CN110143850A - Single-column steam-driven energy-saving methanol multi-effect rectification method without by-product fusel oil - Google Patents
Single-column steam-driven energy-saving methanol multi-effect rectification method without by-product fusel oil Download PDFInfo
- Publication number
- CN110143850A CN110143850A CN201910453840.6A CN201910453840A CN110143850A CN 110143850 A CN110143850 A CN 110143850A CN 201910453840 A CN201910453840 A CN 201910453840A CN 110143850 A CN110143850 A CN 110143850A
- Authority
- CN
- China
- Prior art keywords
- tower
- product
- pressure
- methanol
- column
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 title claims abstract description 258
- 238000000034 method Methods 0.000 title claims abstract description 58
- 239000001760 fusel oil Substances 0.000 title claims abstract description 16
- 239000006227 byproduct Substances 0.000 title claims description 7
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 27
- 239000002994 raw material Substances 0.000 claims abstract description 15
- 239000002351 wastewater Substances 0.000 claims abstract description 11
- 239000000498 cooling water Substances 0.000 claims abstract description 7
- 238000009833 condensation Methods 0.000 claims abstract description 4
- 230000005494 condensation Effects 0.000 claims abstract description 4
- 239000000047 product Substances 0.000 claims description 51
- 238000011084 recovery Methods 0.000 claims description 34
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 claims description 16
- 239000000446 fuel Substances 0.000 claims description 10
- 238000000605 extraction Methods 0.000 claims description 9
- 238000004821 distillation Methods 0.000 claims description 3
- 238000010438 heat treatment Methods 0.000 claims description 3
- 238000004064 recycling Methods 0.000 claims 2
- 235000008733 Citrus aurantifolia Nutrition 0.000 claims 1
- 238000010795 Steam Flooding Methods 0.000 claims 1
- 235000011941 Tilia x europaea Nutrition 0.000 claims 1
- 239000004571 lime Substances 0.000 claims 1
- 238000002156 mixing Methods 0.000 claims 1
- 238000000746 purification Methods 0.000 claims 1
- 238000005194 fractionation Methods 0.000 abstract description 20
- 238000005406 washing Methods 0.000 abstract description 10
- 238000010992 reflux Methods 0.000 abstract description 6
- 238000005265 energy consumption Methods 0.000 description 7
- 239000000126 substance Substances 0.000 description 5
- 230000008901 benefit Effects 0.000 description 4
- 239000003245 coal Substances 0.000 description 4
- 238000004519 manufacturing process Methods 0.000 description 4
- 238000005516 engineering process Methods 0.000 description 3
- 239000012535 impurity Substances 0.000 description 3
- 230000010354 integration Effects 0.000 description 3
- LCGLNKUTAGEVQW-UHFFFAOYSA-N Dimethyl ether Chemical compound COC LCGLNKUTAGEVQW-UHFFFAOYSA-N 0.000 description 2
- 239000002920 hazardous waste Substances 0.000 description 2
- 230000001476 alcoholic effect Effects 0.000 description 1
- 238000004364 calculation method Methods 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 238000010168 coupling process Methods 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000009826 distribution Methods 0.000 description 1
- 239000003814 drug Substances 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 239000012847 fine chemical Substances 0.000 description 1
- 239000007788 liquid Substances 0.000 description 1
- 239000012074 organic phase Substances 0.000 description 1
- 239000000575 pesticide Substances 0.000 description 1
- 239000004033 plastic Substances 0.000 description 1
- 229920003023 plastic Polymers 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 238000003860 storage Methods 0.000 description 1
Classifications
-
- 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
- C07C29/74—Separation; Purification; Use of additives, e.g. for stabilisation
- C07C29/76—Separation; Purification; Use of additives, e.g. for stabilisation by physical treatment
- C07C29/80—Separation; Purification; Use of additives, e.g. for stabilisation by physical treatment by distillation
-
- 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
- Y02P20/10—Process efficiency
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
本发明涉及一种不副产杂醇油的单塔蒸汽驱动节能型甲醇多效精馏方法，包括如下步骤：粗甲醇原料进入预分塔，塔顶蒸汽依次经过二级冷凝，随后进入水洗塔，冷凝器及水洗塔出口凝液进入回流罐，不凝气从水洗塔塔顶采出，预分塔塔底再沸器由来自高压塔塔顶的一股甲醇蒸汽驱动，预分塔塔底产品进入常压塔；常压塔塔顶采出精甲醇产品，塔顶冷凝器用工艺冷却水进行冷却，塔底再沸器由来自中压塔塔顶甲醇蒸汽驱动，常压塔塔底产品进入中压塔；中压塔塔顶采出精甲醇产品，塔底再沸器由来自高压塔塔顶的一股甲醇蒸汽进行加热，塔底产品进入高压塔；高压塔塔顶采出精甲醇产品，塔底再沸器采用工程蒸汽进行加热，塔底得到合格的净化废水。
The invention relates to a single-column steam-driven energy-saving methanol multi-effect rectification method without by-producing fusel oil, which comprises the following steps: the crude methanol raw material enters a pre-fractionation tower, and the tower top steam undergoes secondary condensation in sequence, and then enters a water washing tower , the condensate at the outlet of the condenser and the washing tower enters the reflux tank, and the non-condensable gas is extracted from the top of the washing tower. The product enters the atmospheric tower; the refined methanol product is extracted from the top of the atmospheric tower, the tower top condenser is cooled with process cooling water, the reboiler at the bottom of the tower is driven by methanol vapor from the top of the medium pressure tower, and the bottom product of the atmospheric tower enters the Medium pressure tower; the refined methanol product is extracted from the top of the medium pressure tower, the bottom reboiler is heated by a methanol vapor from the top of the high pressure tower, and the bottom product enters the high pressure tower; the refined methanol product is extracted from the top of the high pressure tower , The reboiler at the bottom of the tower is heated by engineering steam, and the bottom of the tower gets qualified purified wastewater.
