CN114774161B - A polygeneration comprehensive utilization system and treatment technology for residual oil treatment of biomass volatile matter - Google Patents
A polygeneration comprehensive utilization system and treatment technology for residual oil treatment of biomass volatile matter Download PDFInfo
- Publication number
- CN114774161B CN114774161B CN202210214656.8A CN202210214656A CN114774161B CN 114774161 B CN114774161 B CN 114774161B CN 202210214656 A CN202210214656 A CN 202210214656A CN 114774161 B CN114774161 B CN 114774161B
- Authority
- CN
- China
- Prior art keywords
- tower
- oil
- distillation tower
- fuel oil
- raw material
- 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.)
- Active
Links
- 239000002028 Biomass Substances 0.000 title claims abstract description 76
- 238000005516 engineering process Methods 0.000 title description 3
- 238000004821 distillation Methods 0.000 claims abstract description 81
- 239000003921 oil Substances 0.000 claims abstract description 79
- 239000000295 fuel oil Substances 0.000 claims abstract description 70
- 239000002994 raw material Substances 0.000 claims abstract description 69
- 238000000197 pyrolysis Methods 0.000 claims abstract description 47
- 230000008016 vaporization Effects 0.000 claims abstract description 43
- 238000009834 vaporization Methods 0.000 claims abstract description 41
- 238000002485 combustion reaction Methods 0.000 claims abstract description 33
- 239000006227 byproduct Substances 0.000 claims abstract description 18
- 238000000034 method Methods 0.000 claims abstract description 15
- 230000008569 process Effects 0.000 claims abstract description 9
- 239000003039 volatile agent Substances 0.000 claims abstract description 6
- 238000000605 extraction Methods 0.000 claims abstract 2
- 239000000047 product Substances 0.000 claims description 62
- 238000005292 vacuum distillation Methods 0.000 claims description 61
- 238000010438 heat treatment Methods 0.000 claims description 44
- 238000010992 reflux Methods 0.000 claims description 15
- 238000002309 gasification Methods 0.000 claims description 12
- 239000000446 fuel Substances 0.000 claims description 6
- 239000000463 material Substances 0.000 claims description 5
- 238000005194 fractionation Methods 0.000 claims description 3
- 238000012545 processing Methods 0.000 claims description 3
- 238000007599 discharging Methods 0.000 claims 15
- 230000006837 decompression Effects 0.000 claims 4
- 238000010079 rubber tapping Methods 0.000 claims 2
- 238000004519 manufacturing process Methods 0.000 description 14
- 239000000571 coke Substances 0.000 description 7
- 239000000126 substance Substances 0.000 description 7
- 239000002956 ash Substances 0.000 description 6
- 239000007791 liquid phase Substances 0.000 description 5
- 238000012546 transfer Methods 0.000 description 5
- 239000004566 building material Substances 0.000 description 4
- 238000006243 chemical reaction Methods 0.000 description 4
- 238000003912 environmental pollution Methods 0.000 description 4
- 238000005984 hydrogenation reaction Methods 0.000 description 3
- 238000012986 modification Methods 0.000 description 3
- 230000004048 modification Effects 0.000 description 3
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 2
- 230000008901 benefit Effects 0.000 description 2
- 239000010882 bottom ash Substances 0.000 description 2
- 239000011449 brick Substances 0.000 description 2
- 229910052799 carbon Inorganic materials 0.000 description 2
- 239000004568 cement Substances 0.000 description 2
- 230000008878 coupling Effects 0.000 description 2
- 238000010168 coupling process Methods 0.000 description 2
- 238000005859 coupling reaction Methods 0.000 description 2
- 238000011161 development Methods 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 239000010881 fly ash Substances 0.000 description 2
- 239000012535 impurity Substances 0.000 description 2
- 239000004005 microsphere Substances 0.000 description 2
- 239000002910 solid waste Substances 0.000 description 2
- -1 that is Substances 0.000 description 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 2
- 241001474374 Blennius Species 0.000 description 1
- 241000209140 Triticum Species 0.000 description 1
- 235000021307 Triticum Nutrition 0.000 description 1
- 239000011280 coal tar Substances 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 239000010813 municipal solid waste Substances 0.000 description 1
- 238000011017 operating method Methods 0.000 description 1
- 239000010902 straw Substances 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G53/00—Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more refining processes
- C10G53/02—Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more refining processes plural serial stages only
- C10G53/04—Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more refining processes plural serial stages only including at least one extraction step
Landscapes
- Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
Description
技术领域Technical field
本发明涉及生物质资源综合利用技术领域，具体涉及一种生物质挥发分处理渣油的多联产综合利用系统及处理工艺。The invention relates to the technical field of comprehensive utilization of biomass resources, and specifically relates to a polygeneration comprehensive utilization system and processing technology for treating residual oil with biomass volatile components.
背景技术Background technique
随着我国经济的发展和人民生活水平的改善，人们越来越认识到对环境和不可再生能源保护的重要性。近些年来各工厂的渣油产量也越来越多，因此如何处理重质原料油和产生的渣油，也是现代化城市管理中的一个重要课题。With the development of our country's economy and the improvement of people's living standards, people are increasingly aware of the importance of environmental and non-renewable energy protection. In recent years, various factories have produced more and more residual oil. Therefore, how to deal with heavy raw oil and the generated residual oil is also an important issue in modern urban management.
当今社会，生物质的来源很多，但都没有进行合理的开发和利用，很多都直接以焚烧或填埋的方式进行处理，并没有将其有效利用。目前还没有类似的用生物质挥发分处理渣油的方案。In today's society, there are many sources of biomass, but they have not been developed and utilized rationally. Many of them are directly disposed of by incineration or landfill, and they are not effectively utilized. There is currently no similar solution for using biomass volatiles to treat residual oil.
专利CN112843764A公开了一种具有卫星式塔釜的减压精馏塔以及常压渣油的减压精馏方法，非常具有时代前沿的发展意义，但卫星实现较为复杂，同时其中没有运用生物质等物质的再次利用；专利CN106753553A公开了一种渣油/煤焦油轻质化生产碳微球的装置及方法，里面也运用了加氢的方法，使其收率进行了提高，并生产我国急需的碳微球，但也没有与生物质相结合。此外，上述专利对于能量与热量耦合部分未见报道。Patent CN112843764A discloses a vacuum distillation tower with a satellite tower and a vacuum distillation method of atmospheric pressure residue oil. It has very cutting-edge development significance, but the satellite implementation is relatively complicated, and biomass, etc. are not used. Reuse of substances; Patent CN106753553A discloses a device and method for lightweighting residual oil/coal tar to produce carbon microspheres. The hydrogenation method is also used to increase the yield and produce the products urgently needed in our country. Carbon microspheres, but also not combined with biomass. In addition, the above-mentioned patents do not report on the coupling part of energy and heat.
