JP5683277B2 - 炭化水素流の冷却方法及び装置 - Google Patents
炭化水素流の冷却方法及び装置 Download PDFInfo
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- JP5683277B2 JP5683277B2 JP2010546326A JP2010546326A JP5683277B2 JP 5683277 B2 JP5683277 B2 JP 5683277B2 JP 2010546326 A JP2010546326 A JP 2010546326A JP 2010546326 A JP2010546326 A JP 2010546326A JP 5683277 B2 JP5683277 B2 JP 5683277B2
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- stream
- cooling
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- hydrocarbon
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- 238000001816 cooling Methods 0.000 title claims description 166
- 150000002430 hydrocarbons Chemical class 0.000 title claims description 139
- 229930195733 hydrocarbon Natural products 0.000 title claims description 138
- 239000004215 Carbon black (E152) Substances 0.000 title claims description 116
- 238000000034 method Methods 0.000 title claims description 40
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims description 101
- 238000004821 distillation Methods 0.000 claims description 46
- 238000011084 recovery Methods 0.000 claims description 23
- 239000003345 natural gas Substances 0.000 claims description 21
- 239000007789 gas Substances 0.000 claims description 19
- 239000007788 liquid Substances 0.000 claims description 10
- 238000002156 mixing Methods 0.000 claims description 10
- 239000003507 refrigerant Substances 0.000 description 31
- 239000000047 product Substances 0.000 description 23
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 description 22
- 239000003949 liquefied natural gas Substances 0.000 description 14
- OTMSDBZUPAUEDD-UHFFFAOYSA-N Ethane Chemical compound CC OTMSDBZUPAUEDD-UHFFFAOYSA-N 0.000 description 13
- 239000001294 propane Substances 0.000 description 11
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 9
- 229910001868 water Inorganic materials 0.000 description 9
- 238000010992 reflux Methods 0.000 description 8
- 239000000446 fuel Substances 0.000 description 7
- IJDNQMDRQITEOD-UHFFFAOYSA-N n-butane Chemical compound CCCC IJDNQMDRQITEOD-UHFFFAOYSA-N 0.000 description 7
- OFBQJSOFQDEBGM-UHFFFAOYSA-N n-pentane Natural products CCCCC OFBQJSOFQDEBGM-UHFFFAOYSA-N 0.000 description 7
- 235000013844 butane Nutrition 0.000 description 6
- 239000001273 butane Substances 0.000 description 5
- 239000000203 mixture Substances 0.000 description 5
- 239000012071 phase Substances 0.000 description 4
- MWRWFPQBGSZWNV-UHFFFAOYSA-N Dinitrosopentamethylenetetramine Chemical compound C1N2CN(N=O)CN1CN(N=O)C2 MWRWFPQBGSZWNV-UHFFFAOYSA-N 0.000 description 3
- 229940112112 capex Drugs 0.000 description 3