Description
技术领域technical field
本发明属于精馏技术领域，涉及煤基甲醇生产过程中大宗化工产品甲醇分离提纯的节能工艺。The invention belongs to the technical field of rectification, and relates to an energy-saving process for separating and purifying bulk chemical product methanol in a coal-based methanol production process.
背景技术Background technique
甲醇是一种大宗化工基础原料，广泛用于各类精细化工、塑料、农药及医药等领域。甲醇经深加工后也可作为一种新型清洁燃料，在世界化工市场中占有重要地位。Methanol is a bulk chemical basic raw material, which is widely used in various fields of fine chemicals, plastics, pesticides and medicine. Methanol can also be used as a new type of clean fuel after deep processing, occupying an important position in the world chemical market.
基于我国富煤少油贫气的现实，煤化工行业迅速发展。煤制甲醇工艺生产的粗甲醇产品，包含二甲醚等轻组分杂质及乙醇、水等重组分杂质。该粗甲醇产品需要经过精馏过程除去各类轻重杂质，得到符合质量要求的精甲醇产品。Based on the reality that my country is rich in coal, low in oil and poor in gas, the coal chemical industry is developing rapidly. The crude methanol product produced by the coal-to-methanol process contains light component impurities such as dimethyl ether and heavy component impurities such as ethanol and water. The crude methanol product needs to go through a rectification process to remove all kinds of light and heavy impurities to obtain a refined methanol product that meets the quality requirements.
甲醇精馏过程能耗约占生产总过程的20-30％，研究甲醇精馏过程节能方法，已成为煤化工企业生存和提高市场竞争力的关键手段，日益受到科研工作者关注。The energy consumption of methanol rectification process accounts for about 20-30% of the total production process. Research on energy-saving methods in methanol rectification process has become a key means for coal chemical enterprises to survive and improve market competitiveness, and has attracted increasing attention of scientific researchers.
传统的甲醇单塔精馏工艺及双塔精馏工艺，尽管其投资相对降低，但是产品质量相对较差、甲醇回收率较低且能耗巨大，已被德国Lurgi公司开发的甲醇三塔精馏工艺及四塔精馏工艺(三塔加回收塔)所取代。目前，国内在建及已建成的甲醇精馏装置几乎全部采用三塔四塔精馏工艺。The traditional methanol single-column rectification process and double-column rectification process, although the investment is relatively low, the product quality is relatively poor, the methanol recovery rate is low and the energy consumption is huge. process and four-column rectification process (three-column plus recovery column). At present, almost all methanol rectification plants under construction and completed in China adopt the three-tower four-column rectification process.
Lurgi三塔精馏工艺由预分塔、高压塔和常压塔组成。预分塔塔顶脱除粗甲醇产品中的轻组分，塔底产品进入高压塔。高压塔塔顶采出的甲醇蒸汽进入常压塔再沸器进行冷凝，为常压塔提供能量，形成双效精馏过程。精甲醇产品分别从高压塔和常压塔塔顶采出，经冷却降温后进入精甲醇储罐。为保证塔顶塔底产品质量，需要在常压塔中段采出一股杂醇油。与两塔精馏工艺相比，三塔工艺增加一个精馏塔，采用高低压的热集成方式降低能耗。三塔四塔工艺甲醇/蒸汽单耗约为1.1～1.5。The three-column rectification process of Lurgi consists of a pre-fractionation column, a high-pressure column and an atmospheric column. The top of the pre-fractionation tower removes the light components in the crude methanol product, and the product at the bottom of the tower enters the high-pressure tower. The methanol vapor extracted from the top of the high-pressure tower enters the reboiler of the atmospheric tower for condensation, which provides energy for the atmospheric tower and forms a double-effect rectification process. The refined methanol product is extracted from the top of the high pressure tower and the atmospheric tower respectively, and then enters the refined methanol storage tank after cooling down. In order to ensure the quality of products at the top and bottom of the tower, it is necessary to produce a fusel oil in the middle section of the atmospheric tower. Compared with the two-column rectification process, the three-column process adds a rectification column, and adopts a high and low pressure heat integration method to reduce energy consumption. The methanol/steam unit consumption of the three-column four-column process is about 1.1 to 1.5.