发明内容Contents of the invention
本发明的目的就是为了克服上述现有技术存在的缺陷而提供一种可以同时将生物质与渣油进行能量与热量再次利用的生物质挥发分处理渣油的多联产综合利用系统及处理工艺。The purpose of the present invention is to overcome the above-mentioned shortcomings of the prior art and provide a polygeneration comprehensive utilization system and processing technology for biomass volatile matter treatment of residual oil that can simultaneously reuse energy and heat of biomass and residual oil. .
本发明的目的可以通过以下技术方案来实现：The object of the present invention can be achieved through the following technical solutions:
一种生物质挥发分处理渣油的多联产综合利用系统，该系统包括：A polygeneration comprehensive utilization system for biomass volatile matter treatment residual oil, the system includes:
燃料油主产出单元，用于将重质原料油中的燃料油提取；The main fuel oil production unit is used to extract fuel oil from heavy feed oil;
汽化单元，用于将重质原料油中的轻组分和重组分进行汽化处理；The vaporization unit is used to vaporize the light components and heavy components in the heavy feed oil;
燃料油副产出单元，用于将重质原料油中重组分中的燃料油提取；Fuel oil by-product unit is used to extract fuel oil from heavy components in heavy feed oil;
生物质热解单元，用于向系统中提供挥发分；Biomass pyrolysis unit, used to provide volatile matter to the system;
所述的汽化单元与燃料油主产出单元交叠于初馏塔；所述的汽化单元与燃料油副产出单元交叠于减压精馏塔；The vaporization unit and the fuel oil main production unit overlap in the primary distillation tower; the vaporization unit and the fuel oil secondary production unit overlap in the vacuum distillation tower;
所述的生物质热解单元与汽化单元交叠于减压精馏塔和初馏塔；所述的生物质热解单元与燃料油副产出单元交叠于减压精馏塔和燃烧炉；所述的生物质热解单元与燃料油主产出单元交叠于装置原料罐和初馏塔。The biomass pyrolysis unit and the vaporization unit overlap in the vacuum distillation tower and the initial distillation tower; the biomass pyrolysis unit and the fuel oil by-product unit overlap in the vacuum distillation tower and the combustion furnace. ; The biomass pyrolysis unit and the main fuel oil production unit overlap in the device raw material tank and primary distillation tower.
进一步地，所述的燃料油主产出单元包括依次连接的：Further, the fuel oil main production unit includes: connected in sequence:
装置原料罐，用于对重质原料油进行预热；装置原料罐设有出口，从罐底部放去水和少量杂质；The raw material tank is installed to preheat heavy raw oil; the raw material tank is equipped with an outlet to drain water and a small amount of impurities from the bottom of the tank;
初馏塔，用于对重质原料油进行分馏；Primary distillation tower, used for fractionating heavy feed oil;
主成品收集罐，用于对分馏提取出的一线燃料油进行收集；The main product collection tank is used to collect the first-line fuel oil extracted by fractionation;
所述的初馏塔分别通过塔顶出料管a和塔底出料管c与汽化单元相连，初馏塔通过侧线出料管b与主成品收集罐相连；The preliminary distillation tower is connected to the vaporization unit through the top discharge pipe a and the tower bottom discharge pipe c respectively, and the preliminary distillation tower is connected to the main finished product collection tank through the side discharge pipe b;
所述的侧线出料管上还设有与初馏塔连接的回流管道。The side discharge pipe is also provided with a reflux pipe connected to the primary distillation tower.
进一步地，所述的燃料油主产出单元还包括用于存储重质原料油的罐区原料罐，所述的罐区原料罐和装置原料罐之间设有输送泵，所述的装置原料罐和初馏塔之间设有换热器组；Furthermore, the main fuel oil production unit also includes a tank area raw material tank for storing heavy raw oil. A transfer pump is provided between the tank area raw material tank and the device raw material tank. The device raw material tank There is a heat exchanger group between the tank and the primary distillation tower;
所述的换热器组包括相互并联的二线换热器、三线换热器和塔底换热器，所述的塔底换热器包括相互串联的塔底初换热器和塔底再换热器。The heat exchanger group includes a parallel second-line heat exchanger, a third-line heat exchanger and a tower bottom heat exchanger. The tower bottom heat exchanger includes a tower bottom primary heat exchanger and a tower bottom re-heat exchanger that are connected in series. Heater.
进一步地，所述的汽化单元包括加热汽化炉、初馏塔和减压精馏塔；Further, the vaporization unit includes a heating vaporization furnace, a primary distillation tower and a vacuum rectification tower;
所述的初馏塔分别通过塔顶出料管a和塔底出料管c与加热汽化炉相连，所述的加热汽化炉与减压精馏塔相连，所述的减压精馏塔通过塔顶出料管A与塔顶出料管a相连；The initial distillation tower is connected to the heating vaporization furnace through the top discharge pipe a and the tower bottom discharge pipe c. The heating vaporization furnace is connected to the vacuum rectification tower. The vacuum rectification tower passes through The discharge pipe A at the top of the tower is connected to the discharge pipe a at the top of the tower;
所述的塔顶出料管a上还设有第一主冷凝器，所述的塔顶出料管A上还设有第二冷凝器。The top discharge pipe A is also provided with a first main condenser, and the top discharge pipe A is also provided with a second condenser.
进一步地，所述的燃料油副产出单元包括减压精馏塔、成品收集罐区和燃烧炉；Further, the fuel oil by-product unit includes a vacuum distillation tower, a finished product collection tank area and a combustion furnace;
所述的成品收集罐区包括第一副成品收集罐、第二副成品收集罐和第三副成品收集罐；所述的减压精馏塔通过第一侧线出料管B1与第一副成品收集罐相连，减压精馏塔通过第二侧线出料管B2与第二副成品收集罐相连，减压精馏塔通过第三侧线出料管B3与第三副成品收集罐相连；The finished product collection tank area includes a first auxiliary product collection tank, a second auxiliary product collection tank and a third auxiliary product collection tank; the vacuum rectification tower communicates with the first auxiliary product through the first side discharge pipe B 1 The finished product collection tank is connected, the vacuum distillation tower is connected to the second auxiliary product collection tank through the second side discharge pipe B 2 , and the vacuum rectification tower is connected to the third auxiliary product collection tank through the third side discharge pipe B 3 ;
所述的减压精馏塔通过塔底出料管C与燃烧炉相连；The vacuum distillation tower is connected to the combustion furnace through the discharge pipe C at the bottom of the tower;
所述的第一侧线出料管B1上还设有第一副冷凝器，所述的第二侧线出料管B2上还设有第二副冷凝器，所述的第三侧线出料管B3上还设有第三副冷凝器。The first side line discharge pipe B1 is also provided with a first auxiliary condenser, the second side line discharge pipe B2 is also provided with a second auxiliary condenser, and the third side line discharge pipe B2 is also provided with a second auxiliary condenser. Pipe B 3 is also provided with a third auxiliary condenser.
