CN104815521B - 基于八塔并联的三元组分的变压吸附分离方法 - Google Patents
基于八塔并联的三元组分的变压吸附分离方法 Download PDFInfo
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- CN104815521B CN104815521B CN201510206109.5A CN201510206109A CN104815521B CN 104815521 B CN104815521 B CN 104815521B CN 201510206109 A CN201510206109 A CN 201510206109A CN 104815521 B CN104815521 B CN 104815521B
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- 238000010521 absorption reaction Methods 0.000 title claims abstract description 34
- 238000000926 separation method Methods 0.000 title claims abstract description 18
- 239000007789 gas Substances 0.000 claims abstract description 102
- 238000006073 displacement reaction Methods 0.000 claims description 37
- 238000000034 method Methods 0.000 claims description 37
- 241000894007 species Species 0.000 claims description 25
- 239000000470 constituent Substances 0.000 claims description 12
- 230000000274 adsorptive Effects 0.000 claims description 7
- OKTJSMMVPCPJKN-UHFFFAOYSA-N carbon Chemical compound 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- PNEYBMLMFCGWSK-UHFFFAOYSA-N AI2O3 Inorganic materials 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- 229910052782 aluminium Inorganic materials 0.000 description 1
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminum Chemical compound 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[Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- UGFAIRIUMAVXCW-UHFFFAOYSA-N carbon monoxide Chemical compound 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[O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 1
- 229910002091 carbon monoxide Inorganic materials 0.000 description 1
