CN111909036A - A DMC production system and method - Google Patents
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- 238000004519 manufacturing process Methods 0.000 title claims abstract description 32
- 238000000034 method Methods 0.000 title claims abstract description 22
- 238000005886 esterification reaction Methods 0.000 claims abstract description 191
- 230000032050 esterification Effects 0.000 claims abstract description 188
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 claims abstract description 129
- 238000003786 synthesis reaction Methods 0.000 claims abstract description 60
- 238000006243 chemical reaction Methods 0.000 claims abstract description 57
- 150000002148 esters Chemical class 0.000 claims abstract description 42
- 230000015572 biosynthetic process Effects 0.000 claims abstract description 38
- GRYLNZFGIOXLOG-UHFFFAOYSA-N Nitric acid Chemical compound O[N+]([O-])=O GRYLNZFGIOXLOG-UHFFFAOYSA-N 0.000 claims abstract description 37
- 229910017604 nitric acid Inorganic materials 0.000 claims abstract description 37
- 239000007788 liquid Substances 0.000 claims abstract description 33
- IOVCWXUNBOPUCH-UHFFFAOYSA-N Nitrous acid Chemical compound ON=O IOVCWXUNBOPUCH-UHFFFAOYSA-N 0.000 claims abstract description 17
- 239000007789 gas Substances 0.000 claims description 41
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 30
- 229910001868 water Inorganic materials 0.000 claims description 27
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 16
- 239000000463 material Substances 0.000 claims description 8
- 229910052757 nitrogen Inorganic materials 0.000 claims description 8
- 238000010992 reflux Methods 0.000 claims description 8
- 239000000203 mixture Substances 0.000 claims description 6
- 239000000126 substance Substances 0.000 claims description 5
- 239000012530 fluid Substances 0.000 claims 1
- 239000002699 waste material Substances 0.000 abstract description 8
- 238000007086 side reaction Methods 0.000 abstract description 6
- 230000006315 carbonylation Effects 0.000 abstract description 4
- 238000005810 carbonylation reaction Methods 0.000 abstract description 4
- 238000002309 gasification Methods 0.000 abstract description 4
- 238000005859 coupling reaction Methods 0.000 abstract description 2
- 238000000066 reactive distillation Methods 0.000 abstract description 2
- IEJIGPNLZYLLBP-UHFFFAOYSA-N dimethyl carbonate Chemical compound COC(=O)OC IEJIGPNLZYLLBP-UHFFFAOYSA-N 0.000 description 48
- BLLFVUPNHCTMSV-UHFFFAOYSA-N methyl nitrite Chemical compound CON=O BLLFVUPNHCTMSV-UHFFFAOYSA-N 0.000 description 10
- MWUXSHHQAYIFBG-UHFFFAOYSA-N nitrogen oxide Inorganic materials O=[N] MWUXSHHQAYIFBG-UHFFFAOYSA-N 0.000 description 6
- 238000003763 carbonization Methods 0.000 description 2
- 238000009833 condensation Methods 0.000 description 2
- 230000005494 condensation Effects 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 238000004821 distillation Methods 0.000 description 2
- 239000000945 filler Substances 0.000 description 2
- 238000010438 heat treatment Methods 0.000 description 2
- 238000012856 packing Methods 0.000 description 2
- 238000003756 stirring Methods 0.000 description 2
- 230000009286 beneficial effect Effects 0.000 description 1
- 125000002915 carbonyl group Chemical group [*:2]C([*:1])=O 0.000 description 1
- 239000013064 chemical raw material Substances 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 238000010168 coupling process Methods 0.000 description 1
- 230000007423 decrease Effects 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 125000000524 functional group Chemical group 0.000 description 1
- 150000003949 imides Chemical class 0.000 description 1
