WO1995006682A1 - Procede et appareil de production d'essence et de gazole a partir de dechets plastiques - Google Patents
Procede et appareil de production d'essence et de gazole a partir de dechets plastiques Download PDFInfo
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- WO1995006682A1 WO1995006682A1 PCT/CN1994/000066 CN9400066W WO9506682A1 WO 1995006682 A1 WO1995006682 A1 WO 1995006682A1 CN 9400066 W CN9400066 W CN 9400066W WO 9506682 A1 WO9506682 A1 WO 9506682A1
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- kettle
- depolymerization
- kettle body
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- catalyst
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Classifications
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- 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
- C10G1/00—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
- C10G1/10—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal from rubber or rubber waste
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F02—COMBUSTION ENGINES; HOT-GAS OR COMBUSTION-PRODUCT ENGINE PLANTS
- F02B—INTERNAL-COMBUSTION PISTON ENGINES; COMBUSTION ENGINES IN GENERAL
- F02B3/00—Engines characterised by air compression and subsequent fuel addition
- F02B3/06—Engines characterised by air compression and subsequent fuel addition with compression ignition
Definitions
- the present invention relates to a method for extracting steam and diesel from waste plastic, and a device designed for implementing the method. More specifically, the technical field to which the present invention pertains is the production of alkane-rich hydrocarbon oil fuels from polyolefin waste plastics, namely polypropylene, poly-Lene, polyphenylene-Lene, polybutene, and the like. Oil can be widely used as industrial power fuel, and can also be used as civilian fuel.
- plastic waste With the widespread use of plastics in human life, plastic waste has increased. Agriculture, packaging, food, and supplies industries have increasingly used plastics as raw materials to process various products. Once they are used, they are discarded as waste, causing new pollution. They are called "white garbage", and they cannot disappear completely within a hundred years. How to deal with them is a matter of global concern. Many attempts have been made to convert unsaturated hydrocarbon polymers into fuels at home and abroad, but no optimal solution has been obtained, and it is difficult to form industrial scale production with economic benefits.
- the general method is to depolymerize waste plastic at high temperature, catalyze cracking and fractional distillation to obtain gasoline and diesel.
- High-temperature depolymerization is carried out in a depolymerization kettle. Generally, the depolymerization is carried out by placing waste plastic in the kettle and heating it at the bottom. At high temperatures, the waste plastic melts and depolymerizes. This type of depolymerization kettle is heated centrally at the bottom. The materials in the depolymerization kettle are heated unevenly, and the temperature at the bottom is too high to carbonize and coke the waste plastic.
- Japanese wipe-type clubs and new Japan-made iron wipe-type clubs disclosed on June 29, 1992 a "manufacturing aromatic hydrocarbon oil using thermally decomposed polyolefin plastics"Methods".
- This method is to collect the collected waste plastic and send it to the screw feeder to heat it up and then press it into the mixing tank to melt it with the thermal decomposition oil (kerosene, etc.) equivalent to 5 times the amount of plastic, and then pump it into another mixing tank.
- the first is the use of simple thermal cracking, which requires high depolymerization temperature, long time, and natural energy consumption; the second is that it is difficult to continue production; the third is that there is no reboiling, reflux, and blending process, and it is impossible to grasp the quality of the oil, which is completely natural Collect fuel.
- the temperature of the fractionation tower needs to be adjusted by a reboiler and the temperature is controlled by reflux; a variety of additives are needed to stop gasification to avoid excessive colloids and the induction period is too short; an octane enhancer is required Adjust gasoline, adjust oil stain with pour point depressant, and so on.
- the purpose of the present invention is to provide a more complete method to overcome the shortcomings of the previous methods and obtain the best results. That is, the cracking is accelerated at a lower temperature and pressure, and then catalytic reboiling and fractional purification are performed to obtain high-quality gasoline and diesel fuel for industrial power.
- Another object of the present invention is to provide a depolymerization kettle for simple dehydration, large heating area, uniform heating, and rapid temperature rise for the depolymerization process in the production of steam and diesel using waste plastics.
- the object of the present invention is achieved in the following manner.
- the present invention uses waste plastics such as polyene, polypropylene, polybenzene, etc. to extract steam and diesel. It is completed by the processes of high temperature depolymerization, catalytic cracking, and fractional purification.
- the high temperature depolymerization temperature is 350-550. . C;
- Catalytic cracking temperature is 300-380'C, using special catalytic cracking agent, JC-01 depolymerizing agent is added during depolymerization.
