WO2011017869A1 - 精对苯二甲酸装置精制单元氢气回收方法及装置 - Google Patents

精对苯二甲酸装置精制单元氢气回收方法及装置 Download PDF

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Publication number
WO2011017869A1
WO2011017869A1 PCT/CN2009/075361 CN2009075361W WO2011017869A1 WO 2011017869 A1 WO2011017869 A1 WO 2011017869A1 CN 2009075361 W CN2009075361 W CN 2009075361W WO 2011017869 A1 WO2011017869 A1 WO 2011017869A1
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hydrogen
heat exchanger
heat
outlet
medium
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PCT/CN2009/075361
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English (en)
French (fr)
Inventor
姚瑞奎
罗文德
周华堂
张莼
汪英枝
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中国石油天然气集团公司
中国纺织工业设计院
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Application filed by 中国石油天然气集团公司, 中国纺织工业设计院 filed Critical 中国石油天然气集团公司
Priority to RU2012105698/04A priority Critical patent/RU2517524C2/ru
Priority to IN1278DEN2012 priority patent/IN2012DN01278A/en
Publication of WO2011017869A1 publication Critical patent/WO2011017869A1/zh

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    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C51/00—Preparation of carboxylic acids or their salts, halides or anhydrides
    • C07C51/42—Separation; Purification; Stabilisation; Use of additives

Definitions

  • the invention relates to a method and a device for recovering hydrogen from a refining unit of a purified terephthalic acid (PTA) device, and mainly relates to the technical field of PTA.
  • PTA purified terephthalic acid
  • the PTA unit consists of two production units, oxidation and refining.
  • the oxidation unit is tasked by oxidizing p-nonylbenzene (PX) to terephthalic acid (TA), which is obtained by crystallization, filtration separation and drying to obtain crude terephthalic acid ( CTA),
  • CTA contains 4CBA (p-carboxybenzaldehyde), p-TA (p-mercaptobenzoic acid) and other impurities, which need to be purified and removed in the refining unit, and the refining unit is hydrotreated to make 4 CB A Restore to pT A.
  • p-TA is soluble in water
  • p-TA S is removed from the TA by crystallization, filtration, and washing; the hydrogenation reaction additionally acts to reduce the color group double bond in the colored impurities to a single bond to decolorize.
  • the content of 4CBA and other impurities in CTA depends on the oxidation unit production process, and the general 4CBA content is 2500 ⁇ 3500PPM.
  • the amount of hydrogen consumed per ton of PTA in production is 0.35 ⁇ 0.4 kg, and the chemical reaction consumption is only 25 ⁇ 30%, that is, the hydrogen consumption is about 4 times of the theoretical consumption of 4CBA hydrogenation reaction.
  • the traditional refined production process is to adjust a large amount of unreacted hydrogen (about 70% of the added amount) through the pressure of the crystallizer to control the discharge of non-condensable hydrogen from the condenser to the venting and eluting tower. Since hydrogen is a flammable and explosive dangerous substance, When hydrogen is discharged into the atmosphere through the leaching tower, a large amount of nitrogen is added for safety, resulting in a large amount of nitrogen and hydrogen consumption. At present, PTA plants at home and abroad use traditional refining processes, and there are no hydrogen recovery methods and recovery measures.
  • the object of the present invention is to overcome the defects of the prior art, and to provide a method and a device for recovering hydrogen from a refining unit of a purified terephthalic acid device, so as to recycle and utilize hydrogen, thereby saving energy and hydrogen resource consumption.
  • a hydrogen recovery method for a refining unit of a purified terephthalic acid unit wherein the non-condensable gas discharged by the crystal flashing is subjected to cooling and depressurization, and the steam is removed to form a hydrogen gas of a suitable purity for recycling.
  • the purity of hydrogen used for recycling is usually not less than 99% vo l.
  • the hydrogen gas formed after the treatment is usually detected, and the purification treatment is performed when the harmful gas exceeds the standard, and the purification treatment method is performed by intermittent purification treatment or partial hydrogen purification, and then mixed with hydrogen gas which is not subjected to purification treatment.
