |
| CN103382404A (en) | New method for benzene elution of coke-oven gas | |
| CN206570285U (en) | A kind of coal oven dithio-gas crude benzene recovery device | |
| CN109423318B (en) | Coal tar deep processing technology for directly extracting industrial naphthalene by adding alkali after atmospheric and vacuum distillation | |
| CN116751613A (en) | Energy-saving negative pressure debenzolization process and system | |
| CN107890684A (en) | A kind of reboiler method negative pressure crude benzol Distallation systm | |
| CN114854461B (en) | Method for regenerating hot lean oil under negative pressure debenzolization process condition | |
| CN215250663U (en) | Negative pressure benzene removal system for preparing superheated steam through electric heating | |
| CN207130213U (en) | A kind of tar cooling and distilling apparatus | |
| CN113842852B (en) | Process and system for annual production of 20 ten thousand tons of methylamine | |
| CN212152190U (en) | Coal tar three-tower continuous deep processing system | |
| CN113201370A (en) | Negative pressure debenzolization process and system for preparing superheated steam through electric heating | |
| CN210495282U (en) | Four-tower distillation and membrane separation integrated system | |
| CN111349476A (en) | Method for improving cleaning effect of crude benzene washing benzene tower | |
| CN217323987U (en) | Two-tower type debenzolization system | |
| CN207734627U (en) | A kind of reboiler method negative pressure crude benzol Distallation systm | |
| CN219709430U (en) | Energy-saving negative pressure benzene removal system | |
| CN221788177U (en) | Energy-saving negative pressure crude benzene distillation device |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| RJ01 | Rejection of invention patent application after publication |
Application publication date: 20200609 |
|
| RJ01 | Rejection of invention patent application after publication |