CN114426454B - Automatic control method and application of front-end depropanization front-end hydrogenation reactor - Google Patents
Automatic control method and application of front-end depropanization front-end hydrogenation reactor Download PDFInfo
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- 238000005984 hydrogenation reaction Methods 0.000 title claims abstract description 257
- 238000000034 method Methods 0.000 title claims abstract description 67
- HSFWRNGVRCDJHI-UHFFFAOYSA-N alpha-acetylene Natural products C#C HSFWRNGVRCDJHI-UHFFFAOYSA-N 0.000 claims abstract description 77
- 125000002534 ethynyl group Chemical group [H]C#C* 0.000 claims abstract description 77
- 238000006243 chemical reaction Methods 0.000 claims abstract description 61
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 claims abstract description 37
- 239000005977 Ethylene Substances 0.000 claims abstract description 37
- IYABWNGZIDDRAK-UHFFFAOYSA-N allene Chemical compound C=C=C IYABWNGZIDDRAK-UHFFFAOYSA-N 0.000 claims abstract description 31
- MWWATHDPGQKSAR-UHFFFAOYSA-N propyne Chemical group CC#C MWWATHDPGQKSAR-UHFFFAOYSA-N 0.000 claims abstract description 31
- 238000004458 analytical method Methods 0.000 claims abstract description 15
- IFYDWYVPVAMGRO-UHFFFAOYSA-N n-[3-(dimethylamino)propyl]tetradecanamide Chemical compound CCCCCCCCCCCCCC(=O)NCCCN(C)C IFYDWYVPVAMGRO-UHFFFAOYSA-N 0.000 claims description 67
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 claims description 42
- 239000001294 propane Substances 0.000 claims description 26
- 230000008569 process Effects 0.000 claims description 23
- 239000001257 hydrogen Substances 0.000 claims description 15
- 229910052739 hydrogen Inorganic materials 0.000 claims description 15
- 238000000926 separation method Methods 0.000 claims description 15
- 239000000463 material Substances 0.000 claims description 11
- 238000005336 cracking Methods 0.000 claims description 9
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims description 8
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims description 8
- 239000007789 gas Substances 0.000 claims description 7
- 150000002431 hydrogen Chemical class 0.000 claims description 7
- OTMSDBZUPAUEDD-UHFFFAOYSA-N Ethane Chemical compound CC OTMSDBZUPAUEDD-UHFFFAOYSA-N 0.000 claims description 6
- QQONPFPTGQHPMA-UHFFFAOYSA-N propylene Natural products CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 claims description 6
- 125000004805 propylene group Chemical group [H]C([H])([H])C([H])([*:1])C([H])([H])[*:2] 0.000 claims description 6
- 238000010223 real-time analysis Methods 0.000 claims description 6
- 238000007670 refining Methods 0.000 claims description 4
- 239000003054 catalyst Substances 0.000 description 10
- 238000004519 manufacturing process Methods 0.000 description 8
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 5
- 229910052799 carbon Inorganic materials 0.000 description 5
- 150000001345 alkine derivatives Chemical class 0.000 description 4
- 150000001336 alkenes Chemical class 0.000 description 3
- 230000003197 catalytic effect Effects 0.000 description 3
- 238000011161 development Methods 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- 238000005516 engineering process Methods 0.000 description 3
- JRZJOMJEPLMPRA-UHFFFAOYSA-N olefin Natural products CCCCCCCC=C JRZJOMJEPLMPRA-UHFFFAOYSA-N 0.000 description 3
- 238000000197 pyrolysis Methods 0.000 description 3
- 239000002994 raw material Substances 0.000 description 3
- KAKZBPTYRLMSJV-UHFFFAOYSA-N Butadiene Chemical compound C=CC=C KAKZBPTYRLMSJV-UHFFFAOYSA-N 0.000 description 2
- KDLHZDBZIXYQEI-UHFFFAOYSA-N Palladium Chemical compound [Pd] KDLHZDBZIXYQEI-UHFFFAOYSA-N 0.000 description 2
- 230000008901 benefit Effects 0.000 description 2
- 238000013461 design Methods 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 229920000642 polymer Polymers 0.000 description 2
- 230000001105 regulatory effect Effects 0.000 description 2
- 150000005671 trienes Chemical class 0.000 description 2
- 239000004215 Carbon black (E152) Substances 0.000 description 1
- 238000010521 absorption reaction Methods 0.000 description 1
- 230000009471 action Effects 0.000 description 1
- 238000004364 calculation method Methods 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 238000004587 chromatography analysis Methods 0.000 description 1
- 230000000052 comparative effect Effects 0.000 description 1
- 238000012790 confirmation Methods 0.000 description 1
- 230000001276 controlling effect Effects 0.000 description 1
- 238000003795 desorption Methods 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
- -1 ethylene, propylene Chemical group 0.000 description 1
- 229930195733 hydrocarbon Natural products 0.000 description 1
- 150000002430 hydrocarbons Chemical class 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 239000007788 liquid Substances 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 229910000510 noble metal Inorganic materials 0.000 description 1
- 238000005457 optimization Methods 0.000 description 1
- 229910052763 palladium Inorganic materials 0.000 description 1
- 239000002574 poison Substances 0.000 description 1
- 231100000614 poison Toxicity 0.000 description 1
- 238000006116 polymerization reaction Methods 0.000 description 1
- 229920000098 polyolefin Polymers 0.000 description 1
- 238000012545 processing Methods 0.000 description 1
- 230000035945 sensitivity Effects 0.000 description 1
- 239000002904 solvent Substances 0.000 description 1
- 238000001179 sorption measurement Methods 0.000 description 1
- 238000004230 steam cracking Methods 0.000 description 1
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C7/00—Purification; Separation; Use of additives
- C07C7/148—Purification; Separation; Use of additives by treatment giving rise to a chemical modification of at least one compound
- C07C7/163—Purification; Separation; Use of additives by treatment giving rise to a chemical modification of at least one compound by hydrogenation
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C7/00—Purification; Separation; Use of additives
- C07C7/148—Purification; Separation; Use of additives by treatment giving rise to a chemical modification of at least one compound
- C07C7/163—Purification; Separation; Use of additives by treatment giving rise to a chemical modification of at least one compound by hydrogenation
- C07C7/167—Purification; Separation; Use of additives by treatment giving rise to a chemical modification of at least one compound by hydrogenation for removal of compounds containing a triple carbon-to-carbon bond
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- Oil, Petroleum & Natural Gas (AREA)
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Abstract
The invention discloses an automatic control method and application of a hydrogenation reactor before front depropanization. The automatic control method of the hydrogenation reactor before the front depropanization comprises the following steps: obtaining analysis data based on the obtained parameters of the hydrogenation reactor before pre-depropanization; adjusting the operation parameters so that the volume content of the CO at the inlet is in a stable state; judging whether the acetylene volume content of the outlet is smaller than a set value omega ppm or not, and adjusting the inlet temperature based on the judging result of the acetylene volume content; judging whether the conversion rate of the methylacetylene and the propadiene in the front hydrogenation reactor is within a set range, and adjusting the inlet temperature of the front hydrogenation reactor based on the judgment result of the conversion rate of the methylacetylene and the propadiene. The method adjusts the inlet temperature based on the volume content of acetylene and the conversion rate of methylacetylene and propadiene, thereby ensuring that the volume content of the outlet acetylene is qualified and simultaneously achieving the purpose of obtaining the optimal ethylene yield.
