KR0141428B1 - Method and apparatus of producing brick using natural stone - Google Patents
Method and apparatus of producing brick using natural stoneInfo
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- KR0141428B1 KR0141428B1 KR1019940022985A KR19940033256A KR0141428B1 KR 0141428 B1 KR0141428 B1 KR 0141428B1 KR 1019940022985 A KR1019940022985 A KR 1019940022985A KR 19940033256 A KR19940033256 A KR 19940033256A KR 0141428 B1 KR0141428 B1 KR 0141428B1
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- high pressure
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- column
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- F25J3/04151—Purification and (pre-)cooling of the feed air; recuperative heat-exchange with product streams
- F25J3/04187—Cooling of the purified feed air by recuperative heat-exchange; Heat-exchange with product streams
- F25J3/04218—Parallel arrangement of the main heat exchange line in cores having different functions, e.g. in low pressure and high pressure cores
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
- F25J3/04078—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression
- F25J3/04084—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression of nitrogen
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
- F25J3/04078—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression
- F25J3/0409—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression of oxygen
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
- F25J3/04284—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams
- F25J3/0429—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams of feed air, e.g. used as waste or product air or expanded into an auxiliary column
- F25J3/04296—Claude expansion, i.e. expanded into the main or high pressure column
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- F25J3/04406—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using a dual pressure main column system
- F25J3/04412—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using a dual pressure main column system in a classical double column flowsheet, i.e. with thermal coupling by a main reboiler-condenser in the bottom of low pressure respectively top of high pressure column
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- F25J3/04406—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using a dual pressure main column system
- F25J3/0443—A main column system not otherwise provided, e.g. a modified double column flowsheet
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- Engineering & Computer Science (AREA)
- Physics & Mathematics (AREA)
- Mechanical Engineering (AREA)
- Thermal Sciences (AREA)
- General Engineering & Computer Science (AREA)
- Health & Medical Sciences (AREA)
- Emergency Medicine (AREA)
- Producing Shaped Articles From Materials (AREA)
- Devices For Post-Treatments, Processing, Supply, Discharge, And Other Processes (AREA)
- Separation By Low-Temperature Treatments (AREA)
Abstract
본 발명은 하기 세가지 면에서 중요한 특징이 있는 극저온 공기 분리 방법에 관한 것이다:The present invention relates to a cryogenic air separation method which is important in three aspects:
(1) 질소-농축 액체의 일부 이상을 생성물로서 증발하고 이송하기 전에 컬럼 시스템으로부터 가압한다는 점;(1) pressurizing at least a portion of the nitrogen-rich liquid from the column system before evaporating and transferring it as a product;
(2) 일부 이상의 공급 공기를, 상기 가압한 질소-농축 스트림과 간접적인 열교환 방식에 의해 일부분 이상을 응축한다는 점; 및(2) condense at least part of the supply air by at least part of the indirect heat exchange with the pressurized nitrogen-enriched stream; And
(3) 고압 칼럼 정상으로부터 나온 증기 질소를 응축한 액체 질소의 일부를 환류로서 고압 칼럼에 복귀시킴과 동시에 남아 있는 부분을 컬럼 시스템으로부터 제거한다는 점.(3) Returning a portion of the liquid nitrogen condensed vapor nitrogen from the high pressure column top to the high pressure column as reflux, while removing the remaining portion from the column system.
Description
제1도 내지 제3도는 본 발명 방법의 세가지 실시 태양의 개략도이다.1 through 3 are schematic diagrams of three embodiments of the method of the present invention.
본 발명은 공기의 극저온 증류에 의한 가압 산소 및 질소 생성물의 제조 방법에 관한 것이다.The present invention relates to a process for producing pressurized oxygen and nitrogen products by cryogenic distillation of air.
가압 산소 및 가압 질소는 많은 상황에서 요구된다. 설비가 및 동력가는 제조 비용에서 중요한 부분이므로, 본 발명의 목적은 가압 산소 및 질소 생성물을 모두 제조하는 방법에 있어서, 설비가 또는 동력가, 또는 둘 모두를 감소시키는 것이다.Pressurized oxygen and pressurized nitrogen are required in many situations. Since equipment cost and power cost are an important part of the manufacturing cost, it is an object of the present invention to reduce equipment cost or power cost, or both, in a process for producing both pressurized oxygen and nitrogen products.
