CN113713720A - Method and equipment for controlling propylene selectivity of carbon-three-liquid phase hydrogenation reactor - Google Patents
Method and equipment for controlling propylene selectivity of carbon-three-liquid phase hydrogenation reactor Download PDFInfo
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- C07C5/02—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by hydrogenation
- C07C5/03—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by hydrogenation of non-aromatic carbon-to-carbon double bonds
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- B—PERFORMING OPERATIONS; TRANSPORTING
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- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
- B01J2208/00008—Controlling the process
- B01J2208/00017—Controlling the temperature
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- B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
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Abstract
The invention discloses a method and equipment for controlling propylene selectivity of a carbon-three-liquid phase hydrogenation reactor. The method for controlling the propylene selectivity of the carbon-three-liquid phase hydrogenation reactor comprises the following steps: obtaining parameters of an inlet and an outlet of a carbon three-liquid phase hydrogenation reactor; obtaining the propylene selectivity of the carbon three-liquid phase hydrogenation reactor based on the inlet and outlet parameters; judging whether the propylene selectivity is within a set value range or not; and adjusting corresponding parameters in the inlet and outlet parameters according to the judgment result to ensure that the propylene selectivity is kept within a set value range. The method and the equipment can achieve the aim of improving the selectivity of the propylene.
Description
Technical Field
The invention belongs to the field of petrochemical industry, and particularly relates to a method and equipment for controlling propylene selectivity of a carbon-three-liquid phase hydrogenation reactor.
Background
Ethylene technology is the leading technology of petrochemical industry, and the ethylene technology level is regarded as an important mark for measuring the development level of the petrochemical industry in China. Trienes (ethylene, propylene, butadiene) produced by an ethylene cracking device are basic raw materials of petrochemical industry, and the high and low yield of the trienes is a main mark for measuring the development level of the national petrochemical industry.
In the ethylene cracking device, naphtha and other liquid hydrocarbon raw materials are subjected to steam cracking and separation, and the carbon-three fraction contains propylene, propane and a small amount of propyne and propadiene (MAPD for short), wherein the MAPD content is about 1-5 percent (volume). In propylene polymerization, MAPD reduces the activity of polypropylene catalysts, affecting the product quality of polymer grade propylene. To remove MAPD from the carbon trisection, catalytic selective hydrogenation and solvent absorption methods are currently used in the industry to remove MAPD. The carbon three liquid phase catalytic hydrogenation method has simple process flow and no environmental pollution, so the application of the catalytic hydrogenation method is increasingly common.
The carbon-three liquid phase hydrogenation reactor unit is an important device of a propylene unit recovery system, and selectively hydrogenates MAPD in the carbon-three fraction to propylene under the action of a catalyst. MAPD, if hydrogenated excessively, will produce propane, oligomers and polymers, resulting in loss of propylene; if the hydrogenation effect of MAPD is not good, the concentration of MAPD at the outlet of the reactor is not controlled in the index requirement range, which causes the unqualified product of propylene and influences the production of downstream devices, so the purity and yield of the propylene product are directly influenced by the operation quality of the hydrogenation reactor.
The carbon three liquid phase hydrogenation catalyst generally adopts transition metals such as palladium, nickel and the like as active components, reaction thermodynamic parameters, surface adsorption and desorption reaction rates and process sensitivity of different catalysts are different, and the optimal performance of the catalyst can be ensured by targeted adjustment and optimization.
At present, the production control of the carbon-liquid phase hydrogenation reactor is generally manually regulated and controlled, and technicians manually regulate and control related parameters. Due to the long cracking and separating flow, complex process and limited labor, the carbon-liquid phase hydrogenation reactor cannot be monitored in real time and adjusted and optimized in an expert level. When unstable conditions such as material composition, pressure, temperature, flow, hydrogen fluctuation and the like occur in a carbon-three hydrogenation system, the stability recovery is very slow by only depending on the liquid phase hydrogenation system, and the superposition phenomenon generated by multiple fluctuations makes the system in a metastable state for a long time, so that acetylene leakage at the outlet of a reactor and excessive hydrogenation of propylene are easy to cause, and the yield of the propylene product and the separation effect of a rectifying tower are influenced.
At present, most of the operations of the carbon-three liquid phase hydrogenation reactors adopt manual experience and manual regulation methods, so that the MAPD concentration in the outlet product of the carbon-three liquid phase hydrogenation reactor is too high, and the propylene selectivity is poor.