Description
Technical Field
The invention belongs to the field of petrochemical industry, and particularly relates to an automatic control method and application of a hydrogenation reactor before front depropanization.
Background
Ethylene technology is a petrochemical tap technology, and the ethylene technology level is regarded as an important sign for measuring the state of petrochemical development. The triene (ethylene, propylene and butadiene) produced by the ethylene cracking device is a basic raw material of petrochemical industry, and the level of the triene yield is a main mark for measuring the national petrochemical development level.
After the liquid hydrocarbon raw materials such as naphtha and the like in the ethylene cracking device are subjected to steam cracking and separation, the carbon two fraction contains ethylene, ethane and a small amount of acetylene, and the acetylene content is about 0.5-3% (volume). In the downstream polymerization reaction, the presence of acetylene can poison the polyolefin promoter and must be removed to obtain polymer grade ethylene. The method for removing acetylene widely used at present is a catalytic selective hydrogenation method. The acetylene in the carbon two fraction is removed by two processes, namely a solvent absorption method and a catalytic selective hydrogenation method.
The catalytic selective hydrogenation method has the advantages of simple process flow, less energy consumption, no environmental pollution, increased yield of target products, and along with the continuous improvement of the performance of the novel efficient hydrogenation catalyst, the application of the hydrogenation method is becoming common, and the method becomes the most commonly used economic and simple method at present. According to the different process routes, it can be divided into front hydrogenation and back hydrogenation. The post-hydrogenation process is suitable for separation processes mainly comprising sequential separation, pre-depropanization and post-hydrogenation and pre-deethanization and post-hydrogenation, and is a process of adding a proper amount of hydrogen into the remaining pure carbon two fractions for hydrogenation after light fractions such as hydrogen, CO, methane and the like contained in pyrolysis gas and heavy fractions such as three carbon or more than four carbon and the like.
The hydrogenation reactor unit before front-end depropanization is an important link for refining ethylene and propylene products, and is used for converting acetylene, methylacetylene (MA) and Propadiene (PD) into ethylene and propylene through selective hydrogenation under the action of a catalyst. If acetylene and MAPD are excessively hydrogenated to ethane and propane, the loss of ethylene and propylene results; or alkyne is polymerized to generate oligomer or even high polymer, which affects the service cycle of the reactor; for example, the hydrogenation activity of the catalyst is poor, so that the acetylene concentration at the outlet of the reactor is not controlled within the index requirement range, and ethylene of the product is unqualified, and the ethylene product and a downstream industrial chain are directly influenced, so that the operation of the hydrogenation reactor before the front depropanization has a critical effect on enterprise benefit and national life.
The palladium noble metal is generally used as an active component of the hydrogenation catalyst before the front depropanization, and the production suppliers comprise China petrochemical catalyst company, CLARIANT company, PHILLIPS company and the like. The thermodynamic parameters of the reaction, the surface adsorption and desorption reaction rates and the process sensitivity of the catalysts of various brands of manufacturers are different, and the optimal performance of the catalysts can be ensured by targeted adjustment and optimization.
At present, the production control of the hydrogenation reactor before the front depropanization generally adopts manual regulation and control, and related parameters are manually regulated and controlled by technicians. Because of the lengthy cracking separation process, complex process and limited personnel energy, the hydrogenation reactor before the front depropanization cannot be monitored, adjusted and optimized in real time. When unstable conditions such as material composition, pressure, temperature, flow, hydrogen and CO fluctuation occur in the hydrogenation system before the current depropanization, the stability is very slow by the hydrogenation system, and superposition phenomenon generated by repeated fluctuation ensures that the system is in a metastable state for a long time, thus easily causing alkyne leakage and ethylene loss at the outlet of the reactor and influencing the ethylene yield of products and the separation effect of the rectifying tower.
At present, most of the operation of the hydrogenation reactor before front-end depropanization adopts a method of manual experience and manual adjustment, so that the excessive hydrogenation of the hydrogenation reactor before front-end depropanization of a single-stage bed or a final-stage bed is easy to cause in order to ensure that acetylene in ethylene products is removed to be qualified, the concentration of acetylene in a final hydrogenation product is continuously 0ppm, and the ethylene loss is larger.
Disclosure of Invention
In view of the above, the invention provides an automatic control method and application of a hydrogenation reactor before front-end depropanization, which at least solves the problem of larger ethylene loss caused by low ethylene selectivity of the hydrogenation reactor before front-end depropanization in the prior art.
In a first aspect, the present invention provides an automatic control method for a hydrogenation reactor before front-end depropanization, comprising:
obtaining analysis data based on the obtained parameters of the hydrogenation reactor before the single-stage bed or the final-stage bed front-of-depropanization;
Adjusting the operation parameters of the single-stage bed or the pre-end-bed depropanization hydrogenation reactor based on the analysis data so that the volume content of CO at the inlet of the single-stage bed or the pre-end-bed depropanization hydrogenation reactor is in a stable state;
Judging whether the volume content of acetylene at the outlet of the hydrogenation reactor before the single-stage bed or the final-stage bed is smaller than a set value omega ppm or not, and adjusting the inlet temperature of the hydrogenation reactor before the single-stage bed or the final-stage bed based on the judging result of the volume content of acetylene;
judging whether the conversion rate of methylacetylene and propadiene in the hydrogenation reactor before the single-stage bed or the final-stage bed is within a set range, and adjusting the inlet temperature of the hydrogenation reactor before the single-stage bed or the final-stage bed is subjected to the front-stage depropanization based on the judgment result of the conversion rate of methylacetylene and propadiene.
