CN103951542A - Apparatus for improving product quality during butane isomerization - Google Patents
Apparatus for improving product quality during butane isomerization Download PDFInfo
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- CN103951542A CN103951542A CN201410144446.1A CN201410144446A CN103951542A CN 103951542 A CN103951542 A CN 103951542A CN 201410144446 A CN201410144446 A CN 201410144446A CN 103951542 A CN103951542 A CN 103951542A
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Abstract
The invention discloses an apparatus for improving product quality during butane isomerization and belongs to the field of organic chemical industry. The apparatus comprises an aromatization reactor group, a light aromatic hydrocarbon separator group and a heavy aromatic hydrocarbon separator group which are successively serially connected by employing pipes. The heavy aromatic hydrocarbon separator group employs normal-pressure operation. Before modification is performed, the product color is light yellow, the heavy aromatic hydrocarbon tower top pressure is 0.15 MPa, the heavy aromatic hydrocarbon tower bottom temperature is 280 DEG C, the coal consumption amount is 75 t/d; and after modification is performed, the product color is pure white, the heavy aromatic hydrocarbon tower top pressure is 0, the heavy aromatic hydrocarbon tower bottom temperature is 220 DEG C, the coal consumption amount is 60 t/d, therefore the product quality is substantially improved. Also normal-pressure operation replaces original pressure operation in a heavy aromatic hydrocarbon tower, and therefore operation is relatively stable and easy to control. Energy consumption also is substantially reduced, energy is saved, and output value is improved.
Description
technical field:
The invention belongs to organic chemical industry field, specifically belong to the device that carbon four isomerization processes are improved the quality of products.
background technology:
Carbon four is butane, chemical formula is C4H10, comprise two kinds of isomerss: normal butane and Trimethylmethane, the mixed liquefied petroleum gas for carbon three and carbon four extracting from oil field gas and wet natural gas, then can obtain mixed c 4 through separation: the mixed gas of normal butane and Trimethylmethane.
Utilization for mixed c 4, wherein a kind ofly be exactly the isomerization to mixed c 4 and produce heavy aromatics and light aromatic hydrocarbons, and the economic benefit of light aromatic hydrocarbons is higher than heavy aromatics, but the light aromatic hydrocarbons extracting in equipment is in the past of low quality, product is with micro-yellow, heavy aromatics tower is also band press operation, and energy consumption is large, and operation easier is also high.
summary of the invention:
Therefore, the present invention has proposed in order to reduce energy consumption, raising product purity and operational stability the device that carbon four isomerization processes are improved the quality of products, comprise aromatization reactor group, light aromatic hydrocarbons separator group and heavy aromatics separator group, aromatization reactor group, light aromatic hydrocarbons separator group and heavy aromatics separator group use pipeline connected in series successively, and heavy aromatics separator group is operating as atmospheric operation.
Described aromatization reactor group comprises heavy aromatics water cooler, raw material reaction product interchanger, feed supplement reaction product interchanger, reaction feed process furnace and aromatization reactor, the cold flow matter outlet of heavy aromatics water cooler is connected with the cold flow matter inlet duct of raw material reaction product interchanger, the cold flow matter outlet of raw material reaction product interchanger is connected with the cold flow matter inlet duct of feed supplement reaction product interchanger, the cold flow matter outlet of feed supplement reaction product interchanger is connected with the inlet duct of reaction feed process furnace, the outlet of reaction feed process furnace is connected with the inlet duct of aromatization reactor, the hot-fluid matter inlet duct of the outlet of aromatization reactor and feed supplement reaction product interchanger is connected, the hot-fluid matter outlet of feed supplement reaction product interchanger is connected with the hot-fluid matter inlet duct of raw material reaction product interchanger, the outlet of raw material reaction product exchanger heat liquid is connected with charging surge tank pipeline.
