WO2021253370A1 - 一种制取甲醇的系统及方法 - Google Patents

一种制取甲醇的系统及方法 Download PDF

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WO2021253370A1
WO2021253370A1 PCT/CN2020/096980 CN2020096980W WO2021253370A1 WO 2021253370 A1 WO2021253370 A1 WO 2021253370A1 CN 2020096980 W CN2020096980 W CN 2020096980W WO 2021253370 A1 WO2021253370 A1 WO 2021253370A1
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methanol
gas
output end
tower
synthesis
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PCT/CN2020/096980
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French (fr)
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周连惠
贡茅
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周连惠
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Priority to PCT/CN2020/096980 priority Critical patent/WO2021253370A1/zh
Priority to AU2020101401A priority patent/AU2020101401A4/en
Priority to ZA2021/09796A priority patent/ZA202109796B/en
Publication of WO2021253370A1 publication Critical patent/WO2021253370A1/zh

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    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
    • C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
    • C01B3/04—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by decomposition of inorganic compounds, e.g. ammonia
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B32/00—Carbon; Compounds thereof
    • C01B32/50—Carbon dioxide
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
    • C07C29/15—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of oxides of carbon exclusively
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
    • C07C29/15—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of oxides of carbon exclusively
    • C07C29/151—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of oxides of carbon exclusively with hydrogen or hydrogen-containing gases
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
    • C07C29/15—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of oxides of carbon exclusively
    • C07C29/151—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of oxides of carbon exclusively with hydrogen or hydrogen-containing gases
    • C07C29/152—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of oxides of carbon exclusively with hydrogen or hydrogen-containing gases characterised by the reactor used
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C31/00—Saturated compounds having hydroxy or O-metal groups bound to acyclic carbon atoms
    • C07C31/02—Monohydroxylic acyclic alcohols
    • C07C31/04—Methanol
    • C—CHEMISTRY; METALLURGY
    • C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
    • C12P—FERMENTATION OR ENZYME-USING PROCESSES TO SYNTHESISE A DESIRED CHEMICAL COMPOUND OR COMPOSITION OR TO SEPARATE OPTICAL ISOMERS FROM A RACEMIC MIXTURE
    • C12P1/00—Preparation of compounds or compositions, not provided for in groups C12P3/00 - C12P39/00, by using microorganisms or enzymes
    • C—CHEMISTRY; METALLURGY
    • C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
    • C25B—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES FOR THE PRODUCTION OF COMPOUNDS OR NON-METALS; APPARATUS THEREFOR
    • C25B1/00—Electrolytic production of inorganic compounds or non-metals
    • C25B1/01—Products
    • C25B1/02—Hydrogen or oxygen
    • C25B1/04—Hydrogen or oxygen by electrolysis of water
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E50/00—Technologies for the production of fuel of non-fossil origin
    • Y02E50/30—Fuel from waste, e.g. synthetic alcohol or diesel
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E60/00—Enabling technologies; Technologies with a potential or indirect contribution to GHG emissions mitigation
    • Y02E60/30—Hydrogen technology
    • Y02E60/36—Hydrogen production from non-carbon containing sources, e.g. by water electrolysis

Definitions

  • the invention relates to the technical field of chemical engineering, in particular to a system and method for preparing methanol.
  • Methanol is an important organic chemical raw material and high-quality fuel, and is widely used in fine chemicals, plastics, medicine, forest products processing and other fields. Methanol is mainly used to produce formaldehyde, and its consumption accounts for half of the total output of methanol. Formaldehyde is an indispensable raw material for the production of various synthetic resins.
  • methanol as methylation reagent can produce methyl acrylate, dimethyl terephthalate, methylamine, methyl aniline, methane chloride, etc.; methanol carbonylation can produce important organic synthesis such as acetic acid, acetic anhydride, methyl formate, etc.
  • Methanol is also an important organic solvent, its solubility is better than ethanol, and can be used to prepare paint.
  • methanol can be used for the separation of some substances in analytical chemistry. Methanol is still a promising clean energy.
  • Methanol fuel has many advantages such as safety, low cost, full combustion, high utilization rate, and environmental protection.