- a CH-02 catalyst In the catalytic cracking, a CH-02 catalyst is used, and the main component of the depolymerization agent JG-01 is A1 2 0 3 or alumina oxide, mica powder, etc .; the main component of the catalyst CH-02 is A1 2 0 3 or silicon aluminum. , Carbon sodium, high temperature binder (such as Gao Lu cement).
- the method of the invention is also suitable for converting waste oil and vegetable oil feet into gasoline and diesel.
- the conversion rate is more than 70%. This method is simple, practical, and effective in turning waste into treasure. Detailed description of the invention
- the depolymerizing agent mentioned here is a depolymerizing agent named JG-01.
- the JG-01 depolymerization agent is composed of 35-42% alumina, 40-45% silicon dioxide, and 6-7% mica powder. Its rhenium is 1% calcium oxide, 1% sodium gaseous, and 3%.
- a double-layer heating reactor is specially designed.
- This reactor (see Figure 1) is equipped with a cylindrical smoke-guiding heat pipe inside, so that the flue gas heat enters the pipe first to heat the material in the kettle. After that, the heat of the flue gas is conducted through the jacket of the outer layer of the reactor, and the heat of the flue gas heats the outer layer of the depolymerization kettle. In this way, the flue gas heat can be double-layered inside the kettle and then jacketed, which can maximize the use of thermal energy, achieve energy saving effects, and improve heat exchange speed.
- the depolymerization kettle includes a kettle body, a uniform material distribution tube, a cover plate for the top of the kettle body, a sewage pipe at the bottom of the kettle body, a uniformly-distributed heat conduction tube in the kettle body, and a molecular sieve partition on the material uniform distribution tube.
- a heavy oil refining feed tube In the middle of the kettle body, there is a heavy oil refining feed tube.
- the upper part of the kettle body shell has an upper support plate connected to the furnace body and the furnace.
- the lower part of the kettle shell has a lower support plate connected to the kettle body and the furnace. Gas exhaust pipe.
- the depolymerization kettle is installed on the heating furnace.
- the heating tube in the kettle communicates with the hearth of the heating furnace.
- the kettle shell between the furnace wall of the heating furnace and the upper and lower support plates of the kettle constitutes a heating sandwich. .
- the catalyst used in the catalysis is a special one, which is a strip-shaped or spherical particle, which is placed on a mesh-shaped partition in the reaction kettle.
- a container on the upper part of the reactor, and place the catalyst in it to allow gaseous products to pass through for catalysis.
- CH-02 used The chemical agent is composed of the following components: tri-aluminum or aluminum silicate 65- 71.3%, rare earth molecular sieve 15%, platinum 0.1-0.2%, nickel 0.5%, sodium carbonate 1 _3% , Adhesive (folded to dry matter) 5_ 10%.
- the catalyzed oil and gas enters the fractionation tower.
- part of the oil and gas enters the condenser through the side branch outlet at the middle and bottom of the fractionation and condenses into gas oil, diesel;
- the inflow to the bottom of the tower is re-boiled and heated up to about 350 ° C to re-evaporate, and then condensed into steam and diesel by the cooler and steam outlet through the cooler.
- the condensed oil is mixed into the mixing tank, and about 0.1-0.2% of the additives are added (commercially used gas refining agents, passivating agents, and pour point depressants), and then an octane number of about 10% is added.
- Promoter, chemical name is methyl tert-butyl ether (MTBE).
- Figure 1 is the depolymerization kettle of the present invention.
- 1 represents the kettle body
- 2 a material uniformly distributed tube
- 3 a heat transfer tube
- 4 a molecular sieve separator
- 5 a gas exhaust tube in the kettle
- 6 a reflux device.
- Cylinder, 7 gas exhaust pipe in the recirculator
- 8 recirculator condensate return pipe
- 9 the kettle is connected to the support plate on the furnace
- 10 heat-couple temperature measuring tube
- 11 thermocouple temperature measuring tube
- 12 sewage pipe
- 13 one manhole
- 14 safety valve
- 15 pressure gauge
- 16 temperature gauge
- 17 pot and bottom support plate
- 18 heatating furnace
- 19 hearth wall
- 20 sandwich, 21 _Fume exhaust pipe.
- the gas exhaust pipe (5) in the kettle of the depolymerization kettle is connected to the reflux body (6), and there is a reflux at the bottom of the reflux body (6).
