CN106568298A - 一种焦炉气制lng联产合成氨装置及控制方法 - Google Patents

一种焦炉气制lng联产合成氨装置及控制方法 Download PDF

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CN106568298A
CN106568298A CN201610955145.6A CN201610955145A CN106568298A CN 106568298 A CN106568298 A CN 106568298A CN 201610955145 A CN201610955145 A CN 201610955145A CN 106568298 A CN106568298 A CN 106568298A
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nitrogen
valve
heat exchanger
main heat
pressure
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章有虎
王晋
苟文广
陈环琴
李猛
杨巧玉
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HANGZHOU ZHONGTAI CRYOGENIC TECHNOLOGY Co Ltd
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Abstract

本发明公开了一种焦炉气制LNG联产合成氨装置及控制方法。该装置包括限流阀、第一冷却器、中压配氮压缩机、第二冷却器、第一手动阀、第一压力控制系统、调节阀、第二压力控制系统、流量控制系统、再沸器、第三冷却器、第四冷却器、第二手动阀、物位阀、主换热器、物位指示仪、低压脱氮塔、压力阀、第三手动阀、高压脱氢塔、第四手动阀、氮氢回收压缩机以及各类管路；采用本发明制LNG，塔顶采用冷热流体混合换热工艺，并且通过液氮的洗涤吸收，可以使高压塔顶气不含甲烷，塔顶含氮气量增加，正好为氢气配氮。此工艺非常适合LNG联产合成氨，通过液氮洗工艺使出高压洗涤塔的合成气氮气含量增加，并满足去合成氨的合成气氢氮比为3：1，此工艺可以使系统能耗降低，并且没有驰放气，省去了驰放气氨洗工序。