미합중국 특허 제5,148,680호는 먼저 액체 산소 및 액체 질소를 고압으로 승압하고, 그것을 공급 공기의 일부와 열교환에 의해 가온하여 적어도 부분적으로 상기 일부를 응축하므로써 냉각 상자로부터 직접 승압하의 산소 및 질소를 생성하는 펌프된 액체 산소(LOX), 펌프된 액체 질소(LIN)공정을 개시하고 있다. 고압 컬럼의 정상으로부터, 응축된 질소 일부를 저압 컬럼에 환류 상태로 공급한다.U. S. Patent 5,148, 680 discloses a pump that first boosts liquid oxygen and liquid nitrogen to a high pressure, warms it up by heat exchange with a portion of the supply air and condenses the portion at least partially to produce oxygen and nitrogen under elevated pressure directly from the cooling box. Liquid oxygen (LOX) and pumped liquid nitrogen (LIN) processes. From the top of the high pressure column, a portion of the condensed nitrogen is fed to the low pressure column at reflux.
본 발명은 고압 산소 및 질소 기체를 생성하기 위해 압축된 공급 공기 스트림을 분리하는 방법에 관한 것으로, 하기⒜내지 ⒣단계를 포함한다:The present invention relates to a process for separating a compressed feed air stream to produce high pressure oxygen and nitrogen gas, comprising the following steps:
(a) 저압 컬럼 및 고압 컬럼을 구비한 이중 컬럼 시스템을 준비하는 단계;(a) preparing a dual column system having a low pressure column and a high pressure column;
(b) 상기 고압 컬럼에 압축 및 냉각된 공급 공기의 일부 이상을 공급하는 단계;(b) supplying at least a portion of the compressed and cooled feed air to the high pressure column;
(c) 상기 고압 컬럼내에서 단계⒝의 공급 공기의 일부를 질소 증기 및 산소-농축 액체로 분리하는 단계;(c) separating a portion of the feed air of step VII into nitrogen vapor and oxygen-rich liquid in the high pressure column;
(d) 고압 컬럼의 하부로부터 저압 컬럼내 중간 지점으로 산소-농축 액체를 공급하는 단계;(d) feeding an oxygen-rich liquid from the bottom of the high pressure column to an intermediate point in the low pressure column;
(e) 상기 고압 컬럼으로부터 질소-농축 증기의 일부 이상을 응축시켜 액체 질소 스트림을 생성하고;그 액체 질소 스트림의 일부를 고압 컬럼의 정상으로 복귀시키고;남아 있는 액체 질소의 일부를 상기 이중 컬럼 시스템으로부터 제거하는 단계;(e) condensing at least a portion of the nitrogen-condensed vapor from the high pressure column to produce a liquid nitrogen stream; returning a portion of the liquid nitrogen stream to the top of the high pressure column; and transferring a portion of the remaining liquid nitrogen to the dual column system. Removing from the;
(f) 상기 이중 컬럼 시스템으로부터 제거된 질소-농축 액체의 압력을 증가시키는 단계;(f) increasing the pressure of the nitrogen-rich liquid removed from the dual column system;
(g) 공급 공기의 일부를 단계(f)의 고압된 질소-농축 스트림과 간접적인 열교환에 의해 냉각하고, 그 일부 이상을 응축시키는 단계; 및(g) cooling a portion of the feed air by indirect heat exchange with the pressurized nitrogen-enriched stream of step (f) and condensing at least a portion thereof; And
(h) 80％이상의 질소를 함유하는 산소 스트림 및 증기 스트림을 상기 저압 컬럼으로부터 회수하는 단계.(h) recovering from the low pressure column an oxygen stream and a vapor stream containing at least 80% nitrogen.
또한 본 발명은 전술한 공정에 있어서, 단계(h)의 산소 스트림이 액체이며, 액체 산소 스트림의 압력을 고압으로 높이고 공급 공기의 제2부위와 간접적인 열교환에 의해 증발시키는 것에 관한 것이다.The present invention also relates to the above-mentioned process, wherein the oxygen stream of step (h) is a liquid and the pressure of the liquid oxygen stream is raised to high pressure and evaporated by indirect heat exchange with the second portion of the feed air.
