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Article(id=1322942341731983675, tenantId=1146029695717560320, journalId=1322258508890079423, issueId=1322941718441623734, articleNumber=null, orderNo=null, doi=10.13809/j.cnki.cn32-1825/te.20250008, pmid=null, cstr=null, oa=null, hot=null, price=null, onlineType=0, articleFormat=0, articleType=null, articleTypeStr=null, receivedDate=1767110400000, receivedDateStr=2025-12-31, revisedDate=null, revisedDateStr=null, acceptedDate=null, acceptedDateStr=null, onlineDate=1793343633348, onlineDateStr=2026-10-30, pubDate=1779724800000, pubDateStr=2026-05-26, doiRegisterDate=null, doiRegisterDateStr=null, onlineIssueDate=1793343633348, onlineIssueDateStr=2026-10-30, onlineJustAcceptDate=null, onlineJustAcceptDateStr=null, onlineFirstDate=null, onlineFirstDateStr=null, sourceXml=null, magXml=null, createTime=1793343633348, creator=13701087609, updateTime=1793343633348, updator=13701087609, issue=Issue{id=1322941718441623734, tenantId=1146029695717560320, journalId=1322258508890079423, year='2026', volume='16', issue='3', pageStart='489', pageEnd='736', issueExtLink='null', onlineDate='null', pubDate='1779724800000', pubDateStr='2026-05-26', beforeIssueId=null, nextIssueId=null, price=null, status=1, issueComplete=1, articleOrder=1, issueType=-1, specialIssue=null, createTime=1793343484745, creator='13701087609', updateTime=1793344165564, updator='13701087609', preIssue=null, nextIssue=null, articleTotal=null, ext={EN=IssueExt(id=1322944574066402279, tenantId=1146029695717560320, journalId=1322258508890079423, issueId=1322941718441623734, language=EN, specialIssueTitle=, coverIllustrator=null, specialIssueEditor=, specialIssueAbout=), CN=IssueExt(id=1322944574070596584, tenantId=1146029695717560320, journalId=1322258508890079423, issueId=1322941718441623734, language=CN, specialIssueTitle=, coverIllustrator=null, specialIssueEditor=, specialIssueAbout=)}, issueFiles=null, downloadFileDto=null}, startPage=694, endPage=701, ext={EN=ArticleExt(id=1322942343325819196, articleId=1322942341731983675, tenantId=1146029695717560320, journalId=1322258508890079423, language=EN, title=Research on dry ice sublimation gas phase injection technology, columnId=1322941621217657699, journalTitle=Petroleum Reservoir Evaluation and Development, columnName=Engineering Techniques, runingTitle=null, highlight=

CO2 flooding is an important component of carbon capture, utilization, and storage (CCUS), effectively improving crude oil recovery and CO2 storage rates. However, conventional liquid CO2 transportation and injection technologies face problems such as strong geographical limitations, long transportation distances, and difficulties in source-sink matching, especially in remote oilfields, leading to rising transportation costs and reduced flooding efficiency. Therefore, it is urgent to develop new low-cost CO2 transportation and injection technologies. By systematically studying the fundamental principles and process characteristics of dry ice (solid CO2) sublimation, a dry ice sublimation gas phase injection process was developed, centered on “dry ice transportation, sublimation reaction, heating and temperature regulation, compression and pressurization, and injection system”. Additionally, technical and economic feasibility evaluations were conducted, and a field test was carried out in well H1P2, Hongzhuang Oilfield, Qintong Sag, Subei Basin. The research results showed that the dry ice sublimation gas phase injection technology could realize efficient conversion of dry ice to gas-phase CO2 at temperatures below 35 ℃. The pressure was increased from 0.1 MPa to the injection pressure through multi-stage compression, and then it was injected into oil wells for huff and puff to enhance oil production, demonstrating technical feasibility. The economic break-even transportation distance for traditional liquid CO2 injection and dry ice sublimation gas phase injection technology was 636.82 km. Compared with liquid CO2 injection technology, an average of 20 kWh of energy consumption per ton of dry ice injected could be saved, resulting in good economic benefits. Well H1P2 sublimated a total of 60 t of dry ice, cumulatively injecting 30 456 m3 of gas-phase CO2. The comprehensive water cut decreased from 95% to 78%, and the daily oil production increased from 0.60 t to a maximum of 3.08 t, achieving efficient utilization and geological storage of CO2. The dry ice sublimation gas phase injection technology fundamentally addresses the limitations of liquid CO2, such as restricted transportation distance, poor regional adaptability, and high difficulty in source-sink matching. Next, by controlling the sublimation rate, optimizing energy utilization, and improving economic efficiency, the application scope of CCUS technology can be expanded, and the large-scale deployment and application of CCUS technology can be further realized, thereby providing important support for achieving the goal of carbon neutrality and green low-carbon development.

