Cigarette tobacco shred heating combined drying method and system based on flavor component control

Abstract

The invention relates to the technical field of heated cigarettes, and discloses a heated cigarette cut tobacco combined drying method and system based on fragrance component control. The combined drying method comprises the following steps: adopting hot air-thin plate combined drying tobacco shreds; obtaining types of flavor components of the tobacco shreds, and constructing a nonlinear prediction equation after combined drying based on the flavor components; linearizing the nonlinear prediction equation to obtain a linear equation; performing Laplace transformation on the linear equation to obtain a transfer function; according to the combined drying method, a PID (Proportion Integration Differentiation) controller is arranged to regulate the drying dehydration fluctuation of the tobacco shreds and control the drying degree of the tobacco shreds in real time based on the transfer function, so that the automatic control based on the flavor components is realized, the loss of the flavor components is reduced, the quality of the tobacco shreds is improved, and the production efficiency and stability are improved.

Description

Technical Field

[0001] The present invention relates to the technical field of heated cigarettes, and in particular to a method and system for combined drying of heated cigarette shreds based on flavor component control. Background Art

[0002] With the rapid development of new tobacco, heated cigarettes have gradually become a hot spot in product research and development. Compared with traditional cigarettes, the basic condition for the new heated cigarettes to smoke is that the tobacco shreds need to be preheated to about 300°C. If the moisture in the tobacco shreds is not fully treated, water vapor will be generated during inhalation, resulting in high smoke temperature. A single drying method cannot meet the moisture requirements of heated cigarette tobacco shreds. At present, the existing technology mainly adopts the "hot air-thin plate" combined drying method. However, the aroma components of the tobacco shreds in the combined drying process cannot be continuously and automatically controlled by the drying degree of the tobacco shreds, so that the excessive drying of the tobacco shreds causes the loss of aroma components, affecting production efficiency and stability; at the same time, there is a lack of target value control for the content of the aroma components of the tobacco shreds, and it is impossible to obtain tobacco shreds with different aroma component contents, which does not meet the production requirements of the aroma component content of the tobacco shreds. Summary of the invention

[0003] In order to overcome the above problems, the present invention provides a method and system for combined drying of heated cigarette tobacco based on flavor component control. The combined drying method adopts hot air-thin plate combined drying of tobacco, then obtains the types of flavor components of the tobacco, and constructs a nonlinear prediction equation after combined drying based on the flavor components, linearizes the nonlinear prediction equation to obtain a linear equation, and then performs Laplace transformation on the linear equation to obtain a transfer function, and sets a PID controller to adjust the drying and dehydration fluctuations of tobacco in real time based on the transfer function, controls the degree of drying of tobacco, realizes automatic control based on flavor components, reduces the loss of flavor components, improves the quality of tobacco, and improves production efficiency and stability.

[0004] In order to achieve the above-mentioned object, the present invention provides a tobacco joint drying method for a heated cigarette production line based on flavor component control, characterized in that the joint drying method comprises:

[0005] Adopt hot air-thin plate combined drying of tobacco;

[0006] Acquiring the types of flavor components of the shredded tobacco, and constructing a nonlinear prediction equation after joint drying based on the flavor components;

[0007] Linearizing the nonlinear prediction equation to obtain a linear equation;

[0008] Performing Laplace transformation on the linear equation to obtain a transfer function;

[0009] The drying temperature of the tobacco shreds is regulated based on the transfer function.

[0010] Preferably, the types of flavor components of the tobacco shreds are obtained, and a nonlinear prediction equation after joint drying is constructed based on the flavor components, including:

[0011] Obtaining the type of the flavor component;

[0012] Obtain the hot air drying dehydration mass percentage fraction and the thin plate drying dehydration mass percentage fraction, and obtain the binary nonlinear prediction equation of the mass fraction of the aroma component according to formula (1).

[0013]

[0014] Wherein, z is the predicted value of the mass fraction of the aroma component, k1 to k 15 are the fitting parameters of the binary nonlinear prediction equation, x is the mass percentage of the thin plate drying and dehydration, y is the mass percentage of the hot air drying and dehydration, h is 0 or 3, m is 0 or 4, n is 0 or 2, p is 0 or 3, and q is 0 or 2.

[0015] Preferably, linearizing the nonlinear prediction equation to obtain a linear equation comprises:

[0016] Obtaining the preset control target value of the mass fraction of the aroma component and the control target value of the mass percentage fraction of the hot air drying and dehydration corresponding to the control target value of the mass fraction, and the control target value of the mass percentage fraction of the thin plate drying and dehydration, and obtaining a univariate linear prediction equation based on the mass fraction of the aroma component according to formula group (2),

[0017]

[0018] Wherein, z is the predicted value of the mass fraction of the aroma component, z0 is the preset control target value of the mass fraction of the aroma component, k1 to k 15 is the fitting parameter of the univariate linear prediction equation, x is the mass percentage of the thin plate drying dehydration, x0 is the control target value of the mass percentage of the hot air drying dehydration, y is the mass percentage of the hot air drying dehydration, y0 is the control target value of the mass percentage of the thin plate drying dehydration, z ′ (x0) is the first derivative of the univariate linear prediction equation for the mass fraction of the aroma component, h is 0 or 3, m is 0 or 4, n is 0 or 2, p is 0 or 3, and q is 0 or 2.