- 229910002090 carbon oxide Inorganic materials 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 235000019516 cod Nutrition 0.000 description 1
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- 230000000694 effects Effects 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 150000002430 hydrocarbons Chemical class 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 238000005649 metathesis reaction Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000006011 modification reaction Methods 0.000 description 1
- 239000003345 natural gas Substances 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 238000007254 oxidation reaction Methods 0.000 description 1
- 230000000149 penetrating Effects 0.000 description 1
- 238000010926 purge Methods 0.000 description 1
- 239000012264 purified product Substances 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 238000010992 reflux Methods 0.000 description 1
- 239000002594 sorbent Substances 0.000 description 1
- NINIDFKCEFEMDL-UHFFFAOYSA-N sulfur Chemical compound 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Abstract
本发明公开基于八塔并联的三元组分的变压吸附分离方法,过程中利用部分产品气回流到塔塔去置换,来进一步提高产品纯度和收率。每个吸附塔都包括吸附、均压降、置换、顺放、逆放、抽空、均压升、轻组分升压中的一步或数步,循环切换工作,间断或连续的产出至少两种产品气。本发明可应用于三元气相体系混合气体的分离,通过变压吸附的方法得到两个纯组分或两个纯组分与一个富集中间组分的气体产品。
Description
[0001] 本发明申请是母案申请"一种多回流的变压吸附方法"的分案申请,母案申请日为 2013年11月11日,母案申请号为2013105580916。
技术领域
[0002] 本发明涉及一种变压吸附分离二元及三元混合气体的分离方法,特别是一种含有 多重回流步骤的变压吸附气体分离方法。
背景技术
[0003] 变压吸附技术作为一种新型的分离方法,被广泛应用于气体的分离与提纯领域。 随着研究的深入,其应用领域也在不断扩大。例如从空气中分离出氮气、氧气,从合成气中 分离得到氢气、一氧化碳,从天然气中分离出甲烷、氢气、二氧化碳等等。变压吸附工艺是利 用不同气体在吸附剂上的吸附量和吸附速率的差异,高压吸附,低压解吸的原理来分离混 合气体。
