CN112010734A - A device and method for producing methanol from synthesis gas coupled with Karina cycle - Google Patents
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- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 title claims abstract description 102
- 230000015572 biosynthetic process Effects 0.000 title claims abstract description 30
- 238000003786 synthesis reaction Methods 0.000 title claims abstract description 30
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 12
- 238000006243 chemical reaction Methods 0.000 claims abstract description 9
- 239000007788 liquid Substances 0.000 claims description 8
- 238000001816 cooling Methods 0.000 claims description 7
- 238000000926 separation method Methods 0.000 claims description 6
- 238000010992 reflux Methods 0.000 claims description 2
- 239000011555 saturated liquid Substances 0.000 claims description 2
- 230000006835 compression Effects 0.000 claims 1
- 238000007906 compression Methods 0.000 claims 1
- 238000009833 condensation Methods 0.000 claims 1
- 230000005494 condensation Effects 0.000 claims 1
- 238000002156 mixing Methods 0.000 claims 1
- 239000007789 gas Substances 0.000 abstract description 27
- 239000002918 waste heat Substances 0.000 abstract description 13
- 238000011084 recovery Methods 0.000 abstract description 8
- 230000008878 coupling Effects 0.000 abstract description 5
- 238000010168 coupling process Methods 0.000 abstract description 5
- 238000005859 coupling reaction Methods 0.000 abstract description 5
- 239000000126 substance Substances 0.000 abstract description 4
- 238000000034 method Methods 0.000 description 21
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 14
- 229910002092 carbon dioxide Inorganic materials 0.000 description 7
- 238000013461 design Methods 0.000 description 5
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 4
- 238000001704 evaporation Methods 0.000 description 4
- 230000008020 evaporation Effects 0.000 description 4
- 238000005457 optimization Methods 0.000 description 4
- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 description 2
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 2
- 235000011114 ammonium hydroxide Nutrition 0.000 description 2
- 239000001569 carbon dioxide Substances 0.000 description 2
- 229910002091 carbon monoxide Inorganic materials 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 239000012530 fluid Substances 0.000 description 2
- 239000001257 hydrogen Substances 0.000 description 2
- 229910052739 hydrogen Inorganic materials 0.000 description 2
- 125000004435 hydrogen atom Chemical class [H]* 0.000 description 2
- 230000010354 integration Effects 0.000 description 2
- 229910052757 nitrogen Inorganic materials 0.000 description 2
- 239000002994 raw material Substances 0.000 description 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 2
- 238000013459 approach Methods 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000012824 chemical production Methods 0.000 description 1
- 230000000052 comparative effect Effects 0.000 description 1
- 150000001875 compounds Chemical class 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 239000002803 fossil fuel Substances 0.000 description 1
- 239000003960 organic solvent Substances 0.000 description 1
- 238000012546 transfer Methods 0.000 description 1
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- 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
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25B—REFRIGERATION MACHINES, PLANTS OR SYSTEMS; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS
- F25B30/00—Heat pumps
- F25B30/02—Heat pumps of the compression type
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- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
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- 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
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
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Abstract
本发明属于化工行业的余热回收领域，涉及一种耦合卡琳娜循环的合成气制甲醇的装置和方法。本发明在不降低合成气制甲醇的总转化率的前提下，采用卡琳娜循环回收合成气制甲醇中的余热，最大程度提高合成气制甲醇耦合卡琳娜循环系统的余热回收量和能量利用效率。
The invention belongs to the field of waste heat recovery in the chemical industry, and relates to a device and method for producing methanol from synthesis gas coupled with Karina cycle. Under the premise of not reducing the total conversion rate of the synthesis gas to methanol, the invention adopts the Karina cycle to recover the waste heat in the synthesis gas to methanol, and maximizes the waste heat recovery amount and energy of the synthesis gas to methanol coupling Karina cycle system. usage efficiency.
Description
技术领域technical field
本发明属于化工行业的余热回收领域，涉及一种耦合卡琳娜循环的合成气制甲醇的装置和方法。The invention belongs to the field of waste heat recovery in the chemical industry, and relates to a device and method for producing methanol from synthesis gas coupled with Karina cycle.
