CN108061428A - 一种纯氮制取装置和工艺 - Google Patents
一种纯氮制取装置和工艺 Download PDFInfo
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- CN108061428A CN108061428A CN201810030626.5A CN201810030626A CN108061428A CN 108061428 A CN108061428 A CN 108061428A CN 201810030626 A CN201810030626 A CN 201810030626A CN 108061428 A CN108061428 A CN 108061428A
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- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 title claims abstract description 511
- 229910052757 nitrogen Inorganic materials 0.000 title claims abstract description 251
- 238000000034 method Methods 0.000 title description 5
- 239000007788 liquid Substances 0.000 claims abstract description 180
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims abstract description 53
- 239000001301 oxygen Substances 0.000 claims abstract description 53
- 229910052760 oxygen Inorganic materials 0.000 claims abstract description 53
- 239000002808 molecular sieve Substances 0.000 claims abstract description 40
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 claims abstract description 40
- 238000001816 cooling Methods 0.000 claims abstract description 39
- 239000007789 gas Substances 0.000 claims abstract description 32
- 230000008929 regeneration Effects 0.000 claims abstract description 12
- 238000011069 regeneration method Methods 0.000 claims abstract description 12
- 238000002156 mixing Methods 0.000 claims abstract description 4
- 239000000047 product Substances 0.000 claims description 25
- 238000004781 supercooling Methods 0.000 claims description 10
- 229910001873 dinitrogen Inorganic materials 0.000 claims description 9
- 238000000605 extraction Methods 0.000 claims description 9
- 239000000428 dust Substances 0.000 claims description 8
- 238000000746 purification Methods 0.000 claims description 8
- 230000000630 rising effect Effects 0.000 claims description 8
- 239000006227 byproduct Substances 0.000 claims description 7
- 239000000126 substance Substances 0.000 claims description 7
- 230000005611 electricity Effects 0.000 claims description 5
- 230000008676 import Effects 0.000 claims description 5
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 3
- 239000002994 raw material Substances 0.000 claims 1
- 238000005265 energy consumption Methods 0.000 abstract description 7
