CN105110291A - 一种焦炉煤气回收制lng联产合成氨的方法 - Google Patents
一种焦炉煤气回收制lng联产合成氨的方法 Download PDFInfo
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- CN105110291A CN105110291A CN201510427832.6A CN201510427832A CN105110291A CN 105110291 A CN105110291 A CN 105110291A CN 201510427832 A CN201510427832 A CN 201510427832A CN 105110291 A CN105110291 A CN 105110291A
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- Prior art keywords
- gas
- synthetic ammonia
- lng
- coke
- oven gas
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- 238000004519 manufacturing process Methods 0.000 title abstract description 4
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- 238000002156 mixing Methods 0.000 claims description 3
- UFWIBTONFRDIAS-UHFFFAOYSA-N naphthalene Chemical compound 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C1=CC=CC2=CC=CC=C21 UFWIBTONFRDIAS-UHFFFAOYSA-N 0.000 claims description 3
- 239000003921 oils Substances 0.000 claims description 3
- 238000003795 desorption Methods 0.000 claims description 2
- 238000007599 discharging Methods 0.000 claims 1
- 238000000926 separation method Methods 0.000 abstract description 4
- 239000002994 raw materials Substances 0.000 abstract description 3
- 230000015572 biosynthetic process Effects 0.000 abstract description 2
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Abstract
本发明公开了一种焦炉煤气回收制LNG联产合成氨的方法，包括以下步骤：气体净化，CO转换，气体分离，制LNG，合成氨。本发明可以解决焦炉煤气中CO和N2难以分离的问题，同时可以解决H2S排放的问题，脱除的H2S、多碳碳氢化合物和CO2可以回炉燃烧，而且热值较高，本方案原料利用率高，提高了焦炉煤气的生产附加值。
Description
技术领域
[0001] 本发明涉及一种焦炉煤气回收制LNG联产合成氨的方法，属于化工合成领域。
背景技术
[0002]中国是世界上焦炭产量最大的国家，在制取焦炭时会产生大量的焦炉煤气，其组成包括 H2 (55-60%), CH4 (23〜27%)、CO (5~8%)、多碳碳氢化合物(2~4%)、CO2 (1.5-3%), N2(3-7%), O2 (0.3-0.8%)和少量稀有气体。如果能合理利用这一资源，每年可以节约数千万吨标准煤。
[0003] 现有焦炭厂焦炉煤气一般用作燃料燃烧、发电或者作为原料制取甲醇、LNG，但都存在价值利用率低的问题。作为燃料用于锅炉或者钢厂乳钢加热时，由于其中H2热值较低，直接燃烧并不合算。用于国内燃气内燃机发电时，同样由于H2热值低，发电效率不高，每方焦炉气仅发1.1度电，且随着时间发电效率越低，价值更低。用焦炉煤气生产甲醇时，存在CO和N2分离困难的问题，尤其对氧含量达到0.6%以上时，分离难度更大，设备投资巨大；利用焦炉煤气制作LNG需要将其中的H2、C0、C02转化成甲烷，同样投资较大，而且甲烷化过程中一部分H2转化成H 20，原料损失较大。
发明内容
[0004] 本发明目的就在于克服上述不足，提供一种焦炉煤气回收制LNG联产合成氨的方法，具体包括以下步骤:
1)气体净化，焦炉煤气进入焦炉煤气气柜进行缓冲后，再依次经过电捕油，TSA脱萘脱焦油，加压后通过干法净化除氧脱硫脱汞，得到净化后的I级混合气体；
2)C0转换，将I级混合气体通入变换器进行转换，混合气体中的CO与水蒸气反应转换为比和CO 2，得到2级混合气体；