- 230000002401 inhibitory effect Effects 0.000 description 1
- 231100001231 less toxic Toxicity 0.000 description 1
- 231100000053 low toxicity Toxicity 0.000 description 1
- 125000000956 methoxy group Chemical group [H]C([H])([H])O* 0.000 description 1
- 125000002496 methyl group Chemical group [H]C([H])([H])* 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 238000007670 refining Methods 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 230000009469 supplementation Effects 0.000 description 1
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- C07C68/00—Preparation of esters of carbonic or haloformic acids
- C07C68/01—Preparation of esters of carbonic or haloformic acids from carbon monoxide and oxygen
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C68/00—Preparation of esters of carbonic or haloformic acids
- C07C68/08—Purification; Separation; Stabilisation
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Abstract
一种DMC生产系统包括合成反应主循环圈；合成反应主循环圈包括DMC合成反应器、循环压缩机、第一酯化塔、酯脱塔；DMC合成反应器一端通过所述的循环压缩机与所述第一酯化塔一端连接；DMC合成反应器另一端通过所述的酯脱塔与所述第一酯化塔另一端连接；DMC生产方法包括所述合成反应主循环反应，酯化并联旁路反应。本发明的优点是，DMC合成羰化偶联反应系统，采用反应精馏酯化并联旁路，满足DMC合成各项工艺参数的同时，保证硝酸还原效率更高，有效降低硝酸的消耗量，使废液硝酸含量更低。有效降低甲醇消耗量，有效降提高返回DMC合成圈气化组分甲醇含量，降低外排废液中甲醇含量。同时减少酯化塔内副反应，减少了硝酸及亚硝酸的生成量，提高酯化反应效率。
A DMC production system includes a synthesis reaction main circulation loop; the synthesis reaction main circulation loop includes a DMC synthesis reactor, a circulation compressor, a first esterification tower, and an ester removal tower; one end of the DMC synthesis reactor passes through the circulation compressor and One end of the first esterification tower is connected; the other end of the DMC synthesis reactor is connected to the other end of the first esterification tower through the ester removal tower; the DMC production method includes the main circulation reaction of the synthesis reaction, and the esterification is connected in parallel Bypass reaction. The advantages of the present invention are that, the DMC synthesis carbonylation coupling reaction system adopts the parallel bypass of reactive distillation and esterification, which can satisfy various process parameters of DMC synthesis, ensure higher nitric acid reduction efficiency, effectively reduce the consumption of nitric acid, and reduce the consumption of nitric acid. The nitric acid content of the waste liquid is lower. It can effectively reduce the consumption of methanol, effectively reduce the methanol content of the gasification components returned to the DMC synthesis circle, and reduce the methanol content in the discharged waste liquid. At the same time, the side reactions in the esterification tower are reduced, the generation of nitric acid and nitrous acid is reduced, and the efficiency of the esterification reaction is improved.
Description
技术领域technical field
本发明涉及应用于气相碳基化法生产DMC的系统及方法。The present invention relates to a system and method for producing DMC by a gas-phase carbonization method.
背景技术Background technique
碳酸二甲酯(dimethyl carbonate，DMC)，是一种低毒、环保性能优异、用途广泛的化工原料，它是一种重要的有机合成中间体，分子结构中含有羰基、甲基和甲氧基等官能团，具有多种反应性能，在生产中具有使用安全、方便、污染少、容易运输等特点。由于碳酸二甲酯毒性较小，是一种具有发展前景的“绿色”化工产品。Dimethyl carbonate (DMC) is a chemical raw material with low toxicity, excellent environmental performance and wide application. It is an important intermediate in organic synthesis. Its molecular structure contains carbonyl, methyl and methoxy groups. and other functional groups, has a variety of reactive properties, and has the characteristics of safe use, convenience, less pollution, and easy transportation in production. Because dimethyl carbonate is less toxic, it is a "green" chemical product with development prospects.
