CN104548862A - Energy-saving method for styrene plant dehydrogenation tail gas treatment system - Google Patents
Energy-saving method for styrene plant dehydrogenation tail gas treatment system Download PDFInfo
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- CN104548862A CN104548862A CN201510061293.9A CN201510061293A CN104548862A CN 104548862 A CN104548862 A CN 104548862A CN 201510061293 A CN201510061293 A CN 201510061293A CN 104548862 A CN104548862 A CN 104548862A
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Abstract
The invention relates to an energy-saving method for a styrene plant dehydrogenation tail gas treatment system. The problems that the consumption of public works is high and the energy consumption of the device is high in the prior art are mainly solved. According to the energy-saving method for the styrene plant dehydrogenation tail gas treatment system disclosed by the invention, dehydrogenation tail gas materials are cooled into a tail gas chiller and are fed into a gas-liquid separator, liquid-phase materials condensed by the gas-liquid separator are discharged to be fed to a subsequent section for treatment, non-condensable gas materials on the top of the gas-liquid separator are mixed and cooled with supplemented cooling water so as to enter a tail gas compressor, the gas materials are compressed and boosted by virtue of a tail gas compressor, the discharged gas phase materials are cooled in the tail gas cooler, and the cooled materials are fed into the subsequent section for treatment. According to the technical scheme, the problems are solved, and the method can be used in styrene plant dehydrogenation tail gas treatment.
Description
Technical field
The present invention relates to a kind of power-economizing method of styrene device dehydrogenated tail gas treatment system.
Background technology
Styrene SM is synthetic resin, ion exchange resin and elastomeric important monomer, can be used to produce butadiene-styrene rubber, polystyrene, foamed polystyrene, also can manufacture the engineering plastics of multiple different purposes from other monomer copolymerizations.Production method mainly contains ethylbenzene catalytic dehydrogenation method and ethylbenzene conjugated oxidation two kinds, wherein more than 90% adopts ethylbenzene catalytic dehydrogenation method to manufacture.In producing phenyl ethylene by ethyl benzene catalytic dehydrogenation process, generation hydrogen, ethylbenzene, cinnamic tail gas need to be recycled.
The dehydrogenation tail gas absorption method of license notification number CN1182090C preparing styrene from ethylbenzene adopts and improves compressor delivery pressure, and the technical scheme reducing absorption tower feeding temperature improves the rate of recovery of aromatic hydrocarbons.Patent application publication CN102266704A styrene device thick hydrogen supercharging recovery method adopts the arene content in four sections of compression process reduction styrene device dehydrogenated tail gas.License notification number CN203704544U styrene device tail gas second dehydration and degreasing unit adopt the process equipment of heat exchanger, separator and absorption tower composition to reduce water content in tail gas to improve the service life of compressor.Cracking gas compressing process in license notification number CN1131189C ethylene production comprises five sections of compressions and two intersegmental direct cooling towers, reduce compressor inlet temperature to improve the disposal ability of compressor, energy-saving and cost-reducing, but the method cannot be used for styrene device.
It is large all to there is the utility consumption such as steam, recirculated water in prior art, the problem that plant energy consumption is high.
The present invention solves the problems referred to above targetedly.
Summary of the invention
Technical problem to be solved by this invention is that in prior art, utility consumption is large, and the problem that plant energy consumption is high, provides a kind of power-economizing method of new styrene device dehydrogenated tail gas treatment system.The method is used for, in the process of styrene device dehydrogenated tail gas, having utility consumption little, the advantage that plant energy consumption is low.
For solving the problem, the technical solution used in the present invention is as follows: a kind of power-economizing method of styrene device dehydrogenated tail gas treatment system, dehydrogenated tail gas material sends into gas-liquid separator after sending into the cooling of tail gas cryogenic device, the liquid phase material that gas-liquid separator condensation is got off is discharged and is sent follow-up workshop section to process, tail-gas compressor is entered after the incoagulable gas material at gas-liquid separator top and supplementary cooling water combination cooling, through tail-gas compressor compression boosting, the gaseous phase materials of discharging enters exhaust gas cooler and cools, and the process of follow-up workshop section sent into by the material after cooling.
In technique scheme, preferably, described tail gas cryogenic device chilled water is as cold medium, and the operating temperature of chilled water is-15 ~ 25 DEG C.
In technique scheme, preferably, described tail-gas compressor is driven by bleeder steam turbine, and steam turbine input high steam, discharges low-pressure steam.
In technique scheme, preferably, described dehydrogenated tail gas material comprises hydrogen, ethylbenzene, styrene, light component, heavy constituent, water, and inlet temperature is 20 ~ 55 DEG C, and inlet pressure is 10 ~ 80kPaA.