Optionally, the parameters of the obtained single-stage bed or end-stage pre-depropanization hydrogenation reactor include:
The inlet temperature of the hydrogenation reactor before the propane removal before the single-stage bed or the end-stage bed, the pressure of the hydrogenation reactor before the propane removal before the single-stage bed or the end-stage bed, the inlet material flow of the hydrogenation reactor before the propane removal before the single-stage bed or the end-stage bed, the inlet acetylene concentration of the hydrogenation reactor before the propane removal before the single-stage bed or the end-stage bed, the outlet acetylene concentration of the hydrogenation reactor before the propane removal before the single-stage bed or the end-stage bed, the inlet MAPD concentration of the hydrogenation reactor before the propane removal before the single-stage bed or the end-stage bed, and the outlet MAPD concentration of the hydrogenation reactor before the propane removal before the single-stage bed or the end-stage bed, or the inlet CO concentration of the hydrogenation reactor before the propane removal before the single-stage bed and/or the end-stage bed.
Optionally, the volume content of the inlet CO of the hydrogenation reactor before the single-stage bed or the final-stage bed front-end depropanization is in a stable state:
The volume content of CO is in the range of omega+/-100 ppm in the set time, wherein omega is the current real-time analysis value of CO.
Optionally, the method determines whether the conversion rate of methylacetylene and propadiene in the hydrogenation reactor before the single-stage bed or the final-stage bed is within a set range, where the set range is:
The MAPD conversion rate of the hydrogenation reactor before the single-stage bed or the final-stage bed front-of-depropanization is kept in a range of theta+/-5%, wherein theta is a set value of the MAPD conversion rate, and MAPD is short for methylacetylene and propadiene.
Alternatively, θ can be in the range of 40-60%, preferably 45-55%.
Optionally, the method judges whether the volume content of acetylene at the outlet of the hydrogenation reactor before the single-stage bed or the final-stage bed is less than a set value omega ppm, wherein the value range of omega is 0.01-1.0, preferably 0.2-0.8.
Optionally, the adjusting the operation parameters of the single-stage bed or the pre-end-bed depropanizing hydrogenation reactor based on the analysis data, so that the inlet CO volume content of the single-stage bed or the pre-end-bed depropanizing hydrogenation reactor is in a stable state, includes:
and judging whether the volume content of CO at the inlet of the hydrogenation reactor before the single-stage bed or the final-stage bed is in a stable state.
Optionally, the determining whether the volume content of acetylene at the outlet of the hydrogenation reactor before the single-stage bed or the final-stage bed is less than a set value Ω ppm, and adjusting the inlet temperature of the hydrogenation reactor before the single-stage bed or the final-stage bed is based on the determination result of the volume content of acetylene, includes:
When the CO volume content at the inlet of the hydrogenation reactor before the single-stage bed or the final-stage bed is in a stable state, judging whether the acetylene volume content at the outlet of the hydrogenation reactor before the single-stage bed or the final-stage bed is less than a set value omega ppm;
if the acetylene volume content is greater than or equal to Ω ppm, the inlet temperature of the hydrogenation reactor before the single-stage bed or the end-stage bed is raised.
Optionally, the determining whether the conversion rate of methylacetylene and propadiene in the hydrogenation reactor before the single-stage bed or the final-stage bed is within a set range, and adjusting the inlet temperature of the hydrogenation reactor before the single-stage bed or the final-stage bed is based on the determination result of the conversion rate of methylacetylene and propadiene, includes:
when the acetylene volume content is smaller than omega ppm, judging whether the MAPD conversion rate is in a set range;
If the MAPD conversion rate is less than the minimum value of the set range, increasing the inlet temperature of the hydrogenation reactor before the single-stage bed or the final-stage bed is subjected to the front-end depropanization;
If the MAPD conversion rate is larger than the maximum value of the set range, the inlet temperature of the hydrogenation reactor before the single-stage bed or the final-stage bed is reduced, wherein MAPD is short for methylacetylene and propadiene.
Alternatively, the inlet temperature of the hydrogenation reactor before the single-stage bed or the end-stage bed is adjusted to be in the range of 35-95 ℃, preferably 55-85 ℃.
Optionally, the inlet temperature of the hydrogenation reactor before the single-stage bed or the final-stage bed is adjusted at a rate ranging from 0.5 to 8 ℃/hour, preferably from 1.0 to 5.0 ℃/hour.
Optionally, the method for calculating the conversion rate of methylacetylene and propadiene in the hydrogenation reactor before the depropanization of the single-stage bed or the end-stage bed comprises the following steps:
Wherein C MAPD is the actual MAPD conversion rate; x inlet is inlet MAPD volume content; x outlet is the volume content of the export MAPD, which is the abbreviation of methylacetylene and propadiene.
In a second aspect, the invention provides a process for refining, hydrogenating and removing cracked gas in a separation process of an ethylene cracking device, which is used for removing acetylene or/and MAPD, and the separation process is a hydrogenation process before front depropanization by using the control method in any one of the first aspects.
Optionally, the method comprises the following steps: the single-stage bed or the end-stage pre-depropanization hydrogenation reactor is an adiabatic bed or an isothermal bed.
Optionally, the composition of the inlet material of the hydrogenation reactor before the single-stage bed or the final-stage pre-depropanization comprises CO, hydrogen, methane, ethylene, ethane, acetylene, propylene, propane and MAPD;
also comprises at least one of C4 fraction and C5+ fraction;
And/or
The hydrogenation reactor before the single-stage bed or the final-stage bed is used for removing propane does not need to be matched with a hydrogenation moderator, and the hydrogenation moderator comprises crude hydrogen and CO.