目前成熟的直接合成DMC的工艺是甲醇羰化偶联法。其中目前在亚酯补充的工序。采用的是搅拌反应釜，存在电耗高，硝酸还原效率低，机械运转设备安全稳定性差等缺点。现采用并联反应精馏酯化工艺，满足DMC合成各项工艺参数的同时，能够保证硝酸还原效率更高，有效降低硝酸的消耗量，确保废液硝酸含量更低。有效降低甲醇的消耗量，有效降提高返回DMC合成圈的气化组分甲醇含量，降低外排废液中甲醇含量。增加了对硝酸还原的反应控制手段，装置运行更稳定，安全性更高。同时减少酯化塔内副反应氮氧化物和水生的副反应，减少了硝酸及亚硝酸的生成量，提高酯化反应效率。At present, the mature technology of direct synthesis of DMC is methanol carbonylation coupling method. Among them, it is currently in the process of imide supplementation. A stirring reaction kettle is used, which has disadvantages such as high power consumption, low nitric acid reduction efficiency, and poor safety and stability of mechanical operation equipment. The parallel reaction distillation and esterification process is now used, which can meet the various process parameters of DMC synthesis, and can ensure higher nitric acid reduction efficiency, effectively reduce the consumption of nitric acid, and ensure that the nitric acid content of the waste liquid is lower. It can effectively reduce the consumption of methanol, effectively reduce the methanol content of the gasification component returned to the DMC synthesis circle, and reduce the methanol content in the discharged waste liquid. The reaction control method for the reduction of nitric acid is added, and the device runs more stably and with higher safety. At the same time, the side reactions of nitrogen oxides and aquatic side reactions in the esterification tower are reduced, the generation amount of nitric acid and nitrous acid is reduced, and the efficiency of the esterification reaction is improved.
发明内容SUMMARY OF THE INVENTION
本发明涉及一种气相碳基化法生产DMC生产系统及方法。DMC合成羰化偶联反应系统，采用反应精馏酯化并联旁路，满足DMC合成各项工艺参数的同时，能够保证硝酸还原效率更高，有效降低硝酸的消耗量，确保废液硝酸含量更低。有效降低甲醇的消耗量，有效降提高返回DMC合成圈的气化组分甲醇含量，降低外排废液中甲醇含量。增加了对硝酸还原的反应控制手段，装置运行更稳定，安全性更高。同时减少酯化塔内副反应氮氧化物和水生的副反应，减少了硝酸及亚硝酸的生成量，提高酯化反应效率。The invention relates to a production system and method for producing DMC by a gas-phase carbonization method. The DMC synthesis carbonylation coupling reaction system adopts the parallel bypass of reactive distillation and esterification to meet the various process parameters of DMC synthesis, and at the same time, it can ensure higher nitric acid reduction efficiency, effectively reduce the consumption of nitric acid, and ensure that the nitric acid content of the waste liquid is higher. Low. It can effectively reduce the consumption of methanol, effectively reduce the methanol content of the gasification component returned to the DMC synthesis circle, and reduce the methanol content in the discharged waste liquid. The reaction control method for the reduction of nitric acid is added, and the device runs more stably and with higher safety. At the same time, the side reactions of nitrogen oxides and aquatic side reactions in the esterification tower are reduced, the generation amount of nitric acid and nitrous acid is reduced, and the efficiency of the esterification reaction is improved.
实现本发明专利目地的技术方案是，一种DMC生产系统包括合成反应主循环圈；The technical scheme for realizing the purpose of the patent of the present invention is that a DMC production system includes a main circulation loop of the synthesis reaction;
所述的合成反应主循环圈包括DMC合成反应器、循环压缩机、第一酯化塔、酯脱塔；The main circulation loop of the synthetic reaction comprises a DMC synthesis reactor, a circulating compressor, a first esterification tower, and an ester removal tower;
所述的DMC合成反应器一端通过所述的循环压缩机与所述第一酯化塔一端连接；One end of the described DMC synthesis reactor is connected with one end of the first esterification tower by the described recycle compressor;
所述的DMC合成反应器另一端通过所述的酯脱塔与所述第一酯化塔另一端连接。The other end of the DMC synthesis reactor is connected with the other end of the first esterification tower through the ester stripping tower.
优选的，所述的DMC生产系统还包括酯化并联旁路；Preferably, described DMC production system also comprises esterification parallel bypass;
所述的酯化并联旁路包括第二酯化塔、增压机；The esterification parallel bypass includes a second esterification tower and a booster;
所述的第二酯化塔下端通过增压机与所述的酯脱塔连接；The lower end of the second esterification tower is connected with the ester stripping tower through a booster;
所述的第一酯化塔与所述的第二酯化塔连接。The first esterification tower is connected with the second esterification tower.
