CN115247085A - Raw oil reaction optimization control method and system - Google Patents
Raw oil reaction optimization control method and system Download PDFInfo
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- CN115247085A CN115247085A CN202210742600.XA CN202210742600A CN115247085A CN 115247085 A CN115247085 A CN 115247085A CN 202210742600 A CN202210742600 A CN 202210742600A CN 115247085 A CN115247085 A CN 115247085A
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- 238000006243 chemical reaction Methods 0.000 title claims abstract description 44
- 238000005457 optimization Methods 0.000 title claims abstract description 22
- 238000000034 method Methods 0.000 title claims abstract description 21
- 238000012937 correction Methods 0.000 claims abstract description 72
- 239000002994 raw material Substances 0.000 claims abstract description 72
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims abstract description 70
- 239000001301 oxygen Substances 0.000 claims abstract description 70
- 229910052760 oxygen Inorganic materials 0.000 claims abstract description 70
- 239000007789 gas Substances 0.000 claims abstract description 18
- 238000001514 detection method Methods 0.000 claims abstract description 14
- 238000005259 measurement Methods 0.000 claims abstract description 12
- 230000015572 biosynthetic process Effects 0.000 claims abstract description 8
- 238000003786 synthesis reaction Methods 0.000 claims abstract description 8
- 239000000463 material Substances 0.000 claims description 6
- 238000004364 calculation method Methods 0.000 claims description 4
- 230000002194 synthesizing effect Effects 0.000 claims description 3
- 239000003921 oil Substances 0.000 description 33
- 238000002309 gasification Methods 0.000 description 15
- 239000000047 product Substances 0.000 description 11
- 239000000295 fuel oil Substances 0.000 description 9
- 238000002485 combustion reaction Methods 0.000 description 7
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 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
- 238000004519 manufacturing process Methods 0.000 description 5
- 230000008901 benefit Effects 0.000 description 4
- 229930195733 hydrocarbon Natural products 0.000 description 4
- 238000005336 cracking Methods 0.000 description 3
- 230000008569 process Effects 0.000 description 3
- 239000004215 Carbon black (E152) Substances 0.000 description 2
- 238000004891 communication Methods 0.000 description 2
- 239000000446 fuel Substances 0.000 description 2
- 150000002430 hydrocarbons Chemical class 0.000 description 2
- 239000007788 liquid Substances 0.000 description 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 2
- 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
- 230000002159 abnormal effect Effects 0.000 description 1
- 229910002091 carbon monoxide Inorganic materials 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 239000007795 chemical reaction product Substances 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 239000001257 hydrogen Substances 0.000 description 1
- 229910052739 hydrogen Inorganic materials 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 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
- 239000002002 slurry Substances 0.000 description 1
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Classifications
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- 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]
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- 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, reading CH of product synthesis gas 4 Calculating the content and carrying out deviation to obtain a correction coefficient of the ratio of the oxygen to the raw material; correcting the correction coefficient to enable the correction coefficient to be within a preset correction range, and obtaining an optimal correction coefficient within the correction range; calculating according to the optimal correction coefficient, the actual raw material measurement 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 a preset raw material demand value to obtain a final raw material set value. The invention can adjust the supply ratio of oxygen and raw materials according to the tail gas components of the synthesis gas product under any condition, so that the reaction can be fully reacted. The product rate is improved, meanwhile, the operation degree of personnel can be effectively reduced, and the efficiency of the personnel in a factory is improved.
Description
Technical Field
The invention belongs to the field of gasification treatment production of raw oil products, and particularly relates to a raw oil reaction optimization control method and system.