Description

一种焦炉气制LNG联产合成氨装置及控制方法
技术领域
本发明涉及化工深冷净化分离装置，尤其涉及一种焦炉气制LNG联产合成氨装置及控制方法。
背景技术
目前国内LNG原料气来源主要分为管道天然气制LNG、焦炉气制LNG、煤制气制LNG等几种主要工艺路线。其中管道天然气液化工艺的经典流程是采用单混合冷剂流程(SMRC)，制冷单元主要配置为一台混合冷剂压缩机和一台冷箱。焦炉气制LNG的常规流程为，一台混合冷剂压缩机为装置提供主要冷量，一台氮气循环压缩机，为分离原料气的高压精馏塔和低压精馏塔塔顶提供冷源。煤制天然气的工艺路线和焦炉气基本一样，主要是看甲烷化后原料气中甲烷的含量以及产品用途，选择不同的液化工艺路线。
常规双塔流程，塔顶采用间壁式换热器，制冷液氮不与原料气接触，因此存在冷热流体的温差损失以及换热器的热阻损失，其适用于焦炉气制甲醇等塔顶只需氢气的工艺路线。此工艺高压塔顶气体氢气纯度相对较高，氮气含量少，并且含有少量甲烷。如要求甲烷含量很低时，则需要塔顶的制冷温度很低，并且能耗很高。
发明内容
本发明的目的是克服现有技术的不足，提供一种焦炉气制LNG联产合成氨装置及控制方法。
一种焦炉气制LNG联产合成氨装置，其特征在于包括限流阀、第一冷却器、中压配氮压缩机、第二冷却器、第一手动阀、第一压力控制系统、调节阀、第二压力控制系统、流量控制系统、再沸器、第三冷却器、第四冷却器、第二手动阀、物位阀、主换热器、物位指示仪、低压脱氮塔、压力阀、第三手动阀、高压脱氢塔、第四手动阀、氮氢回收压缩机；
空分氮气管路分别穿过限流阀、第一冷却器、中压配氮压缩机、第二冷却器进入主换热器，空分氮气管路穿出主换热器后分成两路,一路穿过第一手动阀与再沸器连接，另一路穿过第四手动阀与高压脱氢塔相连；
原料焦炉气管路穿过调节阀进入主换热器，原料焦炉气管路穿出主换热器再穿过低压脱氮塔，然后再顺次穿过主换热器、第三手动阀进入高压脱氢塔；
来自BOG压缩机的焦炉气管路进入低压脱氮塔，低压脱氮塔与再沸器相连；
氮氢混合管路由高压脱氢塔塔顶穿出后分别穿过主换热器、第二压力控制系统进入合成氨工序；
冷凝液管路由高压脱氢塔塔底穿出后穿过压力阀进入低压脱氮塔；
再沸器顶部穿出的氮气管路穿过主换热器与位于冷限流阀与第一冷却器之间的空分氮气管路相连；再沸器侧边穿出焦油气管路依次穿过主换热器、第二压力控制系统、氮氢回收压缩机后与原料焦炉气管路相连；
LNG管路由低压脱氮塔塔底穿出后分别穿过主换热器、物位阀进入LNG储罐；
一号混合冷剂管路依次穿过主换热器、第二手动阀、第四冷却器、主换热器；
二号混合冷剂管路依次穿过主换热器、流量控制系统、第三冷却器、主换热器、流量控制系统。
作为优选，所述的一种焦炉气制LNG联产合成氨装置，其特征在于所述的高压脱氢塔顶部氮氢混合管路中合成气氮氢比为3:1。
作为优选，所述的一种焦炉气制LNG联产合成氨装置，其特征在于所述的第一压力控制系统由压力阀和压力指示控制组成。
作为优选，所述的焦炉气制LNG联产合成氨装置的控制方法，其特征在于包括以下步骤：
1)打开第二手动阀，一号混合冷剂依次穿过主换热器、第二手动阀、第四冷却器，再进入主换热器，此时，二号混合冷剂穿过主换热器、流量控制系统，再进入主换热器与一号混合冷剂穿出主换热器。
2)原料焦炉气a经过调节阀进入主换热器冷却第一次液化得到液态焦炉气,进入低压脱氮塔分离出氮气，再进入主换热器冷却第二次液化得到液态氢气和LNG的混合物，打开第三手动阀，液态氢气和液态甲烷混合物进入高压脱氢塔将氢气和LNG分离。
3)打开限流阀、第一手动阀与第四手动阀，空分氮气穿过限流阀、第一冷却器、中压配氮压缩机、第二冷却器后进入主换热器冷却液化得到液氮，液氮进入高压脱氢塔与低压脱氮塔；
4)进入低压脱氮塔的液氮从再沸器顶部流出，穿过主换热器后与空分氮气混合；
5)低压脱氮塔中产生的氮气流出穿过压力阀进入高压脱氢塔，与从第四手动阀进入的液氮和高压脱氢塔分离出的氢气混合，利用压力阀控制氮气流入的量使得氮氢比例1：3；
6)高压脱氢塔中分里出来的LNG进入LNG储罐，物位阀对LNG储罐中的量进行控制；