优选的，所述的DMC生产系统还包括酯化并联旁路；所述的酯化并联旁路包括塔顶冷凝器、第二酯化塔、增压机，在所述第二酯化塔上端设有精馏部件，所述的第二酯化塔内气体通过精馏部件排出所述第二酯化塔；Preferably, the DMC production system also includes an esterification parallel bypass; the esterification parallel bypass includes a column top condenser, a second esterification tower, and a booster, and at the upper end of the second esterification tower A rectification part is provided, and the gas in the second esterification tower is discharged from the second esterification tower through the rectification part;
所述的第二酯化塔下端通过增压机与所述的酯脱塔连接；The lower end of the second esterification tower is connected with the ester stripping tower through a booster;
所述的第二酯化塔上端精馏部件通过塔顶冷凝器与第一酯化塔连接；The upper rectification part of the second esterification tower is connected with the first esterification tower through the overhead condenser;
所述的第一酯化塔与所述的第二酯化塔连接。The first esterification tower is connected with the second esterification tower.
进一步讲，所述的塔顶冷凝器通过回流管与所述的第二酯化塔连接。Further, the column top condenser is connected with the second esterification column through a reflux pipe.
进一步讲，在所述的回流管上设有回流液罐。Further, a return liquid tank is provided on the return pipe.
进一步讲，所述的通过管道向第二酯化塔补充水和/或甲醇和/或硝酸和/或亚硝酸一种或几种的组合液体。Further, the second esterification tower is supplemented with one or more combination liquids of water and/or methanol and/or nitric acid and/or nitrous acid through the pipeline.
一种DMC生产方法包括所述合成反应主循环反应，第一酯化塔3气体经过循环压缩机，进入DMC合成反应器、酯脱塔加压、反应、分离后得到DMC产品；A DMC production method comprises the main circulation reaction of the synthesis reaction, the gas of the
所述酯化并联旁路反应，酯脱塔排出气体包括氮气、CO、甲醇、MN、NOX、CO2之一或几种组合，气体经增压机加压后进入第二酯化塔中、第一酯化塔塔液进入第二酯化塔中，在第二酯化塔内与硝酸和/或甲醇和/或水和/或亚硝酸液体混合物反应，生产酯类物资并产生热量，气态酯类物质、甲醇、水进入第二酯化塔的精馏部件，经过精馏部件后，水被分离，甲醇及酯类物质与合成气一起进入第一酯化塔。In the parallel bypass reaction of esterification, the exhaust gas of the esterification tower includes one or several combinations of nitrogen, CO, methanol, MN, NOx , and CO2 , and the gas enters the second esterification tower after being pressurized by a booster. , the first esterification tower liquid enters the second esterification tower, reacts with nitric acid and/or methanol and/or water and/or nitrous acid liquid mixture in the second esterification tower, produces ester materials and generates heat, The gaseous esters, methanol and water enter the rectification part of the second esterification tower. After passing through the rectification part, the water is separated, and the methanol and esters enter the first esterification tower together with the synthesis gas.
一种DMC生产方法包括合成反应主循环反应、酯化并联旁路反应；A DMC production method comprises a main circulation reaction of a synthesis reaction and a parallel bypass reaction of esterification;
所述合成反应主循环反应，第一酯化塔气体经过循环压缩机，进入DMC合成反应器、酯脱塔加压、反应、分离后得到DMC产品；In the main circulation reaction of the synthesis reaction, the gas of the first esterification tower passes through the circulation compressor and enters the DMC synthesis reactor, and the esterification tower is pressurized, reacted and separated to obtain the DMC product;
所述酯化并联旁路反应，酯脱塔排出气体包括氮气、CO、甲醇、MN、NOX、CO2之一或几种组合，气体经增压机加压后进入第二酯化塔中、第一酯化塔塔液进入第二酯化塔中，在第二酯化塔内与硝酸和/或甲醇和/或水和/或亚硝酸液体混合物反应，生产酯类物资并产生热量，气态酯类物质、甲醇、水进入第二酯化塔反应后一起进入第一酯化塔。In the parallel bypass reaction of esterification, the exhaust gas of the esterification tower includes one or several combinations of nitrogen, CO, methanol, MN, NOx , and CO2 , and the gas enters the second esterification tower after being pressurized by a booster. , the first esterification tower liquid enters the second esterification tower, reacts with nitric acid and/or methanol and/or water and/or nitrous acid liquid mixture in the second esterification tower, produces ester materials and generates heat, The gaseous esters, methanol and water enter the second esterification tower for reaction and then enter the first esterification tower together.
