Low efficiency, negative impacts on the environment and non-profitable operations are the main shortcomings of out-dated industrial processes. Such systems can be reconstructed and improved in the direction of multi-product operations. The study of this article focuses on the development of a method for multi-product operations by reconstructing out-dated industrial processes. This article contains the theory of a developed method that enables the updating of existing process units and integrated systems on the basis of reconstruction scenarios and pathways. The goals of the set out method are: 1) to maintain the existing process units and chemical plants to a greater extent, 2) to enable the potential for finding new process alternatives and technological solutions, 3) to provide a streamlined operation for all subsystems and total systems, 4) to promote environmental and social responsibilities, and 5) to apply the concept of the presented reconstruction method to non-profitable industrial processes. In regard to multi-product operations, a conceptual model is a suitable tool for the reconstruction of industrial processes. It connects several software tools and so enables quick decision-making between process alternatives. A reconstruction method provides foresight into the possible improvements to existing industrial processes. In comparison with the indirect synthesis of DME (simple reconstruction pathway), the lower operating costs from the direct synthesis of DME (complex reconstruction pathway) were confirmed.
Low efficiency, negative effects on the environment and non-profitable operations are the main shortcomings of outdated industrial processes [
The examined study of this article focuses on the development of a method of multi-product production for reconstructing out-dated industrial processes. This article contains the theory of the developed method that enables the updating of existing process units and integrated systems on the basis of reconstruction scenarios and pathways. The reconstruction pathway covers analysis of the current state of a chemical plant, the search for alternatives regarding multi-product production, simulation of process alternatives using computer-aided software, the search for mathematical connections between chemical and physical quantities, mathematical modelling of a super-structure, and quantitative evaluation of the results from the reconstruction method. This can be implemented after case study of an existing MeOH plant as to whether the plant is non-profitable. MINLP mathematical model is based on simple and complex reconstruction scenarios that can be examined in more de- tail during case-studies regarding indirect and direct syntheses of DME from MeOH or direct from natural gas (NG).
The goals of the presented set method are: 1) to maintain the existing process units and chemical processes to a greater extent, 2) to enable the potential for finding new process alternatives and technological solutions, 3) to provide a streamlined operation of all subsystems and systems, 4) to promote environmental and social responsibilities, and 5) to use mentioned method of multi-product operational processes on related industrial processes.
The chapter presents: the basic theory of a multi-product operation, the method of reconstructing pathways and scenarios, MINLP mathematical modelling of simple and complex reconstructive pathways within a super- structure model, the connection of computer-aided software for data capture, the creation of mathematical connections between physical and chemical quantities, and process of optimization.
The Multi-product operation basic function represents the inlet of raw materials, formed chemical products and produced fuels. More synthesis fuels (for example, DME, H2, olefins, gasoline, etc.) and produced energy can be generated within a chemical process from fossil fuels, water and air. Such systems are multi-feed/ multi-product (MFMP). The Multi-product operation includes single-feed/multi-product (SFMP) and/or MFMP operations.
The reconstruction method of multi-product production for an industrial process is displayed in
When reconstructing existing plants, multi-product production is based on the basic principle of flexibility. So fossil fuels, such as NG and coal, as well as bio-mass, bio-gas, corn, etc. can be used during the gasification process. When in taking one or more raw materials it is possible to simultaneously produce a number of chemical products. Their productivity depends on the chemical potential and demands in the market. When feeding into the process it is possible to choose between alternative raw materials that are economically appropriate or accessible.
The objective function of a reconstructed industrial process in the direction of multi-product operation is based on the maximized annual profit from individual process alternative
At conditions:
and:
Incomes present:
sales of all generated products
sales of fuels
Expenses on an annual basis represent:
the cost of all raw materials used
the cost of utility consumption used
exhaust emission taxes
amortization of additional process units
additional operating costs during the process
Equation (1a) represents the total mass balance of raw materials on the feed into the process and is equal to the mass out-feed of products from the process. Inequalities Equation (1b) and Equation (1c) represent a possible consumption of raw materials on the feed into the i-th alternative or produced mass capacity of an individual product according to market demand. Inequalities Equation (1d) and Equation (1e) represents the activation or deactivation of individual raw material/product of i-th process alternative.
Reconstructions of existing chemical processes are carried out in three main directions: 1) change of productivity (new products and more products), 2) change in the method of obtaining the product/-s (new processes and technologies) and 3) modification on the side of raw materials (different input raw materials). The method of reconstruction pathways is based on: a situation analysis of the existing plant, a search for process alternatives and technologies, and on computer simulation of selected process schemes.
Based on the state of the industrial process, the following questions are raised:
1) How to choose a potential process alternative for transforming the inlet of raw materials into multi-product production?