- FEBLZLNTKCEFIT-VSXGLTOVSA-N fluocinolone acetonide Chemical compound C1([C@@H](F)C2)=CC(=O)C=C[C@]1(C)[C@]1(F)[C@@H]2[C@@H]2C[C@H]3OC(C)(C)O[C@@]3(C(=O)CO)[C@@]2(C)C[C@@H]1O FEBLZLNTKCEFIT-VSXGLTOVSA-N 0.000 description 3
- 238000005057 refrigeration Methods 0.000 description 3
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 2
- 239000000654 additive Substances 0.000 description 2
- 230000000996 additive effect Effects 0.000 description 2
- 230000006837 decompression Effects 0.000 description 2
- NNPPMTNAJDCUHE-UHFFFAOYSA-N isobutane Chemical compound CC(C)C NNPPMTNAJDCUHE-UHFFFAOYSA-N 0.000 description 2
- 238000004781 supercooling Methods 0.000 description 2
- 238000010792 warming Methods 0.000 description 2
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 description 1
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 1
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 1
- 239000006096 absorbing agent Substances 0.000 description 1
- 239000002253 acid Substances 0.000 description 1
- 150000004945 aromatic hydrocarbons Chemical class 0.000 description 1
- 229910002092 carbon dioxide Inorganic materials 0.000 description 1
- 239000001569 carbon dioxide Substances 0.000 description 1
- 238000003763 carbonization Methods 0.000 description 1
- 230000006835 compression Effects 0.000 description 1
- 238000007906 compression Methods 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 239000002737 fuel gas Substances 0.000 description 1
- 239000007792 gaseous phase Substances 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 239000001307 helium Substances 0.000 description 1
- 229910052734 helium Inorganic materials 0.000 description 1
- SWQJXJOGLNCZEY-UHFFFAOYSA-N helium atom Chemical compound [He] SWQJXJOGLNCZEY-UHFFFAOYSA-N 0.000 description 1
- 239000001257 hydrogen Substances 0.000 description 1
- 229910052739 hydrogen Inorganic materials 0.000 description 1
- 229910000037 hydrogen sulfide Inorganic materials 0.000 description 1
- 238000002347 injection Methods 0.000 description 1
- 239000007924 injection Substances 0.000 description 1
- 239000012263 liquid product Substances 0.000 description 1
- QSHDDOUJBYECFT-UHFFFAOYSA-N mercury Chemical compound [Hg] QSHDDOUJBYECFT-UHFFFAOYSA-N 0.000 description 1
- 229910052753 mercury Inorganic materials 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 239000003208 petroleum Substances 0.000 description 1
- 238000010587 phase diagram Methods 0.000 description 1
- 239000011593 sulfur Substances 0.000 description 1
- 229910052717 sulfur Inorganic materials 0.000 description 1
- 150000003464 sulfur compounds Chemical class 0.000 description 1
- 238000011144 upstream manufacturing Methods 0.000 description 1
- 239000012808 vapor phase Substances 0.000 description 1