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CO₂驱油是CO₂捕集、利用与封存（CCUS）的重要组成部分，可有效提高原油采收率与CO2封存率，但传统液相CO₂运输与压注技术存在地域限制强、运输距离远、源汇匹配难等问题，尤其在偏远油田应用受限，导致运输成本攀升、驱油效益下滑，亟须开发低成本 CO₂运输压注新技术。通过系统研究干冰（固态CO2）升华基本原理与工艺特性，研发形成以“干冰输送、升华反应、加热调温、压缩升压和压注系统”为核心的干冰升华气相压注工艺，同时开展技术与经济可行性评价，并在苏北盆地溱潼凹陷红庄油田H1P2井开展矿场试验。研究结果表明：干冰升华气相压注工艺技术可实现35 ℃以下干冰向气相CO2的高效转化，并经多级压缩将压力从 0.1 MPa 提升至压注压力，再注入油井中进行吞吐增油，具备技术可行性；传统液相CO2压注和干冰升华气相压注技术的经济平衡运输距离为636.82 km，与液相CO2压注技术相比，平均每吨干冰压注可节约能耗20 kWh，经济效益较好；H1P2井共升华干冰60 t，累计压注气相CO2 30 456 m3，综合含水率由95%降至78%，日产油量由0.60 t最高升至3.08 t，实现了CO2的高效利用与地质封存。干冰升华气相压注技术从根本上解决了液相CO2运输距离受限、地域适应性差、源汇匹配难度大等问题。下一步，可通过控制升华速率、优化能量利用、提升经济性等方式，进一步扩大该技术的应用范围，推动CCUS技术的大规模推广与应用，为实现碳中和目标与绿色低碳发展提供重要支撑。

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陈兴明（1971—），男，本科，高级工程师，主要从事CO2环保捕集与应用、油气田开发研究等工作。地址：江苏省南京市建邺区江东中路375号金融城9号楼，邮政编码：210019。E-mail：

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刘方志（1983—），男，硕士，高级工程师，主要从事CCUS-EOR、油气田开发技术服务等工作。地址：江苏省泰州市海陵区南通路99号，邮政编码： 225300。E-mail：
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陈兴明（1971—），男，本科，高级工程师，主要从事CO2环保捕集与应用、油气田开发研究等工作。地址：江苏省南京市建邺区江东中路375号金融城9号楼，邮政编码：210019。E-mail：

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陈兴明（1971—），男，本科，高级工程师，主要从事CO2环保捕集与应用、油气田开发研究等工作。地址：江苏省南京市建邺区江东中路375号金融城9号楼，邮政编码：210019。E-mail：

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Summarization of dry ice purge technology[J]. Low Temperature and Specialty Gases, 2005, 23(2): 12-14., articleTitle=Summarization of dry ice purge technology, refAbstract=null)], funds=null, companyList=[AuthorCompany(id=1322942345372639566, tenantId=1146029695717560320, journalId=1322258508890079423, articleId=1322942341731983675, xref=1, ext=[AuthorCompanyExt(id=1322942345376833871, tenantId=1146029695717560320, journalId=1322258508890079423, articleId=1322942341731983675, companyId=1322942345372639566, language=EN, country=null, province=null, city=null, postcode=null, companyName=null, departmentName=null, remark=1 Research Institute of Exploration and Development, Sinopec East China Oil & Gas Company, Nanjing, Jiangsu 210019, China), AuthorCompanyExt(id=1322942345385222480, tenantId=1146029695717560320, journalId=1322258508890079423, articleId=1322942341731983675, companyId=1322942345372639566, language=CN, country=null, province=null, city=null, postcode=null, companyName=null, departmentName=null, 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label=Table 1, caption=Physical property parameters of CO2 （modified from reference［22］）, figureFileSmall=null, figureFileBig=null, tableContent=
物性参数物性参数
临界温度/℃31.1气态密度/(kg/m3)7.74
临界压力/MPa7.38液态密度/(kg/m3)1 178
临界体积/(cm3/mol)94固态密度/(kg/m3)1 512.4
临界密度/(kg/m3)468标态密度/(kg/m3)1.976 8
临界黏度/(mPa∙s)0.040 4标态黏度/(mPa∙s)0.013 8
临界压缩系数0.315三相点/(℃，MPa)-56.6，0.52
临界偏心因子0.2250.101 MPa条件下固态升华温度/℃-78.5
临界偏差系数0.2740 ℃条件下水中溶解度/g0.385
), ArticleFig(id=1322942349835379065, tenantId=1146029695717560320, journalId=1322258508890079423, articleId=1322942341731983675, language=CN, label=表1, caption=