  • the non-condensable gas may be cooled and depressurized by the following steps:
  • the heat exchanger exchanges heat with the heat absorption medium of the third heat exchanger, and recycles the heat release medium gas discharged from the third heat exchanger as hydrogen of a suitable purity.
  • the singularity of the heat-dissipating medium of the heat-receiving medium after the heater group is 39. 0-39. 9 bar
  • the temperature of the second heat exchanger is the desalinated water heater of the refining unit
  • the heat absorbing medium is demineralized water
  • the pressure of the exothermic medium gas after passing through the second heat exchanger is 17. 0-17. 9 bar
  • the temperature is 1 69-171 °C
  • the third heat exchanger uses the cooling water heat exchanger of the refining unit
  • the heat absorbing medium is cooling water, after the third heat exchange
  • the pressure of the gas portion of the exothermic medium after the device is 1 0. 0-1 0. 9 bar
  • the temperature is 39-41 °C.
  • a hydrogen recovery device for a refining unit of a purified terephthalic acid unit comprising a hydrogen press, further comprising a cooling and pressure reducing device, wherein an inlet of the cooling and pressure reducing device is connected to a non-condensable gas outlet of a crystallizer group of the refining unit, The outlet of the cooling and pressure reducing device is connected to the inlet ⁇ of the hydrogen compressor.
  • the non-condensable gas separated after passing through the crystallizer group by the hydrorefined slurry can be subjected to a temperature reduction and pressure reduction treatment, and then compressed and recycled.
  • the non-condensed hydrogen does not need to be discharged through the leaching tower and the safety of nitrogen, solves the problem of hydrogen and nitrogen loss, basically does not change the original production process, the investment is basically unchanged, and is simple and easy. More importantly, it saves energy consumption (sterol, nitrogen, steam), and the comprehensive energy consumption per ton of finished product is reduced by 6. 6kg of standard oil, saving about 10 million yuan per year, and the economic benefits are remarkable.
  • the present invention provides a hydrogen recovery unit for a refining unit of a purified terephthalic acid unit, including a hydrogen press, and a cooling and pressure reducing device, wherein the inlet of the cooling and pressure reducing device is connected to the crystallization of the refining unit.
  • the non-condensable gas outlet of the set of devices, the outlet of the temperature reducing and pressure reducing device is connected to the inlet of the hydrogen press.
  • the temperature reducing and pressure reducing device may include a heater group, a first restrictor, a second heat exchanger, a second restrictor and a third heat exchanger, and the heat releasing medium outlet of the heater group is connected to the first An inlet of the restrictor, an outlet of the first restrictor is connected to a heat release medium inlet of the second heat exchanger, and a heat release medium outlet of the second heat exchanger is connected to the second restrictor
  • the inlet of the second restrictor is connected to the heat medium port of the third heat exchanger, and the heat release medium outlet of the third heat exchanger constitutes an outlet of the temperature reducing and pressure reducing device.
  • the non-condensable gas reaches the hydrogen inlet condition after several times of temperature reduction and pressure reduction treatment: the temperature is
  • the pressure is 10 bar and the hydrogen purity is greater than 99% vol.
  • the restrictor can usually use a restrictor orifice plate (R0), which can control a certain amount of gas discharge, thereby achieving the effect of reducing pressure.
  • R0 restrictor orifice plate
  • the heater group may use a CTA slurry heater group of the refining unit, wherein the exothermic medium of the heater group is steam and non-condensable gas discharged from the crystallizer group, and the heat absorbing medium is a slurry, the first
  • the second heat exchanger can use the demineralized water heater of the refining unit.
  • the exothermic medium of the demineralized water heater is steam and non-condensable gas discharged through the first restrictor, and the heat absorbing medium is demineralized water, demineralized water.
  • the temperature is raised, which is convenient for later washing of the filter cake,
  • the three heat exchangers can use a cooling water heat exchanger.
  • the heat releasing medium of the cooling water heat exchanger is steam and non-condensable gas discharged through the second current restrictor, and the heat absorbing medium is cooling water.