- the condensate reflux pipe (8) is connected to the kettle (1) and refluxed
- the outer end of the material uniform distribution tube (2) is connected to a feeder such as an extruder.
- the entire depolymerization kettle is installed on the heating furnace (18), and is supported on the heating furnace by a lower support plate (17).
- a sandwich (21) is formed between the furnace wall (19) of the heating furnace and the shell of the kettle body (1).
- the flue gas discharge pipe (21) is connected to the equipment to be heated in the next process, such as a cracking kettle.
- FIG. 2 is a schematic diagram of the production device of the present invention.
- 1 represents the extruder; 2—depolymerization kettle; 3—sandwich flue; 4 flue inside a kettle; 5—return tower; 6—flue pipe connection; 7—catalytic cracking kettle; 8— The flue inside the kettle; 9 a sandwich flue; 10-partition; 11-catalyst; 12- smoke exhaust pipe; 13- gas exhaust pipe; 14-fractionating tower body; 15- condenser; 16- electric heating temperature regulator; 17—gas-liquid separator; 18—filler; 19—heating furnace; 20—feeding port; 21—diesel output pipe; 22—gasoline output pipe; 23—non-condensable gas discharge pipe; 24—residual oil discharge pipe (and solution Poly kettle 2 is connected).
- the present invention will be further described with examples.
- the gas enters the fractionation column (14) through catalytic cracking, and the temperature of the entering column is controlled at 200-30CTC, and the tray is filled in the column.
- One or two diesel output pipes (21) are arranged at about one-half of the tower to let the diesel distill out, and the temperature here is about 210.
- At about C it is condensed by the condenser (15), and the collected liquid is diesel oil;
- 1-2 gasoline output pipes (22) are set at an appropriate distance from the tower section to let the gasoline distill.
- the temperature of this oil is about 140'C. It is condensed by the condenser (15), and the collected liquid is gasoline.
- the collected gasoline and diesel can also be processed by filtering and decoloring to make it more pure.
- the decolorizing filter may be activated carbon, activated clay, or the like.
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- Engineering & Computer Science (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Life Sciences & Earth Sciences (AREA)
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- General Chemical & Material Sciences (AREA)