[0019] Preferably, performing Laplace transform on the linear equation to obtain a transfer function comprises:

[0020] Constructing a joint drying model;

[0021] Obtaining the mass percentage error of the thin plate drying and dehydration and the mass percentage error of the aroma component;

[0022] The mass fraction error is converted using formula group (2);

[0023] Formula (3) is used to determine a linear equation based on the mass percentage error of the thin plate drying and dehydration and the mass fraction error of the aroma component according to the conversion result.

[0024]

[0025] Among them, e x is the mass percentage error of the thin plate drying and dehydration, e z is the mass fraction error of the aroma component, x0 is the control target value of the mass percentage fraction of the hot air drying dehydration, z ′ (x0) is the first derivative of the univariate linear prediction equation of the mass fraction of the aroma component;

[0026] Obtaining the input and output of the joint drying model, and performing the Laplace transform on the input and output of the joint drying model using formula (3);

[0027] Formula (4) is used to determine the transfer function based on the result of Laplace transformation:

[0028]

[0029] Among them, G (S) is the transfer function, E x(S) is the output of the combined drying model, which is the error between the control target value and the actual value of the mass percentage fraction of the thin plate drying and dehydration, E z(S) is the input of the joint drying model, is the error between the control target value and the actual value of the mass fraction of the aroma component, z ′ (x0) is the first derivative of the univariate linear prediction equation for the mass fraction of the aroma component.

[0030] Preferably, regulating the drying temperature of the shredded tobacco based on the transfer function comprises:

[0031] Using a PID controller to obtain a control target value of the mass fraction of the aroma component and an error between the control target value and an actual value of the mass fraction of the aroma component;

[0032] The PID controller is used to obtain the error between the control target value and the actual value based on the mass percentage fraction of the thin plate drying and dehydration based on the transfer function of the aroma component;

[0033] The PID controller is used to control the temperature of the thin plate by the temperature controller to obtain the actual value of the mass fraction of the aroma component;

[0034] When the actual value of the mass fraction of the flavor component is equal to the control target value of the mass fraction of the flavor component, the PID controller is turned off to obtain the tobacco shreds after combined drying;

[0035] When the actual value of the mass fraction of the aroma component is less than the control target value of the mass fraction of the aroma component, the PID controller re-acquires the control target value of the mass fraction of the aroma component and the error between the control target value and the actual value of the mass fraction of the aroma component.

[0036] Preferably, the working numerical range of the hot air drying dehydration mass percentage fraction is 0-10%, and the working numerical range of the thin plate drying dehydration mass percentage fraction is the union of 0 and 6%-16%.

[0037] Preferably, the types of flavor components include at least one of non-enzymatic browning reaction products, phenylalanine degradation products, carotenoid degradation products and ceramsite degradation products.

[0038] Preferably, the moisture content of the tobacco shreds after combined drying is less than or equal to 3%.

[0039] The second aspect of the present invention provides a tobacco joint drying system for a heated cigarette production line based on flavor component control, the joint drying system comprising:

[0040] Hot air drying device;

[0041] A sheet drying device, arranged at the rear end of the hot air drying device, for drying the shredded tobacco after being processed by the hot air drying device;

[0042] A temperature controller, the temperature controller being electrically connected to the hot air drying device and the thin plate drying device;

[0043] A PID controller, the PID controller is electrically connected to the thin plate drying device, the hot air drying device and the temperature controller, and is used to execute the combined drying method as described in any one of the above claims.

[0044] Preferably, the combined drying system comprises an online near infrared analyzer for detecting the mass fraction of the aroma component in real time;

[0045] The thin plate drying device is a drum-type wire drying device, and the hot air drying device is an airflow-type wire drying device.

[0046] Through the above technical scheme, the combined drying method can adopt hot air-thin plate combined drying of shredded tobacco, and then obtain the types of aroma components of the shredded tobacco, and construct a nonlinear prediction equation after combined drying based on the aroma components, and obtain the preset control target value of the mass fraction of the aroma component and the control target value of the mass percentage fraction of the hot air drying and dehydration corresponding to the control target value of the mass fraction, and the control target value of the mass percentage fraction of the thin plate drying and dehydration as the working point, and obtain the linear equation by numerical linearization of the working point, and then perform Laplace transformation on the linear equation based on the error of the mass percentage fraction of the thin plate drying and dehydration and the error of the mass fraction of the aroma components, and then construct a combined drying model, control the input and output of the model to obtain a transfer function, set a PID controller to adjust the drying and dehydration fluctuations of the shredded tobacco in real time based on the transfer function, control the degree of drying of the shredded tobacco, realize automatic control based on the aroma components, reduce the loss of aroma components, improve the quality of the shredded tobacco, and improve the efficiency and stability of production. BRIEF DESCRIPTION OF THE DRAWINGS

[0047] Figure 1 is a flowchart of a combined drying method for heated cigarette shreds based on flavor component control according to an embodiment of the present invention;