본 발명의 방법에는 하기 3가지 중요한 특성이 있다:The method of the present invention has three important characteristics:
(1) 질소-농축 액체의 일부 이상을 생성물로서 증발하고 이송하기 전에 컬럼 시스템으로부터 가압시키는 것;(1) pressurizing at least a portion of the nitrogen-rich liquid from the column system before evaporating and transferring it as a product;
(2) 공급 공기의 일부 이상을, 상기 가압한 질소-농축 스트림과 간접적인 열교환 방식에 의해 적어도 부분적으로 응축시키는 것;(2) condensing at least a portion of the feed air at least partially by indirect heat exchange with the pressurized nitrogen-enriched stream;
(3) 고압 컬럼의 정상으로부터 나온 증기 질소를 응축한 액체 질소의 일부를 고압 컬럼에 환류로서 복귀시킴과 동시에 남아 있는 부분을 컬럼 시스템으로부터 제거하는 것.(3) Returning a portion of the liquid nitrogen condensed vapor nitrogen from the top of the high pressure column as reflux to the high pressure column and removing the remaining portion from the column system.
바람직한 유행에서는, 단계⑶에서 컬럼 시스템에서 나오는 액체 질소의 다른 일부는 단계(1) 의 질소-농축 액체이다. 단계(1) 의 질소-농축 액체를 컬럼 시스템내의 다른 위치로부터 회수할 때, 단계(3)의 다른 일부의 액체 질소의 유속은 0 이 될 수 있다.In a preferred fashion, the other part of the liquid nitrogen coming out of the column system in step VII is the nitrogen-rich liquid of step (1). When recovering the nitrogen-rich liquid of step (1) from another location in the column system, the flow rate of the liquid nitrogen of the other part of step (3) can be zero.
가장 바람직한 유형에서는, 컬럼 시스템으로부터 액체 산소의 일부를 고압으로 펌프하고, 또한 적어도 부분적으로 응축된 공급 공기 스트림의 일부와 열교환에 의해 증발시킨다. 이것은 고압 산소 생성물 스트림을 함께 생성시킬 것이다.In the most preferred type, a portion of the liquid oxygen from the column system is pumped to high pressure and also evaporated by heat exchange with at least a portion of the partially condensed feed air stream. This will produce a high pressure oxygen product stream together.
본 발명의 방법은 몇가지 구체적인 실시 태양을 참고로 가장 잘 이해될 수 있다.The method of the present invention may be best understood with reference to some specific embodiments.
제1도는 본 발명의 한 실시 태양이다. 제1도에 의하면, 압축되고 오염물이 제거된 공급 공기, 라인(100)은 먼저 두 개의 서브 스트림인, 라인(102) 및 (120)으로 분리된다. 제1서브 스트림인 라인(102)를 열교환기(1)내에서 극저온으로 냉각시키고, 팽창기 유출액 라인(108)과 혼합하여 고압컬럼 공급라인(11)을 형성시키고, 그 후 고압 컬럼(5)에 공급한다. 다른 서브 스트림인 라인(120)을 응축기(14)에 의해 추가로, 압력을 상승시키고, 냉각시킨 뒤, 라인(14) 및 (124)의 두부분으로 추가로 분리시켰다. 그 제1부분인 라인(140)을 열교환기 (2)에서 중간 온도로 냉각시킨 뒤 팽창기 내에서 팽창시켰다. 그 팽창기 유출액인 라인(108)을 상기 냉각 공기의 제1부분인 라인(106)과 혼합하여 고압 컬럼 공급 라인(110)을 형성한다. 또한, 그 제2부분인 라인(124)를 팽창기(12)에 기계적으로 결합되어 있는 압축기(11)에 의해 압축한다. 이후에 추가 압축된 그 제2부분을 후기 냉각하고, 열교환기(2)에서 -220℉이하, 바람직하게는 -250℉이하의 온도(이렇게 하면, 조밀한 유체가 됨)로 추가 냉각하고, 두 개의 부분 라인(157) 및 (158)로 분리한다. 이 조밀한 유체의 제1부분인 라인(157)을 고압 컬럼(5)의 중간 지점에 공급할 수 있다. 남은 부분인 라인(158)을 차 냉각기(3)에서 추가로 차냉각(subcool)시킨다.1 is an embodiment of the present invention. According to FIG. 1, compressed and decontaminated feed air, line 100 is first separated into two sub-streams, lines 102 and 120. The first sub-stream, line 102, is cooled to cryogenic temperature in the heat exchanger 1 and mixed with the expander effluent line 108 to form a high pressure column feed line 11, and then to the high pressure column 5 Supply. Another substream, line 120, was further separated by two parts, lines 14 and 124, after the pressure was raised, cooled by the condenser 14. Line 140, its first part, was cooled to medium temperature in heat exchanger 2 and then expanded in an expander. Line 108, the expander effluent, is mixed with line 106, the first portion of the cooling air, to form a high pressure column feed line 110. In addition, the second portion of the line 124 is compressed by the compressor 11 which is mechanically coupled to the expander 12. The later compressed second part is subsequently cooled and further cooled in a heat exchanger (2) to a temperature below -220 ° F, preferably below -250 ° F (this results in a dense fluid), Into two partial lines 157 and 158. Line 157, the first portion of this dense fluid, can be fed to the intermediate point of the high pressure column 5. The remaining portion, line 158, is further subcooled in the car cooler 3.
