CN101629085A - Method for designing driving system for circulating hydrogen compressor of hydrocarbon hydrogenation device - Google Patents
Method for designing driving system for circulating hydrogen compressor of hydrocarbon hydrogenation device Download PDFInfo
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- CN101629085A CN101629085A CN200810161543A CN200810161543A CN101629085A CN 101629085 A CN101629085 A CN 101629085A CN 200810161543 A CN200810161543 A CN 200810161543A CN 200810161543 A CN200810161543 A CN 200810161543A CN 101629085 A CN101629085 A CN 101629085A
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- hydrogen compressor
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Abstract
The invention provides a method for designing a driving system for a circulating hydrogen compressor of a hydrocarbon hydrogenation device. A steam supply system driving a steam turbine of the circulating hydrogen compressor comprises a steam storage tank, wherein under a condition that a steam source stops steam supply, the steam storage tank keeps on supplying steam to ensure continuous operation of the circulating hydrogen compressor until a hydrogenation reactor completes oil removing or replacement. The method can ensure safe shutdown of the device, and is particularly applicable to the hydrogenation device of coal tar containing heavy distillate.
Description
Technical field
The present invention relates to a kind of method for designing driving system for circulating hydrogen compressor of hydrocarbon hydrogenation device, the method for designing driving system for circulating hydrogen compressor that relates to a kind of coal tar hydrogenating unit especially relates more particularly to a kind of method for designing driving system for circulating hydrogen compressor that contains the coal tar hydrogenating unit of last running.
Background technology
As everyone knows, coal tar, particularly contain the last running coal tar of (being higher than 370 ℃) such as conventional boiling point, more particularly contain the coal tar of high viscosity last running, because the metal content height of its last running, sulphur content height, nitrogen content height, the burnt matter asphalt content of aromatic hydrocarbons height, the easy coking of high temperature, in its hydro-upgrading reaction process, use protective material, metal remover inevitably, take off the carbon residue agent, several in the catalyzer such as sweetening agent, denitrfying agent, aromatic hydrocarbons saturator; Because the sulphur content height of its lighting end (being lower than 370 ℃), nitrogen content height, the burnt matter asphalt content of aromatic hydrocarbons height, the easy coking of high temperature such as conventional boiling point; sometimes oxygen level height; sometimes olefin(e) centent height; in its hydro-upgrading reaction process, use protective material, reductor, metal remover inevitably, take off the carbon residue agent, several in the catalyzer such as sweetening agent, denitrfying agent, aromatic hydrocarbons saturator.
During ordinary production, on the beds from front to back, the oil hydrogenation degree from shallow to deep, hydrogen richness is more and more higher, metal content, sulphur content, nitrogen content, aromaticity content is more and more lower, but the part hydro carbons on the anterior beds, under hydroconversion condition, still have suitable hydrogenation leeway, and easily coking under hot conditions, therefore, when device has an accident, if circulating hydrogen compressor shuts down, will cause reaction bed temperature to raise fast on the one hand, take place " temperature runaway ", easily cause simultaneously the beds coking, the accelerator activator inactivation shortens the cycle of operation as a result, reduces the reactor mechanical property simultaneously even forms damage or destruction.
Therefore, during device accident (such as power cut of whole factory), must guarantee that circulating hydrogen compressor remains in operation finishes de-oiling (gas circulation de-oiling) or displacement (with the oil displacement of the close boiling range of unsuitable coking) until the coal tar hydrogenating reactor, guarantees to realize hydrogenation reaction part emergency.
With etc. boiling range conventional oil base hydrocarbon hydrogenation device catalyzer air speed (A) compare, contain the coal tar of last running, to contain the catalyzer air speed (B) of hydro-upgrading reaction process of coal tar of high viscosity last running in particular much lower, such as A 2～10 times of B, be equal-volume stock oil amount of finish hydrogenation unit, the catalyst for coal tar hydrogenation modification amount is 2～10 times of petroleum base hydrocarbon hydrogenation device catalytic amount.Based on these characteristics, determined the coal tar hydrogenating reactor to finish de-oiling or metathetical time (TB), finish the many of de-oiling or metathetical time (TA) length than petroleum base hydrocarbons hydrogenation reactor, about TB=(2～10) TA, for the hydro-upgrading reactor of the coal tar that contains high viscosity last running, finishing de-oiling or metathetical time (TB) approximately is 10～30 minutes or longer time.