Disclosure of Invention
In view of the above, the present invention provides a method and an apparatus for controlling propylene selectivity in a carbon-three liquid phase hydrogenation reactor, which at least solve the problem of poor propylene selectivity in the prior art.
In a first aspect, the present invention provides a method for controlling propylene selectivity in a carbon-three liquid phase hydrogenation reactor, comprising:
obtaining parameters of an inlet and an outlet of a carbon three-liquid phase hydrogenation reactor;
obtaining the propylene selectivity of the carbon three-liquid phase hydrogenation reactor based on the inlet and outlet parameters;
judging whether the propylene selectivity is within a set value range or not;
and adjusting corresponding parameters in the inlet and outlet parameters according to the judgment result to ensure that the propylene selectivity is kept within a set value range.
Optionally, the access parameters include:
the method comprises the following steps of (1) the temperature of a material at an inlet of a carbon three-liquid phase hydrogenation reactor, the hydrogen alkyne ratio of the material at the inlet of the carbon three-liquid phase hydrogenation reactor, the pressure of the material at the inlet of the carbon three-liquid phase hydrogenation reactor, the flow rate of the material at the inlet of the carbon three-liquid phase hydrogenation reactor, the hydrogen flow rate at the inlet of the carbon three-liquid phase hydrogenation reactor, the concentration of hydrogen at the inlet of the carbon three-liquid phase hydrogenation reactor, the concentration of propylene at an inlet of the carbon three-liquid phase hydrogenation reactor, the concentration of MAPD at an outlet of the carbon three-liquid phase hydrogenation reactor, and the concentration of MAPD at an outlet of the carbon three-liquid phase hydrogenation reactor.
Optionally, the adjusting, according to the determination result, corresponding parameters in the inlet and outlet parameters to selectively maintain the propylene within a set value range includes:
judging whether the concentration of MAPD at the inlet of the carbon-three liquid phase hydrogenation reactor is a first preset value or not;
if not, adjusting the MAPD concentration at the inlet of the carbon-three liquid phase hydrogenation reactor to a first preset value;
judging whether the concentration of the hydrogen at the inlet of the carbon three-liquid phase hydrogenation reactor is a second preset value;
and if not, adjusting the concentration of the hydrogen at the inlet of the carbon-three liquid phase hydrogenation reactor to be a second preset value.
Optionally, the first preset value is 2.2, the error of the first preset value is ± 0.3%, the error of the first preset value is ± 0.1%, the error of the second preset value is 4.0, the error of the second preset value is ± 0.5%, and the error of the second preset value is ± 0.2%.
Optionally, the adjusting, according to the determination result, corresponding parameters in the inlet and outlet parameters to selectively maintain the propylene within a set value range includes: when the MAPD concentration at the inlet of the carbon three-liquid phase hydrogenation reactor is a first preset value and the hydrogen concentration at the inlet of the carbon three-liquid phase hydrogenation reactor is a second preset value;
when the propylene selectivity is within the set value range, not adjusting corresponding parameters;
when the propylene selectivity is lower than the lower limit value of the set value, reducing the corresponding parameter;
when the propylene selectivity is higher than the upper limit value of the set value, the corresponding parameter is increased.
Optionally, the corresponding parameters include:
the temperature of the material at the inlet of the carbon-three liquid phase hydrogenation reactor and the pressure of the material at the inlet of the carbon-three liquid phase hydrogenation reactor;
the corresponding parameters for the reduction are: reducing the temperature of the material at the inlet of the carbon three-liquid phase hydrogenation reactor and the pressure of the material at the inlet of the carbon three-liquid phase hydrogenation reactor, and preferentially reducing the temperature of the material at the inlet of the carbon three-liquid phase hydrogenation reactor;
and/or
The corresponding parameters are improved as follows: and (3) increasing the temperature of the material at the inlet of the carbon three-liquid phase hydrogenation reactor and the pressure of the material at the inlet of the carbon three-liquid phase hydrogenation reactor, and preferentially increasing the temperature of the material at the inlet of the carbon three-liquid phase hydrogenation reactor.
Optionally, the adjustment range of the temperature of the material at the inlet of the carbon three-liquid phase hydrogenation reactor is 20-65 ℃, and preferably 25-45 ℃.
Optionally, the adjustment rate range of the inlet material temperature of the carbon three-liquid phase hydrogenation reactor is 0.5-8.0 ℃/hour, and preferably 2.0-5.0 ℃/hour.
