工艺描述中英文.docx

1、工艺描述中英文Page 1 of 11Process Description 工艺描述x0119.07.2010M. SchmidtM. WarterM. SchmidtStatusIssueDateDescriptionPrepared byChecked byApproved byForm: &AA-Q-PP 2020.610.014 (EN) / Issue 01 dated 3.6.09Refer to protection notice ISO 16016Table of Contents 1 GENERAL总则. 32 PROCESS UNITS 工艺单元. 32.1 PROCES

2、S UNIT 11 INLET FACILITIES 工艺单元11-入口设备 . . 42.2 PROCESS UNIT 13 MERCURY-REMOVAL 工艺单元13 汞脱除. 42.3 PROCESS UNIT 12 CO2 REMOVAL 工艺单元12- CO2 脱除 . 42.4 PROCESS UNIT 16 DEHYDRATION工艺单元 16-脱水. 62.5 PROCESS UNIT 23 NATURAL GAS LIQUEFACTION工艺单元23 天然气液化 . . 82.6 PROCESS UNIT 41 - MRC COMPRESSION工艺单元41-MRC压缩 .

3、 92.7 PROCESS UNIT 47 MRC MAKE-UP UNIT 工艺单元47-MRC补充单元. 102.8 PROCESS UNIT 78 TANK RETURN GAS COMPRESSION 工艺单元78-储罐返回气压缩. 101 General 总述The LNG Plant is designed for a production of approx. 1200 tons per day net LNG equivalent to a natural gas feed flow of 62500 Nm/h. The plant is capable to operate

4、at 50-110 % of design capacity.LNG装置设计LNG生产能力约1200吨/天， 净液化天然气相当于天然气原料气流率62500 标方/小时。 该工厂能在设计能力50110的负荷下运行。 The plant consists of following process units: (Please refer to the Block Diagram, doc. no. &AA P-FD 1001.001 inAttachment 1-1)Downstream of the Feed Gas Inlet Facilities (Unit 11) the feed gas

5、 is freed from mercury (Unit 13). Subsequently the feed gas is sweetened in the CO2 removal unit (Unit 12), before the sweet feed gas is dehydrated (Unit 16).此装置由以下工艺单元组成：（请参照附件1-1的方框图， 文件编号&AA P-FD 1001.001 ）经过下游的原料气入口过滤（单元11）， 原料气与汞分离 (单元13)，与氧分离(单元14)。 随后，原料气在二氧化碳脱除单元（单元12）中被低硫化，然后，低硫原料气进行脱水（单元16

6、）。The dry and pretreated feed gas is then liquefied and subcooled (Unit 23) by means of a mixed refrigerant cycle(Unit 41). A part of the nitrogen contained in the feed gas is removed and released to atmosphere.在23单元， 干燥、预热的原料气通过混合制冷剂循环（单元41）液化、过冷。 原料气中的一部分氮气被脱除， 排放到大气中。 The produced LNG is stored s

7、lightly above ambient pressure and facilities are provided to export this LNG via trucks (Unit 73).产生的LNG在略高于环境压力下存储，并提供设施经装车(单元73)出口LNG。The liquefaction process is based on a patented and highly efficient single mixed refrigerant cycle. The main equipment of the liquefaction unit consists of a robu

8、st spiral wound heat exchanger and a barrel type compressor driven by an variable speed electrical motor.液化工艺采用高效的单混合制冷剂循环专利技术。液化单元的主要设备由运行稳定的螺旋缠绕换热器和一个由变速电机驱动的筒式压缩机组成。 2 Process Units工艺单元(Please refer to the Process Flow Diagrams, doc. no. &AA P-FF 1001 to 1009 and the Material Balance, doc. No.&AA

9、 P-CB 1012)（请参照工艺流程图， 文件编号：&AA P-FF 1001 1009 和物料热平衡，文件编号&AA P-CB 1012。）The below figures are valid for operation with feed gas No. 7 Gas Source (design case) under design conditions (feed pressure 4.5 MPag, feed temperature 21C, ambient temperature 21C) with an LNG net production of approx. 1200 to