CO2的物性参数（据参考文献[22]修改）

, figureFileSmall=null, figureFileBig=null, tableContent=
物性参数物性参数
临界温度/℃31.1气态密度/(kg/m3)7.74
临界压力/MPa7.38液态密度/(kg/m3)1 178
临界体积/(cm3/mol)94固态密度/(kg/m3)1 512.4
临界密度/(kg/m3)468标态密度/(kg/m3)1.976 8
临界黏度/(mPa∙s)0.040 4标态黏度/(mPa∙s)0.013 8
临界压缩系数0.315三相点/(℃，MPa)-56.6，0.52
临界偏心因子0.2250.101 MPa条件下固态升华温度/℃-78.5
临界偏差系数0.2740 ℃条件下水中溶解度/g0.385
), ArticleFig(id=1322942349906682234, tenantId=1146029695717560320, journalId=1322258508890079423, articleId=1322942341731983675, language=EN, label=Table 2, caption=Characteristics of dry ice at different temperatures, figureFileSmall=null, figureFileBig=null, tableContent=
温度/℃物态蒸气压/MPa升华速率
-100.0固态0.001 01极低
-78.5升华点0.101 00中等
-50.0固态0.525 20较高
-20.0固态2.474 50高
0固态3.474 40很高
20.0固态5.706 50极高
), ArticleFig(id=1322942349998956923, tenantId=1146029695717560320, journalId=1322258508890079423, articleId=1322942341731983675, language=CN, label=表2, caption=

干冰在不同温度下的特性

, figureFileSmall=null, figureFileBig=null, tableContent=
温度/℃物态蒸气压/MPa升华速率
-100.0固态0.001 01极低
-78.5升华点0.101 00中等
-50.0固态0.525 20较高
-20.0固态2.474 50高
0固态3.474 40很高
20.0固态5.706 50极高
), ArticleFig(id=1322942350061871484, tenantId=1146029695717560320, journalId=1322258508890079423, articleId=1322942341731983675, language=EN, label=Table 3, caption=Parameter summary, figureFileSmall=null, figureFileBig=null, tableContent=
参数参数来源参数值
qh/(kJ/kg)实验数据573.6
qv/(m³/s)实验数据0.08
ρc/(kg/m³)实验数据1.787
cp/[J/（kg·℃）]实验数据799.7
ts/℃干冰表面温度-78.5
tg/℃出口气体平均温度1.5
), ArticleFig(id=1322942350124786045, tenantId=1146029695717560320, journalId=1322258508890079423, articleId=1322942341731983675, language=CN, label=表3, caption=

参数汇总

, figureFileSmall=null, figureFileBig=null, tableContent=
参数参数来源参数值
qh/(kJ/kg)实验数据573.6
qv/(m³/s)实验数据0.08
ρc/(kg/m³)实验数据1.787
cp/[J/（kg·℃）]实验数据799.7
ts/℃干冰表面温度-78.5
tg/℃出口气体平均温度1.5
), ArticleFig(id=1322942350191894910, tenantId=1146029695717560320, journalId=1322258508890079423, articleId=1322942341731983675, language=EN, label=Table 4, caption=Cost comparison of two injection techniques, figureFileSmall=null, figureFileBig=null, tableContent=
压注技术CO2运输相态原料购买成本/（元/t）

运输成本/

（元/t·km）

压注作业成本/（元/t）
液相CO2压注液相CO22561.094
干冰升华气相压注干冰640~8440.2~0.5164
), ArticleFig(id=1322942350284169599, tenantId=1146029695717560320, journalId=1322258508890079423, articleId=1322942341731983675, language=CN, label=表4, caption=

2种压注技术成本对比

, figureFileSmall=null, figureFileBig=null, tableContent=
压注技术CO2运输相态原料购买成本/（元/t）

运输成本/

（元/t·km）

压注作业成本/（元/t）
液相CO2压注液相CO22561.094
干冰升华气相压注干冰640~8440.2~0.5164
), ArticleFig(id=1322942350342889856, tenantId=1146029695717560320, journalId=1322258508890079423, articleId=1322942341731983675, language=EN, label=Table 5, caption=Cost comparison of two injection technologies in Dunhuang oil area，Qinghai oilfield, figureFileSmall=null, figureFileBig=null, tableContent=
压注技术压注量（气相）/m³CO2运输相态运输量/t原料购买成本/元运输成本/元

其他费用

（压注费、人工费等）/元

费用合计/元
液相压注30 800液相CO260.515 48848 4005 68769 575
干冰升华气相压注干冰60.038 40014 4009 84062 640
), ArticleFig(id=1322942350414193025, tenantId=1146029695717560320, journalId=1322258508890079423, articleId=1322942341731983675, language=CN, label=表5, caption=

