CN115247085B - Raw oil reaction optimization control method and system - Google Patents
Raw oil reaction optimization control method and system Download PDFInfo
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- CN115247085B CN115247085B CN202210742600.XA CN202210742600A CN115247085B CN 115247085 B CN115247085 B CN 115247085B CN 202210742600 A CN202210742600 A CN 202210742600A CN 115247085 B CN115247085 B CN 115247085B
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- 238000006243 chemical reaction Methods 0.000 title claims abstract description 35
- 238000000034 method Methods 0.000 title claims abstract description 21
- 238000005457 optimization Methods 0.000 title abstract description 5
- 239000002994 raw material Substances 0.000 claims abstract description 85
- 238000012937 correction Methods 0.000 claims abstract description 73
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims abstract description 72
- 239000001301 oxygen Substances 0.000 claims abstract description 72
- 229910052760 oxygen Inorganic materials 0.000 claims abstract description 72
- 239000007789 gas Substances 0.000 claims abstract description 21
- 238000001514 detection method Methods 0.000 claims abstract description 18
- 230000015572 biosynthetic process Effects 0.000 claims abstract description 12
- 238000003786 synthesis reaction Methods 0.000 claims abstract description 12
- 238000004364 calculation method Methods 0.000 claims abstract description 7
- 239000003921 oil Substances 0.000 description 29
- 238000002309 gasification Methods 0.000 description 16
- 239000000047 product Substances 0.000 description 11
- 239000000446 fuel Substances 0.000 description 10
- 238000002485 combustion reaction Methods 0.000 description 7
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 6
- 229910052799 carbon Inorganic materials 0.000 description 6
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 6
- 238000004519 manufacturing process Methods 0.000 description 5
- 238000010586 diagram Methods 0.000 description 3
- 239000000295 fuel oil Substances 0.000 description 3
- 229930195733 hydrocarbon Natural products 0.000 description 3
- 150000002430 hydrocarbons Chemical group 0.000 description 3
- 229910002091 carbon monoxide Inorganic materials 0.000 description 2
- 238000004891 communication Methods 0.000 description 2
- 238000005336 cracking Methods 0.000 description 2
- 229910052739 hydrogen Inorganic materials 0.000 description 2
- 239000007788 liquid Substances 0.000 description 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 2
- 239000004215 Carbon black (E152) Substances 0.000 description 1
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 1
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 1
- 238000003723 Smelting Methods 0.000 description 1
- 230000005856 abnormality Effects 0.000 description 1
- 239000007795 chemical reaction product Substances 0.000 description 1
- 238000003776 cleavage reaction Methods 0.000 description 1
- 238000005520 cutting process Methods 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 239000001257 hydrogen Substances 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 238000005259 measurement Methods 0.000 description 1
- 238000012544 monitoring process Methods 0.000 description 1
- 230000008092 positive effect Effects 0.000 description 1
- 238000004886 process control Methods 0.000 description 1
- 239000012495 reaction gas Substances 0.000 description 1
- 230000035484 reaction time Effects 0.000 description 1
- 238000006722 reduction reaction Methods 0.000 description 1
- 238000010517 secondary reaction Methods 0.000 description 1
- 239000002893 slag Substances 0.000 description 1
- 239000002002 slurry Substances 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
- C10J3/72—Other features
- C10J3/723—Controlling or regulating the gasification process
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P90/00—Enabling technologies with a potential contribution to greenhouse gas [GHG] emissions mitigation
- Y02P90/02—Total factory control, e.g. smart factories, flexible manufacturing systems [FMS] or integrated manufacturing systems [IMS]
Landscapes
- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Combustion & Propulsion (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Organic Chemistry (AREA)
- Hydrogen, Water And Hydrids (AREA)
Abstract
The invention discloses a raw oil reaction optimization control method, which comprises the steps of reading CH 4 content of product synthesis gas, and performing deviation calculation to obtain a correction coefficient of oxygen to raw material ratio; correcting the correction coefficient so that the correction coefficient is positioned in a preset correction range, and obtaining the optimal correction coefficient in the correction range; calculating according to the optimal correction coefficient, the actual raw material measured value and the raw material set value to obtain a set value of the actual oxygen controller; and calculating according to the optimal correction coefficient, the current oxygen amount detection value and the preset raw material requirement value to obtain a final raw material set value. The invention can adjust the supply proportion of oxygen and raw materials according to the components of the tail gas of the synthetic gas product under any condition, so that the reaction can fully react. The product rate is improved, meanwhile, the operation degree of personnel can be effectively reduced, and the efficiency of factory personnel is improved.