背景技术Background technique
甲醇是主要的有机化工原料之一，可用作优良的有机溶剂和生产各种有机化工产品的必要原料。此外，甲醇是世界上交易量最大(前五位)的工业化合物之一，也是化石燃料的替代品。随着科学技术的发展，甲醇的应用越来越广泛，甲醇的市场需求前景广阔。合成气制甲醇工艺是一种能源密集型化工生产过程，有效利用余热可以提高能源利用率和经济效益。Methanol is one of the main organic chemical raw materials, which can be used as an excellent organic solvent and a necessary raw material for the production of various organic chemical products. In addition, methanol is one of the most traded (top five) industrial compounds in the world and an alternative to fossil fuels. With the development of science and technology, the application of methanol is more and more extensive, and the market demand of methanol has a bright prospect. The synthesis gas-to-methanol process is an energy-intensive chemical production process, and the effective use of waste heat can improve energy utilization and economic benefits.
文献(A novel pinch-based method for process integration andoptimization of Kalina cycle.Energ Convers Manage 2020,112630.)报道了过程和卡琳娜循环优化的拓展热集成模型，可用于优化流股的温度和流量。The literature (A novel pinch-based method for process integration and optimization of Kalina cycle. Energ Convers Manage 2020, 112630.) reports an extended thermal integration model for process and Kalina cycle optimization, which can be used to optimize the temperature and flow of the stream.
文献(A structural optimization approach in process synthesis—II:Heatrecovery networks.Comput Chem Eng 1983；7(6):707-21.)报道了拓展的转运模型，该模型可用于综合换热网络结构。The literature (A structural optimization approach in process synthesis—II: Heatrecovery networks. Comput Chem Eng 1983; 7(6):707-21.) reports an extended transport model that can be used to synthesize heat transfer network structures.
目前合成气制甲醇的余热回收技术有两种：(1)在流程参数确定情况下，热力循环由流程中的单一流股驱动；(2)在流程参数确定情况下，流程和热力循环进行热集成，分步实现循环结构优化和换热网络设计。At present, there are two waste heat recovery technologies for methanol production from syngas: (1) when the process parameters are determined, the thermodynamic cycle is driven by a single stream in the process; (2) when the process parameters are determined, the process and the thermodynamic cycle are heated Integrated, step-by-step realization of cycle structure optimization and heat exchange network design.
目前文献在进行合成气制甲醇余热回收时，主要是通过热力循环回收低品位余热，没有考虑流程中热量的产生和利用，这样导致流程的能量利用率较低，循环可回收的余热量也较少。因此，如何设计耦合热力循环的合成气制甲醇是实现节能减排、提高能源利用率的关键。At present, when the waste heat recovery from synthesis gas to methanol is carried out in the literature, the low-grade waste heat is mainly recovered through the thermodynamic cycle, and the generation and utilization of heat in the process are not considered. few. Therefore, how to design a coupled thermodynamic cycle synthesis gas to methanol is the key to realize energy saving and emission reduction and improve energy utilization.
发明内容SUMMARY OF THE INVENTION
为解决上述问题，本发明提供一种耦合卡琳娜循环的合成气制甲醇的方法和装置，考虑了合成气制甲醇中热量产生和利用，同时优化流程和循环参数的合成气制甲醇和卡琳娜循环耦合设计的装置，最大程度提高合成气制甲醇的余热回收量和能量利用率。In order to solve the above-mentioned problems, the present invention provides a method and device for producing methanol from synthesis gas coupled with Karina cycle, which considers the generation and utilization of heat in the production of methanol from synthesis gas, and simultaneously optimizes the process and cycle parameters. The Linna cycle coupling design device maximizes the waste heat recovery and energy utilization rate of synthesis gas to methanol.
本发明的技术方案：Technical scheme of the present invention:
一种耦合卡琳娜循环的合成气制甲醇的装置，包括一个透平、一个节流阀、一个泵、一个反应器、两个分离器、两个混合器、两个压缩机、三个冷凝器和八个换热器。A device for producing methanol from syngas coupled with Karina cycle, comprising a turbine, a throttle valve, a pump, a reactor, two separators, two mixers, two compressors, and three condensers and eight heat exchangers.