进一步讲，所述第二酯化塔6各反应室温度控制50-100℃。Further, the temperature of each reaction chamber of the
进一步讲，所述塔顶冷凝器5冷凝回流温度控制40-80℃。Further, the condensation reflux temperature of the column top condenser 5 is controlled at 40-80°C.
本发明有如下有益效果：The present invention has the following beneficial effects:
1、本发明采用工作原理是：是将酯化工艺应用于气相碳基化法生产DMC，能够保证DMC合成反应不做大的工艺调整，满足DMC生产的需求。1. The working principle of the present invention is as follows: the esterification process is applied to the gas-phase carbonylation method to produce DMC, which can ensure that the DMC synthesis reaction does not require large process adjustments and meets the needs of DMC production.
2、该工艺：能够保证硝酸还原效率更高，有效降低硝酸的消耗量，有效降低硝酸的消耗量，反应釜排出硝酸的浓度为2%-5%，本专利中第二号酯化塔排出的硝酸浓度为0.15%-0.5%，并确保废液硝酸含量更低，另采用反应塔替代反应釜，反应塔不用搅拌，其反应的过程不受搅拌速率的影响。2. This process: it can ensure higher nitric acid reduction efficiency, effectively reduce the consumption of nitric acid, and effectively reduce the consumption of nitric acid. The concentration of nitric acid discharged from the reactor is 2%-5%, and the second esterification tower in this patent discharges The concentration of nitric acid is 0.15%-0.5%, and the nitric acid content of the waste liquid is guaranteed to be lower. In addition, a reaction tower is used to replace the reaction kettle. The reaction tower does not need to be stirred, and the reaction process is not affected by the stirring rate.
3、该工艺：有效降低甲醇的消耗量，有效降提高返回DMC合成圈的气化组分甲醇含量，降低外排废液中甲醇含量。3. This process: effectively reduce the consumption of methanol, effectively reduce and increase the methanol content of the gasification component returned to the DMC synthesis circle, and reduce the methanol content in the discharged waste liquid.
4、该工艺：增加了对硝酸还原的反应控制手段，装置运行更稳定，安全性更高。4. The process: the reaction control means for the reduction of nitric acid is added, the device operation is more stable, and the safety is higher.
5、在第二酯化塔上端设有精馏部件，第二酯化塔及其上精馏部件与塔顶冷凝器相配合形了精馏反应体系，有效控制第二酯化塔内的反应温度，使其内的反应温度波动就小，其原理是，当第二酯化塔内的反应温度过高时，产生的水蒸气就过多，在塔顶冷凝器吸热回，水蒸气变成水回流至第二酯化塔内的水量也变多，从而实现对第二酯化塔内过高的反应温度进行降温，当第二酯化塔内的反应温度过低时，产生的水蒸气就较少，在塔顶冷凝器吸热回，水蒸气变成水回流至第二酯化塔内的水量也变少，第二酯化塔内反应温度会升高。5. A rectification part is arranged at the upper end of the second esterification tower, and the second esterification tower and its upper rectification part cooperate with the tower top condenser to form a rectification reaction system, which effectively controls the reaction in the second esterification tower The principle is that when the reaction temperature in the second esterification tower is too high, there will be too much water vapor, which will absorb heat back in the top condenser, and the water vapor will change. The amount of water that becomes water back to the second esterification tower also increases, so as to realize cooling the excessively high reaction temperature in the second esterification tower, when the reaction temperature in the second esterification tower is too low, the water produced There is less steam, and the heat is absorbed in the top condenser, and the amount of water returned to the second esterification tower from water vapor becomes less, and the reaction temperature in the second esterification tower will increase.