青海油田敦煌油区2种压注技术成本对比

, figureFileSmall=null, figureFileBig=null, tableContent=
压注技术压注量（气相）/m³CO2运输相态运输量/t原料购买成本/元运输成本/元

其他费用

（压注费、人工费等）/元

费用合计/元
液相压注30 800液相CO260.515 48848 4005 68769 575
干冰升华气相压注干冰60.038 40014 4009 84062 640
), ArticleFig(id=1322942352117080450, tenantId=1146029695717560320, journalId=1322258508890079423, articleId=1322942341731983675, language=EN, label=Table 6, caption=Experimental data of dry ice sublimation gas phase injection process, figureFileSmall=null, figureFileBig=null, tableContent=
时间

电加热功率/

kW

反应器装置压力/MPa

反应器出口温度/

℃

反应器内温度/

℃

瞬时流量/（m³/h）阶段压注量/m³压缩机出口压力/MPa
2020-09-01T09:00900.108.237203.24 876.86.30
2020-09-02T09:00900.116.635212.35 095.26.32
2020-09-03T09:00900.109.038205.04 920.06.30
2020-09-04T09:00900.115.735214.95 157.66.31
2020-09-05T09:00900.1217.040218.35 239.26.32
2020-09-06T09:00900.1112.039215.35 167.26.32
), ArticleFig(id=1322942352200966531, tenantId=1146029695717560320, journalId=1322258508890079423, articleId=1322942341731983675, language=CN, label=表6, caption=

干冰升华气相压注流程试验数据

, figureFileSmall=null, figureFileBig=null, tableContent=
时间

电加热功率/

kW

反应器装置压力/MPa

反应器出口温度/

℃

反应器内温度/

℃

瞬时流量/（m³/h）阶段压注量/m³压缩机出口压力/MPa
2020-09-01T09:00900.108.237203.24 876.86.30
2020-09-02T09:00900.116.635212.35 095.26.32
2020-09-03T09:00900.109.038205.04 920.06.30
2020-09-04T09:00900.115.735214.95 157.66.31
2020-09-05T09:00900.1217.040218.35 239.26.32
2020-09-06T09:00900.1112.039215.35 167.26.32
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干冰升华气相压注工艺技术研究
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陈兴明 1 , 刘方志 2
油气藏评价与开发 | 工程工艺 2026,16(3): 694-701
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油气藏评价与开发 |工程工艺 2026 , 16 (3) : 694 -701
干冰升华气相压注工艺技术研究
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陈兴明（1971—），男，本科，高级工程师，主要从事CO2环保捕集与应用、油气田开发研究等工作。地址：江苏省南京市建邺区江东中路375号金融城9号楼，邮政编码：210019。E-mail：

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陈兴明（1971—），男，本科，高级工程师，主要从事CO2环保捕集与应用、油气田开发研究等工作。地址：江苏省南京市建邺区江东中路375号金融城9号楼，邮政编码：210019。E-mail：

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陈兴明1 , 刘方志2
作者信息
  • 1　中国石化华东油气分公司勘探开发研究院，江苏　 　南京　 　210019
  • 2　中国石化华东石油局液碳公司，江苏　 　泰州　 　225300
通讯作者:
刘方志（1983—），男，硕士，高级工程师，主要从事CCUS-EOR、油气田开发技术服务等工作。地址：江苏省泰州市海陵区南通路99号，邮政编码： 225300。E-mail：
作者简介:

陈兴明（1971—），男，本科，高级工程师，主要从事CO2环保捕集与应用、油气田开发研究等工作。地址：江苏省南京市建邺区江东中路375号金融城9号楼，邮政编码：210019。E-mail：