Described light aromatic hydrocarbons separator group comprises charging surge tank, reaction product air-cooler, reaction product watercooler, reaction product vapor-liquid separation tank, rich gas compressor, stabilizer tower fresh feed pump, stabilizer tower, stablizes overhead air cooler, stablizes tower top watercooler, light aromatic hydrocarbons water cooler, stablize return tank of top of the tower and stable tower top reflux pump, charging surge tank, reaction product air-cooler, reaction product watercooler is connected with reaction product vapor-liquid separation tank successively pipeline, reaction product vapor-liquid separation tank deck is connected with rich gas compressor pipeline, at the bottom of reaction product vapor-liquid separation tank, be connected with stabilizer tower fresh feed pump pipeline, rich gas compressor is connected with stabilizer tower pipeline respectively with stabilizer tower fresh feed pump, stablizing tower top is connected with stabilizer tower static headspace gas water cooler pipeline, stablize overhead air cooler, stablize tower top watercooler, stablizing return tank of top of the tower is connected with stable tower top reflux pump successively pipeline, stablizing tower top reflux pump is connected with stabilizer tower pipeline, at the bottom of stabilizer tower, be connected with light aromatic hydrocarbons water cooler pipeline, light aromatic hydrocarbons water cooler is connected with heavy aromatics tower pipeline.
Described heavy aromatics separator group comprises heavy aromatics tower, heavy aromatics tower top water cooler, heavy aromatics return tank of top of the tower, heavy aromatics trim the top of column pump and heavy aromatics product pump; Heavy aromatics tower top is connected with heavy aromatics tower top water cooler pipeline, heavy aromatics tower top water cooler, heavy aromatics return tank of top of the tower and heavy aromatics trim the top of column pump successively pipeline are connected, heavy aromatics trim the top of column pump is connected with heavy aromatics tower pipeline, at the bottom of heavy aromatics tower, be connected with the hot-fluid matter inlet duct of heavy aromatics water cooler, the hot-fluid matter outlet of heavy aromatics water cooler is connected with heavy aromatics product pump pipeline.
Mixed c 4 from tank field is first vaporized through the incoming stock reaction product interchanger of heavy aromatics water cooler heat exchange and reaction product heat exchange, then continues heat exchange at feed supplement reaction product interchanger, enters the heating of reaction feed process furnace, enters aromatization reactor and reacts.
Reaction product enters charging surge tank successively after feed supplement reaction product interchanger, raw material product interchanger, through reaction product air-cooler and reaction product watercooler, enter reaction product vapor-liquid separation tank again and carry out vapor-liquid separation, reaction gaseous stream after the separation of reaction product vapor-liquid separation tank enters rich gas compressor supercharging, gives stabilizer tower ftercompction.
At the bottom of reaction product vapor-liquid separation tank tank, liquid phase stream is with entering stabilizer tower after the pressurization of stabilizer tower fresh feed pump, stabilizer tower gas phase is first through stablizing overhead air cooler and the condensation of stable tower top watercooler, phlegma enters stabilizer tower return tank, a phlegma part enters stablizes tower top reflux pump as stablizing trim the top of column, a part is when product extraction device, and the liquid phase in stabilizer tower is from entering heavy aromatics tower after light aromatic hydrocarbons cooler heat exchangers at the bottom of tower.
At the bottom of stabilizer tower, liquid phase enters heavy aromatics tower to carry out weight component separated after cooling, the light component of tower top is through the condensation of heavy aromatics overhead condenser, at the bottom of entering heavy aromatics return tank of top of the tower tank, liquid phase is after heavy aromatics tower return tank boosts, a part is as trim the top of column, the defective lighter hydrocarbons of another part enter reaction product vapor-liquid separation tank, and at the bottom of heavy aromatics tower tower, heavy aromatics passes through heavy aromatics product pump carrying device through the heat exchange of heavy aromatics water cooler.
Before improvement, the micro-Huang of product colour, heavy aromatics tower top pressure is 0.15Mpa, heavy aromatics column bottom temperature is 280 ℃, and consumption of coal is 75t/d, after improvement, product colour is pure white, and heavy aromatics tower top pressure is 0, and heavy aromatics column bottom temperature is 220 ℃, consumption of coal is 60t/d, and quality product significantly improves, and heavy aromatics tower changes atmospheric operation into by original band press operation simultaneously, more stable easily control during operation, energy consumption also obviously reduces, and save energy improves the output value.
accompanying drawing explanation:
Fig. 1 is the device connection diagram that carbon four isomerization processes are improved the quality of products.