이 차냉각된 부위인 라인(162)를 그후 저압 컬럼(6)의 정상에 환류로서 공급한다.This quenched portion, line 162, is then fed to the top of the low pressure column 6 as reflux.
고압 컬럼(5)에 공급되는 라인(110) 및 (157)을 증류하여 질소 증기 스트림 및 산소-농축 하부 액체로 분리시킨다. 증기 질소를 저압 칼럼(6)의 하부에 위치한 재끓임 장치(roboiler)/콘덴서에서 응축시켰다. 이 액체 질소의 일부를 환류로서 고압 컬럼(5)에 복귀시켰다. 남아 있는 부위인 라인(40)을 생성물 액체 질소 라인(600)과 가압된 액체 질소 라인(410)으로 분리한다. 가압한 액체 질소 라인(410)을 그후 펌프(13)에 의해 고압으로 펌프하고 열교환기(2)내에서 가열 및 증발하여 고압이며 주위 온도와 가까운 상태의 기체 질소 생성물 라인(400)을 얻는다.Lines 110 and 157 fed to the high pressure column 5 are distilled off to separate the nitrogen vapor stream and the oxygen-rich bottom liquid. Vapor nitrogen was condensed in a reboiler / condenser located at the bottom of the low pressure column (6). A portion of this liquid nitrogen was returned to the high pressure column 5 as reflux. The remaining portion, line 40, is separated into product liquid nitrogen line 600 and pressurized liquid nitrogen line 410. The pressurized liquid nitrogen line 410 is then pumped to high pressure by the pump 13 and heated and evaporated in the heat exchanger 2 to obtain a gaseous nitrogen product line 400 at high pressure and close to ambient temperature.
고압 컬럼(5)로부터 나온 산소-농축된 하부 액체 라인(10)을 저압 컬럼(6)의 중간 지점으로 공급한다. 이 스트림 및 저압 컬럼(6)의 정상에 공급된 액체 공기 라인(162)를 저압 컬럼(6)에서 증류하고 하부 액체 산소 및 80％이상의 질소를 함유하는 상부 질소-농축 물로 분리시킨다. 하부 액체 산소의 일부인 라인(20)을 저압 컬럼(6)의 하부로부터 제거한 후 액체 산소 생성물 라인(700) 및 열교환기(1)내에서 주위 온도 가까이 까지 증발하고 가열하여 기체 산소 생성물 라인(200)으로 제거한다. 그 상부 질소-농축물을 저압 컬럼(6)의 정상으로부터 라인(30)에 의해 제거하고 라인(30)을 차냉각기(3)에서 가열하고 라인(304) 및 (312)의 두 부분으로 분리한다. 그후, 이 두 개의 스트림을 배출하거나 또는 공기 정화 흡착 베드에서 재생되기 전에 열교환기(1)과(2)에서 각각 주위 온도까지 가열한다.The oxygen-concentrated lower liquid line 10 from the high pressure column 5 is fed to the midpoint of the low pressure column 6. This stream and the liquid air line 162 fed to the top of the low pressure column 6 are distilled in the low pressure column 6 and separated into upper nitrogen-concentrated water containing lower liquid oxygen and at least 80% nitrogen. A portion of the bottom liquid oxygen 20 is removed from the bottom of the low pressure column 6 and then vaporized and heated to near ambient temperature in the liquid oxygen product line 700 and heat exchanger 1 to heat the gaseous oxygen product line 200. To remove it. The upper nitrogen-concentrate is removed from the top of the low pressure column 6 by line 30 and the line 30 is heated in the subcooler 3 and separated into two parts of lines 304 and 312. . These two streams are then heated to ambient temperature in the heat exchangers 1 and 2, respectively, before being discharged or regenerated in an air purification adsorptive bed.