6、塔顶冷凝器有效控制进入第一酯化塔的气体含水率，因为气体含水率下降，从而抑制了第一酯化塔内气体生亚硝酸的副反应，使之生成MN的主反应效率更高。6. The top condenser effectively controls the water content of the gas entering the first esterification tower, because the water content of the gas decreases, thereby inhibiting the side reaction of nitrous acid generated from the gas in the first esterification tower, so that the main reaction efficiency of MN is generated. higher.
附图说明Description of drawings
下面结合附图和实施对本发明作进一步说明。The present invention will be further described below in conjunction with the accompanying drawings and implementation.
图1为本发明示意图。Figure 1 is a schematic diagram of the present invention.
图2为本发明优选示意图。Figure 2 is a preferred schematic diagram of the present invention.
如图中，DMC合成反应器1、循环压缩机2、第一酯化塔3、回流液罐4、塔顶冷凝器5、第二酯化塔6、酯脱塔7、增压机8。As shown in the figure,
具体实施方式：Detailed ways:
如图1中，一种DMC生产系统包括合成反应主循环圈；所述的合成反应主循环圈包括DMC合成反应器1、循环压缩机2、第一酯化塔3、酯脱塔7；As shown in Figure 1, a DMC production system includes a synthesis reaction main circulation circle; the synthesis reaction main circulation circle includes a
所述的DMC合成反应器1一端通过所述的循环压缩机2与所述第一酯化塔3一端连接；所述的DMC合成反应器1另一端通过所述的酯脱塔7与所述第一酯化塔3另一端连接。One end of the described
优选的，所述的DMC生产系统还包括酯化并联旁路；所述的酯化并联旁路包括第二酯化塔6、增压机8； 所述的第二酯化塔6下端通过增压机8与所述的酯脱塔7连接；增压机8采用离心式压缩机或者离心式高速风机；优选的，第二酯化塔6分成1-N段，各段内设置加热蒸汽盘管。经过增压机8升压后的气体，分成1-N股进入第二酯化塔6，Preferably, the DMC production system also includes an esterification parallel bypass; the esterification parallel bypass includes a
所述的第一酯化塔3与所述的第二酯化塔6连接。The
工作原理：经过增压机8升压后的气体，分成1-N股进入第二酯化塔6。第一酯化塔3与第二酯化塔6采用管道连接，第一酯化塔3塔液进入第二酯化塔6。通过管道向第二酯化塔6补充水和/或甲醇和/或硝酸和/或亚硝酸等反应物料。经过第二酯化塔6分成1-N段反应的气体，汇合到一起后进入，第二酯化塔6底部。第二酯化塔6各反应室温度控制50-100℃，第二酯化塔6发生硝酸和亚硝酸与甲醇生成亚硝酸甲酯（MN）、生成的气体进入第一酯化塔3，与在第一酯化塔3内主反应生成MN汇合、合成气含（氮气、CO、甲醇、MN、NOX、CO）经过循环压缩机2，DMC合成反应器1、酯脱塔7加压、反应、分离后得到DMC产品。Working principle: The gas boosted by the
如图2中，一种DMC生产系统包括合成反应主循环圈；所述的合成反应主循环圈包括DMC合成反应器1、循环压缩机2、第一酯化塔3、酯脱塔7；As shown in Figure 2, a DMC production system includes a synthesis reaction main circulation circle; the synthesis reaction main circulation circle includes a
所述的DMC合成反应器1一端通过所述的循环压缩机2与所述第一酯化塔3一端连接；所述的DMC合成反应器1另一端通过所述的酯脱塔7与所述第一酯化塔3另一端连接。One end of the described
优选的，所述的DMC生产系统还包括酯化并联旁路；所述的酯化并联旁路包括塔顶冷凝器5、第二酯化塔6、增压机8，在所述第二酯化塔6上端设有精馏部件（精馏部件为在第二酯化塔6上端装填的一段填料，填料可以是规整填料或者闪堆填料），所述的第二酯化塔6内气体通过精馏部件排出所述第二酯化塔6；Preferably, the DMC production system also includes an esterification parallel bypass; the esterification parallel bypass includes a tower top condenser 5, a