[0004] 传统变压吸附气体分离方法通常只能获得一种产品,想要同时的到难吸附组分与 易吸附组分大多采用多段变压吸附的方法或者引入置换步骤。多段法使得装置整体投资变 得巨大,操作变得复杂;通过引入置换步骤后可以的到两种产品气,但只能以增加吸附塔个 数或辅助设备如缓冲罐来达到提高两种产品纯度的方法,而且置换尾气一般要重新回收用 以提尚收率。
发明内容
[0005] 本发明的目的在于提供一种改进的变压吸附工艺,克服已有技术中存在的上述问 题,降低系统动力学消耗和固定投资费用。
[0006] 本发明的技术目的通过下述技术方案予以实现:
[0007] -种多回流的变压吸附方法,采用吸附塔并联方式予以连接,并在管路中设置缓 冲罐、真空栗和压缩机,将待处理的原料气体在并联吸附塔之间通过缓冲罐、真空栗和压缩 机实现气体在并联吸附塔的塔顶或者塔底之间的多次回流,以实现原料气体中组分的分 离,以在吸附塔的塔顶取得轻组分、吸附塔的塔底取得重组分。
[0008] 在所述吸附塔内装入活性氧化铝、细孔硅胶、活性碳或者分子筛中的一种。
[0009] 对于二元组分的分离。采用双塔并联模式,两塔变压吸附分离空气的流程图如附 图1所示:
[0010] 第一吸附塔(图中标识为A)与第二吸附塔(图中标识为B)并联,在第一吸附塔和原 料气进口之间的管路上设置第一控制阀V-1,在第二吸附塔和原料气进口之间的管路上设 置第二控制阀V-2;
[0011] 在所述第一吸附塔的塔顶通过管路与第二吸附塔的塔顶相连,在两者连接管路上 设置第五控制阀V-5;在所述第一吸附塔的塔顶通过管路与轻组分接收装置(图中未标出) 相连,并在管路上设置第三控制阀V-3,;在所述第二吸收塔的塔顶通过管路与轻组分接收 装置(图中未标出)相连,并在管路上设置第四控制阀V-4;
[0012] 在所述第一吸附塔的塔底通过管路与真空栗相连,并在管路上设置第六控制阀V-6,还通过管路与压缩机相连,并在管路上设置第八控制阀V-8;在所述第二吸收塔的塔底通 过管路与真空栗相连,并在管路上设置第七控制阀V-7,还通过管路与压缩机相连,并在管 路上设置第九控制阀V-9;
[0013] 所述真空栗和压缩机分别通过管路与缓冲罐相连。
[00M] 在进行变压吸附时,采用并列的两个吸附塔,将原料气中的易吸附气体经过吸附 塔吸附浓缩,不易吸附组分从塔顶流出,得到多种产品气,其工艺流程的每个循环包括吸 附、降压、抽空、进料、升压:
[0015] (1)所述的进料位置为吸附塔中间某一位置进料,最优选取塔内气相组成与原料 气组成相等的点进料。进料可以选择低压塔低压进料和高压塔高压进料的两种方式。
[0016] (2)所述的吸附过程为采用塔底重组分强制部分回流置换不易吸附组分,使其从 塔顶采出部分作为轻产品部分用于低压塔升压冲洗。
[0017] 上述吸附过程具体为:低压原料气通过进口阀门从吸附塔A中部进入,同时从吸附 塔B顶部采出的不易吸附产品部分回流至吸附塔A顶部,吸附塔A底部通过真空栗对易吸附 组分进行解吸;塔A与塔B进行连接均压升压,均压的方法可以采用塔顶一塔顶,塔底一塔底 的方式;将真空缓冲罐中得到的易吸附组分加压后通入吸附塔A对其进行升压;达到压力后 通过置换作用从塔A顶部采出不易吸附组分,当易吸附组分将从塔顶穿透时停止置换步骤; 通过连接塔A与塔B进行均压降压;压力降低后用真空栗抽空得到易吸附组分送入真空缓冲 罐,同时部分作为易吸附组分产品采出。
[0018] 对于三元组分的分离,采用多塔并联模式,其中八塔变压吸附分离空气的流程图 如附图3所示:
[0019] 所述第一吸附塔(A塔)塔顶通过第五管路与轻组分缓冲罐相连,并在第五管路中 设置控制阀V5-A;其余七个吸附塔的塔顶通过各自连接管路与第五管路相连,并在各自连 接管路上设置控制阀(V5-B至V5-H);
[0020] 所述第一吸附塔(A塔)塔顶通过第七管路与中间组分缓冲罐相连,并在第七管路 中设置控制阀V7-A;其余七个吸附塔的塔顶通过各自连接管路与第七管路相连,并在各自 连接管路上设置控制阀(V7-B至V7-H);