Lurgi四塔精馏工艺在三塔工艺的基础上，增加一个回收塔以提高甲醇收率。与三塔工艺类似，回收塔也需要侧线采出一股杂醇油以保证产品质量。杂醇油可以认为是含水量大于1000ppm的醇类有机相。中国专利200610013269.9公开了一种“甲醇双效精馏节能节水系统及工艺”，该工艺基于广泛采用的Lurgi四塔精馏工艺，利用蒸汽冷凝水的热量，重新设计了换热网络，从而达到了节能的目的，该工艺的甲醇/蒸汽单耗约为1.0。On the basis of the three-column process, the Lurgi four-column distillation process adds a recovery column to improve the methanol yield. Similar to the three-column process, the recovery column also needs to produce a fusel oil sideline to ensure product quality. The fusel oil can be considered to be an alcoholic organic phase with a water content greater than 1000 ppm. Chinese patent 200610013269.9 discloses a "methanol double-effect rectification energy-saving and water-saving system and process", which is based on the widely used Lurgi four-column rectification process, and uses the heat of steam condensed water to redesign the heat exchange network, so as to achieve For the purpose of energy saving, the methanol/steam unit consumption of this process is about 1.0.
中国专利201010563457.5公开了一种“大型甲醇多效精馏节能装置及甲醇多效精馏节能工艺”，该工艺所用的主要设备包括预精馏塔、第二精馏塔、加压塔、常压塔和回收塔五个塔，其中第二精馏塔、加压塔和常压塔塔顶分别采出精甲醇产品，回收塔塔顶塔底分别采出杂醇油和净化废水。第二精馏塔与预精馏塔构成双效精馏，加压塔和常压塔构成双效精馏，甲醇/蒸汽单耗约为0.85。中国专利200910022575.2公开了“一种甲醇多效精馏工艺”，该工艺在四塔精馏工艺的基础上新增一个精馏塔，构成了五塔精馏工艺。其中设计高-中-低三塔形成多效精馏，并且回收塔与预分塔构成双效精馏，最终甲醇/蒸汽单耗约为0.7。中国专利201710342561.3公开了“一种热泵和多效耦合的甲醇精馏方法”，该工艺包括脱轻塔、常压塔I、常压塔II、加压塔和回收塔五个塔，其中常压塔I采用热泵精馏技术，将其塔顶的蒸汽压缩后供给塔底再沸器，加压塔与常压塔II构成双效精馏，脱轻塔与回收塔构成双效精馏。但是由于压缩机投入成本高，尽管在能耗上有所降低，总体经济效益仍缺乏评估。Chinese patent 201010563457.5 discloses a "large-scale methanol multi-effect rectification energy-saving device and methanol multi-effect rectification energy-saving process". The main equipment used in this process includes a pre-rectification tower, a second rectification tower, a pressurized tower, and an atmospheric pressure tower. There are five towers in the tower and the recovery tower, of which the second rectification tower, the pressurized tower and the atmospheric pressure tower are respectively extracted from the top of the refined methanol product, and the recovery tower is extracted from the top and bottom of the tower to extract the fusel oil and purified waste water. The second rectification tower and the pre-rectification tower form double-effect rectification, the pressurized tower and the atmospheric pressure tower form double-effect rectification, and the unit consumption of methanol/steam is about 0.85. Chinese Patent No. 200910022575.2 discloses "a methanol multi-effect rectification process", which adds a rectifying tower to the four-column rectification process to form a five-column rectification process. Among them, the high-medium-low three towers are designed to form multi-effect rectification, and the recovery tower and the pre-fractionation tower form double-effect rectification, and the final methanol/steam unit consumption is about 0.7. Chinese patent 201710342561.3 discloses "a heat pump and multi-effect coupling method for methanol rectification". The process includes five towers: light removal tower, atmospheric pressure tower I, atmospheric pressure tower II, pressurization tower and recovery tower, wherein atmospheric pressure The tower I adopts the heat pump rectification technology, and the vapor at the top of the tower is compressed and then supplied to the reboiler at the bottom of the tower. However, due to the high input cost of the compressor, despite the reduction in energy consumption, the overall economic benefits are still lacking.