  • the substitution of gasoline has become one of the development directions of vehicle fuels; in addition, fuel-grade methanol is used for Heating and power generation can also meet environmental protection requirements.
  • Methanol can also be bio-fermented to produce methanol protein, which is rich in vitamins and protein and has the advantages of high nutritional value and low cost. It is used as a feed additive and has broad application prospects.
  • the existing methanol production system does not consider the use of organic waste to produce the CO 2 and CO required for the production of methanol in the raw material for methanol production.
  • the various equipment in the system are not reasonably integrated to reduce the process and cost.
  • the by-products produced during the preparation process are not well recycled, which wastes valuable resources.
  • the purpose of the present invention is to provide a system and method for preparing methanol to solve the deficiencies of the prior art.
  • a system for preparing methanol including a water electrolysis reactor for preparing hydrogen, a fermentation tank for preparing CO 2 and CO, a methanol synthesis gas compressor, a tower gas preheater, and methanol
  • a synthesis tower a methanol condenser, a methanol separator, a methanol expansion tank, a booster pump
  • the oxygen output end of the water electrolysis reactor is connected to the fermentation tank
  • the hydrogen output end of the water electrolysis reactor is connected to a methanol synthesis gas compressor
  • the output end of the fermentation tank is connected to a methanol synthesis gas compressor
  • the output end of the methanol synthesis gas compressor is connected to the first input end of the tower gas preheater
  • the first output end of the tower gas preheater is connected to the methanol synthesis tower
  • An input end, the output end of the methanol synthesis tower is connected to the second input end of the tower gas preheater, the second output end of the tower gas
  • the methanol synthesis tower is a tubular isothermal reactor, in which the XNC-98 methanol synthesis catalyst is installed in the tube, and boiling boiler water is outside the tube.
  • the methanol condenser is A methanol condenser and B methanol condenser in parallel.
  • the methanol separator is further provided with a purge gas output port, and the purge gas output port is connected to a gas-fired power generation device.
  • the methanol expansion tank is further provided with an expansion gas outlet, and the expansion gas outlet is connected to a fuel gas device.
  • a method for preparing methanol includes the following steps:
  • the water in the water electrolysis reactor is electrolyzed to produce hydrogen and oxygen, and the oxygen produced is input to the fermentation tank containing organic waste to produce CO 2 and CO.
  • the hydrogen, CO 2 and CO are compressed to 5.14 MPa by the methanol synthesis gas compressor.
  • methanol synthesis gas After entering the tower gas preheater heated to 225 °C, into the methanol synthesis tower, methanol synthesis gas under the action of the catalyst, the following reaction occurs:
  • the synthesis gas (255°C, 4.9MPa) from the methanol synthesis tower is processed by the tower gas preheater and the methanol condenser in turn, and then enters the methanol separator.
  • the crude methanol is separated in the methanol separator, and the separated crude methanol enters the methanol expansion After the tank is decompressed to 0.4MPa, it is sent to the rectification device for processing to obtain refined methanol.
  • the methanol separator also emits circulating gas, a part of the purge gas is discharged before the booster pump is pressurized, and the purge gas is decompressed to the fuel gas power generation system, and the expansion gas discharged from the top of the methanol expansion tank is defueled gas system.
  • the methanol separator also separates the mixed gas and fresh gas, which are mixed in proportion and sent to the methanol synthesis tower to continue the synthesis reaction after being boosted by a booster pump.
  • the present invention uses organic waste to produce CO 2 and CO needed by it, and makes full use of resources;
  • the hydrogen produced by the reactor is one of the chemical reactants for the preparation of methanol, while the combined reaction of oxygen and the organic waste fermentation tank produces CO 2 and CO.
  • One equipment simultaneously produces two necessary The reactant does not need to set up other equipment and procedures, reducing procedures and costs.
  • the mixed gas separated by the methanol separator is mixed with fresh gas in a certain proportion and then sent to the methanol synthesis tower to continue the synthesis reaction after being boosted by a booster pump.
  • the circulating gas from the methanol separator discharges a part of the purge gas before pressurization, and the purge gas is decompressed to the fuel gas power generation system; the expansion gas discharged from the top of the methanol expansion tank is used for the fuel gas system. It can be seen that the by-products produced during the preparation process are well recycled.