[0048] Figure 2 It is a flowchart of performing Laplace transform on a linear equation to obtain a transfer function in a method for combined drying of heated cigarette shreds based on flavor component control according to an embodiment of the present invention;

[0049] Figure 3 It is a flowchart of controlling the drying temperature of shredded tobacco based on a transfer function in a combined drying method for heated shredded cigarette tobacco based on flavor component control according to an embodiment of the present invention;

[0050] Figure 4 It is an actual value control curve when the control target value of the non-enzymatic browning reaction product is 20.53 μg / g when the hot air drying dehydration mass percentage fraction and the sheet drying dehydration mass percentage fraction are 3.5% and 12.5% ​​respectively in the combined drying method for heated cigarette shreds based on flavor component control according to one embodiment of the present invention;

[0051] Figure 5 It is an actual value control curve when the control target value of phenylalanine degradation products is 11.49 μg / g when the hot air drying dehydration mass percentage fraction and the sheet drying dehydration mass percentage fraction are 2.5% and 13.5% respectively in the combined drying method for heated cigarette shreds based on flavor component control according to one embodiment of the present invention;

[0052] Figure 6It is an actual value control curve when the hot air drying dehydration mass percentage fraction is 2% and the sheet drying dehydration mass percentage fraction is 14% in the combined drying method for heated cigarette shreds based on flavor component control according to one embodiment of the present invention, and the control target value of carotenoid degradation products is 99.14 μg / g;

[0053] Figure 7 This is an actual value control curve when the control target value of cedarwood degradation products is 20.53 μg / g when the hot air drying dehydration mass percentage fraction is 4% and the thin plate drying dehydration mass percentage fraction is 12% in the combined drying method for heated cigarette shredded tobacco based on flavor component control according to an embodiment of the present invention. DETAILED DESCRIPTION

[0054] The specific implementation of the embodiment of the present invention is described in detail below in conjunction with the accompanying drawings. It should be understood that the specific implementation described here is only used to illustrate and explain the embodiment of the present invention, and is not used to limit the embodiment of the present invention.

[0055] In the embodiments of the present invention, unless otherwise specified, directional words such as "up, down, top, bottom" are usually used with reference to the directions shown in the drawings or are used to describe the relative positional relationships of components in the vertical, perpendicular or gravity direction.

[0056] In addition, if there are descriptions involving "first", "second", etc. in the embodiments of the present invention, the descriptions of "first", "second", etc. are only used for descriptive purposes and cannot be understood as indicating or suggesting their relative importance or implicitly indicating the number of the indicated technical features. Therefore, the features defined as "first" and "second" may explicitly or implicitly include at least one of the features. In addition, the technical solutions between the various embodiments can be combined with each other, but they must be based on the ability of ordinary technicians in the field to implement them. When the combination of technical solutions is contradictory or cannot be implemented, it should be deemed that such a combination of technical solutions does not exist and is not within the scope of protection required by the present invention.

[0057] like Figure 1 FIG. 1 is a flowchart of a combined drying method for heated cigarette shreds based on flavor component control according to an embodiment of the present invention; Figure 1 The combined drying method may include:

[0058] In step S10, the shredded tobacco is dried by hot air-thin plate combination;

[0059] In step S11, the types of aroma components of the tobacco are obtained, and a nonlinear prediction equation after joint drying is constructed based on the aroma components;

[0060] In step S12, the nonlinear prediction equation is linearized to obtain a linear equation;

[0061] In step S13, Laplace transform is performed on the linear equation to obtain a transfer function;

[0062] In step S14, the drying temperature of the tobacco shreds is regulated based on the transfer function.

[0063] In such Figure 1 In the method shown, step S10 adopts hot air-thin plate combined drying of shredded tobacco, where the shredded tobacco is first dried by hot air at high temperature and then by thin plate at low temperature, so as to control the drying speed and improve the quality of the shredded tobacco.

[0064] Step S11 obtains the types of aroma components of tobacco shreds, takes the hot air drying dehydration mass percentage fraction and the thin plate drying dehydration mass percentage fraction as independent variables, takes the aroma component mass fraction of tobacco shreds as the dependent variable, and constructs a nonlinear prediction equation after joint drying based on the aroma components.

[0065] Step S12 linearizes the nonlinear prediction equation to obtain a linear equation, obtains the preset control target value of the mass fraction of the aroma component and the control target value of the mass percentage fraction of the hot air drying and dehydration corresponding to the control target value of the mass fraction, and the control target value of the mass percentage fraction of the thin plate drying and dehydration, and brings them into the nonlinear prediction equation for linearization processing.

[0066] Step S13 performs Laplace transformation on the linear equation to obtain a transfer function, constructs a joint drying model, converts the mass percentage error of the thin plate drying dehydration and the mass fraction error of the aroma component to generate a change formula for the input and output of the joint drying model, and performs Laplace transformation based on the formula to obtain a transfer function.

[0067] In step S14, a PID controller is used to process the control target value of the mass fraction of the aroma component and the error between the control target value and the actual value of the mass fraction of the aroma component, and the error between the control target value and the actual value of the thin plate drying dehydration mass percentage fraction is obtained based on the transfer function, and the temperature of the temperature controller is controlled and adjusted in real time to obtain the tobacco after combined drying.