According to the invention, the operation parameters of the hydrogenation reactor before the single-stage bed or the final-stage pre-bed depropanization are adjusted, so that the volume content of CO at the inlet of the hydrogenation reactor before the single-stage bed or the final-stage pre-bed depropanization is in a stable state, and then the inlet temperature of the hydrogenation reactor before the single-stage bed or the final-stage pre-bed depropanization is adjusted based on the volume content of acetylene and the conversion rate of methyl acetylene and propadiene at the outlet of the hydrogenation reactor before the single-stage bed or the final-stage pre-bed depropanization, and meanwhile, the inlet temperature is adjusted based on the volume content of acetylene and the conversion rate of methyl acetylene and propadiene as judging standards, so that the purpose of obtaining the optimal ethylene yield is achieved while the volume content of outlet acetylene is ensured to be qualified.
Drawings
Exemplary embodiments of the present invention will be described in more detail with reference to the accompanying drawings.
FIG. 1 shows a flow chart of a method of automatically controlling a pre-depropanizer pre-hydrogenation reactor in accordance with one embodiment of the present invention;
FIG. 2 shows a schematic diagram of a prior art pre-depropanization hydrogenation reactor process flow in an olefin plant;
FIG. 3 illustrates a functional block diagram of a pre-depropanizer pre-hydrogenation reactor control system in accordance with one embodiment of the present invention;
FIG. 4 shows a graph of the variation of the process conditions of a pre-depropanizer pre-hydrogenation reactor in accordance with one embodiment of the present invention;
Wherein:
1-depropanizer, 2-dearsenification reactor, 3-first stage bed reactor, 4-second stage bed reactor, 5-final stage bed reactor and 6-dryer.
Detailed Description
The following describes specific embodiments of the present invention in detail. It should be understood that the detailed description and specific examples, while indicating and illustrating the invention, are not intended to limit the invention.
The present invention will be further described with reference to examples, but the scope of the present invention is not limited to these examples.
The multi-stage bed and the end-stage bed are all hydrogenation reactors before front depropanization of the corresponding stage bed. The multi-stage bed front-depropanization front-hydrogenation reactor is a multi-stage bed series front-depropanization front-hydrogenation reactor system; each section of bed reactor of the hydrogenation reactor before the multi-section bed front-depropanization is designed as an adiabatic bed or an isothermal bed.
The main operating conditions of the hydrogenation reactor before pre-depropanization are two: the hydrogen to alkyne ratio and the inlet feed temperature.
Embodiment one:
As shown in fig. 1, an automatic control method of a hydrogenation reactor before front-end depropanization comprises the following steps:
Step S101: obtaining analysis data based on the obtained parameters of the hydrogenation reactor before the single-stage bed or the final-stage bed front-of-depropanization;
optionally, the parameters of the obtained single-stage bed or end-stage pre-depropanization hydrogenation reactor include:
The inlet temperature of the hydrogenation reactor before the propane removal before the single-stage bed or the end-stage bed, the pressure of the hydrogenation reactor before the propane removal before the single-stage bed or the end-stage bed, the inlet material flow of the hydrogenation reactor before the propane removal before the single-stage bed or the end-stage bed, the inlet acetylene concentration of the hydrogenation reactor before the propane removal before the single-stage bed or the end-stage bed, the outlet acetylene concentration of the hydrogenation reactor before the propane removal before the single-stage bed or the end-stage bed, the inlet MAPD concentration of the hydrogenation reactor before the propane removal before the single-stage bed or the end-stage bed, and/or the outlet MAPD concentration of the hydrogenation reactor before the propane removal before the single-stage bed or the end-stage bed and/or the end-stage bed.
The analysis data is data obtained by summarizing the acquired data. In a specific application scenario, the analysis processing can be performed in a logic computing chip such as a controller.
Step S102: adjusting the operation parameters of the single-stage bed or the pre-end-bed depropanization hydrogenation reactor based on the analysis data so that the volume content of CO at the inlet of the single-stage bed or the pre-end-bed depropanization hydrogenation reactor is in a stable state;
Optionally, the volume content of the inlet CO of the hydrogenation reactor before the single-stage bed or the final-stage bed front-end depropanization is in a stable state:
The volume content of CO is in the range of omega+/-100 ppm in the set time, wherein omega is the current real-time analysis value of CO.
Step S103: judging whether the volume content of acetylene at the outlet of the hydrogenation reactor before the single-stage bed or the final-stage bed is smaller than a set value omega ppm or not, and adjusting the inlet temperature of the hydrogenation reactor before the single-stage bed or the final-stage bed based on the judging result of the volume content of acetylene;
optionally, the method judges whether the volume content of acetylene at the outlet of the hydrogenation reactor before the single-stage bed or the final-stage bed is less than a set value omega ppm, wherein the value range of omega is 0.01-1.0, preferably 0.2-0.8.
Step S104: judging whether the conversion rate of methylacetylene and propadiene in the hydrogenation reactor before the single-stage bed or the final-stage bed is within a set range, and adjusting the inlet temperature of the hydrogenation reactor before the single-stage bed or the final-stage bed is subjected to the front-stage depropanization based on the judgment result of the conversion rate of methylacetylene and propadiene.
Optionally, the method for calculating the conversion rate of methylacetylene and propadiene in the hydrogenation reactor before the depropanization of the single-stage bed or the end-stage bed comprises the following steps:
Wherein C MAPD is the actual MAPD conversion rate; x inlet is inlet MAPD volume content; x outlet is the volume content of the export MAPD, which is the abbreviation of methylacetylene and propadiene.
Optionally, the method determines whether the conversion rate of methylacetylene and propadiene in the hydrogenation reactor before the single-stage bed or the final-stage bed is within a set range, where the set range is:
The MAPD conversion rate of the hydrogenation reactor before the single-stage bed or the final-stage bed front-of-depropanization is kept in a range of theta+/-5%, wherein theta is a set value of the MAPD conversion rate, and MAPD is short for methylacetylene and propadiene.
Alternatively, θ can be in the range of 40-60%, preferably 45-55%.
Optionally, the adjusting the operation parameters of the single-stage bed or the pre-end-bed depropanizing hydrogenation reactor based on the analysis data, so that the inlet CO volume content of the single-stage bed or the pre-end-bed depropanizing hydrogenation reactor is in a stable state, includes:
and judging whether the volume content of CO at the inlet of the hydrogenation reactor before the single-stage bed or the final-stage bed is in a stable state.