- 238000011084 recovery Methods 0.000 abstract description 7
- 238000009833 condensation Methods 0.000 description 5
- 230000005494 condensation Effects 0.000 description 5
- 239000006096 absorbing agent Substances 0.000 description 4
- 238000001704 evaporation Methods 0.000 description 3
- 230000008020 evaporation Effects 0.000 description 3
- 238000010438 heat treatment Methods 0.000 description 3
- 230000006835 compression Effects 0.000 description 2
- 238000007906 compression Methods 0.000 description 2
- 235000019628 coolness Nutrition 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 238000001914 filtration Methods 0.000 description 2
- 239000012530 fluid Substances 0.000 description 2
- 238000000926 separation method Methods 0.000 description 2
- 229910000831 Steel Inorganic materials 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- CUZMQPZYCDIHQL-VCTVXEGHSA-L calcium;(2s)-1-[(2s)-3-[(2r)-2-(cyclohexanecarbonylamino)propanoyl]sulfanyl-2-methylpropanoyl]pyrrolidine-2-carboxylate Chemical compound [Ca+2].N([C@H](C)C(=O)SC[C@@H](C)C(=O)N1[C@@H](CCC1)C([O-])=O)C(=O)C1CCCCC1.N([C@H](C)C(=O)SC[C@@H](C)C(=O)N1[C@@H](CCC1)C([O-])=O)C(=O)C1CCCCC1 CUZMQPZYCDIHQL-VCTVXEGHSA-L 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 239000011521 glass Substances 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 229910052573 porcelain Inorganic materials 0.000 description 1
- 239000010959 steel Substances 0.000 description 1
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- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
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- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
- F25J3/04048—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of cold gaseous streams, e.g. intermediate or oxygen enriched (waste) streams
- F25J3/0406—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of cold gaseous streams, e.g. intermediate or oxygen enriched (waste) streams of nitrogen
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- F25J3/04151—Purification and (pre-)cooling of the feed air; recuperative heat-exchange with product streams
- F25J3/04163—Hot end purification of the feed air
- F25J3/04169—Hot end purification of the feed air by adsorption of the impurities
- F25J3/04181—Regenerating the adsorbents