进一步地，所述的第一侧线出料管B1和/或第二侧线出料管B2与装置原料罐之间进行换热连接；所述的第一侧线出料管B1和/或第二侧线出料管B2上设有与减压精馏塔相连的回流管道。Further, the first side line discharge pipe B 1 and/or the second side line discharge pipe B 2 are heat exchange connected with the device raw material tank; the first side line discharge pipe B 1 and/or The second side discharge pipe B 2 is provided with a reflux pipe connected to the vacuum distillation tower.
进一步地，所述的生物质热解单元包括装置原料罐、初馏塔、生物质热解反应器、燃烧炉和减压精馏塔；Further, the biomass pyrolysis unit includes a device raw material tank, a primary distillation tower, a biomass pyrolysis reactor, a combustion furnace and a vacuum distillation tower;
所述的燃烧炉分别与生物质热解反应器和装置原料罐换热连接；所述的生物质热解反应器的出料口分别与减压精馏塔、初馏塔和燃烧炉相连，生物质热解反应器与装置原料罐换热连接。The combustion furnace is connected to the biomass pyrolysis reactor and the device raw material tank for heat exchange respectively; the discharge port of the biomass pyrolysis reactor is connected to the vacuum distillation tower, the initial distillation tower and the combustion furnace respectively. The biomass pyrolysis reactor is heat exchange connected with the raw material tank of the device.
一种基于如上所述生物质挥发分处理渣油的多联产综合利用系统的处理工艺，该处理工艺包括以下步骤：A treatment process based on a polygeneration comprehensive utilization system for biomass volatile treatment residual oil as described above. The treatment process includes the following steps:
(a)将罐区原料罐中的重质原料油由输送泵送入装置原料罐，在装置原料罐中被加热；(a) The heavy raw oil in the raw material tank in the tank area is sent to the device raw material tank by the transfer pump, and is heated in the device raw material tank;
(b)重质原料油经由换热器组，回收热量后，进入初馏塔中减压蒸馏；(b) The heavy feed oil passes through the heat exchanger group, recovers heat, and then enters the primary distillation tower for vacuum distillation;
(c)初馏塔中减压蒸馏的馏分分别进入到主成品收集罐和加热汽化炉，经加热汽化炉加热后进入减压精馏塔(c) The fractions distilled under reduced pressure in the initial distillation tower enter the main finished product collection tank and the heating vaporization furnace respectively. After being heated by the heating vaporization furnace, they enter the vacuum rectification tower.
(d)减压精馏塔中减压蒸馏的馏分分别进入到成品收集罐区、燃烧炉和加热汽化炉中；(d) The fractions distilled under vacuum in the vacuum distillation tower enter the finished product collection tank area, combustion furnace and heating vaporization furnace respectively;
(e)生物质热解反应器中产生的挥发分进入到减压精馏塔和初馏塔中，生物质热解后产生的挥发分中的小分子物质可提高各线产油的C/H原子比，提高产油的质量；同时产生的热量与装置原料罐中进行换热，将重质原料油进行加热，实现对热量的再次利用。(e) The volatile components produced in the biomass pyrolysis reactor enter the vacuum distillation tower and the primary distillation tower. The small molecular substances in the volatile components produced after biomass pyrolysis can increase the C/C of the oil produced in each line. The H atomic ratio improves the quality of the oil produced; at the same time, the heat generated is exchanged with the raw material tank of the device to heat the heavy raw oil to realize the reuse of heat.
进一步地，步骤(c)具体为：Further, step (c) is specifically:
初馏塔塔顶的馏分经第一主冷凝器冷凝后收集，及时送入加热汽化炉中作为燃料燃烧；The fraction at the top of the primary distillation tower is collected after being condensed by the first main condenser, and is promptly sent to the heating gasification furnace for combustion as fuel;
初馏塔的侧线馏分为一线燃料油，一部分用回流泵打回初馏塔，用来控制初馏塔温度，一部分进入主成品收集罐，作为产品出售；The side stream of the primary distillation tower is a first-line fuel oil, part of which is pumped back to the primary distillation tower by a reflux pump to control the temperature of the primary distillation tower, and part of which enters the main finished product collection tank and is sold as a product;
初馏塔中剩余物料进入加热汽化炉中加热，经加热汽化炉加热后进入减压精馏塔；The remaining materials in the primary distillation tower enter the heating vaporization furnace for heating, and then enter the vacuum rectification tower after being heated by the heating vaporization furnace;
步骤(d)具体为：Step (d) is specifically as follows:
减压精馏塔塔顶馏分经第二冷凝器冷却后送至加热汽化炉作燃料；The overhead fraction of the vacuum distillation tower is cooled by the second condenser and then sent to the heating gasification furnace as fuel;
减压精馏塔第一侧线馏分为一线燃料油，经第一副冷凝器冷却后送至第一副成品收集罐，作为产品出售。The first side stream of the vacuum distillation tower is the first-line fuel oil, which is cooled by the first auxiliary condenser and sent to the first auxiliary finished product collection tank for sale as a product.