2) Which reconstruction pathway to choose in order to achieve a new desired state (B) of the existing plant?
3) Can reconstruction be carried out with the help of mathematical modelling?
4) Is it possible to confirm the usefulness of the analysed method on the existing process?
Existing chemical plants are satisfactorily optimized according to the assumption, but nevertheless do not bring economic profit. In order to improve this, simple and complex reconstructive pathways are at our disposal. From a technical point of view simple reconstruction pathways represent easy but less efficient improvements. These improvements are: replacement of the existing raw materials with new ones, a combination of inlet fossil and renewable fuels, changes in the process parameters and the production of new products. Alternatively the upgrading of existing processes, where products from the raw materials within a new part of the process are currently being produced. A more complex type of reconstruction concerns topological changes to the existing process units, replacements of reactors with new ones.
The examined mathematical model includes the results of various software tools (ASPEN PLUS, SYNHEAT and Excel), thus enabling quick decision-making between potential process alternatives. As far as heat analysis is concerned, Duran and Grossmann [
The mathematical model of the process’ super-structure (
The big-M formulation [
An analysis of the existing chemical synthesis process of MeOH was conducted and an overview of simple and complex reconstruction pathways was designed by using the reconstructive method of multi-product production. These reconstruction pathways represent the indirect (simple) or direct (complex) pathways.
The existing chemical plant for the synthesis of MeOH from NG had a capacity of 150,000 tons per year, and has been further analysed by the authors Kovač and Bencik [
DME synthesizes from NG over 3-stages along an indirect pathway of the synthesis. The basic process operations of DME formation are: 1) preheating of raw MeOH, 2) reaction of dehydration until DME, 3) separation and purification of the products and 4) the recycling of non-reactive reactants back to the reactor.
The conceptual alternative process schemes were considered on the basis of the listed literature, and upgraded for the existing industrial process shown in the case study.
The alternative process scheme A (Appendix II) represents a low-pressure synthesis process for the production of DME from raw MeOH. This process scheme was further examined by the authors [
In the direct pathway regarding synthesis, DME is formed directly from SNG by a catalysed dehydration reaction. A bi-functional catalyst with 2-active places within a single reactor enables simultaneous formation and dehydration of MeOH until the formed product. Formation of the product from SNG is represented by reactions (R1)-(R4).
The conceptual alternative process schemes were considered on the basis of the listed literature, and upgraded for the existing industrial process shown in the case study.
The alternative process scheme E (Appendix VI) represents a direct synthesis process for the production of
DME from NG at HP. This process scheme was further examined by the authors [
The presented method of reconstruction pathways regarding multi-product production was tested on an existing MeOH process. An analysis of the prior state of the chemical process was made, and simple and complex reconstruction scenarios were predicted. Simulations of potential process alternatives were conducted by ASPEN PLUS computer-aided software [
An MINLP mathematical model enables selection between simple or complex reconstruction pathways on the basis of included process alternatives. A simple reconstruction pathway is based on an indirect synthesis of DME from MeOH. The alternatives are presented using four process alternatives: from A to D. The second reconstruction pathway is a complex one and is based on a direct synthesis of DME that is presented using two alternatives: E and F.
A general mathematical model (Appendix I) was built within the GAMS language on the basis of reviewing the reconstruction scenarios and the simulations of individual process alternatives. It is formulated with total mass balances, heat balances, temperatures, and flow pressures. The main chemical components (DME, MeOH, H2O, CO and CO2) are included within the system. The examined study describes such basic mathematical connections as mentioned in the theory regarding specific mathematical connections, applicable only to the analysed plant. The general mass balance of the reactor is adjusted to the synthesis of DME and pure MeOH, where mathematical connections (Equation (41)-Equation (43)) are applicable. In the mathematical model, the incomes from the sale of both products (DME and MeOH) of individual process alternative are presented by equation (Equation (44)). The income from the sale of MPS is the result of utilizing the exothermic reaction. The equation in the model is shown by mathematical connection (Equation (45)). This study included only CO2 emissions. Emission fees are the result of releasing greenhouse gases into the environment and are presented by equation (Equation (46)). The additional operating costs of complex reconstruction pathways are not the main focus of this study and are therefore assessed as a fixed operating cost of the modified plant.