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- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Description
用废旧塑料提取汽、柴油的方法和设备
发明背景
1.发明领域
本发明涉及用废 1曰塑料提取汽、柴油的方法以及为实施此方法所 设计的设备。 更具体地说,本发明所涉及的技术领域属于用聚烯烃类 废 1曰塑料即聚丙烯、聚 L烯、聚苯 L烯、聚丁烯等生产富含烷烃的烃油 燃料,这种烃油能广泛用作工业动力燃料,也可作民用燃料。
随着塑料在人类生活中广泛应用,塑料垃圾随之增多,农业、包装 业、食品业、曰用品工业等越来越多以塑料为原料加工各种产品。 它们 一经使用后便弃之为废物,造成了新的污染,被称为 "白色垃圾",它 们在儿百年内也不能完全消失。 如何将它们加以处理是全世界关注的 问题。将不饱和烃的高分子聚合物转化为燃料的方法,囯内外都做过 许多尝试,但都未能获得最佳方案,很难形成工业化的有经济效益的 规模生产。
2.现有技术
在此之前,国内外都有众多的科研部门和企业作过有益的探索,取 得了许多成果。 一般的方法是将废塑料高温解聚,催化裂解和分馏,从 而得到汽、柴油。高温解聚是在解聚釜内进行的,一般的解聚在釜是釜 内放入废塑料,在底部加热,在高温下,废塑料熔融解聚,这种解聚釜由 于在底部集中加热,使解聚釜内的物料受热不均匀,底部温度过高使废 塑料炭化、 结焦,要经常停炉清理,难以正常工作,并使废塑料转换为 汽、柴油的转化率降低。例如日本抹式会社、新日本制铁抹式会社(专利 申请公开号:特开平 4一 180995)于 1992年 6月 29 日公开了一种 "用热 分解聚烯烃类塑料制造芳香族糸烃油的方法"。这种方法是^收集的废 塑料粉碎送入螺旋送料机升温后压入混合槽中与予先投入的相当于塑 料 5倍的热分解油(煤油等)进行熔解,再泵入另一混合槽热分解; 将 气态生成物导入圆筒体雾化再通过固定床催化后冷却, 收集混合烃
油。 这是一种不能单独用于汽油或柴油动力的混合油,实用价值不高。 在中囯,于 1993年 10月 31 日公开了辽宁省普兰店市供销社运输公司 申请的"利用废旧塑料与合成纤维提炼燃油的方法 "专利(专利申请号 CN92102375. 8) o该方法是用废塑料予先装入反应釜内升温升压,密封 进行高温裂解,然后用水冷却降压,在常压下再升温气化蒸馏、分馏、 冷凝,根据不同温度收集不同温度点的馏份,得到汽油、柴油。
他们的成功处在于能将废塑裂解为烃油,其不足处 是显而易见 的。
一是采用单纯的热裂解,解聚温度要求高,时间长,自然能耗也多; 二是难以连续化生产;三是没有再沸和回流、调配过程,无法把握油料 的质量,完全是自然收集燃料。 须知,废旧塑料裂解后需要靠再沸器调 整分馏塔温度,并采用回流控制温度;需要使用多种添加剂昉止氣化避 免胶质过多发生和诱导期过短; 需要用辛烷值增进剂调整汽油,用降 凝剂调整染油,等等。
本发明的目的
本发明的目的在于提供一种较完善的方法以克服以前方法的不足 而取得最佳效果。即在较低温度与压力下加速裂解,尔后经催化再沸、 分馏精制而获得高质量的符合工业动力用的汽油、柴油。
本发明的另一目的是为用废塑料提取汽、柴油生产中的解聚过程 提供一种结枸简单、受热面积大、受热均匀、升温快的解聚釜。
本发明概述
本发明的目的是用以下方式来实现的。 本发明用废旧塑料即聚 烯、 聚丙烯、聚笨 烯等提取汽、柴油的方法,它由高温解聚、催化裂 解、和分馏精制的工艺过成完成, 高温解聚的温度为 350—550。C ; 催 化裂解温度为 300— 380'C,使用特殊的催化裂解剂,解聚过程中加入 JC-01解聚剂。催化裂解时使用 CH— 02催化剂,解聚剂 JG— 01的主 要組分为 A1203或氲氧化吕、云母粉等;催化剂 CH— 02的主要組分为 A1203或硅駿铝、碳駿钠、高温粘结剂(如高 吕水泥)。
本发明方法还适用于用废油、植物油脚转化为汽、柴油。 用本发明 的从废塑料、废油、废植物油脚提取汽、柴油的方法,其转化率达 70% 以上。 本方法 单、实用、变废为宝效益好。
本发明的详细叙述
本发明的技术方案是这样实现的:
首先将废旧塑料洗涤干净,并晒干或烘干,(最好粉碎成小片,小块 状),用挤塑机(或手工直接投入)将废塑料与解聚剂按比例混合在挤塑 机内,一般废塑料与解聚剂比例为 500: 1— 5,初步塑化后送入解聚釜 中进行熔化解聚。这里提到的解聚剂是被命名为 JG— 01的解聚剂。本 JG-01解聚剂是由 35— 42%二氧化二铝、 40— 45%二氣化硅、6— 7% 云母粉,其佘为 1 %氧化钙、 1 %氣化钠、 3%氧化钾、0. 5— 1 %的氡化 镁等組成,经在 150'C脱去吸附水,并在 350— 400'C下脱去结晶水后, 充分研磨、混合均匀而制得。为了加速熔解特别设计了一种双层加热反 应釜,这种反应釜(见附图 1)在内部设置了柱形导烟热管,让烟气热首 先进入该管让其对釜内物料加热。 尔后,烟气热再经反应釜外层夹套 导出,烟气热再对解聚釜外层加热。这样,烟气热先釜内后夹套双层,能 最大限度利用热能,达到节能效果,也提高热交换速度。
该解聚釜包括釜体、物料匀布管、釜体顶部的入孔盖板、釜体底部 的排污管、釜体内有均布的导热管,在物料匀布管之上有分子筛隔板, 在釜体中部有重质油回炼进料管,釜体外壳上部有釜体与炉膛连接上 支撑板,釜体外壳下部有釜体与炉膛连接下支撑板,在釜体项部有釜内 气体排气管。 使用时,将解聚釜安装在加热炉上,釜内的加热管与加热 炉的炉膛相通,加热炉的炉膛壁与釜体的上支撑板和下支撑板之间的 釜体外壳組成加热夹层。