减压精馏塔第二侧线馏分为二线燃料油，经与装置原料罐换热后，再经第二副冷凝器冷却后，一部分用回流泵打回减压精馏塔，用来控制精馏塔侧线温度；一部分经泵送至成品第二副成品收集罐，作为产品出售；The second side stream of the vacuum distillation tower is the second-line fuel oil. After exchanging heat with the raw material tank of the device, and then being cooled by the second auxiliary condenser, part of it is pumped back to the vacuum distillation tower using a reflux pump to control the distillation. Tower side line temperature; part of it is pumped to the second collection tank of finished products and sold as products;
减压精馏塔第三侧线馏分为三线燃料油，经与装置原料罐换热后，经第三副冷凝器冷却后，一部分用回流泵打回至减压精馏塔，用来控制精馏塔侧线温度，一部分进入第三副成品收集罐，作为产品出售；The third side line fraction of the vacuum distillation tower is the third line fuel oil. After exchanging heat with the raw material tank of the device and being cooled by the third auxiliary condenser, part of it is pumped back to the vacuum distillation tower using a reflux pump to control the distillation. A part of the tower side line temperature enters the third secondary product collection tank and is sold as product;
减压精馏塔塔底馏分为减压渣油，即重油，进入到燃烧炉中与生物质热解反应器中产生的半焦一同燃烧，为生物质热解反应器提供热量，实现热量循环，此外，所述减压精馏塔塔底的馏分可以通过燃烧炉重新利用，也可以通过冷凝器冷却后作为商品油卖出，两种方法都可行。The bottom fraction of the vacuum distillation tower is vacuum residual oil, that is, heavy oil, which enters the combustion furnace and is burned with the semi-coke produced in the biomass pyrolysis reactor to provide heat for the biomass pyrolysis reactor and realize heat circulation. , In addition, the fraction at the bottom of the vacuum distillation tower can be reused through the combustion furnace, or can be sold as commercial oil after cooling through the condenser. Both methods are feasible.
进一步地，所述装置原料罐中加热的温度为65-75℃，静置1.5-2.5h；Further, the heating temperature in the raw material tank of the device is 65-75°C and left to stand for 1.5-2.5 hours;
所述初馏塔的塔顶馏分为45-55℃的混合油气，初馏塔的侧线馏分为145-155℃的一线燃料油；所述加热汽化炉的加热温度为375-385℃；The top fraction of the primary distillation tower is mixed oil and gas at 45-55°C, and the side fraction of the primary distillation tower is first-line fuel oil at 145-155°C; the heating temperature of the heating gasification furnace is 375-385°C;
所述减压精馏塔的塔顶馏分为45-55℃的混合油气，减压精馏塔的第一侧线馏分为145-155℃的一线燃料油，减压精馏塔的第二侧线馏分为液相温度235-255℃的二线燃料油，减压精馏塔的第三侧线馏分为液相温度315-325℃的三线燃料油，减压精馏塔的塔底馏分为355-365℃的减压渣油；The overhead fraction of the vacuum distillation tower is mixed oil and gas at 45-55°C, the first side fraction of the vacuum distillation tower is first-line fuel oil at 145-155°C, and the second side fraction of the vacuum distillation tower is It is a second-line fuel oil with a liquid phase temperature of 235-255°C. The third side fraction of the vacuum distillation tower is a third-line fuel oil with a liquid phase temperature of 315-325°C. The bottom fraction of the vacuum distillation tower is 355-365°C. of vacuum residue oil;
所述燃烧炉的运行温度为850-900℃。以有效控制NOx的生成排放，且有利于保持灰渣的活性，使得燃烧后的灰渣中底灰和飞灰含量小于2％，可以直接作为建材原料，进而通过作为建材原料制作砖块、水泥等高附加值产品以得到充分利用，从而实现了半焦、灰分的资源化利用，且有效减少了环境污染。The operating temperature of the combustion furnace is 850-900°C. In order to effectively control the generation and emission of NOx, and to maintain the activity of the ash, the content of bottom ash and fly ash in the burned ash is less than 2%, which can be directly used as building material raw materials, and then used as building material raw materials to make bricks and cement. Such high value-added products can be fully utilized, thereby realizing the resource utilization of semi-coke and ash, and effectively reducing environmental pollution.
与现有技术相比，本发明具有以下优点：Compared with the prior art, the present invention has the following advantages:
(1)本发明将重质原料油送入精馏塔中，经过与两次精馏，可以得到所需的一线、二线和三线油，同时从精馏塔出来的油都可再次进行热量交换，与原料区进行换热，减少了装置原料区出的热量输入，对热量进行了大范围的回收，符合当下能源利用的热潮；(1) In the present invention, the heavy raw material oil is fed into the distillation tower. After two distillations, the required first-line, second-line and third-line oils can be obtained. At the same time, the oil coming out of the distillation tower can be exchanged for heat again. , exchange heat with the raw material area, reducing the heat input from the raw material area of the device, and recovering heat on a large scale, which is in line with the current energy utilization boom;
(2)本发明在精馏塔前加入了生物质热解反应器，生物质热解产生的挥发分带有大量的热量与小分子物质，利用生物质的挥发分，类似于加氢反应，分两路去往精馏塔与装置原料管，使得初馏塔与减压精馏塔中的商品油质量大大提高，同时也使渣油在整个能量与热量循环中处于重要的位置，完成了热量的闭环。(2) The present invention adds a biomass pyrolysis reactor in front of the distillation tower. The volatile components produced by biomass pyrolysis contain a large amount of heat and small molecular substances. Utilizing the volatile components of biomass is similar to a hydrogenation reaction. It is divided into two paths to the distillation tower and the equipment raw material pipe, which greatly improves the quality of the commercial oil in the primary distillation tower and vacuum distillation tower. At the same time, it also puts the residual oil in an important position in the entire energy and heat cycle, completing the Closed loop of heat.
(3)本发明在反应过程中，关于生物质的选择可以是多样性的，该反应和系统对原料的适应性广，且综合利用程度高。当下社会生物质的再次利用也是研究者们讨论的热点，本系统中的生物质热解反应器中的原料可多样选择，适用于海藻、小麦秸秆、湿垃圾等其他生物质的综合利用；(3) In the reaction process of the present invention, the selection of biomass can be diverse. The reaction and system have wide adaptability to raw materials and have a high degree of comprehensive utilization. The reuse of biomass in current society is also a hot topic discussed by researchers. The raw materials in the biomass pyrolysis reactor in this system can be selected from a variety of sources, and is suitable for the comprehensive utilization of other biomass such as seaweed, wheat straw, and wet garbage;
(4)本发明生物质挥发分中所含有的小分子物质，可以提高整个系统中的精馏产油率，同时也避免了固体废弃物(半焦和渣油)对环境的污染问题，最终同时实现生物质与渣油的洁净、高效利用。(4) The small molecular substances contained in the biomass volatiles of the present invention can improve the distillation oil production rate in the entire system, and at the same time avoid the environmental pollution problems of solid waste (semi-coke and residual oil). Ultimately, At the same time, the clean and efficient utilization of biomass and residual oil is achieved.