Optionally, the determining whether the volume content of acetylene at the outlet of the hydrogenation reactor before the single-stage bed or the final-stage bed is less than a set value Ω ppm, and adjusting the inlet temperature of the hydrogenation reactor before the single-stage bed or the final-stage bed is based on the determination result of the volume content of acetylene, includes:
When the CO volume content at the inlet of the hydrogenation reactor before the single-stage bed or the final-stage bed is in a stable state, judging whether the acetylene volume content at the outlet of the hydrogenation reactor before the single-stage bed or the final-stage bed is less than a set value omega ppm;
if the acetylene volume content is greater than or equal to Ω ppm, the inlet temperature of the hydrogenation reactor before the single-stage bed or the end-stage bed is raised.
Optionally, the determining whether the conversion rate of methylacetylene and propadiene in the hydrogenation reactor before the single-stage bed or the final-stage bed is within a set range, and adjusting the inlet temperature of the hydrogenation reactor before the single-stage bed or the final-stage bed is based on the determination result of the conversion rate of methylacetylene and propadiene, includes:
when the acetylene volume content is smaller than omega ppm, judging whether the MAPD conversion rate is in a set range;
If the MAPD conversion rate is less than the minimum value of the set range, increasing the inlet temperature of the hydrogenation reactor before the single-stage bed or the final-stage bed is subjected to the front-end depropanization;
If the MAPD conversion rate is larger than the maximum value of the set range, the inlet temperature of the hydrogenation reactor before the single-stage bed or the final-stage bed is reduced, wherein MAPD is short for methylacetylene and propadiene.
Alternatively, the inlet temperature of the hydrogenation reactor before the single-stage bed or the end-stage bed is adjusted to be in the range of 35-95 ℃, preferably 55-85 ℃.
Optionally, the inlet temperature of the hydrogenation reactor before the single-stage bed or the final-stage bed is adjusted at a rate ranging from 0.5 to 8 ℃/hour, preferably from 1.0 to 5.0 ℃/hour.
The specific adjustment steps are as follows:
(1) Confirming whether the CO volume content omega at the inlet of the hydrogenation reactor before the pre-depropanization is in a stable state, and continuing to (2) for interpretation if the CO volume content omega at the inlet of the hydrogenation reactor before the pre-depropanization is in the stable state; if not in a steady state, no automatic adjustment is performed.
(2) And (3) confirming whether the real-time outlet acetylene volume content of the hydrogenation reactor before the single-stage bed or the final-stage bed is less than a set value omega ppm. Continuing to (3) making a determination if the real-time outlet acetylene volume content is less than Ω ppm; the inlet temperature is increased if the real-time outlet acetylene content is greater than or equal to Ω ppm.
(3) If MAPD conversion rate of the hydrogenation reactor before the single-stage bed or the final-stage bed front-of-the-propane removal is within a range of theta+/-5%, the inlet temperature is not adjusted; if the MAPD conversion rate of the hydrogenation reactor before the single-stage bed or the final-stage bed is less than theta-5%, the inlet temperature is increased; if the MAPD conversion in the hydrogenation reactor prior to the single-stage or end-stage pre-depropanization is greater than θ+5%, the inlet temperature is reduced. The inlet temperature is the inlet temperature of the hydrogenation reactor before the depropanization of the single-stage bed or the end-stage bed.
(4) The steps (1) to (3) are one self-control period, and after the judgment and completion, the controller returns to the standby state to wait for the start of the next self-control period.
In a specific implementation, in an industrial device, acetylene in the feed component is removed from about 1000ppm to less than 1ppm in a single-stage bed or a hydrogenation reactor before the end-stage bed is usually controlled by the temperature of the reactor. Because the priority of acetylene hydrogenation is superior to that of Methylacetylene (MA) and Propadiene (PD), MAPD hydrogenation development is greatly improved along with the removal of acetylene at the outlet. Through extensive industrial data groping, the embodiment establishes a corresponding relationship among MAPD conversion rate, outlet acetylene concentration and ethylene selectivity, and improves ethylene yield by preventing acetylene from over-hydrogenation of the hydrogenation reactor before pre-depropanization.
This example is designed for the daily steady state operation of the hydrogenation reactor prior to the single bed or end bed depropanization. The flow rate of the material flow, the concentration of CO and hydrogen and other conditions can all influence the operation of the reactor. In general, this example can be applied to the normal fluctuation and variation of the flow rate of the hydrogenation reactor, the concentration of CO and hydrogen, and other conditions before the front-end depropanization. When the fluctuation range of conditions such as the volume content of CO is too large, the modularized automatic control system of the hydrogenation reactor before front-end depropanization can be switched to other control methods or automatically control in specific scenes according to requirements.
In this embodiment, the controller is located in a distributed control system, i.e. a DCS system or a server, of the hydrogenation reactor before front-end depropanization, and a control logic program in the controller collects the volume contents of CO, acetylene and MAPD at the inlet and outlet of the hydrogenation reactor before front-end depropanization of a single-stage bed or a final-stage bed, and automatically collects the analysis results and calculation data to store them in a fixed memory unit.
In an embodiment, a control logic program in the controller automatically maintains and adjusts the inlet temperature of the single-stage bed or the end-stage pre-depropanization hydrogenation reactor according to the monitored acetylene volume content at the outlet of the single-stage bed or the end-stage pre-depropanization hydrogenation reactor, the MAPD conversion rate and the change trend, and automatically realizes the stable operation of the pre-depropanization hydrogenation reactor and obtains the optimal ethylene selectivity.
In an embodiment, the main control variable of the control logic program of the controller is the inlet temperature of the hydrogenation reactor before the single-stage bed or the end-stage bed front-end-depropanization, and the main regulating variable is the inlet temperature of the hydrogenation reactor before the single-stage bed or the end-stage bed front-end-depropanization.
The control method provided by the embodiment is that in the production process of the hydrogenation reactor before the pre-depropanization, the controller adjusts the inlet temperature of the hydrogenation reactor before the pre-depropanization of the single-stage bed or the final-stage bed according to the volume content of acetylene at the outlet of the hydrogenation reactor before the pre-depropanization of the single-stage bed or the final-stage bed and the conversion rate of MAPD under the condition that the volume content of CO at the inlet is kept in a stable state.
More specifically, the acetylene volume content at the outlet of the hydrogenation reactor before the single-stage bed or the final-stage bed is controlled below a set value omega ppm by adjusting the operation parameters of the reactor under the condition that the CO volume content at the inlet is kept in a stable state, and the MAPD conversion rate is further kept within a range of theta+/-5% of the set value, so that higher ethylene selectivity is obtained.
