子分类：
| 序号 | 专利名 | 申请号 | 申请日 | 公开（公告）号 | 公开（公告）日 | 发明人 |
|---|---|---|---|---|---|---|
| 1 | 低孔隙率的无水碳酸钠 | CN201280060515.X | 2012-11-10 | CN103998378A | 2014-08-20 | J·克拉特亚科; H-K·佩特; T·韦德尔; G·莫德尔摩格 |
| 本发明涉及用在药物制剂和食品工业中的高纯度、低孔隙率的无水碳酸钠。还提供制备所述碳酸钠的新方法。 | ||||||
| 2 | 从钠矿的盐水生产钠盐的方法 | CN94192254.5 | 1994-01-13 | CN1039436C | 1998-08-05 | W·C·科彭哈弗; D·E·史密斯; G·F·尼德林豪斯 |
| 一种从含碳酸钠和碳酸氢钠的盐水生产含钠化学品的方法，其特征在于，通过在100℃至140℃的温度下加热盐水以蒸发水分，将碳酸氢钠转变为碳酸钠并从中除去得到的二氧化碳，将得到的具有降低的碳酸氢钠含量的盐水与足以使在得到的盐水中所有残存的碳酸氢钠均转变成碳酸钠的氢氧化钠水溶液反应，冷却经氢氧化钠处理的盐水至5℃至25℃的温度，沉淀出十水合碳酸钠晶体，从其母液中分离十水合碳酸钠晶体，熔化分离的十水合碳酸钠晶体以生成碳酸钠溶液，加热所得到的碳酸钠溶液至60℃以上110℃以下的温度以蒸去水分，沉淀出一水合碳酸钠晶体，从其母液中分离出一水合碳酸钠晶体，煅烧分离的一水合碳酸钠晶体以生成苏打灰并回收苏打灰。 | ||||||
| 3 | 低孔隙率的无水碳酸钠 | CN201280060515.X | 2012-11-10 | CN103998378B | 2016-12-14 | J·克拉特亚科; H-K·佩特; T·韦德尔; G·莫德尔摩格 |
| 本发明涉及用在药物制剂和食品工业中的高纯度、低孔隙率的无水碳酸钠。还提供制备所述碳酸钠的新方法。 | ||||||
| 4 | 用于从矿石生产气体的方法 | CN201080006994.8 | 2010-02-09 | CN102307809B | 2016-01-13 | 弗朗西斯·库斯特里; 佩里内·达瓦纳; 克劳德·克里亚多; 时达伊·周 |
| 用于从一种矿石、并且特别是从天然碱矿中生产一种气体的方法，所述气体具有以干气体表示的、大于25体积百分比的二氧化碳浓度，以及一个挥发性有机化合物的量，这个量对于每千克所产生二氧化碳是小于700mg。该方法包括以下步骤：将该天然碱矿压碎，将压碎的天然碱引入到伴有间接加热的一个旋转煅烧滚筒中，在该煅烧装置中将压碎的天然碱进行煅烧，从该煅烧装置中收集煅烧的天然碱并且从煅烧装置中收集通过天然碱矿煅烧所产生的气体，从而组成生产的气体。 | ||||||
| 5 | 制备碳酸钾的工艺和设备 | CN94102912.3 | 1994-03-17 | CN1092379A | 1994-09-21 | R·希尔德豪尔; K·丹尼克 |
| 碳酸钾煅烧物或水合物制备装置中的粉末或研磨料加入结晶和固体分离后的湿离析盐并混合。有或无混合物循环的搅拌器安装在离析盐的固体分级及煅烧物和水合物制备装置入口之间。碳酸钾水合物的制备时部分煅烧物粉末与离析盐或粉末和离析盐的混合物混合。碳酸钾水合物用搅拌器制备，省去制备碳酸钾水合物的加热干燥装置。本发明免除了粉末返回结晶工艺，解决了大量形成粉末和附聚物的问题，提高了生产能力，产品颗粒结构得到改善。 | ||||||
| 6 | 用于从矿石生产气体的方法 | CN201080006994.8 | 2010-02-09 | CN102307809A | 2012-01-04 | 弗朗西斯·库斯特里; 佩里内·达瓦纳; 克劳德·克里亚多; 时达伊·周 |
| 用于从一种矿石、并且特别是从天然碱矿中生产一种气体的方法，所述气体具有以干气体表示的、大于25体积百分比的二氧化碳浓度，以及一个挥发性有机化合物的量，这个量对于每千克所产生二氧化碳是小于700mg。该方法包括以下步骤：将该天然碱矿压碎，将压碎的天然碱引入到伴有间接加热的一个旋转煅烧滚筒中，在该煅烧装置中将压碎的天然碱进行煅烧，从该煅烧装置中收集煅烧的天然碱并且从煅烧装置中收集通过天然碱矿煅烧所产生的气体，从而组成生产的气体。 | ||||||
| 7 | 制备冻干的碳酸氢钠的方法 | CN200680037872.9 | 2006-09-01 | CN101282908A | 2008-10-08 | M·V·R·克里斯南; B·瓦沙斯塔; S·加德 |
| 本发明提供一种制备冻干的结晶碳酸氢钠的方法。 | ||||||
| 8 | 从钠矿的盐水生产钠盐的方法 | CN94192254.5 | 1994-01-13 | CN1124503A | 1996-06-12 | W·C·科彭哈弗; D·E·史密斯; G·F·尼德林豪斯 |
| 一种从含碳酸钠和碳酸氢钠的盐水生产含钠化学品的方法，其特征在于，通过在100℃至140℃的温度下加热盐水以蒸发水分，将碳酸氢钠转变为碳酸钠并从中除去得到的二氧化碳，将得到的具有降低的碳酸氢钠含量的盐水与足以使在得到的盐水中所有残存的碳酸氢钠均转变成碳酸钠的氢氧化钠水溶液反应，冷却经氢氧化钠处理的盐水至5℃至25℃的温度，沉淀出十水合碳酸钠晶体，从其母液中分离十水合碳酸钠晶体，熔化分离的十水合碳酸钠晶体以成碳酸钠溶液，加热所得到的碳酸钠溶液至60℃以上110℃以下的温度以蒸去水分，沉淀出一水合碳酸钠晶体，从其母液中分离出一水合碳酸钠晶体，煅烧分离的一水合碳酸钠晶体以生成苏打灰并回收苏打灰。 | ||||||
| 9 | 纯碱减水剂及其工艺和使用方法 | CN92106693.7 | 1992-08-28 | CN1083022A | 1994-03-02 | 丁永发 |
| 一种用于碳酸钠产品生产的减水制剂和用法，属于碳酸盐生产技术领域。它是应用以醇醚和酚醚表面活性剂为主剂，有机硅为消泡剂，醇类和去离子水为溶剂，各组分的重量百分比为：醇醚型表面活性剂 5—10％酚醚型表面活性剂 25—40％有机硅消泡剂 1—5％醇类 1—5％去离子水 40—68％用这种制剂对纯碱的中间产物碳酸氢钠进行化学减水处理，使其含水量相对降低5—20％。 | ||||||
| 10 | 空孔含量が少ない無水炭酸ナトリウム | JP2014545123 | 2012-11-10 | JP2015500195A | 2015-01-05 | イェンス クラトユク、; ハンス−クルト ペト、; トールシュテン ヴェーデル、; ギュンター モデルモグ、 |
| 本発明は、医薬配合物及び食品産業において使用するための空孔量が少ない高純度の無水炭酸ナトリウムに関する。さらに、この炭酸ナトリウムの製造のための新規な方法が提供される。 | ||||||
| 11 | Easily dissolvable sodium bicarbonate and its production | JP1004089 | 1989-01-20 | JPH01282118A | 1989-11-14 | NAKAYA KEIICHI; SATO KUNIO |