[0021] 所述第一吸附塔(A塔)塔顶通过控制阀V6 - A与第六管路相连,其余七个吸附塔的 塔顶通过各自控制阀(V6-B至V6-H)与第六管路相连;
[0022] 所述第一吸附塔塔底通过第四管路与第一压缩机相连,并在第四管路中设置控制 阀V4-A;所述第一压缩机与重组分缓冲罐相连;其余七个吸附塔的塔底通过各自连接管路 与第四管路相连,并在各自连接管路上设置控制阀(V4-B至V4-H);
[0023] 所述第一吸附塔塔底通过第三管路与真空栗相连,并在第三管路中设置控制阀 V3-A;所述真空栗与重组分缓冲罐相连;其余七个吸附塔的塔底通过各自连接管路与第三 管路相连,并在各自连接管路上设置控制阀(V3-B至V3-H);
[0024] 所述第一吸附塔塔底通过第二管路与第二压缩机相连,并在第二管路中设置控制 阀V2-A;所述第二压缩机与中间组分缓冲罐相连;其余七个吸附塔塔底通过各自连接管路 与第二管路相连,并在各自连接管路上设置控制阀(V2-B至V2-H);
[0025] 所述八个吸附塔塔底通过各自连接管路与第一管路相连,并在各自连接管路上设 置控制阀(VI -A至VI - H),所述第一管路与原料气进气口相连。
[0026] 在进行变压吸附时,采用并列的多个吸附塔,利用原料气中的各组分在吸附剂内 吸附量的差异,在不同时间及步骤下得到多种产品气,其工艺流程的每个循环包括吸附、置 换一、降压、顺放、置换二、抽空、均压升、终升压:
[0027] (1)原料气为三组分的混合气体,且在预定吸附剂内组分间吸附容量有明显差异 以达到分离的目的。
[0028] (2)置换一采用的气体为富集中间组分的气体经加压后从塔底进入,置换的压力 与吸附压力相同。
[0029] (3)置换二采用的为从塔底采出的最易吸附组分经塔底进入,置换压力采用常压 至吸附压力间的某一压力进行。
[0030] 上述变压吸附过程的具体过程为:原料气加压后经管道从塔底进入吸附塔内,将 组分按吸附量从小到大记为难、中、易,此时在塔内也会形成三个传质区当中吸附组分波峰 到达某一位置但未穿透时停止进料;将另一个塔在顺放过程和第二次置换过程中采出的富 集中间组分的气体加压后从塔底通入进行第一次置换,置换废弃也为难吸附组分采出,当 中间组分将要穿透时停止第一次置换;将此吸附塔与其他吸附塔连接进行N次均压(N大于 等于2小于吸附塔个数),是的塔内压力降低,回收死空间内的难吸附组分,并提高中间组分 的浓度;进行第二次置换,采用抽真空阶段塔底采出的易吸附组分做原料气从塔底通入,同 时在塔顶得到置换尾气为富含中间组分产品气,当易吸附组分将要穿透时停止进料;当第 二次置换压力高于常压时加入顺向降压步骤,从塔顶得到中间组分产品气,此时易吸附组 分已经完全穿透;抽真空步骤从塔底得到高纯度的易吸附组分并使吸附床得到再生;在抽 真空结束后,用来自其他高压吸附塔的气体对其进行N次均升压过程,此过程与均压降压过 程相对应;在均压结束后,为了达到塔内压力变化平稳的目的,采用部分高压力的难吸附产 品气通过终升压管路回流至塔内,使塔内压力达到吸附压力为下次循环做好准备。多个吸 附塔并列建立,交替顺序进行以上的吸附一再生循环过程,便可实现对于三元组分的分离 提纯的目的。
[0031] 在本发明的技术方案中,变压吸附过程中选用共有2-24台吸附塔并列安装。
[0032] 在本发明的技术方案中,原料气进料过程采用低压进料,进料位置为塔内气相组 成与原料气相一致处。
[0033] 在本发明的技术方案中,多次回流步骤包括塔底抽真空得到重组分加压后回流至 另一塔进行吸附置换,置换得到轻组分部分回流至低压塔内进行冲洗再生与升压。
[0034] 在本发明的技术方案中,多次回流步骤包括采用部分中间产品的第一次置换,采 用塔底易吸附组分产品的第二次置换,采用部分难吸附组分回流进行中终升压。
[0035] 在本发明的技术方案中,第一次置换采用中间组分产品气加压后回流,得到置换 尾气与吸附尾气一致为难吸附组分产品气,而取消置换尾气回收步骤。
