An energy-saving dimethyl ether high-efficiency vaporization mixing method using CO as carrier gas

Abstract

The invention discloses an energy-saving dimethyl ether efficient vaporization and mixing method using CO as carrier gas, and relates to the technical field of dimethyl ether vaporization. In the process of injecting gaseous CO and gaseous dimethyl ether into a carbonylation reactor, a transfer structure of a transfer gas bin is added to "isolate" the dimethyl ether vaporizer and the carbonylation reactor to avoid mutual influence and interference between the temperature environment and pressure of the two. The essence of the method is to "pre-mix" the gaseous CO and the gaseous dimethyl ether. On this basis, a first-order equilibrium model, a second-order equilibrium model and a third-order equilibrium model are set. Based on the pressure and temperature changes of the three, the mixing process and the injection process of the gaseous CO and the gaseous dimethyl ether are maintained in an interrelated manner on the basis that the temperature / pressure does not actively influence and interfere. Specifically, the third-order equilibrium model is used as a front step, and the temperature of the dimethyl ether and the amount of gas added to the carbonylation reactor by the mixed gas are controlled by balancing the fluctuation value to maintain the overall vaporization and carbonyl reaction process.

Description

Technical Field

[0001] The invention relates to the technical field of dimethyl ether vaporization, and in particular to an energy-saving dimethyl ether high-efficiency vaporization mixing method using CO as carrier gas. Background Art

[0002] Using methanol produced by the coke oven gas comprehensive utilization project as raw material, ethanol is synthesized through a series of chemical reactions such as carbonylation and hydrogenation. In essence, ethanol is produced by the dimethyl ether method. High-purity CO and hydrogen are obtained through gas separation technology. Methanol is dehydrated and separated to obtain dimethyl ether. After dimethyl ether is vaporized, it is mixed with CO and enters the carbonylation reactor to produce methyl acetate.

[0003] Factors that affect the carbonylation reaction include: temperature, time, pressure and pH value. In particular, the temperature and pressure are explained as follows: the carbonyl synthesis reaction temperature ranges from 150-250°C, and the reaction pressure ranges from 1.0 to 2.5 MPa. a However, the vaporization temperature of dimethyl ether is much lower than the reaction temperature of carbonyl synthesis, and the vaporization pressure is also different from the reaction pressure. Then, when gaseous dimethyl ether mixed with CO enters the carbonylation reactor, it will not only affect the temperature and pressure inside the carbonylation reactor, but also indirectly affect the temperature and pressure inside the dimethyl ether vaporizer, directly affecting the vaporization process and the carbonylation reaction process, such as affecting the product generation efficiency and product purity.

[0004] To this end, this application proposes a solution. Summary of the invention

[0005] The object of the present invention is to provide an energy-saving and efficient dimethyl ether vaporization and mixing method using CO as a carrier gas. When CO and gaseous dimethyl ether are mixed and introduced into a carbonylation reactor for carbonylation reaction, since there is an obvious difference between the temperature / pressure in the dimethyl ether vaporization process and the temperature / pressure inside the carbonylation reactor, in the process of direct mixing and gas injection, the temperature / pressure inside the dimethyl ether vaporizer and the carbonylation reactor interfere with each other, directly affecting the product generation efficiency and product purity.

[0006] The object of the present invention can be achieved by the following technical scheme: an energy-saving dimethyl ether efficient vaporization and mixing method using CO as a carrier gas, comprising a dimethyl ether vaporizer, a carbonylation reactor, a CO gas storage tank, a transfer gas bin and a control system, wherein the dimethyl ether vaporizer and the CO gas storage tank respectively inject gaseous dimethyl ether and gaseous CO into the transfer gas bin to form a mixed gas in the transfer gas bin, and the mixed gas is injected into the carbonylation reactor for a carbonylation reaction process, the dimethyl ether vaporizer and the CO gas storage tank are connected to a primary pipeline corresponding to the transfer gas bin, the transfer gas bin is connected to a secondary pipeline corresponding to the carbonylation reactor, the primary pipeline corresponding to the dimethyl ether vaporizer and the CO gas storage tank is respectively provided with a first node and a second node, and the secondary pipeline is provided with a third node;

[0007] The control system is composed of a data integration unit, a data hierarchical analysis unit and a collaborative control unit. The data integration unit is used to collect dynamic data, variable data and basic data, and input the dynamic data and variable data into the data hierarchical analysis unit.