Optionally, the adjustment range of the pressure of the material at the inlet of the carbon three-liquid phase hydrogenation reactor is 1.0-3.0MPa, and preferably 1.7-2.5 MPa.
Optionally, the adjustment rate range of the material pressure at the inlet of the carbon three-liquid phase hydrogenation reactor is 0.02-0.5 MPa/hour, and preferably 0.05-0.2 MPa/hour.
Optionally, the set value is (x-y)%,
the value range of x and y is 60-90, preferably 75-85.
Optionally, the value range of the difference between y and x is 5-25, preferably 10-15.
Alternatively to this, the first and second parts may,
in a second aspect, the present invention provides an automatic control apparatus for a carbon three liquid phase hydrogenation reactor, comprising:
a memory storing executable instructions;
a processor executing said executable instructions in said memory to implement the method for controlling propylene selectivity in a carbon three liquid phase hydrogenation reactor of any one of the first aspect.
The method analyzes the propylene selectivity of the carbon-three-liquid phase hydrogenation reactor based on the parameters at the inlet and outlet of the carbon-three-liquid phase hydrogenation reactor, and dynamically adjusts corresponding parameters to keep the propylene selectivity within a set interval value, thereby improving the propylene selectivity.
Drawings
Exemplary embodiments of the present invention will be described in more detail by referring to the accompanying drawings.
FIG. 1 shows a flow diagram of a method for controlling propylene selectivity in a carbon three liquid phase hydrogenation reactor according to one embodiment of the present invention;
FIG. 2 illustrates a functional block diagram of an automatic control apparatus for a carbon three liquid phase hydrogenation reactor in accordance with an embodiment of the present invention;
FIG. 3a shows a schematic diagram of a propylene selectivity variation of a control process for propylene selectivity in a carbon three liquid phase hydrogenation reactor according to an embodiment of the present invention;
FIG. 3b shows a schematic of the pressure swing of a control process for propylene selectivity using a carbon three liquid phase hydrogenation reactor according to one embodiment of the present invention;
FIG. 3c shows a schematic of inlet temperature variation for a control process for propylene selectivity in a reactor employing a carbon three liquid phase hydrogenation according to an embodiment of the present invention;
FIG. 3d shows a graphical representation of a control process outlet MAPD variation for propylene selectivity in a reactor employing a carbon three liquid phase hydrogenation in accordance with an embodiment of the present invention;
figure 4 shows a prior art outlet MAPD concentration schematic for a carbon three liquid phase hydrogenation reactor.
Detailed Description
The following describes in detail specific embodiments of the present invention. It should be understood that the detailed description and specific examples, while indicating the present invention, are given by way of illustration and explanation only, not limitation.
The present invention will be further described with reference to the following examples, but the scope of the present invention is not limited to these examples.
Methylacetylene and propyne are the same substance;
MAPD concentration is the volume content of Methyl Acetylene (MA) and Propadiene (PD) at the inlet of the carbon-three hydrogenation reactor;
the hydrogen concentration is the volume content of the hydrogen at the inlet of the carbon-three hydrogenation reactor;
the temperature of the material at the inlet of the carbon-three liquid phase hydrogenation reactor is simply referred to as the material temperature;
the hydrogen-alkyne ratio of the inlet material of the carbon-three liquid phase hydrogenation reactor is simply called as the hydrogen-alkyne ratio;
the material pressure at the inlet of the carbon-three liquid phase hydrogenation reactor is simply referred to as the material pressure;
the material flow at the inlet of the carbon-three-liquid phase hydrogenation reactor is simply called material flow;
the MAPD concentration at the inlet of the carbon-three liquid phase hydrogenation reactor is referred to as inlet MAPD concentration for short;
the hydrogen flow at the inlet of the carbon-three liquid phase hydrogenation reactor is simply referred to as hydrogen flow;
the concentration of hydrogen at the inlet of the carbon-three liquid phase hydrogenation reactor is simply referred to as hydrogen concentration;
the outlet MAPD concentration of the carbon-three liquid phase hydrogenation reactor is simply referred to as the outlet MAPD concentration.
The operating conditions affecting the carbon three liquid phase hydrogenation reactor mainly comprise: inlet MAPD concentration, hydrogen concentration, feed temperature and feed pressure. In order to obtain the optimal selectivity of the carbon three liquid phase hydrogenation reactor, the following methods can be adopted: the inlet MAPD and hydrogen concentration are stably kept in a certain range, and proper material temperature and material pressure are selected.