Description
Technical Field
The invention belongs to the field of raw oil product gasification treatment production, and particularly relates to a raw oil reaction optimization control method and system.
Background
Is used as a raw material for gasification (oil raw material such as residual oil). Raw materials are prepared and enter a gasification furnace in a dry type or slurry type, and the raw materials, steam and oxygen are subjected to reduction reaction at high temperature and high pressure in the gasification furnace to generate synthesis gas. Synthesis gas is predominantly CO and H 2 (greater than 85% by volume) and minor amounts of CO 2 and CH 4. The overall reaction is as follows:
In the control of the prior art, the control of the raw material fuel oil and the oxygen supply is realized by the steps of calculating the required oxygen amount according to the total oxygen supply amount, the combustion oxygen demand amount and the combustion oxygen demand amount; calculating fuel oil demand according to the required oxygen amount and the oxygen-oil ratio; comparing the fuel demand with a smelting mode fuel set value, and selecting the lowest value as a final set value of a fuel controller; calculating a first oxygen demand according to the fuel oil set value and the oxygen-fuel ratio; detecting the current fuel quantity of the fuel, and calculating a second oxygen demand according to the current fuel quantity detection value of the fuel and the oxygen-fuel ratio; and comparing the first oxygen demand with the second oxygen demand, and selecting the highest oxygen demand as the fuel combustion oxygen demand. In the prior art, for gasification, due to the complexity of reaction, the process personnel is required to have extremely high judgment on the reaction in the furnace (influencing factors include the heat value of raw materials, the deviation of oxygen quality and the error of flow per se), and the ratio of oxygen to raw materials is controlled and modified according to the components; in addition, during equipment manufacture, the gasification device should be provided with corresponding matched systems such as slag discharging and the like, and the manufacture and maintenance have great cost.
Disclosure of Invention
The invention aims to provide a raw oil reaction optimal control method and system, which are used for solving the problems of high process requirements and high cost.
In order to solve the problems, the technical scheme of the invention is as follows:
the optimized control method for the reaction of the raw oil comprises the following steps:
S101: reading CH 4 content of the product synthesis gas, and performing deviation calculation to obtain a correction coefficient of the oxygen to raw material ratio;
S102: correcting the correction coefficient to ensure that the correction coefficient is positioned in a preset correction range, so as to obtain an optimal correction coefficient;
S104: calculating according to the optimal correction coefficient, the current oxygen amount detection value and the preset raw material requirement value to obtain a final raw material set value;
S105: and calculating according to the optimal correction coefficient, the actual raw material measured value and the preset raw material set value to obtain the set value of the actual oxygen controller.
Further preferably, before step S101, a correction coefficient may be further input according to actual requirements to skip step S101.
In step S102, the preset correction range is determined according to the property of the raw oil and the reaction scale.
Further preferably, step S103 is further included after step S102, and the oxygen enrichment condition is selected to improve the optimal correction factor according to the actual reflection situation.
Specifically, in step S104, a raw material theoretical set value is calculated according to the current oxygen amount detection value and the optimal correction coefficient, and the raw material theoretical set value is compared with the raw material demand value to obtain a final raw material set value, where the raw material theoretical set value=the current oxygen amount detection value and the optimal correction coefficient.
Specifically, in step S105, the actual raw material measured value and the raw material set value are compared and selected to select a lower value, and the lower value and the optimal correction coefficient are calculated to obtain the set value of the actual oxygen controller;
Wherein the actual oxygen controller set point = raw material lower value x optimal correction factor.
The raw oil reaction optimizing control system is provided with the raw oil reaction optimizing control method according to any one of the above, and comprises a collecting device, a control operation device and an executing device;
The acquisition module is used for reading CH 4 content of the product synthesis gas, measuring a value of an actual raw material and a current oxygen amount detection value and uploading the values to the control operation module;
the control operation device is used for performing deviation calculation according to the CH 4 content of the product synthesis gas to obtain a correction coefficient of the oxygen to raw material ratio; correcting the correction coefficient to ensure that the correction coefficient is positioned in a preset correction range, so as to obtain an optimal correction coefficient; calculating according to the optimal correction coefficient, the actual raw material measured value and the raw material set value to obtain a set value of the actual oxygen controller; calculating according to the optimal correction coefficient, the current oxygen amount detection value and the preset raw material requirement value to obtain a final raw material set value; generating corresponding instructions according to the set value of the actual oxygen controller and the set value of the final raw material, and sending the corresponding instructions to the execution device;
the execution device is used for receiving the instruction of the control operation device so as to control the ratio of the actually input oxygen to the raw material.