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- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- F25J3/04151—Purification and (pre-)cooling of the feed air; recuperative heat-exchange with product streams
- F25J3/04187—Cooling of the purified feed air by recuperative heat-exchange; Heat-exchange with product streams
- F25J3/04193—Division of the main heat exchange line in consecutive sections having different functions
- F25J3/04206—Division of the main heat exchange line in consecutive sections having different functions including a so-called "auxiliary vaporiser" for vaporising and producing a gaseous product
- F25J3/04212—Division of the main heat exchange line in consecutive sections having different functions including a so-called "auxiliary vaporiser" for vaporising and producing a gaseous product and simultaneously condensing vapor from a column serving as reflux within the or another column
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- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
- F25J3/04284—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams
- F25J3/0429—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams of feed air, e.g. used as waste or product air or expanded into an auxiliary column
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- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
- F25J3/04284—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams
- F25J3/0429—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams of feed air, e.g. used as waste or product air or expanded into an auxiliary column
- F25J3/04303—Lachmann expansion, i.e. expanded into oxygen producing or low pressure column
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- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- F25J3/04406—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using a dual pressure main column system
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- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
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- F25J2200/50—Processes or apparatus using separation by rectification using multiple (re-)boiler-condensers at different heights of the column
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
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- F25J2205/00—Processes or apparatus using other separation and/or other processing means
