石油与天然气化工
石油與天然氣化工
석유여천연기화공
CHEMICAL ENGINEERING OF OIL AND GAS
2013年
5期
534-539
,共6页
酸性水原料罐%污染治理%酸性水脱气罐%循环液缓冲罐%油封%H2S%氨
痠性水原料罐%汙染治理%痠性水脫氣罐%循環液緩遲罐%油封%H2S%氨
산성수원료관%오염치리%산성수탈기관%순배액완충관%유봉%H2S%안
sour water feed tanks%pollution treatment%sour water degassing drum%tempera-ture%pressure%recycle liquid surge drum%oil seal%H2 S%ammonia
提供了一种对酸性水原料罐排放气污染进行综合治理的方法。该法不同于以往的吸附法、吸收法或冷凝法，而是根据酸性水汽提装置的工艺特点，通过改变工艺流程和操作条件，最大限度地降低酸性水原料罐中易挥发组分的浓度，实现污染治理。主要措施包括：①将酸性水脱气罐操作压力降低到0．05～0．10 M Pa；②用汽提塔塔底净化水的低温余热将进酸性水脱气罐的酸性水加热至55～60℃，使酸性水脱气罐在较高的操作温度下操作；③将单塔汽提中的一、二、三级分凝液或双塔汽提中的氨汽提塔塔顶回流罐的液相返回物流送入一个循环液缓冲罐中，然后用泵升压并送至酸性水原料泵出口的酸性水管线上；④将酸性水原料罐中油层厚度适当增加至600～900 mm ，形成油封，以有效地阻止H2 S等恶臭气体组分从酸性水原料罐中逃逸等。上述措施实施后，酸性水原料罐在正常操作状态下无恶臭气体排出。该法具有不需要外部的吸附剂、吸收剂或冷冻剂，投资及运行费用低，操作简单，没有二次污染的优点。
提供瞭一種對痠性水原料罐排放氣汙染進行綜閤治理的方法。該法不同于以往的吸附法、吸收法或冷凝法，而是根據痠性水汽提裝置的工藝特點，通過改變工藝流程和操作條件，最大限度地降低痠性水原料罐中易揮髮組分的濃度，實現汙染治理。主要措施包括：①將痠性水脫氣罐操作壓力降低到0．05～0．10 M Pa；②用汽提塔塔底淨化水的低溫餘熱將進痠性水脫氣罐的痠性水加熱至55～60℃，使痠性水脫氣罐在較高的操作溫度下操作；③將單塔汽提中的一、二、三級分凝液或雙塔汽提中的氨汽提塔塔頂迴流罐的液相返迴物流送入一箇循環液緩遲罐中，然後用泵升壓併送至痠性水原料泵齣口的痠性水管線上；④將痠性水原料罐中油層厚度適噹增加至600～900 mm ，形成油封，以有效地阻止H2 S等噁臭氣體組分從痠性水原料罐中逃逸等。上述措施實施後，痠性水原料罐在正常操作狀態下無噁臭氣體排齣。該法具有不需要外部的吸附劑、吸收劑或冷凍劑，投資及運行費用低，操作簡單，沒有二次汙染的優點。
제공료일충대산성수원료관배방기오염진행종합치리적방법。해법불동우이왕적흡부법、흡수법혹냉응법，이시근거산성수기제장치적공예특점，통과개변공예류정화조작조건，최대한도지강저산성수원료관중역휘발조분적농도，실현오염치리。주요조시포괄：①장산성수탈기관조작압력강저도0．05～0．10 M Pa；②용기제탑탑저정화수적저온여열장진산성수탈기관적산성수가열지55～60℃，사산성수탈기관재교고적조작온도하조작；③장단탑기제중적일、이、삼급분응액혹쌍탑기제중적안기제탑탑정회류관적액상반회물류송입일개순배액완충관중，연후용빙승압병송지산성수원료빙출구적산성수관선상；④장산성수원료관중유층후도괄당증가지600～900 mm ，형성유봉，이유효지조지H2 S등악취기체조분종산성수원료관중도일등。상술조시실시후，산성수원료관재정상조작상태하무악취기체배출。해법구유불수요외부적흡부제、흡수제혹냉동제，투자급운행비용저，조작간단，몰유이차오염적우점。
This article provides a comprehensive treatment of the effluvial gas of sour water feed tanks .Different from normal treatment such as adsorption ,absorption or condensation ,and based on the process characteristics of sour water stripper ,this method decreases the volatile components content maximally by changing process flow and operating conditions . The main measures include :① The operating pressure of sour water degassing drum is kept as low as pos-sible (0 .05-0 .1 MPa);② Sour water in degassing drum is heated to 55-60 ℃ using low tem-perature waste heat of purifying water from the stripping bottom to make the degassing drum op-erated in higher temperature .③ The first ,second and third stage condensate liquid in single stripping tower or the return liquid from ammonia stripping reflux drum in double stripping tow-er is sent to a recycle liquid surge drum ,and then is pumped to the outlet pipe of sour water feed pump;④The thickness of oil layers in sour water feed tanks increases to 600-900 mm to form oil seal ,preventing H2 S or other effluvial compounds running out of the sour water feed tanks . After the above measures are taken ,there would have no effluvial gas discharging from the sour water feed tanks in normal operating conditions .This method has several advantages ,such as no need of additional adsorbent ,absorbent or coolant ,low investment and operation cost ,simple operation and no secondary pollution .
