焦油萘

Tar naphthalene

從煤焦油中分離出來的萘稱之為焦油萘在高溫煤焦油中萘約占8-12%從焦油精餾塔側線切取出溫度區間為210-230℃的萘油餾分經過洗滌脫酚再精餾分離輕組分便可得到凝固點為78℃純度為96%的工業萘

The naphthalene separated from coal tar is called tar naphthalene. In high-temperature coal tar, naphthalene accounts for about 8-12%. The naphthalene oil fraction with a temperature range of 210-230 ℃ is cut from the side line of the tar distillation tower. After washing, dephenolization, and distillation to separate the light components, industrial naphthalene with a solidification point of 78 ℃ and a purity of 96% can be obtained

工業萘中含雜質硫茚（1-3%）甲基萘（1-2%）及少量茚焦油堿和焦油酸經過進一步酸洗和蒸餾可得到硫含量小于0.1%凝固點為79℃的精萘若需要進一步精制使硫含量低于0.05%則需采用加氫精制工藝

Industrial naphthalene contains impurities such as sulfur indene (1-3%) and methyl naphthalene (1-2%), as well as a small amount of indene tar alkali and tar acid. After further acid washing and distillation, refined naphthalene with sulfur content less than 0.1% and a solidification point of 79 ℃ can be obtained. If further refinement is needed to make the sulfur content less than 0.05%, the hydrogenation refining process is required

用工業萘小批量生產精萘的流程如下將硫酸加入熔融的萘中脫水攪拌后靜置分離廢酸再加入98%的硫酸在85-95℃條件下攪拌40分鐘靜置分離廢酸在攪拌下加入37%的甲醛溶液在85-95℃條件下攪拌50分鐘加溫水攪拌后靜置分層聚合物及磺化物料用10%氫氧化鈉溶液中和PH到7-8靜置后除去廢堿蒸餾冷卻可得到精萘產品

The process for producing refined naphthalene in small batches using industrial naphthalene is as follows: 1. Add sulfuric acid to molten naphthalene, dehydrate it, stir it, and then let it stand to separate the waste acid. 2. Add 98% sulfuric acid and stir it at 85-95 ℃ for 40 minutes. 3. Let it stand to separate the waste acid. 3. Add 37% formaldehyde solution and stir it at 85-95 ℃ for 50 minutes. 4. Stir with warm water and let it stand. 3. Layer the polymer and sulfonated material. 4. Neutralize the pH to 7-8 ℃ with a 10% sodium hydroxide solution. After standing, remove the waste alkali and distill and cool it to obtain refined naphthalene. Product:

石油萘

Petroleum naphthalene

石油萘的原料來自于催化重整催化裂化和烴類裂解等過程的重芳烴組分在催化重整油中甲基萘的含量約為55%首先經過萃取和吸附從原料餾分中分離出萘的各種同系物然后采用催化臨氫脫烷基的方法以Cr2O3-Al2O3為催化劑在400-800℃和0.5-7兆帕下進行臨氫脫甲基反應反應產物經冷卻氣相物質后蒸餾除去輕組分苯甲苯二甲苯等后進一步精餾可得到石油萘產品產品用溶劑吸收和溶劑洗滌的方法進行提純純度可達99.73%

The raw material of petroleum naphthalene comes from the heavy aromatic components of catalytic reforming, catalytic cracking, and hydrocarbon cracking processes. The content of methyl naphthalene in catalytic reforming oil is about 55%. Firstly, various homologous compounds of naphthalene are separated from the raw material fraction through extraction and adsorption. Then, catalytic hydrogenation dealkylation is carried out using Cr2O3-Al2O3 as the catalyst at 400-800 ℃ and 0.5-7 MPa. The reaction product is cooled by gas-phase substances. After further distillation to remove light components such as benzene, toluene, xylene, etc., petroleum naphthalene products can be obtained. The products are purified using solvent absorption and solvent washing methods, with a purity of up to 99.73%

據估計以輕柴油為裂解原料的年產30萬噸的乙烯裝置可副產焦油9萬噸其中萘和萘潛量為4-5萬噸

It is estimated that an ethylene plant with an annual production of 300000 tons using light diesel as cracking raw material can produce 90000 tons of tar as a byproduct, with a potential of 40000 to 50000 tons of naphthalene and naphthalene

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