第一分离器SE1的顶部与透平TU进口端连接，第一分离器SE1的底部与第四换热器HE4进口端连接，第四换热器HE4出口端和第七换热器HE7的进口端连接；第七换热器HE7的出口端与节流阀VA进口端连接，节流阀VA出口端和透平TU的出口端均与混合器M1进口端连接。第一混合器M1出口端与第九换热器HE9进口端连接，第九换热器HE9出口端与第一冷凝器CE1的进口端连接。第一冷凝器CE1的出口端与泵PU进口端连接，然后泵PU出口端与第九换热器HE9进口端、第九换热器HE9出口端与第八换热器HE8进口端、第八换热器HE8出口端与第五换热器HE5进口端、第五换热器HE5出口端与第三换热器HE3进口端、第三换热器HE3出口端与第一换热器HE1进口端依次连接。第一换热器HE1的出口端与第一分离器SE1进口端连接。The top of the first separator SE1 is connected to the inlet end of the turbine TU, the bottom of the first separator SE1 is connected to the inlet end of the fourth heat exchanger HE4, the outlet end of the fourth heat exchanger HE4 and the inlet of the seventh heat exchanger HE7 The outlet end of the seventh heat exchanger HE7 is connected to the inlet end of the throttle valve VA, and the outlet end of the throttle valve VA and the outlet end of the turbine TU are both connected to the inlet end of the mixer M1. The outlet end of the first mixer M1 is connected to the inlet end of the ninth heat exchanger HE9, and the outlet end of the ninth heat exchanger HE9 is connected to the inlet end of the first condenser CE1. The outlet end of the first condenser CE1 is connected to the inlet end of the pump PU, and then the outlet end of the pump PU is connected to the inlet end of the ninth heat exchanger HE9, the outlet end of the ninth heat exchanger HE9 is connected to the inlet end of the eighth heat exchanger HE8, the eighth heat exchanger HE8 The outlet end of the heat exchanger HE8 and the inlet end of the fifth heat exchanger HE5, the outlet end of the fifth heat exchanger HE5 and the inlet end of the third heat exchanger HE3, the outlet end of the third heat exchanger HE3 and the inlet end of the first heat exchanger HE1 connected in sequence. The outlet end of the first heat exchanger HE1 is connected to the inlet end of the first separator SE1.
第一压缩机CO1出口端与第二冷凝器CE2进口端连接，第二冷凝器CE2出口端与第二压缩机CO2进口端连接。第二压缩机CO2出口端和第二分离器SE2顶部分别与第二混合器M2进口端连接，然后第二混合器M2出口端分别与第七换热器HE7进口端和第六换热器HE6进口端连接，然后第七换热器HE7和第六换热器HE6的出口端混合后，与第四换热器HE4进口端连接，第四换热器HE4出口端与第二换热器HE2进口端连接，最后第二换热器HE2出口端与反应器RE进口端连接。反应器RE出口端与第二换热器HE2进口端连接，第二换热器HE2出口端与第三换热器HE3进口端连接，第三换热器HE3出口端分别与第五换热器HE5进口端和第六换热器HE6进口端连接，然后第五换热器HE5出口端和第六换热器HE6出口端同时与第八换热器HE8进口端连接，最后第八换热器HE8出口端与第三冷凝器CE3进口端连接，第三冷凝器CE3出口端与第二分离器SE2进口端连接。The outlet end of the first compressor CO1 is connected to the inlet end of the second condenser CE2, and the outlet end of the second condenser CE2 is connected to the inlet end of the second compressor CO2. The CO2 outlet end of the second compressor and the top of the second separator SE2 are respectively connected to the inlet end of the second mixer M2, and then the outlet end of the second mixer M2 is respectively connected to the inlet end of the seventh heat exchanger HE7 and the sixth heat exchanger HE6 The inlet end is connected, and then the outlet ends of the seventh heat exchanger HE7 and the sixth heat exchanger HE6 are mixed, and then connected to the inlet end of the fourth heat exchanger HE4, and the outlet end of the fourth heat exchanger HE4 is connected with the second heat exchanger HE2 The inlet end is connected, and finally the outlet end of the second heat exchanger HE2 is connected with the inlet end of the reactor RE. The outlet end of the reactor RE is connected to the inlet end of the second heat exchanger HE2, the outlet end of the second heat exchanger HE2 is connected to the inlet end of the third heat exchanger HE3, and the outlet end of the third heat exchanger HE3 is respectively connected to the fifth heat exchanger The inlet end of HE5 is connected to the inlet end of the sixth heat exchanger HE6, then the outlet end of the fifth heat exchanger HE5 and the outlet end of the sixth heat exchanger HE6 are connected to the inlet end of the eighth heat exchanger HE8 at the same time, and finally the eighth heat exchanger The outlet end of HE8 is connected to the inlet end of the third condenser CE3, and the outlet end of the third condenser CE3 is connected to the inlet end of the second separator SE2.