  • a hydrogen generating device is further disposed between the cooling water heat exchanger of the refining unit and the hydrogen press, and the inlet and outlet of the hydrogen producing device are respectively connected to the cooling water heat exchanger exothermic medium outlet of the refining unit And the inlet of the hydrogen press.
  • the heater group may further be provided with a condensate outlet of a heat release medium, the condensate outlet of the heat release medium is connected to an inlet of the condensate tank, and the gas outlet of the condensate tank is connected to the first current limit through a pipe Gas inlet.
  • the slurry outlet of the crystallizer set is typically connected to a slurry inlet of a filter scrubber, the filter cake outlet of the filter scrubber being connected to a material inlet of a dryer, the wash inlet of the filter being connected to the refining unit
  • the heat-absorbing medium inlet of the desalinated heater of the refining unit is connected to the heat-absorbing medium outlet of the steam heat exchanger through a pipe, and the steam heat exchanger can make the temperature of the demineralized water more Further improvement, in order to facilitate the later heating to a temperature of about 125 ° C by the desalinated heater to ensure the effect of washing the filter cake with brine.
  • the washing outlet of the filter is connected to the inlet of the mother liquid recovery unit, and the recovery outlet of the mother liquid recovery unit is connected to the oxidation unit, and the filter is used for solid-liquid separation of the slurry discharged from the crystallizer group, and the solid is a filter cake, and is washed by demineralized water. After drying in a dryer, a PTA product is formed. The mother liquor recovery supernatant is sent to the leaching, and the concentrated liquid is returned to the oxidation unit for recycling. The gas generated during the drying process is sent to the atmosphere after being rinsed, and the eluent recovery cycle is facilitated. use.
  • the hydrogen recovery unit may further be provided with a rinsing tower provided with inlets respectively connected to the liquid outlet of the condensate tank and the liquid outlet of the desalinated heater of the refining unit.
  • the liquid discharged from the condensate tank and the desalinated heater enters the rinsing tower for recycling.
  • the hydrogen recovery method of the refining unit of the refined terephthalic acid unit is carried out, and the non-condensable gas discharged by the crystallization treatment is subjected to cooling and depressurization, and the steam is removed to form a hydrogen gas of a suitable purity for recycling.
  • the crystallizer group of the refining unit separates and separates the gas and the slurry after the refining reaction, and the discharged gas includes steam and non-condensable gas, which serves as an exothermic medium and enters the heater group to exchange heat with the heat absorbing medium of the heater group.
  • the gas fed by the first restrictor decompression and current limiting is sent to the second heat exchanger as a heat release medium, and exchanges heat with the heat absorption medium of the second heat exchanger; the second heat exchanger
  • the discharged heat release medium gas is subjected to pressure reduction and current limiting via the second restrictor; the gas sent out by the second flow restrictor pressure reduction current is sent to the third heat exchanger as the heat release medium, and the third heat exchanger
  • the heat absorbing medium performs heat exchange, and the heat release medium gas discharged from the third heat exchanger is recycled as hydrogen of a suitable purity.
  • the non-condensable gas discharged from the first restrictor orifice plate has a high temperature and contains a large amount of steam.
  • the demineralized water heater heats up, the large amount of water vapor in the non-condensable gas is condensed and then passed through the condensate of the demineralized water heater.
  • the outlet is discharged into the rinsing tower and discharged into the atmosphere or reused.
  • the slurry discharged through the crystallizer group is filtered through a filter, and the filtered cake is subjected to demineralized water.
  • the washing is carried out and dried by a drier to finally obtain a PTA product.
  • the temperature is required to reach about 125 ° C, and the filtered mother liquor is recovered by the mother liquid recovery device and the dope is introduced into the oxidation unit.

