16版DOC1-Project Summary

annual output of 5,000 tons of tert - butylamine project Project Summary Xiangtan University 3+2=Team - 1 - CatalogueI. Project introduction- 1 -1.1 Project background- 1 -1.2 Project information- 2 -. Process design- 2 - Technological innovation- 4 -3.1 Process scheme and equipment innovation- 4 -3.1.1 Use of membrane separator- 4 -3.1.2 Use of the fractionating tower next door- 5 -3.2 Process scheme and equipment innovation- 6 -3.2.1 Use of the fractionating tower next door- 6 -3.2.2 Application of dual-effect rectification technology- 7 -3.2.3 Add a waste liquid recycling treatment section- 8 -. Energy-saving design- 9 -V. Equipment design- 9 -.Control system- 9 -.Safety design- 10 -. Site selection and site layout- 12 -.Economic analysis- 15 - Description of projectI. Project introduction1.1 Project backgroundIn recent years, with the enhancement of global environmental awareness, new green chemical products and chemical processes have emerged to replace the harmful chemicals and traditional processes that affect ecological balance, air and water pollution.The future development of tert - butylamine products has come into being, so that the application of tert - butylamine has further development.For example, it is synthesized from tert-butylamine and n-tert-butyl-2-benzothiazolidine-sulfonamide (rubber accelerator NS) and n-tert-butyl2-benzothiazolidine-sulfonamide (TBSI).At present, tert-butylamine is used as the main raw material of synthetic rubber vulcanization accelerator NS in foreign countries, while tert-butylamine produced in China is mainly used as the synthetic material of drug rifampicin.During the eleventh five-year plan period, the development strategy of Chinas rubber additives industry is to further adjust product structure and reduce costs.The product structure adjustment first reduced the production ratio of high toxicity, low efficiency and heavy pollution naphthylamine anti-aging agents and thiazole accelerators, and increased the proportion of secondary sulfonamide promoters.The demand for tert-butylamine will increase substantially.According to literature statistics, the proportion of rubber accelerators in China in 1995 was 55% of thiazole accelerators, 25% of secondary sulfonamides and 20% of others.According to the requirements of the 11th five-year plan, the production ratio of secondary sulfonamide accelerators in China will reach 50% this year.At present, the main types of secondary sulfonamides accelerators in China are nobsn-oxadiethylbenzene and thiazo-2-sulfonamide. Due to the presence of secondary amine groups in NOBS molecules, it is easy to form n-nitrosamine structures that can cause cancer during the vulcanization process.Developed foreign countries such as west Germany, Japan and the United States have banned the use of NOBS in the production of rubber tires, and are replacing NOBS with NS.As a kind of aftereffect accelerator, NS does not produce n-nitrosamine which can cause cancer in the vulcanization process. It also has the advantages of general secondary sulfonamide accelerators.Therefore, NS in the current concept of green tires has become a highly valued variety.Under such market demand, this project aims to rebuild a 50 million ton/year tert-butylamine production plant based on qilu petrochemical company. The plant is located in qilu industrial park, zibo city, shandong province.The company was founded in 1966, and after 50 years of construction, it has developed into a large oil processing, petrochemical, coal chemical, natural gas chemical, salt chemical industry as a whole, complete set of large-scale oil refining, chemical, chemical fiber joint enterprises.The total investment is expected to be 180 million yuan, which is expected to be completed and put into production within two years.1.2 Project information(I) project name: annual output of 5,000 tons of tert - butylamine projectName and nature of the sponsor: qilu petrochemical company (state-owned enterprise)(3) project construction content, location, scale and objectives:This project is a reconstruction and expansion project for qilu petrochemical company, which is expected to produce 5,000 tons of tert-butylamine annually. The plant is located in linzi qilu chemical industrial park, zibo city, shandong province. The total investment is expected to be 180 million yuan, which is expected to be completed and put into production within two years.Nature of the investment project: reconstruction. Process design(1) MTBE synthesis sectionAfter the extraction of butadiene, the residual carbon 4 from the outside tank area of the boundary zone entered the carbon 4 raw material tank V0101 of the device after being measured.The methanol from the self-provided tank outside the boundary zone enters the methanol raw material tank V0102 of the device after being measured.The residual liquid raw material and methanol raw material are respectively pressurized by the feed pump P0101A/B and P0102A/B. The pressurized methanol is mixed into the MTBE synthetic raw material mixer M0101 in a certain proportion with the pressurized residual liquid.Hybrid materials by the raw material preheater E0101 preheating, raw material preheater by low pressure steam heating, the temperature controller to control the temperature within 80 and then into the reactor.Finally, the material after the reaction is discharged from the bottom of the reactor and sent to V0103 in the coarse MTBE buffer tank via preheater E0102.