[0008] In the data classification analysis unit, a first-order balance model associated with the first node is established with dynamic data, a third-order balance model associated with the third node is established with dynamic data, and a second-order balance model associated with the transfer gas tank is established with basic data and the first-order balance model, and the first-order balance model, the second-order balance model and the third-order balance model are respectively substituted into the collaborative control unit;

[0009] In the collaborative control unit, the third-order balance model is used as the preceding step, and the preceding calculation process in the third-order balance model associated with the second-order balance model is established. The balance fluctuation value is obtained in the preceding calculation process, and the balance fluctuation value is substituted into the second-order balance model and the first-order model, and the first node, the second node and the third node are controlled respectively to perform node collaborative actions.

[0010] It is further set as follows: the dynamic data are used to represent the temperature value and pressure value in the dimethyl ether vaporizer and the carbonylation reactor respectively, and T a , P a Indicates the temperature and pressure values ​​in the dimethyl ether vaporizer, T b , P b The variable data is used to represent the temperature and pressure values ​​in the carbonylation reactor. The variable data is used to represent the temperature and pressure values ​​in the transfer gas warehouse, which are represented by T0 and P0. The basic data represents the initial temperature of the gaseous CO in the CO storage tank, which is represented by T c To express.

[0011] It is further set as follows: In the first-order equilibrium model, T a Preset normal temperature value The calculation method for establishing the first-order equilibrium model M is: Among them As the pressure value of gaseous dimethyl ether, M is the first-order equilibrium value, and the second-order equilibrium model is established as m a , C a 、m b , C b They respectively represent the mass and specific heat capacity of gaseous dimethyl ether and gaseous CO injected into the transfer gas warehouse.

[0012] It is further set as follows: In the previous step, according to T b , P b Establish real-time curves of temperature value-reaction time and pressure value-reaction time respectively, and preset Tb and the average temperature b in P and the average pressure are respectively established in two real-time curve graphs with T b , and with P b between the balanced fluctuation values, which are respectively expressed as

[0013] It is further set that proximity values 0.09 and 0.13 are respectively established in X t and Y t , and the first-order balance values in the first-order balance model are substituted, and the node collaborative actions are set as follows:

[0014] A1: When 0 < X t < 0.09 and 0 < Y t < 0.13, the node collaborative action is not executed; when Y t > 0.13, the gas quantity Q t supplied to the carbonylation reactor per unit time of the mixed gas is set, and the gas quantity in the second-order balance model is optimized to Q t *(1 + Y t - 0.13) by using the third-order balance model;

[0015] A2: When X t > 0 and Y t < 0, the gas quantity in the second-order balance model is optimized to Q t *(1 - Y t + 0.13) by using the third-order balance model, and when X t > 0.09, the temperature of the mixed gas in the transfer gas storage bin is optimized to T0*(1 - X t + 0.09), and the T a in the dimethyl ether vaporizer is adjusted in the reverse direction;

[0016] A3: When X t < 0 and Y t > 0, the temperature of the mixed gas is optimized to T0*(1 + X t + 0.09), and the T a in the dimethyl ether vaporizer is adjusted in the reverse direction;

[0017] A4: When X t < 0 and Y t < 0, it indicates that the inside of the carbonylation reactor is in an environment state of too high temperature and too high pressure, and the gas quantity of the transfer gas to the carbonylation reactor and the temperature of the mixed gas are reduced simultaneously according to A1 to A3.