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  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Engineering & Computer Science (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
  • Separation By Low-Temperature Treatments (AREA)
  • Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)

Abstract

本发明涉及一种精对苯二甲酸装置精制单元氢气回收方法及装置， 该方法将结晶闪蒸排出的不凝气体经过降温和降压后， 去除其中的蒸汽， 形成适宜纯度的氢气循环使用。该装置包括氢压机， 还包括降温降压设备，所述降温降压设备的入口连接精制单元的结晶器组的不凝气体出口， 所述降温降压设备的出口连接所述氢压机的入口。 由于本发明可以将结晶器组分离排出的不凝气体通过降温降压处理后再循环利用， 基本上不改变原有的生产工艺， 投资基本不变， 且简单易行，更重要的是节省能源消耗，经济效益显著。

Description

说 明 书
精对苯二曱酸装置精制单元氢气回收方法及装置 技术领域
本发明涉及精对苯二曱酸（PTA )装置精制单元氢气回收方法及 装置， 主要涉及 PTA的技术领域。
背景技术
PTA装置由氧化和精制两个生产单元组成， 氧化单元任务是将对 二曱苯（PX ) 氧化生成对苯二曱酸（TA ), 通过结晶、 过滤分离、 干 燥获得粗对苯二曱酸 ( CTA ), CTA中含有 4CBA (对羧基苯曱醛）、 p-TA (对曱基苯曱酸）及其他杂质， 需在精制单元净化去除， 精制单元釆 用加氢精制方法， 使 4 CB A还原成 p-T A。
由于 p-TA可溶于水， 通过结晶、 过滤、 洗涤处理， 将 p-TA S炱从 TA 中去除； 加氢反应另外作用是使有色杂质中有色基团双键还原成 单键而脱色。 CTA中 4CBA和其他杂质含量取决于氧化单元生产工艺， 一般 4CBA含量为 2500 ~ 3500PPM。 生产上每吨 PTA耗用氢气量为 0. 35 ~ 0. 4kg , 而化学反应消耗量仅为加入量 25 ~ 30% , 即氢气用量 为 4CBA加氢反应理论消耗量 4倍左右。
传统精制生产工艺是将大量未反应氢气（约为加入量的 70% )通 过结晶器压力调节， 控制不凝氢气从冷凝器排放至放空淋洗塔， 由于 氢气是易燃易爆危险物质，所以氢气经淋洗塔排入大气时，为了安全， 又要加入大量氮气， 造成大量氮气、 氢气消耗。 目前国内外 PTA装置 均釆用传统精制工艺， 工程上无氢气回收方法方案及回收措施。
发明内容 本发明的目的在于克服现有技术的缺陷，提供一种精对苯二曱酸 装置精制单元氢气回收方法及装置， 以将氢气回收利用， 节省能源和 氢资源消耗。
本发明是通过以下技术方案实现的：
一种精对苯二曱酸装置精制单元氢气回收方法，结晶闪蒸排出的 不凝气体经过降温和降压后， 去除其中的蒸汽， 形成适宜纯度的氢气 循环使用。
用于循环使用的氢气纯度通常不低于 99%vo l。
通常对处理后形成的氢气进行检测，在有害气体超标时进行净化 处理，所述净化处理方式釆用间歇式净化处理或将部分氢气进行净化 后再与不进行净化处理的氢气混合。
可以依次经过下列步骤对所述不凝气体进行降温和降压：
( 1 ) 将结晶器组排出的蒸汽和不凝气体作为放热介质送入加热 器组， 与加热器组的吸热介质进行热交换；
( 2 ) 将加热器组排出的放热介质液体部分送入凝液罐， 将所述 凝液罐分离出来的气体和所述加热器组排出的放热介质气体部分经 第一限流器进行减压限流；