  • Fig. 1 is a schematic structural diagram of a system for preparing methanol according to an embodiment of the invention.
  • a system for preparing methanol includes a water electrolysis reactor for preparing hydrogen 1, a fermentation tank for preparing CO2 and CO, a methanol synthesis gas compressor 3, and a tower gas preheater 4 , Methanol synthesis tower 5, methanol condenser 6, methanol separator 7, methanol expansion tank 8, booster pump 9, the oxygen output end of the water electrolysis reactor 1 is connected to the fermentation tank 2, and the hydrogen output end of the water electrolysis reactor 1 is connected Methanol synthesis gas compressor 3, the output end of the fermentation tank 2 is connected to the methanol synthesis gas compressor 3, the output end of the methanol synthesis gas compressor 3 is connected to the first input end of the tower gas preheater 4, and the first output of the tower gas preheater 4 The end is connected to the first input end of the methanol synthesis tower 5, the output end of the methanol synthesis tower 5 is connected to the second input end of the tower gas preheater 4, the second output end of the tower gas preheater 4 is connected to the m
  • the methanol synthesis tower 5 is a tubular isothermal reactor, in which the XNC-98 methanol synthesis catalyst is installed in the tube, and the boiling boiler water is outside the tube.
  • the methanol condenser 6 is a methanol condenser A and a methanol condenser B connected in parallel.
  • the methanol separator 7 is also provided with a purge gas output port, and the purge gas output port is connected to a gas-fired power generation device.
  • the methanol expansion tank 8 is also provided with an expansion gas outlet, and the expansion gas outlet is connected to a fuel gas device.
  • the present invention also provides a method for preparing methanol, including the following steps:
  • the water in the water electrolysis reactor 1 is electrolyzed to produce hydrogen and oxygen, and the oxygen produced is input to the fermentation tank 2 containing organic waste to produce CO 2 and CO.
  • the hydrogen, CO 2 and CO are compressed together by the methanol synthesis gas compressor 3 After reaching 5.14MPa, it is heated to 225°C through the inlet gas preheater 4 and enters the methanol synthesis tower 5.
  • the methanol synthesis gas undergoes the following reactions under the action of the catalyst:
  • the synthesis gas (255°C, 4.9MPa) from the methanol synthesis tower 5 is processed by the tower gas preheater 4 and the methanol condenser 6 in turn, and then enters the methanol separator 7.
  • the crude methanol is separated in the methanol separator 7, and the separated
  • the crude methanol enters the methanol expansion tank 8 and is decompressed to 0.4 MPa and then sent to the rectification device for processing to obtain refined methanol.
  • the methanol separator 7 also circulates gas, and discharges a part of the purge gas before the booster pump 9 is pressurized. After the purge gas is decompressed, it goes to the fuel gas power generation system.
  • the methanol separator 7 also separates the mixed gas and the fresh gas, which are mixed in proportion and sent to the methanol synthesis tower 5 to continue the synthesis reaction after being boosted by the booster pump 9.
  • the working principle of the present invention is:
  • the water in the water electrolysis reactor 1 is electrolyzed to generate hydrogen and oxygen, and the generated oxygen is input to the organic waste fermentation tank 2 to produce CO 2 and CO.
  • the hydrogen, CO 2 and CO are compressed to 5.14 by the methanol synthesis gas compressor 3 After MPa, it is heated to 225°C through the inlet gas preheater 4 and enters the methanol synthesis tower 5.
  • the methanol synthesis gas undergoes the following reactions under the action of the catalyst:
  • the methanol synthesis tower 5 is a tubular isothermal reactor, in which the XNC-98 methanol synthesis catalyst is installed in the tube, and the boiling boiler water is outside the tube.
  • the reaction releases a large amount of heat Q, which is transmitted to the boiler water through the tube wall, and produces a large amount of medium-pressure steam (3.9MPa) saturated steam, which is sent to the steam pipe network after decompression.
  • the by-product steam ensures that the reaction in the methanol synthesis tower 5 tends to be constant, and the reaction temperature can also be adjusted by the pressure of the by-product steam.
  • the synthesis gas (255° C., 4.9 MPa) from the methanol synthesis tower 5 is processed by the tower gas preheater 4 and the methanol condenser 6 in sequence, and then enters the methanol separator 7 where the crude methanol is separated.