Known a kind of petroleum base method for designing driving system for circulating hydrogen compressor of hydrocarbon hydrogenation device is, the water vapor steam turbine is adopted in the driving of circulating hydrogen compressor, the steam-supplying system of steam turbine, at power vapour source (boiler) taking place stops under the condition of steam supply, power system capacity and boiler continue the ability of steaming, can keep circulating hydrogen compressor a bit of time (several minutes) of remaining in operation is used to carry out de-oiling or displacement, and this system does not establish special-purpose vapour storage tank.
The method for designing driving system for circulating hydrogen compressor of hydrocarbon hydrogenation device that a kind of steam-supplying system of the present invention contains vapour storage tank does not appear in the newspapers.
First purpose of the present invention is to provide a kind of coal tar hydrogenating unit method for designing driving system for circulating hydrogen compressor that contains high viscosity last running.Second purpose of the present invention is to provide a kind of coal tar hydrogenating unit method for designing driving system for circulating hydrogen compressor that contains last running.The 3rd purpose of the present invention is to provide a kind of coal tar hydrogenating unit method for designing driving system for circulating hydrogen compressor.The 4th purpose of the present invention is to provide a kind of method for designing driving system for circulating hydrogen compressor of hydrocarbon hydrogenation device.
Summary of the invention
A kind of method for designing driving system for circulating hydrogen compressor of hydrocarbon hydrogenation device, it is characterized in that: gas (vapour) turbine is adopted in the driving of circulating hydrogen compressor, air feed (vapour) system of gas (vapour) turbine contains gas storage (vapour) jar, stop under the condition of air feed (vapour) in power gas (vapour) generation source, gas storage (vapour) jar lasting air feed (vapour), guarantee that circulating hydrogen compressor remains in operation, finish de-oiling or displacement until hydrogenator.
Feature of the present invention further is: power gas can be any suitable source of the gas, be generally water vapor.
Feature of the present invention further is: hydrogenation unit is a coal tar hydrogenating unit.
Feature of the present invention further is: hydrogenation unit is the coal tar hydrogenating unit that contains last running.
Feature of the present invention further is: hydrogenation unit is the coal tar hydrogenating unit that contains high viscosity last running.
Feature of the present invention further is: circulating hydrogen compressor is a whizzer.
Feature of the present invention further is: stop in the vapor generation source under the condition of steam supply, vapour storage tank continues steam supply, and steam turbine outlet steam enters atmosphere.
Feature of the present invention further is: stop in the vapor generation source under the condition of steam supply, vapour storage tank continues steam supply, and circulating hydrogen compressor remains in operation generally at least 5 minutes time, at least 15 minutes usually, preferably at least 30 minutes.
Feature of the present invention further is: gas (vapour) turbine, raw oil pump gas (vapour) turbine and circulating hydrogen compressor gas (vapour) turbine, shared same air feed (vapour) system are adopted in the driving of hydrogenation unit raw oil pump.
Embodiment
According to the present invention, gas (vapour) turbine is adopted in the driving of circulating hydrogen compressor of hydrocarbon hydrogenation device, air feed (vapour) system of gas (vapour) turbine contains gas storage (vapour) jar, stop under the condition of air feed (vapour) in power gas (vapour) generation source, gas storage (vapour) jar lasting air feed (vapour), guarantee that circulating hydrogen compressor remains in operation, finish de-oiling or displacement until hydrogenator.
According to the present invention, power gas can be any suitable source of the gas, be generally water vapor.
According to the present invention, hydrogenation unit is a hydrocarbon hydrogenation device, its stock oil can be coal tar, in particular contain the coal tar of last running, more particularly contain the coal tar of high viscosity last running, can also be petroleum base residual oil.
According to the present invention, circulating hydrogen compressor can be reciprocating engine, whizzer preferably.
According to the present invention, stop in the vapor generation source under the condition of steam supply, vapour storage tank continues steam supply, and steam turbine outlet steam enters atmosphere, can reduce the vapour storage tank volume.