- F25J2205/60—Processes or apparatus using other separation and/or other processing means using adsorption on solid adsorbents, e.g. by temperature-swing adsorption [TSA] at the hot or cold end
- F25J2205/66—Regenerating the adsorption vessel, e.g. kind of reactivation gas
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- F25J2215/00—Processes characterised by the type or other details of the product stream
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- F25J2235/00—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams
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- F25J2245/00—Processes or apparatus involving steps for recycling of process streams
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- F25J2250/00—Details related to the use of reboiler-condensers
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Abstract
本发明公开一种纯氮制取装置,包括过滤器、透平空气压缩机、空气预冷机组、交替使用的分子筛吸附器、电加热器、增压后冷却器、主换热器、膨胀机、精馏塔I、精馏塔II、冷凝蒸发器I、冷凝蒸发器II、过冷器、液氮泵、冷箱。本发明采用压力空气膨胀制取装置所需冷量,可以膨胀至一定压力后进入精馏塔II参与精馏,提取率高,能耗低;或膨胀至常压,压比高,制冷量效率高,制冷量大,可以减少装置启动时间,节省用电量,提取率更高、能耗更低,后经复热后出冷箱,混合部分污氮气用作交替使用的分子筛吸附器再生气,降低了再生污氮气中的含氧量,有效延长电加热器的使用寿命。
Description
技术领域
本发明涉及空气分离技术领域,具体涉及一种纯氮制取装置和工艺。
背景技术
随着化工、电子、新材料、瓷钢业、玻璃等行业技术发展和革新,对氮气需求量急速增加,同时对氮气纯度也提出了更高的要求。
目前市场上的常用的纯氮设备分为两种:单塔制氮和双塔制氮,单塔制氮流畅可制取一定压力的产品氮气直接供用户使用,该种流程形式虽然结构简单,但装置提取率较低,产品单耗高,不适合大规模用氮气量的需求;双塔制氮可以制取常压氮气或压力为0.1-0.2MpaG的低压氮气,装置提取率高,能耗较单塔制氮低,但是由于产品压力较低,产品氮气需要经氮气压缩机压缩后才能满足用户对氮气压力的要求。
发明内容
本发明的目的是提供一种纯氮制取装置和工艺,以解决现有技术的不足。
本发明采用以下技术方案:
一种纯氮制取装置,包括过滤器、透平空气压缩机、空气预冷机组、交替使用的分子筛吸附器、电加热器、增压后冷却器、主换热器、膨胀机、精馏塔I、精馏塔II、冷凝蒸发器I、冷凝蒸发器II、过冷器、液氮泵、冷箱,
过滤器、透平空气压缩机、空气预冷机组、交替使用的分子筛吸附器、电加热器、增压后冷却器、膨胀机的增压端设于冷箱外,主换热器、膨胀机、精馏塔I、精馏塔II、冷凝蒸发器I、冷凝蒸发器II、过冷器、液氮泵设置于冷箱内,精馏塔II设于精馏塔I之上,冷凝蒸发器I设于精馏塔I和精馏塔II之间,冷凝蒸发器II设于精馏塔II之上;
过滤器、透平空气压缩机、空气预冷机组、交替使用的分子筛吸附器依次连接,交替使用的分子筛吸附器分别和主换热器、膨胀机的增压端连接,主换热器和精馏塔I底部的原料空气进口连接;膨胀机的增压端和增压后冷却器连接,增压后冷却器和主换热器连接,主换热器的原料空气部分复热出口和膨胀机连接,膨胀机再和精馏塔II底部的原料空气进口连接;
精馏塔I顶部的高压氮气出口分别和主换热器、冷凝蒸发器I连接,主换热器连接外部管道以提供高压氮气产品,冷凝蒸发器I的液氮出口分别和精馏塔I顶部、过冷器、冷箱外液氮存储罐连接,过冷器和精馏塔II顶部连接,其中,冷凝蒸发器I的液氮出口和精馏塔I顶部的连接管路上设有角式冷阀,过冷器和精馏塔II顶部的连接管路上设有节流阀;
精馏塔I底部的液空出口和过冷器连接,过冷器再和精馏塔II中部连接,其中,过冷器和精馏塔II中部连接的管路上设节流阀;
精馏塔II顶部的低压氮气出口分别和主换热器、冷凝蒸发器II连接,主换热器连接外部管道以提供低压氮气产品;
精馏塔II底部的富氧液空出口和冷凝蒸发器II连接,其连接管路上设有节流阀;
冷凝蒸发器II的低压液氮出口分别和精馏塔II顶部、液氮泵连接,液氮泵和精馏塔I顶部连接,液氮泵和精馏塔I顶部的连接管路上设有角式冷阀;冷凝蒸发器II的污氮气出口和过冷器连接,过冷器和主换热器连接,主换热器分别和电加热器、外部放空管道连接,电加热器和交替使用的分子筛吸附器连接。
