WO2007139392A1 - A modified solvay process, and uses thereof for processing co2-containing gas streams and for desalination - Google Patents

A modified solvay process, and uses thereof for processing co2-containing gas streams and for desalination Download PDF

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Publication number
WO2007139392A1
WO2007139392A1 PCT/NO2007/000186 NO2007000186W WO2007139392A1 WO 2007139392 A1 WO2007139392 A1 WO 2007139392A1 NO 2007000186 W NO2007000186 W NO 2007000186W WO 2007139392 A1 WO2007139392 A1 WO 2007139392A1
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ammonia
chloride
carbon dioxide
ammonium
gas
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PCT/NO2007/000186
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French (fr)
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Omar Chaalal
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Enpro As
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    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01D—COMPOUNDS OF ALKALI METALS, i.e. LITHIUM, SODIUM, POTASSIUM, RUBIDIUM, CAESIUM, OR FRANCIUM
    • C01D7/00—Carbonates of sodium, potassium or alkali metals in general
    • C01D7/18—Preparation by the ammonia-soda process
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/46—Removing components of defined structure
    • B01D53/62—Carbon oxides
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B9/00—General methods of preparing halides
    • C01B9/02—Chlorides
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01C—AMMONIA; CYANOGEN; COMPOUNDS THEREOF
    • C01C1/00—Ammonia; Compounds thereof
    • C01C1/02—Preparation, purification or separation of ammonia
    • C01C1/026—Preparation of ammonia from inorganic compounds
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01C—AMMONIA; CYANOGEN; COMPOUNDS THEREOF
    • C01C1/00—Ammonia; Compounds thereof
    • C01C1/16—Halides of ammonium
    • C01C1/164—Ammonium chloride
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01C—AMMONIA; CYANOGEN; COMPOUNDS THEREOF
    • C01C1/00—Ammonia; Compounds thereof
    • C01C1/26—Carbonates or bicarbonates of ammonium
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01D—COMPOUNDS OF ALKALI METALS, i.e. LITHIUM, SODIUM, POTASSIUM, RUBIDIUM, CAESIUM, OR FRANCIUM
    • C01D7/00—Carbonates of sodium, potassium or alkali metals in general
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01D—COMPOUNDS OF ALKALI METALS, i.e. LITHIUM, SODIUM, POTASSIUM, RUBIDIUM, CAESIUM, OR FRANCIUM
    • C01D7/00—Carbonates of sodium, potassium or alkali metals in general
    • C01D7/12—Preparation of carbonates from bicarbonates or bicarbonate-containing product
    • C01D7/123—Preparation of carbonates from bicarbonates or bicarbonate-containing product by thermal decomposition of solids in the absence of a liquid medium
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01F—COMPOUNDS OF THE METALS BERYLLIUM, MAGNESIUM, ALUMINIUM, CALCIUM, STRONTIUM, BARIUM, RADIUM, THORIUM, OR OF THE RARE-EARTH METALS
    • C01F11/00—Compounds of calcium, strontium, or barium
    • C01F11/20—Halides
    • C01F11/24—Chlorides
    • C01F11/28—Chlorides by chlorination of alkaline-earth metal compounds
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01F—COMPOUNDS OF THE METALS BERYLLIUM, MAGNESIUM, ALUMINIUM, CALCIUM, STRONTIUM, BARIUM, RADIUM, THORIUM, OR OF THE RARE-EARTH METALS
    • C01F5/00—Compounds of magnesium
    • C01F5/26—Magnesium halides
    • C01F5/30—Chlorides
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/66—Treatment of water, waste water, or sewage by neutralisation; pH adjustment
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L3/00—Gaseous fuels; Natural gas; Synthetic natural gas obtained by processes not covered by subclass C10G, C10K; Liquefied petroleum gas
    • C10L3/06—Natural gas; Synthetic natural gas obtained by processes not covered by C10G, C10K3/02 or C10K3/04
    • C10L3/10—Working-up natural gas or synthetic natural gas
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L3/00—Gaseous fuels; Natural gas; Synthetic natural gas obtained by processes not covered by subclass C10G, C10K; Liquefied petroleum gas
    • C10L3/06—Natural gas; Synthetic natural gas obtained by processes not covered by C10G, C10K3/02 or C10K3/04
    • C10L3/10—Working-up natural gas or synthetic natural gas
    • C10L3/101—Removal of contaminants
    • C10L3/102—Removal of contaminants of acid contaminants
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2251/00—Reactants
    • B01D2251/20—Reductants
    • B01D2251/206—Ammonium compounds
    • B01D2251/2062—Ammonia
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2251/00—Reactants
    • B01D2251/40—Alkaline earth metal or magnesium compounds
    • B01D2251/402—Alkaline earth metal or magnesium compounds of magnesium
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2251/00—Reactants
    • B01D2251/40—Alkaline earth metal or magnesium compounds
    • B01D2251/404—Alkaline earth metal or magnesium compounds of calcium
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/50—Carbon oxides
    • B01D2257/504—Carbon dioxide
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
    • C02F2103/08—Seawater, e.g. for desalination
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
    • C02F2103/18—Nature of the water, waste water, sewage or sludge to be treated from the purification of gaseous effluents
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02C—CAPTURE, STORAGE, SEQUESTRATION OR DISPOSAL OF GREENHOUSE GASES [GHG]
    • Y02C20/00—Capture or disposal of greenhouse gases
    • Y02C20/40—Capture or disposal of greenhouse gases of CO2
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/151—Reduction of greenhouse gas [GHG] emissions, e.g. CO2

Definitions

  • a modified Solvay process and uses thereof for processing C02-containing gas streams and for desalination
  • the present invention relates to a method for processing an input gas stream, as appears in the preamble of the following claim 1.