Research on dry ice sublimation gas phase injection technology
XINGMING CHEN1 , FANGZHI LIU2
Affiliations
  • 1 Research Institute of Exploration and Development, Sinopec East China Oil & Gas Company, Nanjing, Jiangsu 210019, China
  • 2 Sinopec East China Petroleum Bureau Liquid Carbon Company, Taizhou, Jiangsu 225300, China
出版时间: 2026-05-26 doi: 10.13809/j.cnki.cn32-1825/te.20250008
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干冰升华  /  气相压注  /  CO2驱油  /  工艺技术  /  相变理论
dry ice sublimation  /  gas phase injection  /  CO2 flooding  /  process technology  /  phase transition theory
陈兴明, 刘方志. 干冰升华气相压注工艺技术研究. 油气藏评价与开发, 2026 , 16 (3) : 694 -701 . DOI: 10.13809/j.cnki.cn32-1825/te.20250008
XINGMING CHEN, FANGZHI LIU. Research on dry ice sublimation gas phase injection technology[J]. Petroleum Reservoir Evaluation and Development, 2026 , 16 (3) : 694 -701 . DOI: 10.13809/j.cnki.cn32-1825/te.20250008
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随着全球对碳减排和高效采油技术的需求日益迫切[1-7]，CO2驱油技术作为一项既能提高原油采收率又能实现CO2地质封存的绿色技术，受到了广泛关注[8-13]。国外从1953年起开展CO2驱研究，其主要目的是提高油田采收率及实现CO2埋存。其中，CO2压注的方式主要有2种：一是液相压注，以槽车运抵压注站的液体CO2为压注介质，通过在压注站内设置CO2液体储罐、压注泵、换热器等设备，用高压泵压注至地下；二是气相管输、超临界态压注，通过捕集回收烟道气，铺设CO2输送管线，采用压缩机增压的方式实现超临界态压注。中国CO2驱油始于20世纪60年代[14-17]，主要以液相压注方式为主。在中国石油大庆、吉林及中国石化华东、胜利、中原等油田都进行了广泛研究、先导试验及推广应用，已成为比较成熟的提高采收率技术[18-21]。例如，吉林油田2008年开展CO2气相管输、超临界态压注先导试验，取得了良好的驱油效果；2010年，吉林油田建成了处理量5×104 m3/d规模的循环压注装置，将CO2驱产出气进行预处理后与长深4区块的CO2气体混合，通过压缩机升压和变温吸附脱水，形成超临界CO2[22]；2021年，胜利油田启动齐鲁石化—胜利油田CCUS项目，建成了中国最长的超临界压力CO2管道，目前运行状态稳定良好[10]。
传统的液相CO2运输和压注技术存在地域限制显著、运输成本高、源汇匹配难等问题，在偏远地区的油田应用受限尤为突出[23]。干冰升华气相压注工艺作为一种创新解决方案，将干冰运到井场后，先加热使其升华、再经二次加热、压缩形成高压气相CO2，最终压注注气井，能有效破解上述技术瓶颈。相比于液相CO2槽车运输单车载重约25 t的上限，干冰采用货车运输时单车载重可达60 t，具备运输量大、储存方便、安全性高等优势；尤其是在无槽车运输条件且油田位置偏远的区域，该方案提供了一种切实可行的替代方案。此外，干冰升华属于吸热过程，其相变焓变始终为正值，此过程需要输入能量以克服分子间的吸引力，这一特性也可拓展应用于各类需要冷却的工业场景。
本文旨在系统研究干冰升华气相压注工艺的技术原理、工艺路线、系统组成、关键参数，探究其在油田驱油领域的应用实践，剖析该技术推广应用过程中的优势与面临的挑战，为其后续工业化应用提供理论支撑和现场实践参考。
1　干冰升华理论与工艺特性
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1.1　干冰升华的基本原理