[0068] Through the above technical scheme, the combined drying method adopts hot air-thin plate combined drying of shredded tobacco, then obtains the types of aroma components of the shredded tobacco, and constructs a nonlinear prediction equation after combined drying based on the aroma components, linearizes the nonlinear prediction equation to obtain a linear equation, and then performs Laplace transformation on the linear equation to obtain a transfer function, and sets a PID controller to adjust the drying and dehydration fluctuations of the shredded tobacco in real time based on the transfer function, controls the degree of drying of the shredded tobacco, realizes automatic control based on the aroma components, reduces the loss of aroma components, improves the quality of the shredded tobacco, and improves the efficiency and stability of production.

[0069] In order to facilitate subsequent processing and ensure the normal use of the combined drying method, in one embodiment of the present invention, obtaining the types of aroma components of tobacco shreds and constructing a nonlinear prediction equation after combined drying based on the aroma components may include the following steps: obtaining the types of aroma components; obtaining the mass percentage fraction of hot air drying dehydration and the mass percentage fraction of sheet drying dehydration, and obtaining a binary nonlinear prediction equation for the mass fraction of the aroma components according to formula (1).

[0070]

[0071] Among them, z is the predicted value of the mass fraction of the aroma component, k1 to k 15 are the fitting parameters of the binary nonlinear prediction equation, x is the mass percentage of dehydration of the thin plate by drying, y is the mass percentage of dehydration by hot air drying, h is 0 or 3, m is 0 or 4, n is 0 or 2, p is 0 or 3, and q is 0 or 2.

[0072] Taking into account the working numerical control of the mass percentage of hot air drying dehydration and the mass percentage of thin plate drying dehydration, it is ensured that the numerical value corresponding to the working point can be substituted into the calculation to complete the linearized nonlinear prediction equation. In one embodiment of the present invention, the linearized nonlinear prediction equation to obtain the linear equation may include the following steps: obtaining the control target value of the mass fraction of the preset aroma component and the control target value of the mass fraction corresponding to the control target value of the mass fraction, and the control target value of the mass percentage of hot air drying dehydration, and the control target value of the mass percentage of thin plate drying dehydration, and obtaining a univariate linear prediction equation based on the mass fraction of the aroma component according to formula group (2).

[0073]

[0074] Among them, z is the predicted value of the mass fraction of the aroma component, z0 is the preset control target value of the mass fraction of the aroma component, k1 to k 15 is the fitting parameter of the univariate linear prediction equation, x is the mass percentage of the thin plate drying dehydration, x0 is the control target value of the mass percentage of the hot air drying dehydration, y is the mass percentage of the hot air drying dehydration, y0 is the control target value of the mass percentage of the thin plate drying dehydration, z ′(x0) is the first derivative of the univariate linear prediction equation of the mass fraction of the aroma component, h is 0 or 3, m is 0 or 4, n is 0 or 2, p is 0 or 3, and q is 0 or 2; the preset control target value of the mass fraction of the aroma component and the control target value of the mass fraction corresponding to the control target value of the mass fraction, the control target value of the mass percentage fraction of hot air drying dehydration, and the control target value of the mass percentage fraction of thin plate drying dehydration can be a set of suitable predicted working point parameters for tobacco combined drying, based on which the aroma component can be quickly regulated to reach the corresponding control target value.

[0075] like Figure 2 The figure shows a flowchart of a transfer function obtained by Laplace transforming a linear equation in a combined drying method for heated cigarette shreds based on flavor component control according to an embodiment of the present invention; Figure 2 In order to realize the automatic control of the flavor components of the tobacco shreds and facilitate the subsequent stable regulation of the hot air-sheet combined drying, the linear equation can be Laplace transformed; in one embodiment of the present invention, the Laplace transform of the linear equation to obtain the transfer function may include the following steps:

[0076] In step S20, a joint drying model is constructed;

[0077] In step S21, the mass percentage error of the thin plate drying and dehydration and the mass percentage error of the aroma component are obtained;

[0078] In step S22, the mass score error is converted using formula group (2);

[0079] In step S23, the linear equation based on the mass fraction error of the thin plate drying dehydration and the mass fraction error of the aroma component is determined according to the conversion result using formula (3).

[0080]

[0081] Among them, e x is the mass percentage error of the thin plate drying and dehydration, e z is the mass fraction error of the aroma component, x0 is the control target value of the mass percentage of hot air drying dehydration, z ′ (x0) is the first derivative of the univariate linear prediction equation for the mass fraction of the aroma component;

[0082] In step S24, the input and output of the joint drying model are obtained, and the input and output of the joint drying model are Laplace transformed using formula (3);

[0083] In step S25, the transfer function is determined based on the result of Laplace transform using formula (4):

[0084]

[0085] Among them, G (S) is the transfer function, E x(S) is the output of the joint drying model, which is the error between the control target value and the actual value of the mass percentage of the thin plate drying dehydration, E z(S) is the input of the joint drying model, is the error between the target value and the actual value of the mass fraction control of the aroma component, z ′ (x0) is the first derivative of the univariate linear prediction equation for the mass fraction of the aroma component.