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- F25J1/0228—Coupling of the liquefaction unit to other units or processes, so-called integrated processes
- F25J1/0229—Integration with a unit for using hydrocarbons, e.g. consuming hydrocarbons as feed stock
- F25J1/0231—Integration with a unit for using hydrocarbons, e.g. consuming hydrocarbons as feed stock for the working-up of the hydrocarbon feed, e.g. reinjection of heavier hydrocarbons into the liquefied gas
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Description
天然ガスは有用な燃料資源であり、また各種炭化水素化合物の資源である。天然ガス流資源又はその近くの液化天然ガス(LNG)プラントでは多くの理由から天然ガスを液化するのが望ましいことが多い。例えば天然ガスは、ガス状よりも液体としての方が容積が小さく、また高圧で貯蔵する必要がないので、一層容易に貯蔵できるし、或いは長距離に亘って輸送できる。
(a)初期炭化水素流を第一分離器に通して初期塔頂流及び混合炭化水素原料流を得る(provide)工程、
(b)該初期塔頂流を冷却、好ましくは液化してLNGのような冷却、好ましくは液化炭化水素流を得る工程、
(c)前記混合炭化水素原料流から第一圧力で少なくともC1塔頂流と1種以上のC2、C3及びC4塔頂流とを分離する工程、
(d)該C2塔頂流、C3塔頂流及びC4塔頂流を含む群の少なくとも1種の少なくとも画分(at least a fraction)を、前記C1塔頂流との添加混合により冷却、好ましくは液化して冷却流を得る工程、及び
(e)更に該冷却流を前記冷却炭化水素流の少なくとも画分で冷却して、第一圧力とほぼ同じ第二圧力で少なくとも一部液化した冷却流を得る工程、
を含む炭化水素流の冷却方法を提供する。
初期炭化水素流を通して初期塔頂流及び混合炭化水素原料流を得るための第一分離器;
該初期炭化水素流を冷却、好ましくは液化して、LNGのような冷却、好ましくは液化炭化水素流を得るための冷却システム;
前記混合炭化水素原料流から少なくともC1塔頂流と1種以上のC2、C3及びC4塔頂流とを分離するためのNGL回収システム;
前記C1塔頂流と添加混合して冷却流を得ることにより、前記C2塔頂流、C3塔頂流及びC4塔頂流を含む群の少なくとも1種の少なくとも画分を冷却するための配合器;
前記冷却流を前記冷却、好ましくは液化炭化水素流の少なくとも画分で更に冷却して、少なくとも一部液化した冷却流を得るための1種以上の熱交換器;
を少なくとも備え、前記C1塔頂流と前記少なくとも一部液化した冷却流との間に膨張器又は圧縮器がない、炭化水素流の冷却装置も提供する。
以下に、単なる例示により添付の非限定的図面を参照して本発明の実施態様及び実施例を説明する。
(a)初期炭化水素流を第一分離器に通して初期塔頂流及び混合炭化水素原料流を得る工程、
(b)該初期塔頂流を冷却、好ましくは液化して冷却、好ましくは液化炭化水素流を得る工程、
(c)前記混合炭化水素原料流から少なくともC1塔頂流と1種以上のC2、C3及びC4塔頂流とを分離する工程、
(d)該C2塔頂流、C3塔頂流及びC4塔頂流を含む群の少なくとも1種の少なくとも画分を前記C1塔頂流で冷却して冷却流を得る工程、及び
(e)該冷却流を前記冷却、好ましくは液化炭化水素流の少なくとも画分で更に冷却して、少なくとも一部液化した冷却流を得る工程、
を含む。
初期炭化水素流を通して初期塔頂流及び混合炭化水素原料流を得るための第一分離器;
該初期炭化水素流を冷却、好ましくは液化して、LNGのような冷却、好ましくは液化炭化水素流を得るための冷却システム;
前記混合炭化水素原料流から少なくともC1塔頂流と1種以上のC2、C3及びC4塔頂流とを分離するためのNGL回収システム;
前記C2塔頂流、C3塔頂流及びC4塔頂流を含む群の少なくとも1種の少なくとも画分を前記C1塔頂流で冷却して冷却流を得るための手段;及び
前記冷却流を前記冷却、好ましくは液化炭化水素流の少なくとも画分で更に冷却して少なくとも一部液化した冷却流を得るための1種以上の熱交換器;
を少なくとも備える。
これによりNGL回収流を適応させるため、主熱交換器中の余分な束の冷却パイプの必要性は回避され、こうして、EP 1469266 A1では統合主熱交換器に必要であった追加のCAPEX及びOPEXを回避できる。
用語“C2+”、“C3+”等は、エタン及びこれより重質の炭化水素、プロパン及びこれより重質の炭化水素等を含有する流れに関する。
初期原料流7の冷却は、初期原料流7の温度を−0℃未満、例えば−10℃〜−70℃の範囲に低下させる工程を含んでよい。
第一蒸留塔12は、第一再沸器13及び第一再沸器蒸気戻り流13aも当該技術分野で公知の方法で有する。
第二C2画分45の温度は、一般に10℃未満、例えば10℃〜−20℃、更に通常、5℃〜−10℃の範囲である。
第二C3画分55及び第二C4画分65の温度は、一般に0℃より高く、通常、0℃〜60℃の範囲である。
また好ましくは少なくとも一部液化した冷却流71は、冷却、好ましくは液化炭化水素流120の40℃以内、好ましくは10℃以内である。
2 液化天然ガスプラント
7 (天然ガス含有)初期原料流
8 (冷却)初期炭化水素流
10 混合炭化水素原料流
12 第一蒸留塔
13 第一再沸器
13a 第一再沸器蒸気戻り流
14 予備冷却用熱交換器
14a 予備冷却用熱交換器
14b 予備冷却用熱交換器
14c 予備冷却用熱交換器
16 第一分離器又はスクラブ塔
18 バルブ
18a 更に冷却された(初期)炭化水素流
20 C1塔頂流
20a (加温)C1塔頂流
21 水及び/又は空気冷却器