当物料在解聚釜升温到 280— 550'C (优选 280— 360。C)时,塑料熔 化、解聚转化为气态生成物(油气)。 油气通过隔板上的催化剂进一步 催化裂解(也可以在及应釜外项部设置一独立的催化釜, ^催化剂置于 其中)。催化温度在 300— 380'C,(优逸 310—330。C )。为了防止在反应 釜中产生的泡沫,粉尘等杂质进入分馏糸统影响质量,特地设计了一 个回流器。 回流器的作用是阻档重組分和粉末等杂质进入分馏塔。 这 个设计是很重要的,否则,油质将受严重影响。
在催化时使用的催化剂是特制的,是条状或圆球状颗粒,它置于反 应釜中的带网眼状的隔板上。 当然也可以在反应釜上部设置一个容器 ^催化剂置于其中让气态生成物通过进行催化。所使用的 CH— 02催
化剂是由以下成份組成:三氣化二铝或硅酸吕 65- 71. 3%,稀土分子 筛 15 %,铂 0. 1 - 0. 2%,镍 0. 5%,碳酸钠 1 _3%,粘合剂(折为干物 质) 5_ 10%。将它们在 150匸脱去吸附水,再于 350— 40CTC下脱去结晶 水,研细,混合均匀而得。催化后的油气进入分馏塔中,这时受油气中组 分与输入塔内油气温度影响,一部份油气经分馏中部和底部的侧支线 出口进入冷凝器,冷凝为气油、 柴油; 一部分落入塔底流入再沸 被 升温到 350'C左右重新蒸发,再经汽、柴油出口经冷却器冷凝为汽、柴 油。冷凝油入调配罐,投入占油品重量 0. 1— 0. 2%左右的添加剂(市售 炼油用的抗氣剂、钝化剂、降凝剂),再加入 10%左右的辛烷值增进剂, 化学名称为甲基叔丁基醚 (MTBE)。 经过上述处理,油品质量符合商品 使用要求。
图 1为本发明的解聚釜,在图 1中, 1代表釜体, 2—物料匀布管, 3 一导热管, 4一分子筛隔板,5—釜内气体排出管, 6—回流器筒体, 7—回 流器内气体排出管, 8—回流器凝聚液回流管, 9一釜体与炉膛连接上 支撑板,10—重质油回炼进料管, 11一热电偶测温管, 12—排污管,13 一人孔,14—安全阀, 15—压力表, 16—温度表,17—釜体与炉膛下支 撑板, 18—加热炉, 19一炉膛壁, 20—夹层,21_烟气排出管。
本解聚釜的釜内气体排出管( 5)与回流器筒体 (6)连接,回流器筒 体( 6)底部有回流^凝聚液回流管(8)与釜体(1)连接,回流器筒体 (6)项部有回流器内气体排出管(7)。物料匀布管(2)底部有若干 cp6mm 的小孔便于物料均匀落入釜内,物料匀布管(2)的外端接加料机如挤 塑机。 整个解聚釜是安装在加热炉(18)上,由下支撑板(17)支撑在加 热炉上,加热炉的炉膛壁( 19)与釜体(1)外壳之间形成夹层(21),烟 气排出管(21 )与下道工序需加热的设备如裂解釜相连。
困 2为本发明的生产装置示意图。
在图 2中: 1代表挤塑机; 2—解聚釜;3—夹层烟道; 4一釜内烟道; 5—回流塔;6—烟道连接管;7—催化裂解釜; 8—釜内烟道; 9一夹层烟 道; 10—隔板; 11—催化剂;12—排烟管;13—气体排管; 14—分馏塔 体; 15—冷凝器; 16—电热温度调节器; 17—气液分离器; 18—填料;19 —加热炉; 20—加料口; 21—柴油输出管;22—汽油输出管;23—不凝气 排出管;24—渣油排出管(与解聚釜 2连通)。
现以实施例对本发明进行进一步说明。
实施例
1.取经清洗、干燥的聚 烯废料 1. 4吨加入加料口(20) ,启动挤塑 机(1),与此同时添加 0. 2%即 2. 8公斤的 JG— 01解聚剂,挤塑机(1) 将废塑料和解聚剂同时螺旋推进解聚釜(21)内;
2.将解聚釜(2)温度升至 280— 500。C ;
3.在催化裂解釜( 7)内放置制成果颗粒的 CH— 02催化剂约 100 公斤左右,经解聚釜(2)裂解的气休进入裂解釜(7)在 CH— 02催化剂 用下,大多数高分子裂解为 C2Q以下的小分子。此时气体保持温度控制 在 300— 380。C左右,如温度过高过低都应采取措施使温度保持在需要 范围内。
4. 气体经催化裂解进入分馏塔( 14),进塔温度控制在 200— 30CTC,并在塔内填充塔板。在塔的约二分之一处设 1一 2个柴油输出管 (21)让柴油馏出,此处温度约 210。C左右,经冷凝器( 15)冷凝,其收集 液即为柴油;在塔项部适当距离设 1—2个汽油输出管( 22),让汽油馏 出,此油温度约 140'C左右,经冷凝器(15)冷凝,其收集液即为汽油。
5.经收集的汽、 柴油还可以经过滤脱色等工序处理,使之更加纯 净。 脱色过滤剂可以是活性炭也可以是活性白土等。
Claims
1. 一种用废旧塑料即 烯、聚丙烯、聚苯 烯等提取汽油、柴油的方 法,它是由高温解聚、催化裂解和分馏精制的工艺过程完成,其特征是 解聚的温度在 350—550'C,催化裂解温度在 300— 380°。
2. 根据权利要求 1所述的方法,其特征在于使用了特制的解聚、催化 剂,在塑料投入解聚釜的同时投入 JG— 01解聚剂进行解聚,在催化釜 中投入 CH—02催化剂进行催化。
JG— 01解聚剂組成为:
三氣化二铝或氲氣化铝 35-42%
二氡化硅 40- 35%
云母粉 6—7 %
氧化镁 0. 5—1 %
氧化钾 3%
氣化钠 1 %
氡化钙 1 %
CH— 02催化剂組成为:
三氡化二吕
或硅駿吕 70%
稀土分子筛 15%
铂 0. 1— 0. 2%
镍 0. 5%
碳駿钠 1一 3 %
粘合剂(折为干物质) 5—10%
3. 根据权利要求 2的方法, 其特征在于解聚过程中加入 JG— 01解聚剂与塑料比例为 2— 10%。; CH- 02催化剂一次性投入 100公 斤左右(与生产蚬模有关, 此数为年产 1000T蚬模,可以反复再生使 用),并予先置于催化釜中。
4. 杈利要求 1的方法,其特征在于解聚温度为 280— 320' ( 。
5. 权利要求 1的方法,其特征在于催化裂解温度保持在 310'C至 330°C。