According to the present invention, stop in the vapor generation source under the condition of steam supply, vapour storage tank continues steam supply, circulating hydrogen compressor remains in operation generally at least 5 minutes time, at least 15 minutes usually, preferably at least 30 minutes, and the vapour storage tank volume requires according to this and the operational condition (temperature and pressure) of gas-turbine outlet/inlet designs.
According to the present invention, gas (vapour) turbine, raw oil pump gas (vapour) turbine and circulating hydrogen compressor gas (vapour) turbine, shared same air feed (vapour) system are adopted in the driving of hydrogenation unit raw oil pump.Stop under the condition of air feed (vapour) in power gas (vapour) generation source, gas storage (vapour) jar lasting air feed (vapour) guarantees that raw oil pump remains in operation, and carries to reactor and stops work with oil.
The invention has the advantages that, stop in the vapour source under the condition of steam supply, vapour storage tank continues steam supply, can guarantee the time that circulating hydrogen compressor remains in operation, finish de-oiling (gas circulation de-oiling) or displacement (using the oil displacement of the close boiling range of unsuitable coking) until hydrogenator, be particularly suitable for containing the hydrogenation unit of the coal tar of last running, guarantee to realize hydrogenation reaction part emergency.
Embodiment
The hydrogenation unit A that contains the coal tar of high viscosity last running, 3.5MPa superheated vapour steam turbine is adopted in the driving of circulating hydrogen compressor, the steam-supplying system of steam turbine contains vapour storage tank, stop under the condition of steam supply in power vapour generation source, vapour storage tank continues steam supply 35 minutes, and steam turbine outlet steam enters atmosphere.Having guaranteed that circulating hydrogen compressor remains in operation finishes displacement until the coal tar hydrogenating reactor, realizes hydrogenation reaction part emergency.
Residuum hydrodesulfurization device B, 3.5MPa superheated vapour steam turbine is adopted in the driving of circulating hydrogen compressor, and the steam-supplying system of steam turbine contains vapour storage tank, stops under the condition of steam supply in power vapour generation source, vapour storage tank continues steam supply 22 minutes, and steam turbine outlet steam enters atmosphere.Having guaranteed that circulating hydrogen compressor remains in operation finishes displacement until the coal tar hydrogenating reactor, realizes hydrogenation reaction part emergency.
Claims (13)
1, a kind of method for designing driving system for circulating hydrogen compressor of hydrocarbon hydrogenation device, it is characterized in that: gas (vapour) turbine is adopted in the driving of circulating hydrogen compressor, air feed (vapour) system of gas (vapour) turbine contains gas storage (vapour) jar, stop under the condition of air feed (vapour) in power gas (vapour) generation source, gas storage (vapour) jar lasting air feed (vapour), guarantee that circulating hydrogen compressor remains in operation, finish de-oiling or displacement until hydrogenator.
2, according to the described method of claim 1, it is characterized in that: power gas (vapour) is water vapor.
3, according to the described method of claim 2, it is characterized in that: hydrogenation unit is a coal tar hydrogenating unit.
4, according to the described method of claim 2, it is characterized in that: hydrogenation unit is the coal tar hydrogenating unit that contains last running.
5, according to the described method of claim 2, it is characterized in that: hydrogenation unit is the coal tar hydrogenating unit that contains high viscosity last running.
6, according to the described method of claim 3, it is characterized in that: circulating hydrogen compressor is a whizzer.
7, according to claim 2 or 3 or 4 or 5 or 6 described methods, it is characterized in that: stop in the vapor generation source under the condition of steam supply, vapour storage tank continues steam supply, and steam turbine outlet steam enters atmosphere.
8, according to the described method of claim 7, it is characterized in that: stop in the vapor generation source under the condition of steam supply, vapour storage tank continues steam supply, and circulating hydrogen compressor remained in operation 5 minutes at least.
9, according to the described method of claim 7, it is characterized in that: stop in the vapor generation source under the condition of steam supply, vapour storage tank continues steam supply, and circulating hydrogen compressor remained in operation 15 minutes at least.