The first embodiment is as follows:
as shown in fig. 1, a method for controlling propylene selectivity in a carbon-three liquid phase hydrogenation reactor comprises:
step S101: obtaining parameters of an inlet and an outlet of a carbon three-liquid phase hydrogenation reactor;
access parameters including: the method comprises the following steps of (1) the temperature of a material at an inlet of a carbon three-liquid phase hydrogenation reactor, the hydrogen alkyne ratio of the material at the inlet of the carbon three-liquid phase hydrogenation reactor, the pressure of the material at the inlet of the carbon three-liquid phase hydrogenation reactor, the flow rate of the material at the inlet of the carbon three-liquid phase hydrogenation reactor, the hydrogen flow rate at the inlet of the carbon three-liquid phase hydrogenation reactor, the concentration of hydrogen at the inlet of the carbon three-liquid phase hydrogenation reactor, the concentration of propylene at an inlet of the carbon three-liquid phase hydrogenation reactor, the concentration of MAPD at an outlet of the carbon three-liquid phase hydrogenation reactor, and the concentration of MAPD at an outlet of the carbon three-liquid phase hydrogenation reactor.
Step S102: obtaining the propylene selectivity of the carbon three-liquid phase hydrogenation reactor based on the inlet and outlet parameters;
step S103: judging whether the propylene selectivity is within a set value range or not;
step S104: and adjusting corresponding parameters in the inlet and outlet parameters according to the judgment result to ensure that the propylene selectivity is kept within a set value range.
Optionally, the adjusting, according to the determination result, corresponding parameters in the inlet and outlet parameters to selectively maintain the propylene within a set value range includes:
judging whether the concentration of MAPD at the inlet of the carbon-three liquid phase hydrogenation reactor is a first preset value or not;
if not, adjusting the MAPD concentration at the inlet of the carbon-three liquid phase hydrogenation reactor to a first preset value;
judging whether the concentration of the hydrogen at the inlet of the carbon three-liquid phase hydrogenation reactor is a second preset value;
and if not, adjusting the concentration of the hydrogen at the inlet of the carbon-three liquid phase hydrogenation reactor to be a second preset value.
Optionally, the first preset value is 2.2, the error of the first preset value is ± 0.3%, the error of the first preset value is ± 0.1%, the error of the second preset value is 4.0, the error of the second preset value is ± 0.5%, and the error of the second preset value is ± 0.2%.
Optionally, the adjusting, according to the determination result, corresponding parameters in the inlet and outlet parameters to selectively maintain the propylene within a set value range includes: when the MAPD concentration at the inlet of the carbon three-liquid phase hydrogenation reactor is a first preset value and the hydrogen concentration at the inlet of the carbon three-liquid phase hydrogenation reactor is a second preset value;
when the propylene selectivity is within the set value range, not adjusting corresponding parameters;
when the propylene selectivity is lower than the lower limit value of the set value, reducing the corresponding parameter;
when the propylene selectivity is higher than the upper limit value of the set value, the corresponding parameter is increased.
Optionally, the corresponding parameters include:
the temperature of the material at the inlet of the carbon-three liquid phase hydrogenation reactor and the pressure of the material at the inlet of the carbon-three liquid phase hydrogenation reactor;
the corresponding parameters for the reduction are: reducing the temperature of the material at the inlet of the carbon three-liquid phase hydrogenation reactor and the pressure of the material at the inlet of the carbon three-liquid phase hydrogenation reactor, and preferentially reducing the temperature of the material at the inlet of the carbon three-liquid phase hydrogenation reactor;
and/or
The corresponding parameters are improved as follows: and (3) increasing the temperature of the material at the inlet of the carbon three-liquid phase hydrogenation reactor and the pressure of the material at the inlet of the carbon three-liquid phase hydrogenation reactor, and preferentially increasing the temperature of the material at the inlet of the carbon three-liquid phase hydrogenation reactor.
(x-y)% represents a propylene selectivity control interval from x% to y%, wherein x% is the lower propylene selectivity limit and y% is the upper propylene selectivity limit.