[0036] 在本发明的技术方案中,在均压阶段将中间组分超标的气体顺着进气方向逐次向 其他正在进行均压升压的吸附塔或均压塔进行2-24次均压降压,同时对应吸附塔或均压 塔进行2-24次均压升压。
[0037] 在本发明的技术方案中,第二次置换采用抽真空得到易吸附组分产品气加压后回 流至塔内,置换尾气作为富集中间组分产品气采出。
[0038] 传统的变压吸附采用高压进料的方式,即吸附压力为循环过程中最高压力,而本 专利对于二元组分的分离可以采用低压进料的方式,这样降低了能耗,可以采用两塔或四 塔以及多塔的操作。三组分的分离通过两次均压的方式得到至少两种高纯度的产品及一种 富集产品。本发明工艺流程将精馏工艺与变压吸附工艺相结合。采用强制或自然回流的多 次回流的工艺使得塔内组分能过清晰分割,通过一套装置得到高纯度的两种或三种物质, 从而达到节能降耗减少投资的目的。
附图说明
[0039] 图1是利用本发明技术方案进行二元组分两塔流程示意图。
[0040] 图2是利用本发明技术方案进行二元组分四塔流程示意图。
[0041] 图3是利用本发明技术方案进行三元组分八塔流程示意图。
具体实施方式
[0042]下面结合具体实施例进一步说明本发明的技术方案。
[0043] 传统两塔变压吸附工艺只能得到一种纯度较高的产品,例如普通的空分制氧工艺 其原料如下表,一般只能得到富氧气,而富氮气由于纯度达不到只能放空。
[0044]
[0045]温度:彡 45 Γ [0046] 实施例1:
[0047] 而利用本发明可以得到同样纯度富氧气体的同时得到高纯度的富氮气,其纯度达 到98.5Vol %。以吸收难易程度来确定轻重组分,轻组分为氧气,重组分为氮气,吸附塔内由 下到上装有分子筛,进料压力为101_130KPa,重组分N 2置换压力为130-300KPa,抽真空压力 为50-70KPa (绝压)。两塔变压吸附分离空气的流程图如附图1所示:
[0048] 第一吸附塔(图中标识为A)与第二吸附塔(图中标识为B)并联,在第一吸附塔和原 料气进口之间的管路上设置第一控制阀V-1,在第二吸附塔和原料气进口之间的管路上设 置第二控制阀V-2;
[0049] 在所述第一吸附塔的塔顶通过管路与第二吸附塔的塔顶相连,在两者连接管路上 设置第五控制阀V-5;在所述第一吸附塔的塔顶通过管路与轻组分接收装置(图中未标出) 相连,并在管路上设置第三控制阀V-3,;在所述第二吸收塔的塔顶通过管路与轻组分接收 装置(图中未标出)相连,并在管路上设置第四控制阀V-4;
[0050] 在所述第一吸附塔的塔底通过管路与真空栗相连,并在管路上设置第六控制阀V-6,还通过管路与压缩机相连,并在管路上设置第八控制阀V-8;在所述第二吸收塔的塔底通 过管路与真空栗相连,并在管路上设置第七控制阀V-7,还通过管路与压缩机相连,并在管 路上设置第九控制阀V-9;
[0051] 所述真空栗和压缩机分别通过管路与缓冲罐相连。
[0052] 循环步骤如下表。
[0053]
[0054] 具体来说,以A塔与B塔在一个周期内交替运行每一个步骤,以构成完整循环达到 连续运行的目的,在一个循环内实现两次回流。
[0055] (1)原料气进气与难吸附组分回流(F/LR)
[0056] 第一控制阀、第三控制阀、第四控制阀、第六控制阀和第九控制阀打开,其余阀门 关闭。第一吸附塔(A塔)处于低压状态,原料气经由V-1在塔内气相组成与进料气组成一致 位置处进料,吸附剂选择性的吸附易吸附组分N 2;同时第一吸附塔塔底气体经过第六控制 阀、真空栗、缓冲罐、压缩机、第九控制阀、第二吸附塔(B塔)、第四控制阀、第三控制阀回流 至第一吸附塔内,回流的部分〇 2,用于塔内吹扫与升压;塔底打开V-6进行抽空得到N2。当压 力升到进料压力101KPa_130KPa后停止。
[0057] (2)均压升压(ER)