[0018] The present invention has the following beneficial effects:

[0019] 1. In view of the process of injecting gaseous CO and gaseous dimethyl ether into the carbonylation reactor for carbonylation reaction, a transfer structure of a transfer gas warehouse is added. Its essence is to "isolate" the dimethyl ether vaporizer and the carbonylation reactor, and avoid the interference caused by the temperature and pressure differences in the operating environment of the two by "pre-mixing" the gaseous CO and gaseous dimethyl ether. In this process, the temperature and pressure conditions of the mixed gas obtained by mixing the gaseous CO and gaseous dimethyl ether are relatively stable, and can be maintained and controlled by the gas volume and the temperature of the gaseous dimethyl ether during the injection process of the gaseous CO and gaseous dimethyl ether;

[0020] 2. In combination with the above content, it is explained again that in the overall process, for the mixing process of gaseous CO and gaseous dimethyl ether and the process of injecting them into the carbonylation reactor, a first-order equilibrium model, a second-order equilibrium model and a third-order equilibrium model are added. The three models will not actively influence and interfere with each other, but the third-order equilibrium model is used as the preceding step, specifically based on the temperature and pressure in the carbonylation reactor and the corresponding equilibrium fluctuation values ​​of the temperature and pressure are set, so as to control the temperature of dimethyl ether and the amount of gas added to the carbonylation reactor in an inversely correlated manner, thereby maintaining the overall vaporization and carbonyl reaction process in a relatively balanced state. BRIEF DESCRIPTION OF THE DRAWINGS

[0021] In order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the drawings required for use in the embodiments or the description of the prior art will be briefly introduced below. Obviously, the drawings described below are only some embodiments of the present invention. For ordinary technicians in this field, other drawings can be obtained based on these drawings without paying creative work.

[0022] Figure 1 This is a connection diagram of an energy-saving dimethyl ether efficient vaporization mixing method using CO as a carrier gas proposed by the present invention;

[0023] Figure 2 A schematic diagram of an energy-saving dimethyl ether high-efficiency vaporization and mixing method using CO as a carrier gas proposed by the present invention;

[0024] Figure 3 A real-time curve diagram of the temperature value in the carbonylation reactor in an energy-saving dimethyl ether high-efficiency vaporization mixing method using CO as a carrier gas proposed by the present invention;

[0025] Figure 4 A real-time curve diagram of the pressure value in the carbonylation reactor in an energy-saving dimethyl ether efficient vaporization mixing method using CO as a carrier gas proposed by the present invention;

[0026] Figure 5The present invention provides an operating block diagram of a control system in an energy-saving dimethyl ether efficient vaporization and mixing method using CO as a carrier gas. DETAILED DESCRIPTION

[0027] The technical solution of the present invention will be clearly and completely described below in conjunction with the embodiments. Obviously, the described embodiments are only part of the embodiments of the present invention, rather than all of the embodiments. Based on the embodiments of the present invention, all other embodiments obtained by ordinary technicians in this field without creative work are within the scope of protection of the present invention.

[0028] Embodiment 1: For the carbonylation reaction process of dimethyl ether mixed with CO, there is a significant difference between the temperature / pressure during the dimethyl ether vaporization process and the temperature / pressure inside the carbonylation reactor. In the process of direct mixed gas injection, the temperature / pressure inside the dimethyl ether vaporizer and the carbonylation reactor interfere with each other, directly affecting the product generation efficiency and product purity. The following technical solution is proposed:

[0029] Reference Figure 1 to Figure 5 In this embodiment, an energy-saving dimethyl ether efficient vaporization and mixing method using CO as a carrier gas includes a dimethyl ether vaporizer, a carbonylation reactor, a CO gas storage tank, a transfer gas bin and a control system. The dimethyl ether vaporizer and the CO gas storage tank respectively inject gaseous dimethyl ether and gaseous CO into the transfer gas bin to form a mixed gas in the transfer gas bin, and the mixed gas is injected into the carbonylation reactor. The dimethyl ether vaporizer and the CO gas storage tank are connected to a primary pipeline corresponding to the transfer gas bin, and the transfer gas bin is connected to a secondary pipeline corresponding to the carbonylation reactor, and both the primary pipeline and the secondary pipeline are connected to a solenoid valve;

[0030] A first node and a second node are respectively arranged on the primary pipeline corresponding to the dimethyl ether vaporizer and the CO gas storage tank, and a third node is arranged on the secondary pipeline. The control system has control authority over the first node, the second node and the third node, and the control system is composed of a data integration unit, a data hierarchical analysis unit and a collaborative control unit. The data integration unit is used to collect dynamic data in the dimethyl ether vaporizer and the carbonylation reactor, variable data in the transfer gas warehouse and basic data in the CO gas storage tank. The variable data is composed of basic data and dynamic data in the dimethyl ether vaporizer converted, and the dynamic data and variable data are input into the data hierarchical analysis unit;