  • the separated crude methanol enters the methanol expansion tank 8 and is decompressed to 0.4 MPa before being sent to the rectification device.
  • the mixed gas separated by the methanol separator 7 is mixed with fresh gas in a certain ratio and then is boosted by the booster 9 and sent to the methanol synthesis tower 5 to continue the synthesis reaction.
  • the recycle gas from the methanol separator 7 discharges a part of the purge gas before pressurization, so as to keep the inert gas constant in the entire recycle loop.
  • the purge gas is decompressed to the gas power generation system; the expansion gas discharged from the top of the methanol expansion tank 8 goes to the fuel gas system.

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Abstract

一种制取甲醇的系统及方法。水电解反应釜（1）的氧气输出端连接发酵池（2），水电解反应釜（1）的氢气输出端连接甲醇合成气压缩机（3），发酵池（2）输出端连接甲醇合成气压缩机（3），甲醇合成气压缩机（3）输出端连接塔气预热器（4）的第一输入端，塔气预热器（4）第一输出端连接甲醇合成塔（5）第一输入端，甲醇合成塔（5）输出端连接塔气预热器（4）的第二输入端，塔气预热器（4）第二输出端连接甲醇冷凝器（6），甲醇冷凝器（6）输出端连接甲醇分离器（7），甲醇分离器（7）输出端连接甲醇膨胀槽（8），甲醇膨胀槽（8）输出端连接增压泵（9），增压泵（9）输出端连接甲醇合成塔（5）第二输入端。利用水电解反应釜产生的氢气为制备甲醇反应物之一，而水电解反应釜产生的氧气与有机垃圾发酵池结合反应产生制备甲醇需要的CO 2和CO，系统中各个设备合理整合，减少工序和成本，制备过程中产生的副产品很好被循环利用。

Description

一种制取甲醇的系统及方法 技术领域：
本发明涉及化工技术领域，尤其涉及一种制取甲醇的系统及方法。
背景技术：
甲醇是重要有机化工原料和优质燃料，广泛应用于精细化工，塑料，医药，林产品加工等领域。甲醇主要用于生产甲醛，消耗量要占到甲醇总产量的一半，甲醛则是生产各种合成树脂不可少的原料。用甲醇作甲基化试剂可生产丙烯酸甲酯、对苯二甲酸二甲酯、甲胺、甲基苯胺、甲烷氯化物等；甲醇羰基化可生产醋酸、醋酐、甲酸甲酯等重要有机合成中间体，它们是制造各种染料、药品、农药、炸药、香料、喷漆的原料，目前用甲醇合成乙二醇、乙醛、乙醇也日益受到重视。甲醇也是一种重要的有机溶剂，其溶解性能优于乙醇，可用于调制油漆。作为一种良好的萃取剂，甲醇在分析化学中可用于一些物质的分离。甲醇还是一种很有前景的清洁能源，甲醇燃料以其安全、廉价、燃烧充分，利用率高、环保的众多优点，替代汽油已经成为车用燃料的发展方向之一；另外燃料级甲醇用于供热和发电，也可达到环保要求。甲醇还可经生物发酵生成甲醇蛋白，富含维生素和蛋白质，具有营养价值高而成本低的优点，用作饲料添加剂，有着广阔的应用前景。