所述的第二酯化塔6下端通过增压机8与所述的酯脱塔7连接；The lower end of the
所述的第二酯化塔6上端精馏部件通过塔顶冷凝器5与第一酯化塔3连接；Described
所述的第一酯化塔3与所述的第二酯化塔6连接，所述的第二酯化塔6采用塔式进行硝酸还原生成MN反应。The
优选的，所述的塔顶冷凝器5通过回流管与所述的第二酯化塔6连接，塔顶冷凝器5及其上端的精馏部件及第二酯化塔6共同构成一个精馏反应体系。Preferably, the column top condenser 5 is connected with the
优选的，在所述的回流管上设有回流液罐4，设有回流液罐4可有效控制液体流量。Preferably, a
优选的，第二酯化塔6分成1-N段，各段内设置加热蒸汽盘管。经过增压机8升压后的气体，分成1-N股进入第二酯化塔6。Preferably, the
优选的，所述的塔顶冷凝器5通过回流管与所述的第二酯化塔6连接。Preferably, the column top condenser 5 is connected to the
优选的，在所述的回流管上设有回流液罐4，Preferably, a
优选的，所述的通过管道向第二酯化塔6补充水和/或甲醇和/或硝酸和/或亚硝酸一种或几种的组合液体。Preferably, the
工作原理：经过增压机8升压后的气体，分成1-N股进入第二酯化塔6。第一酯化塔3与第二酯化塔6采用管道连接，第一酯化塔3塔液进入第二酯化塔6。通过管道向 第二酯化塔6补充水和/或甲醇和/或硝酸和/或亚硝酸等反应物料。第二酯化塔6设置一个精馏段。回流液罐4，塔顶冷凝器5、第二酯化塔6及其上端的精馏部件共同构成一个精馏反应体系。经过第二酯化塔6分成1-N段反应的气体，汇合到一起后进入，第二酯化塔6底部。第二酯化塔6各反应室温度控制50-100℃，塔顶冷凝器5冷凝回流温度控制40-80℃。部分气体经过增压机8，第二酯化塔6及其上端的精馏部件、塔顶冷凝器5，通过管道连接构成酯化并联旁路反应后的循环气回到第一酯化塔3。可以通过第二酯化塔6内蒸汽盘管，塔顶冷凝器5，共同控制第二酯化塔6温度。通过酯化并联旁路反应后的循环气回主循环圈，经过循环压缩机2，DMC合成反应器1、酯脱塔7加压、反应、分离后得到DMC产品。Working principle: The gas boosted by the
一种DMC生产方法包括所述合成反应主循环反应，第一酯化塔3气体经过循环压缩机2，进入DMC合成反应器1、酯脱塔7加压、反应、分离后得到DMC产品；A DMC production method includes the main circulation reaction of the synthesis reaction, the gas of the
所述酯化并联旁路反应，酯脱塔7排出气体包括氮气、CO、甲醇、MN、NOX、CO2之一或几种几组，气体经增压机8加压后进入第二酯化塔6中、第一酯化塔3塔液（塔液包括甲醇、水、硝酸、亚硝酸任一之或几种组合）进入第二酯化塔6中，在第二酯化塔6内与硝酸和/或甲醇和/或水和/或亚硝酸液体混合物反应，生产酯类物资并产生热量，合成气态酯类物质、甲醇、水进入第二酯化塔6的精馏部件，经过精馏部件后，水被分离，甲醇及酯类物质与合成气一起进入第一酯化塔3。For the parallel bypass reaction of esterification, the exhaust gas of the
一种DMC生产方法，其特征在于：所述方法包括合成反应主循环反应、酯化并联旁路反应；A DMC production method, characterized in that: the method comprises a synthesis reaction main circulation reaction and an esterification parallel bypass reaction;
所述合成反应主循环反应，第一酯化塔3气体经过循环压缩机2，进入DMC合成反应器1、酯脱塔7加压、反应、分离后得到DMC产品；In the main circulation reaction of the synthesis reaction, the gas of the
所述酯化并联旁路反应，酯脱塔7排出气体包括氮气、CO、甲醇、MN、NOX、CO2之一或几种几组，气体经增压机8加压后进入第二酯化塔6中、第一酯化塔3塔液进入第二酯化塔6中，在第二酯化塔6内与硝酸和/或甲醇和/或水和/或亚硝酸液体混合物反应，生产酯类物资并产生热量，气态酯类物质、甲醇、水进入第二酯化塔6反应后一起进入第一酯化塔3。For the parallel bypass reaction of esterification, the exhaust gas of the
较其他酯化工艺，能保证DMC合成过程，更安全、稳定，原材料利用效率更高。Compared with other esterification processes, it can ensure the DMC synthesis process, which is safer, more stable, and has higher utilization efficiency of raw materials.