进一步地,膨胀机不和精馏塔II连接,而和主换热器连接,主换热器再连接至电加热器;冷凝蒸发器I的液氮出口分别和精馏塔I顶部、冷箱外液氮存储罐连接,其中,冷凝蒸发器I的液氮出口和精馏塔I顶部的连接管路上设有角式冷阀。
利用第一种纯氮制取装置进行纯氮制取,包括如下步骤:
步骤一、将原料空气经过滤器过滤掉灰尘和机械杂质后,进入透平空气压缩机将空气压缩到设定压力;之后经空气预冷机组预冷后进入交替使用的分子筛吸附器中纯化;
步骤二、将纯化后的原料空气部分用于仪表空气,其余部分分为两股,一股直接进入主换热器被返流气体冷却至饱和并带有一定含湿后进入精馏塔I底部参与精馏;另一股经过膨胀机的增压端增压及增压后冷却器冷却后进入主换热器被返流气体部分冷却至一定温度后,抽出进入膨胀机膨胀制取装置所需冷量,膨胀后空气引入精馏塔II底部参与精馏;
步骤三、空气经精馏塔I精馏后分离为高压氮气和液空,高压氮气分成两股,一股直接引出经过主换热器复热后出冷箱作为产品供用户,另一股引入冷凝蒸发器I和富氧液空换热,高压氮气被冷凝为液氮,引出部分液氮进入精馏塔I作为回流液,引出部分液氮经过冷器过冷后节流进入精馏塔II作为回流液,另引出其余部分液氮作为副产品;液空经过过冷器过冷后节流进入精馏塔II参与精馏;
步骤四、膨胀后空气、液空和液氮在精馏塔II中被分离为低压氮气和富氧液空,引出部分低压氮气经主换热器复热后作为产品供用户,其余低压氮气引入冷凝蒸发器II;部分富氧液空被精馏塔I引出的高压氮气汽化作为精馏塔II的上升气,其余富氧液空经节流后引入冷凝蒸发器II;
步骤五、在冷凝蒸发器II中低压氮气和富氧液空进行换热,低压氮气被冷凝为低压液氮,富氧液空被汽化为污氮气;引出部分低压液氮经液氮泵增压后引入精馏塔I顶部作为回流液,其余低压液氮引入精馏塔II顶部作为回流液;污氮气经过过冷器、主换热器复热后出冷箱,一部分由电加热器加热后引入交替使用的分子筛吸附器作为再生气,其余放空。
利用第二种纯氮制取装置进行纯氮制取,包括如下步骤:
步骤一、将原料空气经过滤器过滤掉灰尘和机械杂质后,进入透平空气压缩机将空气压缩到设定压力;之后经空气预冷机组预冷后进入交替使用的分子筛吸附器中纯化,将水分、CO2、C2H2等物质去除;
步骤二、将纯化后的原料空气部分用于仪表空气,其余部分分为两股,一股直接进入主换热器被返流气体冷却至饱和并带有一定含湿后进入精馏塔I底部参与精馏;另一股经过膨胀机的增压端增压及增压后冷却器冷却后进入主换热器被返流气体部分冷却至一定温度后,抽出进入膨胀机膨胀制取装置所需冷量,膨胀后空气经主换热器复热后出冷箱,和后续部分污氮气混合,由电加热器加热后引入交替使用的分子筛吸附器作为再生气;
步骤三、空气经精馏塔I精馏后分离为高压氮气和液空,高压氮气分成两股,一股直接引出经过主换热器复热后出冷箱作为产品供用户,另一股引入冷凝蒸发器I和富氧液空换热,高压氮气被冷凝为液氮,引出部分液氮进入精馏塔I作为回流液,另引出其余部分液氮作为副产品;液空经过过冷器过冷后节流进入精馏塔II参与精馏;
步骤四、液空在精馏塔II中被分离为低压氮气和富氧液空,引出部分低压氮气经主换热器复热后作为产品供用户,其余低压氮气引入冷凝蒸发器II;部分富氧液空被精馏塔I引出的高压氮气汽化作为精馏塔II的上升气,其余富氧液空经节流后引入冷凝蒸发器II;
步骤五、在冷凝蒸发器II中低压氮气和富氧液空进行换热,低压氮气被冷凝为低压液氮,富氧液空被汽化为污氮气;引出部分低压液氮经液氮泵增压后引入精馏塔I顶部作为回流液,其余低压液氮引入精馏塔II顶部作为回流液;污氮气经过过冷器、主换热器复热后出冷箱,一部分和膨胀后空气混合,由电加热器加热后引入交替使用的分子筛吸附器作为再生气,其余放空。
本发明的有益效果:
1、本发明采用压力空气膨胀制取装置所需冷量,可以膨胀至一定压力后进入精馏塔II参与精馏,提取率高,能耗低;或者膨胀至常压,压比高,制冷量效率高,制冷量大,可以减少装置启动时间,节省用电量,提取率更高、能耗更低,后经复热后出冷箱,混合部分污氮气用作交替使用的分子筛吸附器再生气,降低了再生污氮气中的含氧量,防止因再生污氮气含氧量过高造成电加热器加热过程过热问题,有效延长电加热器的使用寿命。
2、本发明增设液氮泵将低压液氮增压后引入高压精馏塔作为回流液,提高了高压氮气提取率,大大降低装置能耗。
3、本发明可制取两种压力等级的氮气产品,同时可制取液氮副产品。
附图说明
图1为本发明一种结构示意图。
图2为本发明另一种结构示意图。
具体实施方式
下面结合实施例和附图对本发明做更进一步地解释。下列实施例仅用于说明本发明,但并不用来限定本发明的实施范围。
一种纯氮制取装置,如图1所示,包括过滤器1、透平空气压缩机2、空气预冷机组3-1、交替使用的分子筛吸附器4、电加热器5、增压后冷却器3-2、主换热器6、膨胀机7、精馏塔I8、精馏塔II10、冷凝蒸发器I9、冷凝蒸发器II11、过冷器12、液氮泵13、冷箱,
过滤器1、透平空气压缩机2、空气预冷机组3-1、交替使用的分子筛吸附器4、电加热器5、增压后冷却器3-2、膨胀机的增压端7-1设于冷箱外,主换热器6、膨胀机7、精馏塔I8、精馏塔II10、冷凝蒸发器I9、冷凝蒸发器II11、过冷器12、液氮泵13设置于冷箱内,精馏塔II10设于精馏塔I8之上,冷凝蒸发器I9设于精馏塔I8和精馏塔II10之间,冷凝蒸发器II11设于精馏塔II10之上;