[0086] Through the above steps, the Laplace change of the linear equation is realized, so as to obtain the combined drying model, and the subsequent regulation of the combined drying model is facilitated according to the transfer function.

[0087] like Figure 3 FIG. 1 is a flowchart of a method for controlling the drying temperature of shredded tobacco based on a transfer function in a combined drying method for heated shredded cigarette tobacco based on flavor component control according to an embodiment of the present invention; FIG. Figure 3 In the process, considering that the transfer function can be used for subsequent automatic regulation to improve the control performance, a PID controller can be used for control; in one embodiment of the present invention, regulating the drying temperature of shredded tobacco based on the transfer function may include the following steps:

[0088] In step S30, a PID controller is used to obtain a control target value of the mass fraction of the aroma component and an error between the control target value and the actual value of the mass fraction of the aroma component;

[0089] In step S31, a PID controller is used to obtain an error between a control target value and an actual value of a thin plate drying and dehydration mass percentage fraction based on the aroma component using a transfer function based on the aroma component;

[0090] In step S32, a PID controller is used to control the temperature of the thin plate by regulating the temperature controller to obtain an actual value of the mass fraction of the aroma component;

[0091] In step S33, when the actual value of the mass fraction of the aroma component is equal to the control target value of the mass fraction of the aroma component, the PID controller is turned off to obtain the tobacco shreds after combined drying;

[0092] In step S34, when the actual value of the mass fraction of the aroma component is less than the control target value of the mass fraction of the aroma component, the PID controller re-obtains the control target value of the mass fraction of the aroma component and the error between the control target value and the actual value of the mass fraction of the aroma component.

[0093] In order to control the aroma components of tobacco shreds and control the dehydration range of combined drying; in one embodiment of the present invention, the working numerical range of the hot air drying dehydration mass percentage fraction is 0-10%, and the working numerical range of the thin plate drying dehydration mass percentage fraction is the union of 0 and 6%-16%. Setting the working numerical ranges of the hot air drying dehydration mass percentage fraction and the thin plate drying dehydration mass percentage fraction facilitates the control of the aroma components and ensures the stability of tobacco shreds production.

[0094] Taking into account the diversity of flavor components of tobacco and meeting the quality requirements of tobacco, in one embodiment of the present invention, the types of flavor components of tobacco include at least one of non-enzymatic browning reaction products, phenylalanine degradation products, carotenoid degradation products and cedarwood degradation products.

[0095] like Figure 4 The figure shows the actual value control curve when the control target value of the non-enzymatic browning reaction product is 20.53 μg / g when the hot air drying dehydration mass percentage fraction is 3.5% and the sheet drying dehydration mass percentage fraction is 12.5% ​​in the combined drying method for heated cigarette shreds based on flavor component control according to one embodiment of the present invention; Figure 4 In one embodiment of the present invention, when the type of flavor component of tobacco shreds is a non-enzymatic browning reaction product, the working value table of tobacco shreds combined drying is obtained according to the nonlinear prediction equation of the mass fraction of the non-enzymatic browning reaction product, which is a table of actual values ​​and predicted values ​​of the mass fraction of the non-enzymatic browning reaction product when the mass percentage fraction of hot air drying dehydration is between 0% and 10%, and when the mass percentage fraction of thin plate drying dehydration is between 0% and 6% and 16%, as shown in Table 1 below.

[0096] Table 1

[0097]

[0098] As shown in Table 1, the correlation coefficient between the predicted results and the actual results is 0.999619; when building an automated controlled combined drying system, the working points of tobacco combined drying during heated cigarette production were selected: the mass percentage of hot air drying dehydration was 3.5%, the mass percentage of thin plate drying dehydration was 12.5%, and the mass fraction of non-enzymatic browning reaction products was 20.53 μg / g. After being substituted into the binary nonlinear prediction equation of the mass fraction of non-enzymatic browning reaction products with respect to the mass percentage of thin plate drying dehydration, it was linearized and derived at the same time to obtain the first-order linear prediction equation of the mass fraction of non-enzymatic browning reaction products. The derivative is 0.9522, and after Laplace transformation, the transfer function between the mass fraction error of the non-enzymatic browning reaction product and the mass percentage error of the thin plate drying dehydration is 1.0502. According to the obtained transfer function value and the set control target value of the non-enzymatic browning reaction product, a PID-controlled combined drying system for the mass fraction of the non-enzymatic browning reaction product is established. The combined drying system is used in the production process of heated cigarettes. The actual value of the mass fraction of the non-enzymatic browning reaction product after combined drying can reach the control target value within 10s, realizing continuous control of the mass fraction of the non-enzymatic browning reaction product after combined drying. The combined drying system has no overshoot, which solves the problem of aroma component loss caused by excessive drying intensity on the production line.

[0099] like Figure 5 The figure shows the actual value control curve when the control target value of phenylalanine degradation products is 11.49 μg / g when the hot air drying dehydration mass percentage fraction is 2.5% and the sheet drying dehydration mass percentage fraction is 13.5% in the combined drying method for heated cigarette shreds based on flavor component control according to one embodiment of the present invention; Figure 5 In one embodiment of the present invention, when the type of flavor component of tobacco shreds is phenylalanine degradation products of tobacco shreds, the working value table of tobacco shreds combined drying is obtained according to the nonlinear prediction equation of the mass fraction of phenylalanine degradation products, which is a table of actual values ​​and predicted values ​​of the mass fraction of phenylalanine degradation products of hot air drying dehydration mass percentage fraction in the range of 0% to 10%, and thin plate drying dehydration mass percentage fraction in the range of 0% and 6% to 16%, as shown in Table 2 below.