现有制备甲醇的方法主要为合成法，合成的化学反应式为：CO+2H 2＝CHOH+Q或者CO 2+3H 2＝CH 3OH+H 2O+Q。现有的制备甲醇的系统在甲醇制备原料上没有考虑利用有机垃圾产生制备其需要的CO 2和CO，同时系统中各个设备没有合理整合，以减少工序和成本。同时，制备过程中产生的副产品没有很好被循环利用，浪费了宝贵的资源。
发明内容：
本发明的目的在于提供一种制取甲醇的系统及方法，以解决现有技术的不足。
发明由如下技术方案实施：一种制取甲醇的系统，包括用于制备氢气的水电解反应釜、用于制备CO 2和CO的发酵池、甲醇合成气压缩机、塔气预热器、甲醇合成塔、甲醇冷凝器、甲醇分离器、甲醇膨胀槽、增压泵，所述水电解反应釜的氧气输出端连接发酵池，所述水电解反应釜的氢气输出端连接甲醇合成气压缩机，所述发酵池输出端连接甲醇合成气压缩机，所述甲醇合成气压缩机输出端连接塔气预热器的第一输入端，所述塔气预热器第一输出端连接甲醇合成塔第一输入端，所述甲醇合成塔输出端连接塔气预热器的第二输入端，所述塔气预热器第二输出端连接甲醇冷凝器，所述甲醇冷凝器输出端连接甲醇分离器，所述甲醇分离器输出端连接甲醇膨胀槽，所述甲醇膨胀槽输出端连接增压泵，所述增压泵输出端连接甲醇合成塔第二输入端。
优选的，所述甲醇合成塔为列管式等温反应器，管内装有XNC-98型甲醇合成催化剂，管外为沸腾锅炉水。
优选的，所述甲醇冷凝器为并联的A甲醇冷凝器和B甲醇冷凝器。
优选的，所述甲醇分离器还设置驰放气输出口，且所述驰放气输出口连接燃气发电装置。
优选的，所述甲醇膨胀槽还设置膨胀气出口，所述膨胀气出口连接燃料气装置。
一种制取甲醇的方法，包括以下步骤：
水电解反应釜里的水经过电解产生氢气和氧气，将产生的氧气输入到装有机垃圾的发酵池产生CO 2、CO，氢气和CO 2、CO一起经甲醇合成气压缩机压缩至5.14MPa后，经过入塔气预热器加热到225℃，进入甲醇合成塔内，甲醇合成气在催化剂作用下发生如下反应:
CO+2H 2＝CHOH+Q
CO 2+3H 2＝CH 3OH+H 2O+Q
甲醇合成塔出来的合成气(255℃，4.9MPa)，依次经过塔气预热器、甲醇冷凝器处理，进入甲醇分离器，粗甲醇在甲醇分离器被分离，分离出的粗甲醇进入甲醇膨胀槽被减压至0.4MPa后送至精馏装置处理得到精甲醇。
优选的，所述甲醇分离器还出来循环气，在增压泵加压前排放一部分弛放气，弛放气减压后去燃气发电系统，甲醇膨胀槽顶部排出的膨胀气去燃料气系统。
优选的，所述甲醇分离器还分离出混合气与新鲜气，按比例混合后经过增压泵升压送至甲醇合成塔继续进行合成反应。
本发明的优点：
1.本发明利用有机垃圾产生制备其需要的CO 2和CO，充分利用资源；
2.本发明系统中各个设备合理整合，比如反应釜产生的氢气为制备甲醇化学反应物之一，而氧气与有机垃圾发酵池结合反应产生CO 2和CO，一个设备同时产生了两种必备反应物，不需要再设置其他设备和工序，减少工序和成本。
实验数据表明，氧气是影响有机垃圾/堆肥，氧气供给充足时，大部分的C转化成Co2而氧气不充足时，只有少部分的C转化成CO 2，供给充足氧气的供应，可以加速有机质分解，缩短堆肥时间，加速堆肥初期温度的上升，减少恶臭气体的产生
3.甲醇分离器分离出的混合气与新鲜气按一定比例混合后经过增压泵升压送至甲醇合成塔继续进行合成反应。从甲醇分离器出来的循环气在加压前排放一部分弛放气，弛放气减压后去燃气发电系统；甲醇膨胀槽顶部排出的膨胀气去燃料气系统。可见，制备过程中产生的副产品很好被循环利用。