一种耦合卡琳娜循环的合成气制甲醇的方法，采用上述的装置，包括如下步骤：A method for producing methanol from synthesis gas coupled with Karina cycle, using the above-mentioned device, comprising the following steps:
步骤(1)、合成气经过第一压缩机CO1压缩后进入第二冷凝器CE2冷凝，然后进入第二压缩机CO2压缩；第二压缩机CO2的出口流股和第二分离器SE2分离出的未反应气体在第二混合器M2中进行混合；混合气体分成两股分别进入第六换热器HE6和第七换热器HE7预热后，再合流依次进入第四换热器HE4和第二换热器HE2预热，然后进入反应器RE进行反应。Step (1), the synthesis gas enters the second condenser CE2 after being compressed by the first compressor CO1 to condense, and then enters the second compressor CO2 to compress; the outlet stream of the second compressor CO2 and the second separator SE2 separate out The unreacted gas is mixed in the second mixer M2; the mixed gas is divided into two parts and respectively enters the sixth heat exchanger HE6 and the seventh heat exchanger HE7 after preheating, and then merges into the fourth heat exchanger HE4 and the second heat exchanger in turn. The heat exchanger HE2 is preheated, and then enters the reactor RE for reaction.
步骤(2)、反应器RE出口的高温气体和进入相应的各个换热器的其它流股依次经过第二换热器HE2、第三换热器HE3、第五换热器HE5和第八换热器HE8进行换热降温后，进入第三冷凝器CE3进一步降低流股温度，然后进入第二分离器SE2进行气液分离；第二分离器SE2顶部为未反应的气体，用于回流继续参与反应，底部为粗甲醇溶液。In step (2), the high temperature gas at the outlet of the reactor RE and other streams entering the corresponding heat exchangers pass through the second heat exchanger HE2, the third heat exchanger HE3, the fifth heat exchanger HE5 and the eighth heat exchanger in turn. After the heat exchanger HE8 conducts heat exchange and cooling, it enters the third condenser CE3 to further reduce the temperature of the stream, and then enters the second separator SE2 for gas-liquid separation; the top of the second separator SE2 is unreacted gas, which is used for reflux to continue to participate. Reaction, the bottom is crude methanol solution.
步骤(3)、泵PU的出口液态流股经过和进入相应的各个换热器的其它流股依次经过第九换热器HE9、第八换热器HE8、第五换热器HE5、第三换热器HE3和第一换热器HE1进行换热升温变为两相态流股，然后进入第一分离器SE1进行气液分离；分离出的气体通过透平TU进行膨胀做功；分离出的液体经过和进入相应的各个换热器的其它流股依次经过第四换热器HE4和第七换热器HE7进行换热降温，然后通过节流阀VA进行节流膨胀。Step (3), the outlet liquid stream of the pump PU passes through and enters the other streams of the respective heat exchangers successively through the ninth heat exchanger HE9, the eighth heat exchanger HE8, the fifth heat exchanger HE5, the third heat exchanger The heat exchanger HE3 and the first heat exchanger HE1 conduct heat exchange and increase the temperature into a two-phase stream, and then enter the first separator SE1 for gas-liquid separation; the separated gas is expanded through the turbine TU to do work; The other streams that the liquid passes through and enters the corresponding heat exchangers sequentially pass through the fourth heat exchanger HE4 and the seventh heat exchanger HE7 for heat exchange and cooling, and then pass through the throttle valve VA for throttling expansion.