CO2通常呈气、液、固3种物态，常温常压下（25 ℃、0.1 MPa）呈气态，化学性质相对稳定，其溶于水中形成碳酸，具有一定腐蚀性（图1），CO2物性参数如表1所示。当CO2的温度处于三相点温度（-56.6 ℃）至临界温度（31.1 ℃）区间时，物态随压力变化发生改变，可呈现气态、液态、固态3种形态；压力较低时为气态；压力升至对应温度的饱和蒸气压以上时，气态液化成液态；压力进一步升高至熔化曲线对应的压力以上时，液态凝固成固态。当温度超过临界温度时：若压力低于临界压力（7.38 MPa），CO₂仅以气态形式存在；若压力同时超过临界压力，CO₂进入超临界状态。干冰（固态CO₂）的稳定存在条件是 “温度低于三相点温度，且压力高于升华线对应的压力”：在此温度下，若控制压力低于升华线对应的压力（远低于三相点压力0.52 MPa），干冰会持续升华并保持气态；若压力高于三相点压力，则需温度升至三相点温度以上，固态才会先熔化为液态，再进一步汽化。因此，在干冰升华过程中，若将压力控制在0~7.38 MPa范围内，温度控制在31.1 ℃以上，干冰升华后CO2可稳定保持气态。
干冰升华是指固态CO2（干冰）不经过液态直接转变为气态的相变过程，其逆过程为凝华（又称气相沉积）。在分子层面，干冰中的CO2分子间主要依赖微弱的色散力（及四级矩作用）；在标准大气压力（0.101 MPa）下，干冰的升华点为-78.5 ℃。当温度达到此点时，表面分子的热运动动能足以抗衡分子间作用力，使其能够脱离晶格直接进入气相，形成持续的升华现象。升华过程需要从环境吸收热量，其热力学强度由摩尔升华焓表征，为正值。在开放环境中，由于气相分子不断扩散，升华过程将持续进行直至固体耗尽[24-25]。
1.2　干冰升华的工艺特性
干冰升华过程具有几个重要特性：首先，在开放系统中，大多数升华的分子会分散在空气中，升华速率大于凝华速率；而在封闭系统中，在固体的升华点处可以建立固体-蒸气平衡。气体与其固体动态平衡时所施加的分压称为蒸气压，干冰在20.0 ℃时的蒸气压高达5.706 50 MPa，这表明干冰具有很高的升华倾向。
为定量关联干冰升华过程的温度、蒸气压与升华速率，基于实验数据表2的趋势性特征，采用分步拟合策略建立简化模型。
1） 温度与蒸气压的关联
首先，假设干冰蒸气压p与绝对温度T（T=t+273.15，t为摄氏温度，单位为℃）满足类 Arrhenius型热力学趋势，对ln p与1/T进行线性拟合，得到关联式：
ln p=-A/T+B
式中：p为干冰蒸气压，单位MPa；T为绝对温度，单位K；A为线性拟合的常数，单位K；B为线性拟合常数。
其中，通过最小二乘法拟合表中“温度-蒸气压”数据，得拟合参数A=3 600 K，B=19。
p=exp(-3 600/T+19)
2） 蒸气压与升华速率的关联
将升华速率“极低、中等、较高、高、很高、极高”量化为等级变量 v（对应量化值 1~6），对v与lnp进行线性拟合，得：
v=0.5ln p+3.3
式中：v为升华速率的相对程度。
该模型通过简化热力学推导，在保留数据趋势一致性的前提下，为干冰升华工艺的参数优化提供了直观、易操作的量化工具，可快速预测不同温度条件下的蒸气压水平及对应升华速率。实验研究表明，在干冰升华平衡过程中，温度上升会直接导致蒸气压（平衡压力）上升。此外，干冰升华速率可以通过外部供热显著提升，采用水流供热可加快干冰升华进程，有效解决自然升华速率较慢的问题。该研究结果可有效为干冰相变发生器的设计提供理论基础。
2　工艺系统与关键技术
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2.1　系统组成与工艺流程
干冰升华气相压注工艺系统主要包括干冰输送、升华反应、加热调温、压缩升压和压注系统等几个核心部分。通过HYSYS软件对干冰升华气相压注工艺流程进行模拟，结果表明：流程运行稳定，气化器温度可达35 ℃以上。具体的工艺流程（图2）如下：
1）干冰运输：采用货车将干冰运输至作业现场。
2）投料过程：通过旋进式投料器（投料速率0~10 t/h）将干冰投放至升华反应器。
3）升华反应：干冰在升华反应器内进行升华，转化为气相CO2。
4）加热处理：升华后的气相CO2由反应器进入气化器，加热至35 ℃以上。在0.1 MPa，288 m³/h的条件下，其他参数录取见表3，通过式（5）和式（6）计算得出：干冰升华所吸收的热量Qs为82 kW，CO2气体升温需要吸收的热量Qg为9.15 kW，最终由式（4）得出干冰升华反应器所提供的最大热量Q为91.15 kW。
Q=Qs+Qg
Qs=qh×qv×ρc
Qg=cp×qv×ρc×∆tc
式中：Q为总热量，单位kW；Qs为干冰升华吸收热量，单位kW；Qg为CO2气体升温吸收热量，单位kW；qh为单位质量干冰升华热，单位 kJ/kg；qv为干冰升华后出口气体的体积流量，单位m³/s；ρc为出口处CO2气体密度，单位kg/m³；cp为气态CO2的恒压比热容，单位J/（kg·℃）；∆tc为干冰表面温度与出口气体温度差，单位℃。
5）缓冲处理：加热后的气相CO2进入CO2缓冲罐，保证压力在0.1~0.3 MPa；
6）压缩压注：缓冲后的气相CO2进入压缩机，经压缩机升压降温后（实验所用压缩机压力最高25 MPa）压注至井内。
2.2　关键技术和设备