  • Alkanolamines encompasses the family of organic compounds of monoethanolamine (MEA), diethanolamine (DEA) and triethanolamine (TEA). The process is undertaken in two steps: Step one: Absorbing
  • Step 2 is very expensive, It uses high pressure, high temperature and releases tons of carbon dioxide in the atmosphere, thus it is a source of atmospheric pollution.
  • a mixture of saline water and ammonia replaces the Alkanolamine.
  • the saline water refers to the produced water from oil and gas fields and further in this document this will be referred to as saline water.
  • the produced water is of high salinity ranging from 4 to five times the salinity of seawater.
  • Saline water is cooled at a temperature suitable for the reaction 2OC is directed to a mixing tank (Tank A).
  • tank A The water in tank A must be well mixed with ammonia from tank B then directed to the absorber D.
  • the natural gas enters the Column D from the bottom. The carbon dioxide in the natural gas reacts as shown in the chemical reactions presented in this innovation.
  • the products are Clean Natural gas ready to be liquefied or delivered to consumers for use.
  • the Ammonium Chloride and Sodium Hydrogencarbonate and water mixture can be separated to give soft water that can be re-injected in the oil and gas field.
  • the present invention relates in particular to a method for processing of water containing an amount of salt.
  • the main objective of the invention is to achieve a method and a novel technique for transforming saline water, which is discharged or rejected from oil and gas field into a useful irrigation water and soda ash compounds (Na 2 CO 3 ).
  • the huge amount of saline water, which is discharged, rejected or dumped back in the oil and gas fields, is a real production problem.
  • the problem is caused by the fact that it causes pressure loss in pipelines and pipes clogging.
  • the carbon dioxide is highly corrosive in presence of water, it has no heating value and is responsible for green house effect.
  • Another object of the invention is to provide for a process enabling operators of oil and gas fields, onshore and offshore, to remove and recover emissions of carbon dioxide in natural gas.
  • the method of the present invention is characterised by the following steps of:
  • step b) reacting said ammonium carbonates from step a) with a saline solution for forming chemical products including alkaline metal carbonate and ammonium chloride, and
  • step b) processing said ammonium chloride from step b) by decomposition to form ammonia and metal chloride and/or hydrochloride acid, and
  • step c) is implemented by using calcium oxide (CaO) to generate calsium chloride as said metal chloride, and/or by using magnesium oxide (MgO) to generate magnesium chloride as said metal chloride.
  • CaO calcium oxide
  • MgO magnesium oxide
  • a further step includes of returning said ammonium chloride generated in step (b) back to step (a) for use in generating said alkaline solution.
  • further steps of the method includes of decomposing said alkaline metal carbonate generated in step (b) into carbon dioxide, and then returning said carbon dioxide back to step (a) for reuse.
  • said carbon dioxide in step (a) is derived from at least one of the following input gas streams:
  • the saline containing solution is a sodium chloride containing solution, and preferably saline, such as a salty NaCI-solution, originating from oil and gas fields.
  • ammonium chloride part is heated, or added calcium oxide, or added magnesium oxide, or mechanically treated to decompose into ammonia, while the hydro chloride, or calcium chloride or magnesium chloride or other part from the decomposition, may be deposited or traded.