( 3 ) 将第一限流器减压限流送出的气体作为放热介质送入第二 热交换器， 与第二热交换器的吸热介质进行热交换；
( 4 ) 所述第二热交换器排出的放热介质气体经第二限流器进行 减压限流；
( 5 ) 将第二限流器减压限流送出的气体作为放热介质送入第三 热交换器， 与第三热交换器的吸热介质进行热交换， 将所述第三热交 换器排出的放热介质气体作为适宜纯度的氢气循环使用。
所述加热器组可以釆用精制单元的 CTA浆料加热器组，其吸热介 质为 CTA 浆料， 经过加热器组后的放热介质气体部分的压力为 39. 0-39. 9 巴， 温度为 242-244 °C , 所述第二热交换器釆用精制单元 的除盐水加热器， 其吸热介质为除盐水， 经过第二次热交换器后的放 热介质气体部分的压力为 17. 0-17. 9巴， 温度为 1 69-171 °C , 所述第 三热交换器釆用精制单元的冷却水换热器， 其吸热介质为冷却水， 经 过第三次热交换器后的放热介质气体部分的压力为 1 0. 0-1 0. 9巴，温 度为 39-41 °C。
一种精对苯二曱酸装置精制单元氢气回收装置， 包括氢压机， 还 包括降温降压设备，所述降温降压设备的入口连接精制单元的结晶器 组的不凝气体出口， 所述降温降压设备的出口连接所述氢压机的入 σ。
由于本发明可以使加氢精制后的浆料经过结晶器组后分离出的 不凝气体通过降温降压处理后， 进行压缩后循环利用。 与传统工艺相 比， 不凝氢气不需要通过淋洗塔排出和氮气的安全保护， 解决了氢气 和氮气的损耗问题， 基本上不改变原有的生产工艺， 投资基本不变， 且简单易行， 更重要的是节省能源消耗（曱醇、 氮气、 蒸汽）， 每吨 ΡΤΑ成品综合能耗下降 6. 6kg标油， 每年可节省约 1 000万元， 经济 效益显著。
附图说明 图 1是本发明的工艺流程示意图。
具体实施方式
如图 1所示，本发明提供了一种精对苯二曱酸装置精制单元氢气 回收装置， 包括氢压机， 还包括降温降压设备， 所述降温降压设备的 入口连接精制单元的结晶器组的不凝气体出口，所述降温降压设备的 出口连接所述氢压机的入口。
所述降温降压设备可以包括加热器组、 第一限流器、 第二热交换 器、 第二限流器和第三热交换器， 所述加热器组的放热介质出口连接 所述第一限流器的入口，所述第一限流器的出口连接所述第二热交换 器的放热介质入口，所述第二热交换器的放热介质出口连接所述第二 限流器的入口，所述第二限流器的出口连接所述第三热交换器的热介 口 , 所述第三热交换器的放热介质出口构成所述降温降压设备的出 口。 不凝气体经过多次降温降压处理后达到氢压机入口条件： 温度为
40°C , 压力为 10巴， 氢气纯度大于 99%vol。
所述限流器通常可以釆用限流孔板（R0 ), 可以控制气体的一定 排放量， 从而达到降压的作用。
所述加热器组可以釆用精制单元的 CTA浆料加热器组，此加热器 组的放热介质为由结晶器组排出的蒸汽和不凝气体，其吸热介质为浆 料， 所述第二热交换器可以釆用精制单元的除盐水加热器， 此除盐水 加热器的放热介质为经第一次限流器排出的蒸汽和不凝气体，其吸热 介质为除盐水， 除盐水温度升高， 便于后期用于滤饼的洗涤， 所述第 三热交换器可以釆用冷却水换热器，此冷却水换热器的放热介质为经 第二次限流器排出的蒸汽和不凝气体， 其吸热介质为冷却水。
所述精制单元的冷却水换热器与所述氢压机之间还设有制氢装 置， 所述制氢装置的进、 出口分别连接所述精制单元的冷却水换热器 放热介质出口和所述氢压机的入口。在进行压缩前的不凝气体检测其 含有的有害气体超标时，可以先将其间歇或部分送去制氢装置净化后 再进入氢压机中压缩回收，如果在进行压缩前的不凝气体若检测其含 有的有害气体未超标时， 则直接送入氢压机中压缩回收。
所述加热器组还可以设有放热介质的凝结液出口，所述放热介质 的凝结液出口连接凝液罐的入口，所述凝液罐的气体出口通过管道连 接所述第一限流器的气体入口。