In figure: heavy aromatics water cooler 1, raw material reaction product interchanger 2, feed supplement reaction product interchanger 3, reaction feed process furnace 4, aromatization reactor 5, charging surge tank 6, reaction product air-cooler 7, reaction product watercooler 8, reaction product vapor-liquid separation tank 9, rich gas compressor 10, stabilizer tower fresh feed pump 11, stabilizer tower 12, stablize overhead air cooler 13, stablize tower top watercooler 14, light aromatic hydrocarbons water cooler 15, stablize return tank of top of the tower 16, stablize tower top reflux pump 17, heavy aromatics tower 18, heavy aromatics tower top water cooler 19, heavy aromatics return tank of top of the tower 20, heavy aromatics trim the top of column pump 21, heavy aromatics product pump 22.
embodiment:
Please refer to the device that carbon four isomerization processes are as shown in Figure 1 improved the quality of products, comprise aromatization reactor group, light aromatic hydrocarbons separator group and heavy aromatics separator group, aromatization reactor group, light aromatic hydrocarbons separator group and heavy aromatics separator group use pipeline connected in series successively, and heavy aromatics separator group is operating as atmospheric operation.
Described aromatization reactor group comprises heavy aromatics water cooler 1, raw material reaction product interchanger 2, feed supplement reaction product interchanger 3, reaction feed process furnace 4 and aromatization reactor 5, the cold flow matter outlet of heavy aromatics water cooler 1 is connected with the cold flow matter inlet duct of raw material reaction product interchanger 2, the cold flow matter outlet of raw material reaction product interchanger 2 is connected with the cold flow matter inlet duct of feed supplement reaction product interchanger 3, the cold flow matter outlet of feed supplement reaction product interchanger 3 is connected with the inlet duct of reaction feed process furnace 4, the outlet of reaction feed process furnace 4 is connected with the inlet duct of aromatization reactor 5, the hot-fluid matter inlet duct of the outlet of aromatization reactor 5 and feed supplement reaction product interchanger 3 is connected, the hot-fluid matter outlet of feed supplement reaction product interchanger 3 is connected with the hot-fluid matter inlet duct of raw material reaction product interchanger 2, the 2 hot-fluid matter outlets of raw material reaction product interchanger are connected with charging surge tank 6 pipelines.
Described light aromatic hydrocarbons separator group comprises charging surge tank 6, reaction product air-cooler 7, reaction product watercooler 8, reaction product vapor-liquid separation tank 9, rich gas compressor 10, stabilizer tower fresh feed pump 11, stabilizer tower 12, stablizes overhead air cooler 13, stablizes tower top watercooler 14, light aromatic hydrocarbons water cooler 15, stablize return tank of top of the tower 16 and stable tower top reflux pump 17, charging surge tank 6, reaction product air-cooler 7, reaction product watercooler 8 is connected with reaction product vapor-liquid separation tank 9 successively pipeline, reaction product vapor-liquid separation tank 9 tops are connected with rich gas compressor 10 pipelines, 9 ends of reaction product vapor-liquid separation tank, are connected with stabilizer tower fresh feed pump 11 pipelines, rich gas compressor 10 is connected with stabilizer tower 12 pipelines respectively with stabilizer tower fresh feed pump 11, stabilizer tower 12 tops are connected with stable overhead air cooler 13 pipelines, stablize overhead air cooler 13, stablize tower top watercooler 14, stablizing return tank of top of the tower 16 is connected with stable tower top reflux pump 17 successively pipeline, stablizing tower top reflux pump 17 is connected with stabilizer tower 12 pipelines, 12 ends of stabilizer tower, are connected with light aromatic hydrocarbons water cooler 15 pipelines, light aromatic hydrocarbons water cooler 15 is connected with heavy aromatics tower 18 pipelines.
Described heavy aromatics separator group comprises heavy aromatics tower 18, heavy aromatics tower top water cooler 19, heavy aromatics return tank of top of the tower 20, heavy aromatics trim the top of column pump 21 and heavy aromatics product pump 22; Heavy aromatics tower 18 tops are connected with heavy aromatics tower top water cooler 19 pipelines, heavy aromatics tower top water cooler 19, heavy aromatics return tank of top of the tower 20 and heavy aromatics trim the top of column pump 21 successively pipeline are connected, heavy aromatics trim the top of column pump 21 is connected with heavy aromatics tower 18 pipelines, the hot-fluid matter inlet duct of 18 ends of heavy aromatics tower and heavy aromatics water cooler 1 is connected, and the hot-fluid matter outlet of heavy aromatics water cooler 1 is connected with heavy aromatics product pump 22 pipelines.