(2) MTBE purification sectionThe material from V0103 buffer tank of crude MTBE is pressurized by reactor feed pump P0201A/B, and then enters the distillation column T0201. The product is discharged from tower kettle and sent to V0201 of crude MTBE product tank.After rectification, the top carbon fraction of the column goes into the rectification of T0202 of the delightening column, and the sold ether carbon tetrad is obtained, in which the content of 1-butene is over 40% (mass fraction).The crude MTBE product tank V0201 materials enter the distillation column T0203 for further distillation, and the MTBE products with purity of more than 98% are obtained in the tower kettle.The methanol solution containing part of MTBE was obtained on the top of the tower, and was fed into the membrane separator S0201 for membrane separation. After separation, high purity methanol was recovered for recycling.(3) MTBE cracking sectionFrom MTBE distillation lateral line production of methyl tert-butyl ether into the preheater E0301 coil with reaction gas from pyrolysis reactor R0301 heat exchange, methyl tert-butyl ether after preheating gas into E0302 superheater tube side by high temperature heat conduction oil heating further, after the reaction temperature will be from the upper inlet into the pyrolysis reactor R0301 tube side.In the cracking reactor R0301, methyl tert-butyl ether was decomposed to form isobutylene and methanol under the catalysis of solid acid catalyst.(4) isobutylene purification sectionAfter the material from V0401 of crude isobutylene buffer tank is decompressed by the pressure reducing valve, the amount of recovery is controlled by the regulating valve and T0402 of the isobutylene deweighting tower is entered.The waste from the tower kettle of iso-butene deweighting tower is mainly unconverted methyl tert-butyl ether, isobutene and a small amount of polymers.After the crude isobutylene passed the distillation column T0401, the low purity methanol was obtained in the tower kettle, and the high purity methanol was obtained for recycling after the methanol recovery column T0403.The process flow diagram is shown in FIG. 4-1.(5) tertiary butylamine synthesis sectionFirst raw material liquid ammonia and isobutylene, respectively, through the pump P0501 and P0502 and transport to preheater E0501, hybrid heating, with the products of reaction, then the heat exchanger E0502, after the heater E0503 heated to set temperature junior reactor R0501 reaction, after the completion of reaction, reaction products and feed mixture in a heat exchanger E0502 cooled to set temperature, ready to separate.(6) tertiary butylamine double - effect distillation sectionMix to feed to the tower T0601 central position, the tower separation unreacted ammonia, the separation of ammonia by the preheater E0601 feeding reaction to the next, tower by using pressure differential pressure to sign the mixed material tower T0502 feed in central position, the tower isolated unreacted isobutylene, separation of isobutylene via compressor C0501 conveying to the next feeding reaction, isolated tower kettle product tert-butylamine, column reactor for reaction system there may be a small amount of water or very small amounts of olefin polymer.The process flow diagram is shown in figure 2-1:FIG. 2-1 process flow chart Technological innovation3.1 Process scheme and equipment innovation3.1.1 Use of membrane separatorThe use of advanced membrane separation technology, the energy consumption is larger, methanol content in low carbon four components, using instead of traditional distillation process and equipment, flow separation with methanol in the feed stocks and MTBE product, make a discharge of MTBE product purity can reach 99.99%, so the method of using membrane separation purification MTBE can receive very good economic returns;Another batch of methanol is produced for recycling, which greatly reduces the amount of fresh methanol supplement and can save about 1.45 million yuan of production cost every year, which has significant economic benefits.Since Aspen Plus does not have a membrane separation simulation unit, the Aspen user model is adopted to simulate the separation process. The simulation diagram is shown in figure 2-2.FIG. 2-2 schematic diagram of membrane separation unit3.1.2 Use of the fractionating tower next doorThe waste liquid waste gas was purified by the next distillation column, and the high purity 1-butene ether carbon 4 was sold as a by-product.The next tower consists of two towers (a main tower and a secondary tower) and a full condenser and a reboiler.In addition, because use next door tower to replace double tower, still can save equipment investment.The simulation flow diagram of the next column is shown in figure 2-3.FIG. 2-3 flow chart of simulation of next door distillation column3.2 Process scheme and equipment innovation3.2.1 Use of the fractionating tower next doorbutylamine rectification, ammonia, isobutene and tert-butylamine are separated by three-column process, namely ammonia distillation column, isobutene rectification column and tert-butylamine distillation column.Because the tert butylamine obtained after reaction contains partial ammonia and isobutylene, the main function of the first two distillation columns is to remove ammonia and isobutylene, so as to further purify tert butylamine.In this design, by adding double-effect distillation in the sixth stage, isobutylene and tert-butylamine were separated in the second column at the same time, so that isobutylene was removed in the second column, so a distillation column was omitted.By optimizing the tertiary butylamine distillation section from three towers to two towers, the process is simplified and the equipment investment is saved.The improved process of tert-butylamine distillation section is shown in FIG. 2-4.FIG. 2-4 flow chart of tertiary butylamine distillation section3.2.2 Application of dual-effect rectification technologyIn the tert-butylamine refining unit, in order to reduce the energy consumption of the distillation column, this project adopts dual-effect distillation technology for the tert-butylamine distillation column. The simulation flow chart of this section is shown in