采用本发明制LNG，塔顶采用冷热流体混合换热工艺，并且通过液氮的洗涤吸收，可以使高压塔顶气不含甲烷，塔顶含氮气量增加，正好为氢气配氮。此工艺非常适合LNG联产合成氨，通过液氮洗工艺使出高压洗涤塔的合成气氮气含量增加，并满足去合成氨的合成气氢氮比为3：1，此工艺可以使系统能耗降低，并且没有驰放气，省去了驰放气氨洗工序。
附图说明
图1为焦炉气制LNG联产合成氨装置示意图；
图中，限流阀1、第一冷却器2、中压配氮压缩机3、第二冷却器4、第一手动阀5、第一压力控制系统6、调节阀7、第二压力控制系统8、流量控制系统9、再沸器10、第三冷却器11、第四冷却器12、第二手动阀13、物位阀14、主换热器15、物位指示仪16、低压脱氮塔17、压力阀18、第三手动阀19、高压脱氢塔20、第四手动阀21、氮氢回收压缩机22。
具体实施方式
如图1所示，一种焦炉气制LNG联产合成氨装置，其特征在于包括限流阀1、第一冷却器2、中压配氮压缩机3、第二冷却器4、第一手动阀5、第一压力控制系统6、调节阀7、第二压力控制系统8、流量控制系统9、再沸器10、第三冷却器11、第四冷却器12、第二手动阀13、物位阀14、主换热器15、物位指示仪16、低压脱氮塔17、压力阀18、第三手动阀19、高压脱氢塔20、第四手动阀21、氮氢回收压缩机22；
空分氮气管路分别穿过限流阀1、第一冷却器2、中压配氮压缩机3、第二冷却器4进入主换热器15，空分氮气管路穿出主换热器15后分成两路,一路穿过第一手动阀5与再沸器10连接，另一路穿过第四手动阀21与高压脱氢塔20相连；
原料焦炉气管路穿过调节阀7进入主换热器15，原料焦炉气管路穿出主换热器15再穿过低压脱氮塔17，然后再顺次穿过主换热器15、第三手动阀19进入高压脱氢塔20；
来自BOG压缩机的焦炉气管路进入低压脱氮塔17，低压脱氮塔17与再沸器10相连；
氮氢混合管路由高压脱氢塔20塔顶穿出后分别穿过主换热器15、第二压力控制系统8进入合成氨工序；
冷凝液管路由高压脱氢塔20塔底穿出后穿过压力阀18进入低压脱氮塔17；
再沸器10顶部穿出的氮气管路穿过主换热器15与位于冷限流阀1与第一冷却器2之间的空分氮气管路相连；再沸器10侧边穿出焦油气管路依次穿过主换热器15、第二压力控制系统8、氮氢回收压缩机22后与原料焦炉气管路相连；
LNG管路由低压脱氮塔17塔底穿出后分别穿过主换热器15、物位阀14进入LNG储罐；
一号混合冷剂管路依次穿过主换热器15、第二手动阀13、第四冷却器12、主换热器15；
二号混合冷剂管路依次穿过主换热器15、流量控制系统9、第三冷却器11、主换热器15、流量控制系统9。
一种焦炉气制LNG联产合成氨装置，其特征在于所述的高压脱氢塔20顶部氮氢混合管路中合成气氮氢比为3:1。
一种焦炉气制LNG联产合成氨装置，其特征在于所述的第一压力控制系统6由压力阀和压力指示控制组成。
一种焦炉气制LNG联产合成氨装置的控制方法，其特征在于包括以下步骤：
1)打开第二手动阀13，一号混合冷剂依次穿过主换热器15、第二手动阀13、第四冷却器12，再进入主换热器15，此时，二号混合冷剂穿过主换热器15、流量控制系统9，再进入主换热器15与一号混合冷剂穿出主换热器15。
2)原料焦炉气a经过调节阀7进入主换热器15冷却第一次液化得到液态焦炉气,进入低压脱氮塔17分离出氮气，再进入主换热器15冷却第二次液化得到液态氢气和LNG的混合物，打开第三手动阀19，液态氢气和液态甲烷混合物进入高压脱氢塔20将氢气和LNG分离。
3)打开限流阀1、第一手动阀5与第四手动阀21，空分氮气穿过限流阀1、第一冷却器2、中压配氮压缩机3、第二冷却器4后进入主换热器15冷却液化得到液氮，液氮进入高压脱氢塔20与低压脱氮塔17；
4)进入低压脱氮塔17的液氮从再沸器10顶部流出，穿过主换热器15后与空分氮气混合；
5)低压脱氮塔17中产生的氮气流出穿过压力阀18进入高压脱氢塔20，与从第四手动阀21进入的液氮和高压脱氢塔20分离出的氢气混合，利用压力阀18控制氮气流入的量使得氮氢比例1：3；
6)高压脱氢塔20中分里出来的LNG进入LNG储罐，物位阀14对LNG储罐中的量进行控制。