所述结晶器组的浆料出口通常与过滤洗涤器的浆料入口相连，所 述过滤洗涤器的滤饼出口与干燥机的物料入口相连，所述过滤器的洗 涤入口连接所述精制单元的除盐水加热器的除盐水出口，所述精制单 元的除盐水加热器的吸热介质入口通过管道与蒸汽换热器的吸热介 质出口相连接， 蒸汽换热器可以使除盐水的温度有更进一步提高， 以 便于后期更易于通过除盐水加热器加热到约 125 °C , 以保证除盐水洗 涤滤饼效果。 所述过滤器的洗涤出口连接母液回收器入口， 所述母液 回收器的回收出口连接氧化单元，过滤器用来将结晶器组排出的浆料 进行固液分离， 固体为滤饼， 经过除盐水洗涤后进入干燥机中干燥后 形成 PTA产品。母液回收清液送去淋洗，浓液进入氧化单元回收利用 , 在干燥过程中产生的气体送入淋洗后排入大气， 淋洗液回收循环利 用。
该氢气回收装置还可以设有淋洗塔，所述淋洗塔设有分别与所述 凝液罐的液体出口和所述精制单元的除盐水加热器的液体出口相连 的入口。凝液罐和除盐水加热器排出的液体进入淋洗塔回收利用。从 一种精对苯二曱酸装置精制单元氢气回收方法，结晶处理排出的 不凝气体经过降温和降压后， 去除其中的蒸汽， 形成适宜纯度的氢气 循环使用。
精制单元的结晶器组将精制反应后的气体和浆料分开并分别排 出， 排出的气体包括蒸汽和不凝气体， 其作为放热介质进入加热器组 与加热器组的吸热介质进行热交换，将加热器组排出的放热介质液体 部分送入凝液罐，将所述凝液罐分离出来的气体和所述加热器组排出 的放热介质气体部分经第一限流器进行减压限流，将第一限流器减压 限流送入的气体作为放热介质送入第二热交换器，与第二热交换器的 吸热介质进行热交换；所述第二热交换器排出的放热介质气体经第二 限流器进行减压限流；将第二限流器减压限流送出的气体作为放热介 质送入第三热交换器， 与第三热交换器的吸热介质进行热交换， 将所 述第三热交换器排出的放热介质气体作为适宜纯度的氢气循环使用。
排出第一道限流孔板的不凝气体温度高且含有较多的蒸汽，经过 除盐水加热器换热时，同时将不凝气体中的大量水蒸汽冷凝后通过除 盐水加热器的凝液出口排入淋洗塔中， 再排入大气或者再利用。
经结晶器组排出的浆料经过滤器过滤，过滤后的滤饼经过除盐水 的洗涤并通过干燥器干燥， 最终得到了 PTA产品， 而为了保证除盐水 洗涤滤饼效果， 需用使其温度达到约 125°C, 过滤的母液经过母液回 收器回收后浓液进入氧化单元。

Claims

权 利 要 求 书
1、 一种精对苯二曱酸装置精制单元氢气回收方法， 其特征在 于结晶闪蒸排出的不凝气体经过降温和降压后， 去除其中的蒸汽， 形 成适宜纯度的氢气， 循环使用。
2、 如权利要求 1所述的精对苯二曱酸装置精制单元氢气回收 方法， 其特征在于所述用于循环使用的氢气纯度不低于 99%vol。
3、 如权利要求 1或 2所述的精对苯二曱酸装置精制单元氢气 回收方法， 其特征在于对处理后形成的氢气进行检测， 在有害气体超 标时进行净化处理，所述净化处理方式为间歇式净化处理或将部分氢 气进行净化后再与不进行净化处理的氢气混合。
4、 如权利要求 1、 2或 3所述的精对苯二曱酸装置精制单元氢 气回收方法，其特征在于依次经过下列步骤对所述不凝气体进行降温 和降压：
( 1 ) 将结晶器组排出的蒸汽和不凝气体作为放热介质送入 加热器组， 与加热器组的吸热介质进行热交换；
( 2 ) 将加热器组排出的放热介质的液体部分送入凝液罐，将 所述凝液罐分离出来的气体和所述加热器组排出的放热介质的气体 部分混合后经第一限流器进行减压限流送出；
( 3 ) 将第一限流器减压限流送出的气体作为放热介质送入 第二热交换器， 与第二热交换器的吸热介质进行热交换；
( 4 ) 所述第二热交换器排出的放热介质气体经第二限流器 进行减压限流送出； ( 5 ) 将第二限流器减压限流送出的气体作为放热介质送入 第三热交换器， 与第三热交换器的吸热介质进行热交换，使第三热交 换器排出的放热介质气体部分符合氢气循环使用的纯度要求，并作为 所述适宜纯度的氢气循环使用。