(a) Firstly, stably keeping the MAPD concentration at the inlet of the reactor at 2.2 +/-0.3%, preferably at 2.2 +/-0.1%, and keeping the hydrogen concentration at 4.0 +/-0.5%, preferably at 4.0 +/-0.2%; if the MAPD concentration or the hydrogen concentration at the inlet of the carbon three-hydrogenation reactor is not in the required range, the adjustment is respectively carried out until the MAPD concentration at the inlet of the carbon three-hydrogenation reactor reaches the required range of 2.2 +/-0.3 percent and the hydrogen concentration reaches 4.0 +/-0.5 percent.
(b) When the selectivity of the propylene reaches (x-y)%, the material temperature or the material pressure is not adjusted;
(c) when the propylene selectivity is lower than x%, reducing the material temperature and the material pressure, and preferentially reducing the material temperature until the propylene selectivity reaches (x-y)%;
(d) when the propylene selectivity is higher than y%, the material temperature and the material pressure are increased, and the material temperature is preferentially increased until the propylene selectivity reaches (x-y)%.
Optionally, the adjustment range of the temperature of the material at the inlet of the carbon three-liquid phase hydrogenation reactor is 20-65 ℃, and preferably 25-45 ℃.
The specific material temperature may be: 20 deg.C, 25 deg.C, 30 deg.C, 35 deg.C, 40 deg.C, 45 deg.C, 55 deg.C, 60 deg.C or 65 deg.C, etc.
Optionally, the adjustment rate range of the inlet material temperature of the carbon three-liquid phase hydrogenation reactor is 0.5-8.0 ℃/hour, and preferably 2.0-5.0 ℃/hour.
The specific material temperature adjustment rate may be: 0.5 deg.C/hr, 1.0 deg.C/hr, 1.5 deg.C/hr, 2.0 deg.C/hr, 2.5 deg.C/hr, 2.0 deg.C/hr, 3.5 deg.C/hr, 4.0 deg.C/hr, 5.5 deg.C/hr, 6.0 deg.C/hr, 6.5 deg.C/hr, 7.0 deg.C/hr, 7.5 deg.C/hr, 8.0 deg.C/hr, etc.
Optionally, the adjustment range of the pressure of the material at the inlet of the carbon three-liquid phase hydrogenation reactor is 1.0-3.0MPa, and preferably 1.7-2.5 MPa.
The specific material pressure may be: 1.0MPa, 1.5MPa, 2.0MPa, 2.5MPa or 3.0 MPa.
Optionally, the adjustment rate range of the material pressure at the inlet of the carbon three-liquid phase hydrogenation reactor is 0.02-0.5 MPa/hour, and preferably 0.05-0.2 MPa/hour.
The specific material pressure adjustment rate may be: 0.02 MPa/hr, 0.03 MPa/hr, 0.05 MPa/hr, 0.07 MPa/hr, 0.1 MPa/hr, 0.12 MPa/hr, 0.18 MPa/hr, 0.2 MPa/hr, 0.23 MPa/hr, 0.29 MPa/hr, 0.3 MPa/hr, 0.35 MPa/hr, 0.37 MPa/hr, 0.4 MPa/hr, 0.41 MPa/hr, 0.47 MPa/hr, 0.5 MPa/hr, etc.
Optionally, the set value is (x-y)%,
the value range of x and y is 60-90, preferably 75-85.
Optionally, the value range of the difference between y and x is 5-25, preferably 10-15.
Specifically, when y is 90, x may have a value of 65, 75, 80, 85, or the like.
When y is 85, x may have a value of 60, 68, 70, 73, 75, 80, etc.
When y is 80, the value of x may be 55, 65, 70, 75, etc.
When y is 75, the value of x may be 50, 60, 65, 70, etc.
When y is 65, the value of x may be 40, 50, 55, 60, etc.
When y is 60, the value of x may be 35, 45, 50, 55, etc.
And the selectivity of propylene is calculated according to the full analysis data of the inlet and the outlet of the carbon-three-liquid phase hydrogenation reactor, and the temperature and the pressure of the inlet material in the carbon-three-liquid phase hydrogenation reactor are automatically adjusted. When the propylene selectivity exceeds the upper and lower limits, simultaneous adjustment of both operating parameters may be undertaken, at a rate that is at the lower end of the adjustable range.
The adjustment range of the inlet material temperature of the carbon three hydrogenation reactor is 20-65 ℃, and the preferable range is 25-45 ℃; the adjustment range of the inlet material pressure of the carbon three hydrogenation reactor is 1.0-3.0MPa, and preferably 1.7-2.5 MPa. If an operating parameter reaches an upper limit, the parameter is kept unchanged, and another operating variable is adjusted. If the material temperature and the material pressure reach the upper limit and can not meet the requirement of propylene selectivity, the operation mode is automatically switched into a manual mode and an alarm is given.