In technique scheme, preferably, the operating temperature of described tail gas cryogenic device is-15 ~ 55 DEG C, and operating pressure is 10 ~ 80kPaA; The operating temperature of gas-liquid separator is-15 ~ 55 DEG C, and operating pressure is 10 ~ 80kPaA; The operating temperature of exhaust gas cooler is 55 ~ 125 DEG C, and operating pressure is 100 ~ 300kPaA.
In technique scheme, more preferably, the operating temperature of described tail gas cryogenic device is 5 ~ 35 DEG C, and operating pressure is 20 ~ 60kPaA; The operating temperature of gas-liquid separator is 5 ~ 35 DEG C, and operating pressure is 20 ~ 60kPaA; The operating temperature of exhaust gas cooler is 75 ~ 95 DEG C, and operating pressure is 200 ~ 260kPaA.
In technique scheme, preferably, the scope of described tail-gas compressor compression ratio is between 2 ~ 10.
In technique scheme, preferably, the scope of described incoagulable gas material and supplementary cooling water mass ratio is between 4 ~ 20:1.
The present invention relates to a kind of energy saving technique of styrene device dehydrogenated tail gas treatment system, dehydrogenated tail gas through circulating water is sent into the tail gas cryogenic device chilled water that the present invention increases newly cools further, condensation, the liquid phase that condensation is got off is discharged through gas-liquid separator, after incoagulable gas injects and supplements cooling water, enter tail-gas compressor, compressed boosting is discharged, and the gas phase of discharge send follow-up workshop section after exhaust gas cooler cools.Adopt method of the present invention, decrease the consumption of the public work such as steam, recirculated water, reduce the power of tail-gas compressor and the thermic load of exhaust gas cooler, the energy consumption of styrene device declines 3.23 ~ 3.95 kilograms and marks oil/ton styrene, achieves good technique effect.
Accompanying drawing explanation
Fig. 1 is the schematic flow sheet of the method for the invention.
1 is tail gas cryogenic device; 2 is gas-liquid separator; 3 is tail-gas compressor; 4 is steam turbine; 5 is exhaust gas cooler; 6 is gaseous phase materials and the mixed material of supplementary cooling water; 7 gaseous phase materials of discharging for tail-gas compressor; 8 is through the cooled material of exhaust gas cooler; 9 is dehydrogenated tail gas material; 10 is through the cooled gas-liquid mixture of tail gas cryogenic device; 11 is high steam; 12 for supplementing cooling water; 13 is liquid phase material; 14 is low-pressure steam.
Below by embodiment, the invention will be further elaborated, but be not limited only to the present embodiment.
Detailed description of the invention
[embodiment 1]
The present invention adopts the energy saving technique of styrene device dehydrogenated tail gas treatment system, and the production scale of Styrene Process is 60,000 tons/year, dehydrogenated tail gas composed as follows:
| Title | Hydrogen | Ethylbenzene | Styrene | Light component | Heavy constituent | Water | Add up to |
| % (weight) | 9.68 | 20.12 | 43.26 | 6.18 | 6.27 | 14.49 | 100.00 |
The inlet temperature of dehydrogenated tail gas is 40 DEG C, and inlet pressure is 60kPaA; The operating temperature of tail gas cryogenic device is 5 DEG C, and operating pressure is 60kPaA; The operating temperature of gas-liquid separator is 5 DEG C, and operating pressure is 60kPaA; The operating temperature of exhaust gas cooler is 40 DEG C, and operating pressure is 260kPaA; Tail-gas compressor compression ratio is 4.3, and chilled water operating temperature is-5 DEG C, and incoagulable gas and supplementary cooling water mass ratio are 10:1; Owing to adopting energy saving technique of the present invention, the consumption of input high steam reduces 1.30 tons/hour, exhaust gas cooler thermic load declines and makes recirculated water consumption reduce 90 tons/hour, supplementary cooling-water consumption reduces 125 kgs/hr, chilled water consumption increases by 36 tons/hour, discharge low-pressure steam consumption and increase by 1.30 tons/hour, styrene device energy consumption declines 1.55 kilograms and marks oil/ton styrene thus.
[embodiment 2]
According to the condition described in embodiment 1 and step, only the production scale of styrene device changes 200,000 tons/year into; Owing to adopting energy saving technique of the present invention, the consumption of input high steam reduces 4.68 tons/hour, exhaust gas cooler thermic load declines and makes recirculated water consumption reduce 300 tons/hour, supplementary cooling-water consumption reduces 418 kgs/hr, chilled water consumption increases by 119 tons/hour, discharge low-pressure steam consumption and increase by 4.68 tons/hour, styrene device energy consumption declines 1.71 kilograms and marks oil/ton styrene thus.