  • the carbon dioxide needed for the process is taken from decomposition of said alkaline metal bicarbonate, or a mixture thereof.
  • the ammonium bicarbonate NH 4 HCO 3 is produced in two steps, the first being that carbon dioxide is combined with the alkaline solution in step 1a forming ammonium carbonate (NH 4 ) 2 CO 3 , which is then reacted with more carbon dioxide and water to form said ammonium bicarbonateNH 4 HCO 3 .
  • reaction is conducted by the following steps:
  • Reaction 4 is similar to reaction 5 that describes the gas sweetening invention used in the EnPro process.
  • carbon dioxide CO 2 may be returned to steps 1a) and 1b), and
  • the method of the invention is used for processing of saline water originating from a desalination plant or an oil or gas field (formation water), said saline water being added to the process of step 2, or for removing carbon dioxide from combustion gas, such as related to power plants driven by the combusting of coal, oil or gas, or from natural gas from oil and gas fields
  • the method is used for removing carbon dioxide from industrial activity, such as in smelting plants causing considerable emissions of carbon dioxide in their exhaust gases.
  • the method may be used for removing carbon dioxide from natural gases.
  • the method may be used for removing carbon dioxide from combustion gases or natural gases, such as related to power plants driven by the combusting of coal, oil or gas or natural gas from for example oil- and gas fields.
  • combustion gases or natural gases such as related to power plants driven by the combusting of coal, oil or gas or natural gas from for example oil- and gas fields.
  • the use areas are defined in claims 10-14.
  • the inventive method is used in a combined process for removing carbon dioxide from combustion and natural gases and for a simultaneous desalination of saline water.
  • the novel technique according to the invention uses a new and revised version of the old Solway process.
  • the carbon dioxide is derived from any CO2 containing exhaust or natural gas originating from a combustion process, or from oil and gas fields, or the carbon dioxide originates from the regeneration of monoethanolamine.
  • the old and well known Solway process use is made of calcium carbonate (CaCO 3 ) and sodium chloride (NaCI), while in the new revised version of Solway process there is no need for using calcium carbonate. It can be replaced by MgO or CaO directly, or other method.
  • the carbon dioxide needed is taken from exhaust gases or from the exhaust of the regeneration of monoethanolamine used in natural gas processing.
  • the ammonium chloride (NH 4 CI) from the process is either
  • the recovered ammonia is recycled and returned to the initial brine or saline solution.
  • the present invention appreciates benefits from employing a more reactive calcium oxide (CaO, slaked lime) or magnesium oxide (MgO) which represent considerably more complex handling problems than less reactive lime Ca(OH) 2 (kalk) as employed in apparatus elucidated in the Norwegian patent document.
  • CaO calcium oxide
  • MgO magnesium oxide
  • a change to a more reactive form of input chemical, for example CaO and/or MgO would initially seem disadvantageous to a person ordinarily skilled in the art, especially when large quantities of materials are concerned as exemplified in the Norwegian document. Further significant changes would be needed to the power station described in Norwegian document to implement the present invention.
  • the apparatus of the Norwegian document would be regarded to be an optimized configuration.
  • step 2 the ammonium hydrogen carbonate of step b) is reacted with the saline water from the oil and gas field or the rejected brine water coming from a desalination plant to form sodium bicarbonate
  • step 3 the NaHCO 3 Js converted into Na 2 CO 3 .
  • the carbon dioxide CO 2 may be returned to step 1.
  • the sodium carbonate NaCO 3 precipitates and may be put to the market.
  • the ammonium chloride is heated to decompose to give ammonia and hydrochloric acid.
  • the ammonia is returned to sub step a).
  • NH4CI > NH 3 + HCI, or
  • the ammonium chloride is added calcium oxide to decompose to give ammonia and calcium chloride.
  • the ammonium chloride is added magnesium oxide to decompose to give ammonia and magnesium chloride.
  • ammonia is treated in a mechanical way to decompose to give ammonia and other material.
  • the ammonia is returned to sub step a).
  • step 2 The product compounds NaHCO 3 and NH 4 CI of step 2), represents the same compounds which are formed according to the Solway Process.
  • this step is not necessary since ammonia chloride NH 4 CI is decomposed into NH 3 and HCI, and the NH 3 is returned to step 1.
  • Said CaO is normally produced by heating of calcium carbonate CaCO 3 as follows:
  • the CO 2 produced here is the extra CO 2 produced so that there is no net use of CO 2 in the standard process.