| PURPOSE: To give both sufficient flowability and ease dissolution to sodium bicarbonate by specifying the dissolving time, abrasion rate and angle of repose of the sodium bicarbonate in which crystalline primary particles aggregate without an org. binder. CONSTITUTION: The targeted sodium bicarbonate is obtd. by mixing a liq. with sodium bicarbonate raw material powder consisting of crystalline primary particle, so that the water content becomes 0.5W10wt.%, by granulating and by drying in a CO 2 gas atmosphere. The sodium bicarbonate is granular sodium bicarbonate (secondary particle), and the dissolving time of the secondary particle is less than 3 times, its abrasion rate is ≤50% and its angle of repose is ≤50°, compared with the primary particle. As the liq. to be added when granulated, water can be used and, however, the abrasion rate is improved by using the liq. capable of forming sodium carbonate soln. as liq. phase existing among primary particles of the granulated material, because of increasing bonding strength among the primary particles. COPYRIGHT: (C)1989,JPO&Japio | ||||||
| 12 | JPS616010B2 - | JP7853978 | 1978-06-30 | JPS616010B2 | 1986-02-22 | IGAWA KAZUNARI; SAITO HIROYUKI; KIKUCHI MITSUO |
| 13 | Manufacture of anhydrous sodium carbonate crystal | JP1147580 | 1980-02-04 | JPS56109819A | 1981-08-31 | NAKAYA KEIICHI; KAWANAMI KOUJI; HIRATA SUEICHI |
| PURPOSE: To manufacture hard anhydrous sodium carbonate crystals of a uniform grain size in an energy saving manner by condensing steam generated from a vessel for depositing sodium carbonae hydrate crystals in a vessel for depositing anhydrous sodium carbonate crystals and suitably circulating an aqueous soln. or a slurry though the vessels. CONSTITUTION: Porous sodium carbonate and supplied water are fed to vessel 1 for depositing sodium carbonate hydrate crystals from lines 5, 6, respectively. A slurry contg. hydrate crystals deposited in vessel 1 is fed to vessel 2 for depositing anhydrous sodium carbonate crystals through line 8, and steam generated in vessel 1 is pressurized with blower 3, fed to vessel 2, and condensed to supply heat to vessel 2. A slurry contg. anhydrous sodium carbonate crystals deposited in vessel 2 is passed through separator 4 to separate the crystals, and the remaining soln. is returned to vessel 2 through line 13. On the other hand, the clarified liq. in vessel 2 is circulated to vessel 1 through line 7. COPYRIGHT: (C)1981,JPO&Japio | ||||||
| 14 | JPS5027800A - | JP4967074 | 1974-05-02 | JPS5027800A | 1975-03-22 | |
| 15 | 수화물 탄산칼륨의 제조방법 | KR1020130054907 | 2013-05-15 | KR101475605B1 | 2014-12-22 | 한웅; 장우성; 조예현; 송기강 |
| 본발명은무수탄산칼륨에, 0.1 내지 19.0중량% 탄산칼륨수용액, 포화탄산칼륨이상의농도를갖는포화탄산칼륨수용액과탄산칼륨결정을혼합시킨혼합용액, 물및 스팀으로이루어진군에서선택되는하나이상의반응물질을가하여반응시키는것을포함하는수화물탄산칼륨의제조방법을제공한다. | ||||||
| 16 | PRODUCTION OF WATER-FREE SODA | EP98966423.0 | 1998-12-22 | EP1042226B1 | 2002-04-10 | MEIJER, Johannes, Albertus, Maria; GEERTMAN, Robert, Michael; OOSTERHOF, Harald; WITKAMP, Geert-Jan; VAN ROSMALEN, Gerda, MAria |