Specifically, the control arithmetic device adopts a DCS control system.
By adopting the technical scheme, the invention has the following advantages and positive effects compared with the prior art: the invention can adjust the supply proportion of oxygen and raw materials according to the components of the tail gas of the synthetic gas product under any condition, so that the reaction can fully react. The product rate is improved, meanwhile, the operation degree of personnel can be effectively reduced, and the efficiency of factory personnel is improved.
Drawings
Various other advantages and benefits will become apparent to those of ordinary skill in the art upon reading the following detailed description of the preferred embodiments. The drawings are only for purposes of illustrating the preferred embodiments and are not to be construed as limiting the invention.
FIG. 1 is a schematic flow chart of a method for optimizing and controlling the reaction of raw oil according to an embodiment of the invention;
FIG. 2 is a graph showing the oxygen to feed ratio correction in accordance with an embodiment of the present invention;
FIG. 3 is a schematic diagram of the correction of oxygen to feed ratio in accordance with the present invention;
FIG. 4 is a schematic diagram of oxygen control according to the present invention;
fig. 5 is a schematic diagram of the raw material control of the present invention.
Detailed Description
In order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the following description will explain the specific embodiments of the present invention with reference to the accompanying drawings. It is evident that the drawings in the following description are only examples of the invention, from which other drawings and other embodiments can be obtained by a person skilled in the art without inventive effort.
For the sake of simplicity of the drawing, the parts relevant to the present invention are shown only schematically in the figures, which do not represent the actual structure thereof as a product. Additionally, in order to simplify the drawing for ease of understanding, components having the same structure or function in some of the drawings are shown schematically with only one of them, or only one of them is labeled. Herein, "a" means not only "only this one" but also "more than one" case.
The invention provides a method and a system for optimizing and controlling the reaction of raw oil, which are further described in detail below with reference to the accompanying drawings and specific embodiments. Advantages and features of the invention will become more apparent from the following description and from the claims.
Example 1
The embodiment provides a raw oil reaction optimization control method. The feedstock enters the gasification unit and its reaction can be roughly divided into three stages: a cracking stage, a gasification stage and a reaction coexistence stage.
In the cracking stage, the raw material and oxygen enter a combustion chamber along with steam, and the raw material is instantaneously evaporated through flame and high temperature of the inner wall of the combustion chamber of the gasification furnace. And in this short period of time, a cleavage reaction occurs, producing carbon, methane, hydrocarbon groups, and the like. In the gasification stage, hydrocarbon radicals react with oxygen to produce a large amount of heat energy. In the coexistence phase of the reaction, further reaction occurs in the gasifier combustion chamber, and the reaction gas is still at high temperature. The gas composition varies slightly due to the secondary reactions of the methane, carbon and water gas shift reactions. According to the water gas shift reaction equation:
if sufficient reaction time is available in the combustion chamber, the reaction product carbon reacts under the prevailing conditions in the reactor:
In actual production, some carbon is always present in the product gas of the gasification reaction. When liquid hydrocarbons are gasified, the carbon produced is typically 1.0wt% of the feed oil, but the carbon production ultimately depends on the ash content in the liquid hydrocarbons of the gasification feedstock.
Methane is produced from the reaction of hydrogen and carbon monoxide:
the control scheme given by this implementation based on the above reaction is as follows:
Referring to fig. 1, first, in step S101, the CH 4 content in the tail gas of the product synthesis gas is read by an analyzer, and a correction coefficient of the oxygen to raw material ratio is obtained by performing deviation calculation. The correction coefficient can be manually selected according to actual requirements, and manual input and cutting can be performed at any time.
Then, referring to fig. 2, in step S102, the correction coefficient is corrected such that the correction coefficient is within a preset correction range to obtain an optimal correction coefficient. The oxygen to raw material ratio can be a fixed value, the correction range is between alpha and beta, and the correction range and the correction curve can be adaptively adjusted according to different raw material properties and the scale of the device.