  • the ammonia compound NH 3 is recirculated from step 4 to step 1.
  • the need for a supply of fresh ammonia may be completely eliminated or highly reduced.
  • the supply of CO 2 comes from the exhaust gas, and from the regeneration of said monoethanolamine used in the natural gas processing, or from the natural gas.
  • A Brine water from desalination plant or saline water (formation water) from oil and gas field
  • H Storage tank of water for irrigation or re-injection in wells.
  • the reactions according to steps 1 and 2 are conducted.
  • Brine water or saline water from A is led into the reactor top D through line 12.
  • Water for irrigation purposes are conducted through line 14 to storage H.
  • step 1 and 2 ammonia chloride and soda ash are separated in F conducting the ammonia chloride product into E, while the soda ash (NaHCO 3 ) is led through line 22 into box 30, and further heated to decompose into CO 2 (at 32) which is returned to the section C, the total CO 2 source of the process.
  • the ammonia NH 3 produced in section E is further conducted through line 34 to section B to form an ammonia solution (in water).
  • Section A which contains an aqueous brine solution originating from a desalination plant or saline water solution originating from oil and gas field.
  • This brine/saline water solution is conducted through line 12 to the reactor top.

Abstract

There is disclosed a method for processing an input gas stream, characterised by the following steps of: a) reacting the carbon dioxide of the input gas stream with an alkaline solution based on ammonia, for the formation of ammonium carbonates; b) reacting said ammonium carbonates from step a) with a saline solution for forming chemical products including alkaline metal carbonate and ammonium chloride; and c) processing said ammonium chloride from step b) by decomposition to form ammonia and metal chloride and/or hydrochloride acid; and d) step c) is implemented by using calcium oxide (CaO) to generate calsium chloride as said metal chloride, and/or by using magnesium oxide (MgO) to generate magnesium chloride as said metal chloride. Preferably the method is used in a combined process for removing carbon dioxide from combustion gas and desalination of water.

Description

A modified Solvay process, and uses thereof for processing C02-containing gas streams and for desalination
The present invention relates to a method for processing an input gas stream, as appears in the preamble of the following claim 1.
An important step in the processing of natural gas (in general denoted as input gas streams) is the carbon dioxide removal known as gas sweetening process. This process is a must prior to natural gas liquefaction to prevent carbon dioxide solidification in the gas plant installation and to eliminate pressure loss in pipelines and pipes clogging. Further, the carbon dioxide is corrosive in presence of water and as an inert gas it has no heating value. Hence, it has to be removed from natural gas.
The most commonly used process is absorption in various amine solutions. It is well known that serious operating problems exist in such amine scrubbing operations. Further, the energy costs for amine scrubbing processes are very high. Thus, for may years chemical engineers have been attracted to new separation techniques requiring less energy, having less operating problem and environmentally friendly.
The actual processes applied in the natural gas sweetening use Alkanolamine. Alkanolamines encompasses the family of organic compounds of monoethanolamine (MEA), diethanolamine (DEA) and triethanolamine (TEA). The process is undertaken in two steps: Step one: Absorbing
When CO2 is absorbed into an aqueous solution of a ternary alkanolamine R1 R2R2N and primary or secondary amine R1 R2NH the following reactions occur at high pressure:
MEA + CO2 => MEA-carbonates + Heat
Step two: Regeneration
MEA-carbonates + Heat => MEA + H2O + CO2
Step 2 is very expensive, It uses high pressure, high temperature and releases tons of carbon dioxide in the atmosphere, thus it is a source of atmospheric pollution.
In the present invention a mixture of saline water and ammonia replaces the Alkanolamine. The saline water refers to the produced water from oil and gas fields and further in this document this will be referred to as saline water. The produced water is of high salinity ranging from 4 to five times the salinity of seawater.
When acidic natural gas is scrubbed in a mixture of saline oil filled water and ammonia a series of chemical reactions takes place in the scrubber as further described later in this document.
Saline water is cooled at a temperature suitable for the reaction 2OC is directed to a mixing tank (Tank A). The water in tank A must be well mixed with ammonia from tank B then directed to the absorber D. The natural gas enters the Column D from the bottom. The carbon dioxide in the natural gas reacts as shown in the chemical reactions presented in this innovation.
The products are Clean Natural gas ready to be liquefied or delivered to consumers for use. The Ammonium Chloride and Sodium Hydrogencarbonate and water mixture can be separated to give soft water that can be re-injected in the oil and gas field.