目前，副产品杂醇油已进入国家危险废物名录，上述所提及的各类工艺技术尽管在能耗上有优势，但都不可避免副产杂醇油。为了避免产生该副产品，需要对精馏工艺进行改造，将杂醇油转化为水含量低于1000ppm的无水混合醇燃料，以提高工艺整体的原料利用率，提高经济效益。At present, the by-product fusel oil has entered the national list of hazardous wastes. Although the various technologies mentioned above have advantages in energy consumption, by-product fusel oil is inevitable. In order to avoid the generation of this by-product, the rectification process needs to be transformed, and the fusel oil is converted into anhydrous mixed alcohol fuel with a water content of less than 1000 ppm, so as to improve the overall raw material utilization rate of the process and improve economic benefits.
发明内容SUMMARY OF THE INVENTION
本发明旨在弥补上述现有精馏工艺过程中的技术不足，提供一种低能耗、高收率且不副产杂醇油的单塔蒸汽驱动节能型甲醇多效精馏工艺。为达到上述目的，本发明技术采用的技术方案如下：The invention aims to make up for the technical deficiencies in the above-mentioned existing rectification process, and provides a single-column steam-driven energy-saving methanol multi-effect rectification process with low energy consumption, high yield and no by-product fusel oil. In order to achieve the above object, the technical scheme adopted by the technology of the present invention is as follows:
一种不副产杂醇油的单塔蒸汽驱动节能型甲醇多效精馏方法，所采用的设备包括预分塔、常压塔、中压塔、高压塔和回收塔五个塔，预分塔塔底通过管路与常压塔中下部相连接；常压塔塔底通过管路与中压塔中下部相连接；中压塔塔底通过管路与高压塔中下部相连接；高压塔侧线采出通过管路与回收塔中下部相连接，所述的方法包括如下步骤：A single-column steam-driven energy-saving methanol multi-effect rectification method without by-producing fusel oil, the equipment used comprises five towers: a pre-fractionation tower, an atmospheric tower, a medium-pressure tower, a high-pressure tower and a recovery tower. The bottom of the tower is connected with the middle and lower parts of the atmospheric tower through pipelines; the bottom of the atmospheric tower is connected with the middle and lower parts of the medium pressure tower through pipelines; the bottom of the medium pressure tower is connected with the middle and lower parts of the high pressure tower through pipelines; the high pressure tower The side line extraction is connected with the middle and lower part of the recovery tower through pipelines, and the method comprises the following steps:
(1)粗甲醇原料进入预分塔，塔顶蒸汽依次经过二级冷凝，随后进入水洗塔，冷凝器及水洗塔出口凝液进入回流罐，不凝气从水洗塔塔顶采出，预分塔塔底再沸器由来自高压塔塔顶的一股甲醇蒸汽驱动，预分塔塔底产品进入常压塔。(1) The crude methanol raw material enters the pre-fractionation tower, and the vapor at the top of the tower undergoes secondary condensation in turn, and then enters the water washing tower. The condenser and the condensate at the outlet of the water washing tower enter the reflux tank, and the non-condensable gas is extracted from the top of the water washing tower. The column bottom reboiler is driven by a methanol vapor from the top of the high pressure column, and the bottom product of the pre-fractionation column enters the atmospheric column.
(2)常压塔塔顶采出精甲醇产品，塔顶冷凝器用工艺冷却水进行冷却，塔底再沸器由来自中压塔塔顶甲醇蒸汽驱动，常压塔塔底产品进入中压塔。(2) The refined methanol product is extracted from the top of the atmospheric tower, the tower top condenser is cooled with process cooling water, the bottom reboiler is driven by methanol steam from the top of the medium pressure tower, and the bottom product of the atmospheric tower enters the medium pressure tower .
(3)中压塔塔顶采出精甲醇产品，塔底再沸器由来自高压塔塔顶的一股甲醇蒸汽进行加热，塔底产品进入高压塔。(3) The refined methanol product is extracted from the top of the medium-pressure tower, and the reboiler at the bottom of the tower is heated by a methanol vapor from the top of the high-pressure tower, and the product at the bottom of the tower enters the high-pressure tower.
(4)高压塔塔顶采出精甲醇产品，塔底再沸器采用工程蒸汽进行加热，塔底得到合格的净化废水。(4) The refined methanol product is extracted from the top of the high-pressure tower, the reboiler at the bottom of the tower is heated by engineering steam, and the bottom of the tower is obtained qualified purified waste water.
(5)高压塔侧线采出一股主要含甲醇、乙醇和水的产品进入回收塔，回收塔塔顶冷凝器利用工艺冷却水进行冷却，回收塔塔顶得到含水量小于1000ppm的燃料醇产品，回收塔塔底再沸器由来自高压塔塔底产品加热，回收塔塔底得到合格的净化废水，与高压塔塔底废水混合后，进入后续水处理系统。(5) a product mainly containing methanol, ethanol and water is extracted from the side line of the high-pressure tower and enters the recovery tower, the tower top condenser of the recovery tower is cooled by using process cooling water, and the recovery tower tower top obtains a fuel alcohol product with a water content of less than 1000ppm, The reboiler at the bottom of the recovery tower is heated by the product from the bottom of the high-pressure tower, and the bottom of the recovery tower obtains qualified purified wastewater, which is mixed with the wastewater at the bottom of the high-pressure tower and enters the subsequent water treatment system.