3)气体分离，将2级混合气体经过PSA变压吸附粗脱碳，大部分多碳碳氢化合物、H2S和CO2被吸附脱除后，再经过分子筛深度脱碳脱水，最后经过膜分离出H2，得到高014浓度的3级混合气体；
4)制LNG，3级混合气体进入冷箱，经液化后制得LNG，液化后剩余的气体通过低压闪蒸塔分离得到4级混合气体；
5)合成氨，4级混合气体通过加压醇烃化，再与步骤3)中膜分离得到的H2混合，再通过补氮调节氢氮比，进入合成氨塔合成氨。
[0005] 进一步，步骤I)中加压后的气体压力为2.4MPa。
[0006] 进一步，步骤3)中经PSA和分子筛吸附的多碳碳氢化合物、H2S和CO2经解吸附后回炉燃烧。
[0007] 进一步，步骤5)中氢氮比按体积比为3:1。
[0008] 进一步，步骤5)合成氨的过程中有合成氨弛放气，驰放气主要是CH4、H2、N2、Ar，通过膜分离出H2，将H2补充到合成氨塔中，余下的混合气循环进入冷箱将混合气中的CH4制成LNG，当AR富集到一定浓度后排放驰放气以释放AR。
[0009] 本发明的有益点在于:1.通过变换将CO与水蒸气反应转换成&和CO 2，巧妙的解决了焦炉煤气中CO和N2较难分离的问题，同时转换生成的H2和分离出的N2又可以作为合成氨的原料，提高了原料利用率。2.通过变压吸附粗脱碳工序脱掉了大部分碳氢化合物、H2S,以及CO2，将这部分气体回炉燃烧。脱碳的同时既将H2S脱除，解决H2S排放问题，又脱除了多碳碳氢化合物，提高了后工段LNG的品质；同时脱除的H2S、碳氢化合物和CO2还可以回炉燃烧，多碳碳氢化合物热值较高，与C(V混合还能保证热值，达到掺烧热值要求。3.通过合成氨后膜分离将H2、CH4、N2分离，循环利用。本方案可以将焦炉煤气的有效成分均回收利用，几乎无损失，提高了焦炉煤气的生产附加值。
附图说明
[0010] 图1是本发明流程不意图。
具体实施方式
[0011] 下面结合附图以及具体实施例对本发明作进一步描述，在此发明的示意性实施例以及说明用来解释本发明，但并不作为对本发明的限定。
[0012] 如图1所示的一种焦炉煤气回收制LNG联产合成氨的方法，包括以下步骤:
1)气体净化，焦炉煤气进入焦炉煤气气柜进行缓冲后，再依次经过电捕油，TSA脱萘脱焦油，加压到2.4MPa后通过干法净化除氧脱硫脱汞，得到净化后的I级混合气体；
2)C0转换，将I级混合气体通入变换器进行转换，混合气体中的CO与水蒸气反应转换为比和CO 2，得到2级混合气体；
3)气体分离，将2级混合气体经过PSA变压吸附粗脱碳，大部分多碳碳氢化合物、H2S和CO2被吸附脱除后，再经过分子筛深度脱碳脱水，最后经过膜分离出H2，得到高014浓度的3级混合气体；
4)制LNG，3级混合气体进入冷箱，经液化后制得LNG，液化后剩余的气体通过低压闪蒸塔分离得到4级混合气体；
5)合成氨，4级混合气体通过加压醇烃化，再与步骤3)中膜分离得到的H2混合，再通过补氮调节氢氮体积比至3:1，进入合成氨塔合成氨。
[0013] 合成氨的过程中有合成氨弛放气，驰放气主要是CH4、H2、N2、Ar，通过膜分离出H2,将H2补充到合成氨塔中，余下的混合气循环进入冷箱将混合气中的CH4制成LNG，当AR富集到一定浓度后排放驰放气以释放AR。
[0014] 本发明的技术方案不限于上述具体实施例的限制，凡是根据本发明的技术方案做出的技术变形，均落入本发明的保护范围之内。
Claims (5)
1.一种焦炉煤气回收制LNG联产合成氨的方法，包括以下步骤: 1)气体净化，焦炉煤气进入焦炉煤气气柜进行缓冲后，再依次经过电捕油，TSA脱萘脱焦油，加压后通过干法净化除氧脱硫脱汞，得到净化后的I级混合气体； 2)C0转换，将I级混合气体通入变换器进行转换，混合气体中的CO与水蒸气反应转换为比和CO 2，得到2级混合气体； 3)气体分离，将2级混合气体经过PSA变压吸附粗脱碳，大部分多碳碳氢化合物、H2S和CO2被吸附脱除后，再经过分子筛深度脱碳脱水，最后经过膜分离出H2，得到高014浓度的3级混合气体； 4)制LNG，3级混合气体进入冷箱，经液化后制得LNG，液化后剩余的气体通过低压闪蒸塔分离得到4级混合气体； 5)合成氨，4级混合气体通过加压醇烃化，再与步骤3)中膜分离得到的H2混合，再通过补氮调节氢氮比，进入合成氨塔合成氨。
2.根据权利要求1所述的一种焦炉煤气回收制LNG联产合成氨的方法，其特征在于:所述的步骤I)中加压后的气体压力为2.4MPa。
3.根据权利要求1所述的一种焦炉煤气回收制LNG联产合成氨的方法，其特征在于:所述的步骤3)中经PSA和分子筛吸附的多碳碳氢化合物、H2S和0)2经解吸附后回炉燃烧。
4.根据权利要求1所述的一种焦炉煤气回收制LNG联产合成氨的方法，其特征在于:所述的步骤5)中氢氮比按体积为3:1。
5.根据权利要求1所述的一种焦炉煤气回收制LNG联产合成氨的方法，其特征在于:所述的步骤5)合成氨的过程中有合成氨弛放气，驰放气主要是CH4、H2、N2、Ar，通过膜分离出H2,将H2补充到合成氨塔中，余下的混合气循环进入冷箱将混合气中的CH 4制成LNG，当AR富集后排放驰放气以释放AR。
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