FIG. 2-5.FIG. 2-5 flow chart of double-effect distillationThe dual-effect rectification technology USES the latent heat of steam on the top of the high pressure tower to provide energy to the low pressure reboiler. By designing the double-effect rectification method to change the traditional conventional rectification method, the condensing heat of ordinary steam is reasonably utilized to realize the thermal integration between the inner column and the tip of the column of the distillation column, and the energy consumption is greatly reduced.It also reduces the input of a condenser and a reboiler.Compared with single column distillation and double - effect distillation, double - effect distillation has higher heat energy efficiency than single - effect distillation, and double - effect distillation is more energy efficient than single - effect distillation.Compared with traditional single column distillation, double - effect distillation can save 15%-35% energy.3.2.3 Add a waste liquid recycling treatment sectionA recovery and treatment section for residual liquid was set up, which effectively recovered methanol, liquid ammonia and isobutene, reduced the use and consumption of raw materials, increased the output of products, and saved the investment of raw materials.The general production process does not further recycle the useful components in the residual liquid, the simplest way is to separate the recombination produced by separation into fuel oil, the exhaust gas pipeline as fuel gas, or the residual liquid to the public works.This practice not only wastes raw materials and products, but also fails to recover the useful components in the residual liquid, increasing the processing cost, especially for the more expensive components, which is even less economical.Therefore, in this design, the residual liquid containing raw material flow shares will be recycled and recycled, as shown in figure 2-6 below:FIG. 2-6 flowchart of recycling residual liquid. Energy-saving designWith the increase of energy price, the traditional high-energy enterprises gradually develop into energy-saving enterprises.Under this trend, energy-saving technology emerges at the historic moment. From the improvement of single equipment to the global thermal integration, energy-saving technology is constantly improved and developed.In this design, according to the actual production situation, we use the latent heat of steam on the top of the high pressure tower to provide energy to the low pressure reboiler. By changing the traditional conventional rectification method by designing a double-effect rectification method, we not only reduce the equipment input of a condenser and a reboiler, but also save energy significantly.In this design, the residual liquid produced in the rectification stage contains usable raw materials, which are further rectified and purified to be recycled. The recycling use of this liquid not only saves the treatment cost of the residual liquid, but also reduces the input of raw materials.V. Equipment designAccording to the simulation results of Aspen plus, we designed the product reaction distillation column T0201, heat exchanger E0102 and MTBE synthesis reactor R0101 in the process, including the basic equipment design parameters and the design of special internal components.Using sw6-2011 and cup-tower software, the process design, basic parameter design and mechanical strength check of Tower equipment in the process were carried out.Use SW6-2011 and Aspen Exchanger Design and Rating of the heat Exchanger process Design, basic parameters selection, Design and mechanical intensity.The mechanical strength of the reactor was checked by SW6-2011.In addition, the pump, storage tank and other equipment were selected and designed, and the pump was selected with intelligent pump selection software, and the strength of the separator and storage tank was checked by sw6-2011.See the first chapter of equipment design selection for details.Control systemIn the design of this project, we first consider the steady state control strategy during normal production.The control system designed by us is mainly composed of DCS distributed control system, which mainly USES information feedback to control valve flow and display pressure, temperature and liquid level of pressure vessels and pipelines. The complex control system used is controlled by the ratio of feeding amount.(1) for the control of liquid centrifugal pump, the pipe characteristic curve is changed by changing the opening degree of the outlet valve of the pump, so as to achieve the purpose of control.(2) for the control of heat exchangers, the main function of such heat exchangers is to heat or cool the process logistics to the target value.This project adopts the control scheme of the heat transfer volume as the operating variable.For process logistics interflow heat exchangers, such heat exchangers are designed to save energy and to heat or cool materials to the target value so that the two streams can fully heat.This project adopts the control scheme of the heat transfer volume as the operating variable.(3) for the control of the reactor, the control of the kettle reactor includes temperature control, liquid level control, and pressure temperature indication;The control of the tubular reactor includes temperature control, liquid level control, and pressure temperature indication.(4) for the control of the distillation column, the control scheme of the distillation column in this project includes the control of the tower body, the control of the tower top condenser, the control of the tower kettle reboiler and the control of the reflux tank.Safety designIn terms of safety design, the following points are mainly met:(1) the process equipment shall be centrally arranged in accordance with the requirements of production, operation safety a