附图说明Description of the drawings
图1为本发明的综合利用系统示意图；Figure 1 is a schematic diagram of the comprehensive utilization system of the present invention;
图中标号所示：罐区原料罐1、输送泵2、装置原料罐3、二线换热器4、三线换热器5、塔底初换热器6和塔底再换热器7、初馏塔8、第一主冷凝器9、主成品收集罐10、加热汽化炉11、生物质热解反应器12、燃烧炉13、减压精馏塔14、第二冷凝器15、第一副冷凝器16、第二副冷凝器17、第三副冷凝器18、第一副成品收集罐19、第二副成品收集罐20、第三副成品收集罐21。The numbers in the figure show: tank area raw material tank 1, transfer pump 2, device raw material tank 3, second-line heat exchanger 4, third-line heat exchanger 5, tower bottom primary heat exchanger 6 and tower bottom reheat exchanger 7, primary Distillation tower 8, first main condenser 9, main finished product collection tank 10, heating gasification furnace 11, biomass pyrolysis reactor 12, combustion furnace 13, vacuum distillation tower 14, second condenser 15, first deputy Condenser 16, second auxiliary condenser 17, third auxiliary condenser 18, first auxiliary product collection tank 19, second auxiliary product collection tank 20, and third auxiliary product collection tank 21.
具体实施方式Detailed ways
下面结合附图和具体实施例对本发明进行详细说明。本实施例在以本发明技术方案为前提下进行实施，给出了详细的实施方式和具体的操作过程，但本发明的保护范围不限于下述的实施例。The present invention will be described in detail below with reference to the accompanying drawings and specific embodiments. This embodiment is implemented on the premise of the technical solution of the present invention, and detailed implementation modes and specific operating procedures are given. However, the protection scope of the present invention is not limited to the following embodiments.
实施例Example
一种生物质挥发分处理渣油的多联产综合利用系统，参考图1，该系统包括：A polygeneration comprehensive utilization system for biomass volatile matter treatment residual oil. Refer to Figure 1. The system includes:
燃料油主产出单元，用于将重质原料油中的燃料油提取；The main fuel oil production unit is used to extract fuel oil from heavy feed oil;
汽化单元，用于将重质原料油中的轻组分和重组分进行汽化处理；The vaporization unit is used to vaporize the light components and heavy components in the heavy feed oil;
燃料油副产出单元，用于将重质原料油中重组分中的燃料油提取；Fuel oil by-product unit is used to extract fuel oil from heavy components in heavy feed oil;
生物质热解单元，用于向系统中提供挥发分；Biomass pyrolysis unit, used to provide volatile matter to the system;
汽化单元与燃料油主产出单元交叠于初馏塔8；汽化单元与燃料油副产出单元交叠于减压精馏塔14；The vaporization unit and the fuel oil main production unit overlap in the primary distillation tower 8; the vaporization unit and the fuel oil secondary production unit overlap in the vacuum distillation tower 14;
生物质热解单元与汽化单元交叠于减压精馏塔14和初馏塔8；生物质热解单元与燃料油副产出单元交叠于减压精馏塔14和燃烧炉13；生物质热解单元与燃料油主产出单元交叠于装置原料罐3和初馏塔8。The biomass pyrolysis unit and the vaporization unit overlap in the vacuum distillation tower 14 and the primary distillation tower 8; the biomass pyrolysis unit and the fuel oil by-product unit overlap in the vacuum distillation tower 14 and the combustion furnace 13; The material pyrolysis unit and the main fuel oil production unit overlap in the raw material tank 3 and the primary distillation tower 8 of the device.
燃料油主产出单元包括依次连接的：装置原料罐3，用于对重质原料油进行预热；装置原料罐3设有出口，从罐底部放去水和少量杂质；初馏塔8，用于对重质原料油进行分馏；主成品收集罐10，用于对分馏提取出的一线燃料油进行收集；初馏塔8分别通过塔顶出料管a和塔底出料管c与汽化单元相连，初馏塔8通过侧线出料管b与主成品收集罐10相连；侧线出料管上还设有与初馏塔8连接的回流管道。The main fuel oil output unit includes: device raw material tank 3, which is connected in sequence, for preheating heavy raw oil; device raw material tank 3 is provided with an outlet to discharge water and a small amount of impurities from the bottom of the tank; primary distillation tower 8, It is used to fractionate heavy raw oil; the main product collection tank 10 is used to collect the first-line fuel oil extracted by fractionation; the primary distillation tower 8 is connected to the vaporization through the top discharge pipe a and the bottom discharge pipe c respectively. The units are connected, and the primary distillation tower 8 is connected to the main finished product collection tank 10 through the side discharge pipe b; the side discharge pipe is also provided with a reflux pipe connected to the preliminary distillation tower 8.
燃料油主产出单元还包括用于存储重质原料油的罐区原料罐1，罐区原料罐1和装置原料罐3之间设有输送泵2，装置原料罐3和初馏塔8之间设有换热器组；换热器组包括相互并联的二线换热器4、三线换热器5和塔底换热器，塔底换热器包括相互串联的塔底初换热器6和塔底再换热器7。The main fuel oil production unit also includes a tank area raw material tank 1 for storing heavy raw oil. A transfer pump 2 is provided between the tank area raw material tank 1 and the device raw material tank 3. Between the device raw material tank 3 and the primary distillation tower 8 There is a heat exchanger group in between; the heat exchanger group includes a parallel second-line heat exchanger 4, a third-line heat exchanger 5 and a tower bottom heat exchanger. The tower bottom heat exchanger includes a series-connected primary heat exchanger 6 at the bottom of the tower. and tower bottom reheat exchanger 7.
汽化单元包括加热汽化炉11、初馏塔8和减压精馏塔14；初馏塔8分别通过塔顶出料管a和塔底出料管c与加热汽化炉11相连，加热汽化炉11与减压精馏塔14相连，减压精馏塔14通过塔顶出料管A与塔顶出料管a相连；塔顶出料管a上还设有第一主冷凝器9，塔顶出料管A上还设有第二冷凝器15。The vaporization unit includes a heating vaporization furnace 11, a preliminary distillation tower 8 and a vacuum rectification tower 14; the preliminary distillation tower 8 is connected to the heating vaporization furnace 11 through the tower top discharge pipe a and the tower bottom discharge pipe c respectively. The heating vaporization furnace 11 It is connected to the vacuum distillation tower 14. The vacuum distillation tower 14 is connected to the tower top discharge pipe a through the tower top discharge pipe A; the tower top discharge pipe a is also provided with a first main condenser 9. The discharge pipe A is also provided with a second condenser 15.