[embodiment 3]
According to the condition described in embodiment 1 and step, only the production scale of styrene device changes 280,000 tons/year into; Owing to adopting energy saving technique of the present invention, the consumption of input high steam reduces 6.72 tons/hour, exhaust gas cooler thermic load declines and makes recirculated water consumption reduce 420 tons/hour, supplementary cooling-water consumption reduces 585 kgs/hr, chilled water consumption increases by 167 tons/hour, discharge low-pressure steam consumption and increase by 6.72 tons/hour, styrene device energy consumption declines 1.80 kilograms and marks oil/ton styrene thus.
[embodiment 4]
According to the condition described in embodiment 1 and step, only the production scale of styrene device changes 600,000 tons/year into; Owing to adopting energy saving technique of the present invention, the consumption of input high steam reduces 15.84 tons/hour, exhaust gas cooler thermic load declines and makes recirculated water consumption reduce 900 tons/hour, supplementary cooling-water consumption reduces 1253 kgs/hr, chilled water consumption increases by 358 tons/hour, discharge low-pressure steam consumption and increase by 15.84 tons/hour, styrene device energy consumption declines 1.89 kilograms and marks oil/ton styrene thus.
[embodiment 5]
According to the condition described in embodiment 2 and step, the production scale of styrene device is still 200,000 tons/year, and only operating condition changes; The inlet temperature of dehydrogenated tail gas is 20 DEG C, and inlet pressure is 10kPaA; The operating temperature of tail gas cryogenic device is-15 DEG C, and operating pressure is 10kPaA; The operating temperature of gas-liquid separator is-15 DEG C, and operating pressure is 10kPaA; The operating temperature of exhaust gas cooler is 55 DEG C, and operating pressure is 100kPaA; Tail-gas compressor compression ratio is 10.0, and chilled water operating temperature is-15 DEG C, and incoagulable gas and supplementary cooling water mass ratio are 4:1; Owing to adopting energy saving technique of the present invention, the consumption of input high steam reduces 4.07 tons/hour, exhaust gas cooler thermic load declines and makes recirculated water consumption reduce 261 tons/hour, supplementary cooling-water consumption reduces 363 kgs/hr, chilled water consumption increases by 104 tons/hour, discharge low-pressure steam consumption and increase by 4.07 tons/hour, styrene device energy consumption declines 1.60 kilograms and marks oil/ton styrene thus.
[embodiment 6]
According to the condition described in embodiment 2 and step, the production scale of styrene device is still 200,000 tons/year, and only operating condition changes; The inlet temperature of dehydrogenated tail gas is 55 DEG C, and inlet pressure is 80kPaA; The operating temperature of tail gas cryogenic device is 55 DEG C, and operating pressure is 80kPaA; The operating temperature of gas-liquid separator is 55 DEG C, and operating pressure is 80kPaA; The operating temperature of exhaust gas cooler is 125 DEG C, and operating pressure is 300kPaA; Tail-gas compressor compression ratio is 3.8, and chilled water operating temperature is 25 DEG C, and incoagulable gas and supplementary cooling water mass ratio are 20:1; Owing to adopting energy saving technique of the present invention, the consumption of input high steam reduces 4.12 tons/hour, exhaust gas cooler thermic load declines and makes recirculated water consumption reduce 264 tons/hour, supplementary cooling-water consumption reduces 368 kgs/hr, chilled water consumption increases by 105 tons/hour, discharge low-pressure steam consumption and increase by 4.12 tons/hour, styrene device energy consumption declines 1.64 kilograms and marks oil/ton styrene thus.
[embodiment 7]
According to the condition described in embodiment 2 and step, the production scale of styrene device is still 200,000 tons/year, and only operating condition changes; The inlet temperature of dehydrogenated tail gas is 45 DEG C, and inlet pressure is 80kPaA; The operating temperature of tail gas cryogenic device is 5 DEG C, and operating pressure is 80kPaA; The operating temperature of gas-liquid separator is 5 DEG C, and operating pressure is 80kPaA; The operating temperature of exhaust gas cooler is 70 DEG C, and operating pressure is 160kPaA; Tail-gas compressor compression ratio is 2.0, and chilled water operating temperature is-5 DEG C, and incoagulable gas and supplementary cooling water mass ratio are 16:1; Owing to adopting energy saving technique of the present invention, the consumption of input high steam reduces 4.59 tons/hour, exhaust gas cooler thermic load declines and makes recirculated water consumption reduce 294 tons/hour, supplementary cooling-water consumption reduces 409 kgs/hr, chilled water consumption increases by 117 tons/hour, discharge low-pressure steam consumption and increase by 4.59 tons/hour, styrene device energy consumption declines 1.69 kilograms and marks oil/ton styrene thus.