Background
Used as a feedstock for gasification (oil-based feedstocks such as residual oil). Preparing raw materials, feeding the raw materials into a gasification furnace in a dry or slurry mode, and carrying out reduction reaction on the raw materials, steam and oxygen in the gasification furnace at high temperature and high pressure to generate synthesis gas. Syngas is predominantly CO and H2 (greater than 85% by volume) and small amounts of CO2 and CH4. The overall reaction is as follows
In the control of the prior art, the control of the raw fuel oil and the oxygen supply is realized by the steps of calculating the required oxygen amount based on the total oxygen supply amount, the combustion oxygen demand amount and the combustion oxygen demand amount; calculating the fuel oil demand according to the required oxygen amount and the oxygen-oil ratio; comparing the fuel oil demand with a smelting mode fuel oil set value, and selecting the lowest fuel oil demand as a final set value of a fuel oil controller; calculating a first oxygen demand according to the fuel oil set value and the oxygen-fuel ratio; detecting the current oil quantity of the fuel oil, and calculating a second oxygen demand according to the current oil quantity detection value of the fuel oil and the oxygen-oil ratio; and comparing the first oxygen demand with the second oxygen demand, and selecting the highest oxygen demand of the two as the fuel combustion oxygen demand. In the prior art, for gasification, due to the complexity of reaction, a technologist is required to have extremely high judgment on the reaction in a furnace (influence factors comprise the calorific value of raw materials, the deviation of oxygen quality and the error of flow per se), and the proportion control and modification of oxygen and raw materials are carried out according to components; in addition, when the equipment is manufactured, the gasification device should be provided with corresponding matching systems for deslagging and the like, and the manufacturing and maintenance costs are higher.
Disclosure of Invention
The invention aims to provide a raw oil reaction optimization control method and a raw oil reaction optimization control system, which aim to solve the problems of high process requirement and high cost.
In order to solve the problems, the technical scheme of the invention is as follows:
a raw oil reaction optimization control method comprises the following steps:
s101: reading CH of product syngas 4 Calculating the content and carrying out deviation to obtain a correction coefficient of the ratio of the oxygen to the raw material;
s102: correcting the correction coefficient to enable the correction coefficient to be within a preset correction range, and obtaining an optimal correction coefficient;
s104: calculating according to the optimal correction coefficient, the current oxygen amount detection value and a preset raw material demand value to obtain a final raw material set value;
s105: and calculating according to the optimal correction coefficient, the actual raw material measurement value and a preset raw material set value to obtain a set value of the actual oxygen controller.
Further preferably, before step S101, a correction coefficient may also be input according to an actual demand to skip step S101.
In step S102, the preset correction range is determined according to the properties of the feedstock oil and the reaction scale.
Further preferably, step S103 is included after step S102, and the oxygen-enriched condition is selected to increase the optimal correction coefficient according to the actual reflection condition.
Specifically, in step S104, a theoretical raw material set value is calculated according to the current oxygen amount detection value and the optimal correction coefficient, and the theoretical raw material set value is compared with the required raw material value, and the larger value is used as the final raw material set value, where the theoretical raw material set value = the current oxygen amount detection value ÷ the optimal correction coefficient.
Specifically, in step S105, a lower value is selected according to the actual raw material measurement value and the raw material set value, and the lower value is compared with the optimal correction coefficient to obtain the set value of the actual oxygen controller;
here, the set value of the actual oxygen controller = the raw material low value × the optimum correction coefficient.
A raw oil reaction optimization control system is provided with the raw oil reaction optimization control method, and comprises an acquisition device, a control operation device and an execution device;
the acquisition module is used for reading CH of product synthesis gas 4 Content, actualThe raw material measurement value and the current oxygen amount detection value are uploaded to a control operation module
Control operation device for synthesizing CH of gas according to product 4 Performing deviation calculation to obtain a correction coefficient of the ratio of the oxygen to the raw material; correcting the correction coefficient to enable the correction coefficient to be within a preset correction range, and obtaining an optimal correction coefficient; calculating according to the optimal correction coefficient, the actual raw material measurement 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 demand value to obtain a final raw material set value; generating a corresponding instruction according to the set value of the actual oxygen controller and the final raw material set value and sending the instruction to an execution device;
the execution device is used for receiving an instruction for controlling the operation device so as to control the ratio of the actually input oxygen to the raw materials.
Specifically, the control arithmetic device adopts a DCS control system.