4利用清洁能源风能和太阳能产生的电力电解水，得到了绿氢和氧气，部分氧气提供给城市农村有机垃圾，加速其堆肥和为生产甲醇的CO 2的产能速度；废弃资源得到合理化最大化利用，符合当代生态循环经济的原则
附图说明：
为了更清楚地说明发明实施例或现有技术中的技术方案，下面将对实施例或现有技术描述中所需要使用的附图作简单地介绍，显而易见地，下面描述中的附图仅仅是发明的一些实施例，对于本领域普通技术人员来讲，在不付出创造性劳动的前提下，还可以根据这些附图获得其它附图。
图1为发明实施例的一种制取甲醇的系统的结构示意图。
具体实施方式：
下面将结合发明实施例中的附图，对发明实施例中的技术方案进行清楚、完整地描述，显然，所描述的实施例仅仅是发明一部分实施例，而不是全部的实施例。基于发明中的实施例，本领域普通技术人员在没有做出创造性劳动前提下所获得的所有其他实施例，都属于发明保护的范围。
如图1所示，一种制取甲醇的系统，包括用于制备氢气的水电解反应釜1、用于制备CO2和CO的发酵池2、甲醇合成气压缩机3、塔气预热器4、甲醇合成塔5、甲醇冷凝器6、甲醇分离器7、甲醇膨胀槽8、增压泵9，水电解反应釜1的氧气输出端连接发酵池2，水电解反应釜1的氢气输出端连接甲醇合成气压缩机3，发酵池2输出端连接甲醇合成气压缩机3，甲醇合成气压缩机3输出端连接塔气预热器4的第一输入端，塔气预热器4第一输出端连接甲醇合成塔5第一输入端，甲醇合成塔5输出端连接塔气预热器4的第二输入端，塔气预热器4第二输出端连接甲醇冷凝器6，甲醇冷凝器6输出端连接甲醇分离器7，甲醇分离器7输出端连接甲醇膨胀槽8，甲醇膨胀槽8输出端连接增压泵9，增压泵9输出端连接甲醇合成塔5第二输入端。
其中，甲醇合成塔5为列管式等温反应器，管内装有XNC-98型甲醇合成催化剂，管外为沸腾锅炉水。甲醇冷凝器6为并联的A甲醇冷凝器和B甲醇冷凝器。甲醇分离器7还设置驰放气输出口，且驰放气输出口连接燃气发电装置。甲醇膨胀槽8还设置膨胀气出口，膨胀气出口连接燃料气装置。
本发明还提供一种制取甲醇的方法，包括以下步骤：
水电解反应釜1里的水经过电解产生氢气和氧气，将产生的氧气输入到装有有机垃圾的发酵池2产生CO 2、CO，氢气和CO 2、CO一起经甲醇合成气压缩机3压缩至5.14MPa后，经过入塔气预热器4加热到225℃，进入甲醇合成塔5内，甲醇合成气在催化剂作用下发生如下反应:
CO+2H 2＝CHOH+Q
CO 2+3H 2＝CH 3OH+H2O+Q
甲醇合成塔5出来的合成气(255℃，4.9MPa)，依次经过塔气预热器4、甲醇冷凝器6处理，进入甲醇分离器7，粗甲醇在甲醇分离器7被分离，分离出的粗甲醇进入甲醇膨胀槽8被减压至0.4MPa后送至精馏装置处理得到精甲醇。
另外，甲醇分离器7还出来循环气，在增压泵9加压前排放一部分弛放气，弛放气减压后去燃气发电系统，甲醇膨胀槽8顶部排出的膨胀气去燃料气系统。甲醇分离器7还分离出混合气与新鲜气，按比例混合后经过增压泵9升压送至甲醇合成塔5继续进行合成反应。
本发明工作原理是：
水电解反应釜1里的水经过电解产生氢气和氧气，将产生的氧气输入到有机垃圾的发酵池2产生CO 2、CO，氢气和CO 2、CO一起经甲醇合成气压缩机3压缩至5.14MPa后，经过入塔气预热器4加热到225℃，进入甲醇合成塔5内，甲醇合成气在催化剂作用下发生如下反应:
CO+2H 2＝CHOH+Q
CO 2+3H 2＝CH 3OH+H 2O+Q
甲醇合成塔5为列管式等温反应器，管内装有XNC-98型甲醇合成催化剂，管外为沸腾锅炉水。反应放出大量的热Q，通过列管管壁传给锅炉水，产生大量中压蒸汽(3.9MPa)饱和蒸汽，减压后送至蒸汽管网。副产蒸汽确保了甲醇合成塔5内反应趋于恒定，且反应温度也可通过副产蒸汽的压力来调节。