10、ns/day.以下数据适用于7号气源（设计工况）在设计条件下（进料压力4.5 MPag,，进料温度21C，环境温度21C），LNG净产量约1200吨/天。2.1 Process Unit 11 Inlet Facilities 工艺单元 11-入口设备(Refer to PFD &AA P-FP 1001.001) （请参照PFD &AA P-FP 1001.001）Feed gas is received from battery limit (BL01) with a pressure of at least 4.6 MPa a and a temperature of +21 C. Po

11、ssible impurities in the feed gas, like solid particles from erosion in the pipeline or condensed free water, are removed in the Inlet Filter Separator 11S01 to prevent damages on downstream equipment.Feed gas composition will be analysed by on-line analyser. Pressure will be controlled to 4.55 MPa

12、and temperature is controlled by Feed Gas Preheater located OBL (outside battery limit) to a minimum of 16C to avoid hydrate formation in 12E05. After filtration the feed gas is fed to the Mercury Removal Unit.来自界区(BL01)的原料气，压力至少4.6MPag，温度21。为防止损坏下游设备，原料气中可能存在的杂质，如管道锈蚀产生的固体颗粒或自由冷凝水，在入口过滤器分离器11 S01排除

13、。 在线分析仪分析原料气组分。原料气 压力控制到4.55MPa, 为避免在原料气加热器12E05形成水合物，位于界区外（OBL）的原料气预加热器加热气体， 温度被控制到不低于16C。过滤后原料气被送入脱汞单元。 2.2 Process Unit 13 Mercury-Removal工艺单元 13- 汞脱除 (Refer to PFD &AA P-FP 1001.001)（请参照PFD&AA P-FP 1001.001）The filtered feed gas is warmed up in Feed Gas Heater 12E05 A/B to approx. 40 C against s

14、weet feed gas leaving the Amine Wash Column 12T01 at 43 C. The warmed up (and superheated) feed gas is then freed from mercury in Mercury Adsorber 13A01. Mercury Adsorber Filter 13S01 serves as a guard and ensures that no particles from the adsorbent are carried over to the downstream process facili

15、ties. A substitution of the exhausted mercury adsorber bed by a new one is necessary after several years.经过滤的原料气在原料气加热器12E05 A/B 中被加热至约40， 低硫化的原料气离开胺洗塔12T01时加热至43。 随后， 加热（过热）的原料气在汞吸附塔13A01中与汞分离。 汞吸附塔过滤器13S01做为防护屏障， 保证不会有吸附剂颗粒被带到下游工艺设备。 汞吸附床在经过几年的使用后需要更换。 2.3 Process Unit 12 CO2 Removal 工艺单元 12- CO2脱

16、除(Refer to PFD &AA P-FP 1001.001 + &AA P-FP 1002.001) （请参照PFD &AA P-FP 1001.001 + &AA P-FP 1002.001)The aMDEA wash process is a BASF license process and is used to remove CO2 from the feed gas. The wash unit is low in investment and operating cost, of stable operation and minor corrosiveness.As solv

17、ent an aqueous Methyldiethanolamine (MDEA) is used, containing an activator in order to increase the rate of the absorption reaction between CO2 and the amine. aMDEA清洗工艺是BASF的专利工艺，用于脱除原料气中的二氧化碳。清洗单元投资小，运行成本低，运行稳定，腐蚀问题很小。采用水性甲基二乙醇胺(MDEA)作为溶剂，里面含有触媒剂以便增加二氧化碳与胺之间的吸附反应速度。The mercury free feed gas enters

18、 the Amine Wash Column 12T01 with a temperature of approx. 40 C and a pressure of 4.38 MPa a and flows from bottom to top through random packages. Introduced LEAN MDEA flows in the counter current flow direction extracting the acid gas. The CO2 forms a weak bond with the alkali. In the topof the col