| A process is presented in which anhydrous soda is crystallized and worked up to produce anhydrous soda crystals with a bulk density from 1300 to 1600 kg/m<3>. The process is characterized in that a solvent is used that allows the crystals to be formed and handled at atomspheric pressure in the presence of water without the monohydrate of soda being formed. | ||||||
| 17 | Process for production of dense soda ash from soda ash fines | EP96201222.5 | 1996-05-02 | EP0742175B1 | 2001-03-21 | Delling, David R; Green, Kevin L; Phillip, James D; Robertson, Donald M |
| 18 | Installation et procédé pour la cristallisation d'une substance minérale et procédé et installation pour la cristallisation de carbonate de sodium monohydraté | EP93200741.2 | 1993-03-15 | EP0562665B1 | 1997-10-01 | Ninane, Léon; Breton, Claude |
| 19 | Method of production of extra light soda | EP89109475.7 | 1989-05-26 | EP0343673A1 | 1989-11-29 | Neuzil CSc, Lubomir, Doz.Ing.; Bejcek CSc, Václav, Dipl.-Ing.; Mocek, CSc, Karel, Dipl.-Ing.; Koza CSc, Václav, Dipl.-Ing.; Erdös, DrSc, Emerich, Doz. Dr. Ing.; Wald, Jiri, Dipl.-Ing.; Vlcek, Anton; Lippert CSc, Erich, Dipl.-Ing. |
The inventive method of production of sodium carbonate is suited for removal of various admixtures from gaseous mixtures especially sulfur dioxide, eventually also sulfur trioxide, nitrogen oxides (NOx), hydrogen chloride, hydrogen fluoride etc. The starting material is represented either by sodium carbonate hydrate with a water content given by its relative molar ratio 7.5<XW≦10.5, or by its mixture with an aqueous solution of sodium carbonate. From this starting material is first prepared a hydrate of sodium carbonate with a water content XW≦7.5 by thermal decomposition or by microwave radiation, whereby the temperature of the hydrate being dicomposed must be kept in the range of 32-35.3°C. With the same results the starting material can also be dried at a temperature of this material of up to 32°C. This hydrate is further dried at a temperature of the hydrate of up to 35.3°C until the water content of the sodium carbonate hydrate reaches a value XW≦4. Thereafter the process is finished by drying at an arbitrary temperature of the sodium carbonate of up to 450°C, whereby the final steps of drying are preferably performed by a gaseous mixture having a temperature above 100°C and containing the component which should be removed. Thus the formed sodium carbonate of the water content XW≦1.05 immediately removes the admixtures from the gaseous mixture. The described method is designed to be utilized both on smaller and bigger sources of admixtures to gases, e.g. in paper and pulp mills or in heat generation plants based on fossil energy sources. |
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| 20 | Procédé et installation pour la fabrication de carbonate de sodium monohydraté | EP82201037.7 | 1982-08-18 | EP0073085B1 | 1986-03-12 | Verlaeten, Jean; Guerdon, Constant; Caubet, Jean; Walter, André |
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