甲醇合成塔5出来的合成气(255℃，4.9MPa)，依次经过塔气预热器4、甲醇冷凝器6处理，进入甲醇分离器7，粗甲醇在甲醇分离器7被分离。分离出的粗甲醇进入甲醇膨胀槽8被减压至0.4MPa后送至精馏装置。甲醇分离器7分离出的混合气与新鲜气按一定比例混合后经过增压泵9升压送至甲醇合成塔5继续进行合成反应。
从甲醇分离器7出来的循环气在加压前排放一部分弛放气，以保持整个循环回路惰性气体恒定。弛放气减压后去燃气发电系统；甲醇膨胀槽8顶部排出的膨胀气去燃料气系统。
以上所述仅为发明的较佳实施例而已，并不用以限制发明，凡在发明的精神和原则之内，所作的任何修改、等同替换、改进等，均应包含在发明的保护范围之内。

Claims (8)

  1. 一种制取甲醇的系统，其特征在于，包括用于制备氢气的水电解反应釜(1)、用于制备CO2和CO的发酵池(2)、甲醇合成气压缩机(3)、塔气预热器(4)、甲醇合成塔(5)、甲醇冷凝器(6)、甲醇分离器(7)、甲醇膨胀槽(8)、增压泵(9)，所述水电解反应釜(1)的氧气输出端连接发酵池(2)，所述水电解反应釜(1)的氢气输出端连接甲醇合成气压缩机(3)，所述发酵池(2)输出端连接甲醇合成气压缩机(3)，所述甲醇合成气压缩机(3)输出端连接塔气预热器(4)的第一输入端，所述塔气预热器(4)第一输出端连接甲醇合成塔(5)第一输入端，所述甲醇合成塔(5)输出端连接塔气预热器(4)的第二输入端，所述塔气预热器(4)第二输出端连接甲醇冷凝器(6)，所述甲醇冷凝器(6)输出端连接甲醇分离器(7)，所述甲醇分离器(7)输出端连接甲醇膨胀槽(8)，所述甲醇膨胀槽(8)输出端连接增压泵(9)，所述增压泵(9)输出端连接甲醇合成塔(5)第二输入端。
  2. 根据权利要求1所述的一种制取甲醇的系统，其特征在于，所述甲醇合成塔(5)为列管式等温反应器，管内装有XNC-98型甲醇合成催化剂，管外为沸腾锅炉水。
  3. 根据权利要求1所述的一种制取甲醇的系统，其特征在于，所述甲醇冷凝器(6)为并联的A甲醇冷凝器和B甲醇冷凝器。
  4. 根据权利要求1所述的一种制取甲醇的系统，其特征在于，所述甲醇分离器(7)还设置驰放气输出口，且所述驰放气输出口连接燃气发电装置。
  5. 根据权利要求1所述的一种制取甲醇的系统，其特征在于，所述甲醇膨胀槽(8)还设置膨胀气出口，所述膨胀气出口连接燃料气装置。
  6. 一种制取甲醇的方法，其特征在于，包括以下步骤：
    水电解反应釜(1)里的水经过电解产生氢气和氧气，将产生的氧气输入到装有有机垃圾的发酵池(2)产生CO 2、CO，氢气和CO 2、CO一起经甲醇合成气压缩机(3)压缩至5.14MPa后，经过入塔气预热器(4)加热到225℃，进入甲醇合成塔(5)内，甲醇合成气在催化剂作用下发生如下反应:
    CO+2H 2＝CHOH+Q
    CO2+3H 2＝CH 3OH+H2O+Q
    甲醇合成塔(5)出来的合成气(255℃，4.9MPa)，依次经过塔气预热器(4)、甲醇冷凝器(6)处理，进入甲醇分离器(7)，粗甲醇在甲醇分离器(7)被分离，分离出的粗甲醇进入甲醇膨胀槽(8)被减压至0.4MPa后送至精馏装置处理得到精甲醇。
  7. 根据权利要求6所述的一种制取甲醇的方法，其特征在于，所述甲醇分离器(7)还出来循环气，在增压泵(9)加压前排放一部分弛放气，弛放气减压后去燃气发电系统，甲醇膨胀槽(8)顶部排出的膨胀气去燃料气系统。
  8. 根据权利要求6所述的一种制取甲醇的方法，其特征在于，所述甲醇分离器(7)还分离出混合气与新鲜气，按比例混合后经过增压泵(9)升压送至甲醇合成塔(5)继续进行合成反应。
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