22 第二蒸留塔
25 減圧流
26 第一熱交換器
27 分離器
28 ポンプ
29 分割器
30 第一塔底流
31 冷却第一塔底流
32 第三蒸留塔
33 第三再沸器
33a 第三再沸器蒸気戻り流
34 水及び/又は空気冷却器のような周囲冷却器
35 分離器
36 ポンプ
38 バルブ
40 C2塔頂流
40a 少なくとも一部凝縮したC2流
42 第四蒸留塔
43 C2還流流
44 C2生成物流
45 第二C2画分
46 第一C2画分
47 第二塔底流
48 減圧第二塔底流
50 C3塔頂流
51 冷却C3塔頂流
52 分離器塔底流
53 C3還流流
54 C3生成物流
55 第二C3画分
56 第一C3画分
57 第三塔底流
58 減圧第二塔底流
59 分割器
60 C4塔頂流
61 冷却C4塔頂流
62 分離器塔底流
63 C4還流流
64 C4生成物流
65 第二C4画分
66 第一C4画分
67 C5+塔底流
68 C5+生成物流
70 冷却流
70a 冷却流
71 少なくとも一部液化した冷却(又は過冷却)流
71a 少なくとも一部液化した冷却流
72 減圧冷却流
72a 減圧配合流
81 配合C3・C4生成物流
82 配合器
84 配合C1・C2流
86 配合器
91 水及び/又は空気冷却器
92 第四再沸器
92a 第四再沸器蒸気戻り流
93 水及び/又は空気冷却器
94 分離器
95 ポンプ
96 分割器
97 配合器
100 第一冷媒流
100a 加温第一冷媒流
110 メタン富化流又は初期塔頂流
112 主熱交換器
114 第二冷媒流
114a 加温第二冷媒流
116 バルブ
118 最終フラッシュ容器
120 冷却又は液化炭化水素流
122 第二熱交換器
122a 熱交換器
124 バルブ
125 バルブ
130 最終フラッシュガス
132 加温最終フラッシュガス流
136 圧縮最終(フラッシュガス)流
138 周囲冷却器
139 燃料流
139a 燃料流
140 液化製品流
200 側流
202 分離器
204 塔底還流流
206 塔頂流
206a 側流
206b 第二画分流、冷却側流又は主塔頂画分
206c 冷却(又は液化)側流
210 主冷媒回路
212 第三熱交換器
214 膨張器
216 バルブ
222 最終原料流
240 分離器
242 配合流
244 第四熱交換器
Claims (13)
- 少なくとも以下の工程:
(a)初期炭化水素流をスクラブ塔に通して初期塔頂流及び混合炭化水素原料流を得る工程、
(b)該初期塔頂流を冷却して冷却炭化水素流を得る工程、
(c)前記混合炭化水素原料流から第一圧力で少なくともC1塔頂流と1種以上のC2、C3及びC4塔頂流とを分離する工程、ここで少なくとも以下の工程:
(i)前記混合炭化水素原料流の少なくとも画分を第一蒸留塔に通してC1塔頂流及び第一塔底流を得る工程、
(ii)該第一塔底流の少なくとも画分を、第二、第三及び第四の蒸留塔を含む群の少なくとも1つに通してC2塔頂流、C3塔頂流及びC4塔頂流を含む群の少なくとも1種を得る工程、
を含み、
(d)該C2塔頂流、C3塔頂流及びC4塔頂流を含む群の少なくとも1種の少なくとも画分を、前記C1塔頂流との添加混合により冷却して冷却流を得る工程、及び
(e)該冷却流を前記冷却炭化水素流の少なくとも画分で更に冷却して、第一圧力とほぼ同じ第二圧力で少なくとも一部液化した冷却流を得る工程、
を含む炭化水素流の冷却方法。 - 工程(b)の冷却工程が液化工程を含み、これにより前記冷却炭化水素流は液化炭化水素流となる請求項1に記載の方法。
- 工程(e)の更なる冷却工程が前記冷却流の過冷却工程を含み、これにより前記少なくとも一部液化した冷却流が過冷却液化流となる請求項1又は2に記載の方法。
- 前記冷却炭化水素流がバルブを通って最終フラッシュ容器の形の最終ガス/液体分離器に入り、塔頂流として最終フラッシュガスおよび液化製品流を提供し、ここで、前記冷却炭化水素流の少なくとも画分が前記最終フラッシュガスであり、工程(e)で前記冷却流が前記冷却炭化水素流の少なくとも画分によりさらに冷却される、請求項1〜3のいずれか1項に記載の方法。
- 前記少なくとも一部液化した冷却流が、引続き前記冷却炭化水素流の少なくとも画分と配合される請求項1〜4のいずれか1項に記載の方法。
- 前記少なくとも一部液化した冷却流と、工程(e)における前記冷却炭化水素流の少なくとも画分との温度差が40℃以内である請求項1〜5のいずれか1項に記載の方法。
- 少なくとも一部液化した冷却流と、工程(e)における前記冷却炭化水素流の少なくとも画分との温度差が10℃以内である、請求項1〜5のいずれか1項に記載の方法。
- それぞれ、前記C2塔頂流、前記C3塔頂流及び前記C4塔頂流を得るため、前記第二蒸留塔、前記第三蒸留塔及び前記第四蒸留塔を準備する工程を更に含む請求項1〜7のいずれか1項に記載の方法。
- 前記C2塔頂流、C3塔頂流及びC4塔頂流の各々の少なくとも画分が、前記C1塔頂流により冷却される請求項8に記載の方法。
- 前記冷却流の温度が0℃未満である請求項1〜9のいずれか1項に記載の方法。
- LNGを得るため、前記炭化水素流が本質的に天然ガスからなる請求項1〜10のいずれか1項に記載の方法。
- 前記C1塔頂流が前記冷却流の一部である請求項1〜11のいずれか1項に記載の方法。
- 初期炭化水素流を通して初期塔頂流及び混合炭化水素原料流を得るためのスクラブ塔;
該初期炭化水素流を冷却して冷却炭化水素流を得るための冷却システム;
前記混合炭化水素原料流から少なくともC1塔頂流と1種以上のC2、C3及びC4塔頂流とを分離するためのNGL回収システム;
前記C1塔頂流と添加混合して冷却流を得ることにより、前記C2塔頂流、C3塔頂流及びC4塔頂流を含む群の少なくとも1種の少なくとも画分を冷却するための配合器;
前記冷却流を前記冷却炭化水素流の少なくとも画分で更に冷却して、少なくとも一部液化した冷却流を得るための1種以上の熱交換器;
を少なくとも備え、前記C1塔頂流と前記少なくとも一部液化した冷却流との間に膨張器又は圧縮器がない、炭化水素流の冷却装置。
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