[0058] 第五控制阀打开,其余关闭;由于在第一步骤中,针对第一吸附塔而言为两进一 出,造成内部气压上升,造成进料不畅,故进料结束后打开阀门V-5将其与第二吸附塔连接 进行均压升压过程,使得其压力继续升高,如图均压的方式采用塔顶一塔顶方式,还可以选 择塔底一塔底或者塔顶一塔底的方式。
[0059] (3)易吸附组分升压(HPP)
[0060] 打开第七和第八控制阀,其余关闭;为了使整体压力变化平稳,需要对均压升压后 的A塔进一步升压,采用抽真空得到的易吸附组分加压后经V-8回流至塔内的方式,使压力 达到置换压力130_300KPa。
[0061] ⑷易吸附组分回流置换(HR/RP)
[0062]打开第二、第三、第四、第七和第八控制阀,其余控制阀关闭;原料气经由V-2在塔 内气相组成与进料气组成一致位置处进料,吸附剂选择性的吸附易吸附组分N2;同时第二 吸附塔(B塔)塔底气体经过第七控制阀、真空栗、缓冲罐、压缩机、第八控制阀至第一吸附塔 (A塔),即将部分易吸附组分加压后经V-8回流至第一吸附塔内,将难吸附组分置换出,从塔 顶经V-3得到,当易吸附组分将要穿透时停止进料。
[0063] (5)均压降压(ED)
[0064] 打开第五控制阀,其余控制阀关闭;由于塔内压力偏高,同时易吸附组分并未完全 穿透,死空间内存在一定量的难吸附组分,将第一吸附塔(A塔)与第二吸附塔(B塔)连接经 第五吸附塔V-5进行均压,回收部分机械能和空间内的气体。
[0065] ⑶抽真空(VU)
[0066] 第六和第九控制阀打开,其余控制阀关闭;均压降后塔内压力降低,打开V-6进行 抽真空步骤将塔内高纯度的易吸附组分解吸入真空缓冲罐并部分回流至另一塔部分作为 产品采出。
[0067] 在整个循环内阀门开关情况如下表格所示,0-开;X-关
[0068]
[0070] 在实施过程中,若是两个吸附塔(A塔和B塔)在高度上无法满足的话,选择将第一 吸附塔A塔拆分为两个吸附塔A1、A2 (两者串联),将第二吸附塔B塔拆分为两个吸附塔B1、B2 (两者串联),原料气通过管路与吸附塔A1塔底、吸附塔A2塔顶相连,并设置第一控制阀,原 料气通过管路与吸附塔B1塔底、吸附塔B2塔顶相连,并设置第二控制阀,如附图2所示。在具 体实施过程中,采用与实施例相同的循环步骤,将吸附塔A1、A2和吸附塔B1、B2分别视为第 一吸附塔A和第二吸附塔B,即可在塔底得到重组分,塔顶得到轻组分。
[0071] 实施例2:
[0072] 本例的原料气为含有二氧化碳的低浓度煤层气或油田火驱尾气,经前端预处理后 得到净化除去其中C2以上的烃类和含硫化合物等杂质。得到组成如下表的气体:
[0073]
[0074] ^温度:<45°C
[0075] 本发明采用一段法将三元组分吸附分离得到至少两种高纯组分及一种伏击组分, 装置流程图如附图3所示,吸附塔A-Η共八台组成的变压吸附装置。吸附塔内装入活性氧化 铝及活性碳,塔顶在不同阶段得到两种产品,塔底得到一种产品,过程中吸附步骤压力为 200KPa-2000KPa (绝压)。经过本发明流程后得到氮气纯度为99.4%,甲烷气纯度为77.1 %, 二氧化碳纯度为99.3%。八台组成的变压吸附装置如附图3所示,所述八个吸附塔并联: [0076] 所述第一吸附塔(A塔)塔顶通过第五管路与轻组分缓冲罐相连,并在第五管路中 设置控制阀V5-A;其余七个吸附塔的塔顶通过各自连接管路与第五管路相连,并在各自连 接管路上设置控制阀(V5-B至V5-H);
[0077] 所述第一吸附塔(A塔)塔顶通过第七管路与中间组分缓冲罐相连,并在第七管路 中设置控制阀V7-A;其余七个吸附塔的塔顶通过各自连接管路与第七管路相连,并在各自 连接管路上设置控制阀(V7-B至V7-H);
[0078] 所述第一吸附塔(A塔)塔顶通过控制阀V6 - A与第六管路相连,其余七个吸附塔的 塔顶通过各自控制阀(V6-B至V6-H)与第六管路相连;
[0079] 所述第一吸附塔塔底通过第四管路与第一压缩机相连,并在第四管路中设置控制 阀V4-A;所述第一压缩机与重组分缓冲罐相连;其余七个吸附塔的塔底通过各自连接管路 与第四管路相连,并在各自连接管路上设置控制阀(V4-B至V4-Η);