The inputted physical and chemical data were taken from the process simulator ASPEN PLUS. All the inputted data of the reconstruction method regarding the 2-product production are summarized in
Quantity | Units/alternative i | A | B | C | D | E | F |
---|---|---|---|---|---|---|---|
[kg・h−1] | 10,525 | 10,525 | 10,525 | 10,525 | 10,525 | 10,525 | |
[kg・h−1] | 33,000 | 33,000 | 33,000 | 33,000 | 33,000 | 33,000 | |
- | 0.9098 | 0.9027 | 0.8975 | 0.9026 | 1.1895 | 1.0924 | |
- | 0.1563 | 0.2041 | 0.2035 | 0.2361 | 0.1960 | 0.1786 | |
- | 0.2316 | 0.9167 | 0.7990 | 0.9167 | 1.67829 | 1.6210 | |
- | 0.00881 | 0.00877 | 0.00876 | 0.00883 | 0.02977 | 0.03420 | |
[˚C] | 230.0 | 270.0 | 280.0 | 270.0 | 240.0 | 240.0 | |
[bar] | 1.2 | 15.0 | 15.0 | 15.0 | 68.0 | 50.0 | |
T1 | [˚C] | 41.0 | 41.0 | 45.0 | 41.0 | 102.0 | 102.0 |
T2 | [˚C] | 120.0 | 250.0 | 250.0 | 250.0 | 240.0 | 230.0 |
Tin, cool | [˚C] | 15.0 | 15.0 | 1.0 | 15.0 | −45.0 | −45.0 |
Tin, heat | [˚C] | 300.0 | 300.0 | 350.0 | 300.0 | 300.0 | 300.0 |
Zcomp | [{0, 1}] | 1 | 0 | 0 | 1 | 0 | 0 |
Pin, comp | [bar] | 1.0 | 1.0 | 1.0 | 30.0 | 30.0 | 30.0 |
Pout, comp | [bar] | 1.2 | 1.2 | 15.0 | 35.0 | 68.0 | 50.0 |
OPER | [kEUR・a−1] | 0 | 0 | 0 | 0 | 7,200 | 5,000 |
Quantity | Unit | Value | Quantity | Unit | Value |
---|---|---|---|---|---|
[kg・(kmol)−1] | 46.00 | [EUR・kg−1] | 0.786 | ||
[kg・(kmol)−1] | 32.00 | [EUR・kg−1] | 0.654 | ||
[kg・(kmol)−1] | 18.00 | [EUR・kg−1] | 0.390 | ||
- | 0.23 | [EUR・(GJ)−1] | 2.620 | ||
- | 0.70 | [EUR・(GJ)−1] | 0.490 | ||
- | 1.002 | [EUR・(GJ)−1] | 4.240 | ||
[kg・(kmol)−1] | −23,400 | ddv | [%] | 20.00 | |
[kg・m−3] | 800.0 | [kEUR・m−2] | 6.121 | ||
[kJ・(kmol・K)−1] | 8.314 | [kEUR・m−3] | 500.0 | ||
[s] | 3,000 | [kEUR] | 20,000.0 | ||
[kW・(K・m2)−1] | 0.500 | [kEUR・(kW)−1] | 100.0 | ||
[kW・(K・m2)−1] | 0.500 | [kEUR] | 500.0 | ||
[kW・(K・m2)−1] | 0.500 | [kEUR・(kgCO2)−1] | 15 ∙ 10-6 | ||
[m2] | 400.0 | [kw] | 500.0 | ||
[m2] | 400.0 | [kEUR・a−1] | 13,000 | ||
[m2] | 400.0 | [h] | 8,760 | ||
[m3] | 100.0 | [a] | 10 |
The study was based on data obtained from the existing MeOH plant. The remaining data were taken from the literature and computer simulations (Aspen Plus). Data processing was conducted using the following computer programs: Excel (collecting of inputted data and results processing), ASPEN PLUS [
This work covered two sets of results. The first part of the results covered the quantitative calculations of the minimal UC of individual process alternatives and economic evaluation of the optimal scenario at the required limits of simple and complex reconstruction pathways. The second part examined the suitability of the reconstruction method regarding multi-product production and economically evaluated the optimal alternative.
Minimal UC was calculated using the SYNHEAT program in the GAMS [
The optimal alternative process scheme E represents a direct synthesis process for the production of DME from NG at high pressure, as in Appendix VI. Pre-formed SNG from the reformer is first cooled to 102˚C and then compressed over 3-stages within the compressors (COMP-1E, COMP-2E and COMP-3E) at 68.0 bars. Cooling of the mixture is necessary due to discharge of the H2O present. The feed into the DME reactor (slurry/liquid phase) (REAC-DME-E) is preheated to 190˚C. The equilibrium chemical reaction of forming DME is conducted over 3 stages (R1-R4). The produced products from the reactor are cooled in a refrigerator (COOL-1E) to 65˚C, and their pressure potentials are exploited with the usage of a gas turbine. Separation of the gas products is carried out in an absorption column (SEP-CO2) at −45.0˚C, where removal is conducted of the CO2 present. Further separation of the liquid mixture is carried out over a series of two distillation columns (DEST-1E and DEST-2E). DME is produced in the first column and the remainder enriched with MeOH, and H2O is separated in the second rectification column. In the latter MeOH arises at the top and H2O at the bottom of the column.