5、 如权利要求 4所述的精对苯二曱酸装置精制单元氢气回收 方法， 其特征在于所述加热器组釆用精制单元的 CTA浆料加热器组， 其吸热介质为 CTA浆料，经过加热器组后的放热介质气体部分的压力 为 39. 0-39. 9巴， 温度为 242-244 °C , 所述第二热交换器釆用精制单 元的除盐水加热器， 其吸热介质为除盐水， 经过第二次热交换器后的 放热介质气体部分的压力为 17. 0-17. 9巴， 温度为 169-171 °C , 所述 第三热交换器釆用精制单元的冷却水换热器， 其吸热介质为冷却水， 经过第三次热交换器后的放热介质气体部分的压力为 10. 0-10. 9巴， 温度为 39-41 °C。
6、 一种精对苯二曱酸装置精制单元氢气回收装置， 包括氢压 机， 其特征在于还包括降温降压设备， 所述降温降压设备的入口连接 精制单元的结晶器组的不凝气体出口，所述降温降压设备的出口连接 所述氢压机的入口。
7、 如权利要求 6所述的精对苯二曱酸装置精制单元氢气回收 装置， 其特征在于所述降温降压设备包括加热器组、 第一限流器、 第 二热交换器、 第二限流器和第三热交换器， 所述加热器组的放热介质 出口连接所述第一限流器的入口，所述第一限流器的出口连接所述第 二热交换器的放热介质入口，所述第二热交换器的放热介质出口连接 所述第二限流器的入口，所述第二限流器的出口连接所述第三热交换 器的热介质入口，所述加热器组的放热介质入口构成所述降温降压设 备的入口 ,所述第三热交换器的放热介质出口构成所述降温降压设备 的出口。
8、 如权利要求 7所述的精对苯二曱酸装置精制单元氢气回收 装置， 其特征在于所述加热器组釆用精制单元的 CTA 浆料的加热器 组， 所述第二热交换器釆用精制单元的除盐水加热器， 所述第三热交 换器釆用精制单元的冷却水换热器 ,所述精制单元的冷却水换热器与 所述氢压机之间还设有制氢装置， 所述制氢装置的进、 出口分别连接 所述精制单元的冷却水换热器放热介质出口和所述氢压机的入口。
9、 如权利要求 8所述的精对苯二曱酸装置精制单元氢气回收 装置， 其特征在于所述加热器组还设有放热介质的凝结液出口， 所述 放热介质的凝结液出口连接凝液罐的入口，所述凝液罐的气体出口通 过管道连接所述第一限流器的气体入口。
10、 如权利要求 6、 7、 8或 9所述的精对苯二曱酸装置精制 单元氢气回收装置，其特征在于所述结晶器组的浆料出口与过滤洗涤 器的浆料入口相连，所述过滤洗涤器的滤饼出口与干燥机的物料入口 相连，所述过滤器的洗涤入口连接所述精制单元的除盐水加热器的除 盐水出口 ,所述精制单元的除盐水加热器的吸热介质入口通过管道与 蒸汽换热器相连接， 所述过滤器的洗涤出口连接母液回收器入口， 所 述母液回收器的回收出口连接氧化单元。
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Publication number Priority date Publication date Assignee Title
CN1264360A (zh) * 1997-07-16 2000-08-23 纳幕尔杜邦公司 纯对苯二甲酸生产中回收氢方法的改进
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* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN1264360A (zh) * 1997-07-16 2000-08-23 纳幕尔杜邦公司 纯对苯二甲酸生产中回收氢方法的改进
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