One of the self-control standards of the carbon three liquid phase hydrogenation reactor is that the inlet MAPD concentration and the hydrogen concentration are carried out according to the standard that the inlet MAPD concentration is 2.2 +/-0.3 percent, preferably 2.2 +/-0.1 percent and the inlet hydrogen concentration is 4.0 +/-0.5 percent, preferably 4.0 +/-0.2 percent; the second automatic control standard of the carbon-three liquid phase hydrogenation reactor is propylene selectivity, and the propylene selectivity is implemented according to the standard that the propylene selectivity is greater than x% and less than y%. The assignment of x and y is modified according to the specific control index of the production device, and the value range of x and y is 0-100, preferably 40-90; y is greater than x; the value of the subtraction of b and a is in the range of 5-25, preferably 10-20.
In the automatic control process of the carbon-liquid phase hydrogenation reactor, the adjustment rate range of the inlet material temperature of the carbon-liquid phase hydrogenation reactor is generally 0.5-8.0 ℃/hour, preferably 2.0-5.0 ℃/hour; the adjustment rate range of the inlet material pressure of the carbon three hydrogenation reactor is 0.02-0.5 MPa/h, and preferably 0.05-0.2 MPa/h. When propylene selectivity is below x% or above y%, simultaneous adjustments to both operating parameters can be used, typically at the lower end of the adjustable rate range. If the propylene selectivity is between (x-y)% the operation is generally not adjusted to maintain the smoothness of the production operation.
Example two:
as shown in fig. 2, an automatic control device for a carbon three-liquid phase hydrogenation reactor comprises: a control server, a network equipment system control network, an embedded server and the like,
the control server at least comprises a memory which stores executable instructions;
a processor executing the executable instructions in the memory to implement the method for controlling propylene selectivity in a carbon three liquid phase hydrogenation reactor of embodiment one.
The controller is positioned in a distributed control system or an upper layer server of the carbon-liquid phase hydrogenation reactor.
The controller (processor) is positioned in a distributed control system (namely a DCS system) of the carbon-three liquid phase hydrogenation reactor or a server connected with the DCS, a control logic program in the controller acquires all-component analysis data at the inlet and the outlet of the reactor, automatically acquires analysis result data, stores the analysis result data in a fixed memory unit (storage) and calculates the real-time propylene selectivity.
The control is divided into two steps: a program initialization phase and an automatic control phase. The execution sequence of the automatic control program is as follows:
1. a program initialization stage:
after the program is started, initializing internal variables of inlet material temperature, material pressure, material flow and hydrogen flow of the carbon-three liquid phase hydrogenation reactor, automatically identifying inlet and outlet analysis data signals and calculating propylene selectivity.
And confirming that all field operations are executed by an operator, inputting normal field analysis data, and preparing to enter an automatic control stage, wherein if the field analysis data are not confirmed, the program is in a waiting state until all the field analysis data are confirmed. And (4) clicking by an operator to assign values of x% and y% of the upper and lower limits of the propylene selectivity and confirming, and then entering an automatic control stage.
2. Self-control phase
After entering the dynamic control program, the control logic program judges whether each control variable in the hydrogenation reactor needs to be adjusted or not by acquiring field data and input inlet MAPD concentration, hydrogen concentration and propylene selectivity data according to a DCS system of the carbon-three-liquid phase hydrogenation reactor and judging every 1-1800 seconds according to a judgment principle, thereby realizing the automatic control of each parameter in the production process of the carbon-three-liquid phase hydrogenation reactor. The shorter the time interval for adjusting the parameters, 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 taken into account.
And adding a controller connected with an OPC server of the original system outside the original DCS, adjusting the process conditions of the carbon-III hydrogenation reactor, and providing the adjustment target to the original DCS in real time so as to realize the control of the carbon-III hydrogenation reactor.