The results listed in
Quantity | Unit\alternative i | A | B | C | D | E | F |
---|---|---|---|---|---|---|---|
QC | [kw] | 5,466.5 | 4,752.4 | 7,716.6 | 6,966.8 | 9,321.0 | 9,670.0 |
QH | [kw] | 2,080.7 | 4,612.3 | 2,754.9 | 8,228.5 | 5,914.7 | 6,010.0 |
[kEUR・a−1] | −1,129.8 | 463.0 | 156.4 | 797.5 | 9,910.7 | 7,338.6 | |
Selection | - | X | X | X | X | X |
m3) with catalyst filler represented the majority of the amortization. The distillation columns were excluded from the amortization. There was no need to purchase an additional heater or cooler within the planned process; it was only necessary to purchase an additional heat exchanger (A ≈ 54.0 m2). Modification of the reformer and operation at high temperatures were additional operating costs, which were estimated to be approximately 7,200 kEUR/a. The total annual profit from the alternatives amounted to more than 9,900 kEUR.
Quantity | Unit | Value | Quantity | Unit | Value |
---|---|---|---|---|---|
y | - | 5 (*) | OPER | [kEUR・a−1] | 7,200 |
[kw] | 9,321.1 | AH | [m2] | - | |
[kw] | 5,914.7 | AC | [m2] | - | |
prih | [kEUR・a−1] | 79,194.6 | AEX | [m2] | 54.0 |
raw | [kEUR・a−1] | 57,985.7 | AREAC | [m3] | 22.0 |
UC | [kEUR・a−1] | 926.7 | PCOMP | [kw] | 211.0 |
TAXE | [kEUR・a−1] | 41.2 | Z | [kEUR・a−1] | 9,910.7 |
AMORT | [kEUR・a−1] | 3,130.4 |
(*) 5th is the optimal process alternative with name E.
The reconstruction method of multi-product production and flexible operation has confirmed the foresight on the possible improvements to existing non-profitable industrial process. The suitability of the method, which can transform MeOH process into a technologically, environmentally, and above all economically more favourable process, was confirmed regarding the examined case.
This article conceptually presented the reconstruction method in regard to the direction of multi-product production regarding industrial processes. The reconstruction technique can be expected to cover: 1) change of productivity, 2) change in the method of obtaining the product/-s and 3) modification on the side of input raw materials. The reconstruction pathway represented: an analysis of the state of chemical plant, the search for simple and complex alternatives regarding multi-product production, simulations of potential process alternatives with an integrated computer-aided software, the search for mathematical connections between chemical and physical quantities, mathematical modelling of a super-structure, and quantitative evaluation of the method’s results. The purpose of mathematical modelling and optimization regarding reconstruction in the direction of multi-product production is the establishment of appropriate formulation. This formulation enables easier decision-making and searching for appropriate solutions between potential reconstructive pathways. Mathematical formulation pre- sents a set of equations and inequality conditions representing mass and energy balances, connections for the size of process equipment, specifications of the temperatures and pressures of individual process units, and restrictive requirements. Mentioned program chooses between simple and complex pathways and process alternatives. Complex reconstruction pathways are more demanding in comparison with simple ones as they represent interference with the already constructed structure of an industrial process. They also represent higher costs, are more effective in most cases and their solutions help to improve the states of the existing plants. Computer-aided software that enables systematic data collection and processing plays an important role during the modelling and optimization.
The prices of raw materials and the prices of market products play important roles in the process of transforming one fuel (for example NG to DME, MeOH, etc.), which are physically, technologically, environmentally and economically more favourable. In comparison with the indirect synthesis of DME (simple reconstruction pathway), the lower operating costs of direct synthesis regarding DME (complex reconstruction pathway) were confirmed. Alternatives to the indirect pathways of the synthesis are cheaper from the point of view of investment contribution during reconstruction but their performances deteriorate. The efficiency of single-step DME from SNG is significantly higher, which justifies the functionality of chemical process planning in this direction.
In the future it will be reasonable to develop reconstruction methods for industrial processes. These reconstruction methods would have to be based on a more efficient yield of reactants (new catalysts), on the production of new products, and on a new process synthesis.
This research work was funded by the Public Agency for the Development of the Republic of Slovenia (ADRS), the Ministry of Education, Science, Culture and Sport, for which we sincerely thank them.