In an embodiment, the MAPD conversion of the hydrogenation reactor before the single-stage bed or the final-stage bed is kept in the range of theta + -5%, wherein theta is a MAPD conversion set value, and the value of theta is in the range of 40-60%, preferably 45-55%.
The value of the acetylene volume content set value omega at the outlet of the hydrogenation reactor before the depropanization of the single-stage bed or the final-stage bed is in the range of 0.01-1.0ppm, preferably 0.3-0.7ppm.
The CO volume content at the inlet of the hydrogenation reactor before pre-depropanization is in a stable state, namely the CO volume content is in the range of omega+/-100 ppm in the previous 1 hour, wherein omega is the current real-time analysis value of CO.
The controller adjusts the operation parameters of the hydrogenation reactor before the single-stage bed or the final-stage bed front-of-depropanization to be the inlet temperature, and the specific self-control adjustment steps are as follows:
(1) Confirming whether the CO volume content omega at the inlet of the hydrogenation reactor before the pre-depropanization is in a stable state, and continuing to (2) for interpretation if the CO volume content omega at the inlet of the hydrogenation reactor before the pre-depropanization is in the stable state; the controller does not make an automatic adjustment if not in a steady state.
(2) And (3) confirming whether the real-time outlet acetylene volume content of the hydrogenation reactor before the single-stage bed or the final-stage bed is less than a set value omega ppm. Continuing to (3) making a determination if the real-time outlet acetylene volume content is less than Ω ppm; the inlet temperature is increased if the real-time outlet acetylene content is greater than or equal to Ω ppm.
(3) If the MAPD conversion rate of the hydrogenation reactor before the single-stage bed or the final-stage bed front-of-the-propane removal is within the range of theta+/-5 percent, the inlet temperature is not adjusted; if the MAPD conversion rate of the hydrogenation reactor before the single-stage bed or the final-stage bed front-of-the-propane removal is less than theta-5%, the inlet temperature is increased; if the MAPD conversion in the hydrogenation reactor before the single-stage bed or the final-stage bed front-of-the-propane removal is more than theta+5%, the inlet temperature is reduced.
(4) The steps (1) to (3) are one self-control period, and after the judgment and completion, the controller returns to the standby state to wait for the start of the next self-control period.
In the embodiment, in the automatic control process of the hydrogenation reactor before the single-stage bed or the final-stage bed front-end depropanization, the CO volume content omega at the inlet of the hydrogenation reactor before the front-end depropanization does not exceed the range of omega+/-100 ppm within the previous 1 hour, and the controller performs the next judgment; the controller does not make an automatic adjustment at this time when the fluctuation is below omega-100 ppm or above omega +100ppm during the previous 1 hour.
Concentrations refer to volume percent content and flow rates refer to mass flow rates, unless otherwise indicated.
In the automatic control process of the hydrogenation reactor before the single-stage bed or the final-stage bed front-of-depropanization, the volume content of acetylene at the control outlet is less than omega ppm. If the acetylene volume content at the outlet is higher than Ω ppm, this indicates the occurrence of under-hydrogenation. Once the acetylene concentration at the inlet suddenly fluctuates too high, the probability of the acetylene volume content at the outlet exceeding 5ppm is high (acetylene leakage), which is easy to cause larger ethylene loss or disqualification of ethylene products.
In the automatic control process of the hydrogenation reactor before the single-stage bed or the final-stage bed front-end depropanization, the MAPD conversion rate is controlled to be more than theta-5% and less than theta+5%. If MAPD conversion is too low or too high, a slight under-or over-hydrogenation is indicated.
The standard of the automatic control system of the hydrogenation reactor before the single-stage bed or the final-stage bed is the concentration of the acetylene at the outlet and the conversion rate of MAPD, and the automatic control system is implemented according to the standard that the volume content of the acetylene at the outlet of the hydrogenation reactor before the single-stage bed or the final-stage bed is less than omega ppm and the conversion rate of MAPD is within the range of theta+/-5 percent. The value of omega ppm is modified according to the specific control index of the production device, and the value range of omega is 0.2< omega <0.8ppm, preferably 0.4< omega <0.6ppm. The value of theta is also modified according to the specific control index of the production device, and the value range of theta is 40-60%, preferably 45-55%.
The adjustment of the controller of the hydrogenation reactor automatic control system before the single-stage bed or the final-stage bed is carried out under the condition of keeping the volume content of the CO at the inlet in a stable state. The current real-time analysis value of the CO volume content of the hydrogenation reactor before the depropanization is omega, the fluctuation of the CO volume content within 1 hour before the current real-time analysis value is omega+/-100 ppm, the current inlet CO volume content can be considered to be in a stable state, and the controller carries out the next judgment. If the CO volume content in the previous 1 hour appears to be greater than omega+100 ppm or less than omega-100 ppm, the autonomous system considers the current inlet CO volume content to be in an unstable state, and the controller does not automatically adjust.
In the process of adjusting hydrogenation control variables by a control logic program of the hydrogenation reactor before the single-stage bed or the final-stage bed, the adjustment range of the inlet temperature of the hydrogenation reactor before the single-stage bed or the final-stage bed is 35-95 ℃, preferably 55-85 ℃. If the inlet temperature reaches the upper limit and the requirement of the acetylene volume content at the outlet of the hydrogenation reactor before the front depropanization cannot be met, the operation mode is automatically switched to a manual mode and an alarm is sent; if the inlet temperature reaches the lower limit and the control standard requirement of MAPD conversion rate of the hydrogenation reactor before the front-end depropanization cannot be met, the operation mode is also automatically switched to a manual mode and an alarm is sent.
In the automatic control process of the hydrogenation reactor before the front-end depropanization, the adjustment rate of the inlet temperature of the hydrogenation reactor before the front-end depropanization of the single-stage bed or the end-stage bed is generally in the range of 0.5-8 ℃/h, preferably 1.0-5.0 ℃/h. If MAPD conversion is within θ.+ -. 5%, the operation is typically not adjusted to maintain the smoothness of the production operation.
The automatic control method of the hydrogenation reactor before the front-end depropanization does not need to be matched with hydrogenation moderators such as crude hydrogen, CO and the like.