[0100] Table 2

[0101]

[0102]

[0103] As shown in Table 2, the correlation coefficient between the predicted results and the actual results is 0.999801; when building an automated controlled combined drying system, the working points of tobacco combined drying during heated cigarette production were selected: the mass percentage of hot air drying dehydration was 2.5%, the mass percentage of thin plate drying dehydration was 13.5%, and the phenylalanine degradation product was 11.49 μg / g. After substituting it into the binary nonlinear prediction equation of the mass fraction of phenylalanine degradation products with respect to the mass percentage of thin plate drying dehydration, it was linearized and derived at the same time to obtain the first-order derivative of the univariate linear prediction equation of the mass fraction of phenylalanine degradation products. The number is 0.483, and after Laplace transformation, the transfer function between the mass fraction error of phenylalanine degradation products and the mass percentage error of thin plate drying dehydration is 2.0704. According to the obtained transfer function value and the set target value of phenylalanine degradation products, a PID-controlled combined drying system for the mass fraction of phenylalanine degradation products is established. The combined drying system is used in the production process of heated cigarettes. The actual value of the mass fraction of phenylalanine degradation products after combined drying can reach the control target value within 5s, realizing continuous control of the mass fraction of phenylalanine degradation products after combined drying. The combined drying system has no overshoot, which solves the problem of aroma component loss caused by excessive drying intensity on the production line.

[0104] like Figure 6 The figure shows the actual value control curve when the control target value of carotenoid degradation products is 99.14 μg / g in the combined drying method for heated cigarette shreds based on flavor component control according to one embodiment of the present invention, when the hot air drying dehydration mass percentage fraction is 2% and the sheet drying dehydration mass percentage fraction is 14%; Figure 6 In one embodiment of the present invention, when the type of flavor component of tobacco shreds is carotenoid degradation products, the working value table of tobacco shreds combined drying is obtained according to the nonlinear prediction equation of the mass fraction of carotenoid degradation products, which is a table of actual values ​​and predicted values ​​of the mass fraction of carotenoid degradation products in the range of hot air drying dehydration mass percentage fraction between 0% and 10%, and in the range of thin plate drying dehydration mass percentage fraction between 0% and 6% and 16%, as shown in Table 3 below.

[0105] Table 3

[0106]

[0107] It can be seen from Table 3 that the correlation coefficient between the predicted results and the actual results is 0.999267; when building an automated controlled combined drying system, the working points of tobacco combined drying during heated cigarette production are selected: the mass percentage of dehydration by hot air drying is 2%, the mass percentage of dehydration by thin plate drying is 14%, and the carotenoid degradation product is 99.14 μg / g. , it was substituted into the binary nonlinear prediction equation of the mass fraction of carotenoid degradation products with respect to the mass percentage fraction of thin plate drying dehydration, and then linearized, and derived at the same time, the first-order derivative of the univariate linear prediction equation of the mass fraction of carotenoid degradation products was obtained to be 20.0273, and the transfer function between the mass fraction error of carotenoid degradation products and the mass percentage fraction error of thin plate drying dehydration was obtained after Laplace transformation, which was 0.0499. According to the obtained transfer function value and the set control target value of carotenoid degradation products, a PID-controlled combined drying system of the mass fraction of carotenoid degradation products was established. The combined drying system was used in the production process of heated cigarettes, and the actual value of the mass fraction of carotenoid degradation products after combined drying could reach the control target value within 5s, realizing the continuous control of the mass fraction of carotenoid degradation products after combined drying. The combined drying system has no overshoot, which solves the problem of aroma component loss caused by excessive drying intensity on the production line.

[0108] like Figure 7 The figure shows the actual value control curve when the control target value of the degradation products of cedarene is 20.53 μg / g when the dehydration mass percentage of hot air drying is 4% and the dehydration mass percentage of thin plate drying is 12% in the combined drying method of heated cigarette shreds based on flavor component control according to one embodiment of the present invention; Figure 7 In one embodiment of the present invention, when the type of flavor component of the tobacco shreds is cephalane degradation products, the working value table of tobacco shreds combined drying is obtained according to the nonlinear prediction equation of the mass fraction of cephalane degradation products, which is a table of actual values ​​and predicted values ​​of the mass fraction of cephalane degradation products when the mass percentage fraction of hot air drying dehydration is between 0% and 10%, and when the mass percentage fraction of thin plate drying dehydration is between 0% and 6% and 16%, as shown in Table 4 below.