The present invention relates in particular to a method for processing of water containing an amount of salt.
More precise the main objective of the invention is to achieve a method and a novel technique for transforming saline water, which is discharged or rejected from oil and gas field into a useful irrigation water and soda ash compounds (Na2CO3). The huge amount of saline water, which is discharged, rejected or dumped back in the oil and gas fields, is a real production problem. The problem is caused by the fact that it causes pressure loss in pipelines and pipes clogging. Furthermore, the carbon dioxide is highly corrosive in presence of water, it has no heating value and is responsible for green house effect.
For areas such as the Gulf regions this is considered to be a well-known problem, which has been investigated for a long time to solve by utilising already accessible material, such as the existing carbon dioxide and saline water.
Another object of the invention is to provide for a process enabling operators of oil and gas fields, onshore and offshore, to remove and recover emissions of carbon dioxide in natural gas.
The method of the present invention, as of claim 1 , is characterised by the following steps of:
a) reacting the carbon dioxide of the input gas stream with an alkaline solution based on ammonia, for the formation of ammonium carbonates,
b) reacting said ammonium carbonates from step a) with a saline solution for forming chemical products including alkaline metal carbonate and ammonium chloride, and
c) processing said ammonium chloride from step b) by decomposition to form ammonia and metal chloride and/or hydrochloride acid, and
d) step c) is implemented by using calcium oxide (CaO) to generate calsium chloride as said metal chloride, and/or by using magnesium oxide (MgO) to generate magnesium chloride as said metal chloride.
Preferably a further step includes of returning said ammonium chloride generated in step (b) back to step (a) for use in generating said alkaline solution. Preferably further steps of the method includes of decomposing said alkaline metal carbonate generated in step (b) into carbon dioxide, and then returning said carbon dioxide back to step (a) for reuse. Preferably said carbon dioxide in step (a) is derived from at least one of the following input gas streams:
(d) exhaust gas from combustion processes;
(e) a process operable to regenerate monoethanolamine; and (T) natural gas.
According to a preferred option, the saline containing solution is a sodium chloride containing solution, and preferably saline, such as a salty NaCI-solution, originating from oil and gas fields.
The ammonium chloride part is heated, or added calcium oxide, or added magnesium oxide, or mechanically treated to decompose into ammonia, while the hydro chloride, or calcium chloride or magnesium chloride or other part from the decomposition, may be deposited or traded.
According to a preferred embodiment, the carbon dioxide needed for the process is taken from decomposition of said alkaline metal bicarbonate, or a mixture thereof.
According to a preferred embodiment, heating an alkaline metal carbonate in a calcinater, such as in a rotary furnace, forms the alkaline metal bicarbonate and said carbon dioxide.
According to another preferred embodiment, the ammonium bicarbonate NH4HCO3 is produced in two steps, the first being that carbon dioxide is combined with the alkaline solution in step 1a forming ammonium carbonate (NH4)2CO3, which is then reacted with more carbon dioxide and water to form said ammonium bicarbonateNH4HCO3.
In a further preferred option, the reaction is conducted by the following steps:
step 1): a) formation of ammonium carbonate (NH4)2CO3 by the reaction: 2NH3 + CO2 +H2O => (NH4)2CO3,
b) transforming (NH4)2CO3 to 2NH4HCO3 by any excess of CO2 : (NH4)2CO3 + CO2 + H2O => 2NH4HCO3 (aq.), step 2):
Reacting ammonium hydrogen carbonate of step 1b) with brine/saline water to form ammonium chloride and sodium-bicarbonate NH4HCO3 + NaCI => NaHCO3 + NH4CI,
step 3)
• Reaction 4. H2O + NaCI + NH3 + CO2 -» NaHCO3 + NH4CI
Reaction 4 is similar to reaction 5 that describes the gas sweetening invention used in the EnPro process.