[0031] In the data classification analysis unit, a first-order equilibrium model associated with the first node is established with the dynamic data in the dimethyl ether vaporizer, a third-order equilibrium model associated with the third node is established with the dynamic data in the carbonylation reactor, and a second-order equilibrium model associated with the transfer gas warehouse is established with the basic data in the CO gas storage tank and the first-order equilibrium model, and the first-order equilibrium model, the second-order equilibrium model and the third-order equilibrium model are respectively substituted into the collaborative control unit;

[0032] In the collaborative control unit, the third-order balance model is used as the preceding step, and the preceding calculation process in the third-order balance model associated with the second-order balance model is established. The balance fluctuation value is obtained in the preceding calculation process, and the balance fluctuation value is substituted into the second-order balance model and the first-order model, and the first node, the second node and the third node are controlled respectively to perform node collaborative actions.

[0033] Basic principle: First of all, it should be explained that: Figure 2 As shown, the essence of the overall solution is that the CO gas storage tank and the dimethyl ether vaporizer continuously inject gaseous CO and gaseous dimethyl ether into the transfer gas bin through the primary pipeline to form a mixed gas in the transfer gas bin, and the mixed gas is finally injected into the carbonylation reactor through the secondary pipeline. Therefore, it can be understood that the essence of the first node, the second node and the third node is an air pump structure. When the solenoid valve is in a connected state, the gas is injected through the air pump structure. On the contrary, when the solenoid valve is in a closed state, the air pump structure is in a state of temporary interruption.

[0034] What needs to be explained about dynamic data and variable data is that they are used to represent the temperature and pressure values ​​in the dimethyl ether vaporizer and carbonylation reactor respectively, so as to express the temperature and pressure values ​​in the dimethyl ether vaporizer and carbonylation reactor respectively. a , P a Indicates the temperature and pressure values ​​in the dimethyl ether vaporizer, T b , P b The variable data is used to represent the temperature and pressure in the carbonylation reactor. Similarly, the variable data is used to represent the temperature and pressure in the transfer gas warehouse, which are represented by T0 and P0 respectively. The basic data only represents the initial temperature of the gaseous CO in the CO storage tank, which is represented by T c To express;

[0035] It should be noted that: the overall scheme is based on the carbonylation reactor as the main body, specifically according to T b , To feedback the reaction rate in the carbonylation reactor, specifically, the third-order equilibrium model is used for feedback. Its essence is: the mixed gas is continuously replenished into the carbonylation reactor, and the continuous replenishment process of the mixed gas "depends" on the transfer gas bin, so there is a correlation between the second-order equilibrium model and the third-order equilibrium model. Similarly, the formation of the mixed gas in the transfer gas bin "depends" on the gas extraction process of the gas pump structure in the CO gas storage tank and the dimethyl ether vaporizer, so there is a correlation between the second-order equilibrium model and the first-order equilibrium model. Then it can be directly understood as: the vaporization process of dimethyl ether and the carbonylation reaction process of the mixed gas are "combined" with each other, but the two are not directly connected, so as to avoid the mutual interference between the vaporization process and the carbonylation reaction process due to temperature / pressure changes.

[0036] Embodiment 2: This embodiment explains and illustrates the first-order equilibrium model, the second-order equilibrium model and the third-order equilibrium model in Embodiment 1:

[0037] The description of the first-order equilibrium model is as follows:

[0038] S1: The CO gas tank is only used as a gas storage structure for CO, so that the corresponding amount of gaseous CO can be directly extracted by the gas pump structure. There are changes in temperature and pressure in the dimethyl ether vaporizer, and when the solenoid valve in the corresponding dimethyl ether vaporizer is in a closed state, the inside of the dimethyl ether vaporizer is in a closed state. With the continuous vaporization process, the amount of gaseous dimethyl ether continues to increase, which leads to an increase in pressure. It should be noted here that dimethyl ether is an explosive and flammable substance. In the continuous vaporization process, at P a Set the critical upper limit value in This part is determined by the internal volume of the dimethyl ether vaporizer. In this embodiment, the critical upper limit value is It is set to a fixed value. It should also be noted that: under standard pressure (1 atmosphere), the vaporization temperature of liquid dimethyl ether is 39.6°C, so at T a Preset normal temperature value in by When the vaporization process continues and the corresponding solenoid valve is in a closed state, the internal pressure of the dimethyl ether vaporizer continues to rise, so the calculation method of the first-order equilibrium model M is: Among them As the pressure value of gaseous dimethyl ether, M is the first-order equilibrium value;