[0109] Table 4

[0110]

[0111] As shown in Table 4, the correlation coefficient between the predicted results and the actual results is 0.998752; when building an automated controlled combined drying system, the working points of tobacco combined drying during heated cigarette production were selected: the mass percentage of dehydration by hot air drying was 4%, the mass percentage of dehydration by sheet drying was 12%, and the cypermethrin degradation product was 31.01 μg / g. After substituting it into the binary nonlinear prediction equation of the mass fraction of cypermethrin degradation products with respect to the mass percentage of dehydration by sheet drying, it was linearized and derived at the same time, and the first-order derivative of the univariate linear prediction equation of the mass fraction of cypermethrin degradation products was obtained as follows: 0.0318, and after Laplace transformation, the transfer function between the mass fraction error of cedarwood degradation products and the mass percentage error of thin plate drying dehydration is 31.4465. According to the obtained transfer function value and the set target value of control of cedarwood degradation products, a PID-controlled combined drying system for the mass fraction of cedarwood degradation products is established. The combined drying system is used in the production process of heated cigarettes. The actual value of the mass fraction of cedarwood degradation products after combined drying can reach the control target value within 5s, realizing continuous control of the mass fraction of cedarwood degradation products after combined drying. The combined drying system has no overshoot, which solves the problem of aroma component loss caused by excessive drying intensity on the production line.

[0112] Considering the quality requirements of the tobacco after drying and controlling the quality of the heated cigarette, in one embodiment of the present invention, the moisture mass percentage of the tobacco after combined drying should be less than or equal to 3% to avoid excessively high smoke temperature caused by water vapor during smoking.

[0113] The second aspect of the present invention provides a tobacco combined drying system for a heated cigarette production line based on flavor component control, the combined drying system comprising a hot air drying device, a thin plate drying device, a temperature controller and a PID controller; specifically, the thin plate drying device can be arranged at the rear end of the hot air drying device, for drying the tobacco processed by the hot air drying device, the temperature controller is electrically connected to the hot air drying device and the thin plate drying device, the PID controller is electrically connected to the thin plate drying device, the hot air drying device and the temperature controller, for executing the combined drying method as described in any of the above claims.

[0114] Taking into account the applicability and practicality of the combined drying process; in one embodiment of the present invention, the combined drying system may also include an online near-infrared analyzer, which can process and monitor a variety of aroma components and provide real-time feedback on the mass fraction of the aroma components; the thin plate drying device may be a drum-type wire drying device, and the hot air drying device may be an airflow-type wire drying device; the drum-type wire drying device gradually dries the tobacco by means of continuously rotating thin plates, and its rotating drying method helps to maintain the temperature and humidity balance in the equipment, thereby better controlling the drying speed and product quality; the airflow-type wire drying device heats the air to a specific temperature and humidity so that the hot air is in full contact with the tobacco, thereby quickly removing moisture from the tobacco.

[0115] Through the above technical scheme, the combined drying method can adopt hot air-thin plate combined drying of shredded tobacco, and then obtain the types of aroma components of the shredded tobacco, and construct a nonlinear prediction equation after combined drying based on the aroma components, and obtain the preset control target value of the mass fraction of the aroma component and the control target value of the mass fraction corresponding to the control target value of the mass fraction. The control target value of the mass percentage fraction of hot air drying and dehydration and the control target value of the mass percentage fraction of thin plate drying and dehydration are used as working points, and the nonlinear prediction equation is processed by numerical linearization of the working point to obtain a linear equation, and then the linear equation is Laplace transformed based on the error of the mass percentage fraction of thin plate drying and dehydration and the error of the mass fraction of the aroma components, and then a combined drying model is constructed, and the input and output of the control model are controlled to obtain a transfer function, and a PID controller is set to adjust the drying and dehydration fluctuations of the shredded tobacco in real time based on the transfer function, control the degree of drying of the shredded tobacco, realize automatic control based on the aroma components, reduce the loss of aroma components, improve the quality of the shredded tobacco, and improve the efficiency and stability of production.

[0116] The preferred embodiments of the present invention are described in detail above in conjunction with the accompanying drawings. However, the present invention is not limited to the specific details in the above embodiments. Within the technical concept of the present invention, the technical solution of the present invention can be subjected to a variety of simple modifications, and these simple modifications all belong to the protection scope of the present invention. It should also be noted that the various specific technical features described in the above specific embodiments can be combined in any suitable manner without contradiction. In order to avoid unnecessary repetition, the present invention will not further describe various possible combinations.

[0117] In addition, various embodiments of the present invention may be arbitrarily combined, and as long as they do not violate the concept of the present invention, they should also be regarded as the contents disclosed by the present invention.

Claims

1. A tobacco shred combined drying method for a heated cigarette production line based on flavor component control, characterized in that: The combined drying method comprises: Adopt hot air-thin plate combined drying of tobacco; Acquiring the types of flavor components of the shredded tobacco, and constructing a nonlinear prediction equation after joint drying based on the flavor components; Linearizing the nonlinear prediction equation to obtain a linear equation; Performing Laplace transformation on the linear equation to obtain a transfer function; The drying temperature of the tobacco shreds is regulated based on the transfer function.