Claims (4)

1.一种焦炉气制LNG联产合成氨装置，其特征在于包括限流阀(1)、第一冷却器(2)、中压配氮压缩机(3)、第二冷却器(4)、第一手动阀(5)、第一压力控制系统(6)、调节阀(7)、第二压力控制系统(8)、流量控制系统(9)、再沸器(10)、第三冷却器(11)、第四冷却器(12)、第二手动阀(13)、物位阀(14)、主换热器(15)、物位指示仪(16)、低压脱氮塔(17)、压力阀(18)、第三手动阀(19)、高压脱氢塔(20)、第四手动阀(21)、氮氢回收压缩机(22)；
空分氮气管路分别穿过限流阀(1)、第一冷却器(2)、中压配氮压缩机(3)、第二冷却器(4)进入主换热器(15)，空分氮气管路穿出主换热器(15)后分成两路,一路穿过第一手动阀(5)与再沸器(10)连接，另一路穿过第四手动阀(21)与高压脱氢塔(20)相连；
原料焦炉气管路穿过调节阀(7)进入主换热器(15)，原料焦炉气管路穿出主换热器(15)再穿过低压脱氮塔(17)，然后再顺次穿过主换热器(15)、第三手动阀(19)进入高压脱氢塔(20)；
来自BOG压缩机的焦炉气管路进入低压脱氮塔(17)，低压脱氮塔(17)与再沸器(10)相连；
氮氢混合管路由高压脱氢塔(20)塔顶穿出后分别穿过主换热器(15)、第二压力控制系统(8)进入合成氨工序；
冷凝液管路由高压脱氢塔(20)塔底穿出后穿过压力阀(18)进入低压脱氮塔(17)；
再沸器(10)顶部穿出的氮气管路穿过主换热器(15)与位于冷限流阀(1)与第一冷却器(2)之间的空分氮气管路相连；再沸器(10)侧边穿出焦油气管路依次穿过主换热器(15)、第二压力控制系统(8)、氮氢回收压缩机(22)后与原料焦炉气管路相连；
LNG管路由低压脱氮塔(17)塔底穿出后分别穿过主换热器(15)、物位阀(14)进入LNG储罐；
一号混合冷剂管路依次穿过主换热器(15)、第二手动阀(13)、第四冷却器(12)、主换热器(15)；
二号混合冷剂管路依次穿过主换热器(15)、流量控制系统(9)、第三冷却器(11)、主换热器(15)、流量控制系统(9)。
2.根据权利要求1所述的一种焦炉气制LNG联产合成氨装置，其特征在于所述的高压脱氢塔(20)顶部氮氢混合管路中合成气氮氢比为3:1。
3.根据权利要求1所述的一种焦炉气制LNG联产合成氨装置，其特征在于所述的第一压力控制系统(6)由压力阀和压力指示控制组成。
4.一种如权利要求1所述的焦炉气制LNG联产合成氨装置的控制方法，其特征在于包括以下步骤：
1)打开第二手动阀(13)，一号混合冷剂依次穿过主换热器(15)、第二手动阀(13)、第四冷却器(12)，再进入主换热器(15)，此时，二号混合冷剂穿过主换热器(15)、流量控制系统(9)，再进入主换热器(15)与一号混合冷剂穿出主换热器(15)；
2)原料焦炉气经过调节阀(7)进入主换热器(15)第一次冷却液化得到液态焦炉气,进入低压脱氮塔(17)分离出氮气，再进入主换热器(15)第二次冷却液化得到液态氢气和LNG的混合物，打开第三手动阀(19)，液态氢气和液态甲烷混合物进入高压脱氢塔(20)将氢气和LNG分离；
3)打开限流阀(1)、第一手动阀(5)与第四手动阀(21)，空分氮气穿过限流阀(1)、第一冷却器(2)、中压配氮压缩机(3)、第二冷却器(4)后进入主换热器(15)冷却液化得到液氮，液氮进入高压脱氢塔(20)与低压脱氮塔(17)；
4)进入低压脱氮塔(17)的液氮从再沸器(10)顶部流出，穿过主换热器(15)后与空分氮气混合；
5)低压脱氮塔(17)中产生的氮气流出穿过压力阀(18)进入高压脱氢塔(20)，与从第四手动阀(21)进入的液氮和高压脱氢塔(20)分离出的氢气混合，利用压力阀(18)控制氮气流入的量使得氮氢比例1：3；
6)高压脱氢塔(20)中分离出来的LNG进入LNG储罐，物位阀(14)对LNG储罐中的量进行控制。
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Application publication date: 20170419