干冰升华气相压注工艺的核心技术与设备性能，对整个系统的运行效率、稳定性及经济性起着决定性作用，各关键设备的技术特征与设计要点如下：
干冰升华反应器（图3—图4）：这是一个密闭反应容器，内部安装有4组25 kW电加热棒和1组隔板以构建可控的干冰升华环境。经式（4）计算，该反应器需提供的最大热量为91.15 kW；结合接线端规格、干冰升华反应器的截面尺寸、电加热元件与干冰接触面最大化的设计原则，最终确定选用4组电加热棒的配置方案。反应器设计需重点兼顾热交换效率、压力容器安全规范和连续运行稳定性等因素。
旋进式投料器：用于控制干冰的投料速率，采用机械传动方式可在0~10 t/h范围内调节。投料器的密封性能对防止CO2泄漏和维持系统压力稳定至关重要。
气化器与加热系统：采用PLC可编程控制技术对4组电加热元件进行调控，每组电加热功率可在0~25 kW范围内动态调节，以此实现干冰升华速率的精准控制。气化后的CO₂气体由气化器进一步升温，通过调节气化器旁通阀开度，将气相 CO₂温度稳定控制在35 ℃以上，确保CO₂全程保持气态，避免在后续压缩工序中发生相变或形成干冰颗粒。系统压力调控则通过压缩机变频调节排量的方式实现，以此稳定干冰升华反应器至压缩机进口段的压力区间。
多级压缩系统：采用四级升压（试验数据：一级由0.10 MPa升至0.40 MPa，二级由0.40 MPa升至1.20 MPa，三级由1.20 MPa升至3.60 MPa，四级由3.60 MPa升至6.30 MPa）的压缩方式，将CO2压力提升至所需的压注压力。控制前三级升压压力不超过CO2超临界压力7.38 MPa，同时需保障压缩过程中温度高于CO₂超临界温度31.1 ℃，确保CO₂始终处于气态。多级压缩中间冷却的设计可降低压缩功耗，提高系统效率。
控制系统：对整个工艺过程的关键运行参数（压缩机进出口温度与压力、CO₂流量、级间冷却介质温度与流量、系统泄漏监测指标等）进行实时监测与闭环控制，保障系统安全稳定运行。
3　挑战及矿场应用效果
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3.1　干冰升华气相压注工艺的优势与挑战
与传统液相CO2压注技术相比，该技术具有以下优势：
1） 解决运输难题：干冰运输地域适应性更强，特别适用于偏远地区、沙漠地区或海上平台等无法采用槽船运输液相CO2的场景。针对运输距离较远且水路运输不可行的偏僻压注井，通常采用货车运输的方式。液相CO2采用槽车运输、干冰采用货车运输，1车干冰（密度1.560 g/cm3）净重60 t，体积约为38.5 m3；1车液相CO2（密度1.178 g/cm3）净重25 t，体积约为21.2 m3。在理想状态下，1 m3干冰可升华约800 m3气相CO2；1 m3液相CO2可气化约600 m3气相CO2。经计算可得：1车干冰升华所得的气相CO2约为1车液相CO2气化所得体积的2.4倍。在干冰升华气相压注技术和液相压注技术中，注气成本主要包括3个部分：原料购置成本、运输成本（槽车）以及压注作业成本（电耗、人工、折旧），可得出注气成本计算公式为：注气成本=原料购置成本+运输成本+压注作业成本，成本参数见表4（数据主要参考华东地区注气作业实际费用标准）。
针对干冰升华气相压注技术和液相压注技术，为得到相同量的气相CO2，假设干冰采用专用货车运输，运输距离为x km，干冰购买成本为液相成本的2.5倍，即640元/t时，干冰的运输成本为0.3元/t·km，计算可得货车运输距离大于636.82 km（同时运输距离超过200 km，液相CO2在槽车罐内气化损失量达到1%以上），采用干冰升华气相压注技术的注气成本更低（图5）。
中国石油青海油田敦煌油区开展油井单井CO2吞吐试验，压注气相CO2 30 800 m3（等效于液相 60.5 t）。该液相CO2压注总成本69 575元（含气费、运输费、压注费、人工费；气源选取就近的金昌气源，距离800 km）；对比采用干冰（60 t）的压注方案，其总成本为62 640元。综合测算表明，采用干冰升华气相吞吐比液相CO2吞吐成本节约6 935元（表5）。
2） 源汇匹配灵活：干冰可在中央场地集中生产，再运输至多个分散的注气现场，有效缓解了源汇匹配问题。
3） 经济性良好：虽然干冰生产成本高于液相CO2，但运输和储存成本的降低，能够使整体经济性在某些场景下更具优势。
尽管干冰升华气相压注工艺具有诸多优势，但在技术研发与应用推广过程中仍面临以下挑战：
1） 升华速率控制：干冰升华速率受温度、压力、颗粒粒径和外部供热等多种因素影响，如何实现其速率的精确控制，是该工艺面临的核心技术难点之一。
2） 能量优化利用：干冰升华是吸热过程，需持续供给外部热源；而后续压注环节的CO2压缩过程为放热过程，如何回收利用压缩热以提高系统整体能效，是亟待解决的关键问题。集成蓄热装置、蓄冷装置的能量梯级利用方案，被证实是提升系统能效的可行路径。
3） 干冰颗粒输送：干冰颗粒在输送过程中易发生堵塞和损失，需进一步优化输送系统的设计。旋进式投料器是一种有效的解决方案，但其在连续运行、大流量工况下的长期稳定性，仍需开展进一步的工业化验证。