2. The combined drying method according to claim 1, characterized in that: Obtaining the types of flavor components of the tobacco shreds, and constructing a nonlinear prediction equation after joint drying based on the flavor components, comprising: Obtaining the type of the flavor component; Obtain the hot air drying dehydration mass percentage fraction and the thin plate drying dehydration mass percentage fraction, and obtain the binary nonlinear prediction equation of the mass fraction of the aroma component according to formula (1). Wherein, z is the predicted value of the mass fraction of the aroma component, k1 to k 15 are the fitting parameters of the binary nonlinear prediction equation, x is the mass percentage of the thin plate drying and dehydration, y is the mass percentage of the hot air drying and dehydration, h is 0 or 3, m is 0 or 4, n is 0 or 2, p is 0 or 3, and q is 0 or 2.

3. The combined drying method according to claim 2, characterized in that: Linearizing the nonlinear prediction equation to obtain a linear equation includes: Obtaining the preset control target value of the mass fraction of the aroma component and the control target value of the mass percentage fraction of the hot air drying and dehydration corresponding to the control target value of the mass fraction, and the control target value of the mass percentage fraction of the thin plate drying and dehydration, and obtaining a univariate linear prediction equation based on the mass fraction of the aroma component according to formula group (2), Wherein, z is the predicted value of the mass fraction of the aroma component, z0 is the preset control target value of the mass fraction of the aroma component, k1 to k 15 is the fitting parameter of the univariate linear prediction equation, x is the mass percentage of the thin plate drying dehydration, x0 is the control target value of the mass percentage of the hot air drying dehydration, y is the mass percentage of the hot air drying dehydration, y0 is the control target value of the mass percentage of the thin plate drying dehydration, z ′ (x0) is the first-order derivative of the univariate linear prediction equation for the mass fraction of the aroma component, h is 0 or 3, m is 0 or 4, n is 0 or 2, p is 0 or 3, and q is 0 or 2.

4. The combined drying method according to claim 3, characterized in that: The linear equation is Laplace transformed to obtain a transfer function, including: Constructing a joint drying model; Obtaining the mass percentage error of the thin plate drying and dehydration and the mass percentage error of the aroma component; The mass fraction error is converted using formula group (2); Formula (3) is used to determine a linear equation based on the mass percentage error of the thin plate drying and dehydration and the mass fraction error of the aroma component according to the conversion result. Among them, e x is the mass percentage error of the thin plate drying and dehydration, e z is the mass fraction error of the aroma component, x0 is the control target value of the mass percentage fraction of the hot air drying dehydration, z ′ (x0) is the first derivative of the univariate linear prediction equation of the mass fraction of the aroma component; Obtaining the input and output of the joint drying model, and performing the Laplace transform on the input and output of the joint drying model using formula (3); Formula (4) is used to determine the transfer function based on the result of Laplace transformation: Among them, G (S) is the transfer function, E x(S) is the output of the combined drying model, which is the error between the control target value and the actual value of the mass percentage fraction of the thin plate drying and dehydration, E z(S) is the input of the joint drying model, is the error between the control target value and the actual value of the mass fraction of the aroma component, z ′ (x0) is the first derivative of the univariate linear prediction equation for the mass fraction of the aroma component.

5. The combined drying method according to claim 1, characterized in that: Regulating the drying temperature of the tobacco shreds based on the transfer function includes: Using a PID controller to obtain a control target value of the mass fraction of the aroma component and an error between the control target value and an actual value of the mass fraction of the aroma component; The PID controller is used to obtain the error between the control target value and the actual value based on the mass percentage fraction of the thin plate drying and dehydration based on the transfer function of the aroma component; The PID controller is used to control the temperature of the thin plate by the temperature controller to obtain the actual value of the mass fraction of the aroma component; When the actual value of the mass fraction of the flavor component is equal to the control target value of the mass fraction of the flavor component, the PID controller is turned off to obtain the tobacco shreds after combined drying; When the actual value of the mass fraction of the aroma component is less than the control target value of the mass fraction of the aroma component, the PID controller re-acquires the control target value of the mass fraction of the aroma component and the error between the control target value and the actual value of the mass fraction of the aroma component.

6. The combined drying method according to claim 2, characterized in that: The working numerical range of the hot air drying dehydration mass percentage fraction is 0-10%, and the working numerical range of the thin plate drying dehydration mass percentage fraction is the union of 0 and 6%-16%.

7. The combined drying method according to claim 1, characterized in that: The types of flavor components include at least one of non-enzymatic browning reaction products, phenylalanine degradation products, carotenoid degradation products, and ceramsite degradation products.

8. The combined drying method according to claim 1, characterized in that: The moisture content of the tobacco shreds after combined drying is less than or equal to 3%.

9. A tobacco joint drying system for a heated cigarette production line based on flavor component control, characterized in that: The combined drying system comprises: Hot air drying device; A sheet drying device, arranged at the rear end of the hot air drying device, for drying the shredded tobacco after being processed by the hot air drying device; A temperature controller, the temperature controller being electrically connected to the hot air drying device and the thin plate drying device; A PID controller, wherein the PID controller is electrically connected to the thin plate drying device, the hot air drying device and the temperature controller, and is used to execute the combined drying method as described in any one of claims 1 to 8.

10. The combined drying system according to claim 9, characterized in that: The combined drying system includes an online near infrared analyzer for real-time detection of the mass fraction of the aroma component; The thin plate drying device is a drum-type wire drying device, and the hot air drying device is an airflow-type wire drying device.

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