优选地：预分塔压力为150-170kPa；常压塔压力为100-110kPa；中压塔压力为240-260kPa；高压塔压力为580-620kPa；回收塔压力为100-120kPa。Preferably: the pressure of the pre-fractionation tower is 150-170kPa; the pressure of the atmospheric tower is 100-110kPa; the pressure of the medium-pressure tower is 240-260kPa; the pressure of the high-pressure tower is 580-620kPa; the pressure of the recovery tower is 100-120kPa.
常压塔塔顶采出精甲醇量占总精甲醇产品的30-35％；中压塔塔顶采出精甲醇量占总精甲醇产品的30-35％；高压塔塔顶采出精甲醇量占总精甲醇产品的30-35％；回收塔塔顶采出含水量小于1000ppm的混合醇燃料产品量占粗甲醇原料量1％。The amount of refined methanol extracted from the top of the atmospheric pressure tower accounts for 30-35% of the total refined methanol products; the amount of refined methanol extracted from the top of the medium pressure tower accounts for 30-35% of the total refined methanol products; the top of the high-pressure tower is extracted from refined methanol The amount of mixed alcohol fuel products with water content less than 1000ppm produced at the top of the recovery tower accounts for 1% of the crude methanol raw material amount.
本发明所述甲醇精馏工艺与现有的甲醇三塔、四塔精馏工艺相比，主要区别是：(1)增加一个中压塔，使得常压-中压-高压三塔实现多效热集成；(2)多效精馏采用逆向低-中-高压力驱动，而不是传统工艺的高-低压驱动(3)利用高压塔塔顶多余的热负荷，与预分塔也形成双效精馏；(4)回收塔采出混合醇燃料而不是传统工艺杂醇油。Compared with the existing three-column and four-column methanol distillation process of the present invention, the main differences are: (1) adding a medium pressure column, so that the atmospheric pressure-medium pressure-high pressure three columns can realize multiple effects Heat integration; (2) Multi-effect rectification adopts reverse low-medium-high pressure drive instead of high-low pressure drive of traditional process (3) Utilizes the excess heat load at the top of the high-pressure tower, which also forms a double-effect with the pre-fractionation tower Rectification; (4) The recovery tower produces mixed alcohol fuel instead of traditional process fusel oil.
本发明优势在于，与传统甲醇三塔四塔双效精馏工艺不同，本发明通过增设一中压塔并调整甲醇采出分布，使得常压-中压-高压塔实现多效精馏热集成，并且高压塔与预分塔也构成双效精馏。整个工艺过程只有高压塔需要外界热源输入，甲醇/蒸汽单耗降至0.6-0.7，相比于传统流程，可大幅降低能耗。此外，通过较少的投资增设一新中压塔，可使常压塔和高压塔的处理负荷降低，从而增加原料处理量，达到扩产的目的。最后，由于传统工艺中生产的杂醇油已经进入国家危险废物名录，本发明通过回收塔塔顶采出含水量小于1000ppm的混合醇燃料，避免了杂醇油的生产，提升总体原料利用率。The advantage of the present invention is that, different from the traditional methanol three-column four-column double-effect rectification process, the present invention adds a medium-pressure column and adjusts the methanol production distribution, so that the atmospheric-medium-pressure-high pressure column can realize the multi-effect rectification heat integration , and the high-pressure tower and the pre-fractionation tower also constitute double-effect rectification. In the whole process, only the high-pressure tower needs external heat source input, and the unit consumption of methanol/steam is reduced to 0.6-0.7, which can greatly reduce the energy consumption compared with the traditional process. In addition, by adding a new medium-pressure tower with less investment, the processing load of the atmospheric tower and the high-pressure tower can be reduced, thereby increasing the processing capacity of raw materials and achieving the purpose of expansion. Finally, since the fusel oil produced in the traditional process has entered the national list of hazardous wastes, the present invention produces a mixed alcohol fuel with a water content less than 1000 ppm at the top of the recovery tower, thereby avoiding the production of fusel oil and improving the overall raw material utilization rate.
附图说明Description of drawings
图1为本发明所示的的不副产杂醇油的单塔蒸汽驱动节能型甲醇多效精馏工艺流程图。Fig. 1 is the single-column steam-driven energy-saving methanol multi-effect rectification process flow diagram without by-product fusel oil shown in the present invention.