[0039] The description of the second-order equilibrium model is as follows:

[0040] S2: Figure 2 As shown in Figure 2, when gaseous CO and gaseous dimethyl ether are extracted and injected into the transfer gas warehouse, the second-order equilibrium model established according to the first law of thermodynamics is: The m a , C a 、m b , C b They represent the mass and specific heat capacity of gaseous dimethyl ether and gaseous CO injected into the transfer gas bin, respectively. The pressure value inside the transfer gas bin is "determined" by gaseous CO and gaseous dimethyl ether, and both the pressure value and the temperature value can be detected by the corresponding gas pressure sensor and temperature sensor. However, in the second-order equilibrium model, the temperature value and the pressure value inside the transfer gas bin can be reversely "determined" by limiting the volume and temperature of gaseous CO and gaseous dimethyl ether injected into the transfer gas bin.

[0041] The description of the third-order equilibrium model is as follows:

[0042] S3: For the carbonylation reaction process in the carbonylation reactor, gaseous methyl acetate is prepared by using the mixed gas and the catalyst, and T is preset in advance according to the carbonylation reactor of different specifications. b , P b The mean temperature in and pressure mean Under the bidirectional conditions of the mean temperature and the mean pressure, it is used to indicate that the carbonylation reaction process in the overall carbonylation reactor is in the optimal state, but it is necessary to use the T b , P b Establish real-time curves of temperature value-reaction time and pressure value-reaction time respectively, and substitute the average temperature and average pressure into the real-time curves of temperature value-reaction time and pressure value-reaction time respectively. For details, please refer to Figure 3 and Figure 4 , the two real-time curves exist independently, but in the third-order equilibrium model, the two real-time curves need to be "overlapped". The front calculation process is to "extract" the temperature and pressure values ​​in the same reaction time, and establish them in the two real-time curves respectively. With T b , With P b The equilibrium fluctuation values ​​between Its essence is: the temperature value in the carbonylation reactor is close to the temperature average, and the pressure value is close to the pressure average. Under the most ideal conditions, the X t =0, However, in specific cases, the following states may exist: X t >0, Y t >0;X t >0, Y t <0;X t <0, Y t >0;X t <0, X t <0.

[0043] Embodiment 3: This embodiment is a summary of Embodiment 1 and Embodiment 2:

[0044] In the collaborative control unit, refer to Figure 3 and Figure 4 , in X t and Y t The proximity values ​​are set to 0.09 and 0.13 respectively, and the following node coordination actions are set:

[0045] Action 1: First, in the dimethyl ether vaporizer, on the basis of M > 0, gaseous dimethyl ether generates control signals for the solenoid valves on the dimethyl ether vaporizer according to the second-order equilibrium model and the third-order equilibrium model, specifically the connection signal and the closing signal. However, on the basis of M < 0, without considering the second-order equilibrium model and the third-order equilibrium model, directly generate the connection signal in the control signals of the solenoid valves on the dimethyl ether vaporizer, and inject the gaseous dimethyl ether into the transfer gas chamber until M > 0 is satisfied;

[0046] Action 2: Based on Action 1, under the condition of M > 0 and associated with X in the third-order equilibrium model t and X t , the node cooperation actions performed are refined as follows:

[0047] A1; When X t > 0 and X t > 0, it is necessary to further calculate the balance fluctuation values of X t and Y t . When 0 < X t < 0.09 and 0 < Y t < 0.13, the node cooperation action is not executed; and because the gas volume in the carbonylation reactor is directly related to the pressure condition, so when Y t > 0.13, this situation indicates that the temperature is too low or the pressure is too low, so it can be directly associated with the second-order equilibrium model to increase the gas volume of the mixed gas in the transfer gas chamber supplemented to the carbonylation reactor, and directly set the gas volume Q t of the mixed gas supplemented to the carbonylation reactor per unit time in the second node, so as to optimize the gas volume in the second-order equilibrium model associated with the third-order equilibrium model to Q t *(1 + Y t - 0.13);