• Reaction 5
(produced saline water or formation water ) + NH3 + (Natural gas + CO2)
( Sweet Natural gas ) + H20 + NH4CI + NaHCO3
step 4):
Converting the dry sodium bicarbonate by heating to give anhydrite sodium carbonate or soda ash:
2NaHCO3 + heat => Na2CO3 + CO2 + H2O,
wherein the carbon dioxide CO2 may be returned to steps 1a) and 1b), and
step 5):
- heating the ammonium chloride to decompose to give ammonia and hydrochloric acid,
NH4CI => NH3 + HCI, and that said ammonia is returned to step 1 a), or
- adding calcium oxide to decompose to give ammonia and calcium chloride, 2NH4CI + CaO => 2NH3 + CaCI2 + H20 and that said ammonia is returned to step 1 a), or
- adding magnesium oxide to decompose to give ammonia and magnesium chloride (note that magnesium is more active than calcium), 2NH4CI + MgO => 2NH3 + MgCI2 + H20 and that said ammonia is returned to step 1 a), or
- other method of decomposing to give ammonia and other material, and that said ammonia is returned to step 1 a).
The above preferred features of the method appear in the independent claims 2-12.
According to the invention the method of the invention is used for processing of saline water originating from a desalination plant or an oil or gas field (formation water), said saline water being added to the process of step 2, or for removing carbon dioxide from combustion gas, such as related to power plants driven by the combusting of coal, oil or gas, or from natural gas from oil and gas fields
According to another preferred use, the method is used for removing carbon dioxide from industrial activity, such as in smelting plants causing considerable emissions of carbon dioxide in their exhaust gases.
Further the method may be used for removing carbon dioxide from natural gases.
Further the method may be used for removing carbon dioxide from combustion gases or natural gases, such as related to power plants driven by the combusting of coal, oil or gas or natural gas from for example oil- and gas fields. The use areas are defined in claims 10-14.
Most preferred the inventive method is used in a combined process for removing carbon dioxide from combustion and natural gases and for a simultaneous desalination of saline water.
The novel technique according to the invention, uses a new and revised version of the old Solway process. In the present process of the invention the carbon dioxide is derived from any CO2 containing exhaust or natural gas originating from a combustion process, or from oil and gas fields, or the carbon dioxide originates from the regeneration of monoethanolamine. In the old and well known Solway process, use is made of calcium carbonate (CaCO3) and sodium chloride (NaCI), while in the new revised version of Solway process there is no need for using calcium carbonate. It can be replaced by MgO or CaO directly, or other method.
The carbon dioxide needed is taken from exhaust gases or from the exhaust of the regeneration of monoethanolamine used in natural gas processing. The ammonium chloride (NH4CI) from the process is either
(i) heated then it sublimates or decompose to give ammonia (NH3) and hydrochloric acid (HCI), or (ii) added calcium oxide to decompose to give ammonia (NH3) and calcium chloride (CaCI2), or (iii) added magnesium oxide to decompose to give ammonia (NH3) and magnesium chloride (MgCI2), or (iv) Decomposed in other ways to give ammonia and other material.
The recovered ammonia is recycled and returned to the initial brine or saline solution.
Reference is also made to Norwegian patent document 317.918. This document discloses a process for desalination of sea water and for cleaning of exhaust gases. Carbon dioxide of exhaust gases is reacted with ammonia in sea water, and bicarbonates and ammonia chloride are formed.
The present invention appreciates benefits from employing a more reactive calcium oxide (CaO, slaked lime) or magnesium oxide (MgO) which represent considerably more complex handling problems than less reactive lime Ca(OH)2 (kalk) as employed in apparatus elucidated in the Norwegian patent document. Obviously, a change to a more reactive form of input chemical, for example CaO and/or MgO, would initially seem disadvantageous to a person ordinarily skilled in the art, especially when large quantities of materials are concerned as exemplified in the Norwegian document. Further significant changes would be needed to the power station described in Norwegian document to implement the present invention. The apparatus of the Norwegian document would be regarded to be an optimized configuration.
The following is a detailed disclosure of the method of the invention Step i
An ammonia solution is combined with the carbon dioxide CO2 coming from the sources mentioned above in two sub steps a) and b):
a) formation of ammonium carbonate (NH4)2CO3 2NH3 + CO2 +H2O => (NH4)2CO3
b) any excess of CO2 will transform (NH4)2CO3 to 2NH4HCO3 (ammoniumhydrogencarbonate) as follows.
(NH4)2CO3 + CO2 + H2O => 2NH4HCO3 (aq.)
Step 2
In step 2 the ammonium hydrogen carbonate of step b) is reacted with the saline water from the oil and gas field or the rejected brine water coming from a desalination plant to form sodium bicarbonate
NH4HCO3 + NaCI => NaHCO3 + NH4CI
Step 3
In step 3, the NaHCO3 Js converted into Na2CO3.
Dry sodium bicarbonate is heated in a rotary furnace (CALCINATER) and gives anhydrite sodium carbonate or soda ash as follows:.