其中：1—预分塔，2—预分塔塔顶一级冷凝器，3—预分塔塔顶二级冷凝器，4—水洗塔，5—预分塔塔顶回流罐，6—预分塔塔底再沸器，7—常压塔，8—常压塔塔顶冷凝器，9—常压塔塔底再沸器，10—中压塔，11—中压塔塔底再沸器，12—高压塔，13—高压塔塔底再沸器，14—回收塔，15—回收塔塔顶冷凝器，16—回收塔塔底再沸器。Among them: 1—pre-fractionation tower, 2—first-stage condenser at the top of pre-fractionation tower, 3-secondary condenser at the top of pre-fractionation tower, 4-water washing tower, 5-pre-fractionation tower top reflux tank, 6-pre-fractionation tower top Separation tower bottom reboiler, 7—atmospheric pressure tower, 8—atmospheric pressure tower top condenser, 9—atmospheric pressure tower bottom reboiler, 10—medium pressure tower, 11—medium pressure tower bottom reboiler 12—high pressure tower, 13—reboiler at the bottom of high pressure tower, 14—recovery tower, 15—recovery tower top condenser, 16—recovery tower bottom reboiler.
具体实施方式Detailed ways
下面结合附图对本发明的设备和方法做进一步说明。The device and method of the present invention will be further described below with reference to the accompanying drawings.
组成如表1所示的75℃粗甲醇原料进入预分塔(1)，预分塔(1)塔顶蒸汽依次经过一级冷凝器(2)和二级冷凝器(3)，分别被冷凝至65℃和40℃，随后进入水洗塔(4)。一级二级冷凝器及水洗塔出口凝液进入回流罐(5)，不凝气从水洗塔(4)塔顶采出。预分塔塔底再沸器(6)由来自高压塔(12)塔顶一股甲醇蒸汽驱动，预分塔(1)塔底产品进入常压塔(7)中下部。占粗甲醇原料量约33％的精甲醇产品从常压塔(7)塔顶采出，常压塔塔顶冷凝器(8)用工艺冷却水进行冷却，常压塔塔底再沸器(9)由来自中压塔(10)塔顶甲醇蒸汽驱动。常压塔(7)塔底产品进入中压塔(10)中下部，中压塔(10)塔顶采出占粗甲醇原料量约33％的精甲醇产品，中压塔塔底再沸器(11)由来自高压塔(12)塔顶的一股甲醇蒸汽进行加热。中压塔(10)塔底产品进入高压塔(12)中下部，高压塔(12)塔顶采出占粗甲醇原料量约33％的精甲醇产品，高压塔塔底再沸器(13)采用0.8MPaG(175℃)公用工程蒸汽进行加热。高压塔(12)塔底得到合格的废水产品。高压塔(12)侧线采出一股主要含甲醇、乙醇和水的产品进入回收塔(14)，侧线采出量约占粗甲醇原料的1％。回收塔塔顶冷凝器(15)利用工艺冷却水进行冷却，回收塔(14)塔顶得到含水量小于1000ppm的燃料醇产品。回收塔塔底再沸器(16)由来自高压塔(12)塔底产品加热。回收塔(14)塔底得到合格的废水产品，与高压塔(12)塔底产品混合后，进入后续水处理系统。经计算，在满足美国AA级甲醇产品要求、净化废水产品要求和燃料醇产品要求的前提下，甲醇蒸汽单耗为0.63。The 75 ℃ crude methanol raw material as shown in Table 1 enters the pre-fractionation tower (1), and the pre-fractionation tower (1) overhead steam passes through the primary condenser (2) and the secondary condenser (3) in turn, and is condensed respectively. to 65°C and 40°C, and then enter the water washing tower (4). The condensed liquid from the primary and secondary condensers and the outlet of the water washing tower enters the reflux tank (5), and the non-condensable gas is extracted from the top of the water washing tower (4). The reboiler (6) at the bottom of the pre-fractionation tower is driven by a methanol vapor from the top of the high-pressure tower (12), and the bottom product of the pre-fractionation tower (1) enters the middle and lower part of the atmospheric tower (7). The refined methanol product, which accounts for about 33% of the raw methanol raw material, is extracted from the top of the atmospheric tower (7), the atmospheric tower top condenser (8) is cooled with process cooling water, and the atmospheric tower bottom reboiler ( 9) Driven by methanol vapor from the top of the medium pressure tower (10). The bottom product of the atmospheric pressure column (7) enters the middle and lower part of the medium pressure column (10), and the refined methanol product, which accounts for about 33% of the crude methanol raw material, is extracted from the top of the medium pressure column (10), and the bottom reboiler of the medium pressure column (11) is heated by a stream of methanol vapor from the top of the high pressure column (12). The product at the bottom of the medium pressure column (10) enters the middle and lower part of the high pressure column (12), and the refined methanol product, which accounts for about 33% of the raw methanol raw material, is extracted from the top of the high pressure column (12), and the high pressure column bottom reboiler (13) Use 0.8MPaG (175℃) utility steam for heating. A qualified waste water product is obtained at the bottom of the high pressure tower (12). A product mainly containing methanol, ethanol and water is extracted from the side line of the high pressure tower (12) and sent to the recovery tower (14), and the output amount of the side line is about 1% of the crude methanol raw material. The recovery tower overhead condenser (15) is cooled by using process cooling water, and the recovery tower (14) overhead obtains a fuel alcohol product with a water content of less than 1000 ppm. The recovery column bottoms reboiler (16) is heated by the bottoms product from the higher pressure column (12). A qualified waste water product is obtained from the bottom of the recovery tower (14), which is mixed with the bottom product of the high-pressure tower (12) and then enters the subsequent water treatment system. After calculation, the unit consumption of methanol steam is 0.63 under the premise of meeting the requirements of AA grade methanol products, purified wastewater products and fuel alcohol products in the United States.