[0080] 所述第一吸附塔塔底通过第三管路与真空栗相连,并在第三管路中设置控制阀 V3-Α;所述真空栗与重组分缓冲罐相连;其余七个吸附塔的塔底通过各自连接管路与第三 管路相连,并在各自连接管路上设置控制阀(V3-Β至V3-Η);
[0081] 所述第一吸附塔塔底通过第二管路与第二压缩机相连,并在第二管路中设置控制 阀V2-A;所述第二压缩机与中间组分缓冲罐相连;其余七个吸附塔塔底通过各自连接管路 与第二管路相连,并在各自连接管路上设置控制阀(V2-B至V2-H);
[0082] 所述八个吸附塔塔底通过各自连接管路与第一管路相连,并在各自连接管路上设 置控制阀(VI -A至VI - H),所述第一管路与原料气进气口相连。
[0083] 吸附装置的一种循环时序表如下:
[0084]
[0085] ⑴吸附步骤(AD)
[0086] 原料气经加压后通过阀门Vl-Α进入吸附塔内,吸附塔内吸附剂选择性的依次吸附 二氧化碳、甲烷和氮气组分,难吸附的部分氮气从出口V5-A流出,一部分作为产品一部分作 为回流气经V5-B进入处于终充压步骤的B塔内进行升压,当吸附剂吸附原料气将近饱和时, 停止进气吸附步骤结束。
[0087] (2)第一次置换步骤(RP1)
[0088] 将富集中间组分甲烷的气体加压到与吸附压力相同后经V2-A回流通入吸附塔内, 通过利用中间组分甲烷的被吸附能力较氮气强的作用对氮气进行置换,置换尾气同样从塔 顶V5-A采出。当甲烷将要穿透时停止通入一次置换气,第一次置换结束。
[0089] ⑶均压降压(ED)
[0090] 第一次置换结束后,吸附塔内死空间及顶部空间内氮气浓度较高,这部分氮气和 压力需要回收利用,为此,把吸附塔内的气体从上部降压,气体从吸附塔顶部V6-A排出经 V6-E/F进入本段已经完成再生的相应吸附塔内,均压降压ED次数可以为1次或多次(2-7 次)。
[0091] ⑷第二次置换步骤(RP2)
[0092]均压步骤ED结束后,此时吸附塔内氮气大部分被置换,吸附有大量的甲烷气及部 分二氧化碳。将富集二氧化碳的气体加压后经V4-A通入塔内依据其被吸附能力较甲烷更强 的原理对吸附塔内甲烷进行置换,置换尾气为富集甲烷的产品气经V7-A进入缓冲罐。当二 氧化碳即将穿透时停止第二次置换步骤。
[0093] (5)顺向放压步骤(CoD)
[0094] 经过第二次置换后塔内甲烷含量降低,但在塔顶和死空间内还残存有大量甲烷, 因此需要回收这部分甲烷同时起到提高二氧化碳纯度的目的,此时顺放气同样为富甲烷气 从塔顶V7-A收集得到。当压力降为常压后,此时塔内二氧化碳完全穿透,停止顺向降压的步 骤。
[0095] ⑶抽真空步骤(VU)
[0096] 顺向放压后塔内吸附的为二氧化碳,通过真空栗将吸附剂吸附的二氧化碳经V3-A 抽出并排如真空缓冲罐内一部分作产品一部分用于加压后回流置换,同时是的吸附塔内吸 附剂得到再生。
[0097] ⑵均压升压步骤(ER)
[0098] 当吸附塔完成再生,利用顺向降压ED步骤排出的气体,从出口端进入吸附塔使其 压力升高,此步骤与顺向降压步骤一一对应。
[0099] ⑶终升压步骤(FR)
[0100] 利用吸附步骤塔顶流出的高压氮气,进行回流对于均压升压后的吸附塔进行最终 升压,使得压力达到吸附压力。
[0101] 具体循环内阀门开关情况表格如下,〇-开;X-关
[0102]
[0104] 以上对本发明做了示例性的描述,应该说明的是,在不脱离本发明的核心的情况 下,任何简单的变形、修改或者其他本领域技术人员能够不花费创造性劳动的等同替换均 落入本发明的保护范围。
Claims (4)