The single-stage pre-bed depropanization pre-hydrogenation reactor is characterized in that a plurality of pre-hydrogenation reactors are connected in series in a pre-depropanization pre-hydrogenation reaction system or only one pre-hydrogenation reactor is used independently; the hydrogenation reactor before the final-stage pre-depropanization is the last-stage bed in the multi-stage bed series-connected pre-depropanization hydrogenation reactor system; the single-stage bed or the end-stage bed pre-depropanization hydrogenation reactor may be a gas phase reactor design of an adiabatic bed or an isothermal bed.
The automatic control of the hydrogenation reactor before front depropanization comprises two steps: program initialization phase and automatic control phase. The execution sequence of the automatic control program is as follows:
1. program initialization stage
After the program is started, firstly, initializing internal variables such as inlet temperature, pressure, flow rate and the like of the hydrogenation reactor before the single-stage bed or the final-stage bed is subjected to the front-end depropanization, and automatically identifying analysis and process data signals such as CO, hydrogen, acetylene, MAPD concentration and the like at the inlet and the outlet of the hydrogenation reactor before the single-stage bed or the final-stage bed is subjected to the front-end depropanization.
The operator confirms that all field operations are performed, the field analysis data is normally input, and the automatic control stage is ready to be entered, and if not confirmed, the program is in a waiting state until all confirmation is performed. And after the operator clicks to start to assign and confirm the ethylene concentration set value omega and the MAPD conversion rate set value theta at the outlet of the hydrogenation reactor before the single-stage bed or the final-stage pre-depropanization, entering an automatic control stage.
2. Self-control stage
After entering an automatic control program, the control logic program obtains field data and input concentration data of the acetylene at the outlet of the reactor according to a DCS system of the hydrogenation reactor before the front depropanization, judges whether the control variable of the reactor needs to be adjusted or not according to a judging principle every 1-1800 seconds, and realizes automatic control of the production process of the front hydrogenation reactor. The shorter the time interval for adjusting the parameter, the better, but at the same time the feedback time for adjusting the control variable signal and the time interval for analyzing the data are considered.
In the production automatic control process of the hydrogenation reactor before front depropanization, an automatic control program monitors important variables such as inlet temperature, catalyst bed temperature, CO and hydrogen concentration, and the like, and once the deviation is overlarge, the program enters a holding state, and simultaneously displays alarm information to carry out sound alarm.
Embodiment two:
The control method in the embodiment is used for the separation flow of the ethylene cracking device, namely a pre-depropanization hydrogenation flow.
In a process for refining and hydrodeoxygenation of pyrolysis gas in a separation flow path of an ethylene pyrolysis device, the device comprises:
The single-stage bed or the end-stage pre-depropanization hydrogenation reactor is an adiabatic bed or an isothermal bed.
The composition of the inlet materials of the hydrogenation reactor before the depropanization of the single-stage bed or the final-stage bed comprises CO, hydrogen, methane, ethylene, ethane, acetylene, propylene, propane and MAPD;
also comprises at least one of C4 fraction and C5+ fraction;
And/or
The hydrogenation reactor before the single-stage bed or the final-stage bed is required to be matched with a hydrogenation moderator, and the hydrogenation moderator comprises crude hydrogen and CO.
The method of example one was applied to a pre-depropanizer pre-hydrogenation reactor in an olefin plant: a controller connected with an OPC server of the original system is added outside the original DCS system, as shown in figure 3, the process conditions of the hydrogenation reactor before the depropanization of the end bed are adjusted, and an adjustment target is provided for the original system DCS in real time, so that the control of the hydrogenation reactor before the depropanization of the end bed is realized.
Firstly, a new controller is used for assigning 0.5ppm to the acetylene concentration set value omega of the outlet of the final-stage bed reactor of the hydrogenation reactor before the front-end depropanization and assigning 45% to the MAPD conversion set value theta, the new controller regulates and controls the MAPD conversion rate of the final-stage bed reactor to fluctuate within the range of 40-50%, and as shown in figure 4, an online control unit automatically adjusts the inlet temperature of the final-stage bed reactor in real time according to the acetylene concentration and the MAPD conversion rate of the outlet of the final-stage bed reactor. The catalyst selectivity of the hydrogenation reactor before front-end depropanization is improved to 12 percent.
Comparative example:
An olefin plant producing 80 ten thousand tons of ethylene in a certain year has 12 cracking furnaces and can process various cracking raw materials from ethane to hydrogenated tail oil and the like. The separation process of the plant adopts a pre-depropanization hydrogenation separation flow, a pre-depropanization hydrogenation reactor is positioned behind a high-pressure depropanization tower, a three-section bed series design is adopted, no standby bed exists, and the three-section bed reactors which are operated are a1 st section bed, a 2 nd section bed and a final section bed pre-depropanization hydrogenation reactor respectively, as shown in figure 2.
When the hydrogenation reactor before the pre-factory depropanization is operated, the DCS is connected with an online chromatograph, and online chromatographic analysis data are directly input into the DCS. The cold and hot material flow before the hydrogenation reactor before the front depropanization is controlled by a DCS system, the temperature of the material at the inlet of the hydrogenation reactor before the front depropanization is kept stable, the concentration of alkyne in the material flow is measured by an online chromatograph at the outlet of the hydrogenation reactor before the front depropanization of the end bed, the acetylene concentration at the outlet of the hydrogenation reactor before the front depropanization of the end bed is ensured to be kept at a level (about 0.01 ppm), and the selectivity of the catalyst of the hydrogenation reactor before the front depropanization of the end bed is kept at about-10%.
The comparison result shows that: compared with the manual control of the original factory, the ethylene selectivity of the hydrogenation reactor before the front depropanization can be obviously improved through the method and the application of the invention. .
The foregoing description of embodiments of the invention has been presented for purposes of illustration and description, and is not intended to be exhaustive or limited to the embodiments disclosed. Many modifications and variations will be apparent to those of ordinary skill in the art without departing from the scope and spirit of the various embodiments described.
The endpoints and any values of the ranges disclosed herein are not limited to the precise range or value, and are understood to encompass values approaching those ranges or values. For numerical ranges, one or more new numerical ranges may be found between the endpoints of each range, between the endpoint of each range and the individual point value, and between the individual point value, in combination with each other, and are to be considered as specifically disclosed herein.