Claims (8)
1. the power-economizing method of a styrene device dehydrogenated tail gas treatment system, dehydrogenated tail gas material sends into gas-liquid separator after sending into the cooling of tail gas cryogenic device, the liquid phase material that gas-liquid separator condensation is got off is discharged and is sent follow-up workshop section to process, tail-gas compressor is entered after the incoagulable gas material at gas-liquid separator top and supplementary cooling water combination cooling, through tail-gas compressor compression boosting, the gaseous phase materials of discharging enters exhaust gas cooler and cools, and the process of follow-up workshop section sent into by the material after cooling.
2. the power-economizing method of styrene device dehydrogenated tail gas treatment system according to claim 1, it is characterized in that described tail gas cryogenic device chilled water is as cold medium, the operating temperature of chilled water is-15 ~ 25 DEG C.
3. the power-economizing method of styrene device dehydrogenated tail gas treatment system according to claim 1, is characterized in that described tail-gas compressor is driven by bleeder steam turbine, and steam turbine input high steam, discharges low-pressure steam.
4. the power-economizing method of styrene device dehydrogenated tail gas treatment system according to claim 1, it is characterized in that described dehydrogenated tail gas material comprises hydrogen, ethylbenzene, styrene, light component, heavy constituent, water, inlet temperature is 20 ~ 55 DEG C, and inlet pressure is 10 ~ 80kPaA.
5. the power-economizing method of styrene device dehydrogenated tail gas treatment system according to claim 1, it is characterized in that the operating temperature of described tail gas cryogenic device is-15 ~ 55 DEG C, operating pressure is 10 ~ 80kPaA; The operating temperature of gas-liquid separator is-15 ~ 55 DEG C, and operating pressure is 10 ~ 80kPaA; The operating temperature of exhaust gas cooler is 55 ~ 125 DEG C, and operating pressure is 100 ~ 300kPaA.
6. the power-economizing method of styrene device dehydrogenated tail gas treatment system according to claim 5, it is characterized in that the operating temperature of described tail gas cryogenic device is 5 ~ 35 DEG C, operating pressure is 20 ~ 60kPaA; The operating temperature of gas-liquid separator is 5 ~ 35 DEG C, and operating pressure is 20 ~ 60kPaA; The operating temperature of exhaust gas cooler is 75 ~ 95 DEG C, and operating pressure is 200 ~ 260kPaA.
7. the power-economizing method of styrene device dehydrogenated tail gas treatment system according to claim 1, is characterized in that the scope of described tail-gas compressor compression ratio is between 2 ~ 10.
8. the power-economizing method of styrene device dehydrogenated tail gas treatment system according to claim 1, is characterized in that the scope of described incoagulable gas material and supplementary cooling water mass ratio is between 4 ~ 20:1.
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106693436A (en) * | 2015-11-13 | 2017-05-24 | 中国石化工程建设有限公司 | Tail gas treatment system for storage tank type material storage facilities |
| CN111036025A (en) * | 2018-10-11 | 2020-04-21 | 中国石化工程建设有限公司 | Method and system for treating styrene pressure relief exhaust gas |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1962029A (en) * | 2005-11-11 | 2007-05-16 | 中国石油化工股份有限公司 | Method for separating dehydrogenated tail gas |
| CN102266704A (en) * | 2010-06-04 | 2011-12-07 | 中国石油天然气股份有限公司 | Crude hydrogen pressurizing and recovering method for styrene device |
| US20120190904A1 (en) * | 2011-01-20 | 2012-07-26 | Fina Technology, Inc. | Hydrogen removal from dehydrogenation reactor product |
| CN103908868A (en) * | 2014-04-15 | 2014-07-09 | 大连理工大学 | Separation method for removing styrene from ethylbenzene-dehydrogenation tail gas and recovering hydrogen |
-
2015
- 2015-02-05 CN CN201510061293.9A patent/CN104548862A/en active Pending
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1962029A (en) * | 2005-11-11 | 2007-05-16 | 中国石油化工股份有限公司 | Method for separating dehydrogenated tail gas |
| CN102266704A (en) * | 2010-06-04 | 2011-12-07 | 中国石油天然气股份有限公司 | Crude hydrogen pressurizing and recovering method for styrene device |
| US20120190904A1 (en) * | 2011-01-20 | 2012-07-26 | Fina Technology, Inc. | Hydrogen removal from dehydrogenation reactor product |
| CN103908868A (en) * | 2014-04-15 | 2014-07-09 | 大连理工大学 | Separation method for removing styrene from ethylbenzene-dehydrogenation tail gas and recovering hydrogen |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106693436A (en) * | 2015-11-13 | 2017-05-24 | 中国石化工程建设有限公司 | Tail gas treatment system for storage tank type material storage facilities |
| CN111036025A (en) * | 2018-10-11 | 2020-04-21 | 中国石化工程建设有限公司 | Method and system for treating styrene pressure relief exhaust gas |
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Application publication date: 20150429 |