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114507136A (en) * | 2022-04-13 | 2022-05-17 | 太原理工大学 | Efficient synthesis method of lithium ion battery electrolyte mixed solvent |
| CN116265056A (en) * | 2021-12-16 | 2023-06-20 | 中国石油化工股份有限公司 | A product separation and refining device and method for CO esterification to dimethyl carbonate |
Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1227839A (en) * | 1999-02-01 | 1999-09-08 | 天津大学 | Process for low-pressure synthesis of dimethyl carbonate by carbon monoxide |
| JP2006022067A (en) * | 2004-07-09 | 2006-01-26 | Mitsubishi Heavy Ind Ltd | System for producing dimethyl carbonate, method for producing dimethyl carbonate, and compound |
| CN103408428A (en) * | 2013-08-14 | 2013-11-27 | 上海戊正工程技术有限公司 | Process for producing dimethyl carbonate from industrial synthetic gas |
| CN203411491U (en) * | 2013-08-14 | 2014-01-29 | 上海戊正工程技术有限公司 | Process system for producing dimethyl carbonate from industrial synthesis gas |
| US20170267615A1 (en) * | 2014-06-05 | 2017-09-21 | Shanghai Wuzheng Engineering Technology Co., Ltd | Method and device system for producing dimethyl oxalate through midhigh and high-pressure carbonylation of industrial synthesis gas and producing ethylene glycol through dimethyl oxalate hydrogenation |
| CN110776424A (en) * | 2019-10-09 | 2020-02-11 | 中盐安徽红四方股份有限公司 | Refining apparatus and process using DMC |
| CN212560052U (en) * | 2020-08-21 | 2021-02-19 | 湖北三宁化工股份有限公司 | DMC production system |
-
2020
- 2020-08-21 CN CN202010852070.5A patent/CN111909036A/en active Pending
Patent Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1227839A (en) * | 1999-02-01 | 1999-09-08 | 天津大学 | Process for low-pressure synthesis of dimethyl carbonate by carbon monoxide |
| JP2006022067A (en) * | 2004-07-09 | 2006-01-26 | Mitsubishi Heavy Ind Ltd | System for producing dimethyl carbonate, method for producing dimethyl carbonate, and compound |
| CN103408428A (en) * | 2013-08-14 | 2013-11-27 | 上海戊正工程技术有限公司 | Process for producing dimethyl carbonate from industrial synthetic gas |
| CN203411491U (en) * | 2013-08-14 | 2014-01-29 | 上海戊正工程技术有限公司 | Process system for producing dimethyl carbonate from industrial synthesis gas |
| US20170267615A1 (en) * | 2014-06-05 | 2017-09-21 | Shanghai Wuzheng Engineering Technology Co., Ltd | Method and device system for producing dimethyl oxalate through midhigh and high-pressure carbonylation of industrial synthesis gas and producing ethylene glycol through dimethyl oxalate hydrogenation |
| CN110776424A (en) * | 2019-10-09 | 2020-02-11 | 中盐安徽红四方股份有限公司 | Refining apparatus and process using DMC |
| CN212560052U (en) * | 2020-08-21 | 2021-02-19 | 湖北三宁化工股份有限公司 | DMC production system |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN116265056A (en) * | 2021-12-16 | 2023-06-20 | 中国石油化工股份有限公司 | A product separation and refining device and method for CO esterification to dimethyl carbonate |
| CN114507136A (en) * | 2022-04-13 | 2022-05-17 | 太原理工大学 | Efficient synthesis method of lithium ion battery electrolyte mixed solvent |
| CN114507136B (en) * | 2022-04-13 | 2022-06-21 | 太原理工大学 | A kind of efficient synthesis method of lithium ion battery electrolyte mixed solvent |
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