6. 一种解聚釜,包括釜体(1)、物料匀布管(2)、釜体(1)顶部的人孔盖 板(13)、釜体(1)底部的排污管(12),其特征在于这种解聚釜是采取在 釜内设置柱形或环形烟道对物料加热后经夹套层导出烟气热的方法, 釜体(1)内有均布的导热管(3),在物料匀布管(2)之上有分子筛隔板( 4),在釜体(1)中部有重质油回炼进管(10),釜体(1)外壳上部有釜体与 炉膛连接上支撑板( 9),釜体(1)外壳下部有釜体与炉膛连接下支撑板 (17),在釜体 (1)项部有釜内气体排气管(5)。
7. 根据权利要求 6所述的解聚釜,其特征在于釜内气体排气管(5) 与回流器筒体( 6)连接,回流器筒体(6)底部有回流器凝聚液回流管 (8)与釜体 (1)连接,回流器筒体 (6)项部有回流器内气体排出管(7)。
8. 根据权利要求 1或 2所述的解聚釜,其特征在于物料匀布管(2)底 部有若干 p6mm的小孔。
Priority Applications (1)
Application Number | Priority Date | Filing Date | Title |
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AU75298/94A AU7529894A (en) | 1993-08-28 | 1994-08-27 | A process for producing gasoline and diesel fuel oil from waste plastics and its apparatus |
Applications Claiming Priority (4)
Application Number | Priority Date | Filing Date | Title |
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CN93234583.2 | 1993-08-28 | ||
CN93111675A CN1099766A (zh) | 1993-08-28 | 1993-08-28 | 用废旧塑料提取汽、柴油的方法 |
CN93111675.9 | 1993-08-28 | ||
CN93234583U CN2172768Y (zh) | 1993-08-28 | 1993-08-28 | 用废塑料、废油、废植物油脚提取汽、柴油用的解聚釜 |
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WO1995006682A1 true WO1995006682A1 (fr) | 1995-03-09 |
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Application Number | Title | Priority Date | Filing Date |
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PCT/CN1994/000066 WO1995006682A1 (fr) | 1993-08-28 | 1994-08-27 | Procede et appareil de production d'essence et de gazole a partir de dechets plastiques |
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AU (1) | AU7529894A (zh) |
WO (1) | WO1995006682A1 (zh) |
Cited By (4)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
EP0702076A1 (en) * | 1994-09-13 | 1996-03-20 | Wartsila Diesel International Ltd. OY | A method for producing fuel for diesel engines from tyres or the like waste rubber material |
WO1997006224A1 (fr) * | 1995-08-08 | 1997-02-20 | Li Xing | Procede relatif a la fabrication d'essence, de carburant diesel et de noir de carbone a partir de dechets de caoutchouc et/ou de matieres plastiques |
US7285186B2 (en) | 2003-12-11 | 2007-10-23 | Zbigniew Tokarz | Transverse-flow catalytic reactor for conversion of waste plastic material and scrap rubber |
WO2020225219A1 (de) * | 2019-05-03 | 2020-11-12 | Biofabrik White Refinery Gmbh | Verfahren und vorrichtung zur verwertung von vorzugsweise polyolefinhaltigen kunststoffabfällen oder -resten |
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US4175211A (en) * | 1977-03-14 | 1979-11-20 | Mobil Oil Corporation | Method for treatment of rubber and plastic wastes |