2NaHCO3 heat => Na2CO3 + CO2 + H2O.
The carbon dioxide CO2 may be returned to step 1.
The sodium carbonate NaCO3 precipitates and may be put to the market.
Step 4
According to the invention, the ammonium chloride is heated to decompose to give ammonia and hydrochloric acid. The ammonia is returned to sub step a). NH4CI => NH3 + HCI, or
the ammonium chloride is added calcium oxide to decompose to give ammonia and calcium chloride. The ammonia is returned to sub step a). 2NH4CI + CaO => 2NH3 + CaCI2 + H2O, or
the ammonium chloride is added magnesium oxide to decompose to give ammonia and magnesium chloride. The ammonia is returned to sub step a). 2NH4CI + MgO => 2NH3 + MgCI2 + H2O, or
the ammonia is treated in a mechanical way to decompose to give ammonia and other material. The ammonia is returned to sub step a).
The product compounds NaHCO3 and NH4CI of step 2), represents the same compounds which are formed according to the Solway Process.
However, in the Solway Process, the ammonia chloride is reacted with lime under heating forming ammonia, calcium oxide and water, as follows: NH4CI + CaO => NH3 + CaCI2 + H2O
In the present invention however, this step is not necessary since ammonia chloride NH4CI is decomposed into NH3 and HCI, and the NH3 is returned to step 1.
Thus the present invention eliminates the step of producing said CaO of the Solway process. Said CaO is normally produced by heating of calcium carbonate CaCO3 as follows:
CaCO3 => CO2 + CaO.
The CO2 produced here, is the extra CO2 produced so that there is no net use of CO2 in the standard process.
Step 2 above represents the standard Solway process (= ammonia- soda process), but usually CO2 used is recycled from the standard step 4, so there is no net use of CO2, and it cannot be used for removing CO2 from exhaust/MEA/natural gas, where only half of the CO2 is recycled.
Thus, according to the invention, the ammonia compound NH3 is recirculated from step 4 to step 1. Thus the need for a supply of fresh ammonia may be completely eliminated or highly reduced. Further, the supply of CO2 comes from the exhaust gas, and from the regeneration of said monoethanolamine used in the natural gas processing, or from the natural gas.
The invention shall be explained further by reference to the figure 1 in which the elements of the process plant are numbered as follows.
A: Brine water from desalination plant or saline water (formation water) from oil and gas field
B: Ammonia solution or ammonia gas
C: Carbon Dioxide from exhaust gases or MEA regeneration or natural gas
D: Solvay tower (reactor)
E: recycled ammonia
F: Solid separator
G: Calcium oxide or Magnesium supply
H: Storage tank of water for irrigation or re-injection in wells.
In the Solway tower D, the reactions according to steps 1 and 2 are conducted. The carbon dioxide from exhaust gases (input gas stream) or MEA regeneration or natural gas directly in C, is conducted into reactor D through line 10. Brine water or saline water from A is led into the reactor top D through line 12. Water for irrigation purposes are conducted through line 14 to storage H.
The products of step 1 and 2 ammonia chloride and soda ash are separated in F conducting the ammonia chloride product into E, while the soda ash (NaHCO3) is led through line 22 into box 30, and further heated to decompose into CO2 (at 32) which is returned to the section C, the total CO2 source of the process. The ammonia NH3 produced in section E is further conducted through line 34 to section B to form an ammonia solution (in water). This solution is further led to Section A, which contains an aqueous brine solution originating from a desalination plant or saline water solution originating from oil and gas field.
This brine/saline water solution is conducted through line 12 to the reactor top. The major advantages of the present invention is that:
• the rejection or dumping of brine/saline water may be eliminated in that the sodium chloride may be used as an reactant in the process,
• carbon dioxide gases in combustion exhaust gases or natural gases may optionally be consumed and eliminated. • the reactant ammonia (NH3) may be circulated in the process.
• there is no need to incorporate any calcium carbonate in the process as is done in the Solway process.

Claims

P A T E N T C L A I M S
1. A method for processing an input gas stream, characterised by the following steps of: a) reacting the carbon dioxide of the input gas stream with an alkaline solution based on ammonia, for the formation of ammonium carbonates, b) reacting said ammonium carbonates from step a) with a saline solution for forming chemical products including alkaline metal carbonate and ammonium chloride, and c) processing said ammonium chloride from step b) by decomposition to form ammonia and metal chloride and/or hydrochloride acid, and d) step c) is implemented by using calcium oxide (CaO) to generate calsium chloride as said metal chloride, and/or by using magnesium oxide (MgO) to generate magnesium chloride as said metal chloride.