过滤器1、透平空气压缩机2、空气预冷机组3-1、交替使用的分子筛吸附器4依次连接,交替使用的分子筛吸附器4分别和主换热器6、膨胀机的增压端7-1连接,主换热器6和精馏塔I8底部的原料空气进口连接;膨胀机的增压端7-1和增压后冷却器3-2连接,增压后冷却器3-2和主换热器6连接,主换热器6的原料空气部分复热出口和膨胀机7连接,膨胀机7再和精馏塔II10底部的原料空气进口连接;
精馏塔I8顶部的高压氮气出口分别和主换热器6、冷凝蒸发器I9连接,主换热器6连接外部管道以提供高压氮气产品,冷凝蒸发器I9的液氮出口分别和精馏塔I8顶部、过冷器12、冷箱外液氮存储罐连接,过冷器12和精馏塔II10顶部连接,其中,冷凝蒸发器I9的液氮出口和精馏塔I8顶部的连接管路上设有角式冷阀,过冷器12和精馏塔II10顶部的连接管路上设有节流阀;
精馏塔I8底部的液空出口和过冷器12连接,过冷器12再和精馏塔II10中部连接,其中,过冷器12和精馏塔II10中部连接的管路上设节流阀;
精馏塔II10顶部的低压氮气出口分别和主换热器6、冷凝蒸发器II11连接,主换热器6连接外部管道以提供低压氮气产品;
精馏塔II10底部的富氧液空出口和冷凝蒸发器II11连接,其连接管路上设有节流阀;
冷凝蒸发器II11的低压液氮出口分别和精馏塔II10顶部、液氮泵13连接,液氮泵13和精馏塔I8顶部连接,液氮泵13和精馏塔I8顶部的连接管路上设有角式冷阀;冷凝蒸发器II11的污氮气出口和过冷器12连接,过冷器12和主换热器6连接,主换热器6分别和电加热器5、外部放空管道连接,电加热器5和交替使用的分子筛吸附器4连接。
上述各部件的功能如下:
过滤器1,用于过滤原料空气中的灰尘和机械杂质;
透平空气压缩机2,用于将过滤后的原料空气压缩到设定压力;
空气预冷机组3-1,用于将过滤、压缩后的原料空气预冷;
交替使用的分子筛吸附器4,用于将过滤、压缩、预冷后的原料空气纯化,去除水分、CO2、C2H2等物质;
电加热器5,用于加热污氮气以再生分子筛吸附器4;
增压后冷却器3-2,用于冷却经膨胀机的增压端7-1增压后的原料空气;
主换热器6,用于将过滤、压缩、预冷、纯化后的原料空气冷却;用于将过滤、压缩、预冷、纯化、增压、冷却后的原料空气部分冷却;用于将高压氮气复热、低压氮气复热、污氮气复热;
膨胀机7,用于将部分冷却后的原料空气膨胀制取冷箱必需冷量;
精馏塔I8,用于将经过滤、压缩、预冷、纯化、冷却后的原料空气低温精馏而分离为高压氮气和液空;
精馏塔II10,用于将膨胀后空气和液空精馏为低压氮气和富氧液空;
冷凝蒸发器I9,用于将高压氮气和富氧液空进行换热,高压氮气液化为液氮,富氧液空汽化作为精馏塔II10的上升气;
冷凝蒸发器II11,用于将富氧液空和低压氮气进行换热,低压氮气被冷凝为低压液氮,富氧液空被汽化为污氮气;
过冷器12,用于将液空、液氮过冷,用于将污氮气复热;
液氮泵13,用于低压液氮增压。
上述低能耗双塔纯氮制取装置制取纯氮,包括如下步骤:
步骤一、将原料空气经过滤器1过滤掉灰尘和机械杂质后,进入透平空气压缩机2将空气压缩到设定压力0.5-1.0MPaA;之后经空气预冷机组3-1预冷至5-8℃后进入交替使用的分子筛吸附器4中纯化,将水分、CO2、C2H2等物质去除;
步骤二、将纯化后的原料空气部分用于仪表空气(图中未标示出),其余部分分为两股,一股直接进入主换热器6被返流气体冷却至饱和并带有一定含湿后进入精馏塔I8底部参与精馏;另一股经过膨胀机的增压端7-1增压及增压后冷却器3-2冷却后进入主换热器6被返流气体部分冷却至一定温度后,抽出进入膨胀机7膨胀制取装置所需冷量,膨胀后空气引入精馏塔II10底部参与精馏;
步骤三、空气经精馏塔I8精馏后分离为高压氮气和液空,高压氮气分成两股,一股直接引出经过主换热器6复热后出冷箱作为产品供用户,另一股引入冷凝蒸发器I9和富氧液空换热,高压氮气被冷凝为液氮,引出部分液氮进入精馏塔I8作为回流液,引出部分液氮经过冷器12过冷后节流进入精馏塔II10作为回流液,另引出其余部分液氮作为副产品;液空经过过冷器12过冷后节流进入精馏塔II10参与精馏;
步骤四、膨胀后空气、液空和液氮在精馏塔II10中被分离为低压氮气和富氧液空,引出部分低压氮气经主换热器6复热后作为产品供用户,其余低压氮气引入冷凝蒸发器II11;部分富氧液空被精馏塔I8引出的高压氮气汽化作为精馏塔II10的上升气,其余富氧液空经节流后引入冷凝蒸发器II11;
步骤五、在冷凝蒸发器II11中低压氮气和富氧液空进行换热,低压氮气被冷凝为低压液氮,富氧液空被汽化为污氮气;引出部分低压液氮经液氮泵13增压后引入精馏塔I8顶部作为回流液,其余低压液氮引入精馏塔II10顶部作为回流液;污氮气经过过冷器12、主换热器6复热后出冷箱,一部分由电加热器5加热后引入交替使用的分子筛吸附器4作为再生气,其余放空。
另一种纯氮制取装置,如图2所示,包括过滤器1、透平空气压缩机2、空气预冷机组3-1、交替使用的分子筛吸附器4、电加热器5、增压后冷却器3-2、主换热器6、膨胀机7、精馏塔I8、精馏塔II10、冷凝蒸发器I9、冷凝蒸发器II11、过冷器12、液氮泵13、冷箱,
过滤器1、透平空气压缩机2、空气预冷机组3-1、交替使用的分子筛吸附器4、电加热器5、增压后冷却器3-2、膨胀机的增压端7-1设于冷箱外,主换热器6、膨胀机7、精馏塔I8、精馏塔II10、冷凝蒸发器I9、冷凝蒸发器II11、过冷器12、液氮泵13设置于冷箱内,精馏塔II10设于精馏塔I8之上,冷凝蒸发器I9设于精馏塔I8和精馏塔II10之间,冷凝蒸发器II11设于精馏塔II10之上;