各塔具体工艺条件见表2。The specific process conditions of each tower are shown in Table 2.
表1原料甲醇组成Table 1 Composition of raw material methanol
表2各塔工艺条件Table 2 Process conditions of each tower
1预分塔回流比为塔顶回流总量与粗甲醇原料进料量比值。 1 The reflux ratio of the pre-fractionation column is the ratio of the total amount of reflux at the top of the column to the feed amount of crude methanol raw materials.
Claims (3)
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201910453840.6A CN110143850A (en) | 2019-05-28 | 2019-05-28 | Single-column steam-driven energy-saving methanol multi-effect rectification method without by-product fusel oil |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201910453840.6A CN110143850A (en) | 2019-05-28 | 2019-05-28 | Single-column steam-driven energy-saving methanol multi-effect rectification method without by-product fusel oil |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN110143850A true CN110143850A (en) | 2019-08-20 |
Family
ID=67593542
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201910453840.6A Pending CN110143850A (en) | 2019-05-28 | 2019-05-28 | Single-column steam-driven energy-saving methanol multi-effect rectification method without by-product fusel oil |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN110143850A (en) |
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110759812A (en) * | 2019-11-12 | 2020-02-07 | 陕西聚能新创煤化科技有限公司 | Recovery method and recovery system of fusel ethanol in methanol rectification process |
| CN111116317A (en) * | 2019-12-31 | 2020-05-08 | 天津市创举科技股份有限公司 | Five-tower four-effect methanol rectification process and equipment |
| CN113087597A (en) * | 2021-03-22 | 2021-07-09 | 国家能源集团宁夏煤业有限责任公司 | Method for rectifying methanol and methanol rectifying system |
| CN113527058A (en) * | 2021-08-18 | 2021-10-22 | 天津大学 | Side-line and bulkhead pre-rectifying tower heat trap multi-effect methanol rectifying method |
| CN113620783A (en) * | 2021-08-18 | 2021-11-09 | 天津大学 | Reverse-forward mixed five-tower three-effect methanol rectification method using pre-rectifying tower as hot hydrazine |
Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1817836A (en) * | 2006-03-10 | 2006-08-16 | 天津大学 | Double-efficient energy-saving and water-saving rectifying system and process for methanol |
| CN101012150A (en) * | 2007-02-07 | 2007-08-08 | 浙江大学 | A method for refining synthetic methanol with heat integration |
| CN101503337A (en) * | 2009-03-19 | 2009-08-12 | 蓝仁水 | Technological process for methanol distillation by using fiver-tower heat integration apparatus |
| CN102039058A (en) * | 2010-11-26 | 2011-05-04 | 天津大学 | Large-scale methanol multi-effect energy-saving rectifying device and process |
| CN107032959A (en) * | 2017-05-16 | 2017-08-11 | 华陆工程科技有限责任公司 | A kind of heat pump and the methanol rectification method of multiple-effect coupling |
| CN109438185A (en) * | 2018-09-04 | 2019-03-08 | 北洋国家精馏技术工程发展有限公司 | A kind of vacuum thermal coupling methanol rectification method and device |
| CN109646980A (en) * | 2018-11-13 | 2019-04-19 | 天津大学 | Without the tower-coupled methanol multi-effect distillation energy saver in fusel oil next door and method |
-
2019
- 2019-05-28 CN CN201910453840.6A patent/CN110143850A/en active Pending
Patent Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1817836A (en) * | 2006-03-10 | 2006-08-16 | 天津大学 | Double-efficient energy-saving and water-saving rectifying system and process for methanol |
| CN101012150A (en) * | 2007-02-07 | 2007-08-08 | 浙江大学 | A method for refining synthetic methanol with heat integration |
| CN101503337A (en) * | 2009-03-19 | 2009-08-12 | 蓝仁水 | Technological process for methanol distillation by using fiver-tower heat integration apparatus |
| CN102039058A (en) * | 2010-11-26 | 2011-05-04 | 天津大学 | Large-scale methanol multi-effect energy-saving rectifying device and process |
| CN107032959A (en) * | 2017-05-16 | 2017-08-11 | 华陆工程科技有限责任公司 | A kind of heat pump and the methanol rectification method of multiple-effect coupling |
| CN109438185A (en) * | 2018-09-04 | 2019-03-08 | 北洋国家精馏技术工程发展有限公司 | A kind of vacuum thermal coupling methanol rectification method and device |
| CN109646980A (en) * | 2018-11-13 | 2019-04-19 | 天津大学 | Without the tower-coupled methanol multi-effect distillation energy saver in fusel oil next door and method |
Non-Patent Citations (5)
| Title |
|---|
| 刘保柱等: "节能型甲醇精馏工艺研究", 《化工进展》 * |