제2도의 실시 태양은 제1도에서 나타낸 것과 유사하다. 그 차이는 다음과 같다. 그 첫 번째는 제2의 압축된 공급 공기 서브 스트림인 라인(124)를 추가하여 더 압축시킨 후 두 개의 서브 부위, 즉 라인(144) 및 (126)으로 분리한다는 것이다. 제1의 서브 부위 즉, 라인(126)을 열교환기(4)에서 가온한 산소 스트림과 간접적인 열교환 방식으로 냉각하고, 추가로 열교환기(4)의 중간 지점에서 두 개의 스트림 즉, 라인(130) 및 (148)로 분리한다. 또한, 제1스트림인 라인(130)을 열교환기(4)에서 가온한 산소와 간접 열교환 방식으로 공기의 임계 온도 이하의 온도로 냉각시킨다. 기타 서브의 부위인 라인(144)를 열교환기(4)의 스트림인 라인(148)과 연결된 열교환기(2)에서 중온으로 냉각하고, 추가하여 -220℉이하, 바람직하게는 -250℉이하의 온도로 냉각한다. -220℉이하로 냉각한 고압 공기 스트림인, 라인(152) 및 (132)를 그후 연결한다. 두 번째는, 저압 컬럼(6)으로 부터 나오는 액체 산소 라인(20)을 펌프(15)에 의해 고압으로 펌프한 후 열교환기(4)에서 주위 온도로 증발 및 가열하는 것이다. 마지막으로는, 임의 조작으로서, 불순한 액체 질소 스트림인 라인(42)를 고압 컬럼의 중간 지점으로부터 회수하고, 차냉각기(3)의 냉각 구역에서 차냉각하고 액체 공기 라인(158)과 함께 저압 칼럼(6)의 정상으로 공급하는 것이다.The embodiment of FIG. 2 is similar to that shown in FIG. The difference is as follows. The first is to add a second compressed feed air substream, line 124, to further compress and then separate it into two sub-sites, lines 144 and 126. The first sub-site, ie line 126, is cooled in an indirect heat exchange manner with the heated oxygen stream in the heat exchanger 4, and further two streams, i.e. line 130, at the midpoint of the heat exchanger 4 ) And (148). In addition, the first stream line 130 is cooled to a temperature below a critical temperature of air by indirect heat exchange with oxygen heated in the heat exchanger 4. Line 144, which is the part of the other sub, is cooled to medium temperature in heat exchanger 2 connected to line 148, which is a stream of heat exchanger 4, and further added to -220 DEG F., preferably -250 DEG F. Cool to temperature. Lines 152 and 132 are then connected, which are high pressure air streams cooled below -220 ° F. The second is to pump the liquid oxygen line 20 from the low pressure column 6 to a high pressure by means of a pump 15 and then evaporate and heat it to ambient temperature in the heat exchanger 4. Finally, as an optional operation, the line 42, which is an impure liquid nitrogen stream, is withdrawn from the middle point of the high pressure column, is cooled in the cooling zone of the differential cooler 3 and the low pressure column with the liquid air line 158 ( It is to be supplied to the top of 6).
제3도는 본 발명의 또 다른 실시 태양이다. 제3도의 실시 태양과 제2도의 실시 태양간의 차이는 제2도는 고압 컬럼(6)의 중간 지점으로부터 회수되는 불순한 액체 질소 스트림인 라인(42)를 차냉각기(3)의 냉각 구역에서 차냉각시키고 저압 컬럼(6)의 정상으로 공급시키지만 제3도는 액체 공기 라인(158)을 저압 컬럼(6)의 중간 지점에 공급한다는 점이다. 실시 태양의 기타 부분은 제2도와 같다.3 is another embodiment of the present invention. The difference between the embodiment of FIG. 3 and the embodiment of FIG. 2 is that FIG. 2 cools the line 42 in the cooling zone of the differential cooler 3, which is an impure liquid nitrogen stream withdrawn from the midpoint of the high pressure column 6. While feeding to the top of the low pressure column 6, FIG. 3 shows that the liquid air line 158 is fed to the midpoint of the low pressure column 6. Other parts of the embodiment are shown in FIG.