US4851601A (en) * | 1988-01-19 | 1989-07-25 | Mobil Oil Corporation | Processing for producing hydrocarbon oils from plastic waste |
CN1042374A (zh) * | 1988-11-03 | 1990-05-23 | 马忠俊 | 废旧塑料提取可燃物的方法 |
CN1062918A (zh) * | 1991-01-04 | 1992-07-22 | 山西省永济县福利塑化总厂 | 废旧塑料生产石油产品的方法 |
CN1075328A (zh) * | 1992-02-12 | 1993-08-18 | 赵太平 | 废塑料连续生产石油产品的方法和设备 |
-
1994
- 1994-08-27 AU AU75298/94A patent/AU7529894A/en not_active Abandoned
- 1994-08-27 WO PCT/CN1994/000066 patent/WO1995006682A1/zh active Application Filing
Patent Citations (5)
Publication number | Priority date | Publication date | Assignee | Title |
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US4175211A (en) * | 1977-03-14 | 1979-11-20 | Mobil Oil Corporation | Method for treatment of rubber and plastic wastes |
US4851601A (en) * | 1988-01-19 | 1989-07-25 | Mobil Oil Corporation | Processing for producing hydrocarbon oils from plastic waste |
CN1042374A (zh) * | 1988-11-03 | 1990-05-23 | 马忠俊 | 废旧塑料提取可燃物的方法 |
CN1062918A (zh) * | 1991-01-04 | 1992-07-22 | 山西省永济县福利塑化总厂 | 废旧塑料生产石油产品的方法 |
CN1075328A (zh) * | 1992-02-12 | 1993-08-18 | 赵太平 | 废塑料连续生产石油产品的方法和设备 |
Cited By (6)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
EP0702076A1 (en) * | 1994-09-13 | 1996-03-20 | Wartsila Diesel International Ltd. OY | A method for producing fuel for diesel engines from tyres or the like waste rubber material |
WO1997006224A1 (fr) * | 1995-08-08 | 1997-02-20 | Li Xing | Procede relatif a la fabrication d'essence, de carburant diesel et de noir de carbone a partir de dechets de caoutchouc et/ou de matieres plastiques |
US7285186B2 (en) | 2003-12-11 | 2007-10-23 | Zbigniew Tokarz | Transverse-flow catalytic reactor for conversion of waste plastic material and scrap rubber |
US7563345B2 (en) | 2003-12-11 | 2009-07-21 | Zbigniew Tokarz | Transverse-flow pyrocatalytic reactor for conversion of waste plastic material and scrap rubber |
US7977518B2 (en) | 2003-12-11 | 2011-07-12 | Zbigniew Tokarz | Transverse-flow pyrocatalytic reactor for conversion of waste plastic material and scrap rubber |
WO2020225219A1 (de) * | 2019-05-03 | 2020-11-12 | Biofabrik White Refinery Gmbh | Verfahren und vorrichtung zur verwertung von vorzugsweise polyolefinhaltigen kunststoffabfällen oder -resten |
Also Published As
Publication number | Publication date |
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AU7529894A (en) | 1995-03-22 |
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