燃料油副产出单元包括减压精馏塔14、成品收集罐区和燃烧炉13；成品收集罐区包括第一副成品收集罐19、第二副成品收集罐20和第三副成品收集罐21；减压精馏塔14通过第一侧线出料管B1与第一副成品收集罐19相连，减压精馏塔14通过第二侧线出料管B2与第二副成品收集罐20相连，减压精馏塔14通过第三侧线出料管B3与第三副成品收集罐21相连；减压精馏塔14通过塔底出料管C与燃烧炉13相连；第一侧线出料管B1上还设有第一副冷凝器16，第二侧线出料管B2上还设有第二副冷凝器17，第三侧线出料管B3上还设有第三副冷凝器18。第一侧线出料管B1和/或第二侧线出料管B2与装置原料罐3之间进行换热连接；第一侧线出料管B1和/或第二侧线出料管B2上设有与减压精馏塔14相连的回流管道。The fuel oil by-product unit includes a vacuum distillation tower 14, a finished product collection tank area and a combustion furnace 13; the finished product collection tank area includes a first by-product collection tank 19, a second by-product collection tank 20 and a third by-product collection tank 21; The vacuum rectification tower 14 is connected to the first auxiliary product collection tank 19 through the first side discharge pipe B 1 , and the vacuum rectification tower 14 is connected to the second auxiliary product collection tank 20 through the second side discharge pipe B 2 connected, the vacuum distillation tower 14 is connected to the third by-product collection tank 21 through the third side outlet pipe B 3 ; the vacuum distillation tower 14 is connected to the combustion furnace 13 through the bottom outlet pipe C; the first side outlet The material pipe B 1 is also provided with a first auxiliary condenser 16, the second side line discharge pipe B 2 is also provided with a second auxiliary condenser 17, and the third side line discharge pipe B 3 is also provided with a third auxiliary condenser Device 18. The first side line discharge pipe B 1 and/or the second side line discharge pipe B 2 are heat exchange connected with the device raw material tank 3; the first side line discharge pipe B 1 and/or the second side line discharge pipe B 2 There is a reflux pipeline connected to the vacuum distillation tower 14.
生物质热解单元包括装置原料罐3、初馏塔8、生物质热解反应器12、燃烧炉13和减压精馏塔14；燃烧炉13分别与生物质热解反应器12和装置原料罐3换热连接；生物质热解反应器12的出料口分别与减压精馏塔14、初馏塔8和燃烧炉13相连，生物质热解反应器12与装置原料罐3换热连接。The biomass pyrolysis unit includes a device raw material tank 3, a preliminary distillation tower 8, a biomass pyrolysis reactor 12, a combustion furnace 13 and a vacuum distillation tower 14; the combustion furnace 13 is connected to the biomass pyrolysis reactor 12 and device raw materials respectively. The tank 3 is connected for heat exchange; the outlet of the biomass pyrolysis reactor 12 is connected to the vacuum distillation tower 14, the primary distillation tower 8 and the combustion furnace 13 respectively, and the biomass pyrolysis reactor 12 exchanges heat with the device raw material tank 3 connect.
一种基于如上生物质挥发分处理渣油的多联产综合利用系统的处理工艺，该处理工艺包括以下步骤：A treatment process based on the above polygeneration comprehensive utilization system for treating residual oil with biomass volatiles. The treatment process includes the following steps:
(a)将罐区原料罐1中的重质原料油由输送泵2送入装置原料罐3，在装置原料罐3中被加热；装置原料罐3中加热的温度为70℃，静置2h；(a) The heavy raw oil in the raw material tank 1 of the tank area is sent to the device raw material tank 3 by the transfer pump 2, and is heated in the device raw material tank 3; the heating temperature in the device raw material tank 3 is 70°C and left to stand for 2 hours. ;
(b)重质原料油经由换热器组，回收热量后，进入初馏塔8中减压蒸馏；(b) The heavy feed oil passes through the heat exchanger group, recovers heat, and then enters the primary distillation tower 8 for vacuum distillation;
(c)初馏塔8中减压蒸馏的馏分分别进入到主成品收集罐10和加热汽化炉11，经加热汽化炉11加热后进入减压精馏塔14；(c) The fractions distilled under reduced pressure in the initial distillation tower 8 enter the main finished product collection tank 10 and the heating vaporization furnace 11 respectively. After being heated by the heating vaporization furnace 11, they enter the vacuum rectification tower 14;
具体为：初馏塔8塔顶的馏分经第一主冷凝器9冷凝后收集，及时送入加热汽化炉11中作为燃料燃烧；Specifically: the fraction at the top of the primary distillation tower 8 is collected after being condensed by the first main condenser 9, and is promptly sent to the heating gasification furnace 11 for combustion as fuel;
初馏塔8的侧线馏分为一线燃料油，一部分用回流泵打回初馏塔8，用来控制初馏塔温度，一部分进入主成品收集罐10，作为产品出售；The side stream of the primary distillation tower 8 is a first-line fuel oil, part of which is returned to the primary distillation tower 8 with a reflux pump to control the temperature of the primary distillation tower, and part of which enters the main finished product collection tank 10 and is sold as a product;
初馏塔8中剩余物料进入加热汽化炉11中加热，经加热汽化炉11加热后进入减压精馏塔14；The remaining materials in the primary distillation tower 8 enter the heating vaporization furnace 11 for heating. After being heated by the heating vaporization furnace 11, they enter the vacuum distillation tower 14;
初馏塔8的塔顶馏分为50℃的混合油气，初馏塔8的侧线馏分为150℃的一线燃料油；加热汽化炉11的加热温度为380℃；The top fraction of the primary distillation tower 8 is mixed oil and gas at 50°C, and the side fraction of the primary distillation tower 8 is first-line fuel oil at 150°C; the heating temperature of the heating gasification furnace 11 is 380°C;
(d)减压精馏塔14中减压蒸馏的馏分分别进入到成品收集罐区、燃烧炉13和加热汽化炉11中；(d) The fractions distilled under reduced pressure in the vacuum distillation tower 14 enter the finished product collection tank area, the combustion furnace 13 and the heating vaporization furnace 11 respectively;
步骤(d)具体为：减压精馏塔14塔顶馏分经第二冷凝器15冷却后送至加热汽化炉11作燃料；Step (d) is specifically: the overhead fraction of the vacuum distillation tower 14 is cooled by the second condenser 15 and then sent to the heating gasification furnace 11 as fuel;
减压精馏塔14第一侧线馏分为一线燃料油，经第一副冷凝器16冷却后送至第一副成品收集罐19，作为产品出售。The first side stream of the vacuum distillation tower 14 is the first-line fuel oil, which is cooled by the first auxiliary condenser 16 and then sent to the first auxiliary product collection tank 19 for sale as a product.