步骤(4)、节流阀VA的出口流股和透平TU的出口流股在第一混合器M1内进行混合；第一混合器M1的出口流股经过和进入第九换热器HE9的其它流股进行换热降温后进入第一冷凝器CE1进一步降温变为饱和液态，然后进入泵PU进行增压。Step (4), the outlet stream of the throttle valve VA and the outlet stream of the turbine TU are mixed in the first mixer M1; the outlet stream of the first mixer M1 passes through and enters the ninth heat exchanger HE9. After heat exchange and cooling, other streams enter the first condenser CE1 for further cooling and become saturated liquid, and then enter the pump PU for pressurization.
本发明具有如下有益效果：The present invention has the following beneficial effects:
本发明在不降低合成气制甲醇的总转化率的前提下，采用卡琳娜循环回收合成气制甲醇中的余热，最大程度提高合成气制甲醇耦合卡琳娜循环系统的余热回收量和能量利用效率。On the premise of not reducing the total conversion rate of synthesis gas to methanol, the invention adopts Karina cycle to recover the waste heat in the synthesis gas to methanol, and maximizes the waste heat recovery amount and energy of the synthesis gas to methanol coupling Karina cycle system usage efficiency.
附图说明Description of drawings
图1为本发明的耦合卡琳娜循环的合成气制甲醇的装置示意图。FIG. 1 is a schematic diagram of a device for producing methanol from synthesis gas coupled with Karina cycle according to the present invention.
图中：In the picture:
SE1第一分离器；SE2第二分离器；M1第一混合器；M2第二混合器；TU透平；CO1第一压缩机；CO2第一压缩机；VA节流阀；PU泵；RE反应器；HE1-8第一-第八换热器；CE1-3第一-第三冷凝器；SE1 first separator; SE2 second separator; M1 first mixer; M2 second mixer; TU turbine; CO1 first compressor; CO2 first compressor; VA throttle valve; PU pump; RE reaction Heat exchanger; HE1-8 first-eighth heat exchanger; CE1-3 first-third condenser;
1-9卡琳娜循环流股；10-19合成气制甲醇流股。1-9 Karina recycle streams; 10-19 syngas-to-methanol streams.
具体实施方式Detailed ways
以下结合附图和技术方案，进一步说明本发明的具体实施方式，并非限制本发明所涉及的范围。The specific embodiments of the present invention are further described below with reference to the accompanying drawings and technical solutions, but do not limit the scope of the present invention.
本发明的耦合卡琳娜循环的合成气制甲醇的装置以及工艺流程如图1所示，其中，第一-第九流股(1-9)为卡琳娜循环流股；第十-第十九流股(10-19)为合成气制甲醇流股。The device and process flow of the synthesis gas to methanol coupled with Karina cycle of the present invention are shown in Figure 1, wherein the first-ninth streams (1-9) are Karina cycle streams; Nineteen streams (10-19) are syngas-to-methanol streams.
实施例Example
合成气入口流股的流量为11450kmol/h、温度为50℃、压力为51.2bar，进料中含氢气67.45％、一氧化碳22.97％、二氧化碳6.86％、水0.23％、氮气2.48％。第二分离器SE2的温度为38℃。合成气制甲醇的反应压力、介质温度和反应器入口温度分别为74.6bar、173.2℃和123.7℃。卡琳娜循环的蒸发温度、蒸发压力、氨水质量分数和工质流量分别为144.3℃、68.5bar、0.894和110.0kg/s。The syngas inlet stream had a flow rate of 11450 kmol/h, a temperature of 50°C, a pressure of 51.2 bar, and the feed contained 67.45% hydrogen, 22.97% carbon monoxide, 6.86% carbon dioxide, 0.23% water, and 2.48% nitrogen. The temperature of the second separator SE2 was 38°C. The reaction pressure, medium temperature and reactor inlet temperature of synthesis gas to methanol were 74.6 bar, 173.2 °C and 123.7 °C, respectively. The evaporation temperature, evaporation pressure, ammonia water mass fraction and working fluid flow rate of Karina cycle were 144.3 °C, 68.5 bar, 0.894 and 110.0 kg/s, respectively.