Firstly, selectively assigning values to propylene of a carbon three-liquid phase hydrogenation reactor of a new controller, wherein the lower limit is 75% and the upper limit is 80%, and ensuring that the concentration of MAPD at the inlet of the carbon three-liquid phase hydrogenation reactor is in the range of 2.0-2.4 mol% and the concentration of hydrogen is 3.8-4.2 mol% by regulating and controlling the new controller, as shown in the graph from 3a to 3d, an online control unit automatically controls the temperature of the material at the inlet of the hydrogenation reactor and the pressure of the material to be regulated in real time. The catalyst selectivity of the carbon-three hydrogenation reactor can be stably maintained at 75%, and meanwhile, the outlet MAPD can be maintained in a qualified state.
Comparative example:
a total of 8 cracking furnaces are used in an olefin plant producing 22 million tons of ethylene every year, and various cracking raw materials from ethane to hydrogenated tail oil can be processed, and 12 million tons of propylene are produced every year. The separation process of the plant adopts a sequential separation flow, a carbon-three-liquid phase hydrogenation reactor is positioned between a hot zone depropanizing tower and a propylene rectifying tower, the carbon-three fraction obtained from the top of the high-pressure depropanizing tower is subjected to heat exchange by a cooler (or a preheater) to reach a required temperature, is subjected to pressure rise by a feed pump, enters a hydrogenation reactor through a raw material dearsenizer, is mixed with hydrogen with a certain hydrogen alkyne ratio in a pipeline, and enters a catalytic bed layer of the reactor for selective hydrogenation reaction, and the carbon-three-liquid phase hydrogenation process of the plant is a liquid phase hydrogenation process.
As shown in fig. 4, when the carbon three reactor of the plant is operated, the inlet material temperature is adjusted by manually controlling the flow rate of cold and hot materials in front of the carbon three reactor through a DCS system; controlling the flow of the prepared hydrogen and adjusting the concentration of the inlet hydrogen. The alkyne concentration in the material flow is measured by the on-line chromatogram of the outlet of the carbon three hydrogenation reactor, the MAPD concentration at the outlet of the carbon three hydrogenation reactor is ensured to be qualified (below 500 ppm), and the selectivity of the catalyst of the carbon three hydrogenation reactor is maintained at 40-50 percent.
The comparison results show that: compared with the manual control of the original factory, the method and the system can obviously improve the propylene selectivity of the carbon three liquid phase hydrogenation catalyst.
Having described embodiments of the present invention, the foregoing description is intended to be exemplary, not exhaustive, and not 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 described embodiments.
The endpoints of the ranges and any values disclosed herein are not limited to the precise range or value, and such ranges or values should be understood to encompass values close to those ranges or values. For ranges of values, between the endpoints of each of the ranges and the individual points, and between the individual points may be combined with each other to give one or more new ranges of values, and these ranges of values should be considered as specifically disclosed herein.
Claims (14)
1. A method for controlling propylene selectivity of a carbon-three-liquid phase hydrogenation reactor is characterized by comprising the following steps:
obtaining parameters of an inlet and an outlet of a carbon three-liquid phase hydrogenation reactor;
obtaining the propylene selectivity of the carbon three-liquid phase hydrogenation reactor based on the inlet and outlet parameters;
judging whether the propylene selectivity is within a set value range or not;
and adjusting corresponding parameters in the inlet and outlet parameters according to the judgment result to ensure that the propylene selectivity is kept within a set value range.
2. The method for controlling propylene selectivity in a carbon three liquid phase hydrogenation reactor according to claim 1, wherein the inlet and outlet parameters comprise:
the method comprises the following steps of (1) the temperature of a material at an inlet of a carbon three-liquid phase hydrogenation reactor, the hydrogen alkyne ratio of the material at the inlet of the carbon three-liquid phase hydrogenation reactor, the pressure of the material at the inlet of the carbon three-liquid phase hydrogenation reactor, the flow rate of the material at the inlet of the carbon three-liquid phase hydrogenation reactor, the hydrogen flow rate at the inlet of the carbon three-liquid phase hydrogenation reactor, the concentration of hydrogen at the inlet of the carbon three-liquid phase hydrogenation reactor, the concentration of propylene at an inlet of the carbon three-liquid phase hydrogenation reactor, the concentration of MAPD at an outlet of the carbon three-liquid phase hydrogenation reactor, and the concentration of MAPD at an outlet of the carbon three-liquid phase hydrogenation reactor.