Next, referring to fig. 3, in step S103, after selecting the optimal correction coefficient in the above correction range, the oxygen enrichment condition may be selected according to the actual reaction situation, so as to increase the oxygen raw material ratio. In this example, in order to ensure the safety of the gasification device, the device is ensured to be stable in the possible gasification reaction abnormality, and in this process, oxygen-enriched conditions are added to ensure the safety thereof.
Further, referring to fig. 5, in step S104, a raw material theoretical set value is calculated by setting a raw material demand value Feed-Feed and based on the current oxygen amount detection value FI-O2 and the optimal raw material oxygen-Oil ratio O2/Oil, and a final raw material set value FI-SV-Oil, which is the maximum value of both, is selected as a raw material set. Wherein, the theoretical set value of raw material=the current oxygen amount detection value FI-O2 ≡optimal correction coefficient O2/Oil.
In this example, in order to prevent the influence of the feed setting on the gasification reaction from being too fast/slow, the rate of change is limited at the feed setting port, typically from 0.85%/min to 1.1%/min of the feed value. Thus far, the present embodiment has been developed for both the input oxygen value and the feedstock value, based on which the corresponding oxygen and feedstock are delivered to the gasification unit.
Further, referring to fig. 4, the process proceeds to step S105, where the actual raw material measurement value FI-Oil is compared with the raw material set value FI-SV-Oil, and the set value SV-O2 of the actual oxygen controller is calculated by selecting the lower value min-Oil and the optimum correction coefficient O2/Oil. Wherein the actual oxygen controller set point SV-o2=raw material lower value min-Oil x optimum correction coefficient O2/Oil. The actual raw material measured value FI-Oil is a value measured by an actual operation device, and the raw material set value FI-SV-Oil is a target value set by a raw material controller.
Example 2
The present embodiment provides a raw oil reaction optimizing control system configured with the raw oil reaction optimizing control method as in embodiment 1, including a collecting device, a control arithmetic device, and an executing device.
The acquisition module is used for reading CH 4 content of the product synthesis gas, an actual raw material measured value and a current oxygen amount detection value and uploading the actual raw material measured value and the current oxygen amount detection value to the control operation module.
The control operation device is used for performing deviation calculation according to the CH 4 content of the product synthesis gas to obtain a correction coefficient of the oxygen to raw material ratio; correcting the correction coefficient to ensure that the correction coefficient is positioned in a preset correction range, so as to obtain an optimal correction coefficient; calculating according to the optimal correction coefficient, the actual raw material measured value and the raw material set value to obtain a set value of the actual oxygen controller; calculating according to the optimal correction coefficient, the current oxygen amount detection value and the preset raw material requirement value to obtain a final raw material set value; and generating corresponding instructions according to the set value of the actual oxygen controller and the set value of the final raw material, and sending the instructions to the execution device.
The control operation device adopts a DCS control system, namely a distributed control system, which is also called a distributed control system. The novel computer control system is relative to the centralized control system, and is developed and evolved on the basis of the centralized control system. The system is a multi-stage computer system which is composed of a process control stage and a process monitoring stage and takes a communication network as a link, integrates 4C technologies such as computer, communication, display and control, and the like, and has the basic ideas of decentralized control, centralized operation, hierarchical management, flexible configuration and convenient configuration.
The execution device is used for receiving the instruction of the control operation device so as to control the ratio of the actually input oxygen to the raw material.
The embodiments of the present invention have been described in detail with reference to the drawings, but the present invention is not limited to the above embodiments. Even if various changes are made to the present invention, it is within the scope of the appended claims and their equivalents to fall within the scope of the invention.
Claims (6)
1. The method for optimally controlling the reaction of the raw oil is characterized by comprising the following steps:
S101: reading CH 4 content of the product synthesis gas, and performing deviation calculation to obtain a correction coefficient of the oxygen to raw material ratio;
S102: correcting the correction coefficient so that the correction coefficient is positioned in a preset correction range to obtain the optimal correction coefficient;
s104: calculating according to the optimal correction coefficient, the current oxygen amount detection value and a preset raw material requirement value to obtain a final raw material set value;
s105: calculating according to the optimal correction coefficient, an actual raw material measured value and a preset raw material set value to obtain a set value of an actual oxygen controller;
In the step S104, a raw material theoretical set value is calculated according to the current oxygen amount detection value and the optimal correction coefficient, and the raw material theoretical set value is compared with the raw material required value, and a larger value is used as the final raw material set value, wherein the raw material theoretical set value=the current oxygen amount detection value ≡optimal correction coefficient;
in the step S105, a lower value is selected by comparing the actual raw material measured value with the raw material set value, and the lower value is calculated with the optimal correction coefficient to obtain a set value of an actual oxygen controller; wherein the actual oxygen controller set point = raw material lower value x the optimal correction factor.