采用本发明中的装置和方法，可最大程度利用和回收合成气制甲醇的能量。整个耦合设计装置的净产功为15206.3kW，该净产功包含了合成气制甲醇的耗功和卡琳娜循环的产功。By adopting the device and method in the present invention, the energy of synthesis gas to methanol can be utilized and recovered to the maximum extent. The net power production of the entire coupling design device is 15206.3kW, which includes the power consumption of synthesis gas to methanol and the power production of Karina cycle.
比较例Comparative example
文献(Design and Control of a Methanol Reactor/Column Process.Ind EngChem Res 2010；49(13):6150-63.)报道了一种合成气制甲醇流程方法，是一种采用常规的卡琳娜循环进行合成气制甲醇流程，具体参数：第二分离器SE2的温度为38℃，合成气制甲醇的反应压力、介质温度和反应器入口温度分别为110bar、264℃和150℃。The literature (Design and Control of a Methanol Reactor/Column Process. Ind EngChem Res 2010; 49(13):6150-63.) reported a process method for producing methanol from syngas, which is a conventional Karina cycle for The specific parameters of the synthesis gas-to-methanol process: the temperature of the second separator SE2 is 38°C, and the reaction pressure, medium temperature and reactor inlet temperature of the synthesis gas-to-methanol are 110bar, 264°C and 150°C, respectively.
合成气和进料参数与实施例相同，具体为：合成气入口流股的流量为11450kmol/h、温度为50℃、压力为51.2bar，进料中含氢气67.45％、一氧化碳22.97％、二氧化碳6.86％、水0.23％、氮气2.48％。Synthesis gas and feed parameters are the same as in the embodiment, specifically: the flow rate of the synthesis gas inlet stream is 11450kmol/h, the temperature is 50°C, the pressure is 51.2bar, and the feed contains 67.45% hydrogen, 22.97% carbon monoxide, and 6.86% carbon dioxide. %, water 0.23%, nitrogen 2.48%.
采用该文献的方法通过卡琳娜循环进行余热回收，其中，卡琳娜循环的蒸发温度、蒸发压力、氨水质量分数和工质流量分别为157.0℃、68.3bar、0.874和91.5kg/s。回收余热后，系统的净产功为8371.4kW。The method of this document is used for waste heat recovery through Karina cycle, wherein the evaporation temperature, evaporation pressure, ammonia water mass fraction and working fluid flow rate of Karina cycle are 157.0°C, 68.3bar, 0.874 and 91.5kg/s, respectively. After recovering the waste heat, the net power output of the system is 8371.4kW.
通过对比发现，本发明的合成气制甲醇耦合卡琳娜循环装置，能够同时优化流程和循环的关键参数，系统的净产功提高了81.6％。Through comparison, it is found that the synthesis gas-to-methanol coupling Karina cycle device of the present invention can simultaneously optimize the key parameters of the process and the cycle, and the net production work of the system is increased by 81.6%.
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Non-Patent Citations (2)
| Title |
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| LUYBEN, WILLIAM L.: "Design and Control of a Methanol Reactor/Column Process", 《INDUSTRIAL & ENGINEERING CHEMISTRY RESEARCH》 * |
| ZHOU CONGCONG 等: "A novel pinch-based method for process integration and optimization of Kalina cycle", 《ENERGY CONVERSION AND MANAGEMENT》 * |
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| CN115305124A (en) * | 2022-07-22 | 2022-11-08 | 重庆大学 | Energy-saving type methanol preparation system and method by methane mixed reforming based on kalina cycle and heat integration |
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