Mixed c 4 from tank field is first vaporized through the incoming stock reaction product interchanger of heavy aromatics water cooler heat exchange and reaction product heat exchange, then continues heat exchange at feed supplement reaction product interchanger, enters the heating of reaction feed process furnace, enters aromatization reactor and reacts.
Reaction product enters charging surge tank successively after feed supplement reaction product interchanger, raw material product interchanger, through reaction product air-cooler and reaction product watercooler, enter reaction product vapor-liquid separation tank again and carry out vapor-liquid separation, reaction gaseous stream after the separation of reaction product vapor-liquid separation tank enters rich gas compressor supercharging, gives stabilizer tower ftercompction.
At the bottom of reaction product vapor-liquid separation tank tank, liquid phase stream is with entering stabilizer tower after the pressurization of stabilizer tower fresh feed pump, stabilizer tower gas phase is first through stablizing overhead air cooler and the condensation of stable tower top watercooler, phlegma enters stabilizer tower return tank, a phlegma part enters stablizes tower top reflux pump as stablizing trim the top of column, a part is when product extraction device, and the liquid phase in stabilizer tower is from entering heavy aromatics tower after light aromatic hydrocarbons cooler heat exchangers at the bottom of tower.
At the bottom of stabilizer tower, liquid phase enters heavy aromatics tower to carry out weight component separated after cooling, the light component of tower top is through the condensation of heavy aromatics overhead condenser, at the bottom of entering heavy aromatics return tank of top of the tower tank, liquid phase is after heavy aromatics tower return tank boosts, a part is as trim the top of column, the defective lighter hydrocarbons of another part enter reaction product vapor-liquid separation tank, and at the bottom of heavy aromatics tower tower, heavy aromatics passes through heavy aromatics product pump carrying device through the heat exchange of heavy aromatics water cooler.
Before improvement, the micro-Huang of product colour, heavy aromatics tower top pressure is 0.15Mpa, heavy aromatics column bottom temperature is 280 ℃, and consumption of coal is 75t/d, after improvement, product colour is pure white, and heavy aromatics tower top pressure is 0, and heavy aromatics column bottom temperature is 220 ℃, consumption of coal is 60t/d, and quality product significantly improves, and heavy aromatics tower changes atmospheric operation into by original band press operation simultaneously, more stable easily control during operation, energy consumption also obviously reduces, and save energy improves the output value.
Claims (4)
1. the device that carbon four isomerization processes are improved the quality of products, it is characterized in that: comprise aromatization reactor group, light aromatic hydrocarbons separator group and heavy aromatics separator group, aromatization reactor group, light aromatic hydrocarbons separator group and heavy aromatics separator group use pipeline connected in series successively, and heavy aromatics separator group is operating as atmospheric operation.
2. the device that carbon four isomerization processes as claimed in claim 1 are improved the quality of products, is characterized in that: described aromatization reactor group comprises heavy aromatics water cooler (1), raw material reaction product interchanger (2), feed supplement reaction product interchanger (3), reaction feed process furnace (4) and aromatization reactor (5), the cold flow matter outlet of heavy aromatics water cooler (1) is connected with the cold flow matter inlet duct of raw material reaction product interchanger (2), the cold flow matter outlet of raw material reaction product interchanger (2) is connected with the cold flow matter inlet duct of feed supplement reaction product interchanger (3), the cold flow matter outlet of feed supplement reaction product interchanger (3) is connected with the inlet duct of reaction feed process furnace (4), the outlet of reaction feed process furnace (4) is connected with the inlet duct of aromatization reactor (5), the hot-fluid matter inlet duct of the outlet of aromatization reactor (5) and feed supplement reaction product interchanger (3) is connected, the hot-fluid matter outlet of feed supplement reaction product interchanger (3) is connected with the hot-fluid matter inlet duct of raw material reaction product interchanger (2), the outlet of raw material reaction product interchanger (2) hot-fluid matter is connected with charging surge tank (6) pipeline.