4 ）经济性提升：目前干冰生产成本相对较高，在一定程度上制约了该技术的规模化推广应用。通过扩大生产规模、优化制备工艺、推进系统集成及强化产业链协同，可进一步降低技术整体成本。
3.2　矿场应用效果
在苏北盆地溱潼凹陷红庄油田H1P2井开展干冰升华气相压注技术矿场试验（图6），压注目的层三垛组一段，该储层孔隙度为19.1%，渗透率为138.5×10-3 µm2，属于中孔中渗储层，地面原油密度介于0.881~ 0.901 g/cm3，地面原油黏度介于115.9~128.2 mPa∙s，地层原油密度在0.844 g/cm3，地层原油黏度14.68 mPa∙s，含硫量为0.22%~0.32%，凝固点为37.0 ℃，初馏点为111 ℃，整体表现为中质油特征。试验过程中，利用货车将干冰运输至注气井现场，并投放至干冰升华反应器中。启动反应器后，打开电加热装置，将电加热功率调至90 kW。随后，反应器出口压力、温度和瞬时流量迅速上升，压力升至0.1 MPa，最高瞬时流量达到218.3 m3/h，升华器内温度稳定在35~40 ℃，开始进行气相压注，试验于2020-09-01T09：00：00启动，连续平稳运行120 h。期间，累计升华干冰60 t，压注气相CO2共计30 456 m3（表6），整套流程运行顺利，成功实现了干冰升华气相压注技术的矿场应用。
吞吐井H1P2开井生产后，综合含水率由95%降至78%，日产油量由0.60 t最高升至3.08 t，油井降水增油效果明显（图7）。截至2021-09-24，H1P2井累增油量为88.13 t；按照原油价格3 000 元/t计算，可获得收益26.44×104 元。
3.3　模拟与试验数据的验证分析
在试验过程中，升华器温度升至35 ℃以上时，反应器出口温度稳定在5 ℃以上（表6）；同时反应器压力控制在0.1 MPa以上且低于三相点压力（0.52 MPa），确保干冰升华后反应器出口的CO₂是气态。如图8所示，AB段为干冰在压力低于三相点压力条件下，随温度升高由固态直接升华成气态的相态变化过程；BC段为CO₂从干冰升华反应器至缓冲罐的相态变化过程（气态CO₂温度从0 ℃升至40 ℃，压力保持0.1 MPa）；CD段为CO₂经压缩机多级压缩，级间冷却，（温度保持40 ℃）的过程，由于温度高于临界温度（31.1 ℃）且压力低于临界压力（7.38 MPa），相态仍为气态。由此可见：试验模拟的升华器温度为35 ℃且压力低于三相点压力（0.52 MPa），满足现场试验的需求，升华后的气相CO₂可实现气相压注。
4　结论
收起
1） 干冰升华是一个吸热相变过程，其相变速率受温度、压力和环境介质条件的显著影响。通过优化干冰升华反应器的结构与操作参数，可有效实现升华速率的精准调控，显著提升气相压注工艺的整体运行效率，为该技术的现场规模化应用奠定了基础。
2） 干冰升华气相压注工艺作为油田提高采收率的创新技术，解决了液相CO2运输距离远、地域限制大、源汇匹配难等问题，在油田提高采收率方面效果显著，可使油井含水率下降，增产效果明显。
3） 该技术当前仍面临升华速率精准调控、能量高效利用及工程经济性提升等关键挑战。未来需要突破升华速率精确控制及多系统集成、新材料开发等多方面研究推动技术进步，使得干冰升华压注工艺技术成本降低20%、升华效率提升至95%以上。随着碳减排战略的深入推进，该技术在油田驱油、CO₂地质封存等领域的应用潜力将进一步释放，可为中国碳中和目标达成及能源行业绿色低碳转型提供重要技术支撑。

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doi: 10.13809/j.cnki.cn32-1825/te.20250008
  • 接收时间：2025-12-31
  • 首发时间：2026-10-30
  • 出版时间：2026-05-26
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  • 收稿日期：2025-12-31
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    1　中国石化华东油气分公司勘探开发研究院，江苏　 　南京　 　210019
    2　中国石化华东石油局液碳公司，江苏　 　泰州　 　225300

通讯作者:

刘方志（1983—），男，硕士，高级工程师，主要从事CCUS-EOR、油气田开发技术服务等工作。地址：江苏省泰州市海陵区南通路99号，邮政编码： 225300。E-mail：
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鹅膏菌科Amanitaceae 2 11 5.26 鹅膏菌属 Amanita 10 4.78
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