19、umn solvent traces are removed by water from the purified gas by means of four additional trays. The wash water for these trays is re-circulated by the Water Circulation Pump 12P01 A/B, a small quantity of water is introduced into the cycle by the Amine Make-Up Water Pump 12P02 A/B as fresh water (d

20、emineralised water) to fulfil the water balance of the amine system.脱汞的原料气在大约40 C 的温度、4.38 MPa的压力下进入胺洗塔12T01，自下而上流过不规整填料。引入的贫MDEA逆向流动，抽出酸性气。二氧化碳与碱形成弱键。利用四个额外塔盘，在塔顶通过水将痕量溶剂从净化气中脱除。这些塔盘的清洗水通过水循环泵12 P01 A/B循环，少量水通过胺水补充水泵12 P02 A/B被作为新鲜水（脱盐水/精制水）引入，以实现胺系统的水平衡。The purified, water saturated gas exits the

21、wash tower with a CO2 content of max. 50 vppm and a temperature of43 C. It is cooled down to approx. 24 C in Feed Gas Heater 12E05 A/B against feed gas from the feed gas filtration.净化过的水饱和气体离开水洗塔， 二氧化碳含量 最大50 vppm和温度43 C， 在原料气加热器12E05 A/B中， 利用来自原料气过滤工段的进料气体 冷却至约24 C 。 The loaded amine solution (RICH

22、 MDEA) originating from the sump of 12T01 is throttled to approx. 0.5 MPa a via control valve and fed to the Amine MP Flash Drum 12D02. The flashed gas from the solvent is routed to the Amine Strip Column off gas stream. Process water originating from 16D01 Feed Gas Water KO Drum is also routed to 1

23、2D02. The loaded solvent from the bottom of 12D02 is heated in Solvent Heat Exchanger 12E01 against hot lean solvent, depressurized to 0.2 MPa a and routed as two phase flow into the middle section of Amine Strip Column 12T02. The gaseous part mixes with the vapour part in the top section of the col

24、umn and enters the backwash trays, where the amine content of the off gas is reduced. The liquid part is distributed onto the packing of the column and stripped with the rising vapour which mainly consists of steam and CO2. After passingthe packing the solvent is collected on a chimney tray and rout

25、ed to the Amine Strip Column Reboiler 12E02where the solvent is partially evaporated using hot oil. The liquid and vapour output of the Amine Strip ColumnReboiler 12E02 is fed back to the sump of the Amine Strip Column 12T02.来自12 T01塔底的加载胺溶液（富MDEA）通过控制阀（使其压力约为0.5MPa）进入到胺中压闪蒸罐12 D02 。 溶剂中闪蒸气体排放到胺汽提塔废

26、气物流。 来自16D01原料气气液分离罐的工艺用水也进入到12D02。从12D02底部装载的溶剂在溶剂加热换热器12E01中被热的贫溶剂加热，降压至0.2 MPa，然后，以两物相形式送入胺提气塔12T02的中间段。气相部分与塔顶的蒸汽混合并进入反洗塔盘，在此，尾气中的胺含量被降低。液相部分被分布在塔填料上，并利用上升蒸汽抽提。上升蒸汽主要由蒸汽和二氧化碳组成。通过填料后，溶剂被收集在一个烟囱状塔盘，并送入胺提气塔再沸器12 E02，在此，部分溶剂被热油蒸发。胺提气塔再沸器12 E02的输出液体和蒸汽被送回胺抽提塔12 T02的塔底。The regenerated solvent leaves

27、the column at the bottom via Solvent Heat Exchanger 12E01 and is pumped by Lean Solvent Pump 12P03 A/B to the middle section of column 12T01 via Lean Solvent Cooler 12E04, where it is cooled down to 40 C against ambient air. Approximately 15% of this flow is routed through the Amine Purge Stream Pre-Filter 12S01 (Cartridge) to remove particles, then through Amine Purge Stream Main Filter 12 S02 (Act