3. the device that carbon four isomerization processes as claimed in claim 1 are improved the quality of products, is characterized in that: described light aromatic hydrocarbons separator group comprises charging surge tank (6), reaction product air-cooler (7), reaction product watercooler (8), reaction product vapor-liquid separation tank (9), rich gas compressor (10), stabilizer tower fresh feed pump (11), stabilizer tower (12), stablizes overhead air cooler (13), stablizes tower top watercooler (14), light aromatic hydrocarbons water cooler (15), stablize return tank of top of the tower (16) and stable tower top reflux pump (17), charging surge tank (6), reaction product air-cooler (7), reaction product watercooler (8) is connected with reaction product vapor-liquid separation tank (9) successively pipeline, reaction product vapor-liquid separation tank (9) top is connected with rich gas compressor (10) pipeline, reaction product vapor-liquid separation tank (9) end, is connected with stabilizer tower fresh feed pump (11) pipeline, rich gas compressor (10) is connected with stabilizer tower (12) pipeline respectively with stabilizer tower fresh feed pump (11), stabilizer tower (12) top is connected with stable overhead air cooler (13) pipeline, stablize overhead air cooler (13), stablize tower top watercooler (14), stablizing return tank of top of the tower (16) is connected with stable tower top reflux pump (17) successively pipeline, stablizing tower top reflux pump (17) is connected with stabilizer tower (12) pipeline, stabilizer tower (12) end, is connected with light aromatic hydrocarbons water cooler (15) pipeline, light aromatic hydrocarbons water cooler (15) is connected with heavy aromatics tower (18) pipeline.
4. the device that carbon four isomerization processes as claimed in claim 1 are improved the quality of products, is characterized in that: described heavy aromatics separator group comprises heavy aromatics tower (18), heavy aromatics tower top water cooler (19), heavy aromatics return tank of top of the tower (20), heavy aromatics trim the top of column pump (21) and heavy aromatics product pump (22); Heavy aromatics tower (18) top is connected with heavy aromatics tower top water cooler (19) pipeline, heavy aromatics tower top water cooler (19), heavy aromatics return tank of top of the tower (20) and heavy aromatics trim the top of column pump (21) successively pipeline are connected, heavy aromatics trim the top of column pump (21) is connected with heavy aromatics tower (18) pipeline, the hot-fluid matter inlet duct of heavy aromatics tower (18) end and heavy aromatics water cooler (1) is connected, and the hot-fluid matter outlet of heavy aromatics water cooler (1) is connected with heavy aromatics product pump (22) pipeline.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201410144446.1A CN103951542A (en) | 2014-04-11 | 2014-04-11 | Apparatus for improving product quality during butane isomerization |
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| Application Number | Priority Date | Filing Date | Title |
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| CN201410144446.1A CN103951542A (en) | 2014-04-11 | 2014-04-11 | Apparatus for improving product quality during butane isomerization |
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Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102190546A (en) * | 2010-03-03 | 2011-09-21 | 中国石油化工股份有限公司 | Method for preparing propylene and aromatic hydrocarbon by virtue of conversion of methanol |
| CN103509600A (en) * | 2012-06-21 | 2014-01-15 | 中国石油天然气股份有限公司 | Method for producing high-octane gasoline blending component by mixed carbon four-hydrocarbon aromatization |
| CN203782055U (en) * | 2014-04-11 | 2014-08-20 | 宁夏金裕海化工有限公司 | Device for improving quality of product in C4 isomerization process |
| CN203782104U (en) * | 2014-04-10 | 2014-08-20 | 宁夏金裕海化工有限公司 | Device for improving yield of products in C4 isomerization process |
-
2014
- 2014-04-11 CN CN201410144446.1A patent/CN103951542A/en active Pending
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102190546A (en) * | 2010-03-03 | 2011-09-21 | 中国石油化工股份有限公司 | Method for preparing propylene and aromatic hydrocarbon by virtue of conversion of methanol |
| CN103509600A (en) * | 2012-06-21 | 2014-01-15 | 中国石油天然气股份有限公司 | Method for producing high-octane gasoline blending component by mixed carbon four-hydrocarbon aromatization |
| CN203782104U (en) * | 2014-04-10 | 2014-08-20 | 宁夏金裕海化工有限公司 | Device for improving yield of products in C4 isomerization process |
| CN203782055U (en) * | 2014-04-11 | 2014-08-20 | 宁夏金裕海化工有限公司 | Device for improving quality of product in C4 isomerization process |
Non-Patent Citations (1)
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| 黄彦科等: "碳四烃芳构化产物的综合利用研究", 《石油炼制与化工》 * |
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Application publication date: 20140730 |