3. The method for controlling the selectivity of propylene in the carbon-three liquid phase hydrogenation reactor according to claim 2, wherein the adjusting the corresponding parameters of the inlet and outlet parameters according to the judgment result to keep the selectivity of propylene within the range of the set value comprises:
judging whether the concentration of MAPD at the inlet of the carbon-three liquid phase hydrogenation reactor is a first preset value or not;
if not, adjusting the MAPD concentration at the inlet of the carbon-three liquid phase hydrogenation reactor to a first preset value;
judging whether the concentration of the hydrogen at the inlet of the carbon three-liquid phase hydrogenation reactor is a second preset value;
and if not, adjusting the concentration of the hydrogen at the inlet of the carbon-three liquid phase hydrogenation reactor to be a second preset value.
4. The method of claim 3, wherein the first predetermined value is 2.2, the error of the first predetermined value is ± 0.3%, the error of the first predetermined value is ± 0.1%, the error of the second predetermined value is 4.0%, the error of the second predetermined value is ± 0.5%, and the error of the second predetermined value is ± 0.2%.
5. The method for controlling the propylene selectivity of a carbon three liquid phase hydrogenation reactor according to claim 3,
the adjusting corresponding parameters in the inlet and outlet parameters according to the judgment result to ensure that the propylene selectivity is kept within a set value range comprises the following steps: when the MAPD concentration at the inlet of the carbon three-liquid phase hydrogenation reactor is a first preset value and the hydrogen concentration at the inlet of the carbon three-liquid phase hydrogenation reactor is a second preset value;
when the propylene selectivity is within the set value range, not adjusting corresponding parameters;
when the propylene selectivity is lower than the lower limit value of the set value, reducing the corresponding parameter;
when the propylene selectivity is higher than the upper limit value of the set value, the corresponding parameter is increased.
6. The method for controlling propylene selectivity in a carbon three liquid phase hydrogenation reactor according to claim 5, wherein the corresponding parameters comprise:
the temperature of the material at the inlet of the carbon-three liquid phase hydrogenation reactor and the pressure of the material at the inlet of the carbon-three liquid phase hydrogenation reactor;
the corresponding parameters for the reduction are: reducing the temperature of the material at the inlet of the carbon three-liquid phase hydrogenation reactor and the pressure of the material at the inlet of the carbon three-liquid phase hydrogenation reactor, and preferentially reducing the temperature of the material at the inlet of the carbon three-liquid phase hydrogenation reactor;
and/or
The corresponding parameters are improved as follows: and (3) increasing the temperature of the material at the inlet of the carbon three-liquid phase hydrogenation reactor and the pressure of the material at the inlet of the carbon three-liquid phase hydrogenation reactor, and preferentially increasing the temperature of the material at the inlet of the carbon three-liquid phase hydrogenation reactor.
7. The method for controlling the propylene selectivity of a carbon three liquid phase hydrogenation reactor according to claim 6,
the adjusting range of the temperature of the material at the inlet of the carbon-three liquid phase hydrogenation reactor is 20-65 ℃, and the preferable temperature is 25-45 ℃.
8. The method for controlling the propylene selectivity of a carbon three liquid phase hydrogenation reactor according to claim 6 or 7,
the adjusting rate range of the temperature of the material at the inlet of the carbon three-liquid phase hydrogenation reactor is 0.5-8.0 ℃/hour, and preferably 2.0-5.0 ℃/hour.
9. The method for controlling the propylene selectivity of a carbon three liquid phase hydrogenation reactor according to claim 6,
the adjustment range of the pressure of the material at the inlet of the carbon three-liquid phase hydrogenation reactor is 1.0-3.0MPa, and preferably 1.7-2.5 MPa.
10. The method for controlling the propylene selectivity of a carbon three liquid phase hydrogenation reactor according to claim 6 or 9,
the adjustment rate range of the material pressure at the inlet of the carbon three-liquid phase hydrogenation reactor is 0.02-0.5 MPa/h, and preferably 0.05-0.2 MPa/h.
11. The method of claim 1, wherein the set point is (x-y)%,
the value range of x and y is 60-90, preferably 75-85.
12. The method for controlling the propylene selectivity in a carbon three liquid phase hydrogenation reactor according to claim 11,
the value range of the difference between y and x is 5-25, preferably 10-15.
13. The method for controlling the propylene selectivity of a carbon three liquid phase hydrogenation reactor according to claim 1,
14. an automatic control equipment of a carbon three-liquid phase hydrogenation reactor is characterized by comprising:
a memory storing executable instructions;
a processor executing said executable instructions in said memory to implement the method of controlling propylene selectivity in a carbon three liquid phase hydrogenation reactor of any one of claims 1 to 13.
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