10, according to the described method of claim 7, it is characterized in that: stop in the vapor generation source under the condition of steam supply, vapour storage tank continues steam supply, and circulating hydrogen compressor remained in operation 30 minutes at least.
11, according to claim 2 or 3 or 4 or 5 or 6 described methods, it is characterized in that: stop in the vapor generation source under the condition of steam supply, vapour storage tank continues steam supply, and circulating hydrogen compressor remained in operation 5 minutes at least.
12, according to claim 2 or 3 or 4 or 5 or 6 described methods, it is characterized in that: stop in the vapor generation source under the condition of steam supply, vapour storage tank continues steam supply, and circulating hydrogen compressor remained in operation 15 minutes at least.
13, according to claim 2 or 3 or 4 or 5 or 6 described methods, it is characterized in that: stop in the vapor generation source under the condition of steam supply, vapour storage tank continues steam supply, and circulating hydrogen compressor remained in operation 30 minutes at least.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN200810161543A CN101629085A (en) | 2008-09-24 | 2008-09-24 | Method for designing driving system for circulating hydrogen compressor of hydrocarbon hydrogenation device |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN200810161543A CN101629085A (en) | 2008-09-24 | 2008-09-24 | Method for designing driving system for circulating hydrogen compressor of hydrocarbon hydrogenation device |
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| CN101629085A true CN101629085A (en) | 2010-01-20 |
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| CN200810161543A Pending CN101629085A (en) | 2008-09-24 | 2008-09-24 | Method for designing driving system for circulating hydrogen compressor of hydrocarbon hydrogenation device |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104987884A (en) * | 2015-05-22 | 2015-10-21 | 中石寰球（北京）工程管理咨询有限公司 | Hydrogenation device and process for production of light fuel oil |
| CN107903944A (en) * | 2017-11-07 | 2018-04-13 | 河北新启元能源技术开发股份有限公司 | The new hydrogen of agent and flushing oil pressure control device are loaded and unloaded in a kind of coal tar hydrogenating |
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| CN1077175A (en) * | 1993-02-02 | 1993-10-13 | 中国五环化学工程公司 | Ammonia-preparing technique from heavy oil |
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| JP2005293949A (en) * | 2004-03-31 | 2005-10-20 | Honda Motor Co Ltd | Fuel gas manufacturing system and operation method of the same |
| CN101265859A (en) * | 2006-12-22 | 2008-09-17 | 曼柴油机欧洲股份公司 | Gas supply system for a drive |
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2008
- 2008-09-24 CN CN200810161543A patent/CN101629085A/en active Pending
Patent Citations (5)
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| CN2092613U (en) * | 1990-12-01 | 1992-01-08 | 中国科学院低温技术实验中心 | Cryogenic compressors |
| CN1077175A (en) * | 1993-02-02 | 1993-10-13 | 中国五环化学工程公司 | Ammonia-preparing technique from heavy oil |
| US20020076339A1 (en) * | 2000-12-15 | 2002-06-20 | Boulware Jim L. | Fuel/hydraulic engine system |
| JP2005293949A (en) * | 2004-03-31 | 2005-10-20 | Honda Motor Co Ltd | Fuel gas manufacturing system and operation method of the same |
| CN101265859A (en) * | 2006-12-22 | 2008-09-17 | 曼柴油机欧洲股份公司 | Gas supply system for a drive |
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104987884A (en) * | 2015-05-22 | 2015-10-21 | 中石寰球（北京）工程管理咨询有限公司 | Hydrogenation device and process for production of light fuel oil |
| CN104987884B (en) * | 2015-05-22 | 2019-04-23 | 江苏湖大化工科技有限公司 | A kind of hydrogenation plant and technique producing light-weight fuel oil |
| CN107903944A (en) * | 2017-11-07 | 2018-04-13 | 河北新启元能源技术开发股份有限公司 | The new hydrogen of agent and flushing oil pressure control device are loaded and unloaded in a kind of coal tar hydrogenating |
| CN107903944B (en) * | 2017-11-07 | 2020-07-28 | 河北新启元能源技术开发股份有限公司 | Pressure control device for loading and unloading agent fresh hydrogen and flushing oil in coal tar hydrogenation |
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Application publication date: 20100120 |