Due to the adoption of the technical scheme, compared with the prior art, the invention has the following advantages and positive effects: the invention can adjust the supply ratio of oxygen and raw materials according to the tail gas components of the synthesis gas product under any condition, so that the reaction can be fully reacted. The product rate is improved, meanwhile, the operation degree of personnel can be effectively reduced, and the efficiency of the personnel in a factory 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 feedstock oil reaction optimization control method according to an embodiment of the present invention;
FIG. 2 is a graph of the oxygen to feed ratio correction for an example of the present invention;
FIG. 3 is a modified schematic of the oxygen to feed ratio of the present invention;
FIG. 4 is an oxygen control schematic of the present invention;
FIG. 5 is a schematic diagram of the feedstock 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 be made with reference to the accompanying drawings. It is obvious that the drawings in the following description are only some examples of the invention, and that for a person skilled in the art, other drawings and embodiments can be derived from them without inventive effort.
For the sake of simplicity, the drawings only schematically show the parts relevant to the present invention, and they do not represent the actual structure as a product. In addition, in order to make the drawings concise and understandable, components having the same structure or function in some of the drawings are only schematically illustrated or only labeled. In this document, "one" means not only "only one" but also a case of "more than one".
The following describes the optimized control method and system for raw oil reaction in detail with reference to the accompanying drawings and specific embodiments. Advantages and features of the present invention will become apparent from the following description and from the claims.
Example 1
This example provides a method for controlling optimization of a feedstock oil reaction. The raw material enters a gasification device, and the reaction can be roughly divided into three stages: cracking stage, gasifying stage and reaction coexisting stage.
In the cracking stage, the raw material and oxygen enter the combustion chamber along with steam, and the raw material is instantaneously evaporated by the flame and the high temperature of the inner wall of the combustion chamber of the gasifier. And in this short time, a cracking reaction occurs to produce carbon, methane, hydrocarbon radicals, and the like. During the gasification stage, the hydrocarbon radicals react with oxygen, producing a large amount of heat energy. In the stage of the reaction coexistence phase, further reaction occurs in the combustion chamber of the gasification furnace, and the reaction gas is still at a high temperature. The gas composition changes slightly due to the secondary reactions of the methane, carbon and water gas shift reactions. According to the water gas shift reaction formula:
if sufficient reaction time is available in the combustion chamber, the reaction product carbon reacts under the conditions prevailing 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 gasified feed.
Production of methane from the reaction of hydrogen and carbon monoxide:
the control scheme given for this implementation based on the above reaction is as follows
Referring to FIG. 1, first in step S101, CH in the product synthesis gas tail gas is read by an analyzer 4 And (4) calculating the content, and performing deviation calculation to obtain a correction coefficient of the ratio of the oxygen to the raw material. The correction coefficient can be artificially selected according to actual requirements, and artificial input and excision can be carried out at any time.
Then, referring to fig. 2, in step S102, the correction coefficient is corrected so that the correction coefficient is within a preset correction range to obtain an optimal correction coefficient. The ratio of oxygen to the raw material 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 within the correction range, an oxygen-enriched condition may be selected according to the actual reaction condition, so as to increase the oxygen material ratio. In the embodiment, in order to ensure the safety of the gasification device, the device is ensured to be stable when the gasification reaction is abnormal, and in the process, oxygen enrichment condition is added to ensure the safety of the gasification device.
Further, referring to FIG. 5, in step S104, a raw material required value Feed-need is set, and a raw material theoretical set value calculated from the current oxygen amount detection value FI-O2 and the optimum raw material oxygen-Oil ratio O2/Oil is selected as a final raw material set value FI-SV-Oil of the maximum value of the two. Wherein, the theoretical set value of the raw material = current oxygen amount detection value FI-O2 ÷ optimal correction coefficient O2/Oil.
In this embodiment, in order to prevent the influence of the excessively fast/slow feed value on the gasification reaction, the rate of change is limited at the feed set value port, and is usually 0.85%/min to 1.1%/min of the feed value. Up to this point, the present embodiment has obtained both the input oxygen value and the feedstock value, based on which the corresponding oxygen and feedstock are delivered to the gasification device.
Further, referring to FIG. 4, in step S105, the actual raw material measurement value FI-Oil is compared with the raw material set value FI-SV-Oil, and a lower value min-Oil and an optimum correction factor O2/Oil are selected to calculate a set value SV-O2 of the actual oxygen controller. Wherein, the set value SV-O2 of the actual oxygen controller = the raw material lower value min-Oil multiplied by the optimal 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 the raw material controller.