1.基于八塔并联的三元组分的变压吸附分离方法,其特征在于,采用吸附塔并联方式 予以连接,并在管路中设置缓冲罐、真空栗和压缩机,将待处理的原料气体在并联吸附塔之 间通过缓冲罐、真空栗和压缩机实现气体在并联吸附塔的塔顶或者塔底之间的多次回流, 以实现原料气体中组分的分离,以在吸附塔的塔顶取得轻组分、吸附塔的塔底取得重组分, 对于三元组分的分离,采用八塔并联模式变压吸附分离: 第一吸附塔塔顶通过第五管路与轻组分缓冲罐相连,并在第五管路中设置控制阀;其 余七个吸附塔的塔顶通过各自连接管路与第五管路相连,并在各自连接管路上设置控制 阀; 所述第一吸附塔塔顶通过第七管路与中间组分缓冲罐相连,并在第七管路中设置控制 阀;其余七个吸附塔的塔顶通过各自连接管路与第七管路相连,并在各自连接管路上设置 控制阀; 所述第一吸附塔塔顶通过控制阀与第六管路相连,其余七个吸附塔的塔顶通过各自控 制阀与第六管路相连; 所述第一吸附塔塔底通过第四管路与第一压缩机相连,并在第四管路中设置控制阀; 所述第一压缩机与重组分缓冲罐相连;其余七个吸附塔的塔底通过各自连接管路与第四管 路相连,并在各自连接管路上设置控制阀; 所述第一吸附塔塔底通过第三管路与真空栗相连,并在第三管路中设置控制阀;所述 真空栗与重组分缓冲罐相连;其余七个吸附塔的塔底通过各自连接管路与第三管路相连, 并在各自连接管路上设置控制阀; 所述第一吸附塔塔底通过第二管路与第二压缩机相连,并在第二管路中设置控制阀; 所述第二压缩机与中间组分缓冲罐相连;其余七个吸附塔塔底通过各自连接管路与第二管 路相连,并在各自连接管路上设置控制阀; 所述八个吸附塔塔底通过各自连接管路与第一管路相连,并在各自连接管路上设置控 制阀,所述第一管路与原料气进气口相连。 所述并联的吸附塔采用在一个周期内交替运行的模式,以构成完整循环达到连续运行 的目的,每个周期包括吸附步骤、第一次置换步骤、均压降压、顺放、第二次置换步骤、抽空、 均压升、终升压: 原料气加压后经管道从塔底进入吸附塔内,将组分按吸附量从小到大记为难、中、易; 将另一个塔在顺放过程和第二次置换过程中采出的富集中间组分的气体加压后从塔底通 入进行第一次置换,置换废气也为难吸附组分采出,当中间组分将要穿透时停止第一次置 换;将此吸附塔与其他吸附塔连接进行均压,塔内压力降低,回收死空间内的难吸附组分, 并提高中间组分的浓度;进行第二次置换,采用抽真空阶段塔底采出的易吸附组分做原料 气从塔底通入,同时在塔顶得到置换尾气为富含中间组分产品气,当易吸附组分将要穿透 时停止进料;当第二次置换压力高于常压时加入顺向降压步骤,从塔顶得到中间组分产品 气,此时易吸附组分已经完全穿透;抽真空步骤从塔底得到高纯度的易吸附组分并使吸附 床得到再生;在抽真空结束后,用来自其他高压吸附塔的气体对其进行均升压过程,此过程 与均压降压过程相对应;在均压结束后,采用部分高压力的难吸附产品气通过终升压管路 回流至塔内,使塔内压力达到吸附压力为下次循环做好准备,交替顺序进行以上的吸附一 再生循环过程,便可实现对于三元组分的分离提纯的目的。
2. 根据权利要求1所述的基于八塔并联的三元组分的变压吸附分离方法,其特征在于, 在所述吸附塔内装入活性氧化铝、细孔硅胶、活性碳或者分子筛中的一种。
3. 根据权利要求1所述的基于八塔并联的三元组分的变压吸附分离方法,其特征在于, 多次回流步骤包括采用部分中间产品的第一次置换,采用塔底易吸附组分产品的第二次置 换,采用部分难吸附组分回流进行终升压;第一次置换采用中间组分产品气加压后回流,得 到置换尾气与吸附尾气一致为难吸附组分产品气,而取消置换尾气回收步骤;在均压阶段 将中间组分超标的气体顺着进气方向逐次向其他正在进行均压升压的吸附塔或均压塔进 行均压降压,同时对应吸附塔或均压塔进行均压升压;第二次置换采用抽真空得到易吸附 组分产品气加压后回流至塔内,置换尾气作为富集中间组分产品气采出。
4. 根据权利要求3所述的基于八塔并联的三元组分的变压吸附分离方法,其特征在于, 在均压阶段,选择均压降压为2-24次,均压升压为2-24次。
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