| 崔国星等: "甲醇变压逆流双效精馏系统工艺模拟与优化", 《吉林化工学院学报》 * |
| 张君涛等: "具有热集成的甲醇多效精馏新工艺及其模拟", 《化学工程》 * |
| 臧楠: ""甲醇精馏工艺模拟计算与优化"", 《中国优秀博硕士学位论文全文数据库(硕士)工程科技Ⅰ辑》 * |
| 范文元: "《化工单元操作节能技术》", 2000 * |
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110759812A (en) * | 2019-11-12 | 2020-02-07 | 陕西聚能新创煤化科技有限公司 | Recovery method and recovery system of fusel ethanol in methanol rectification process |
| CN110759812B (en) * | 2019-11-12 | 2023-12-05 | 陕西聚能新创煤化科技有限公司 | Recovery method and recovery system for ethanol miscellaneous alcohol in methanol rectification process |
| CN111116317A (en) * | 2019-12-31 | 2020-05-08 | 天津市创举科技股份有限公司 | Five-tower four-effect methanol rectification process and equipment |
| CN113087597A (en) * | 2021-03-22 | 2021-07-09 | 国家能源集团宁夏煤业有限责任公司 | Method for rectifying methanol and methanol rectifying system |
| CN113527058A (en) * | 2021-08-18 | 2021-10-22 | 天津大学 | Side-line and bulkhead pre-rectifying tower heat trap multi-effect methanol rectifying method |
| CN113620783A (en) * | 2021-08-18 | 2021-11-09 | 天津大学 | Reverse-forward mixed five-tower three-effect methanol rectification method using pre-rectifying tower as hot hydrazine |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN110143850A (en) | Single-column steam-driven energy-saving methanol multi-effect rectification method without by-product fusel oil | |
| CN101570466B (en) | Multi-effect rectifying process of methanol | |
| CN1817835A (en) | Double-efficient energy-saving methanol rectifying apparatus and method | |
| CN1328232C (en) | Double-efficient energy-saving and water-saving rectifying system and process for methanol | |
| CN111792685B (en) | System and method for continuously recycling NMP from NMP wastewater | |
| CN108101748B (en) | Four-tower three-effect methanol rectification energy-saving process method and device | |
| CN1317248C (en) | Methanol double-effect rectification energy-saving equipment and method | |
| CN110404285B (en) | Four-tower distillation and membrane separation integrated system and method for distilling ethanol | |
| CN106075947A (en) | Methanol four tower double-effect heat pump energy-saving equipment and method | |
| CN111437619A (en) | Multi-tower differential pressure energy-saving anhydrous alcohol distillation system and anhydrous alcohol energy-saving production method | |
| CN104151135A (en) | Molassess raw material top-grade alcohol distillation and waste liquid concentration thermal coupling device and process | |
| CN109438185B (en) | Vacuum thermal coupling methanol rectification method and device | |
| CN109646980B (en) | Energy-saving device and method for fusel oil-free dividing wall column coupled with methanol multi-effect rectification | |
| CN113233960B (en) | Multi-effect methanol rectification process method and device for avoiding ethanol accumulation | |
| CN110483249A (en) | A kind of six tower quadruple effect rectificating method of single column steam drive type methanol of not by-product fusel oil | |
| CN107488104B (en) | An energy-saving rectification system and an energy-saving rectification method for purifying fusel oil | |
| CN219323881U (en) | Five tower four effect refining plant of crude methyl alcohol | |
| CN210117345U (en) | Four-tower four-effect crude methanol refining process system | |
| CN111821821A (en) | Device and method for recycling fusel oil in methanol production | |
| CN103706136A (en) | Double-rectifying-tower series separation and purification method for recovery of methyl tert-butyl ether-tetrahydrofuran in waste liquid in statins synthesis process | |
| CN215906119U (en) | Multi-effect methanol rectification process method device for avoiding ethanol accumulation | |
| CN216366648U (en) | MVR combines with recovery tower to be used for device that weak alcohol retrieved | |
| CN205099600U (en) | Fuel ethanol purification system | |
| CN103130227A (en) | Production device and production method for trichlorosilane full thermal coupling integration multi-effect distillation | |
| CN113634004A (en) | Six-tower reverse four-effect methanol rectification method with pre-rectifying tower as heat source |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| RJ01 | Rejection of invention patent application after publication | ||
| RJ01 | Rejection of invention patent application after publication |
Application publication date: 20190820 |