2. A method as claimed in claim 1 , including a further step of returning said ammonium chloride generated in step (b) back to step (a) for use in generating said alkaline solution.
3. A method as claimed in claim 1 or 2, including further steps of decomposing said alkaline metal carbonate generated in step (b) into carbon dioxide, and then returning said carbon dioxide back to step (a) for reuse.
4. A method according to the preceding claims, wherein said carbon dioxide in step (a) is derived from at least one of the following input gas streams:
(d) exhaust gas from combustion processes;
(e) a process operable to regenerate monoethanolamine; and
(f) natural gas.
5. Method according to any of the preceding claims, characterised in that the saline containing solution is a sodium chloride containing solution.
6. Method according to any of the preceding claims, characterised in that the saline containing solution is saline, such as a salty NaCI-solution, originating from an oil or gas field.
7. Method according to any of the preceding claims, characterised in that said ammonium chloride is (i) heated to decompose into ammonia or (ii) added calcium oxide to decompose into ammonia or (iii) added magnesium oxide to decompose into ammonia or (iv) other method used to decompose into ammonia.
8. Method according to any of the preceding claims, characterised in that the hydro chloride or calcium chloride or magnesium chloride or other material part from the decomposition, are deposited or traded.
9. Method according to any of preceding claims, characterised in that the carbon dioxide needed for the process originates from decomposition of said alkaline metal bicarbonate, or a mixture thereof.
10. Method according to any of the preceding claims, characterised in that said alkaline metal bicarbonate and said carbon dioxide is formed by heating an alkaline metal carbonate in a calcinater, such as in a rotary furnace.
11. Method according to any of preceding claims, characterised in that the ammonium bicarbonate NH4HCθ3 is produced in two steps, the first being that carbon dioxide is combined with the alkaline solution in step 1a forming ammonium carbonate (NH4)2CO3, which is then reacted with more carbon dioxide and water to form said ammonium bicarbonateNH4HCO3.
12. Method according to any of the preceding claims, characterised in that the reaction is conducted by the following steps:
step 1): a) formation of ammonium carbonate (NhU)2CO3 by the reaction: 2NH3 + CO2 +H2O => (NH4)2CO3, b) transforming (NH4)2CO3 to 2NH4HCO3 by any excess of CO2 : (NH4)2CO3 + CO2 + H2O => 2NH4HCO3 (aq.), step 2): reacting ammonium hydrogen carbonate of step 1b) with brine water or saline water to form ammonium chloride and sodium-bicarbonate
NH4HCO3 + NaCI => NaHCO3 + NH4CI, step 3): converting the dry sodium bicarbonate by heating to give anhydrite sodium carbonate or soda ash:
NaHCO3 + heat => Na2CO3 + CO2 + H2O, wherein the carbon dioxide CO2 may be returned to steps 1a) and 1b), and
step 4): heating the ammonium chloride to decompose to give ammonia and hydrochloric acid,
NH4CI => NH3 + HCI, and that said ammonia is returned to step 1 a), or adding calcium oxide to decompose to give ammonia and calcium chloride,
2NH4CI + CaO => 2NH3 + CaCI2 + H20 and that said ammonia is returned to step 1 a), or
-adding magnesium oxide to decompose to give ammonia and magnesium chloride,
2NH4CI + MgO => 2NH3 + MgCI2 + H20 and that said ammonia is returned to step 1 a), or
other method to decompose to give ammonia and other material and that said ammonia is returned to step 1 a).
13. Use of the method according to any of the preceding claims, for processing of brine water originating from a desalination plant or saline water from oil and gas fields or any other source, said brine or saline water being added to the process of step 2.
14. Use of the method according to any of the preceding claims, for removing carbon dioxide from combustion gas or natural gas, such as related to power plants driven by the combusting of coal, oil or gas or natural gas from for example oil- and gas fields.
15. Use of the method according to any of the preceding claims, for removing carbon dioxide from industrial activity.
16. Use of the method according to any of the preceding claims, in a combined process for removing carbon dioxide from combustion and natural gases and for a simultaneous desalination of saline water.
PCT/NO2007/000186 2006-05-30 2007-05-30 A modified solvay process, and uses thereof for processing co2-containing gas streams and for desalination WO2007139392A1 (en)

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