[0048] A2: When X t > 0 and Y t < 0, directly obtain the absolute value of Y t , and indirectly obtain the absolute value of Y t - 0.13, so as to optimize the gas volume in the second-order equilibrium model associated with the third-order equilibrium model to Q t *(1 - Y t + 0.13). At the same time, it is also necessary to be associated with the first-order equilibrium model and the second-order equilibrium model. Specifically, when 0 < X t < 0.09, the temperature value of the mixed gas in the transfer gas chamber is not adjusted, but when X t > 0.09, optimize the temperature of the mixed gas in the transfer gas chamber to T0*(1 - X t + 0.09), and because the Tc of gaseous CO is a fixed value, so only through And reversely adjust the T in the dimethyl ether vaporizer a ;

[0049] A3: In X t <0 and Y t >0, the transfer gas warehouse does not adjust the gas volume of the carbonylation reactor, and on the basis of satisfying M>0, increases the T in the dimethyl ether vaporizer a , first obtain X t The absolute value of and the absolute value of 0.09, so the temperature of the mixed gas is optimized to T0*(1+X t +0.09), reverse adjustment of T in the dimethyl ether vaporizer a ;

[0050] A4: In X t <0, Y t <0, directly means that the temperature and pressure in the carbonylation reactor are too high, and it is necessary to reduce the gas volume and mixed gas temperature of the transit gas to the carbonylation reactor at the same time. For details, please refer to A1~A3.

[0051] In summary: in the process of injecting gaseous CO and gaseous dimethyl ether into the carbonylation reactor, a transfer structure of a transfer gas bin is added to "isolate" the dimethyl ether vaporizer and the carbonylation reactor to avoid mutual influence and interference between the temperature environment and pressure of the two. Its essence is to "pre-" mix the gaseous CO and gaseous dimethyl ether. On this basis, a first-order equilibrium model, a second-order equilibrium model and a third-order equilibrium model are set up. Based on the pressure and temperature changes among the three, on the basis that the temperature / pressure does not actively influence and interfere, the mixing process and injection process of the gaseous CO and gaseous dimethyl ether are maintained in a mutually related manner. Specifically, the third-order equilibrium model is used as the front step, and the temperature of dimethyl ether and the amount of gas added to the carbonylation reactor by balancing the fluctuation value are controlled to maintain the overall vaporization and carbonyl reaction process.

[0052] The above contents are merely examples and explanations of the structure of the present invention. The technicians in this technical field may make various modifications or additions to the specific embodiments described or replace them in a similar manner. As long as they do not deviate from the structure of the invention or exceed the scope defined by the claims, they should all fall within the protection scope of the present invention.

[0053] In the description of this specification, the description with reference to the terms "one embodiment", "example", "specific example", etc. means that the specific features, structures, materials or characteristics described in conjunction with the embodiment or example are included in at least one embodiment or example of the present invention. In this specification, the schematic representation of the above terms does not necessarily refer to the same embodiment or example. Moreover, the specific features, structures, materials or characteristics described can be combined in any one or more embodiments or examples in a suitable manner.

[0054] The preferred embodiments of the present invention disclosed above are only used to help explain the present invention. The preferred embodiments do not describe all the details in detail, nor do they limit the invention to only specific implementation methods. Obviously, many modifications and changes can be made according to the content of this specification. This specification selects and specifically describes these embodiments in order to better explain the principles and practical applications of the present invention, so that those skilled in the art can understand and use the present invention well. The present invention is limited only by the claims and their full scope and equivalents.