상기 상세한 설명에서 증명된 바와같이 본 발명은 미합중국 특허 제5,148,680호(배경 기술 공정)에 교수된 공정과는 다른데, 배경 기술에 언급된 공정은 고압 컬럼 정상으로부터 환류로서 저압 컬럼으로 가는 증기 질소로부터 응축된 액체 질소 스트림을 가지는데 반해, 본 발명은 고압 컬럼의 상부로부터 나온 증기 질소를 응축시킨 액체 질소를 일부, 환류로서 고압 칼럼으로 복귀시키고, 일부는 증류 컬럼 시스템 밖으로 제거한다. 본 발명에서는 상기 액체 질소는 환류로서 저압 컬럼에 전혀 공급되지 않는다.As demonstrated in the above description, the present invention differs from the process taught in US Pat. No. 5,148,680 (background process), wherein the process referred to in the background art condenses from steam nitrogen going from a high pressure column top to a low pressure column as reflux. In contrast to having a liquid nitrogen stream, the present invention recovers, in part, reflux the liquid nitrogen condensed vapor nitrogen from the top of the high pressure column to the high pressure column, and partly out of the distillation column system. In the present invention, the liquid nitrogen is not supplied to the low pressure column at all as reflux.
명백히, 본 발명은 미합중국 특허 제5,148,680호의 저 압축 기계에 드는 비용에 비해 유리한 점을 가지고 있다. 그러나 제1도 및 제2도의 실시 태양을 사용하면, 본 발명의 사이클에는 저압 컬럼의 정상 구역이 없기 때문에 추가의 경비 절감을 발생시킨다. 또한, 제3도의 실시 태양을 사용하면, 저압 칼럼에 대한 불순한 환류를 배제하기 때문에 트레이를 최적화하여 산소 및 질소의 최적 회수율을 얻을 것이다. 최적의 회수율은 자본 또는 동력 또는 둘 모두를 절약할 수 있다. 제2도의 실시 태양을 사용하는 시뮬레이션을 한 결과를 하기표에 요약하였다. 생성물인 산소(스트림(200)) 및 질소(스트림(400) 및 (600))의 순도는 각각, 98％ O₂및 6 vppm O₂였다.Clearly, the present invention has an advantage over the cost of a low compression machine of US Pat. No. 5,148,680. However, using the embodiments of FIGS. 1 and 2, the cycle of the present invention results in additional cost savings since there are no normal zones of low pressure columns. In addition, using the embodiment of FIG. 3, the trays will be optimized to achieve optimal recovery of oxygen and nitrogen since eliminating impure reflux to the low pressure column. Optimum recovery can save capital, power, or both. The results of the simulations using the embodiment of FIG. 2 are summarized in the table below. The purity of the products, oxygen (stream 200) and nitrogen (streams 400 and 600), were 98% O 2 and 6 vppm O 2, respectively.
본 발명, 특히, 부분적으로 응축된 공급 공기 부분의 한 부위가 불순한 환류로 저압 컬럼의 상부로 공급될 때, 및 생성물의 압력이 높은 지점에서는, 저압 컬럼내에 어떠한 질소 환류도 없음으로 인해 얻어진 낮은 산소 회수율은 전체적인 에너지 낭비 또는 자본 낭비를 일으키지 않는다는 것이 본 발명의 예기치 않았던 잇점이다. 본 발명의 공정은 특히, 산소 및 질소 모두를 매우 고압 상태에서 필요로 할 때 유리하다.Low oxygen obtained in the present invention, in particular when a portion of the partially condensed feed air portion is fed to the top of the low pressure column with impurity reflux and at a point where the product pressure is high, no nitrogen reflux in the low pressure column It is an unexpected advantage of the present invention that the recovery does not cause overall energy waste or capital waste. The process of the present invention is particularly advantageous when both oxygen and nitrogen are required at very high pressures.
본 발명은 몇가지 구체적인 실시 태양을 참고로 기술하였다. 이 실시 태양들은 본 발명에 어떤 제한으로 비춰져서는 안된다. 본 발명의 범위는 하기 특허 청구 범위로부터 확정되어야 한다.The present invention has been described with reference to some specific embodiments. These embodiments should not be viewed as limiting to the present invention. The scope of the invention should be confirmed from the following claims.
Claims (15)
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| KR1019940022985A KR0141428B1 (en) | 1993-09-15 | 1994-12-08 | Method and apparatus of producing brick using natural stone |
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| KR1019940022985A KR0141428B1 (en) | 1993-09-15 | 1994-12-08 | Method and apparatus of producing brick using natural stone |
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| KR100439519B1 (en) * | 2000-12-21 | 2004-07-15 | 주식회사 길종합건축사사무소 | Boundary stone using natural stone and manufacturing method thereof |
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| KR100439519B1 (en) * | 2000-12-21 | 2004-07-15 | 주식회사 길종합건축사사무소 | Boundary stone using natural stone and manufacturing method thereof |
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