Example 2
This embodiment provides a raw oil reaction optimization control system configured with the raw oil reaction optimization control method as in embodiment 1, and including an acquisition device, a control arithmetic device, and an execution device.
The acquisition module is used for reading CH of product synthesis gas 4 Content, actual raw material measurement value and current oxygen amount measurement valueAnd uploading to a control operation module.
Control arithmetic device for synthesizing CH of gas according to product 4 Performing deviation calculation to obtain a correction coefficient of the ratio of the oxygen to the raw material; correcting the correction coefficient to enable the correction coefficient to be within a preset correction range, and obtaining an optimal correction coefficient; calculating according to the optimal correction coefficient, the actual raw material measurement 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 quantity detection value and a preset raw material demand value to obtain a final raw material set value; and generating a corresponding instruction according to the set value of the actual oxygen controller and the final raw material set value and sending the instruction to an execution device.
The control operation device adopts a DCS control system, namely a distributed control system, which is also called a distributed control system. Compared with a centralized control system, the novel computer control system 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 of computers, communication, display, 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 an instruction for controlling the operation device so as to control the ratio of the actually input oxygen to the raw materials.
The embodiments of the present invention have been described in detail with reference to the accompanying drawings, but the present invention is not limited to the above embodiments. Even if various changes are made to the present invention, it is still within the scope of the present invention if they fall within the scope of the claims of the present invention and their equivalents.
Claims (8)
1. A raw oil reaction optimization control method is characterized by comprising the following steps:
s101: reading CH of product syngas 4 Calculating the content and carrying out deviation to obtain a correction coefficient of the ratio of the oxygen to the raw material;
s102: correcting the correction coefficient to enable the correction coefficient to be within a preset correction range, and obtaining the optimal correction coefficient;
s104: calculating according to the optimal correction coefficient, the current oxygen quantity detection value and a preset raw material demand value to obtain a final raw material set value;
s105: and calculating according to the optimal correction coefficient, the actual raw material measurement value and the preset raw material set value to obtain the set value of the actual oxygen controller.
2. The method for controlling feedstock oil reaction optimization according to claim 1, wherein before the step S101, the correction coefficient may be input according to actual demand to skip the step S101.
3. The method for controlling feedstock oil reaction optimization according to claim 1, wherein in step S102, the preset correction range is determined based on the feedstock oil property and the reaction scale.
4. The method for controlling feedstock oil reaction optimization according to claim 1, further comprising a step S103 after the step S102, wherein an oxygen-rich condition is selected to increase the optimum correction coefficient according to an actual reaction condition.
5. The method for controlling feedstock oil reaction optimization according to claim 1, wherein in step S104, a theoretical feedstock material set value is calculated from the current oxygen amount detection value and the optimal correction factor, and the theoretical feedstock material set value is compared with the required feedstock material value, and the larger value is used as the final feedstock material set value, wherein the theoretical feedstock material set value = the current oxygen amount detection value ÷ the optimal correction factor.
6. The method for controlling feedstock oil reaction optimization according to claim 1, wherein in step S105, a lower value is selected based on the actual feedstock measurement value and the feedstock set value, respectively, and the selected lower value is compared with the optimum correction factor to calculate a set value of an actual oxygen controller;
here, the set value of the actual oxygen controller = the raw material lower value × the optimum correction coefficient.
7. A raw oil reaction optimization control system configured with the raw oil reaction optimization control method according to any one of claims 1 to 6, characterized by comprising an acquisition device, a control arithmetic device and an execution device;
the acquisition module is used for reading CH of product synthesis gas 4 The content, the actual raw material measured value and the current oxygen amount detected value are uploaded to a control operation module
The control arithmetic device is used for synthesizing CH of gas according to products 4 Performing deviation calculation to obtain a correction coefficient of the ratio of the oxygen to the raw material; correcting the correction coefficient to enable the correction coefficient to be located in a preset correction range, and obtaining the optimal correction coefficient; calculating according to the optimal correction coefficient, the actual raw material measurement 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 demand value to obtain a final raw material set value; generating a corresponding instruction according to a set value of an actual oxygen controller and the final raw material set value, and sending the instruction 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 materials.
8. The raw oil reaction optimization control system according to claim 7, wherein the control arithmetic device employs a DCS control system.
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