过滤器1、透平空气压缩机2、空气预冷机组3-1、交替使用的分子筛吸附器4依次连接,交替使用的分子筛吸附器4分别和主换热器6、膨胀机的增压端7-1连接,主换热器6和精馏塔I8底部的原料空气进口连接;膨胀机的增压端7-1和增压后冷却器3-2连接,增压后冷却器3-2和主换热器6连接,主换热器6的原料空气部分复热出口和膨胀机7连接,膨胀机7和主换热器6连接,主换热器6再连接至电加热器5;
精馏塔I8顶部的高压氮气出口分别和主换热器6、冷凝蒸发器I9连接,主换热器6连接外部管道以提供高压氮气产品,冷凝蒸发器I9的液氮出口分别和精馏塔I8顶部、冷箱外液氮存储罐连接,其中,冷凝蒸发器I9的液氮出口和精馏塔I8顶部的连接管路上设有角式冷阀;
精馏塔I8底部的液空出口和过冷器12连接,过冷器12再和精馏塔II10中部连接,其中,过冷器12和精馏塔II10中部连接的管路上设节流阀;
精馏塔II10顶部的低压氮气出口分别和主换热器6、冷凝蒸发器II11连接,主换热器6连接外部管道以提供低压氮气产品;
精馏塔II10底部的富氧液空出口和冷凝蒸发器II11连接,其连接管路上设有节流阀;
冷凝蒸发器II11的低压液氮出口分别和精馏塔II10顶部、液氮泵13连接,液氮泵13和精馏塔I8顶部连接,液氮泵13和精馏塔I8顶部的连接管路上设有角式冷阀;冷凝蒸发器II11的污氮气出口和过冷器12连接,过冷器12和主换热器6连接,主换热器6分别连接至电加热器5和外部放空管道,电加热器5再和交替使用的分子筛吸附器4连接。
上述各部件的功能如下:
过滤器1,用于过滤原料空气中的灰尘和机械杂质;
透平空气压缩机2,用于将过滤后的原料空气压缩到设定压力;
空气预冷机组3-1,用于将过滤、压缩后的原料空气预冷;
交替使用的分子筛吸附器4,用于将过滤、压缩、预冷后的原料空气纯化,去除水分、CO2、C2H2等物质;
电加热器5,用于加热污氮气和膨胀后空气以再生分子筛吸附器4;
增压后冷却器3-2,用于冷却经膨胀机的增压端7-1增压后的原料空气;
主换热器6,用于将过滤、压缩、预冷、纯化后的原料空气冷却;用于将过滤、压缩、预冷、纯化、增压、冷却后的原料空气部分冷却;用于将膨胀后空气复热、高压氮气复热、低压氮气复热、污氮气复热;
膨胀机7,用于将部分冷却后的原料空气膨胀制取冷箱必需冷量;
精馏塔I8,用于将经过滤、压缩、预冷、纯化、冷却后的原料空气低温精馏而分离为高压氮气和液空;
精馏塔II10,用于将液空精馏为低压氮气和富氧液空;
冷凝蒸发器I9,用于将高压氮气和富氧液空进行换热,高压氮气液化为液氮,富氧液空汽化作为精馏塔II10的上升气;
冷凝蒸发器II11,用于将富氧液空和低压氮气进行换热,低压氮气被冷凝为低压液氮,富氧液空被汽化为污氮气;
过冷器12,用于将液空过冷,用于将污氮气复热;
液氮泵13,用于低压液氮增压。
上述双塔正流纯氮制取装置制取纯氮,包括如下步骤:
步骤一、将原料空气经过滤器1过滤掉灰尘和机械杂质后,进入透平空气压缩机2将空气压缩到设定压力0.5-1.0MPaA;之后经空气预冷机组3-1预冷至5-8℃后进入交替使用的分子筛吸附器4中纯化,将水分、CO2、C2H2等物质去除;
步骤二、将纯化后的原料空气部分用于仪表空气(图中未标示出),其余部分分为两股,一股直接进入主换热器6被返流气体冷却至饱和并带有一定含湿后进入精馏塔I8底部参与精馏;另一股经过膨胀机的增压端7-1增压及增压后冷却器3-2冷却后进入主换热器6被返流气体部分冷却至一定温度后,抽出进入膨胀机7膨胀制取装置所需冷量,膨胀后空气经主换热器6复热后出冷箱,和后续部分污氮气混合,由电加热器5加热后引入交替使用的分子筛吸附器4作为再生气;
步骤三、空气经精馏塔I8精馏后分离为高压氮气和液空,高压氮气分成两股,一股直接引出经过主换热器6复热后出冷箱作为产品供用户,另一股引入冷凝蒸发器I9和富氧液空换热,高压氮气被冷凝为液氮,引出部分液氮进入精馏塔I8作为回流液,另引出其余部分液氮作为副产品;液空经过过冷器12过冷后节流进入精馏塔II10参与精馏;
步骤四、液空在精馏塔II10中被分离为低压氮气和富氧液空,引出部分低压氮气经主换热器6复热后作为产品供用户,其余低压氮气引入冷凝蒸发器II11;部分富氧液空被精馏塔I8引出的高压氮气汽化作为精馏塔II10的上升气,其余富氧液空经节流后引入冷凝蒸发器II11;
步骤五、在冷凝蒸发器II11中低压氮气和富氧液空进行换热,低压氮气被冷凝为低压液氮,富氧液空被汽化为污氮气;引出部分低压液氮经液氮泵13增压后引入精馏塔I8顶部作为回流液,其余低压液氮引入精馏塔II10顶部作为回流液;污氮气经过过冷器12、主换热器6复热后出冷箱,一部分和膨胀后空气混合,由电加热器5加热后引入交替使用的分子筛吸附器4作为再生气,其余放空。
Claims (4)
1.一种纯氮制取装置,其特征在于,包括过滤器、透平空气压缩机、空气预冷机组、交替使用的分子筛吸附器、电加热器、增压后冷却器、主换热器、膨胀机、精馏塔I、精馏塔II、冷凝蒸发器I、冷凝蒸发器II、过冷器、液氮泵、冷箱,
过滤器、透平空气压缩机、空气预冷机组、交替使用的分子筛吸附器、电加热器、增压后冷却器、膨胀机的增压端设于冷箱外,主换热器、膨胀机、精馏塔I、精馏塔II、冷凝蒸发器I、冷凝蒸发器II、过冷器、液氮泵设置于冷箱内,精馏塔II设于精馏塔I之上,冷凝蒸发器I设于精馏塔I和精馏塔II之间,冷凝蒸发器II设于精馏塔II之上;