Claims (11)
1. An automatic control method of a hydrogenation reactor before front depropanization, which is characterized by comprising the following steps:
obtaining analysis data based on the obtained parameters of the hydrogenation reactor before the single-stage bed or the final-stage bed front-of-depropanization;
Adjusting the operation parameters of the single-stage bed or the pre-end-stage pre-depropanization hydrogenation reactor based on the analysis data, so that the inlet CO volume content of the single-stage bed or the pre-end-stage pre-depropanization hydrogenation reactor is in a stable state, wherein the stable state is that:
The volume content of CO is within the range of omega+/-100 ppm in the set time, wherein omega is the current real-time analysis value of CO;
Judging whether the volume content of acetylene at the outlet of the hydrogenation reactor before the single-stage bed or the final-stage bed is smaller than a set value omega ppm or not, and adjusting the inlet temperature of the hydrogenation reactor before the single-stage bed or the final-stage bed based on the judging result of the volume content of acetylene; omega has a value ranging from 0.01 to 1.0;
If the volume content of acetylene is greater than or equal to omega ppm, increasing the inlet temperature of the hydrogenation reactor before the single-stage bed or the final-stage bed is subjected to the front-end depropanization;
When the acetylene volume content is smaller than omega ppm, judging whether the conversion rate of methyl acetylene and propadiene in the hydrogenation reactor before the single-stage bed or the final-stage pre-depropanization is within a set range, and adjusting the inlet temperature of the hydrogenation reactor before the single-stage bed or the final-stage pre-depropanization based on the judgment result of the conversion rate of the methyl acetylene and the propadiene;
If the MAPD conversion rate is smaller than the minimum value of the set range, increasing the inlet temperature of the hydrogenation reactor before the single-stage bed or the final-stage bed is subjected to the front-end depropanization; if the MAPD conversion rate is larger than the maximum value of the set range, reducing the inlet temperature of the hydrogenation reactor before the single-stage bed or the final-stage bed front-of-depropanization, wherein MAPD is short for methylacetylene and propadiene;
the setting range is as follows:
The MAPD conversion rate of the hydrogenation reactor before the single-stage bed or the final-stage bed front-of-depropanization is kept in a range of theta+/-5%, wherein theta is a set value of the MAPD conversion rate, and the value range of theta is 40-60%;
The parameters of the obtained hydrogenation reactor before the single-stage bed or the final-stage bed front-end depropanization comprise:
The inlet temperature of the single-stage bed or the end-stage pre-depropanization hydrogenation reactor, the pressure of the single-stage bed or the end-stage pre-depropanization hydrogenation reactor, the inlet material flow of the single-stage bed or the end-stage pre-depropanization hydrogenation reactor, the inlet acetylene concentration of the single-stage bed or the end-stage pre-depropanization hydrogenation reactor, the outlet acetylene concentration of the single-stage bed or the end-stage pre-depropanization hydrogenation reactor, the inlet MAPD concentration of the single-stage bed or the end-stage pre-depropanization hydrogenation reactor, the outlet MAPD concentration of the single-stage bed or the end-stage pre-depropanization hydrogenation reactor and/or the inlet CO concentration of the single-stage bed or the end-stage pre-depropanization hydrogenation reactor;
the adjustment range of the inlet temperature of the hydrogenation reactor before the depropanization of the single-stage bed or the end-stage bed is 35-95 ℃.
2. The method for automatically controlling a pre-depropanization hydrogenation reactor according to claim 1, wherein the value of θ is in the range of 45 to 55%.
3. The method for automatically controlling a pre-depropanization hydrogenation reactor according to claim 1, wherein Ω ranges from 0.2 to 0.8.
4. The method for automatically controlling a pre-depropanization-front hydrogenation reactor according to claim 1, wherein said adjusting the operation parameters of the single-stage bed or the pre-end-bed depropanization-front hydrogenation reactor based on the analysis data so that the inlet CO volume content of the single-stage bed or the pre-end-bed depropanization-front hydrogenation reactor is in a steady state comprises:
and judging whether the volume content of CO at the inlet of the hydrogenation reactor before the single-stage bed or the final-stage bed is in a stable state.
5. The method for automatically controlling a pre-depropanizing hydrogenation reactor according to claim 1, wherein the inlet temperature of the single-stage bed or the final-stage bed pre-depropanizing hydrogenation reactor is adjusted to 55-85 ℃.
6. The method for automatically controlling a pre-depropanization hydrogenation reactor according to claim 1, wherein the adjustment rate of the inlet temperature of the single-stage bed or the pre-depropanization hydrogenation reactor is in the range of 0.5-8 ℃/hr.
7. The method for automatically controlling a pre-depropanization hydrogenation reactor according to claim 6, wherein the adjustment rate of the inlet temperature of the single-stage bed or the pre-depropanization hydrogenation reactor is in the range of 1.0-5.0 ℃/hr.
8. The method for automatically controlling a pre-depropanization hydrogenation reactor according to claim 1, wherein the method for calculating the conversion rate of methylacetylene and propadiene in the single-stage bed or the final-stage bed pre-depropanization hydrogenation reactor is as follows:
；
In the method, in the process of the invention, Is the actual MAPD conversion rate; Is inlet MAPD volume content; Is the outlet MAPD volume content.
9. A process for refining, hydrogenating and removing cracked gas in the separation flow of ethylene cracker is used to remove acetylene and/or MAPD,
The control method according to any one of claims 1 to 8, wherein the separation process is a hydrogenation process before pre-depropanization.
10. The process for the refined hydrodeoxygenation of cracked gas in the separation scheme of an ethylene cracking plant according to claim 9, comprising:
The single-stage bed or the end-stage pre-depropanization hydrogenation reactor is an adiabatic bed or an isothermal bed.
11. The process for the refined hydrogenation removal of cracked gas in the separation scheme of an ethylene cracking plant according to claim 10, wherein the composition of the inlet material of the hydrogenation reactor before the single-stage bed or the final-stage bed front-of-the-propane removal comprises CO, hydrogen, methane, ethylene, ethane, acetylene, propylene, propane and MAPD;
also comprises at least one of C4 fraction and C5+ fraction;
And/or
The hydrogenation reactor before the single-stage bed or the final-stage bed is used for removing propane does not need to be matched with a hydrogenation moderator, and the hydrogenation moderator comprises crude hydrogen and CO.
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| 实时优化技术在碳三加氢反应器上的应用;肖波;石油石化绿色低碳;第5卷(第1期);第1节第1段，第3.1节第1-2段，第3.2节第1段，第4节1-4段，第6节第1段 * |
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