减压精馏塔14第二侧线馏分为二线燃料油，经与装置原料罐3换热后，再经第二副冷凝器17冷却后，一部分用回流泵打回减压精馏塔14，用来控制精馏塔侧线温度；一部分经泵送至成品第二副成品收集罐20，作为产品出售；The second side fraction of the vacuum distillation tower 14 is the second-line fuel oil. After exchanging heat with the device raw material tank 3, and then being cooled by the second auxiliary condenser 17, part of it is pumped back to the vacuum distillation tower 14 with a reflux pump. to control the temperature of the side line of the distillation tower; part of it is pumped to the finished product and second auxiliary product collection tank 20 for sale as a product;
减压精馏塔14第三侧线馏分为三线燃料油，经与装置原料罐3换热后，经第三副冷凝器18冷却后，一部分用回流泵打回至减压精馏塔14，用来控制精馏塔侧线温度，一部分进入第三副成品收集罐21，作为产品出售；The third side line fraction of the vacuum distillation tower 14 is the third line fuel oil. After exchanging heat with the device raw material tank 3 and being cooled by the third auxiliary condenser 18, part of it is pumped back to the vacuum distillation tower 14 with a reflux pump. To control the temperature of the side line of the distillation tower, part of it enters the third by-product collection tank 21 and is sold as a product;
减压精馏塔14塔底馏分为减压渣油，即重油，进入到燃烧炉13中与生物质热解反应器12中产生的半焦一同燃烧，为生物质热解反应器12提供热量，实现热量循环，此外，减压精馏塔14塔底的馏分可以通过燃烧炉13重新利用，也可以通过冷凝器冷却后作为商品油卖出，两种方法都可行；The bottom fraction of the vacuum distillation tower 14 is vacuum residue oil, that is, heavy oil, which enters the combustion furnace 13 and is burned with the semi-coke produced in the biomass pyrolysis reactor 12 to provide heat for the biomass pyrolysis reactor 12 , to achieve heat circulation. In addition, the fraction at the bottom of the vacuum distillation tower 14 can be reused through the combustion furnace 13, or can be cooled through the condenser and sold as commercial oil. Both methods are feasible;
燃烧炉13的运行温度为850-900℃。以有效控制NOx的生成排放，且有利于保持灰渣的活性，使得燃烧后的灰渣中底灰和飞灰含量小于2％，可以直接作为建材原料，进而通过作为建材原料制作砖块、水泥等高附加值产品以得到充分利用，从而实现了半焦、灰分的资源化利用，且有效减少了环境污染。The operating temperature of the combustion furnace 13 is 850-900°C. In order to effectively control the generation and emission of NOx, and to maintain the activity of the ash, the content of bottom ash and fly ash in the burned ash is less than 2%, which can be directly used as building material raw materials, and then used as building material raw materials to make bricks and cement. Such high value-added products can be fully utilized, thereby realizing the resource utilization of semi-coke and ash, and effectively reducing environmental pollution.
减压精馏塔14的塔顶馏分为50℃的混合油气，减压精馏塔14的第一侧线馏分为150℃的一线燃料油，减压精馏塔14的第二侧线馏分为液相温度240℃的二线燃料油，减压精馏塔14的第三侧线馏分为液相温度320℃的三线燃料油，减压精馏塔14的塔底馏分为360℃的减压渣油。The overhead fraction of the vacuum distillation tower 14 is mixed oil and gas at 50°C, the first side fraction of the vacuum distillation tower 14 is the first-line fuel oil at 150°C, and the second side fraction of the vacuum distillation tower 14 is the liquid phase. Second-line fuel oil with a temperature of 240°C, third-line fuel oil with a liquid phase temperature of 320°C, and vacuum residue oil with a liquid phase temperature of 360°C.
(e)生物质热解反应器12中产生的挥发分进入到减压精馏塔14和初馏塔8中，生物质热解后产生的挥发分中的小分子物质可提高各线产油的C/H原子比，提高产油的质量；同时产生的热量与装置原料罐3中进行换热，将重质原料油进行加热，实现对热量的再次利用。(e) The volatile components generated in the biomass pyrolysis reactor 12 enter the vacuum distillation tower 14 and the primary distillation tower 8. The small molecular substances in the volatile components generated after biomass pyrolysis can increase the oil production of each line. The C/H atomic ratio improves the quality of the oil produced; at the same time, the heat generated is exchanged with the raw material tank 3 of the device to heat the heavy raw oil, thereby realizing the reuse of heat.
综上，本发明的主要技术点在于在精馏塔前加入了生物质热解反应器12，生物质热解产生的挥发分带有大量的热量与小分子物质，利用生物质的挥发分，类似于加氢反应，使得初馏塔8与减压精馏塔14中的商品油质量大大提高，同时也使渣油在整个能量与热量循环中处于重要的位置，完成了热量的闭环。在反应过程中，关于生物质的选择可以是多样性的，该反应和系统对原料的适应性广，且综合利用程度高。生物质挥发分中所含有的小分子物质，可以提高整个系统中的精馏产油率，同时也避免了固体废弃物(半焦和渣油)对环境的污染问题，综合考虑了资源、环境与社会经济效益，实现了生物质与渣油的科学利用。To sum up, the main technical point of the present invention is to add a biomass pyrolysis reactor 12 in front of the distillation tower. The volatile matter produced by biomass pyrolysis contains a large amount of heat and small molecular substances. Using the volatile matter of biomass, Similar to the hydrogenation reaction, the quality of the commercial oil in the primary distillation tower 8 and the vacuum distillation tower 14 is greatly improved. At the same time, the residual oil plays an important position in the entire energy and heat cycle, completing the closed loop of heat. During the reaction process, the selection of biomass can be diverse. The reaction and system have wide adaptability to raw materials and a high degree of comprehensive utilization. The small molecular substances contained in biomass volatiles can improve the distillation oil production rate in the entire system, and at the same time avoid the environmental pollution problems of solid waste (semi-coke and residual oil), taking into account the comprehensive consideration of resources and environment. and social and economic benefits, realizing the scientific utilization of biomass and residual oil.