过滤器、透平空气压缩机、空气预冷机组、交替使用的分子筛吸附器依次连接,交替使用的分子筛吸附器分别和主换热器、膨胀机的增压端连接,主换热器和精馏塔I底部的原料空气进口连接;膨胀机的增压端和增压后冷却器连接,增压后冷却器和主换热器连接,主换热器的原料空气部分复热出口和膨胀机连接,膨胀机再和精馏塔II底部的原料空气进口连接;
精馏塔I顶部的高压氮气出口分别和主换热器、冷凝蒸发器I连接,主换热器连接外部管道以提供高压氮气产品,冷凝蒸发器I的液氮出口分别和精馏塔I顶部、过冷器、冷箱外液氮存储罐连接,过冷器和精馏塔II顶部连接,其中,冷凝蒸发器I的液氮出口和精馏塔I顶部的连接管路上设有角式冷阀,过冷器和精馏塔II顶部的连接管路上设有节流阀;
精馏塔I底部的液空出口和过冷器连接,过冷器再和精馏塔II中部连接,其中,过冷器和精馏塔II中部连接的管路上设节流阀;
精馏塔II顶部的低压氮气出口分别和主换热器、冷凝蒸发器II连接,主换热器连接外部管道以提供低压氮气产品;
精馏塔II底部的富氧液空出口和冷凝蒸发器II连接,其连接管路上设有节流阀;
冷凝蒸发器II的低压液氮出口分别和精馏塔II顶部、液氮泵连接,液氮泵和精馏塔I顶部连接,液氮泵和精馏塔I顶部的连接管路上设有角式冷阀;冷凝蒸发器II的污氮气出口和过冷器连接,过冷器和主换热器连接,主换热器分别和电加热器、外部放空管道连接,电加热器和交替使用的分子筛吸附器连接。
2.根据权利要求1所述的纯氮制取装置,其特征在于,膨胀机不和精馏塔II连接,而和主换热器连接,主换热器再连接至电加热器;冷凝蒸发器I的液氮出口分别和精馏塔I顶部、冷箱外液氮存储罐连接,其中,冷凝蒸发器I的液氮出口和精馏塔I顶部的连接管路上设有角式冷阀。
3.利用权利要求1所述的纯氮制取装置进行纯氮制取,其特征在于,包括如下步骤:
步骤一、将原料空气经过滤器过滤掉灰尘和机械杂质后,进入透平空气压缩机将空气压缩到设定压力;之后经空气预冷机组预冷后进入交替使用的分子筛吸附器中纯化;
步骤二、将纯化后的原料空气部分用于仪表空气,其余部分分为两股,一股直接进入主换热器被返流气体冷却至饱和并带有一定含湿后进入精馏塔I底部参与精馏;另一股经过膨胀机的增压端增压及增压后冷却器冷却后进入主换热器被返流气体部分冷却至一定温度后,抽出进入膨胀机膨胀制取装置所需冷量,膨胀后空气引入精馏塔II底部参与精馏;
步骤三、空气经精馏塔I精馏后分离为高压氮气和液空,高压氮气分成两股,一股直接引出经过主换热器复热后出冷箱作为产品供用户,另一股引入冷凝蒸发器I和富氧液空换热,高压氮气被冷凝为液氮,引出部分液氮进入精馏塔I作为回流液,引出部分液氮经过冷器过冷后节流进入精馏塔II作为回流液,另引出其余部分液氮作为副产品;液空经过过冷器过冷后节流进入精馏塔II参与精馏;
步骤四、膨胀后空气、液空和液氮在精馏塔II中被分离为低压氮气和富氧液空,引出部分低压氮气经主换热器复热后作为产品供用户,其余低压氮气引入冷凝蒸发器II;部分富氧液空被精馏塔I引出的高压氮气汽化作为精馏塔II的上升气,其余富氧液空经节流后引入冷凝蒸发器II;
步骤五、在冷凝蒸发器II中低压氮气和富氧液空进行换热,低压氮气被冷凝为低压液氮,富氧液空被汽化为污氮气;引出部分低压液氮经液氮泵增压后引入精馏塔I顶部作为回流液,其余低压液氮引入精馏塔II顶部作为回流液;污氮气经过过冷器、主换热器复热后出冷箱,一部分由电加热器加热后引入交替使用的分子筛吸附器作为再生气,其余放空。
4.利用权利要求2所述的纯氮制取装置进行纯氮制取,其特征在于,包括如下步骤:
步骤一、将原料空气经过滤器过滤掉灰尘和机械杂质后,进入透平空气压缩机将空气压缩到设定压力;之后经空气预冷机组预冷后进入交替使用的分子筛吸附器中纯化,将水分、CO2、C2H2等物质去除;
步骤二、将纯化后的原料空气部分用于仪表空气,其余部分分为两股,一股直接进入主换热器被返流气体冷却至饱和并带有一定含湿后进入精馏塔I底部参与精馏;另一股经过膨胀机的增压端增压及增压后冷却器冷却后进入主换热器被返流气体部分冷却至一定温度后,抽出进入膨胀机膨胀制取装置所需冷量,膨胀后空气经主换热器复热后出冷箱,和后续部分污氮气混合,由电加热器加热后引入交替使用的分子筛吸附器作为再生气;
步骤三、空气经精馏塔I精馏后分离为高压氮气和液空,高压氮气分成两股,一股直接引出经过主换热器复热后出冷箱作为产品供用户,另一股引入冷凝蒸发器I和富氧液空换热,高压氮气被冷凝为液氮,引出部分液氮进入精馏塔I作为回流液,另引出其余部分液氮作为副产品;液空经过过冷器过冷后节流进入精馏塔II参与精馏;
步骤四、液空在精馏塔II中被分离为低压氮气和富氧液空,引出部分低压氮气经主换热器复热后作为产品供用户,其余低压氮气引入冷凝蒸发器II;部分富氧液空被精馏塔I引出的高压氮气汽化作为精馏塔II的上升气,其余富氧液空经节流后引入冷凝蒸发器II;
步骤五、在冷凝蒸发器II中低压氮气和富氧液空进行换热,低压氮气被冷凝为低压液氮,富氧液空被汽化为污氮气;引出部分低压液氮经液氮泵增压后引入精馏塔I顶部作为回流液,其余低压液氮引入精馏塔II顶部作为回流液;污氮气经过过冷器、主换热器复热后出冷箱,一部分和膨胀后空气混合,由电加热器加热后引入交替使用的分子筛吸附器作为再生气,其余放空。
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