2. The method according to claim 1, wherein the correction coefficient is further inputted according to actual demand to skip the step S101 before the step S101.
3. The method according to claim 1, wherein in the step S102, the preset correction range is determined based on the property of the raw oil and the reaction scale.
4. The method according to claim 1, further comprising step S103, after said step S102, of selecting an oxygen enrichment condition to increase the optimal correction factor according to the actual reflection condition.
5. A raw oil reaction optimizing control system provided with the raw oil reaction optimizing control method according to any one of claims 1 to 4, characterized by comprising a collecting device, a control arithmetic device, and an executing device;
The acquisition device is used for reading CH 4 content of the product synthesis gas, an actual raw material measured value and a current oxygen amount detection value and uploading the actual raw material measured value and the current oxygen amount detection value to the control operation module;
the control operation device is used for performing deviation calculation according to the CH 4 content of the product synthesis gas to obtain a correction coefficient of the oxygen to raw material ratio; correcting the correction coefficient so that the correction coefficient is positioned in a preset correction range to obtain the optimal correction coefficient; calculating according to the optimal correction coefficient, the actual raw material measured value and the raw material set value to obtain a set value of the actual oxygen controller; calculating according to the optimal correction coefficient, the current oxygen amount detection value and a preset raw material requirement value to obtain a final raw material set value; generating corresponding instructions according to the set value of the actual oxygen controller and the set value of the final raw material, and sending the corresponding instructions to the execution device;
the execution device is used for receiving the instruction of the control operation device so as to control the ratio of the actually input oxygen to the raw material.
6. The system according to claim 5, wherein the control arithmetic device is a DCS control system.
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| CN102399594A (en) * | 2011-12-30 | 2012-04-04 | 华东理工大学 | A Method for Optimizing the Operating Conditions of "Texaco Gasifier" Online |
| CN106582284A (en) * | 2016-12-14 | 2017-04-26 | 河南华润电力古城有限公司 | Automatic control method and system of thermal-power-unit SCR denitration ammonia spraying |
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| US5396416A (en) * | 1992-08-19 | 1995-03-07 | Continental Controls, Inc. | Multivariable process control method and apparatus |
| JP2003090244A (en) * | 2001-09-17 | 2003-03-28 | Honda Motor Co Ltd | Control device for internal combustion engine |
| US20040226217A1 (en) * | 2003-05-16 | 2004-11-18 | University Of Chicago | Fuel processor for producing hydrogen from hydrocarbon fuels |
| CA2678213C (en) * | 2007-02-19 | 2010-09-21 | Richard Allan Sederquist | Method of operating a syngas generator |
| US8352228B2 (en) * | 2008-12-23 | 2013-01-08 | Exxonmobil Upstream Research Company | Method for predicting petroleum expulsion |
| JP5720327B2 (en) * | 2011-03-11 | 2015-05-20 | 株式会社Ihi | Control device |
| CN106773718B (en) * | 2017-01-22 | 2023-09-26 | 航天长征化学工程股份有限公司 | Oxygen-carbon ratio control system and gasification furnace oxygen-coal ratio control method thereof |
| CN108192668B (en) * | 2017-12-28 | 2020-05-26 | 陕西延长石油（集团）有限责任公司 | Oxygen-coal ratio control method |
| CN113217944A (en) * | 2021-05-12 | 2021-08-06 | 阳春新钢铁有限责任公司 | Method for controlling oxygen-coal ratio of waste steel baking |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN102399594A (en) * | 2011-12-30 | 2012-04-04 | 华东理工大学 | A Method for Optimizing the Operating Conditions of "Texaco Gasifier" Online |
| CN106582284A (en) * | 2016-12-14 | 2017-04-26 | 河南华润电力古城有限公司 | Automatic control method and system of thermal-power-unit SCR denitration ammonia spraying |
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