Claims

1. An energy-saving dimethyl ether efficient vaporization mixing method using CO as carrier gas, characterized in that: The invention comprises a dimethyl ether vaporizer, a carbonylation reactor, a CO gas storage tank, a transfer gas bin and a control system. The dimethyl ether vaporizer and the CO gas storage tank respectively inject gaseous dimethyl ether and gaseous CO into the transfer gas bin to form a mixed gas in the transfer gas bin, and the mixed gas is injected into the carbonylation reactor to carry out a carbonylation reaction process. The dimethyl ether vaporizer and the CO gas storage tank are connected with a primary pipeline corresponding to the transfer gas bin, and the transfer gas bin is connected with a secondary pipeline corresponding to the carbonylation reactor. The primary pipelines corresponding to the dimethyl ether vaporizer and the CO gas storage tank are respectively provided with a first node and a second node, and the secondary pipeline is provided with a third node; The control system is composed of a data integration unit, a data hierarchical analysis unit and a collaborative control unit. The data integration unit is used to collect dynamic data, variable data and basic data, and input the dynamic data and variable data into the data hierarchical analysis unit. In the data classification analysis unit, a first-order equilibrium model associated with the first node is established with the dynamic data in the dimethyl ether vaporizer, a third-order equilibrium model associated with the third node is established with the dynamic data in the carbonylation reactor, and a second-order equilibrium model associated with the transfer gas warehouse is established with the basic data in the CO gas storage tank and the first-order equilibrium model, and the first-order equilibrium model, the second-order equilibrium model and the third-order equilibrium model are respectively substituted into the collaborative control unit; In the collaborative control unit, the third-order balance model is used as a front step, and the front calculation process of the third-order balance model in the second-order balance model is established, the balance fluctuation value is obtained in the front calculation process, and the balance fluctuation value is substituted into the second-order balance model and the first-order model, and the first node, the second node and the third node are controlled respectively to perform node collaborative actions; The dynamic data are used to represent the temperature and pressure values ​​in the dimethyl ether vaporizer and carbonylation reactor, respectively. a , P a Indicates the temperature and pressure values ​​in the dimethyl ether vaporizer, T b , P b The variable data is used to represent the temperature and pressure values ​​in the carbonylation reactor. The variable data is used to represent the temperature and pressure values ​​in the transfer gas warehouse, which are represented by T0 and P0. The basic data represents the initial temperature of the gaseous CO in the CO storage tank, which is represented by T c To express; In the first-order equilibrium model, T a Preset normal temperature value The calculation method for establishing the first-order equilibrium model M is: Among them As the pressure value of gaseous dimethyl ether, To represent P a The critical upper limit value in , M is the first-order equilibrium value, and the second-order equilibrium model is established as m a , C a 、m b , C b They represent the mass and specific heat capacity of gaseous dimethyl ether and gaseous CO injected into the transfer gas bin respectively; In the previous step, according to T b , P b Establish real-time curves of temperature value-reaction time and pressure value-reaction time respectively, and preset T b , P b The mean temperature in and pressure mean In two real-time curve graphs, With T b , With P b Balance fluctuation value X t and Y t , the calculation process is expressed as:

2. The energy-saving dimethyl ether efficient vaporization mixing method using CO as carrier gas according to claim 1 is characterized in that: In X t and Y t The approximate values ​​of 0.09 and 0.13 are established respectively, and the first-order equilibrium values ​​in the first-order equilibrium model are substituted, and the node coordination actions are set as follows: A1: When 0 < X t < 0.09 and 0 < Y t < 0.13, the node collaborative action is not executed; when Y t > 0.13, set the gas volume Q t supplemented to the carbonylation reactor per unit time of the mixed gas, and optimize the gas volume in the second-order equilibrium model to Q t * (1 + Y t - 0.13); A2: In X t >0 and Y t <0, get Y t , Y t The absolute value of -0.13 is used to optimize the gas volume in the second-order equilibrium model associated with the third-order equilibrium model as Q t *(1-Y t +0.13), and in X t >0.09, optimize the temperature of the mixed gas in the transfer gas chamber to T0*(1-X t +0.09), and reversely adjust the T in the dimethyl ether vaporizer a ; A3: In X t <0 and Y t >0, the transfer gas warehouse does not adjust the gas volume of the carbonylation reactor. When M>0 is satisfied, the T in the dimethyl ether vaporizer is increased. a , first obtain X t The absolute value of and the absolute value of 0.09, so the temperature of the mixed gas is optimized to T0*(1+X t +0.09), reverse adjustment of T in the dimethyl ether vaporizer a ; A4: In X t <0, Y t <0, indicating that the temperature and pressure inside the carbonylation reactor are too high. According to A1 to A3, the gas volume and mixed gas temperature of the transit gas to the carbonylation reactor are reduced simultaneously.

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