本发明将整个环节设计成为闭环，无需外界提供热量，自给自足，完成了整个系统的循环。本发明将生物质、重质原料油、渣油等有机结合，实现生物质能量的科学、高效、综合利用。生物质热解产生的半焦还可以继续燃烧提供热量，实现热量的耦合。The invention designs the entire link into a closed loop, does not require external heat, is self-sufficient, and completes the cycle of the entire system. The invention organically combines biomass, heavy raw material oil, residual oil, etc. to achieve scientific, efficient and comprehensive utilization of biomass energy. The semi-coke produced by biomass pyrolysis can continue to be burned to provide heat to achieve heat coupling.
以上所述，仅是本发明的较佳实施例而已，并非是对本发明作其它形式的限制，任何熟悉本专业的技术人员可能利用上述揭示的技术内容加以变更或改型为等同变化的等效实施例。但是凡是未脱离本发明技术方案内容，依据本发明的技术实质对以上实施例所作的任何简单修改、等同变化与改型，仍属于本发明技术方案的保护范围。The above are only preferred embodiments of the present invention, and are not intended to limit the present invention in other forms. Any skilled person familiar with the art may make changes or modifications to equivalent changes using the technical contents disclosed above. Example. However, any simple modifications, equivalent changes and modifications made to the above embodiments based on the technical essence of the present invention without departing from the content of the technical solution of the present invention still fall within the protection scope of the technical solution of the present invention.
Claims (4)
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202210214656.8A CN114774161B (en) | 2022-03-07 | 2022-03-07 | A polygeneration comprehensive utilization system and treatment technology for residual oil treatment of biomass volatile matter |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202210214656.8A CN114774161B (en) | 2022-03-07 | 2022-03-07 | A polygeneration comprehensive utilization system and treatment technology for residual oil treatment of biomass volatile matter |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN114774161A CN114774161A (en) | 2022-07-22 |
| CN114774161B true CN114774161B (en) | 2024-02-02 |
Family
ID=82423303
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202210214656.8A Active CN114774161B (en) | 2022-03-07 | 2022-03-07 | A polygeneration comprehensive utilization system and treatment technology for residual oil treatment of biomass volatile matter |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN114774161B (en) |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102041023A (en) * | 2009-10-16 | 2011-05-04 | 中国石油化工股份有限公司 | Method for improving residual oil hydrogenation by blending biological grease |
| CN106833736A (en) * | 2017-03-29 | 2017-06-13 | 山东铂铠环保科技有限公司 | A kind of method of waste oil regeneration base oil |
| CN109337703A (en) * | 2018-11-07 | 2019-02-15 | 山东理工大学 | A Biomass Continuous On-Line Catalytic Preparation of High-Quality Oil-Gas Integrated Device |
Family Cites Families (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2012092468A1 (en) * | 2010-12-30 | 2012-07-05 | Kior Inc. | Production of renewable biofuels |
| US20150073188A1 (en) * | 2012-03-01 | 2015-03-12 | The Trustees Of Princeton University | Processes for producing synthetic hydrocarbons from coal, biomass, and natural gas |
-
2022
- 2022-03-07 CN CN202210214656.8A patent/CN114774161B/en active Active
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102041023A (en) * | 2009-10-16 | 2011-05-04 | 中国石油化工股份有限公司 | Method for improving residual oil hydrogenation by blending biological grease |
| CN106833736A (en) * | 2017-03-29 | 2017-06-13 | 山东铂铠环保科技有限公司 | A kind of method of waste oil regeneration base oil |
| CN109337703A (en) * | 2018-11-07 | 2019-02-15 | 山东理工大学 | A Biomass Continuous On-Line Catalytic Preparation of High-Quality Oil-Gas Integrated Device |
Non-Patent Citations (1)
| Title |
|---|
| 我国催化裂化能量回收机组的发展;吴文伟, 张涌, 凌之光;炼油设计(01);全文 * |
Also Published As
| Publication number | Publication date |
|---|---|
| CN114774161A (en) | 2022-07-22 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN101624531B (en) | Device for preparing bio-oil by utilizing biomass spouted fluidized bed through pyrolysis and fractional condensation | |
| CN101457147B (en) | No-oxygen pyrolysis gasification processing device of urban domestic garbage and technique thereof | |
| CN102031133B (en) | Device and method for producing biological fuel oil by quickly cracking biomass | |
| CN101531910A (en) | System for rapidly pyrolysing and liquefying biomass | |
| CN108017109B (en) | A method for recycling BDO waste liquid | |
| CN105152863B (en) | Method for recovering ethylene glycol and acetaldehyde from polyester wastewater | |
| CN114774161B (en) | A polygeneration comprehensive utilization system and treatment technology for residual oil treatment of biomass volatile matter | |
| CN109626784B (en) | An anti-clogging sludge continuous thermal hydrolysis system | |
| CN105602600A (en) | Kitchen garbage pyrolysis oil-preparation energy-saving treatment system | |
| CN102994127A (en) | Low-rank coal multi-stage fluidized bed coal chemical industry multiple production system and method | |
| CN211551605U (en) | Pyrolysis gas cooling system of pyrolysis furnace of thermal power plant | |
| CN105757674B (en) | The system and method for carbonaceous organic material thermal decomposition product heat energy utilization | |
| CN220098916U (en) | Organic solid waste pyrolysis recycling system utilizing cyclic heat carrier coupled carbon slag heat energy recovery | |
| CN112453018A (en) | Wet garbage poly-generation comprehensive utilization system and process | |
| CN107244948A (en) | A kind of system and method for domestic garbage pyrolysis compost treatment | |
| CN111704931A (en) | A combustible solid waste staged oxygen-enriched gasification synergistic treatment system | |
| CN114308981B (en) | Multi-generation comprehensive utilization system and treatment process for treating wet garbage by supercritical water | |
| CN110437856A (en) | A kind of combustible solid wastes by utilizing rapid pyrolysis method and device based on zeolite porous media and more physical chemistry fields | |
| CN110591765A (en) | RDF pyrolysis gas noncondensable gas clean system | |
| CN206316130U (en) | The system for handling house refuse | |
| CN205347174U (en) | Utilize plus sludge drying of living beings and processing apparatus that carbomorphism combined together | |
| CN212339251U (en) | Domestic waste and organic hazardous waste cooperative processing system | |
| CN211546415U (en) | Combustible solid waste fast pyrolysis device based on zeolite and multiple physical and chemical fields | |
| CN209890555U (en) | System for gardens rubbish utilization as a resource | |
| CN210601548U (en) | Medium-low temperature pyrolysis coal gas heat recycling device |
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 | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant |